GB2239489A - Harnessing of low grade heat energy - Google Patents

Abstract

A vapourising heat exchanger, 2, through which flows a suitable fluid, 1, (such as a refrigerant) for absorbing, via vapourisation, surrounding heat, eg, low grade heat contained in rivers and tidal flows, 3, is followed by a vapour compressor, 5, followed by a further heat exchanger, 7, followed by a turbine, 15. The energy produced by the turbine, 15, may power the compressor, 5. Heat may be transferred via heat exchangers 7, 11 and fluid flow 8 to a further fluid to drive a further turbine 12. Alternative heat exchange circuits are disclosed (Figs. 1A, 1B, 1D) and reference is made to the possible use of a variety of different turbines and a variety of uses of the power generated. Details of the thermodynamic process involved are also discussed. <IMAGE>

Description

THE HARNESSING OF HEAT ENERGY VIA THROTTLE ENERGY CONVERSION

THE HARNESSING OF NATURAL PLANET HEAT INVOLVING THROTTLE ENERGY CONVERSION Introduction There are of course many sources of heat available to us on the planet, Earth,

and quite a number of means have been devised to harness heat1conversion into turbine rotational energy for direct use or for further conversion into electrical power. However, the invention herein differs in that it will

provide a means for harnessing the very low grade heat contained in the natural flowing waters on the planet, e.g. at temperatures of the order of 5-20"C, for which, as far as I am aware, no means has yet been devised to harness such heat in the form of turbine rotational energy and on a large scale.Thus, as inferred it is considered that the invention could become applied for very large scale production of power. However, the invention could potentially also become applied for the harnessing of all normal heat sources, and to the harnessing of the heat of compression of the ARC cycle, i.e. the heat of compression when air or some other gas is adiabatically compressed - see my PA 8728601, and whilst it is considered that very large tQ small scale production of power via this invention could beomce via the harnessing of the low grade heat of natural flowing waters quite extensively in the future on and all over the Planet where suitable sites exist and for ships' power, a further smallandlarge scale area of usage could potentially be via combining with an ARC cycle based upon air to yield triple purpose Plants for combined Power, Rainmaking and Refrigeration. With an advantage over the Plants of this type under PA8728601 being that the Plants herein could be fully selfcontained with respect to fluid condensation without the need to consume rainmaking capacity and without the need for cooling towers or a cold water supply when achieving the former. Thus such Plants would be fully closed-cycle and self-contained and could be placed anywhere on the Planet to give the triple capacity, with the only resource required at site of usage being the normal air of the atmosphere and some humidity in the atmosphere for precipitation as rain via application of cold exhaust air from the ARC cycle. However, these plants may not become as capable of producing as much accompanying power capacity as those under PA8728601 potentially could.Nonetheless suchplants should produce some surplus of power once developed to a reasonably efficient

level, when oneervisage that a major area of use for this type of Plant in the future could become for the setting up of large agricultural ventures in arid and desert lands where the only resource for hundreds of miles all around is simply air with a sufficiently high humidity, which could be as Britain's normal humidity levels although would obviously be better to be higher, and where power needs would not be very high in ratio with required rainmaking capacity. With the Plant therefore able to provide all the power needs of such a venture.

Thus, as implied, several process variations will become discussed herein but they are all based upon a similar process type of basically the same process circuitry and all having in common a particular sub-system, which in fact is the part of the circuitry of all the processes that distinguishes their process circuitry from the circuitry of existing processes, and indeed is that part of the circuitry on which they all rely to function for the harnessing of heat energy.Thus, all other facets of the processes are carrie dout in one form or another in existing processes with the only extra being the sub-system which if it works in practice as well as will be theorised herein then all the processes will potentially be possible that depend upon the sub-system,

among them being that which will make it potentially possible to harness the low grade heat contained in the natural waters of the Planet when Mathematical Models will show that Plants of the order of 2000 MWhr at one site of natural flowing waters should be well within any capacity limitations of the process at such sites.While with regard to the cooling of the water that this would bring about it is probably appropriate to combine this discussion with the content of the recent Horizon programme, BBC 2 Sunday 14 February 1988 dealing with the Planet's climate in which it was stated that the climate was heating up and that this could lead to the Planet's waters rising by 1-1 metres by the year 2050. Therefore, whilst wide-scale and extensive application of the process all over the Planet may not have a very significant impact on the overall temperature of the Planet, the more widescale and extensive the better from the point

of view or maintaining tne presenl/szeaay state of the Planet, everybody's present habitat.

In at least one main method of operation this process type could also be adapted for use in Space and on the other Planets, as the process type under PA8728601.

Thus the process tvoe couldrbecome aDnlied for the extensive develonment

of the arid and desert lands on Earth andltor the similarly barren landscapes on theother planets of the solar System in the new Age in one form or another and I think it is intended that America spearheads the way into Space via their recently announced 'Pathfinder Programme', whilst Britain spearheads a similar 'Pathfinder Programme' on this planet leading to its further extensive development agnd encompassing parts not yet reached properly by the advancing front of civilisation but currently crying out for development.

they are a range of processes that are again based upon free and abundantly available sources of energy which could become very widely and extensively used for the further aevelopment of the Planet, but at this Applied Theory stage everything being dependent upon whether the sub-system will function in practice, in contrast to the range of processes under the aforementioned Patent Application which really possess no unknowns at my Applied Theory stage. Thus at such a stage in this current work, in contrast, the processes to be discussed herein will all be dependent, but solely dependent upon, the success of otherwise of the sub-system, which however I hasten to add seems feasible to me at my Applied Theory stage.But having said that some current text books state that it would not be possible to convert to usable energy in the part of the process circuitry where it is hoped to achieve such energy conversion via the means of the sub-system, and therefore from the outset I leave this open to debate.

However, the sub-system in fact is itself a very simple system in Applied Theory, but perhaps will be deemed by some to possess some element of doubt at such a stage in the development of threse range of processes1 which I generally refer to as the Alternative Brierley Porcesses.

As implied by the heading the sub-system is in effectathrottle energy conversion,, which is upgraded energy that in existing processes becomes dissipated to waste via passing through a throttling device wherein the upgraded energy becomes transferred into the latent heat energy mode of the fluid, to finish with fluid in both the liquid and vapour phases at the end of the throttling process.The sub-system simply aims to convert this otherwise transferred energy into turbine energy and in this alternative way downgrade the upgraded enerov contained in-the fluid. in the Drocess obtainina usable turbine

energy and finishing with the fluid/still fully in the liquid phase

the upgraded energy will become transferred to a turbine rather than into the latent heat energy mode of the fluid, which will also have advantages since the liquid phase state is required for commencing the next cycle of the process. However, whilst the concept sounds simple and indeed may be simple it in fact took me a while in the first place to try to get beyond present day thinking on throttle energy conversion as for example given on page 37 of the text book 'Refrigeration and Aid Conditioning' by W.

F. Stoecker, which I make mention of from the outset in order to add the element of doubt and not raise too many hopes at this stage.

A further aspect which I will make mention of from the outset is that much

of the discussion herein, particularly that on the Çbv-system, is still at an evolvinq and breakina throuah staae and as such is at a verv basic

and rudimentary level based more on1xperience and not yet really in the modern scientific terms that have now become established. However, this is not to say that the latter type of treatment on the work should not subsequently become applied and on the contrary the work herein will serve as a prime example in the total work that I have undertaken where after my very basic treatment it should be possible to apply more modern approaches to the system. Perhaps from here to Kingdom Come as the saying is.

Probably the analogy could be drawn with subsequent more sophisticated treatment on the human body after its early evolution to a bare stage.

Although perhaps a closer analogy would be that hereinllay most of the inners of the body/system bare for subsequent treatment, or a combination of both. Or at least to a level at which the system should become sufficiently open for serious debate and consideration for future development and further scientific treatment.

The sub-system in fact represents one of the final main keys that will hang together the whole of the work that I have undertaken, without which probably half the projects would not work in practice, but if successful in practice then a whole new field of technology will become opened up from which could mushroom many new systems, processes, projects, and industry leading to and for the betterment of our civilisation on the planet.

Thus there follows a somewhat basic discussion of this range of process types and of the sub-system on which they will all solely depend, of an evolving nature, with the writing itself being at a similar stage and really a final first drafting, but I have taken the decision that it is probably better to try to get the concept across as quickly as possible now in order to then be in a position to convey the feasibility of all the work that I have undertaken at this point in the work, since with

full potential picture then better and pressing decisions as to the better ways forward into the new Age can be made. Taking the view that it is better to try to achieve this at this stage.However, moreso than this a further aspect that I have to consider being that if I am expected to be the Son of Man referred to in the Holy Bible then I have and have had a high responsibility in trying to fulfil the expectations of those who place their faith and beliefs in the Holy Bible and in the expected Coming of the Son of Man referred to therein, and indeed in trying to convince people of this aspect in this very sceptical, agnostic and atheistic World. Thus, my decision has been that such aspects required the addition of the ensuing work and contribution at this stage, albeit in a somewhat rough but ready state. In order to then and thereby convince people moreso of the above aspects, re St.John Chap 10 v 38 and, indeed, to then and thereby more fully encompass my intended overall contribution to the establishing of the Kingdom of God come Heaven on the Planet as referred to in the Holy Bible and as in accordance with the Lord's Prayer.

Hence my apologies in advance, but I hope the appropriate readers will appreciate that it has been a very difficult task. Moreover, in the case of the sub-system to be discussed herein it is probably better to show my deliberations fairly close to their original evolution for the sake of more thorough scrutinisation in view of the fact that it is considered to be not a possible system. And indeed for the sake of more

in-depth understanding by readers who may notjbe ot tne scientitic traternity but nonetheless are required to understand the system, e.g. politicians and potential investors in the work at this juncture.Which, in fact, for the whole of the work in general is probably meant to be an intended aspect of work for the sake of a deeper understanding of the World in the future by ordinary folk and perhaps to instill more endearment towards the World of Science and technology on which it will be based. Perhaps also to provide one meaningful means by which all people can become born of the true Spirit and to in turn thereby provide one of several qualifications required for their entry into the Kingdom of God. Ref: The Gospel according to St John Chapter 3 verses 5 to 7.The implication being that as far as God and Christ are concerned the beings of people are not in God's Kingdom of God but only if and when they subsequently become born again of that which is of true Spirt to become truly born again in some way and/or one way or another, and perhaps the work in its entirety is intended to have mass appeal for mass conversion to God's Kingdom of God ways and into the true Spirit of that Kingdom. Thus possibly related dimensions to my work that will be pursued further. However, 'Except A Man be Born Again He Cannot see The Kingdom of God'. Amos Chap 4 v 12; St. John Chap 3 v 3. Therefore, I hope readers will persevere with the ensuing writing since whilst my ideas contained therein commence off somewhat cloudy, I think that by the end of the day people will acquire a fairly clear understanding of them and I take this opportunity to thank you all and for persevering and bearing with me during these stages of my work on the Planet. Drawing a parallel with birth, one could perhaps correctly take the view that my work at this stage comprises evolving, developing and delivering the wherewithal to give Life unto the Earth, ie, the eggs.

And who knows, I may even add to people's faith in God, The Son and the Holy Ghost, ie, HG. When it would then remain for God, The Son and HG to have the same faith in people.

Process Description

Firstlylthe basic process, then the possible variations of the process and other possible heat sources.

The basic process is schematically depicted on Fig. 1 and intended to function as follows.

Commencing at stage 1 a refrigerant initially in the liquid phase passes through pipework to unit-2 which is a heat exchange/absorbing unit submerged beneath natural flowing waters-3, e.g. a tidal flow at the mouth of a river estuary, wherein the refrigerant flowing through absorbs the natural heat contained in the waters flowing over the submerged pipework of the heat exchange unit and gradually changes to the vapour phase from the liquid phase as the heat enters the latent heat energy mode of the refrigerant, which will thterefore be heat absorption that will all take place at the same temperature until every last drop of liquid phase has been vapourised, and more specifically at the Bpt of the liquid refrigerant as under the vapour pressure that it is under, which would

IATS. pressure as in the pipework, 4, carrying the vapourised refrigerant to the next stage.

The next stage being a vapour compression unit, 5, Which could be of any

type and will adiabatically compress the vapour/lnitially at lAIS to a high pressure and therefore heat of compression temperature suitable for generating vapour or steam pressure in a subsequent stage of the process.

Thus in effect the refrigerant will absorb and carry the heat of the natural flowing waters in its vapour phase to the comrpessor which will then upgrade the absorbed heat to a high temperature by placing into the vapour mechanical compression energy, when all the absorbed latent heat will become transferred into. and become uDaraded in.the harnessable kinetic energy mode of the

retrigeranx s vaspour pnas ein tne exampies or tne process to De / nerein.

After compression the hot compressed refrigerant vapour passes to heat exchange unit 7 via pipework 6, wherein a proportion of the upgraded heat contained in the vapour becomes transferred to a fluid flow 8 counterflowing through the heat exchange unit as indicated by the flow arrows 9 which then carries the transferred heat via pipework 10 into a vapour or steam generator 11. Therein to raise vapour or steam pressure for driving turbine 12. The fluid for carrying the heat into the generator could be of any susbtance found suitable for carrying the heat since the process could be made fully closed-cycle with respect to all its fluids , as will be further discussed.However, at this stage it can just be assumed to be water becoming pumped out of the flowing waters and then pressurised to a sufficient pressure to be able to become heated to the required temeperature via the transferring heat without boiling, with the water flow containing any residual heat simply flowing back into the flowing waters as indicated via pipework 13. However, obviously it would be better for this cycle to be closed-cycle both from the point of view of then only requiring to become pressurised once at the outset and also from the point of view of placing back into the system the residual heat left remaining in this fluid flow on exit from the generator, 11, which is a mode of operation that becomes

the startina Doint mode of operation that one would aDDlv in Practice.

involving the residual heat contained in the fluid flow becoming transferred to the liquid phase of the refrigerant at stage 1 before the refrigerant then flows on to absorb fresh heat input from the flowing waters, with the cooled fluid flow becoming piped back to heat exchange unit 7

tor tne next cycle ot tne process. However,1 an alternative way Of operating the process could be for the hot compressed refrigerant vapour 6 to pass directly through the vapour or steam generator 11 without the intermediary of fluid 8/9/10/13 to carry the heat into the generator, and from there pass directly on to the refrigerant's next stage in the process which in fact is the system being referred to as the sub-system herein.Therefore since transference of the heat to the fluid in the generator would probably be achieved most efficiently in this way and since there would not then be another fluid possessing residual heat energy which could only become Dlaced back into the svstem via Dlacina the heat into the refriaerant at

stage 1 as a part ot tne neatprocess then perhaps one would endeavour to operate the process in this alternative way from the outset of putting the process into practice.However, at this stage in this discussion of the process it is simpler to discuss the sub-system, 14, in the form indicated on Fig l/SRdepicting as it does a flow from the exit side of the compressor directly into the sub-system, 14, with a proportion of the heat it contains becoming removed en route via heat exchange unit 7, which then becomes carried into the generator 11. Therefore, discussing the sub-system in this basic, easy to understand, form which in any case would

be the way that one started off with the process.The transference of the heat to fluid 9 will be under conditions of constant pressure cooling with respect to the refrigerant fluid 15 and be as in a normal refrigerant refrigeration cycle with respect to this aspect and, as in a normal refrigeration cycle,could become fully condensed to the liquid phase inside the heat exchanqe unit 7 and be fully liquid by the time staqe 15 is reached whilst

still remaining under a constant pressure, i.e. that becoming1createdfly the compressor 5 and in the refrigerant vapour phase in pipework 6. Thus as heat is taken out of the refrigerant vapour it will still remain under the original compression pressure even if it becomes condensed fully back to the liquid phase. and then even if some sub-cool inc of the liquid phase

miscarried out.Some references in relation to such aspects can be found under: (1) Refrigeration and Air Conditioning, by W. F. Stoecker pages 30-46, e.g. Fig. 3-14 page 46, which in fact indicates a very slight pressure drop in practice on the sub-cooled example cycle.

(2) Principles of Refrigeration by Roy J. Dossat pages 97-150, e.g. Fig. 8-9 on page 146.

(3) As in the McGraw Hill Encyclopedia of Science and Technology.

. . . However in the

main example that 1 propose to / herein tt is intended to firstlvcomDress the vapour to well above the critical Pressure

and temperature and then oniyl down to the critical temperature region whilst still remaining under the pressure well above the critical pressure.

Thus in this example bv the time the refriaerant fluid reaches staae 15

in the heat exchange unit 7 it will in fact bervérging on the liquid phase but really in the state in which there is said to be little distinguishable difference between the vapour and liquid phases since at this Applied Theory Dre-practical phase it is considered that the fluid commencinq off in such

a state may perform better in sub-system 14. Which in fact is/a turbine, 15, inside an enclosed chamber 14. The concept therefore being that the fluid still under the original compressor pressure, continually becoming created as the refrigerant fluid flows around the process circuit, will, instead of passing through a normal throttling device to lower the pressureenthalpy energy contained in the fluid at such a stage in such a circuit via effecting transference of the energy into the latent heat energy mode of the fluid as the fluid passes through the throttling device, pass through a turbine and transfer the pressure-enthalpy energy to a turbine to convert the energy into usable turbine energy whilst itself becomes lower in pressure enthalpy content, hopefully all the way back down to ground state, i.e.

IATS and the temeprature associated with IATS for the particular refrigerant fluid passing around the process circuit. In the way that any fluid under pressure can produce turbine energy whilst itself loses pressure energy due to transference of the pressure energy to the turbine. Remember the compressor will continually be pumping compressed vapour into pipework 6 and the fluid at stage 15 will still be under the same continuous pressure, which will therefore be capable of continuously forcing the fluid at stage 15 through a turbine which will rotate on so doing whilst the fluid itself will lose energy by a corresponding amount.And by the time the fluid exits from the turbine it is hoped that it will have transferred all its energy content to the turbine down to ground state and will itself exit at ground state all in the liquid phase and ready to commence another cycle of the process. Whilst the energy contained in the fluid is pressureenthalpy energy and not simply pressure energy - as for example in normal hydropower or hydraulic fluid pressure harnessing - eg, as in diesel-hydraulic locomotives, it will be demonstrated following that this could be very possible to achieve and that the turbine energy that becomes created here could therefore be sufficient to continuously sustain the compressor, energy input requirement. To leave remining all the turbine energy becoming produced via the removed heat in the turbogenerating equipment 11 and 12 for output supply.Otherwise all this turbine energy would have to become used internally to sustain the compressor and none would be available for output supplyand such a process would then only have use for refrigeration via the fluid at stage 1 in the circuit on exit from whatever system becomes used to depressurise the fluid at stage 14.

Nonetheless perhaps the basis of a useful refrigeration process requiring of no external energy input. However, returning to the main process under discussion which I hope to show will in fact be capable of producing power in the way described.

Thus this is the sub-system that has to work for the main process to be successful and all its possible variations, and to achieve all that could be achieved via the application of these processes in the furtherance of the creation of Heaven on Earth in accordance with the Lord's Prayer if only the sub-system were to be successful in practice as being day dreamed about herein.

In some of the processes the sub-system may be required to be more successful than in others since in some of them the refrigerant fluid at stage 15 may be more in the distinct liquid phase, which may or may not detract from the transference of the pressure-enthalpy energy to the turbine.

However, tne exampie reTrigeranx cnosen Tor Inelexample aemonstration nerein of the process will not only still be in the vapour-liquid state at stage 15 just prior to passing through the sub-system but the Pressure-Enthalpy diagram that will be constructed for the refrigerant cycle is particularly good for conveying the feasibility of the Applied Theory with all aspects of the cycle being in a fairly ideal state for conveying belief in the process.It, therefore, follows that the refrigerant to be chosen will probably be the ideal refrigerant for the process. But of course the use of other refrigerants could and probably would prove to be equally as ideal in practice. However, the particular refrigerant chosen being Refrigerant-21 of a normal Bpt. under tATS. vapour pressure of 8.92"C and a critical pressure and temeprature of 51 ATS and 178.5"C respectively and the Pressure-Enthalpy diagram cycle for this demonstration model is given on Fig. 2, which I will briefly run through at this stage before then discussing various facets of the process in more detail. But firstly very briefly discussing the two main turbine types that could be employed in the sub-system which may be an aspect somewhat puzzling to some at this stage.

Turbine Types For reasons which will become clearer during the course of ensuing discussion it was first considered that a reaction turbine of the type depicted on Fig. 1 could become the better turbine type to employ for this process if not from the outset of the practical development of the process.

For the as yet uninitiated it is simply a turbine that,when a pressurised liquid flows through,revolves under the same type of force that causes a garden sprinkler of the type revolve or a fireman to be forced backwards when holding a fire hose throuqh which is flowinq water under pressure

with the difference here being thatithe equivalent or the foreman moving backwards under and with the same force of the water pressure, to leave the water standing still on exit from the nozzle. Similarly it is the same force that propels a jet aircraft forward to leave a vapour trail standing still in the atmosphere.In ensuing discussion I briefly discuss this mechanism of transference of power a little further, but for first principles the McGraw-Hill Encyclopedia of Science and Technoloqy qives

a good, readily understanaaDie,1account ot tne type ot mecnanism involved under Propulsion, page 16, more specifically under Propulsion principle.

However, the work then subsequently evolves further and the use of a simpler impulse turbine type comes to the fore once more, simply of the type where a fluid jet issuing forth from a fixed nozzle strikes the impellers of the more normally used impulse turbine typesfor liquid phase systems, e.g. perhaps of the Pelton Wheel type although there could be several approaches depending non the method of operation and in fact

of the

n e%r4ad s dF better1 operation that I finally evolve and bringingthe use of an impulse turbine perhaps back into pole position once more could/would in fact be based uDon a different tvDe of design approach more akin to the

impeller blades of a

turbine, as will become clearer. However, to aid with the discussion in general I include a diagram on Fig. 1G showing a simple sub-system arrangement based upon an impulse turbine of a Pelton Wheel type of design where a fluid jet issuing forth from a fixed nozzle strikes the impeller of the more normally used impulse turbine type for liquid phase systems, e.q, perhaps of the Pelton Wheel type although there could be several approaches depending upon the method of operation and the above possibly better method of operation that I finally evolve and bringing the use of an impulse turbine

pro t7 bls pabRs back into pole position once

based upontedifferent type of design approach more akin to the impeller blades of

turbine

FTg. 1D However, to aid with the discussion in general I includeFediagram on Fig. iC showing a simple sub-system arrangement based upon an impulse turbine of a Pelton Wheel type of design.

Thus, as implied, a number of methods of operation evolve and similarly the choice between whether a reaction turbine or an impulse turbine type could in the fullness of time be dependent on the particular method of operation chosen or necessary for the particular system, again as will become clearer during the course of ensuing discussion.

A description of the Reaction Turbine of the type depicted on Fig. 1 is given in the Mcgraw-Hill Encyclopedia of Science and Technology under Turbine, page 173.

The Pressure-Enthalpy Diagram for the Demonstration Model based upon Refrigerant-21: Fig. 2: The P-E diagram on Fig. 2 is in fact based upon somewhat scanty data, which however should be sufficiently accurate to convey the cycle of the fluid in the process and to convey belief in the feasibility of the process.

Consider the cycle commences at point A on the P-E diagram which corresponds with the circuit at stage 1 on Fig 1, i.e. where the refrigerant should be fully in the liquid phase and just flowing down the pipework entering the flowing waters, 3, towards the submerged heat exchange unit, 2.

If on passing through the turbine of the sub-system the refrigerant does pass on all its pressure-enthalpy energy to the turbine then it will exit at normal pressure IATS. and the normal temperature thermodynamically associated with normal pressure IATS., which for Refrigerant-21 is 8.92"C.

However, if the temperature is in excess of that thermodynamically associated with the pressure of the fluid at any stage during passing through the turbine then a vapour fraction will become produced and the fluid would exit from the turbine as a liquid-vapour mixture with some of the P-E energy having becoming transferred to the turbine, which it must if the turbine rotates at all which it must if a fluid initiallv under a hich oressure is

Dassinq through the turbine. This insteaa1Decomlnq transterrec into tne

latent heat energy mode of the fluid to form vapour fraction as when passing through athrottling device which,however,doesn't produce any turbine energy but dissipates to waste all the energy.However, in the process under discussion some vapour fraction may still become produced but by a very much reduced amount if indeed any at all, because if the turbine rotates which it must then it must do so due to energy from the fluid becoming transferred to the turbine, which it must do in large nroDortion.as anv fluid under pressure Dassina throuah anv turbine, e.a.

as in normal hydropower harnessing or as in the hydraulic fluidjunder more similar pressurisation in a diesel-hydraulic locomotive engine. Thus energy that becomes imparted to the turbine cannot be energy that becomes transferred into a latent heat energy mode and therefore the vapour fraction produced will be very much less if indeed any will become produced at all.

However, if any does become produced over and above the saturated vapour pressure associated with the pressure of the fluid at IATS., or to put it another way, if some heat energy requires to be flashed off then this will flash off in the normal way to create a fraction of fluid vapour that will

enter the enclosed chamber, 14, of the sub-systemjwith the liquid fraction flowing to the base of the chamber as indicated at a temperature thermodvnamicallv associated with the saturated vanour Dressure above. which under the planet's atmosphere of IATS. could itself be IATS. simply

zcans Of by1 feeding the vapour fraction produced back to the intake chamber of the compressor 5 throuah niework under its own steam. which has been indicated on Fia.

1 via pipework 16.

psrC b tLie f/J fd w;i d rCdn - - This/then fluid flux surplus to requirements and simply continuously circulating around its circuit serving no useful purpose.

But the point is that even if a vapour fraction became produced it could be dealt with in the normal way and the liquid phase falling to the base of the chamber would in this normal way still become rendered back at the temperature associated with an SVP of IATS, which for Refrigerant-21 is 8.920C, for any heat energy not becoming imparted to the turbine.

Thus at stage 1 in the process the refrigerant will be all that fully in the liquid phase at a temperature of 8.92"C under its own SVP of IATS.

With any vapour fraction becoming vented off via pipework 16 back to the compressor intake for no extra energy input. However, the compression stroke will require more energy input to deal with the extra vapour and therefore it is probably better to try to avoid a vapour fraction becoming produced. Having said that more heat of compression for removing would become produced with which to generate power via equipment 11 and 1L Which, however, would only have a one-pass heat conversion efficiency of 40% and therefore the overall energy balance of the process would be better if no vapour fraction became produced since then none of the heat energy would become lost in a latent heat fraction if no vapour fraction became produced.

For the purposes of this Demonstration Model of the process it will have fn hP accllmvol that the ntiir1 flowing wstPrc arP thence of thP hntter onllntriPc

which fluctuate around a temeprature of 200C,, in order then to be well in excess of the temeprattre of the refrigerant and that required for absorption of the desired quantity of heat.This then an area where this particular refrigerant would lose its more ideal. nature for use in colder waters as those closer to home, when the process could become based upon R-l14for example,of a corresponding temperature of 3.77"C which could be equally as ideal in practice.

On flowing below the water line the refrigerant liquid will immediately commence to absorb heat from the waters flowing past the pipework and begin to vapourisebecausethe pressure that the liquid will be under will be IATS.

of vapour pressure on both the inlet and exit side of the submerged heat exchange unit, 2, i.e. as the vapour pressures at intake to the compressor 5. Thus under such a pressure then heat flowing through the pipework of the heat exchange unit, which of course it must if the pipework is made of a good heat conducting material, will in effect flash off the refrigerant liquid with the creation of a valour ohase corresoondina with the amount

of heat absorbed. Or to put it another way,ithej'conductinq

reacnes tne iiquia retrigerant1will go into its latent neat energy mode under such a pressure and create vapour by an amount corresponding with the amount of heat that enters the fluids latent heat energy mode.And in so doing the refrigerant fluid will remain at the same temperature of 8.92aC, and on flowing through the pipework will gradually change thus as increasing amounts of heat enter into the fluid's latent heat energy mode, commencing as 100% liquid, then a 90%/10% liquid/vapour mixture to a 10%/90% liquid/ vapour mixture and eventually 100% vapour. Which is a process which corresponds with the fluid state passing from state A to state B on the P-E diagram.The fluid vapour will then probably heat up to the temperature of the flowing waters, i.e. 20"C., which corresponds with state C and which will then be the state of the fluid vapour as it becomes piped to and enters the intake of the compressor, 5, i.e. vapour at IATS. and 20"C. The total amount of heat energy that the fluid will have absorbed from the water in passing from state A to state B and then to state C as it flows through the submerged pipework will be approximately 240 KJ per KG of flowing refrigerant fluid, as indicated by the horizontal linear coordinate of enthalpyri.e.

heat energy. The compressor 5 will then adiabatically compress the vapour, and in this Demonstration Model to a pressure of approximately 100 ATS. to produce aheat of compression temperature of approximately 350"C, which corresponds with elevated pressure state D on the P-E diagram.The amount of additional energy in the form of mechanical compression energy input to the compressor will be equivalent to approximately a further 140KJ of energy per KG of refrigerant fluid flow, which on the P-E diagram corresponds with the amount of enthalpy energy equivalent from point C to point D1 as can become read off from the horizontal enthalpy coordinate, and which in turn is the amount of mechanical energy required to be placed into the fluid in an adiabatic compression of the fluid vapour on following the constant entropy line to the elevated pressure, which will be the course the vapour state will take unders such a compression, i.e. onein which no heatenerqy

is allowed to be lost from the system during the compression/via good thermal insulation of the system.Therefore, from the startinq point of state A there will now be a total of 240 KJ/KG + 140 KJ/KG = 380 KJ/KG

-ntiolp/inrthe fluid at State D which on the circuit diagram Fig. will be the state of the fluid in pipework 6 on exit from the compressor 5.

The fluid will then ao on to have some of its heat removed in heat exchanae

unit 7 under conditions of constant pressure/which then in turn will go on to generate turbopower via equipment 11 and 12 and which will take the state of the refrigerant fluid to state E on the P-E diagram, which is the state in which the fluid will still be at a pressure of 100 ATS but will have become cooled down to around 1700C. which is still ouite a hioh

temperature for the~refrigerant at 1/U.59C with the pressure of the fluid at 100 ATS still well above its critical pressure of 51 ATS. Thus the state of the fluid at this stage, which corresponds with stage 15 on Fig.

1 circuit diagram, could be said to be just in the liquid phase but still with many of the characteristics and properties of the vapour phase from the point of view of the interrelationships between molecules one to another and,therefore,from the point of view of the ease with which they will flow and streamline and impart energy to a turbine. The amount of heat energy becoming removed in heat exchange unit 7 in passing from state D to state E will be approximately 140 KJ/KG of flowing refrigerant fluid, which if then going lnto become converted at a rate of 40% one pass heat conversion efficiency would yield 56 KJ/KG of energy for output supply, i.e. equivalent to 23% of the heat energy initially absorbed from the natural flowing waters, i.e. 240 KJ/KG.Thus a reasonable output rate if this is all such a process would yield for output supply since the natural flowing water heat energy would be free and in abundant supply on site and would be becoming delivered directly to the site by Nature for free. And an interesting aspect to note at this stage is that removal of 140 KJ/KG to give this output supply still leaves 100 KJ/KG of energy in the fluid when comoared with the 240

sa/su initially aDsorDea. but ot course wnat it ls/nopea to De achieved via the sub-system is in effect the recycling of the 140 KJ/KG of mechanical compression energy that subsequently becomes placed into the fluid after absorbing the 240 KJ/KG in order to raise to the pressure of 100 ATS. from 1 ATS.

in what in effect will be a normal turbine-compressor cycle with a difference in that the fluid will essentially be in the liquid phase at the turbine stage.

However, the 100 KJ/KG to spare will further ensure that sufficient energy is likely to become yielded by the sub-system for full sustaining of the compressor energy input. Or to put it another way, at state E there will be aDDroxi

mately 240 KJ/KG of#pressure-enthalpy energy in the fluid#compared with the fluid At state A back at ground state, as can become read off the horizontal axis from point A to point E.

potentially become nlcould potentally become Imparted to the turbine of the sub-system but with only 140 KJ/KG being required to become placed back into the compressor in the form of turbine mechanical energy. Thus this

up to this point would system#need to have an overall efficiency of 58% for the overall process to be very successfull,having itself an efficiency of 23%.Thus from state E, corresponding with stage 15 on Fig 1 circuit diagram, the fluid will become passed through the turbine of the sub-system and commence to impart its 240 KJ/KG of pressure-enthalpy energy content to the turbine, which it must do to some extent as in preceding discussion.

Assuming that the energy only becomes imparted to the turbine to the full extent at the beginning when the fluid still possesses many characteristics and properties of the vapour phase but then may begin to drop off in efficiency of energy transference at some stage during the process,on Following a straight line from state E to state A by the time the fluid reaches the Sat, liquid line at state F the fluid would still possess approximately 100 KJ/KG of energy and still be at approximately 30 ATS at 80 C from the 100 ATS and 1700C at state E at the commencement of the process and could have already imparted 140 KJ/KG to te turbine of the sub-system. Thus, the process is beginning to sound as though it may be feasible.

However, firstly still at the P-E diagram stage. An aspect to be aware of is that the less the temperature of the fluid vapour on entry into the compressor then the less energy input that will be required to raise the fluid vaDour to the Pressure of 100 ATS. and 3500C because the less the

initial temperature then the closer1the constant entropy line of the adiabatic compression to the vertical. However the less will be the total energy content in the fluid at state D but only by a pro-rata amount, with the advantage that the energy then required to be recycled back to sustain the compressor will be less with the same amount of heat energy initially having been absorbed, i.e. the 240 KJ/KG from state A to state B/C.

This aspect therefore being the reverse of optimum conditions discussed for the process under my Patent Application No. 872601 which required the constant entropy line to be at a miximised slope from the vertical.

However, having said that there could be advantage in pre-heating the vapour further which could be achieved via transferring some of the recycling heat from the turbogenerator equipment, 11, into the vapour flow at stage 4 then going on to transfer the remainder into the refrigerant at stage 1, ason Fig.. 1A. Which will then be capable of achieving an appreciably higher temperature for the same elevated pressure of 100 ATS. which would then in turn be capable of generating at a higher working temperature to bring a steam turbogenerating process well within the range of the process.

Whilst for the temperature of 350"C chosen for the main Demonstration Model herein it is intended to use a refrigerant fluid of lower Bpt than water as the fluid in the turbogenerating part of the process, i.e. as the fluid from which vapour pressure will be generated in the vapour generator, and then flow along pipework 17 to the turbine 12. Or conversely if the vapour flow at stage 4 becomes pre-heated before entry into the compressor then this would enable the same temperature of 3500C to be achieved for a lower level of vapour pressurisation, which however would require more energy input because the constant entropy line to the desired heat of compression temperature would be leaning over further from the vertical.However, from the point of view of transferring energy to the turbine of the subsystem then there may be advantage in commencing with a maximised fluid pressure, which if so and when coupled with an advantage of less energy input required to be placed into the compressor then this could be the better way to operate the process. Which if so could mean that a steam based turbogenerating process could in fact be better than that intended to be used in the main Mathematical Model herein because with no subsequent

the compression would continue along the same constant-entropy line as that on the P-E diagram to a higher pressure to achieve the heat of compression temperature level that would then be required.And therefore on subsequent harnessing of the fluids energy in the sub-system the energy may become imparted better if commencing at an even higher pressure and the same temperature as state E on the PE diagram, e.g. if commencing at say state G. Thus in practice it will be a question of choosing the most optimum fluid for the turbo generating part of the process and then finer optimisation of all the parameters involved in order to maximise upon the energy balance of the optimum process.And of course the fluid used in the

half of the process whilst being independent of the fluid used in the turbogenerating part would also have to be a part of the optimisation since some could perform better than others in terms of the energy recycling cycle possessing as they do differing critical temperatures and pressure points and latent heat absorption capacities, etc., and obviously the normal Bpt of this fluid in relation to the temperature of the available flowing waters would have to be right in the first place, although with respect to the latter aspect a method becomes evolved herein which could potentially facilitate for use with variable water temperature.

Relating further to the P-E diagram of the process under the aforementioned Patent Application, which in contrast and in reverse was that of a turbogenerating process. However not fully in reverse because the line from stateA to the equivalent of state E on that diagram, i.e. the energy required to be placed into the liquid phase in the first place in order to raise to and thereby overcome the pressure of the vapour pressure above, would not in fact be to the equivalent of state E on this P-E diagram, but rather to the equivalent of hypothetical state H since at such a stage in such a process there is not yet any other added energy to the fluid.

Whilst in the reverse process under discussion at the stage the turbine will harness the energy of the liquid phase the liquid will contain all the added energy represented by the difference in states between state H and state E, as can be read off from the horizontal axis, and in the main Demonstration Model herein comprised of the equivalent of all the absorbed heat from the flowing waters, which is energy that would not be in the reverse system of a turbogenerating process at the point of pressurising the liquid phase thereof to equal and thereby overcome the vapour pressure of the vapour phase above and acting down on the very much colder liquid phase at the respective stages in the two process.

Now going somewhat deeper, albeit in my somewhat unorthodox, unconventional and old fashioned manner, mainly based upon experience and not really in the mould that has become established, for which I apologise in advance.

Ten coming back to further of my discussion on the P-E cycle of the process, which I suppose could also be deemed to be old fashioned discussion in a more traditional and early mould of generations past. But everything has to start off life at a basic beginning and therefore I hope the modern scientific fraternity will bear with my somewhat simplistic, early stage, deliberations still in the breaking through phase, and the significance of the above discussion will become more apparent during the course of my further deliberations.

For this firstly recalling my early days at Cromptons conducting fluidity viscosity testing on dissolved paper in the solute cuprammonium hydroxide.

For the same mass of dissolved paper in the same quantity of solute for the same initial potential head of resultant solutions I well remember that some solutions exited from the base of the columns of liquid at a very much slower rate than did others indicating a very much stronger paper but a very much lower kinetic energy value for the fluid flow exiting from the hole at the base of the column of liquid, if one was interested in such a value. Thus, for the same mgh value for the columns of liquids some gave a very much higher kinetic energy value for the resultant flows of the liquids coming out of the hole at the bottom of the potential head. Similarly in the case of my experience in testing the viscosities of different inks and paints. Therefore, developing further.

However firstly it should be fully understood that whilst in the Demonstration Model I commence with the fluid in the liquid-vapour region it is fundamentally the pressure-enthalpy energy of a liquid that is becoming harnessed in one of the two main wavs that the enerav of liauids under Pressure become

narnessea, i.e. via X reaction turbine1type depicted on rig 1 or via an ordinary impusle turbine type, e.g. a Pelton Wheel. And not the expansion energy that becomes harnessed when the energy of a vapour under pressure becomes harnessed as vapour expands to a lower pressure and temperature.Although this type of energy harnessing would seem to be that which Stoecker on page 37 of his text book 'Refrigeration and Air Conditioning' is referring to which he quite rightly states would not be possible to acquire but then differing in that he then draws the conclusion that the pressure-enthalpy energy content of the fluid at such a stage in such a circuit could not become harnessed.Whilst I am postulating that the energy should he harnessable in the wav under discussion However, if one were to simply acquire

thelnormal mgh value of the pressure head as for a cold liquid then following calculation will show that one would only acquire about one twentieth of the 240 KJ/KG of pressure-enthalpy energy from state E to state A on the P-E diaqram of Fi9 2, and which it is being postulated should

'nort sabl ro Sote sextet 6r cher belharnessable,in the way under discussion.

How this will arisetbe due to the fact that the heat energy contained in the fluid and not present in cold liquid at normal temperature but present in the liquid fluid at state E at a level of 240 KJ/KG of heat energy above the heat energy content of cold fluid at state H, will loosen the Van-der-Waal bonding between molecules to such an extent that the fluidity of the liquid will in turn increase to such an extent that when under a given pressure head the liquid mass of the hot fluid will flow from the bottom of the fluid head at a very much increased fluid flow rate and such that the kinetic energy of the hot fluid flow will be some 20 times that of the normal cold fluid

pe-r nl t of flçtd tass f l flow/ As following data, calculations, equations and further discussion will tend to confirm.

Which, however, is probably more a mechanical engineering view of the mechanics of the fluid flow system rather than that of a thermodynamic expert, but it is what would happen in practice and be the practical effect of the heat on the fluid and be the property of the hot fluid, i.e. its fluidity, that one would probably measure in order to predetermine and pre-set the dimensions of the harnessing turbine nozzles in order to harness its pressure-enthalpy energy. However, it will be a system that one could approach in a number of ways from the foundation of scientific knowledge now built up. From the pure theory of the effect on the Van der Waal bonding between molecules.When the addition of heat to the fluid will cause the electrons surrounding each molecule to excite and be raised to a high energy state creating an increased level of electromagnetic forces surrounding each molecule all of like poles which will therefore then push each other apart with more force than when in the cold state when the opposite poles at the centre of the moleculesiolrld have a higher effect in attracting the surrounding opposite poles of other molecules around. One could perhapsenvis2ge the electrons surrounding each molecule to be in concentric speed lanes increasing in speed from the centre around a circular speed track with higher heat levels then raising the electrons to higher speed lanes and therefore the overall range of speeds covered by the electrons.To have the effect of creating a higher overall level of electromagnetism surrounding each molecule, all of like pole. Which will then cause a

effect between molecules of higher intensity, whilst the opposite poles in the centre will not be able to exert as much attracting force on the other molecules via attracting the opposite poles surrounding each molecule whon through the higher opposite pole surrounding each molecule.Thus the

molecules one to another will be less loosely heidtwith a high level ot-

heat content in the fluid compared with theiVan der Waal bonding that wsllS;ke place when

which in turn will cause them to flow faster when under an applied pressure than the cold liquid would flow under the same applied pressure and therefore a given mass of fluid would possess a higher 1/2mv2 energy value on flow when hot than when cold.Basically because each molecule would be randomly moving around in the hot liquid at a faster rate prior to causing them to flow all in the same direction, just as in the vapour phase, Ref: Open University S101 Science course Unit 8 page 41, due to the looser Van der Waal bonding between molecules and therefore when they are all made to flow in the same direction they will still be travelling faster one to another and create a faster flowing flow under a given applied pressure. Just as in the case of a vapour.

However, in a vapour some of the initial kinetic energy becomes lost by transferring back into the latent heat energy mode on expansion/depressurisation.

Whilst for the equivalent in the liquid phase perhaps the fluid flow will slow down quicker on transferring energy from the liquid to the turbine, when cooling and depressurisation will take place, due to contraction of the fluid on cooling through higher Van der Waal attraction forces becoming created on cooling. Causing the impartation of kinetic energy of flow to tail off quicker, e.g. as when flowing around the curves of a pelton wheel type of impeller, than one would expect.You see, whilst for a straight line change on a P-E diagram one can read the associated energy change as enthalpy energy equivalents directly off the horizontal axis. the oressure-enthalov energy content of the fluid is reallv reDre-

sented by the area beneath the lineof change and therefore if, being postulated, the change from E to A gives a concave curve to give less area beneath the curve in going from E to A then one would not be able to read the associated energy change in enthalpy energy equivalents directly off the horizontal axis in the way that I have been doing so far for this

energy change. / J J as hot compressed fluid the energy content is upgraded enthalpy energy, which on the loss of some energy will not then be the initial upgraded level of energy less the transferred amount of energy but will be at a lower level of upgraded energy than the foregoing would quantify. Which is easily explained by a consideration of the h my2 energy equation and due to the fact that energy is related to the square of the velocity of the molecules and not a linear relationship.

Thus as the molecules slow down on cooling their transferable kinetic energy will slow down at a faster rate by a squared realtionship. Or to put it another way, the original intake of absorbed heat becomes upgraded to a higher level and will be at a certain level of upgraded i mv2 energy at a certain level. But now if one loses some pressure energy by transference to the turbine then the remaining absorbed heat energy will not now be at the same level of upgraded energy because it is now under a

lower1 pressure and therefore the new energy content will not be the original uDaraded enerav less the amount that has been lost because the associated

loss of1 pressure energy will itself cause the remaining absorbed neat energy to be at a lower upgraded level. Which is postulated theory that cross-links with that given on page 112 of my Patent Application No. 8728601.

Thus the loss of energy will not be at the rate of loss of increments of the original d mv2 level of energy, which is the origin of logarithmic pressure axis arising from the v squared relationship with pressure drop/ temperature drop, but each increment loss of h mv2 energy will be at a lower level of d mv2 energy each increment. In turn arising from the fact that on cooling the Van der Waal bonding between molecules becomes stronger drawing the molecules closer together to a lower level of b mv2 energy content than that represented by the original my2 level of energy less that which has been lost. Thus the loss of energy may not follow a constant line to give a straight line relationship between pressure and enthalpy energy but may be a concave line.And could perhaps be the opposite of an isothermal expansion to an adiabatic expansion, where the former yields around twice the energy of the latter and would be a convex curve on the normal P-E diagram in comparison to the straight line of the adiabatic expansion in following the constant entropy line for such an expansion. To therefore yield around half the energy than that represented by the enthalpy energy on the horizontal axis, which on the cycle under discussion does represent the original intake of heat energy as at constant pressure. Thus the loss of energy moy not follow a constant line where for each increment loss of energy the ratio of energy to temperature remains the same.Or to put it another way,

tne rate OT lOSS Or temperature, i.e. speea or moiecuies, I at tne same rate, but rather the deacceleration of the molecules rrag be at a faster

rate than the rate of each increment of energy, to1 not gave a constant line for loss in energy on the P-E diagram but a concave line.

Ho S evera getting back down to Earth and to the more practically orientated theory. Out of which however I may not have as firmly concluded as I may from such an approach to the system that one may only acquire around half the energy of the total originally in the fluid down to ground level.

when one considers this aspect also from the point of view of the fluidity property of the fluid then one arrives at the same conclusion because the fluid fluidity will not remain at the original fluidity but become thicker with loss of each increment of energy due to the cooling that takes place with loss of each increment of energy.With the effect that perhaps for the total energy obtainable from the system one should base on the mean fluidity of the fluid over the range of fluidities that it passes C" through on passing to ground state, rather than simply1 the initial fluidity of the fluid at its hottest. Which is postulated theory that becomes confirmed via the above approach, which also usefully cross-links with the postulated theory on a similar theme under the aforementioned PA to confirm that theory.

has evolved in my mind the foregoing aspects of the system have become clearer and in later discussion it becomes concludeda z

that the line of the depressurisation of the fluid is1likely to follow the curve of the liquid line on the fluid's P-E diagram, which will arise from the fact that at the start the upgraded fluid could potentially transfer all its P-E enthalpy content and finish possessing none, but of course the final liquid state will still possess P-E enthalpy energy from the final state down to absolute zero.However, the curve from the upgraded state down to the final state will be determined by the rate at which the fluid contracts and in effect it tus be this energy of contraction that will be left remaining in the final liquid at the end of the downgrading process and resulting from transference of kinetic energy to the turbine in this case. Moreover, it then becomes clear that the energy that could pctcntså become transferred to the turbine will be that amount that can become directly read off from the enthalpy axis of the P-E diagram from the initial upgraded state to the final liquid state at ground level.Thus in the upper half of the curve,fluid contraction subtracting from the fluid jet's ability to transfer its kinetic energy of forward motion will be at a

slower rate~ then will begin to influence the transference of kinetic energy at a faster rate on the steeper lower half of the curve. To finally finish having re-possessed a proportion of the initial external kinetic energy by an amount which will correspond with the amount of P-E enthalpy energy that the final liquid would have to contain to exist in the final liquid state. However, having concluded thatsif one had a linear pressure axis on the P-E diagram then perhaps the depressurisation line would be straight or even concave in practice.Nonetheless the foregoing conclusion could still hold when considering in the context of rate of energy transference, i.e. energy transferred in unit time, since energy will become transferred at a faster rate the higher the fluid pressure for a unit of pressure drop in pressure. On the other hand perhaps fluid contraction subtracting from transferable energy would take place at a correspondingly faster rate the higher the pressure of unit pressure drop, On the other hand perhaps fluid contraction subtracting from transferable energy would take place at a coCrespondingly faster rate the higher the pressure of unit pressure drop.

However at this early stage in the evolution of the work I will remain with discussion based on the foregoing

but which may not be wholly correct at this stage with respect to such aspects of the system but suffice it to sav here that as a general rule of thumb.

the initial P-E enthalpy amount may become reduced in the directlratio of fluid volumes before and after the turbine with respect to the amount of the energy thereof that could become transferred to the turbine, which is an aspect of this type of liquid based system that becomes concluded will be the equal and opposite of an energy proportion entering the latent heat energy mode in a vapour expansion harnessing system where the fluid, of course, expands in further equal and opposite contrast.

general energy balance equation can be expressed as follows: E = mgh + i p + t PV + U In which: represents the sum total of all the energy involved, which could be all,or some, or anyone of the 4 types of energy on the RHS of the energy balance and are as follows the energy present that may be stored as the energy of a potential head of liquid phase or as the pressure of a gas, vapour, or steam,acting down on a liquid phase, as in the system under discussion when IATS. of pressure above normal IATS. pressure is equivalent to 33.4 ft of water mass acting down under the forces of gravity

Amv In the svstem under discussion it is, hoped to convert all the enerv present

into this form of energylsa liquid phase fluid flow with as fast a velocity as possible, consuming all the energy present in order to render as fast a flow as possible, in order that in turn the liquid flow will then possess a maximised quantity of kinetic energy of forward motion on harnessing by a suiable turbine able to harness a maximised amount of the kinetic energy of the fluid flow as efficiently as possible, e.g. a Pelton Wheel

turbine as in nyoropower narnessing whlct/lnsteau or a vapour pressure acting down on the fluid flow has a head of water acting down on the fluid jets of such a system.

a PV This represents the energy that may be obtainable from a system in the form of expansion energy as expansion takes place from a small volume under a high pressure to a larger volume under a lowered pressure. However in the system under discussion the potential for this type of energy will not be present, since it only applies to the vapour phase of a fluid and on the contrary some conraction of the liquid will take place on cooling to probably result in reducing the commencing kinetic energy level that actually becomes harnessed to perhaps half of the commencing kinetic energy level, as discussed in the preceding and as will become further discussed.

U This represents anv heat energy nrcsnnt.which will be Dresent in the svsterri

under discussion andlit is hoped will add to the mv level ot energy produced in the liquid flow on harnessing the potential head energy in the ways being discussed. In practice by increasing the fluidity of the

liquid tiow to cause it to flow faster under a given/potential head of pressure as created by the continuous production of compressed vapour at stage 6 on Fig. 1.

The faster the velocity of the liquid flow then the more kinetic energy of forward motion that it will possess and the more energy it will impart to the turbine in accordance with the energy equation: KE = lmvz

Thus the faster a given massifs travellingthe more impartable kinetic energy of forward motion it will possess.In the remainder of the fluid's circuit the same mass could cycle around the circuit at the same speed it would normally do, but if in the sub-system part the presence of the heat causes it to flow faster through the turbine thereof than it would normally do then more energy will become imparted to the turbine by a correspondirqamount, with the same mass of fluid then continuing on around the circuit at the same speed it would normally do until it gets to the turbine of the sub-system again, when the increase in its speed through the turbine will depend upon how much heat is left remaining in the liquid after the heat exchange system of the preceding stage, which of course could be a variable of the system and in practice it will be a case of balancing the two ways that energy becomes harnessed in the process in order to maximise on the total energy that becomes produced. With then the required proportion of energy becoming recycled inernally to the comressor from any or both of the two sources of turbine energy production and the remainder being for output supply.Whilst the work herein so far has shown that the commencing level of kinetic energy at the sub-system turbine could be well in excess of that required to be recycled internally in practice it will depend upon how much of the commencing energy can actually become harnessed under the probable conditions of the contraction effect in the liquid on cooling under the strengthening of the Van der Waal forces therein on cooling reducing the potentially harnessable energy by an unknown amount at this stage. Which could be around half.

However, in the case of the example system under discussion based upon the refrigerant fluid R-21, since the volume of fluid at the critical point is 1.9 cc per gram compared with 0.73 cc per gram for the liquid at 250C under normal SVP pressure for this temeprature, representing conraction to 38.4% of the commencing volume, then perhaps this is the reduction in harnesable energy that one would acquire. If so then it would be very much the same level of energy reduction that takes place in harnessing the expansion energy in the vapour phase due to loss into the latent heat energy mode in such a case.

commence off around 40% and from such a starting position become improvable to ày 50%.Which if so would then be better than the one-pass efficiency level achievable via steam turbogenerating systems now at a maximised level of 40%, and therefore in such a case one would maximise upon the energy that can become harnessed via the sub-system which however could not take place to the total exclusion of the turbogenerating process since one would have to remove heat energy to render the fluid in the liquid phase in the first place, and all the heat energy would have to become converted for the process -to produce any surplus power for output supply. Unless one simply wanted a Heat Plant based on a process that could harness the natural heat contained in the natural sources under discussion. When one could remove heat by an amount

to leave the sub-system just capable of sustaining the compressor.

Thus, for a power process one would require both heat conversion systems operating in the process simultaneously and alternatively it may be found in practice that one would maximise upon the amount of one-pass energy that could be obtained via the turbogenerating system, and then harness any residual energy in the liquid phase via the sub-system maximising as much as possible for the amount of residual energy left. On the other hand, such maximisation may take place when one leaves sufficient heat in the fluid to leave it still in the critical temperature region at the start of the sub-system process.A point to be aware of is that this aspect of the process is concerned with the one-pass heat conversion efficiency levels and not the overall conversion levels as possible to become improved upon by recycling heat for a further pass through the turbines, since the compressor has to be kept continually going and therefore the required quantity of energy for recycling tolcompressor will be required on each pass through the turbine, over and above which the process has then to produce a surplus of energy each pass for output supply. Having said that the latent heat energy from the turbogenerating process will be able to become recycled, whilst the corresponding loss due to liquid phase contraction in the sub-system would not be recyclable energy in the same sense, Therefore since the latent heat energy of the heat passing around the turbogenerating circuit is recyclable then this too could be a reason for maximising upon the amount of heat conversion via this route since this would enable one to minimise upon the fresh heat absorbing equipment which in turn would lower capital costs which in turn would be the only costs.And especially so if the whole process was automated with no ongoing labour costs being required. There will also be a further reason which I

in ensuing discussion but briefly stating here that in my first efforts to overcome present day thinking on Throttle Energy Conversion I spent many months on a writing I have referred'to as Throttle Energy Conversion in past correspondence informing people of the work that I am carrying out with a view to attracting some interim funding. Tn'hilst at that stage no funding was forthcoming from any of the quarters tried that work, whilst only halfway to the full depth of understanding I have evolved of this system nowconcentrates on a possible method for increasing upon energy output from the sub-system by means of partial vacuum creation on the exit side of the turbine of the sub-system, which if successful could overcome some of the reduction in energy due to liquid contraction by drawing the liquid, which in effect would probably reduce the level of fluid contraction or to put it another way maintain the liquid closer to the commencing volume on cooling as it passes through the turbine to in turn reduce the level of reduction in energy due to contraction. Or it may simply cause the liquid flow to flow faster increasing the energy output by an amount corresponding with the power of the partial vacuum.Either way the technique may be capable of improving upon the energy output to levels of 50 to 60 to 70% from the poss'ibiM starting point level of 40% and in so doing add BGS general to the total energy Production level,

I.e. Deiow around alalezenergy, wnicn rrlby Decome maximisea upon the colder the starting point temperature of the fluid since one would then be commencing the process closer to ground state. However, in comencing at a lower temperature then the initial potentially possible kinetic energy level would of course be lowered and it may not be as efficiently harnessable.On the other hand it should be remembered that even at a substantially lower initial temperature for the process the fluid would still be close to its Bpt and a very long way away from its Fpt. which for R-21 is -1350C under normal pressure.

Unlike when harnessing water at normal temperature when it is in a state very close to its solid state. Thus the Van der Waal bonding would still be very loosened. Moreover, just a little extra sub-cooling would take the system further away from the liquid vaporisation line to reduce the risk of loss of energy via transference into the fluid's latent heat energy mode. Thus via sub-coolingto an optimum one could maximise upon the amount of BGS energy possible to acquire by applying the partial vacuum technique to the liquid turbine system, whilst at the same time maximising upon the amount of heat going around the turbogenerating cycle.Thus whilst at one stage I have considered that the earlier work may not be too applicable in practice it could well be that one would in fact aim to add as much BGS Energy to the liquid turbine system

which would probably require sub-cooling to an optimum level between on the one hand partial vacuum creation and on the other maintaining Van der Waal bond loosening, and in this way maximise upon the total amount of energy becoming created between the two systems. It also occurs to me that in sub-cooling further then the fluid contraction on further cooling at the turbine stage of the sub-svstem would be less because the commencing volume would be less and

therefore in this way one couldjmaximise upon one-pass energy conversion level.

Thus it is beginning to seem that the earlier work could be far more useful than I subsequently considered that it may at one stage in the evolution of this process since most factors involved are now beginning to point to a modus operandi in which one may in fact try to maximise upon partial vacuum creation at the liquid turbine and in this way maximise upon GS Energy addition to the total energy output, in turn maximising upon the total energy production between the two systems.

It is of course also becomingapparent that there are many facets of the liquid system that are very similar to the various facets of the vapour system, either having an equal and opposite similarity or a more direct similarity. The latest of these being that the technique that may be possible to apply to try to create a partial vacuum on the exit side of the turbine will be akin to condensation vacuum energy creation in the normal vapour system, which as will become clearer in the ensuing discussion of the system will be in an \inside- Oiltl category of similarity.

Taking this opportunity to recap, some of the other similarities being:1. Reduction in harnessable energy due to Van der Waal contraction of the fluid being akin to loss of energy in the latent heat energy mode of a vapour based system in which the fluid vapour expands in further equal and opposite contrast.

2. Optimising for a vapour compression constant entropy line close to the vertical being equal and opposite to optimising for the vapour expansion constant entropy line to lean over from the vertical as much as possible.

3.

sub-cooling of the liquid prior to entry to the harnessing turbine would be equal and opposite to optimised super-heating of vapour prior to entry to the harnessing turbine. Perhaps to a minimised level in contrast to a maximised level to give further equal and opposite similarity.

4. Perhaps the energy of the liquid would become harnessed via harnessing it as a reaction force via the type of reaction turbine depicted on Fig 1, which in the original work was chosen because it was considered that the partial vacuum power could become better applied to the liquid flow via such a system, which would then be equal and opposite to harnessing the kinetic energy of a vapour flow via harnessing it as impulse energy.

5. Maximising upon the pre-expansion of a vapour flow would be equal and opposite to maximising upon the pre-liquid contraction before passing through the liquid turbine.

6. All of which together with the partial vacuum aPPlication similaritv with

conaensation vacuum application in a. vapour system1amout to six fairly

convincing reasons why one shouldlhave reasnable faith and belief-in the system at this stage. However it is all in the mind at the moment and therefore continuing on with this expansion of my first draft of this discussion on the process. Which I continue on with as follows.

If one considers the sub-system from a mechanical engineering standpoint then one may look at the system and think yes, one should be able to harness

mgh value of the liquid phase as under the potential head of the/vapour pressure acting down on the liquid phase in the normal way and where IATS. of pressure above the liquid phase over IATS. normal pressure would give the equivalent of 33.4 ft head of water.But one's consideration may only go this far and one may not go on to realise the effect of heat in the liquid phase of such a system and more specifically the effect that this would have on the amount of kinetic energy of forward motion that could then become created in comparison to a normal

system-wnen tninKing would Delreiated to nyoropower narnessing or cola water which

commences with the liquid very close to its freezing point and therefore very close to the solid phase of the liquid in the first place. Although in such a system it could prove possible to add BGS Energy to the power output by means of the technique mentioned and farmer discussed

At this stage therefore, firstly considering the energy that one would obtain if just the mgh energy component of the system became obtained. Which for the example being given based on R-21 would be as follows: E = mgh = imv 2 When for a normal hydropower system: m = mass of water in lbs g = force exerted on the mass of water due to gravity as 32 ft/secz h = the height of the head of water in feet Which gives the answer in Ft poundals and to convert to Ft. pounds requires dividing by 32. And therefore the equation in such a case can be regarded as E = mh.

Thus for the system under discussion it will simply be a case of converting the pressure acting down on the liquid phase into feet of water potential head equivalent. Then inserting in the equation E = mh to give the answer in Ft lbs.

Thus m = mass = 1 KG = 2.2 Ibs h = 100 x 33.4 Ft.

Therefore E = 2.2x 100 x 33.4 Ft. lbs = 7348 Ft lbs (weight) 1 KJ = 737.6 Ft ibs (weight) Therefore: E = 7348 = 10 KJ/KG 737.6 Thus just 10 KJ/KG and not the 240 KJ/KG that is initially present in the fluid at State E on the P-E diagram of the process on Fig. 2.

Therefore, a way to view the system is to first consider that a

that had been sub-cooled all the way down to normal temperature whilst still maintaining the pressure of 100 ATS acting down on the liquid and in the absence of any technqiues aimed at obtaining BGS energy would give 1OKJ/KG of energy on harnessing in the normal ways of harnessin hydropower down to normal pressure. Which of course could be a way to operate the process and in being at such a high level of sub-cooling then there would be no risk of a vapour fraction becoming produced during the harnessing of the pressur energy that the liquid is under. Then from such a starting position consider the effect of adding heat energy to the liquid on the one hand and on the other, the effect of

iPPpSpossible techniques for adding BGS Energy.Therefore at this stage just considering further the effect of adding heat energy. Although in the fullness of time it be a case of finding the optimum position between these two parameters as in optimisation with heat energy harnessing via the linked turbogenerating process in order to maximise upont he overall energy balance of the process.

Basing on the value of 10 KJ/KG for the normal energy yield from such a system this energy yield would have to become increased by some 20 times in order to approach the 240 KJ/KG level of energy yield. Which sounds a lot but, reducing to 200 KJ/KG to err on the conservative sides would only require the velocity of the fluid flow to become increased by 4.5 times in accordance with the equation KE = 12mv2 in which the actual fluid flow velocity for 20 times more KE would only be required to increase by 120 = 4.5 times.It is important to grasp here that this is not to say that the fluid mass flow rate inpipework 6 or at stage 15 or at any stage before the turbine would have to, therefore, be travelling 4.5 times faster, and to help with better understandin of this aspect I will refer to the use of an impulse turbine of the type discussed in the preceding. If the mass flow rate were to have to increase by 4.5 times then of course the mass parameter in the equation would increase by 4.5 times in unit time, which

stay at unity and in fact in practice could only stay at unity anyway

the increase in the velocity parameter taking place and causing the increase in the energy of the fluid flow at this stage in the circuit of the fluid's cycle.Therefore, trying to clarify this aspect further by referring to the diagram of the impulse turbine on FigiC. Under conditions of a higher liquid fluidity giving rise to a higher velocity liquid flow under the given applied pressure of 100 ATS., then for the mass flow rate to remain the same one would have to reduce the CSA dimensions of the nozzle creating the liquid jet for impact with the impellers of the turbine. In order then for the same mass of fluid to exit from th nozzle in unit time. Otherwise if one left the nozzle at the same GSA dimension then the effect would be to lose all the pressure.

Thus in order to maintain constant pressure conditions the mass flow rate would have to remain constant and with a liquid possessing a higher fluidity giving rise to a higher velocity flow under a given pressure then the CSA dimension of the nozzle would have to be reduced accordingly. Then the same mass of liquid would be flowing out of the nozzle in unit time. However, by the same token in order for that mass of liquid to exit from a much smaller sized nozzle in the same time, then it would have to be travelling at a much faster speed through the nozzle exit by a corresponding amount. Which is theory that crosslinks with the system under my Patent No. 2126963 entitled 'Air Power for Propulsion'.

Therefore, in the equation KE = inv2 the mass parameter will be the same but the velocity parameter will become increased in accordance with the increase in the fluidity property of the liquid on heating. However, it could

be argued ,.that the velocity parameter in the equation relates to the

mass riOw rate, which in terms or the time it-takes a given togas mass to go from the exit

to the impellors of the turbine will in fact remain the same and in such a sense the velocity of the mass will indeed

remain the same. However, I ask you to consider two identical large1 masses each comprised of the very same number of very tiny identical micro masses of liquid fluid.The first called large mass A, which is the cold mass, and the second called large mass B, which is the hot mass. Now consider the kinetic energy of forward motion of each micro mass in both large mass A and large mass B. Those in cold large mass A will have a KE = i1 x 12, and those in hot mass B will have a KE = i x 1 x 4.5', in comparison and if my theorising is correct.The criteria for which being that given these are the KE values of each of the respective micromasses in each of the respective large masses, can they have such KE values for the same large mass flow rate.

would be simply given by the numberof micro masses times the mass of a micro mass and would be the same in both cases,

the sum of the KE values of take micro masses travelling from nozzle to impellor gor each

4.52 = 20 times more in the case of the sum of the KE values of the hot micro masses in comparison to the sum of the KE values of the cold micro masses exiting out of the jet nozzle. But the total large mass transferred in unit time would be the same for both masses.However

that the micromasses would possess the above differences in KE values between the hot and cold micromasses and that the total KE values would be the simple arithmetic sum of all the KE values of each micromass in each large mass and that the total mass transferred inunit time would be given by the identical number of micromasses times the identical weight of each identical micromass.

Thus, what I'm really trying to say is that the mass flow rate would remain at unity but this would not be the velocity value that one would place in the

equation KE = imv' for the two systems, but rather1 the velocity value at micro masses. Then times their number to give the mass flow rate. In effect one could visualise the hot micromasses having to queue up in a longer queue to pass through a smaller GSA nozzle, with each then having to travel faster in order for the same amount of fluid to become transferred in unit time. But in each travelling faster then on impact with the impellors of the turbine they each impart 20 times more energy if having to each travel 4.5 times faster.

Than do each of the same number of cold masses travelling 4.5 slower from nozzle to impellor. Slight confusion here, but simply clarified because remember in the cold micromasses able to go through a larger GSA nozzle for the maintenance of fluid pressure then more would go through together side by side by a pro-rata quantity and therefore whilst each is travelling 4.5 times slower more are goingthrough together side by side, i.e. in parallel as opposed to in series, to keep the large mass flow rate the same.But each will still impart 20 times less energy on impact and there will be the same number becoming transferred in unit time, and the sum of each micro mass energy will be the total energy transferred for the transference of a given large mass which will therefore be 20 times less for the cold mass but the total amount of mass transferred in unit time will be the same.

Or to use more scientific terminology one should view the system in terms of lagrangian description concerned with individual particles in fluid flow rather than in terms of eulerian description concerned with mass flow rate when considering the kinetic energy properties of the respective fluid flows.

The foregoing treatment of the description confirming this view.

Thus the effect of the heat on the fluidity of the liquid phase would in practice onlv have to increase its fluiditv bv 4.5 times in terms of the velocitv that each individual

therein would flow1 under a given applied pressure tor the flow to then be capable of imparting 20 times more energy to a turbine for a given mass flow rate. Which would seem well within envisionable range recalling my fluidity testing days when some would take of the order of 30 seconds and others 5 minutes, and considering the amount of heat present and the effect this would have on the shearability between adjacent planes of fluid flow.

Thus one could set about acquiring the mgh value of the system in the normal way for such a system and in the way that one would for such a system. Which lroveyeRwould not work unless the liquid had first become sub-cooled all the way down to normal temperature because the pre-determined GSA of the nozzle jet creator would be too large for the increased fluidity of a hot liquid and one would probably disappear in a hot cloud of vapour.

But if one did then reduce the GSA of the nozzle to that required for the fluidity of the hot fluid and indeed to that required to maintain all the fluid Pressure in the circuit from compressor to nozzle exit. then based

upon tne tfleorising to rate one snoula ot)tain morerKinetic energy ny an amount

corresponding with the level at added heat energy present but/less by the reduction that liquid contraction will make as the micro masses impart their kinetic energy.In other words when the liquid micro masses impact with the impellers of the turbine their impact will become reduced because the internal forces of Van der Waal will draw in the micro mass to a smaller volume and tessan the impact to some extent or other. Um. Big question mark here to some extent. However, I remain with the view that the reduction can be no more than the percentage represented by the change of volume, if that, as

in toregoing discussion, i.e. perhaps a/reduction to 40% from the theoretical maximum, For this liquid phase systeme perhaps there would be a gradual shift from the langrangian description to the eulerian description of the system as the temperature on sub-cooling approaches ground temperature.When at ground temperature the description type becomes fully eulerian in any case because then just the straight mgh value of the system would be obtained with no increase in adjacent layer shearability due to heating, etc.

Thus each micro mass of liquid striking the impellors of the turbine would probably simply Dull their initial nunches to some extent or other. but

remember they would be solid micro masses of liquid andleven more solid as the Van der Waal bonding tightens up on the liquid phase becoming cooler and more 'liquid'.

At this stage therefore saTe data on increase in fluidity with temperature for the liquids concerned is required in order to further confirm the theorising to date. However, firstly before quoting some actual known values the equation actually relating viscosity to flow velocity is as follows: = (P1-P2)r4t 8V1 Where (P1-P2) will be 100 ATS.

r = the radius of the jet nozzle 1 = In the context herein this could be regarded as unit length, 1, of fluid jet that a given volume of fluid will pass through in time, t, ie, the forward velocity of the finally created fluid jet, as becomes further deliberated upon.

V = the totalvolume flow flow rate in unit time, i.e. not the linear forward velocity of the fluid jet, which will be dependent upon the radius.

Really therefore it is the relationship towards, the length of the queue, that we are concerned with here, which in turn is determined by the nozzle radius.

For a given system everything will be constant including mass flow rate and therefore viscosity will be inversely proportional to length of liquid in the liquid phase jet queue in unit time, i.e. to its linear forward velocity, and since fluidity is the reciprocal of viscosity then the linear forward velocity of the liquid jet will be directly proportional to fluidity which in turn is inversely proportional to viscosity. however I will leave further

Now giving some known values for the viscosity of liquids at different temperatures in order to see whether the linear forward velocities of the liquid jets thereof would in practice be such as to give the required increases in the total kinetic energy of the liquid jet flows.Whilst I have not yet been able to acquire a full range of data on the fluorocarhon range of refrigerants, the general data in east includes a range of viscosities for water and carbon

tetrachloride,1the closestvin chemical and physical property nature to the fluorocarbons and from which they are derived. Therefore I intend to give these values following in support of the theory under discussion.

Viscosity in centipoises, - cp.

Fluidity in reciprocal centipoises, Temperature C Water Carbon Tetrachloride Viscosity - Fluiditv Viscosity - Fluidity cp d 0 C 1.787 0.56 1.329 0.75 15 C 1.139 0.88 1.038 0.96 200C 1.002 1.0 0.969 1.03 30 C 0.7975 1.25 0.843 1.19 40 C 0.6529 1.53 0.739 1.35 500C 0.5468 1.83 0.651 1.54 60 C 0.4665 2.14 0.585 1.71 700C 0.4042 2.47 0.524 1.91 800C 0.3547 2.82 0.468 2.14 0 C 0.3147 3.18 0.426 2.35 100 C 0.2818 3.55 0.384 2.6 Extracted from Weast's service to Mankind.

Then additionally for the fluorocarbon refrigerants the following liquid phase viscosity data is generally available at just one temperature quoted to be 250C.

Viscosity (cp) of liquid phase at 250C.

Refrigerant Name Formula Viscosity Fluidity cp d R-ll CCl3F 0.42 2.38 R-12 CCL2F2 0.26 3.85 R-13 CC1F3 0.016 62.5 R-13B1 CBrF3 0.15 6.66 R-14 CF4 0.02 50.0 R-21 GHGl2F 0.34 2.94 R-22 CHC1F2 0.23 4.35 R-23 CHF3 0.016 62.5 R-112 C2C14F3 1.21 0.826 R-113 C2C13F3 0.68 1.47 R-114 C2C12F4 0.38 2.63 R-114B2 C2Br2F4 0.72 1.39 R-115 C2ClF3 0.26 3.85 R-116 C2Fg The viscosity value in poises is defined as the force per unit area in dynes equired to sustain a unit velocity gradient in cms. per sec per cm. normal to the direction of flow when two adjacent planes of a fluid are under a shear force.Thus the higher the above viscosity values then the more force that is required to be applied to shear adjacent molecular planes of the fluid.

And conversely the lower the above viscosity values then the lower the shear force that has to be applied. Thus the lower the viscosity value then the less the applied force that is required to cause the fluid to flow. Or,

conversely and more relevant to the system under discussion, for the same supplied force on a liquid the easier it will flow the lower the viscosity of the liquid.

Thus the foregoing values therefore show that on increasing the temperature of the liquids a very substantial lowering of the liquid viscosity does in fact take place on heating and conversely therefore that the same substantial increase in the flows fluidity will take place, i.e. in the ease with which it will flaw under a given applied pressure on heating. Thus assuming all these relationships are direct for a given set of working conditions, as in preceding discussion, then it could be concluded from the above data that the linear forward velocity of a water flow through the same nozzle CSA at an elevated temperature of 1000C would be 6.34 times the linear velocity of the equivalent water jet at OOC, assuring the same pressure head is becoming applied in both cases.

Whilst for carbon tetrachloride the corresponding factor would be 3.46 times. Which according to the foregoing theorising would be the way in which the heat energy in the respective liquids could add to the normal mgh value and become harnessed in the normal ways of harnessing the energy of a potential head of pressure. Assuming the normal mgh value becomes harnessed at 15 C,tsSthe velcclk Inzeasefactors would be 4 and 27 for water and CC1,

respectively, then giveltheoretical kinetic energy value increases of 16 and 7.3 respectively in accordance with the equation KE = imY2 and the preceding theorising, which could then became reduced to 40: by the Van der Waal contraction effect to 6.4 times and 2 times respectively.For interest sake the normal mgh value of cold water in the system under discussion would be the value of 1OKJ/KG s whilst the amount of heat energy contained in water between 1500

and 100VC is 357KJ/KS, butal6 timesloniy give a value at 16OKJ/KG at kinetic energy,and 6.4 times 64 KJ/KG. Thus it would not seem a very good way of harnessing heat energy if water is the fluid.However, assuming the fluorocarbons exhibit similar factor differences as CC14 then there would seem to be quite good agreement with the estimated values to date, i.e. that the theoretical kinetic energy value would give around the pressure-enthalpy energy in the liquid, ie, the approximate value of 200KJ/KG between cold state A and hot state E on Fig.

2.

To further show the foregoing on Fig.3 I have constructed a graph of the foregoing fluidity values against temperature and extrapulated to

ONE HUNDRED AND EIGHTY OC From which it can readily be ascertained that at 1700C the fluidity of Carbon Tetrachloride liquid would be a value a good 4.5 times that of the cold liquid at 150C, whilst for water the fluidity factor increase would be even higher at over 6 times which will probably arise from the additional loosening of bonding that will occur due to loosening of the extra of hydrogen bonding in the case of water.

Thus, whilst I don't have values for the increase in the fluidity values of the specific refrigerants becoming applied herein, e.g. R-21, under the influence of increasing temperature most liquids are said to behave similarly on heating with respect to effect on their fluidity as in accordance with the generally applicable relationship: Viscosity = Ae BIRT Loge Viscosity = Log A + B RT Where R is the general gas constant and A and B are constants for a specific fluid.

Thus from the latter equation one can envisage a straight line y = mx + c graph applying for any specific liquid where the y axis is the loge of viscosity and temperature is the x axis. Then from this one can envisage how increase in temperature along the x axis will cause

factor changes in viscosity for any liquid plotted on the graph.

Therefore, since most liquids are said to behave similarly on heating with respect to effect on their fluidity property then in the case of R-21 at least, having as it does a chemical constitution quite close to that of carbon tetrachloride and comparatively close in Bpt, its fluidity property should increase by a similar factor on heating as carbon tetrachloride and, therefore, similarly have a fluidity property some 4.5 times higher at 1700C than it's fluidity property at normal ground temperature, i.e. as at Point E on the P-E diagram on Fig.2 compared with the fluidity property at Point A. Which then in turn would give a 4.52 = 20 times increase in the fluid jet kinetic energy of forward motion in accordance with the fluid jet kinetic energy equation KE = 1/2 MV2.

Which in turn would represent around the level of enthalpy energy in the fluid as in the fluid state at Point E and as could become read off the horizontal axis of the P-E diagram in enthalpy energy terms.

Of course, one could use carbon tetrachloride itself as the fluid in the system in place of R-21 which in terms of chemical constitution would be from CHC12F to CH4 but obviously only in combination with a higher temperature heat source suitable for use with the higher temperature boiling point range of Cm14, which has a normal Bpt of 76.50C at lATS. compared with R-21 at 90C. Such a heat source could be as providable when in combination with the ARC process for the provision of heat to the pro

cess sincelat fairly moderate air pressures of the order of 25ATS. in the ARC cycle heat of compression temperatures of the order of 500 C should become yielded, although in the absence of full data.

Now reiterating the above in the context of the basic fluidity equation: 8V1 Fluidity = (pal - P2)r4t If all the physical parameters that appear in the equation are the same for the hot fluid system as for the cold fluid system, i.e. the nozzle of the system and its CSA and also the pressure head, an d if the fludity value on the LHS of the equation is 4.5 times higher for the hot fluid than for the cold fluid then the volume of fluid through the same nozzle outlet must be 4.5 times higher. Now since the nozzle outlet will be the same CSA dimension in both cases the forward velocity of the hot fluid must also be 4.5 times faster in this being given simply by fluid volume flow in unit time divided by CSA, by definition, and if the fluid jet flow is 4.5 times faster then it must at this pre-impact stage possess a kinetic energy of impact of 4.52 = 20 times that of the cold fluid jet.That is, if we are talking about the flow of a

mass in anit time in both cases, which we are not but please bear with me and all will be revealed and become clear in due course in this evolving discussion, and at this stage simply consider that even though the mass flow rate would increase for the hot fluid under the foregoing conditions, a

proportion of the flowing hot fluid would be 1 unit of mass in the comparison with the cold fluid system

would be travelling at the 4.5 times faster velocity as part and parcel of the whole mass flow.

Thus assuming the pre-impact kinetic energy value of the hot fluid jet is 20 times the cold fluid jet value of 1OKJ/KG, i.e. 200KJ/KG, and that the transferred energy will become reduced to 40% in practice due to the fluid contraction effect on impact then for the example system herein based on R-21 and quantified on Fig.2 one would obtain around 40% of this maximum value in practice because of the VdW contraction effect. Which in the examrle herein based.on R-21 would zive n an amount of energy that would just fall short of

n ,ed cryzreg,n ener9Lv ct thel140KJ/KG, i.e. around 1OOKJ/KG. With the remainder then possible to be made up from that being produced in the turbogenerating part of the process. Which however is itself 40% of 140KJ/KG, i.e. 56KJ/KG.And therefore based on these figures there would onlv be 16KJ/KG of Dower left for external suDDlv. Therefore in Dractice

in order to maximise upon the energy output one mayl suh-cool to a maximiseb temperature, say all the way down to 100 C, which would be possible via heat exchange unit 7 on Fig 1 and then similarly it would be possible to convert the removed heat energy with at least a 40as times an 807. heat transference efficiency, and if heat exchanging directly into the turbogenerating fluid as

alternative method of operation then probably one could sub-cool to an even lower temperature with an improved heat transference efficiency.However, the turbogenerating fluid

have to be one of the low Bpt type for maximised transference of heat down to as low a temperature as possible and not a water based system, but then there may not be much gain if any. For example if R11 was the turbogenerating fluid of normal Bpt. 240C and as applied under PA 8728601, then heat transference all the way down to 10000 would be possible to achieve, i.e. sub cooling all the way down to state I on the P-E diagram on Fig 2, which could then become converted with an efficiency of at least 40%.

However, the quantity of heat energy from state E to State I is 240KJ/KG and 40% conversion would only yield lOOKJ/KG. Whilst the remaining residual energy would then be equivalent to only 140KJ/KG which if it too became converted at a level of 40% then only 56KJ/KG of energy would be actually acquired, to give a total of 156KJ/KG with at least 140KJ/KG of energy being required to be recycled each cycle. Thus operating the process this way round may not yield any advantage.

Therefore, as the process under PA 8728601, it is beginning to seem that the process under discussion may require even more fine optimising of all the parameters with all the various sub-processes having to become/having to have become developed to their highest efficiency levels than the process under the above patent in order for the process to yield a reasonable quantity of surplus energy for external supply. Moreover, it is beginning to seem even more so now that the addition of BGS Energy to the liquid turbine system may be required and therefore that the earlier work may be of more practical contributory use than considered at one stage.

However in the overall energy balance of the process it may depend upon which of the two turbines can be made to have the highest efficiency. For example if they both commence 40% the turbogenerating process based on R-ll could perhaps become developed to give an efficiency of say 45% one-pass heat energy conversion, but the liquid turbine system with added BGS energy could be made to have a one-pass efficiency level of say 50% in total with respect to the initial P-E energy. Which however may be an efficiency level only achievable at one sub-cooled commencing temperature, with conversion efficiency falling off on either side.Although it may be an efficiency level that one could better achieve commencing at state E at 17000 with BGS energy addition. On the other hand, if sub-cooling down to state I was carried out to give a commencing temperature of 100 C then BGS energy may be more possible to add to give an effective 50% conversion level for all this energy including the added BGS energy, Which if so could Rive an overall

better energy balance because/turt)ogeneratlng part or tne process couia still be at its maximum efficiency level within the range of heat conversion levels.

Then to add to these considerations would be the best way to minimise optimise the compression energy requirement, whilst maintaining the two energy outputs at their optimum maximum.

Therefore, having consideration to all the various aspects, for the purposes of ensuing theoretical Demonstration Models I will still assume that sub-cooling down to state E is taking place. i.e. to a temDerature of 1700C, but that the

240EJ/RG of energy left remaining

become converted low a level of 50Y,. Which in fact is made more likely by the fact that . its War I have not yet discussed

further aspects of the process

couldboost tne energy yield tram the liquid system in a different way than adding BGS energy.

the

exclusion

the latter but perhaps to improve upon the efficiency by the same amounts

I will briefly make mention of at this stage.

For the benefit of readers referring them to the diagram that I referred to for arriving at following conclusions. This being Fig. 106 on page 147 of the text book 'Concise Physics' by R. B. Morrison. Which perhaps indicates that a liquid just bordering over its liquid line, as could be the case for the system under discussion, e.g. as from state F to stateA on the P-E diagram Fig. 2. undergoes a Dressure boost as the initial stages of vapourisation take

place, which could#and to the energy output more than the removal of

fraction at energy/into the latent heat energy mode would detract.Which again would seem to have equal and opposite similarity to the vapour process where sne may aim for just a fraction of condensation on imparting energy to a turbine.

Or more likely aim to just avoid any condensation since not only would this remove kinetic energy but also there would be a pulling punch of impact effect.

Moreover, if such a pressure boost were obtainable by just bordering over the

F b A on depressurising in the turbine from state F to state A then it would seem to me that it would be more impartable to a turbine at such a stage if it took place inside the inners of a reaction turbine of the type depicted on Fig. 1 as the liquid phase flowed through the turbine. Rather than on impact with impellors of a turbine of the Pelton Wheel type when the boost pressure released at such a stage would probably not become imparted to the impellers but be lost to the surrounding atmosphere.

if it took place whilst the fluid was still entrapped inside a reaction turbine then it should be a

pressure boost tnat would all become imparted to tne turbine. In which case then

the earlier writing may be more useful from this point of view1 because in a further large part of thatwork I concentrate on exartltning in theory and in

the inner workings of this type of turbine.Moreover, at the least in such a turbine since the fluid is totally entrapped within the turbine until it exits from the nozzles thereof having imparted all its energy before doing so, then the volume reduction which I am theorising could result in an energy yield reduction to 40% could become maintained more so in order that the energy conversion level remains higher at say 50%. Remember, all the energy would be obtainable if the fluid did not contract on imparting energy and cooling and the of the fluid jet then and thereby becoming reduced by a pulling of the punch effect.Therefore, if inside the reaction turbine bordering over the liquid line has the effect of maintaining fluid volume with just the same pressure being maintained then the graph of the energy impartation would not tail off as much with cooling and the overall energy conversion level could become 50% rather than 40%.

Thus a further built in aspect would seem to be that whilst one could not apply normal harnessing methods based upon fluid expansion it would seem that some very fine optimisation and tuning where the liquid system could just border into the fractional vapourisation regions could yield some rewards for one's endeavours, not in expanding but rather in reducing the amount of contraction that takes place and would otherwise reduce the energy yield, via means of causing a little of the kinetic energy to enter the vapour phase of the fluid and in so doing causing a boost in outwardly forcing Van der Waal energy to counteract some of the Van der Waal contraction taking place in the liquid phase, and compensatinR by an amount well in excess of the small amount of kinetic

energy tnat one nas to consume in achieving tunis. -inererore lttcoula probably be more regar

a volume boost rather than a pressure boosts to volume that would otherwise be reducing at a faster rate under Van der Waal contraction that would otherwise be taking place to a larger extent.

Or evenaisa volume maintenance effect. Which would be more in keeping with laws of conservation of energy hut could make all the difference and becomes explained by Van der Waal's equation relating pressure and volume extending on the normal simplified equation, i.e.:- PV = RT, to take the actual volume of the molecules into account via the equation:

Which would become more applicable the closer to the liquid phase -the system ar,cI as small fractions/bubbles of vapour

just barely vapourising from the liquid phase in the way that one can see them form clinging to the sides when boiling water in a glass beaker at an early stage somewhat prior to actual boiling.

Thus a further aspect of the system that could require some very fine optimisation between several internal fluid parameters, but at just the optimum point could potentially make the difference between say 40% and 50% energy conversion efficiency and probably very realistically.

more equal and opposite similarities with vapour turbine systems are now unfolding. For example liquid contraction being equal and opposite to vapour expansion on passage to the other end of an expansion turbine, when the energy becoming transferred also tails off. Thus the reaction turbine of Fig. 1 could be termed a liquid contraction turbine, etc.

Thus all I can do at this pre-practical Applied Theory stage with a process that may yield far higher efficiency levels than being theorised or may just be bordering on those required is to conclude efficiency levels that would make the process worthwhile in practice whilst trying to remain within probable limits

Ihus for this I would like to use an optimistic efficency level of 45% for 140 KJ/KG of the heat energy becoming converted by a turbogenerating process based upon R-ll as theorised possible under the aforementioned patent, and a 50%

level of conversion

the remaining 240KJ/KG of heat energy via the liquid turbine, with 140KJ/KG of energy being required for the compressor input at a 90% level of efficiency. Which would then give an energy balance as follows:1 140 x 45 = 63KJ/KG 100 2 240 x 50 = 120KJ/KG 100 Thus the sum of the two turbine energy yields being: ONE HUNDRED AND EIGHT, KJ/KG Actually for use.

The compressor then requiring:155 KJ/KG To leave remaining: 25KJ/KG Which, if I say: 24 EJ/KG would then represent 10% of the original intake of 240KJ/KG each cycle.

Therefore I intend to base theoretical Demonstration Models on this amount of energy at this stage. Which is somewhat disappointing but perhaps in the fullness of time the compressor input level could be optimum minimised to increase upon this output level. Moreover, perhaps the hot liquid flow would not pull its punch in the way being discussed. Or at least to the pessimistic extent being estimated at this stage.

But then again perhaps one could never do better than 40e' heat conversion efficiency levels throughout on average. When the process would then just break even with 152 KJ/KG of turbine energy becoming yielded for use and 155 KJ/KG being required by the compressor. However, I will assume that ingenious people will be able to develop the process to the utmost of perfection and similarly optimise all the parameters thereof to the utmost of perfection, basing on fluids for the heat absorbing/vapour phase compression part and for the turbogenerating part that interact in such a way as to give the highest overall energy balance on perfecting the process and fine tuning their parameters.And then that the process could potentially kick-off at a 10% level of energy for output supply when compared with the energy being absorbed each cycle, which remember will include recycled heat each cycle from the turbogenerating process to reduce the capacity of natural heat absorption required each cycle.

Then again the addition of BGS energy to the liquid turbine could make all the difference. Remember one only has to render the vapour compression and the liquid turbine system just self-sustaining to leave remaining for output supply all the energy being produced by the turbogenerating part for output supply.

And the process only just falls short of achieving this on fairly pessimistic estimations based only on Applied Theory. With no practical experimentation having yet been carried out. For example 40% of 240KJ/KG for the liquid turbine would yield a realistic 1OOKJ/KG of turbine energy for actual use and that required for the compressor could be closer to 130KJ/KG than 150KJ/KG. Whilst 40% of 140KJ/KG for the turbogenerating process. as obtainable via steam is 55KJ/KG.

30KJ/KG of which would have to go to the compressor. To leave 25KJ/KG of output supply. Or 10% of the heat absorbed each cycle. Thus I think such a level should be obtainable at the kick-off.

The fact is the values I am basing this work on at this more general and empirical phase of the work are not based on very detailed data, albeit should be ideally, and the value of 140KJ/KG that I have used for the compression part of the cycle is probablyare uppec vafice, with the actual accurate value probably being closer to 120KJ/KG for vapour becoming compressed from state C and could possibly be closer to llOKJ/KG if becoming compressed from state B, i.e. from 1 ATS. at 90C. Which if so would then give a 10% surplus of energy for the 40% levels of energy conversion in each system, i.e. 40% of (230 + 140) = 148KJ/KG with say 125KJ/RG actually having to be placed into the compressor.To leave remaining 23KJ/KG for output supply, i.e. just short of 10% of 240KJ/KG initially abosrbed heat.

Thus, as a general rule of thumb for this process one would prdbably compress as close to the saturated vapour line as possible to follow a line of maximum

uprightness or sheerness which one could abbreviate to LOMUlto place in the vernacular of the work under PA 8728601, whilst for the liquid phase side of

the cycle then one would wish to try to maximise on the slope1 at this leg at the cycle. However, generally and similarly one would aim to follow the saturated liquid line, which in fact is probably the curve one would achieve in practice since in the early stages of harnessing the energy of a fluid jet then one would expect to impart energy at a faster rate, which then fell off with decreasing pressure.In contrast to the adiabatic compression of a vapour which would follow its constant entropy line, although the liquid stage would be similarly adiabatic in this process in the sense that no other heat energy would be being placed in during harnessing and no heat energy would be becoming removed in any other way than via transference to the turbine. Thus under such conditions then the depressurisation of the liquid could well closely follow the curve of the saturated liquid line. Which if so would then represent a line of appreciably more gradient than the compression line at maximised uprightness.

And perhaps the Critical Point marks the spot on a P-E diagram from where one should ideally commence the liquid stage of the cycle for an ideal amount of gassing for volume maintenance on the way down. I do not know at this prepractical stage, my aim being to try to get as close possible via a process of talking around all the various factors involved. And in so doing convey my line of thinking on the various facets of the process to others. However I take this opportunity to apologies for not yet basing this work on exact data at times.

Before briefly discussing the technique by which one could perhaps add BGS energy to the liquid turbine yield, discussing further aspects related to viscosity, albeit this

not being my field but which I think would be a very important aspect of the process to get just right, with the performance of the process probably declining rapidly on either side of the optimum peak. Not only from the point of view of achievingoptimum fluidity conditions but also then getting the internals of a reaction turbine at just the right design to allow for the gradual contraction of the fluid therein on cooling to be just right without loss of fluid pressure for the optimum fluidity level. Then to combine with this either the optimum pressure boost effect or the optimum BGS energy addition. . One recalls the

long endeavours that Parsons had to carry out to get thetdesign just right in

vapour expansion turbines, but then of course with great reward resulting from his endeavours both in the field of turbogenerating and also aeroengines, and probably the same will be the case for the liquid turbine system under discussion.

Thus , I conclude that

the work under the aforementioned patent

off some old technology, the possible new technology under discussion/will indeed probably be a new beginning in a new field of technology, albeit having many facets closely related to present day systems and processes. However, with further regard to fluidity.

So far I have not mentioned the effect that high pressures will have on the factor relationships between the viscosity/fluidity values. Under the McGraw- Hill encyclopedia it doth state with respect to this aspect that very high hydrostatic pressures generally increase the viscosity of liquids, sometimes quite markedly. Adding to this that perhaps the increase is more marked the higher the temperature for a given very high hydrostatic pressure, which would seem probable.Therefore in the factor comparisons that I have made it would seem probable that the effect of very high hydrostatic pressures would be to increase the higher temperature viscosities more so than the lower temperature ones to increase upon the factor relationship if anything, which I then apply to Rive the factor increase in kinetic energy for the liquid at higher temperature

compared with

ground temperature# which I taKe to be the normal mgn value that one could calculate for the system, to recap.Information also states that viscosity reduces fairly linearly with increasing temperature in accordance with the relationship log## viscosity being inversely proportioned to liquid temperature,

the rate of change of viscositv/fluiditv does in fact increase with increasing temperature and extra

palatian rives a value of,5.0far carbon tetrachlaride at l7OUC. Since the

value is 1.U at ZUV(: then the factor increase in fluidity isl5.U times, which is just over the factor increase value which gives the desired increase in kinetic energy when placed in the equation KE = 1/2 MV2.Thus, whilst the values for water do not correlate with the amount of heat energy present, those for carbon tetrachloride do. Which

arise from the fact that such liquids have very much more flowability and streamlining properties arising from the fact that they are free from strong hydrogen bonding unlike water. Thus the individual molecules of such liquids will be far freer to flow and give kinetic energy of forward flow equivalent to the random kinetic energy of the heat energy present.Whilst in

Which would not matter when one is bent on just obtaining the mgh value of the water mass, but only when one wishes to add to this the random kinetic energy of heat energy contained in the liquid,

which of course is Çhat/gives rise to the temperature in the first place and simply requiring of all lining up in the forward vector in order to be able to fully harness.

It follows that there could indeed be advantage in maximising upon the initial temperature since the random kinetic energy present would then be more stream

linable all into the forward vector and the/energy harnessing efficiency is therefore likely to be higher for a higher working temperature of temperature change. Thus the working temperature of 1700C becomes supported, which

to push to one hundred and eighty to maximise upon the volume boost and BGS energy addition - notwithstanding some earlier discssion in which I considered that maximising on the pre sub-cooling could be the way to maximise on BGS energy addition.

Of course, the viscosity and fluidity of liquids is already a very large field of science, and scientific and technological development into the process under discussion would obviously mushroom further growth and interest in this field.

But here being more the effect of heat addition rather than the effect of

suDstance anaitiory, ana tne Kinetic energy parameter being tnat wnlcn is or interest rather than just viscosity and fluidity.

Fortunately the viscosity and fluidity values quoted are obtained using a constant head pressure via an externally applied pressure

are corrected for change in the mgh value of the total pressure as the liquid flows out of a tube. Ref 'Viscosity and its Measurement' by A. Dinsdale and F. Moore, pages 1 to 25 and of particular interest being the Bury method of correction for changing potential head on page 20 thereof.

since the system under discussion is solely concerned with a continuous constant applied pressure head then normally quoted viscosity values will directly apply and the preceding treatment of the system based on such values will be in order. However, there art some methods which just base on the value obtained from a gradually disappearing column of liquid between two marks, which give values termed the kinematic viscosity, and which has to become multiplied by the liquid density to give actual viscosity. Now in the system under discussion one could pehaps regard the slowing down of the liquid flow due to contraction, (i.e. not just simply due to

for a constant pressure head system to in fact be the equivalent of loss of fluidity due to loss of potential head in a changing head method.The two then counteracting and the initial viscosity value being that which applies throughout the whole process. However, this would not be correct because change in density as the liquid cools down would be changing the kinematic viscosity value by a pro-rata amount and therefore the preceding theorising will still be in order. Which so far boils down to the conclusion that the initial energy level ever wi 11 not become harnessed bv the

system but become reduced

decrease in liquid volume, which nnay accurately quantify the pulling punch power of Van der Waal's internal forces of self-restraint on the negative side of the energy balance of the system.

Simply thinking of this in terms of ratio of change of surface area of pressure exertion in all directions should verify this in one's mind's eye, e.g. basing on the image of a cube or sphere where surface area is directly related to r and change in surface area to r3 - r3 One can envisage that the pressure power of the pressure head becomes transferred into the liquid as in hydraulic fluid, with then each cube or sphere exerting pressure energy to the turbine in all three dimensional planes of the x, y, and z axis

envisionable inside the interior of a reaction turbine of the type depicted on Fig. 1. Then that the pressure power transferred will be directly proportional to the full cubic surface area for any cube or sphere travelling through in unit time at any stage. Thus if the cube or sphere also shrinks as well as losing kinetic energy of forward motion then the linear forward velocity will also lower by a corresponding amount in unit time of passage of a given mass of fluid, to add to the change that loss of forward kinetic energy is making to the linear forward velocity. Which is probably the better way of looking at this aspect in practice. However it will still become quantified by an amou t

change in volume at the liquid, since contraction will t)e raKing place in all three dimensions of the liquid not just in the forward direction but also in the width and depth of the liquid flow by equal amounts.To cause the reduction in flow velocity due to this effect to reduce by an amount the volume of the liquid reduces during the time that it is flowing and imparting its kinetic energy, whereupon the liquid will cool and also contract. Which would not take place to a significant noticeable level when harnessing the normal mgh value of water at normal temperatures during imparting the kinetic energy of its flow to a turbine. In other words therefore,in the system under discussion a proportion of the kinetic energy of the liquid flow will become lost but not to the turbine, rather due to contraction of the fluid on imparting its energy and thereby cooling, all the stages of which it must go through when transferring the energy down to ground state.Therefore during such a process the contraction effect subtracting from kinetic energy of forward jet flow would in turn subtract from the energy becoming imparted to the impellors of the turbine. However, I do not wish to sound

certain about this aspect before any practical experimentation to confirm the theorising. Having said that the theory seems to become confirmed by a consideration of the practically determined fluidity values quoted for carbon tetrachloride as follows. If one extrapolates those values to 1700C and then take the mean value from 200C to 1700C then a value of 2.8 is obtained, which I am theorising should be the value one should probably base upon when using fluidity measurement to quantify the effect that heat addition will make on the normal mgh energy value of cold fluid, rather than simply the initial fluidity value.But I could be wrong. However, on a straightforward impulse fluid jet view where the jet is first formed based on fluid of the initial fluidity, then on impact with the impellers of a turbine one can envisage that the contraction effect on energy imparted would manifest itself as a pulling of the punch of impact effect, as indeed is found in practice in the use of vapour turbines when some condensation to a smaller fluid volume for a given mass of the fluid takes place.

Thus if one bases on the mean fluidity value then a kinetic energy value of just 1/2m2.82 = 7.84 times is obtained which would give a value of 78.4 KJ/KG and not the 20 times the normal level of 10 KJ/KG as would be given by basing on the initial fluidity value.

around 40% of the initial level of energy. Which

is present in the fluid at the start but as in a vapour system probably not all harnessable, which in such a system is due to a proportion of the energy transferring into the latent heat energy mode, whilst in the system under discussion in equal and opposite contrast being due to contraction of the fluid under internal Van der Waal forces re-exerting themselves and in effect getting back hold of or re-restraining progressively increasing amounts of the kinetic energy during impartation of the energy to the impellors of a turbine, in comparison to the amount the Van der Waal forces can hold onto and restrain at higher levels of heat content in the fluid.However, probably the higher the initial temperature and pressure then the more will be the energy proportion that will become imparted on the upper part of the fluidity curve, but bearing in mind that fluidity falls off more rapidly on the upper half of the curve.

However the point being that the upper half possesses more fluidity property in the first place when compared to the lower half against the proportions of temperature differences, i.e. kinetic energy differences involved between the upper and lower halves.

Thus again there are many similarities with a vapour system.

The volume contraction view is perhaps a better view when considering what is happening inside certain parts of a reaction turbine of the type depicted on Fig. 1, although effect on linear velocity will be equally as applicable.

Further of my thinking at this stage then includes the possibility of reducing the rate of decrease in fluidity by the addition of substances to the basic fluid in the closed-cycle circuit of the process, perhaps by creating a molecular surface effect to gain some advantages from perhaps being able to thereby create some thixotropic or non-Newtonian flow behaviour, which of course would not add to the kinetic energy but perhaps make it easier to streamline all into one direction and/or maintain fluidity longer on cooling under a given applied pressure.

With further regard to the density parameter, the viscosity values quoted for elevated temperatures will in any case of course relate to fluid that has the lower density at elevated temperature and therefore will directly relate anyway.

Thus, in this part of the discussion of the proces I have essentially taken a straightforward practical view, as I see this to be and then tried to give some insights into some of the surrounding theory involved, again as I see this to be. With a view to determining how in practice would be the better way to set about obtaining the energy and then how to maximise upon the energy, which it now seems may be particularly important to achieve in this process otherwise it may fall just short. In relation to this aspect one recalls that early attempts to harness steam power only achieved 1% efficiency with respect to the heat absorbed, as in Stephenson's Rocket, but with perseverance and further development reached the levels of 405 which we are able to enjoy today and only at such high levels could we viably be obtaining our power today by such a means.Thus the process under discussion could be in a similar category, although in being abe to see the future from off the shoulders of those that went before since the days of Stephenson then probably initial development would be more successful and similar progress be at a more accelerated rate in unit time.

Thus, I have first considered the sub-system asla normal liquid pressure head and then considered the effect of temperature on such a system, when it becomes revealed that the fluidity of the liquid would increase by such an amount that the total energy that would be obtained would in fact be that which corresponds with the total

contained in the hot liquid under an applied pressure. And in the example herein be some 20 times the energy yield at 1700C than the normal level of mgh energy one could expect to obtain from the system at normal temperatures, requiring the liquid jet to increase in forward linear velocity/fluidity by only 4.5 times, i.e. well within practical envisionability.

Then combining with this view the thinking that if the kinetic heat energy becomes transferred to the turbine then it cannot, nor could, any longer have to be transferred into the latent heat energy mode to remove and therefore one would also gain the advantage that the fluid would finish fully in the liquid phase ready for a further cycle of the process. But then dampening faith in the process a little by introducing the volume contraction effect and its probable effect of probably reducing the energy yield by a pro-rata amount. However, I hope there will be sufficient faith and belief left remining, and to hopefully give a boost in this direction following I briefly discuss the potentially possible technique for adding BGS energy

which I deal with in more depth in my earlier writing 'Throttle Energy Conversion'.

BGS ENERGY ADDITION: Referred to in the above writing as: Kinetic Energy Advantage or KEA: In the first place when trying to make this system work I was working with refrigerant cycles close to those of present day refrigerant refrigeration cycles involving the initial compression to a lower pressure than the critical pressure

for the fluid which, on removal of the heat of compression) well in the liquid phase to the left of the liquid line and

diagram somewhat below the critical pressure and temperature for the fluid.

Thus at the sub-system stage commencing well in the liquid phase but still

as a hot liquid fairly close ta,ar1 on the liquid line. Which in the first place it was considered would be the conditions of the sub-system operation for the Advanced Brierly Process and probably some of the other potentially possible processes that could apply the sub-system to then be able to work successfully. Whilst under such conditions one would probably obtain the same energy proportion it would probably fall shorter of that required to sustain the compressor than as under the conditions of the main example process under discussion herein in which it would be possible to have working conditions well above the critical pressure and temperature of the fluid.Which in fact

Cou 1J be possible working conditions for the other processes just for the sub-system part of the processes. However, in the beginning I was working in a lower range and on trying to think of ways to increase upon the energy yield one of the techniques I came up with was a technique for adding partial vacuum energy to the energy yield, which in practice would be below ground state energy addition to the system to give some kinetic energy gain.

The principle of the concept is in fact very simple but in the first place is best explained in relation to a reaction turbine of the type depicted on Fig.

1, which in fact may be the only type of turbine to which one could successfully apply the technique, with this being the reason I concentrated on the application of such a turbine in the first place. However, lateron in ensuing discussion my views change on this aspect more towards the use of a method based upon an impulse fluid jet turbine, ie, as on Fig. 1D.

Thus the concept is one of first housing the turbine in a fully enclosed chamber and such that its only outlet is that at the base beneath a deep layer of liquid fluid down which the liquid flows to the next stage at the rate that it is exitingfrom the nozzles of the turbine, as depicted on Fig. 1. Then via

externally applied suction evacuata the chamber to create a vacuum or partial vacuum inside. Which would then be vacuum energy that became added to the fluid passing through the turbine and from the liquid imparted to the turbine.

The way it would do this would be to draw the fluid to longer fluid than if normal IATS pressure was the external pressure, and such that the side pressure of the fluid flawing through the turbine was not normal IATS, as would be the case for IATS normal pressure being the external pressure, but the pressure of the externally applied vacuum. With the forward dynamic pressure of the fluid flow then increasing by a corresponding amount as in accordance with Bernoulli's equation, which Would then be the kinetic energy level that becomes imparted to the turbine. Requiring of an even smaller nozzle GSA for an even faster

velocity, which in a reaction turbine in fact stands still with the turbine being caused to travel faster in the opposite direction.Thus

and thereby the power at the vacuum1 become transferred to the reaction turbine, adding to the level of power that one would obtain down to just normal IATS.

pressure. In the earlier writing I derive that the normal level of streamlining that one can achive under IATS. external pressure is about 5/6th of the way from the fully random state to the fully streamlined state, with 1/6th of the way to go to become fully streamlined. At which stage the side pressure of the fluid would be zero by definition of pressure and a fully streamlined flow, when in fact no molecules would be travelling in any vectors other than straight forward

molecular bombardment for any pressure creation to either side of the straight forward vector.

that kinetic energy which is normally still left exerting to the sides under IATS. external pressure becomes added to that exerting in the straight forward vector to add to the forward dynamic pressure, i.e. the pressure energy that then becomes imparted to the turbine.I also derive that the final 1/6th of streamlining into the fuly straightforward vector will in fact increase the relative flow velocity by a factor of 1.73 to increase the power of the fluid relative flow by 73%. Thus a full vacuum in the chamber could add this amount of energy, equivalent to the power of itself, to the energy yield. But in so doing the liquid fluid will then exit from the nozzles in a very much colder state when the kinetic energy thereof left remaining re-randomises because up to a maximum of 73% more of the kinetic energy in the fluid will become added to the normal level of forward aligned kinetic energy and become imparted to the turbine than would be the case for liquid exiting under normal IATS. conditions. Now a liquid exiting under normal conditions should do so at 90C for R-21 and be under its own saturated vapour pressure of IATS.But a liquid exiting at a verv much colder temDerature will Droduce

a much lower SVP in the/chamber, i.e. that which thermodynamically corresponds with the very cold temperature. Thus, whilst the initial vacuum would have to become created by an external means it should then be self-sustaining to some level. Which if so would then be additional power which continually became added to the trubine yield in a fully self sustaining manner. Although probably not quite since the pressure inside the chamber would probably gradually creep back up again. However, the amount of energy input required to maintain a steady state partial vacuum each cycle could potentially be very small in comparison to the increased energy output. Very simply the thinking being that if the initial power of the vacuum becomes transferred tQ the liquid and

then tram the liquid to the turbine in the way described thenjliquid must transfer more of its kinetic energy content to the turbine, and if it does then it must exit colder, and if it does then it must have a SVP less than IATS., which

then must helvacuum power that will continue to become added to the energy yield, ad infinitum, in a self-sustaining manner. In the main process under discussion the liquid head for the next

could then be of sufficient height to give IATS. pressure in total acting on the liquid phase in the subsequent submerged heat exchange unit on this side of said unit.

This then the way that it is considered that the equivalent of condensation vacuum power in a normal vapour turbine system could become added to the liquid turbine system, which in perfected practice could possibly increase the nett power output from the liquid turbine by some 50% over that which one would otherwise acquire. Thus on the cycle P-E diagram on Fig. 2 the state of the liquid inside the chamber of the system could be continuously maintained at say state J mainly via the self-sustaining action described, but perhaps partly by some added suction power to remove any increase in vapour content therein each cycle.With the temperahlre of the fluid then raising to 90C as it passes through the submerged heat exchange unit, but the flow of the liquid being such

this temperature cannot conduct back to the liquid in the chamber which would therefore continue to maintain itself at a very cooled temperature, which in turn would continue to maintain the law SVP above the very cold liquid phase inside the chamber, which in turn would be a pressure well below IATS. continually acting on the exit side of the turbine, adding to the turbine yield in a very similar way to that in which condensation vacuum energy becomes added to vapour

turbine power yield

becomes transferred as pre-expansiont, i.e. further vapour expansionin the forward vector resulting from more forward alignment

at molecules in the vapourlbecoming streamlined through the entry nozzles to the - turbine to increase upon the forward linear velocitv of the vapour jet

for a given mass of vapour flow6 An equal and opposite similarity

c( the liquid reaction turbine under discussion will be that the extra 1/6th streamlining of the liquid moleucles due to the vacuum suction on the exit side will in fact take place in the (long) nozzles on the exit side, and force backwards with a corespondingly higher farce. If you consider each molecule and its sphere of energy influence in the streamlined state to be as though a log.With initially many

in all random directions which then become all lined up in series initially to the normal 5/6th level of alignment to give a normal level of energy transference, but then going on to the full alignment level. Then at the full alignment level the linear forward vector total length of the sum of the logs would be longer, with however the same total mass flowing in unit time and therefore for the latter to be the case then the linear forward velocity of the logs must increase, which will then add to the energy yield in exactly the same way as discussed in relation to the effect of increasing fluidity due to heating.

in the use of a reaction turbine whilst the same alignment will take place as the liquid fluid exits from the exit nozzles, it will not be as an impulse system with the nozzle stationary and the liquid fluid jet issuing forth at an even faster velocity, but rather the effect will be to push the turbine arm further backwards in unit time, whilst the liquid itself should have zero velocity with respect to the surrounds, albeit exiting from a nozzle which is travelling back in the opposite direction at the same speed the liquid would otherwise be travelling at if the nozzle was held fixed. To become manifest as a rotation speed in the case df a reaction turbine,

whilstin / a jet engine then a Jet Plane becomes

propelled in the opposite direction leaving the vapour trail standing in midair.However, in the system under discussion whilst the liquid flow will similarly be left standing in the chamber after exit from the nozzles it will fall to the bottom of the chamber under the force of gravity,which of course will still be acting on the liquid in a vacuum environment on Earth.

Furthermore, I am) given to understand that the power of Jet Engines can become increased upon in a similar manner by application of rear wake zone partial vacuum forces created as the Plane travels forward. If so then this would confirm some of the theory for the system under discussion. With a similar means of adding power hoping to be achievable in the air power propulsion system discussed under Patent No. GB 2126 963B. - (Which the more I think about must function as I have theorised.However, pressing on.) Of course, it may be simpler to apply an impulse turbine of a Pelton Wheel type, certainly in theory, but in the use of such a turbine type it may not be possible to transfer the power of the vacuum to the liuid flow if at all, since when the jets are flowing they will be fully connecting nozzle exit to impellors and the vacuum would then only be able to exert on the sides of the liquid, perhaps to pull the molecules into the side vector and further away from forward alignment rather than add to forward alignment. Whereas the opposite will be the case for a reaction turbine type since the vacuum will become exerted

directly onto tne forward alignment vector and as sucn could before ertective than transference of the power thereof all the way through to pre-expansion in a vapour turbine.

Thus again the most essential aspect of the system will be to get the reduction in the GSA of the nozzles just right for the increased elongation of the liquid flow in the forward vector giving rise to a corresponding reduction in the GSA dimension of the flow for the same mass flow rate in unit time, etc., as discussed in relation to fluidity. To reiterate if the liquid flow imparts more kinetic energy from itself to the turbine then it must fall to the bottom of the chamber at a much colder temperature than normal, and therefore must create a SVP pressure inside the chamber much lower than IATS.To thereby maintain the vacuum in the chamber, but perhaps with a little external assistance

Then another subsequent reason for using this type of reaction turbine could be for - more successful application of the liquid volume maintenance technique which conceivably now could be carried out in the same cycle of the process, whilst initially I considered that perhaps one could only acquire one or the other but not both together. Since on the one hand if one goes for volume maintenance then one would probably be left with a small vapour fraction which would destroy the low SVP of cold fluid, and the self-sustaining vacuum power would very rapidly be lost.Then on the other hand, I first thought that for this reason it would probably be better to sub-cool to as far as possible first before trying to go for BGS energy, with the further thinking that if one thereby initially got closer to BGS energy then one should be able to add more. However,

perhaps the higher the initial temperature of the liquid then the better will be the streamlinability of the liquid under the applied

pressure above to the normal 5/6th level, then all the. ay'to tull forward

alignment with the addition of vacuum suction force/ the other end of the

However for BGS energy addition it would be still necessarv to avoid

a vapour fraction exiting from the nozzles of the turbine1 with the liquidphasQ.

However, if one looks at this leg of the cycle as drawn on Fig. then one can see that in passing from E to J the fluid state could pass through some sticky phase where the volume maintenance effect could take place and be beneficial to the amount of transferred energy in these phases and still come out clear fully in the liquid phase by the time it reaches state J. Which really would be better for the view of the system from the standpoint of conservation of energy since if no vapour phase exits then no kinetic energy could have become lost in such a way, but on the way through the system could be in a state of flux backwards and forwards between the liquid and early gassing stages with

final swing being fully into the liquid phase for exit, but with the intermediary stage gassing adding something to the total energy yield.

Probably via simply de-accelerating the rate at which liquid volume contraction would otherwise lower the transferable kinetic energy. To leave the energy present upgraded for longer than it would otherwise stay upgraded as it becomes transferred, etc., and for this using a fraction of the kinetic energy to cause gassing, which however does not beocme lost because on the final swing of the state of flux becomes transferred permanently back into the liquid phase and there able to become harnessed as BGS energy via the application of the

technique.Thus in practice in a reaction turbine with a long nozzle the gassing could just take place part way along the long nozzles

with the tiny gas bubbles created maintaining the liquid volume for a1 time nut which then diappear as they approach the nozzle exit under the changing thermodynamic conditions along the length of the nozzle inside the length of the liquid flow therein.

see through nozzles in combination with stroboscope vision of the rotating turbine would be useful as well as ones in which one could accurately infinitely vary their GSA dimension at any stage along their length.

creation of vapour bubbles would add to the volume of the fluids vr to put it another way, would remove some volume such that the remainder of the liquid phase, whicho,uld be most of the fluid, would be occupying a small space surrounding space than it would otherwise do and therefore in that smaller space would not lose pressure as much due to its own contraction because the fractional gassing within the liquid would be counteracting to some extent or other. The liquid phase would still be contracting to the same extent for the temperature, but the effect of that contraction in creating a pulling of the punch effect would be reduced because the gassing taking place at the same time would maintain the volume of the liquid with respect to the volume space inside the casing of the turbine.Then closer to the exit of the nozzles the gas bubbles would disappear and the liquid would beomce fully aligned as lining up logs to still give the same backward forcing reaction force. Drawing the parallel with a jet engine or rocket propulsion) if one for example looks at Fig. 4.3 on page 131 of 'Mechanics of Flight' by A. C. Kermode then the gassing inside the liquid flow would take place close to the front of the rocket engine and perhaps just on the inside of the front plate. To leave the remainder of the fluid flow mechanics as normal.Which in the case of the reaction turbine would be at the

but

could take place in the leg before the liquid goes round the corner

witn tne same erect1 wnicn alternatively could be viewed as pushing the liquid along quicker than it would otherwise be travelling by means of filling some space up that the liquid cannot then occupy and would instead become pushed forward at a faster rate. Then when the flow goes around the final bend into the final leg of the turbine it could function as normal with the bubbles disappearing. But in entering the final leg at a faster rate then this would add to the

speed of the flow at exit form the nozzles of the turbine providing the GSA dimensions where reduced in accordance with the disappearance of the bubbles.

Thus,

both volume maintenance and BGS energy could be achieved simultaneously and the fact that to 'achieve the latter would require the avoidance of a vapour fraction creation which in turn would limit volume maintenance to that which just avoided permanent consumption of kinetic energy in a latent energy mode would seem to be propbably the optimum conditions anyway for getting the most nett energy advantage from volume maintenance and would be more in accordance with laws of conservation of energy. Then the fact that such optimum conditions would be at a maximised temperature should improve the efficiency of energy transference by virtue of fluidity not becoming lost as quickly in the first half of energy transference when most of the AGS energy, i.e. Above Ground Energy,

become transferred.Then the higher temeprature would improve upon the overall alignability of the liquid flow for the addition of BGS Energy in the manner described. Thus perhaps it would be better to

both simultaneously because the optimum conditions for both could occur at the same time as the optimum conditions for optimum gassing. Having said that one could take the gassing even further to the destruction of the BGS Energy system but which may be more beneficial even though some energy would then become permanently removed into a latent heat energy mode. Personally therefore at this stage I think taking to QO for both simultaneouslv in the same Drocess could nive the highest energy yield.Which

fir5ny is1 likely to be around 40% of the initiallv contained

energy for the normal system in accordance with reduction in volume6 which could then be improvable up to say 50%, on application of the techniques for improving upon the energy yield, or in the case of volume maintenance reduce the loss in energy due to liquid contraction. In fact the addition of BGS Energy could also be viewed in such a light, although it would be necessary to achieve the full forward alignment of the molecules of the liquid flow via application of the vacuum power in order for the liquid to exit super cool and thereby maintain the low SVP inside the chamber.Obviously, it follows from the earlier estimations that an increase of 50% energy yield from the sub system would be better to be the final achievable level of improvement for the process to eventually turn out to be very successful and worthwhile in a range of envisonable appliations and processes. Some of which I discuss in a following section, One could push the initial starting temperature up for the subsystem to say

result in a permanent vapour fraction without it then being possible to add BGS energy and with the removal of some energy that may otherwise be harnessable. Thus in initial experiments it would probably be better to sub-cool to around 1500C and see if BGS energy can be added. Then push the initial temperature up in stages to find the position for oDtimum overall enerv vield.Obviouslv under conditions of harnessing

the energy thelline would not pass vertically back down to ground state with the creation of a very large vapour fraction as in existing cycles in which a throttle device is used to deliberately transfer the energy into the latent heat energy mode in order to effect its removal. It is easier to consider this aspect in terms of an impulse turbine system. In such a system the initial fluid jet will be created from the fluid in state E and it is only after the fluid jet strikes the impellors of the turbine that it will begin to transfer energy, and in striking tke impellors of the turbine it must impart its forward aligned kinetic energy to the impellors, which then could not, nor would be required to, transfer into the latent heat energy mode in order to effect its removal.Thus the fluid will lose kinetic energy of forward motion by transference to the turbine and the line from state E to ground state must slopeto the left by an amount such that the quantity of transferred energy corresponds with the enthalpy energy equivalen amount on the horizontal axis, for an adiabatic system. Otherwise the energy balance of the system would not add up properly.

However, perhaps some vapour fraction would be produced as the hot liquid jet travels from the jet nozzle to the impellers, which however could be a very short distance partially or fully enclosed, but could be a further reason for using a reaction turbine because the equivalent stage would be fully inside the turbines (long) nozzles and the fluid would exit already in its cold state by thz time it exits when it re-randomises. Therefore there could be no tendency for the fluid to vapourise at the equivalent stage because it would not be being subjected to the external pressure and temperature of the surrounding atmosphere. However, the use of an impulse jet system may be considered to be more suitable for initial trials of the system since they are more commonly in use. If so then the Pelton Wheel type impellors would probably have to be re-designed to allow for the slowing down of the fluid jet at a different rate than normal cOldvater for which current designs apply. Thus perhaps from the outset it would be better to base the system on reaction turbines which in contrast in the beginning may only require the GSA of their nozzle exits pre-setting at the correct dimensions for the system. Moreover, the exercise on probable energy yields seems to indicate that one would probably have to try to add to the energy yield in some way from the outset, which may only be achievable by the use of reaction turbines in the ways discussed.To recap 40% conversion of the initial energy level of 240 KJ/KG at state E

9Igonly 96 KJ/KG, which may be the maximum level of conversion one could achive via an impulse turbine even when one has spent a lot of time designing the impellors of the turbine for the system, but such a level would really fall too short of that required for the compressor leaving very little of the energy from the other turbine for output supply.Whilst with the use of a reaction turbine then it should be possible to apply both the volume maintenance technique and BGS energy addition simultaneously to give higher levels of effective conversion, e.g. 50% of 240 KJ/KG is 120 KJ/KG and the system would then almost be capable of self-sustaining itself, whilst at 60% effective conversion then the yield would be 144 KJ/KG and very probably the system could then fully sustain itself to leave all the energy of the other turbine for output supply. Which would be the goal, not only to make the main process under discussion more viable, but also for use of the sub-system in other potentially possible processes.Therefore, from the outset it

be better to start development based on a reaction turbine of the type depicted on Fig. 1, since one could then realistically hope to eventually achieve levels of conversion which would make the system very viable. However, on the questionof the energy balance these energy values also do not add up on a cursory examination since if thefluid comences off with 240 KJ/KG of enthalpy energy equivalent and only 100-140 KJ/KG becomes imparted to the turbine what has happened to the other 100-140 KJ/KG of energy. Well. it will in fact be the enthalDv energy left

remaining in the liquid From1 to state A as can become read off from the horizontal axis of the P-E diagram. Which however was present in the first place.But we are back at the theory of loss of upgraded energy, which in theory would all be harnessable if all the energy could be harnessed whilst the fluid is at the fully upgraded state for the system, but it will not be able to be as in the equal and opposite case of steam pressure harnessing.

Thus as the fluid transfers energy to the turbine the energy which is left will be at a lower level of upgrading and the energy the fluid then possesses will not be the initial energy less the amount that has been transferred. Therefore to balance the energy balance of the system one way would probably be to quantify the internal energy of restraint that Van der Waal forces are able to re-apply on the external translational kinetic energy of the molecules of the fluid as kinetic energy becomes lost, i.e. on the remaining kinetic energy.

However at this stage I still leave open to question whether or not the initial amount of potentially harnessable energy would in fact in practice reduce to

levels of around 40% on actually trying to harness theenergy due to Van der Waal forces re-restraining the kinetic energy by progressively increasing amounts or, basing on the more practical views, due to fluid volume contraction or due to loss of fluidity on progressive impartation of the kinetic energy to a turbine.

Thus, there are many ways to the view the system, all of which I have not gone into herein but all those that I have would seem to add up quite well.

However, perhaps the question should also be posed,why bother with this process type when thereis that under my PA. No. 8728601. Perhaps the answer being that when the subsystem does eventually become perfected to a selfsustaining level then all the persevering will be achived and when all the persevering is over then the whole new horizons that now become opened up for the future by thy final achieving of the process under the above patent could easily become improved upon and extended upon.Further-more, whilst in following modelling of the process I give some indication of the potential for the system on improving upon those horizons for the further creation of Heaven on this Planet, as in accordance with the Lord's Prayer, who can say what other eventual scope there would be for the system in the future should it prove possible to perfect the subsystem to a self-sustaining level. Perhaps via the means that

e.g. some gassing to give some volume maintenance followed by addition of BGS Energy to the system. When at a 50% conversion level all becomes more possible and worthwhile.

Finally, perhaps I could conclude this part of the discussion by saying that the sub-system process looks hopeful

but not overwhelmingly so although could potentially become an extremely useful addition to the processes and systems of Kingdom Come, A-Z, since in theory it is considered that it could be rendered self-sustaining in practice. And indeed would have to be for much of my further work in Kingdom Come, A-Z, to become a reality in practice.

ALTERNATIVE METHOD OF OPERATION IN A HIGHER PRESSURE RANGE Referring to the list of fluidity values for the range of refrigerants, I could perhaps be forgiven for not yet having addressed the question of what difference will be made by basing on a refrigerant with a very high fluidity from the outset, e.g. as for COIF2 or CF4 or CHEFS, if indeed the temperature range of such refrigerants would allow their use in the system under discussion. Whilst it could possibly be apt to say God only knows I will have a go at removing this veil at this stage and of course it is a prime example of a veil still remaining and there may be others, but who can say at this stage what removal of this veil and possibly others still remaining may reveal.May I also say with the more obvious alternative pun not being intended, but in the sense obviously intended then I think it is a good metaphoric view of the process involved in evolving a new system, which in the beginning is usually somewhat obscure in one's mind and only very simply generally conceived but then gradually becomes clearer and more possible as one uncovers it's veils of obscurity. Eventually to reach a stage at which it becomes feasible enough to be able to convey to others, when the clear picture is usually very simple again but in a very different and possible way as distinct from still being regarded as impossible.However, in trying to take a system from the impossible stage to the possible stage

the minds of others can involve many terrible trials and tribulations for the person trying to achieve such work on this planet, and in my case at least can be regarded as trying to achieve the Will of God on the planet and as according to the Lord's Prayer, against the Will of some others bent on different pursuits.

However, progressing on.

Of course the very low temperature range of these refrigerants gives a clue since such fluids would in fact be a gas at normal ground level temperature and pressure, and already contain considerable quantities of their ground level enthalpy heat energy in the higher energy modes of the liquid. Since the fluidity values are quoted as being at 250C I will assume that those with Bpt.

lower than 250C and Would be gas at 250C apply to tests carried out at least at the pressure they would have to be under to remain liquid at 250C. But for uniformity of comparison then they must all have been carried out under the same pressure, or at least all corrected to the same pressure. Of course, if not then simply being carried out under different pressures could give rise to

differences. However I will assume that the values all related to the same pressure and for the purposes of this discussion one which is at a sufficient level to render them all in the liquid phase at 250C basing on the probable fact that for a given pressure then the fluidity values will relate regardless of the pressure.Under such conditions, therefore, the state of some fluids under the given pressure and temperature of just 250C would be very close to the Critical Point for the fluid whilst others would be well in their liquid phase and much lower down their particular P-E diagram. Yet others would be well in the liquid phase but still close to their Critical Pressure. The three refrigerants with the very high fluidity values being in the former category.This view of the state of the different liquid refrigerants under the same pressure at 25"C, therefore, explains the large difference in the fluidity properties of the various liquids, and in fact to a large extent confirms the preceding theorising related to a consideration of just one fluid in various states on its own particular P-E diagram since the three liquids with high fluidity values will in effect by in a state which corresponds with the state of R-21 at an elevated state on this refrigerant's P-E diagram, whilst at 25"C under the given pressure then R-21 will be much further to the left in the liquid phase but still close to its Critical Pressure and in effect as though having become sub-cooled at the given pressure.Elucidating further, at the given pressure of the fluidity tests at 250C for the purposes of the more general discussion one could consider that the refrigerants all possessed the same amount of pressure-enthalpy energy, although this will depend upon their comparative heat capacities for the pressure and temperature whichjhowever;, are all fairly close for the whole range of refrigerants.Thus asuming that they all possess the same quantity of P-E energy then they would all be in the same position on a P-E diagram relative to the pressure and enthalpy Co- ordinates, but their actual state diagrams will all be in different positions relative to the co-ordinates and at the given pressure and temperature of 250C the state of some will be close to their particular Critical Point in a very upgraded state, where the Van der Waal bonding will be very loosened giving rise to the very high fluidity values, whilst others will be in states which for them represent a very downgraded state and where their Van der Waal bonding is very much stronger giving rise to low fluidity values.

Tt therefore follows that if in the svstem under discussion it were Dossible

to work in a much higher pressure range then this would makethe use at tluids exhibiting very high fluidity values at normal temperature. This in fact should be possible since one could place into the enclosed chamber of the sub-system vapour at a high pressure and more specifically at the lower pressure of the higher pressure range. Then fluid that exited from the turbine inside the chamber would exit at this pressure from the higher pressure of the working pressure range, and if the vapour pressure already inside the chamber was at the saturated vapour pressure for the temperature of the exiting fluid then it would remain fully in the liquid and not be required to flash off any fluid in a vapour phase.However in practice it may exit at a pressure and temperature marginally higher than the SVP inside the chamber represented, which would then flash off some heat in a vapour phase and this would add to the vapour pressure already inside the chamber, although this would depend upon the efficiency of transference of the fluid's P-E energy to the turbine.

Therefore, in practice it may be necessary to maintain steadier state conditions in some way, which would probably be achievable by simply continuously bleeding off a little vapour pressure. Therefore, given that in practice it would be possible to maintain steady state conditions then the fluid exiting from the turbine would essentially still all be maintained in the liquid phase via the saturated vapour pressure level that was already present in the chamber, and from there could flow on to the heat absorbing unit as a liquid in the normal way but now a liquid under a much higher pressure as that required to maintain the fluid in the liquid phase.But the point to grasp at this stage is that the pressure on this side of the system once placed into the enclosed chamber as vapour pressure would serve to continuously maintain the fluid in the liquid phase on this side of the system, without the need to continuously maintain the required pessure in some other way and it follows that the fluid would not need to flash off any pressure-enthalpy energy into a vapour phase on its exit from the turbine inside the chamber, albeit it still being at a high pressure relative to normal ground state pressure of IATS. However, its temperature at this stage would have to be sufficiently low for the subsequent absoprtion of heat, which if natural water heat would

as low as say 90C, i.e. as the working temperature for R-21.Thus at the chamber stage if the fluid did not exit from the turbine at such a temperature then vapour therein would have to be bled away at a sufficient rate to subsequently give the desired temperature of liquid for the next heat absorbing stage via flashing off any residual pressure-enthalpy energy. However, if the subsequent heat to be absorbed was that of the heat of compression of an ARC cycle then the system could also operate in a higher temperature range, but at this stage still considering such a method of operation in the context of harnessing the low grade heat of natural flowing waters. Thus, the liquid phase of the refrigerant at 9 C but under a high SVP pressure to maintain in the liquid phase in the way described would then pass through the heat absorbing unit and therein absorb heat. When on the addition of further heat it would then vapourise in the normal way, but with the difference that the vapour pressure thereby generated wound also have to be at the higher SVP associated with the temperature of 9"C for the refrigerant. Which would in turn have to be the pressure of the vapour on the other side of the unit between the unit and the inlet to the compressor. Which however would be the lower pressure of the higher working pressure range, but the vapour would still be at 9 C at this stage assuming no further heating took place. Thus the compressor could then take in this vapour and compress to the higher pressure of the pressure range in order to upgrade the absorbed heat to the temperature required for the turbogenerating part of the process.Which could become removed whilst still maintaining the high pressure of the working pressure range in the normal way.

Thus the fluid could then pass onto the turbine of the sub-system and there transfer energy which took its pressure down to the lower pressure of the higher working pressure range. And the same cycle could then commence again.

In such a method of operation the only requirement would be that under the lower pressure the Liquid still possessed a capacity for absorbing heat in a latent heat energy mode. In other words the lower pressure would not have to be that high such that at this stage the fluid was under a pressure close to or above its Critical Pressure. In order that when the liquid phase passed through the heat absorbing unit it could in fact absorb heat into a latent heat energy mode, albeit havirgbecome reduced in heat absorbing capacity.

Now if one considers the refrigerant CC1F3 in this context, i.e. one of those exhibiting a very high fluidity, the general data reveals that its Critical Temperature is 28.90C and its Critical Pressure 38.2 ATS. Therefore for this refrigerant at 9 C under the SVP pressure required to maintain it in the liquid phase, say 25ATSw in the absence of full data, then it would in fact still possess a high latent heat capacity and in fact possibly still around half the latent heat capacity at its ground level since it is only in the last stages of pressurisation that latent heat capacity falls off very rapidly with iXncreasing pressure.Whilst he other two refrigerants in the high fluidity category, i.e., CF4 and CHF1, have Critical Temperature of -45.670C and 25.9"C respectively. Thus the former probably could not be applied in this way and the latter would not be as suitable. Thus basing this alternative method of operation on CClF3, i.e. R-13.

In its latent heat capacity becoming substantially reduced to half or less the compression stage would not in fact have to handle more fluid throughput for the creation of a given level of enthalpy energy in the fluid at the end of the compression stage, as can readily be seen from a consideration of the P-E diagram on Fig. 2, but the equivalent of state D would be very much higher above the Critical Pressure and Temeprature for the refrigerant.Thus it then being question of how much energy would be yielded at the sub-system stage where the depressurisation would be passing from the high pressure of the compressor, which could in fact still be 100 ATS, down to the lower pressure of say 2s ATS, in comparison to the amount of energy required to be placed into the compressor to raise the subsequent vapour stage from the pressure of ATS back up to 100 ATS. once more in the next cycle of the process.

At this stage in this work this is the part that God only knows, but theorising what may be the situation basing on past knowledge.

Well in this system the fluid at the louver pressure at the end of the subsystem process will still in fact possess a very high fluidity in comparison to the equivalent stage in the use of R-21, and in fact close to the quoted value of 62.5 for R-13 at 250C. And at the higher pressure and temperature at the start of the sub-system process presumably the fluidity of the fluid will be very much higher resulting from the higher level of P-E energy in the fluid at that stage. Thus it will be a question of how much energy is yieldable in passing from these two fluidty states, which as inferred may, therefore, only be at the level one would obtain in the use of R-21 in passing between two lower fluidity states, as one would expect of course to comply with the laws of conservation of energy.However, having said that the transference of the energy may be very much more efficient in the higher working range.

Which would be in keepeing with a consideration of the P-E diagram and the lowering gradient of the liquid line with increasing pressure and and temperature, assuming the energy transference curve could follow a similar line.

Moreover, it would also be in keeping with the fluidity increasing at an increased rate with increasing pressure and temperature. Thus the higher

the working Fluidity range thenlthe'more the enthalpy energy that

could become transferred of the initial amount of energy present.

Thus such a method of operation could well be an alternative way to increase upon the 40n level of transferred energy postulated for this stage of the system in preceding discussion, perhaps to a fully self-sustaining level.

Again there are many similarities and equal and opposite similarities with systems devised hitherto on the Planet aimed at the creation of Heaven on the Planet, and indeed with the systems devised in my work. For example it would seem to be the equal and opposite of the BGS Energy addition system in the preceding and there are similarlities with the process under PA 8728601, which also can be operated in an elevated pressure range or with the addition of vacuum energy. Then there are similarities in relation to working between different ranges of properties for different fluids.

An advantage could be that it may be a method of operation that works f efficeintly based upon a simpler impulse turbine of the Pelton Wheel type in comparison to the more complex use of a reaction turbine. However, in the use of such a turbine then it would Drobablv be necessarv to re-desien

the curvature shaping at the impellors thereon to add thelettect or reducing volume/fluidity lowering the forward linear velocity of the fluid jet.

However, it will be a questionof whether the energy of the fluid jet can become transferred before vapourisation of the fluid in the jet to the vapour phase takes place which whilst still at the higher end of the range would otherwise vapourise off under the lower SVP in the surrounding enclosed chamber. But should the kinetic energy be fully transferable to the turbine and finish at a temeprature which thermodynamically relates to the surrounding vapour pressure then the surrounding vapour pressure will in fact be the SVP pressure for the lqiuid attemperature it finishes and no fluid vapourisation would then take place.Moreover if any flashing did take place then it would build up the vapour pressure inside the enclosed chamber to have the effect of suppressing further vapourisation at some level and a steady state should be establishable perhaps in combination with bleeding off some vapour or perhaps adding to the pressure, in equal and opposite similarity to the BGS energy system Which could

be efected via a pressurising diaphragm or piston on one of the side walls of the chamber with which one could sensitively and infinitely vary the volume of the chamber, i.e. reduce for increased vapour pressure and vice-versa, which of course would hardly consume any energy.

Thus in such a way it would be possible to increase the existing vapour pressure inside the chamber in order to suppress any tendency for vapourisation to take place.

A further advantage of operating the sub-system in the higher pressure range as possible via the use of R-13 would be that one could in fact set the liquid in the chamber at a lower temperature simply by lowering the lower vapour pressure of the working pressure range. Which would be advantageous when trying to harness the low grade heat in colder waters, i.e. in such a way it would be possible to take the heat absorbing temperature of the liquid phase to as low as 10C to give a maximised temperature gradient between water and refrigerant fluid whilst still avoiding freezing for use of the same system in waters with temperatures as low as say 50C. Indeed this would be a parameter variable of the process for maximising on energy output in any case.

1 It must be posible to pre-fill the enclosed chamber with the desired optimum vapour pressure.

2 It must be possible to streamline the fluid at the high pressure and temperature state into a fluid jet, which in effect would be a liquid jet but at a somewhat higher temperature than normal temperature.

3 But then it would be a question of whether when issuing forth out of an impulse jet nozzle it would flash heat off in the usual way or whether it could reach the impellors of the turbine and could impart all its forward aligned kinetic energy to the impellors of the turbine before any flashing took place. To then take the temperature, i.e. kinetic energy, of the fluid jet to a temperature that would not flash under the conditions of the surrounding vapour pressure to leave the fluid fully remaining in the liquid phase for the next cycle.

4 Alternatively a reaction turbine of the type depicted on Fig. 1 could probably still be applied when premature vapour flashing would not be the same problem because the fluid will impart all the energy that it is goingto impart to the turbine before it exits from the turbine nozzle.

However, I think this may be the second approach to try in this case, whilst in equal and opposite contrast it could be the first approach

to try when trying to add BGS energy in a lower pressure range1 in contrast extending below normal IATS. pressure. Although there is obviously a question mark over the use of this type of turbine anyway in such a system, and if in practice it was found that only an impulse turbine could be applied then the higher pressure method of operation could

be the better approach for such a system. Having said that one draws the similarity with a jet or rocket engine system and one thinks that perhaps the mechanics of the system under discussion would simply be an addition to such science and technology.A rotating motion becoming created rather than a linear motion, but basically the same mechanics being involved.

5 The energy that is yielded by the most successful turbine must be close to that required for the compressor.

Thus, at this stage it would seem that the fluidity parameter is taking on even more central importance Firstly the effect of temperature on, or to put it another way heat addition to, the fluid and now the initial fluiditiy of the liquid at our ground level conditions and then the effect on this parameter of adding further heat.

Thus another aspect that God only knows at this stage, (but which will become revealed for and by the lucky chaps and/or lasses that take the work from

here ScÈrn and carry out the first stages of the practical work#is which way will improve upon the efficiency the most.#g,Via the addition of BGS vacuum energy

working#range of liquid phase tluidity, or, a higher energy transference effeiciency

I rE tStr, ie 5 woa / working ín a higher range of liquid phase fluidity. At this stage my feelings are that both methods

perhaps become perfectable to around the same 50-60% energy conversion level

that the system working in the higher fludiitv range mav show improvement quicker at less cost and

time via an impulse turbine but then1 may nave to turn to the use at a reaction turbine for further improvement. Whilst a reaction turbine

have to be used from the outset to try to add BGS Energy.Then a further aspect will be that some processes in which the sub-system could be applied could morewso pre-dictate the range of properties that are required of the refrigerant, and more specifically the working pressure and temperature range thereof at either end of the workingrange. For example, perhaps when applied in the Advanced Brierley Process. Therefore, I think development should be in both directions and would have to be anyway all the way to final perfection since only then would one find out what God only knows at the beginning of such a stage in the work and indeed at this stage. Um.

Perhaps needless to say, at least to the scientific fraternity, it would seem

at this stage that thejsystem is probably intended for the future and therefore that one way or another it will probably be possible to be rendered viable and worthwhile, probably all the way to a self-sustaining level and if so then the sub-system at least could well prove to be one of the most successful

systems in terms of today's and / , and indeed in the more CBenraL terms of scientific, terrestrial, and cosmic values too since one outlet for the subsystem could be in processes able to produce a triple purpose capacity for power, rainmaking and refrigeration in a more convenient manner than the process under PA 8728601, since two main benefits could ensure.Firstly, condensation of the turbogenerating fluid would be carried out inside the process by the process without destroying ARC cycle exhaust cold air yield, and secondly in so doing the ARC cycle could be operating at a lower capacity for the process and therefore require less energy from the process to make up its energy shotfall. Thus, then and thereby such values of the spectrum of values on this Planet, presumably when as in Heaven, becoming superimposed and synonymous. Which in fact is an aspect that will probably apply to the whole of my work on this occasion.

However, I must re-emphasise again that I am in no way being definite about the certainty of this process sincethe circuit of the process has been around for almost half a century possessing the problem of depressurisation of the fluid from an upgraded state to a lower state with the only means being adopted being via a throttling device, and indeed with DeoDle of obviouslv high minds stating that this would be the onlv wav.

Iheretare perhaps I am being arrogant, i.e. high minded / a talse nature, to theorise otherwise.And the fluid could issue forth out of the nozzle system of any turbine type as a liquid vapour mixture with none or very litle of the P-E energy having become transferred to the turbine before the energy instead becomes transferred into the latent heat energv mode of the fluid.

Or in the case of the useof an impulse turbine,theforce of the fluid jet

on striking the impellors1 disappear in a cloud at vapour rather than becoming transferred to the turbine before the fluid has a chance to converted the vapour phase. However, with respect to this aspect it should be understood that such a mechanism would be very different than the mechanism involved in a steam or vapour impulse jet system where a proportion of energy has no option but to pass into the latent heat energy mode of the fluid at lower pressures and temperatures on transferring energy to the turbine and thereby becoming rendered in such a lower grade state. Which of course is the equivalent mechanism in such a system to that of fluid contraction in the system under discussion at lower pressures and temperatures on transferring energy, when again the fluid would have no option but to conform to it's state conditions, albeit an equal and opposite mechanism. Thus, these two facets of the system must not become confused.Moreover, the very way that the fluid becomes maintained in the liquid phase in the system under discussion and indeed goes deeper into the liquid phase is via transference of kinetic energy to the turbine. Thus on transference of energy in this system, which must come first providing vapourisation can be avoided en route, the fluid is likely to go deeper into the liquid phase via cooling and contraction then taking place, as well as removal of the energy anyway.

Furthermore,if one considered thchigherpressure range system based upon CC1FJ, i.e. R-13, then at the high pressure of such a system the fluid state would commence a very long way above the Critical Point for R-13 even if only pressurised to say 100 ATS to again give a fluid temperature at the compression stage of around 300-3500C (in the absence of full data), since the Critical Temperature and Pressure for this fluid are 28.90C and 38.2 ATS.

the fluid could again be around 1700C and 100 ATS at the start of the sub-system process.Butthen on imparting kinetic energy to the turbine will only go down

ok say 25 ATS. at the temperature that thermodynamically corresponds with such a pressure, which in the absence of full data will be around 50C. Remember the presure could go all the way down to ground state and therefore from this point of view there should be no difficulty in just going down to around just 25ATS to give the desired

temperature for the next cycle. Thus the above is an important aspect to grasp in this mode of operation which I emphasise in following discussion since on depressurising on transferring energy there wouldn't in fact be a latent heat energy mode for energy to otherwise transfer into almost all the way down to the ground state pressure of the system, ie, 25 ATS.However, it could prove easier to achieve via a reaction turbine of the type depicted on Fig. 1, which could be very readily controlled for fluid exit pressure simply via adjustment of the CSA of the exit nozzle thereof, whilst in the use of an impulse turbine one would have to try to prematurely terminate the impartation of the fluid jet energy. Which however would seem possible via appropriate design and dimensions of thecurvature of Pelton Wheel impellors,ormcre simply via adjusting the angle of impact on the impellors of a different type of design, e.g. of the type having angled impellors set around the periphery of a turbine blade, which would perhaps be the simpler approach. Then it should also be remembered that already surrounding the turbine will be saturated vapour pressure of the fluid's vapour phase at the desired pressure of 25 ATS.

to which the fluid on impact with the impellors will be fully exposed) (again there being some eaual and opposite similarlity here with methods of operating the process under PA 8728601),

hohNetract from the energy of rotation of the turbine in the way of air resistance. Therefore perhaps

in such a system one would adopt the use of the reaction turbine type straight away from the outset, since it would be very easy to design the outer casing for minimum vapour resistance. However, there would inevitably be some turbulence created and there would be the rear wake zone to consider which would tend to deplete the zone immediately at nozzle exit of vapour at 25 ATS.

In which case the pressure drop could go further than to just 25 ATS. to give more energy yield, with the fluid on exit still going on to adjust to the surrounding SVP pressure to which it would then become subjected to. However, in so adjusting from the lower temperature that would thereby be created in the first place to the higher desired temperature for the next cycle then some vapour condensation of the vapour already existing in the chamber would take place.Which of course is a desirable way round from the pointof view of no vapour flashing subsequently taking place and the maintenance of the fluid fully in the liquid phase at this stage, but would require a continuous external feed of vapour into the chamber at the SVP of 25 ATS. by an equal amount to what which is condensing, which however would only involve a small fraction.

Which then would be an aspect of this method of operation in equal and opposite contrast to the BGS energy system.

Therefore taking all aspects into consideration and the larger perceptions of extensions on existing advanced technology in several areas and fields of advanced technology then the use of a reaction turbine of the type depicted on Fig. 1 is beginning to come to the fore as perhaps also being the better approach for the high pressure range method of operation, notwithstanding some earlier discussion. Obviously the full bent arms of the turbine could be fully covered with one full tear drop shaping for the outer casing. Or alternatively the whole of the bent arms could be covered in one unit so that the unit simply appeared as though a disc in external appearance with fluid issuingforth from nozzles all around, when one can envisage that there could in fact be little resistance to rotation from the vapour above and below.However. it mav be

a question of which design gives the overall better auvantage)as witn aauea rear wake zone energy creation through design.

Having said the above, the same could in fact be the can for impulse turbine use, i.e. there could be little resistance to the rotation of a rotating

design and the surrounding vapour need not be surrounding at the actual point of impact with the impellors thereof, only when the fluid falls to the bottom of the chamber since no matter what its state immediately after impact it will adjust to the surrounding SVP conditions afterwards.Thus on impact the liquid fluid jet could again go to a lower temperature and pressure to increase upon

energy transference, whichl could be deemed to be a stage aKin to adding bUS energy only taking place higher up the P-E diagram, then on the subsequent liquid cascading to the bottom of the chamber it would adjust back up again to 25 ATS. and associated SVP temperature involving some condensation of vapour,

etc. Ihus one can envisage a rotating disc/spinning the surrounding vapour off such that it presented very much reduced resistance to rotation, with fixed nozzles very close up to the periphery of the disc, where the angled impellors would be, and the liquid jet imparting more energy than just that down to 20 ATS., but then subsequently adjusting back up to this pressure and associated temperature, which may not involve much condensation of vapour, although the liquid would have to extract heat from the adiabatically stored vapour in order to become at the same temperature which in turn would cause some condensation.

All of which is somewhat finer detail and away from the main point that I intended to make at the beginning of this particular discussion. Which was when considering the fluid's tendency to create a vapour phase then in the high pressure range method of operation this would be less likely to take place because it is not until the fluid jet at 100 ATS and 1700C imparted energy all the way down to 38 ATS. and 28.90C could any energy transference into a latent heat energy mode take place because there would/be one present

during all of that stage of the energy transference the fluid jet would be above the Critical Point state whereonly then do latent heat modes in the fluid

become present.

In Coll rOs{;when considering

thel M energy addition system trom this standpoint in mind it would be a question of pre sub-cooling to a level which avoided vapourisation, albeit perhaps enabling some very early stage bubble formation for a volume maintenance advantage. Which however may then require vapour removal from the chamber by a corresponding amount, although they should in fact condense and disappear under the final state of the fluid on imparting all the energy thereof.

Whilst the higharpressure range method of operation will have advantages of ease of flexibility simply by adjustment of the SVP in the enclosed chamber, which in theory could also readily enable very low temperatures for refrigeration as well as readily facilitating for waters of different temperatures, which could be a distinct advantage when wishing to use the same system under the different seasonal temperatures and in facilitating for the differences that exist as one goes form one part of the World to another, I still have an open mind as to which method would actually give the highest increase in energy yield. But obviously the high fluidity range system is perhaps the most attracting at this stage.One can envisage the disc shaped impulse turbine

spinning around in the horizontal plane in the centre of the enclosed chamber, with fixed nozzles pointing directly downwards above and symmetrically all around the periphery of the spinning

flat disy, where there would be small angled impelloers through which the jets jet would flow vertically downwards, then exit from the underside and fall to the bomm of the chamber after imparting their energy to the tubine, and then adjusting to the surrounding conditions of SVP vapour presure at 25 ATS., or thereabouts, already permanently present in the enclosed chamber, but becoming replenished to make up any condensation that may take place.

Different conditions then being effected by a combination of adjusting the impellors of the turbine, not for highest transference efficiency as is usually the case but more simply for the P-E energy that one desires to be left remaining in the liquid jet on exit from the underside of the turbine, and SVP vapour pressure in the enclosed chamber.

Therefore. I would d Drobablv.

recommend such an approach as a starting point torl K-13 the retrlgerant. The goals beingfirstly to get as close to a self-sustaining level as Possible

for the comp'essor input/sub-system turbine output system, then,the low-grade heat temeprature range that one can cover via adjustment of the same system based on the same refrigerant whilst still maintaining a similar level of efficiency.Whilst a starting point for the impellor design could be that of the hydraulic fluid turbines inside diesel-hydraulic locomotives, when the liquid jets would probably not be vertically down but slightly angled themselves, which in fact could be the basis of easier adjustment since in effect such adjustment could involve rendering the energy transference efficiency worse if initially designed with the potential for highest energy transference efficiency down to an appreciable lower pressure than 25 ATS.. etc.An aspect to bear in mind is that it is the higher working fluidity

range via wnicn one is, trying to improve upon erriciency beyond tne Dasic 4ua, level and any other due to transference to a lower pressure would be a bonus.

However, the liquid fluid flow under such circumstances would probably also exit at a lower temperature than that of the surrounding vapour at 25 ATS. and would therefore tend to condense some of the vapour reducing the desired pressure of 25 ATS. above the liquid phase for the next cycle, ie, that of heat absorption and revapourisation at the pressure of 25 ATS. so that the compression input energy becomes less in the vapour already being at 25 ATS.

at intake to the compressor. Therefore, a better technique here than the foregoing would be one of using the heat source, eg, that of natural flowing waters, to reheat the liquid phase at the bottom of the enclosed chamber such that in the steady state of the process the required amount of revapourisation into the chamber was taking place for that becoming precipitated.

Thus to recap 9 the compressor input energy in the high fluidity range method of operation iJould only be required to compress from 25 ATS. to 100 ATS. compared with 1 ATS. to 100 ATS. in the case of the original system based upon R-21, and the fact that the fluid under such a pessure would only possess around half or less of its latent heat capacity would not require more fluid throughput for the compressor to have to compress for a given amount of heat of impression energy at a given temperature, since in effect to the compressor stage it would just be as though 25 ATS. of vapour compression had already been carried out before the compressor then carries out the remaining 75 ATS.

of pressurisation. Therefore, a further advantage of operating in such a manner will be that for the same heat of compression energy level at the turbogenerating stage and then at the start of the sub-system stage will only

75 of that required for a compresion from IATS. to the same level of pressure, temperature, and heat of compression energy. But then at the sub system stage one would only obtain energy from lOGATS to 25 ATS, reDresentinR

ot the initial energy quantity at~ the start of this stage.However,

points being that when that of the energy is transferred in this system then it may do so at a higher level of efficiency in transferring all the energy in the upper three quarters of the pressure range through a range of much higher fluidity values, and therefore the energy yield obtained

likely to sustain the compressor energy input. Because the initial amount of energy will still be the equivalent of the

value of 240 KJ/KG and thenBOS of this for that potentially harnessable in this system, i.e. 192 KJ/KG. While thecanpressor input requirement will still be the equivalent of7SX of 120 KJ/KG = 90 KJ/KG.And the transference efficiency level could well have gone up to soy of 192 = 96 KJ/KG

could then be a self-sustaining system. Obviously I now need more accurate data to determine the values involved more accurately, including the P-E diagrams for the full range of refrigerants, and of other possible fluids. However, the energy transference efficiency

boil down to a ratio of liquid volumes before and after, or alternatively

be compute by taking the mean fluidity value of the high fluidity range and placing

into the equation KE = W2 where V2 can be fluidity2 tar, empirical comparative

However, more accurately one could compute the actual linear forward velocity of fluid jet that the fluidity value actually represents for the actual applied constant pressure head, and then obtain the KE values in absolute terms rather than via an empirical route. However, further considering the empirical approach at this stage. The lower fluidity value of the liquid after passage through the turbine will in fact still be a very high value close to the value of 62.5, i.e. this will be fluidity that is still remaining in the liquid on exit from the turbine of the system and will arise form the fact that the liquid state at this stage in the process for this fluid and still at 25 ATS. pressure will be close to the Critical point state for the fluid.Thus the actual energy that becomes imparted

to the turbine will1 hot arise from this fluidity but

the increase in this fluidity that is caused by the extra pressure-enthalpy energy in

the liquid before the sub-system stage.Whilst not1 wishing to become bagged down with the nitty-gritty of the more detailed and complex calculation at this early stage obviously it could prove possible to equate fluidity measurement to the actual kinetic energy of the fluid jet flow and then equate this measurement to the enthalpy energy contained in the fluid for any particular state on its P-E diagram for any particular fluid for the purposes of quantifying and having better practical control over the parameters of the process, as well as being an approach to combining the mechanical engineering view to the thermodynamic view, and also probably to a more in-depth view involving quantifying Van der Waal forces.However, the main aspect at this stage is that the fluid on exit from the turbine of the sub-system will at that stage possess the high fluidity value because it will still be an upgraded state as necessarily still under a pressure of 25 ATS., and the actual energy yield will arise inmghlpractice from the effect on this base level of fluidity for the system of the additional P-E energy present in the fluid before the sub-system.

a high base level of fluidity will presumably give rise td"1fluid jet which on the exit side of the turbine vould still possess a high forward velocity under a given applied pressure then the increase in fluid jet velocity that is required to yield the forward kinetic energy equivalent

the additional P-E energy in the fluid

not in fact need to be all that much higher, and therefore nor the fluidity increase. Which can be gathered from a consideration of

values for velocity, v, in the equation KE = imv' before and after the turbine.

that the level of additional P-E energy in the fluid before the turbine could well effect the necessary increase in fluidity in order to yield its equivalent as transferred kinetic energy of fluid jet to the turbine. However, my aim at this early stage with respect to such aspects of the system being more to push the door ajar to possible future approaches to quantifying for control over the various parameters.

Moreover, with regards to my work on this system to date probably the analogy could be drawn with the P-E diagram for R-13, which has the bulk of its phase state diagram below ground level with anormal BDt. of 1 ATS. at minus 81.4 C.

and only has the top part sticking out above the Planet's ground

rather as the tip of an iceberg with the remainder in the waters of the sea. But nonetheless sufficient to work on and sufficient to be able to be used at the Planet's ground level in the way discussed. However, as in the case of an icaberg, probably still with much in the waters of the sea and yet to be revealed, which conveniently progresses to discussions on to two further aspects of the system.

Firstly

prove possible to add Bonus Energy to the energy yield for a system operating in a high fluidity range as tn the preceding discussion

not be possible because any extra energy yield beyond that to the lower pressure

2ATS. in the example for R-13 that one may be able to acquire would become balanced by the energy that one would then have to consume in replacing condensed vapour by SVP vapour at 25 ATS. , since if in the transference of the fluid's jet energy went beyond the lower pressure and temperature conditions generally prevailing inside the chamber, then initially the exiting fluid jet would be colder than the SVP conditions of the surounding vapour and would therefore initially have an effect of condensing some vapour as equilibrating of temperature took place. However, the general SVP conditions inside the chamber would be colder than the natural flowing waters containing the heat one is subsequently harnessing. By definition of the necessary conditons for harnessing the heat. Therefore one could flow this water also around the chamber and transfer back into the fluid therein the necessary amount of heat required to revapourise the condensed vapour, from the natural heat in the water.

In this way therefore one could try to acquire as much Bonus Energy as possible and in effect replace the extra energy taken out of the fluid at this stage

heat energy contained in the water. When one would not then require to consume energy in replacing the vapour. Moreover, in practice the liquid jet would be exiting from the underside of the turbine still at a very high speed, as indicated by the high fluidity that would still be existing at such a stage, and therefore would reach the bottom of the chamber and enter the layer of liquid phase already existing there very quickly.Which could then render the system easier to heat back up in such a way, although it would not really make a lot of difference since one could easily control the heat input at this stage to maintain the desired SVP pressure and temperaature in a steady state no matter how or by how much the interim condensation, which in practice in the steady state would probably be continually falling as rain between the fluid jets with then vapour becoming generated off the surface of the liquid at a controlled rate corresponding with the amount of fluid in the falling rain.

Thus and thereby in effect at the subsystem stage one could directly convert

heat contained in the waters into turbine energy, which would then add to that required for the compressor input, in addition to the system absorbing and yielding the other amounts of energy. However, remember that the central parameters would be heat of flowing waters and the temperature that the liquid phase would have to be set at to be able to absorb that heat along the length of the heat absorbing unit. Which in turn would pre-determine what the associated SVP of the vapour inside the chamber would have to be in order to give the required temperature of liquid phase for absorbing the heat of the flowing waters in the desired size of heat absorbing unit.Therefore, this would have to be the general SVP level inside the chamber to which pressure level the energy yield may be falling short, although further remember that it is in working in the hither fluiditv range in the first place that

one / noping to improve upon tne ettective energy transterence etticiency.

Therefore, it will be a question of how much Bonus Energy one can acquire under the general external conditions of vapour at a high saturated pressure immediately surrounding the exit side of the turbine, e.g. 25 ATS. for R13. And under the conditions of the heat energy equivalent of the Bonus Energy having to be placed back into the fluid inside the chamber at the same rate from a further volume of the natural flowing waters. But with respect to the latter aspect if one can thereby render the sub-system fully self-sustaining via direct conversion

then it could be

way to harness the heat energy as via the turbogenerating system.

Which

the would be required to yield/surplus energy from the process, but under such conditions neabr then all be available for external supply. The fact that the fluid jet could still have a high forward velocity on the

exit side could1 be advantageous with regard to avercamingthe external pressure, which f polarised into forward dynamic pressure of a fluid jet could overcome the surrounding random pressure by an amount approaching a factor of around 1.40 times.If so then the fluid jet CSA at exit could approach being 30% smaller at such a stage if still well streamlined, ie, as opposed to having become re-randomised, transferring the increased forward dynamic pressure that a 30% reduction in CSA would represent for the same mass flow on passage through the turbine. Thus the keys here would be energy impartion rather than impact, with subsequent channels through the impellors being designed to re-streamline the fluid jet before exit on the other side.

Then te additional approach would be to try to deplete the zone immediately on the exit side of the turbine in some way, so that the fluid jet could overcome the external pressure by an even higher amount. In the case of the disc

impulse turbine rotating in the horizontal plane in the centre of

chamber, then it could prove possible to fix some vapour

shapings protruding down from the underside on the side of the channel exits that rotate into the vapour, in order to sweep the vapour aside and such that the external vapour pressure on the channel exist side of the shapings becomes depleted in a localised wake zone manner to a pressure somewhat lower than the general vapour Dressure.However. such amethod in such a svstem

will depend upon the exura I eslsLance

to rotation compared with the gains.

perhaps the main way for this type of turbine will be in the art of designing the channels through the imnellors so as to re-streamline

tfle could let at exit.In tact since thevould,be under a relatively high

pressure1 then perhaps there could be normal

shaped nozzleson the exit side of each channel through the impellorsJ although the type of

design employed in an alternating fixed and rotating blade turbine could be a better starting point, which re-streamline as the fluid becomes channelled through the fixed blades readv for imDact with the next rotating hl ade. The

ditterencesin the system under discussion would be?tYat the fluid would be con

tracting as it depressurises and cools instead of expanding anyone would leave off the last few blades at the required elevated pressure drop rather than going all the way down to ground level and beyond.However, a depleted rear wake zone effect could probably be created in a better way via the use of a reaction turbine of the type depicted on Fig. 1, adding further to the Bonus Energy that could be obtained in this way. In fact, with four good streamlining tear drop shapings for the four arms of the reaction turbine depicted on Fig. 1, one can envisage that the full ring through which the tear drops would travel could become almost fully depleted since the vapour phase through which they would be travelling would be continuously being pushed aside by the tear drop shapings of the four units. Perhaps to such an extent that the transference of the fluid's energy could take place all the way down to 1 ATS. or below. Very credibly so in my mind's eye since one can envisage that just the sides of the tear drop shapings continuously rotating around in a circle very fast would keep the vapour phase to either side of the tear drops and not in the part where the liquid phase of the fluid is actually exiting from the rear of the tear drops.

the surrounding vapour phase then becomin*that to which the exiting liquid phase subsequently becomes subjected to and thermodynamically associated with as soon as it falls through the vapour to the bottom of the chamber under gravity. Thus in such a way it may prove possible to acquire Bonus Energy all the way down to 1 ATS.

and below. Whilst the input to the ccmpressor would still remain the same, i.e. commencing with the vapour already at the pressure of 25 ATS. Which could reDresent a 2s% imProvement in this energy balance if possible

F 5S down to 1 ATS and therefore in such a case could take

40T conversion level to u,

could1 possibly become increased even further by a vacuum effect becoming created actually inside the depleted ring and acting directly on the fluid exiting from the turbine nozzles.

However, 2s ATS. vapour pressure would be quite a high vapour pressure to keep fully at bay by such a system and especially if a vacuum were competing for the vapour. But nonetheless one can envisage that such a system could create a vacuum inside the ring through which the tear drops are travelling, with each one compounding a rear wake zone effect, and especially if travelling very fast. Therefore, such a system will involve optimising between maximising upon rotation speed against minimisation of vapour resistance, and could perhaps be/become a better approach than via the preceding impulst turbine method for this type of method of operation of the process.Certainly it would be a method that extended further on some of the more advanced advancing fronts of science and technology leading into the new Age and being a basis for that Age.

However, having said that and taking up the point further with respect to impartation rather than impact, impartation is really that which takes place in a Pelton Wheel type of turbine in contrast to impact in the case of normal impellor blades. Therefore, perhaps the use of a modified Pelton Wheel would be the better approach for the foregoing method of operation as based upon R13 since one can similarly envisage such a turbine rotating in the horizontal plane and perhaps even more effectively spinning the surrounding vapour at 25 ATS. away from the actual impellors of such a turbine and such that impartation could take place all the way down to normal 1 ATS. pressure.

Thus in such ways it

be possible to increase upon energy yield by an appreciable amount in a system which could already have a higher level of energy conversion than the basic level of 40%. Thus supposing 50% of 240 KJ/KG becomes converted to yield a level of 120 KJ/KG then this becomes increased by 33% to 160 KJ/KG, then such a yield could be in surplus of that reauired to fullv sustain the compressor.

the water heat absorbing

capacity for the charnber lonly require to be 40 KJ/KG of fluid throughput which compares with the 240 KJ/KG being absorbed by the fluid in the earlier system discussed based upon R-21 in the subseauent main heat absorbing stage,

which brings the discussion to the second tacet at, suDsequent thinking, as follows, but firstly stating that perhaps it would be more realistic to think that the sub-system could perhaps be rendered just self-sustaining by such means, but nontheless realistically so and which is all that would be required for the ideal to be achievable.

turbogenerating

be yielded for only half the latent heat absorbing capacity, or thereabouts, then the required capacity of main heat absorbing equipment would be reduced by a pro-rata amount.

Trying not to confuse this aspect, but in effect the base level of heat that becomes continually recycled in the process would in the system under discussion based upon R-13 be becoming recycled already in a partially upgraded form compared with a system in which the liquid phase is under 1 ATS pressure.

Which would also apply to its base level of latent heat. Therefore a part of the base level of latent heat will already be upgraded in the external kinetic energy mode under the pressur of 2ATS., and therefore the fluid will be required to absorb less latent heat. However, as far as the stage in the fluid's circuit involving the turbogenerating system and then the subsequent sub-system is concerned, the fluid will still contain the full amount of absorbed heat

But the difference being that a proportion of the upgraded heat then becomes continuously recycled, rather than going down to and commencing the next cycle at base level.

Thus in the use of R-13 in the high fluidity range method of operation the required main heat absorbing equipment could be reduced by around half for the same compressor and turbogenerator capacity, but if in combination with the new technique for adding Bonus Energy then the total heat absorbing capacity could be increased by up to 50% but to give a total still three quarters of that which would be required for the system based upon the R-2lfluid.

And the Process could not only now be yielding all the turbozeneratinz energy

for external supply but could also noah be 'yielding a surplus at the sub-system turbine stage. Thus under such conditions the efficiency of the process as expressed in terms of energy output compared with total absorbed heat could be around 33% for a process in which the sub-system is just rendered self- sustaining, and up to 40 for a proces which could produce a surplus ~ of Bonus Energy at the sub-system stage in ever improving ways.However, realistically perhaps just less than self-sustaining with respect to the subsystem would be achievable via this route unless BGS energy below 1 ATS. was managed to become added, which probably wouldn't be achievable via the Pelton Wheel method but perhaps via progressing on to the Reaction Turbine method, etc, in keeping with developing stages of progress.

As a final aspect of this discussion at this early stage,

and thereby emphasising the beginning part. For the sub-system based upon R-13 fluid it is probably incorrectly described as being throttle energy conversion, which would apply to a system where the upgraded fluid would otherwise have to become depressurised by effecting transference of energy into the fluid's latent heat energy mode.Whilst in the system under discussion the fluid would not in fact possess a latent heat energy mode for 80% of the time that it would be transferring because it would be commencing off a long way above

the Critical Faint for R-31 at 289oC and 38.2 ATS, which in fact are1 quite close to the state the fluid would be at the end of depressurisation, which in the absence of data would be around the assumed pressure level of 25 ATS.

to give an assumed associated liquid phase temperature of around 50C. Thus towards the end of such a system the fluid could be prone to some vapourising.

However, the main point to grasp is this: after having imparted the bulk of the kinetic energy that it is required to impart to exist as a liquid phase under 25 ATS. vapour pressure not only would there be hardly any energy left to have to vapourise off, but by that time the fluid would be well over to the left in the liquid phase by very definition of having transferred its kietic energy when ,on the loss of the energy to the turbine4 the fluid state must be moving to the left by a ccrresponding amount on the enthalpy energy equivalent axis of the P-E diagram.Nonetheless the fluid state could just enter the early stages of bubble formation during the last 20% of energy transference, although one could very readily sub-cool to a lower temperature in the first place in order to avoid any such effects if undesired, and convert the heat energy in the turbogenerating process instead. An aspecttould be that one would have to

as far as was necessary in the first place in order to ensure that the state of the fluid was liquid at the start of the sub-system process, and did not expand as a vapour.However, I think it would be correct to say that on removal of a appreciable amounts of heat from a fluid vapour phase wherein the heat has been adiabatically generated as a result of an adiabatic compression, as will be the case here, then the resultant fluid could only behave as a liquid and not expand as though a vapour on depressurisation and further cooling thereby brought about, i.e. the Van der Waal bondingwould be bound to draw the fluid molecules closer together to form a liquid phase. For the simple

reason1 the fluid would not then possess the energy to expand as a vapour, which would become even less on imparting kinetic energy of fluid jet to a turbine in the pathway of the fluid jet.And especially so if the removed heat is somewhat in excess of the heat of comDression energy amount. which

could possibly be the generallthumb in relation to this aspect. If so since the compression energy input could be around 100 units and the removed heat energy around 150 units then the system should function as theorised. But to reiterate a further aspect, I in no way wish to sound absolutely certain about any of my Applied Theory on this process for the stated reasons in the introduction.However, having said that and not to unnecessarily throw too much cold sea on the process in this necessarily optimistically leaning phase, it could obviously be possible to sub-cool to as far as necessary whilst stil( maintaining the initial presure in order to ensure that the subsequent fluid behaves as though a liquid under pressure. Then it will be a question of how much energy will be yielded, which in turn Will depend upon how much P-E energy is still left remaining after the turbogenerating stage and the effect it is having on fluid fluidity in practice.

{owever, still addressing the question of whether or not the system will in fact work in practice in the way being theorised. At the compressor outlet stage the compressor will continuously be pumping out random vapour at the high pressure of say 100 ATS., which in turn will continuously be exerting a pressure of 100 ATS onto the fluid passing through the fluid creation nozzle at the entry to the sub-system turbine. Therefore as in any system of the type, some energy must potentially be yielded at the start, but the question being by how much. Will it be the normal mgh level that such a pressure would give in a cold system using a cold fluid.Or will the P-E energy in the hot fluid affect the fluid fluidity to such an extent that the same pressure exertion will now yield a higher quantity of energy by an amount corresponding with the level of additional P-E energy in the hot fluid, as basically being theorised. Then a further aspect beinswhether or not vapourisation will take place instead in the usual way, even though in theory the initial fluidity of the fluid could indeed give rise to the P-E energy becomirgharnessable by such a means.Yet a further aspect to consider beimwhether or not the fluid conraction that will take Dlaceiand the effect of this on the

or*J rdlocity linear velocity of the fluid jet,would in any case outweigh the increase in fluid jet velocity resulting from the additional P-E energy contained in the fluid jet at the start.Then to add to these doubts is the fact that such a method of operation does not 'apparently' seem to have beentried before, even though basically the same fluid circuitry has been in operation for several decades in various processes using a throttling device to dissipate away the energy of depressurisation into a latent heat vapour phase instead, coupled with the fact that the alternative of the sub-system approach is basically simple in an initial conceptual phase, albeit becoming fairly complex as one determines and evolves the various factors involved. Therefore, needless to say I must remain with doubts about the practical feasibility of the sub-system at this applied theory, pre-practical stage when 'bearing' all these aspects in mind, even after my fairly lengthy deliberations and treatment to date. While on the optimistic side stating that nonetheless the process seems feasible to me in theory, and more than this the many opposite and/or equal similarities with turbine systems on the other side of the P-E diagram of fluids in the vapour phase leads one into thinking that the technology evolved herein could well be an intended next phase giving rise to the further Ascent of Man on the Planet, starting as it does where older technology leaves off and advancing as it would some of the existing forefronts of advancing technology and applying as it could some of the more advanced science of advancing technology in various fields

of such science.Then a final aspect probably now to seriously consider in the same vein beinsthat the human race is probably now intended to be the verge of 'passing' from the Age of Pisces, i.e. of the Fish, into the AGe of Aquarius and whether the references to the closer meanins of Pisces under 538 and 641 apply under 'Roget's Thesaurus', perhaps particularly that under 641, I would not know. However, obviously the technology could prove to be a central feature of such an Age, harnessing as it potentially could the natural heat contained in the rollers of the oceans of the World and in the waters of the Earth in general, as well as that in air and of direct solar heat. Or deep below the rollers of the ocean if at depth beneath the waves, the deeper significance of which becoming more apparent.

However, having said that, the closer meanings of Aquarius under Roget's Thesaurus references 348 and 636 could in fact become fulfilled by my work under my PAs 8720291 and 8728601. But I think would become very much more fulfilled on the addition to the work of the present processes under discussion, not least the part related to the science of fluids in motion.

Therefore, having due consideration to all these potentially additional aspects, pressing on regardless to a conclusion of this early stage early phase work, potentially leading to potentially a new intended Age on the Planet, presumably pre-ordained by and therefore desired by the Powers Beyond that Be, presumably if we 'pass' from one Age into the next Age. Um. Convents which apply to everyone of course. Thus, perhaps I'm intended to be The Saviour.

On the technical front, a key at this stage to whether or not the process will be feasible in practice probably lies in the general data available on the fluorocarbon refrigerants in Weast on pages E-32 and 33, and more specifically the viscosity value for R-13 liquid compared with those of the other liquid phases of these refrigerants.Since if as assumed the value for R-13 relates to a position on the P-E diagram for R-13 close to the Critical Point of this fluid, as it must for the test to have been carried out on the liquid phase, then one can perhaps assume that this in part at least probably gives rise to the high fluidty value for this fluid compared with the lower fluidity values of fluids where the viscosity test would probably have been carried out with the state of the fluid much lower down their particular P-E diagram well into the liquid phase. If so then this to some extent may confirm that on causing the lower fluidity fluids to be closer to their Critical Points by adding P-E energy then they too would exhibit an equivalent increase in their fluidity.

And indeed this becomes confirmed by the actual values given for water and carbon tetrachloride on increasing temeprature, and indeed bv the general

equation loge viscosity neing1inversely proportional to absolute temperature.

Therefore, perhaps this aspect is still teaching grandmother to suc) < eggs.

However, my hypothesis then being that for the same fluid under the same applied pressure exertion the fluid in the higher fluidity state could yield more energy by virtue of it being able to flow faster, which it must do by very definition of fluidity. Then, that the way this energy becomes yielded is because it can deliver a Riven

of fluid to the turbine in unit time whereby and wherein each individual micro mass of the fluid makingup the full given mass of fluid can travel at a much faster velocity by virtue of being able to be drawn out further through a much smaller nozzle by virtue of possessing a much higher fluidity giving rise to the higher linear velocity being possible through a smaller nozzle.With the simple arithmetic sum of all the kinetic energies of the micro masses then simply adding up to more energy being yielded by the fluid in unit time for passage of a Riven mass of the fluid. Which is basically one view of the system of my car project entitled 'Air Power for Propulsion'. You see a low viscosity by very definition means that adjacent lavers of the fluid will shear far more easilv under

a given applied torce than1a high viscosity and theretore a Riven applied force will enable the fluid to shear more easilv when the fluid tries to

get out of the nozzle exit) envlsaglng/ln the mind's eye to be one of the micro masses inside the fluid inside the nozzle and looking forward to the light at the end of the tunnel.Now if presented with a bottle neck then the given applied force would not be able to force a given mass of fluid out in unit time and one would have to increase the size of the bottle neck to get a given mass of fluid out of the nozzle in unit time. But if the fluid had a much higher fluidity then one could reduce the size of the bottle neck and still force out the given mass of the fluid in unit time under a given applied force because that force could shear the fluid at a faster rate by definition. Indeed, in order to maintain the fluid pressure back to the compressor outlet the nozzle outlet would have to become reduced accordingly in the first place for a hotter fluid since it would then possess a higher fluidity due to its increased temperature.Therefore as one of the Riven number of identical micro masses in a given mass of fluid and in goings from nozzle exit to impellor one must have to travel faster to allow the given number of identical micro masses out in unit time than would be the case if more of the identical micro masses had to go out of the nozzle exit in parallel,l Jside by side, in unit time. And in so doing the micro masses must each impart more energy in accordance with the equation for the kinetic energy of linear forward motion of a mass KE = i mv' where it can be seen that energy is directly proportional to the square of the velocity of the forward motion of the mass. To then given a higher energy yield in total forthpassage of a given mass of fluid in unit time. IÇ in relation to this aspect one envisages an impulse turbine blade With many small impellors all around its periphery, then envisage the turbine blade to be rotating at a fast speed under the impact force of the fixed fluid jets. Then in practice one can envisage the system to be as though successive micro masses of fluid were stricking successive impellors as the turbine blade rotates.If one then took the given micro mass weight to be that of the weight of fluid striking each impellor for the higher fluidity fluid having a faster velocity fluid jet and causingthe turbine blade to rotate faster, then one can further envisage that the mass of fluid striking each impellor in the corresponding system having lower fluidity fluid, a slower jet, and causing a slower rotating turbine bladejwould be comprised of several of the micro masses of the given micro mass weight for the passage of the same total amount of fluid mass in unit time. Which would impart less energy than the same number of micro masses striking the impellor in the former system, because they would be the same number of micro masses but travelling slower.From this one can also see that the surface area of impact for this number of micro masses would be the same, even though in the latter system they would be all striking one impellor over a larger surface area of impellor, and in the former striking several successive impellors but the same surface area of impact in total.

Thus, whilst trying to find flaws with my theorising it would seem to be to be sound so far. But I could be wrong.

Envisaging this aspect of the system from inside the fluid inside the nozzle, or just standing to one side of the nozzle exit outside. Or both. One can see that if the fluidity value was actually expressed as length of fluid coming out of the nozzle exit in unit time under the given constantly applied pressure, then this would be a direct measurement of the velocity of the fluid jet, which in turn could be placed directly into the equation KE = 2mv2 to give an absolute measurement for the energy of the fluid jet in unit time based directly on the fluidity measurement, as opposed to empirical. Which should be an amount of energy that corresponds with the pressure-enthalpy content of the fluid at the start.Or at least the increase in kinetic energy resulting from an increased length of fluid in ut time, i.e. a higher fluidity expressed as above, in turn resulting from a higher fluidity fluid due to possessing more P-E energy at the start, should correspond to the increase in P-E energy. Where the difference in the actual fluid length measurement will have a squared relationship to the differences between the two energy values. It follows from the preceding discussion that for this type of treatment it would be solely dependent on the fluid length in unit time and independent of whatever the differences in the CSA of the fluid jets for further simplication.It also follows that it should then be possible to relate this more meaningful fluidity measure ment for this system to the normal value bapsed upon the force required to shear adjacent layers of fluid, and of course the ease with which the applied force is able to do this is that which gives rise to that applied force being able to force higher fluidity fluid through a smaller GSA nozzle and create a longer length of fluid in unit time for a given mass of fluid in the first place. Which in turn would be related to the Van der Waal bonding energy between adjacent layers in this type of system, which will become loosened on heating to cause the adjacent layers of fluid to shear more easily under a given applied force, i.e. to have a higher fluidity.

Thus the ease with which the applied force is able to line the fluid up into a longer, faster moving, queue will be directly related to shearing force required to do this. Of course the way in practice one would probably measure the fluid length in unit time would be very simply from the CSA measurement of the nozzle exit and the volume of fluid passing through in unit time, when the fluid length would simply be given by volume of fluid in unit time divided by the CSA of the nozzle and and the fluid jet that it creates.

Which would then give a fluidity measurement, which in fluidity terms would be very meaningful and one which could be placed directly into the equation KE = 2mv n to directly give the energy of the fluid jet, and moreover a measurement that should be easily convertible to force required to shear adjacent planes of fluid in absolute terms. Also stating that fluid length in unit timz,i.e. linear forward velocity,is a basic key to calculating for and understanding much of the work. Or to express it a different way, the speed the micro masses of a given mass have to travel at to all go from A to B in a given time. Then a given micro mass having to travel faster in going from A to B for the deliverance of a given total weight of the mass in unit weight of the mass in unit time will deliver more accompanying energy etc.

Whilst on this subject also stating that if the units of velocity are in feet per second, or length of fluid in feet per second, and the mass weight in pounds. Then the initial KE value would be in Ft Poundals persec., which then has to become divided by the force of gravity in feet per sec', i.e.

32 ft/sec', to give the energy value in Ft Pounds per second which would then be in one of the normal ways of expressing power and easily converted to KJ/sec by dividing by 737.6. Then to give in KJ/KG as expressed on the P-E diagram then it would simply be a question of how much weight of fluid was involved per second.

General Discussion Continued: To relate the shear force in absolute energy terms to the actual force of the fluid jet, or to the increase in the force of the fluid jet on increasing pressure-enthalpy content from that of the ground state it would first be a question of how much surface area of the fluid jet was becoming sheared per second. On a first consideration one may think that the reduction in shear force required.to shear the full surface area of a given length of fluid

jet woula pernaps/equate to the gain in the power of the given length of fluid jet. However, calculations indicate that this is not the case and in fact reveal that the actual absolute value for the reduction in shearing energy is very small in comparison to the gain in the power of the fluid jet.Thus, an explanation for this is as follows.

When the fluid jet becomes formed at the nozzle actual shearing of adjacent planes of the fluid only has to take place around the outside surfaces of the fluid jet, i.e., between the two fluid planes involved at the point where the mass of the fluid jet is passing through the nozzle and the restriction of the nozzle is holding back fluid all around the mass of fluid that is actually passing through the nozzle.

It follows therefore that within the mass of fluid actually passing through the nozzle there will be numerous adjacent planes of fluid in the longitudinal direction of the fluid jet that would not in fact have to undergo any shearing.

Therefore, to equate the reduction in shearing energy in absolute energy terms to the gain in the energy/power of the fluid jet, probably this would in fact be given by adding up all the reduction in shearing energy

all the adjacent planes of fluid,

in the fluid jet itself. When the total sum of the reduction in shearing energy actually between the adjacent planes within the fluid jet itself will probably directly equate to the gain in the power of the fluid jet resulting from the increased pressure-enthalpy energy content of the fluid and which is also giving rise to the reduction in shearing energy. But the actual shearing energy required to produce a fluid jet of longer length in unit time will only involve shearing just the two adjacent planes all around the outside surface of the fluid jet becoming formed and will of course involve a lesser amount of shearing energy the higher the enthalpy content in the fluid, whilst the higher the enthalpy content in the fluid the higher will be the velocity power of the fluid jet. However, one would of course expect the reduction in shearing energy as a result of the increased enthalpy content to relate in some way to the gain in the power of the fluid jet in similarly resulting from the increased enthalpy content and also resulting from the reduction in shearing energy. Or, to put it another way, gain in the fluidity of the fluid.And probably the various parameters involved

become equatable in the above manner

the fluid property 'reduction in shearing energy' resulting from the increased P.E. energy content in the fluid probably bearing a very real and meaningful relationship to the gain in the power of the fluid jet, as one would expect, but in the above manner.

In other words, the fluid property 'reduction in shearing energy' will still be present in the fluid of the fluid jet that passes through the nozzle and therefore one would expect that loss in energy value actually contained within the fluid of the fluid jet itself to directly equate to the gain in the power of the fluid jet, which it probably will. And not in fact to the reduction in shearing energy in absolute energy terms involved just on the outer surface of the fluid jet on its formation, but nonetheless the two energy values and related properties of the fluid probably being very much related in the way discussed. Thus one isn't in fact gaining a large energy advantage for lesser energy exertion, and in such a manner the energy balance will become restored.

Perhaps a partial po. allet could be drawn with a very large mass travelling through air, when the forward kinetic energy of motion of the very large mass itself could in fact bear little relationship to the actual energy that has to be placed into the very large mass to maintain its forward motion and indeed, therefore, to maintain its forward kinetic energy of motion and which could become fully exerted on impact, since the energy one has to place in only has to overcome the resistance to forward motion to replace the energy of the total forward kinetic energy of the large mass that becomes taken out by the forces acting on the large mass and resisting its forward motion as it is travelling forward.Thus, whilst one may expect the energy that one has to place into the large mass to maintain its forward motion would directly equate to the forward kinetic energy of the mass as could become experienced on impact, the two energy values in fact bear little relationship in theoretical terms and could also bear little relationship in practice as indicated by the fact that simply to streamline the large mass would reduce substantially the amount of energy that would then have to be placed into the large mass to maintain its forward motion against the resistance component of the air, but the kinetic energy of impact of the large mass would still remain the same.

Of course, to create the forward motion of the large mass in the first place then one has to place in energy that will directly equate to its energy of forward motion, which is a stage that would be analoguous to placing in the P-E energy into the mass of the system under discussion, which then remains in the mass apart from that which is taken out during the course of passing through the system. Thus one could relate the latter to repossession of energy via the internal Van der Waal forces in the fluid mass in the system under discussion, and a component of this overall general view will be the shearing energy required at the point of forming the fluid jet.When for a high P-E. energy content in the fluid the Van der Waal forces will not be able to attract adjacent molecules/planes very strongly and the required shearing energy at the point of forming the fluid jet at the nozzle will be very much reduced, but with an equal increase in the power of the fluid jet becoming formed. Which in the large mass analogy would be equivalent to continuing to place into the large mass the same arount of energy for a large mass whose resistance to forward motion has been very much reduced, when its kinetic energy of impact would then similarly become increased, i.e., in practice the large mass would increase in velocity. Which would also be the case for the fluid jet on lowering its shearing resistance energy by adding enthalpy energy for the same pressure energy exertion, in effect.

Thus, an actual fluidity measurement in absolute energy terms will relate to the increase in the power of the fluid jet in the above way, but if measured as actual linear length of fluid coming out of the nozzle in unit time then there will be a more direct relationship since one would then be measuring the velocity of the fluid jet in effect and the kinetic energy of its impact would be given by the equation KE = MVZ. For example, as when the energy value for a potential head, i.e., mgh, becomes equated to the above equation in order to determine the velocity of the water jet and thereby the nozzle CSA dimension required in hydropower harnessing via a Pelton Wheel.In such a case the mgh energy becomes converted into the 2MV2 energy of a water jet and the actual velocity of the water jet is given by:

However, in the system under discussion and in the context currently being discussed the velocity of the fluid jet is simply becoming determined in a different manner since one cannot equate to just the equivalent of the mgh value for the hot fluid. Therefore in some way one will have to equate to the equivalent of the mgh value for the system, as one could equate to for the cold fluid at ground state, plus the additional heat energy in the fluid bove ground state.Where ground state for the system in this context could perhaps be defined as the state at which the equivalent of the mgh value for the system does equal the 12MV2 energy value becoming obtained, which in turn would give the ground state fluid jet velocity.

Thus, under the conditions of increased heat content in the fluid above that which will give rise to the above relationship then another approach will have to be adopted to the determination of the velocity of the fluid jet, which in modern approaches to the fluid flow may become determined in some other way, but herein I am basing on a very simplified approach via fluidity measurement.

No doubt more complex and definitive treatmentsvill become carried out in subsequent years to come should the system get past first base and progress further. One only has to glance through the text book 'The Liquid State' by Dr. J.A. Pryce, 1966, Senior Lecturer in Physics at the Sir John Cass College, London, to see how complex future treatment on the system being discussed could

become. whereintte/states that advances in the study or the liquid state nave really only been made in the last thirty years in contrast to similar definitive treatment on gases and solids, and that his treatment of the subject matter is but a simplified version.

Probably the reason why advances in such theory have tended to lag behind the theory of solids and gases is because no large scale practical basis of a central core nature has been in operation hitherto.

However, obviously such theory could potentially become one of the main areas for the theoretical

understanding and treatment of matter in the future should the system under discussior and the processes that it could give rise to come to pass, to supersede and extend upon such work on gases and solids. Which would also be in keeping with my view that such work could become the foundation for a whole new start in central core science and technology. However, at this early stage, and not to be daunted, I will continue on with my very early days approach in comparison since I think that I am meant to try to convey the concept of the system in as simplified a manner as possible. Therefore, whilst apologising to such people as Dr. Pryde, I will continue on with my very early days treatment aimed at trying to convey the concept, during the course of which hopefully arriving reasonably close to possibly better approaches to the system. Or at least to better starting points for its practical development. Which are really comments that apply to the whole of the work that I have undertaken and now commencing to put forward as possible areas for progress in science and technology in the future aimed at the betterment of our civilisation here on the planet. Which covers a very broad spectrum and therefore can only be dealt with by me in a very general manner at this stage.

Having said that, the earlier emperical treatment requires to be more definitive even from the point of view of the initial determination of trying to see whether or not the concept would in fact be feasible in practice in the first place.

Therefore to recap. At that initial stage in my evolution of the concept I simply took the view that if the cold fluid gave a certain fluidity value and the hot fluid gave 4.5 times the value then this in practice would mean that the hot fluid flow exiting from the base of the test equipment of the type employed in paper fluidity testing would be doing so at a 4.5 times faster rate for equipment of the same dimensions and therefore the respective kinetic energies of the two fluid flows would be in the ratio of 4.52 times for the flow of a given mass of fluid, in accordance with the equation KE = eMV2. Which would then be a factor that could become related to the absolute energy value that one might expect to obtain from the cold fluid simply due to the mgh energy value of the system.For 1KG of cold fluid this being calculated as: mgh = 1 x 33.9 x 100 Ftlbs per lb of fluid = 3390 Ftlbs per 1b of fluid = 10 KJ per KG of fluid For fluid under a vapour pressure head of 100 ATS.

Then if: 10 KJ/KG = 12MVZ in which the velocity is one unit of velocity the corresponding 21 MV2 value in which the velocity is 4.5 times would be in the ratio of 1 to 20 times i.e., 200 KJ/KG. Where one unit of velocity could be regarded as the fluid jet velocity that becomes obtained from the fluid in the ground state when just the mgh energy value becomes obtained from the pressure head to which the fluid is externally being subjected.

Thus,in Sls very simple manner I endeavoured to explain a simple view of the system based upon a consideration of the effect of the P-E energy acting on and in the fluid on the fluidity property of the fluid and how the effect could indeed result in it being likely that the energy equivalent of at least a substantial proportion of the P-E energy to which the fluid in total was being subjected to both internally and externally could additionally be obtained on suitablv harnessing via a normal mgh energy harnessing method over

and above the normal/level or mgh energy tar a given applied pressure head, i.e., the external component of the P-E energy to which the fluid is being subjected, and which one might expect to obtain via the cold fluid containing none of the internal heat energy component, and because it contains none of the latter. The internal heat energy component giving rise to the increased fluidity of the fluid, which then in turn gives rise to the increased fluid flow rate under the given, i.e., the same, externally applied pressure head component.

Thus, perhaps it could be generally said that the cold fluid is the ground state, and that the ground state is in turn a state of the fluid in which the internal Van der Waal bonding energy has fully repossessed all the P-E content of the fluid. Or in the case of a fluid already in the cold ground state already has full possession of the pressure-enthalpy content in the fluid, and the fluid simply behaves as a mass on harnessing the pressure head via a normal method, with none of the enthalpy energy,.i.e., heat energy, that it contains in such a ground state becoming transferred nor indeed is transferrable.

In which case then from such a standpoint the reverse could be stated, i.e., the energy acting on and in the fluid only becomes reduced to the pressure component of the pressure-enthalpy of the fluid because none of the enthalpy content-of the fluid, at the ground state does, nor can, become transferred.

Which in practical terms would mean that it would not also become reduced in temperature on harnessing the pressure head energy. Or does it? - In normal hydropower harnessing. However, since water the fluid in such a system is only a few degrees of heat above its solid state then probably the internal Van der Waal bonding therein, also comprised of strong hydrogen bonding, has full possession of all the kinetic energy, i.e., heat energy, in the fluid. Nonetheless, perhaps some lowering of temperature is noted in such systems, perhaps particularly those involving the actual creation of fluid jets in combination with the Pelton Wheel type of turbine.Whilst in contrast when water mass simply tumbles through a normal axial turbine type no streamlining of the kinetic energy content could take place and, therefore, in such a system one would expect the

fluid to behavesimply as a mass, wherein the molecules one to another neither shear under the applied pressure head nor become aligned but remain in random motion in all directions. Thus in such a system one would expect the level of energy obtained to simply equate to the mgh energy value of the pressure head, with no accoitipanying transferrence of heat energy.Or to put another way one would expect the velocity of the water flow to simple equate to the mgh energy value of the system as follows:

When for the system under discussion the parameter (2gh) will equate to the pressure head as comprised of a high random vapour pressure continuously acting on the liquid phase

Thus, under such conditions the energy obtained will simply be that which corresponds to the externally applied pressure head component of the total pressure-enthalpy to which the fluid is being subjected. Furthermore, I think I'm correct in thinking that in hydropower harnessing the same energy amount would be expected to be obtained from the potential head of water via the method of the formation of fluid jets which then impact onto a Pelton Wheel, as via the method of more simply flowing the water through an axial type of turbine.In which case then one wouldn't expect any more accompanying temperature loss in the former method, and if there is no temperature loss via either method then one must simply be harnessing the mgh potential energy of the fluid water pressure head in both cases, which I think is found to be so in practice.

Now add heat energy to the fluid to a temperature well above the defined ground state of the fluid and the Van der Waal bonding holding the molecules of the fluid together in very nearly a solid state will become very much loosened and will shear under the given applied pressure, and will also be very much more alignable all into the forward direction. However, it may be important to discern the difference between these two facets of the fluid, since simply the fact that planes of the fluid will shear at a faster rate under a given applied pressure will alone probably give rise to the basic level of energy increase, whilst to also align the molecules into among streamlined state could give rise to bonus energy over and above the expected basic level from the increase in fluidity of the liquid, as will be elucidated upon followIng.

Thus on adding heat energy to the fluid the fluidity of the liquid compared with that in its ground state will increase and result in a corresponding increase in the velocity of fluid flow under a given applied pressure, the external component of the total energy to which the liquid is now becoming subiected. And, therefore, it could be stated that the velocity, v, will now be given by:

v =ts/(2gh equiv.), i.e., the defined ground state velocity of the fluid flow under a given applied Pressure) + (the difference that adding heat energy makes to the fluid flow velocity under the given applied pressure).Under such conditions then the bonds holding planes of molecules together will give way far easier under the shearing effect of a given applied force at the nozzle and would go through the nozzle aperture at a very much faster rate under the given applied force, and in turn, the force of the fluid jet created will consequently have a higher kinetic energy of impact. If the fluid jet velocity increases by 4.5 times in terms of its linear forward velocity as it should if its fluidity value is 4.5 times then its kinetic energy of impact will increase by 20 times in accordance with the energy equation for any mass travelling at speed, i.e., KE = 2iM\72. Thus the effect of the added heat energy already and thereby having become converted into harnessable kinetic energy of the forward motion of mass.With then any bonus energy one could potentially add resulting from any extra streamlining that one may be able to induce into the streamlining fluid jet. However

be a case of trying to achieve the potential maximum for the pressure head and hot fluid via correct shaping of streamlining nozzle in the first place as well as subsequently when one tries to add partial vacuum energy.

However, this is getting ahead of the current discussion somewhat and firstly at this stage I am considering the situation of just forming the hot fluid jet to the normal level of streamlining, associated with lATS. pressure on the other side of the fluid jet creating nozzle under the pressure head on the entry side to the nozzle. When the mass flow rate

remain at unity and be the same as for the cold fluid in order for the pressure head to be maintained but each micro mass within that mass of fluid passing through anecessJly smaller nozzle CSA will be travelling at 4.5 times faster speed due to the lower shearing energy between molecular planes of the fluid and be at the normal level of streamlining associated with lATS. external pressure.Thus there are reallv two differences comPared with the situation of the cold fluid

taking place simultaneously. un tne one nana tne pressure neaa1aDle to force the same mass of fluid throuqh a smaller CSA in a given time due to the lower

shearing energy property of the hot fluid, and additionally the tluid1atle to become more streamlined into the forward vector again because of the looser Van der Waal bonding between molecules. However, probably the two would be fully combined effects down to the normal level of shearing and streamlining of the hot fluid associated with lATS. external Pressure.With the maximum velocity increase to the normal level becoming the factor of 4.5 times compared with the cold fluid when involving a combination of the lower shearing and fully associated higher streamlining effects. But perhaps there would be some small scope for inducing further streamlining into the mass flow rate under a given pressure head via means of appropriate nozzle entry shaping to forward align the fluid molecules better than they would normally do when undergoing the shearing process.To then induce an even longer and thinner length of fluid for a given mass flow rate in unit time, which then comprised micro massatravelling at a slightly faster speed than the normal 4.5 times. ? However, just considering the situation of the fluid jet speed becoming 4.5 times faster due to the heat in the fluid lowering the shearing energy between planes of the fluid which then gives a fluid jetofsome 20 times more initial kinetic energy value than the equivalent cold fluid jet.This in fact is a stage where

explaining is required and indeed where some addition to the over simplified view of the emperical treatment is required, before discussing additional streamlining effects, which really could be regarded as having pointed in the right direction although later treatment seems to confirm that the early approach could perhaps become an accurate way to approach the system. However, in preceding discussion close to the beginning of this particular part of the discussion aimed at trying to further determine whether or not the system would be successful in practice I deliberately left out of the description at that stage the fact that the fluid will expand on heating, which may have added to the confusion of the micro mass description at that point in view of past thinking on this system.However, the effect of

the heat will of course1re to expand fluid as the molecules thereof become forced further apart under the effect of the heat and take up positions of higher intermolecular distances between molecules. Thus in the initial state of the fluid there will be less mass in one of the unit volumes of fluid, or conversely I mass of fluid in the hot fluid state will occupy 2.5 unit volumes in accordance with the difference in densities between hot and cold fluid. Which in this System,in contrast to vapour system,on impact with the impellors of a turbine will progressively become a volume wherein will become the closer packed mass as exists in the cold fluid on subsequent harnessing of the kinetic energy of the fluid jet, giving rise to cooling, giving rise to fluid contraction.Thus here can be envisaged the concept of the internal Van der Waal forces repossessing the energy of the mass, which would mean drawing in the loosened molecules into a smaller space and restricting their individual motion until they become as the cold state once more closer to their solid state. However, at the start the effect of the heat energy content in the fluid will not only be to reduce the shearing energy between adjacent planes and thereby increase upon the fluidity of the fluid, but the new loosened Van der Waal bondinq

reiationsnip Between molecules Will De sucn tnat tneylexlst rurtner apart from one another in the energy equilibrium of the fluid state, which of course is an aspect fully interrelated with the lowering shearing energy requirement between

within the fluid. With the molecules then progressively becoming closer together on fluid cooling and contraction of the mass whose kinetic energy of impact is becoming harnessed until they once again occupy the space they occupy at ground state temperature and pressure, which in turn will progressively subtract from the actual kinetic energy of impact that the fluid jet can impart of its initial kinetic energy of forward motion on the initial creation of the fluid jet, when the kinetic energy of forward motion will arise from both the pressure head acting externally on the fluid and the extra of the heat energy acting internally in the fluid to lower the shearing energy requirement between adjacent planes in the fluid.Albeit probably very rapidly subtracting from the energy as a pulling of the punch of impact effect.

Thus in many respects if not in every respect the system is different from the harnessingofthe P-E energy content of a vapour in an equal but opposite manner, wherein the P-E energy content of the vapour subsequently becomes harnessed via expansion of the fluid from a smaller volume to the larger volume

the vapour phase will exist at1normal temperature and pressure albeit toe

initial smaiier voiume pernaps/larger tnan tne starting large voiume or tne fluid in the liquid phase, although not necessarily.However, I have already deliberated over this comparison and therefore I will not do so again here but obviously it is an aspect of the system that one could go very deep into and no doubt some people will in the decades of the development of the technology should it ever reach such a stage.

Thus the fluid will also expandj which is an aspect that will have to be incorporated intotheviews of the system to date based solely on a consideration of the effect of the heat energy on the fluidity parameter of the fluid. In fact effect on the volume. parameter could have been a different starting point from which to commence considering the system. However, deliberations from the two different starting points would eventually merge and indeed the increase in fluid volume is desirable to meet the demand of the system that the increase in fluid jet velocity is required to be achieved for the same mass flow rate in unit time, without which this necessary criteria may not in fact be as achievable.Thus, it follows that this is an important aspect of the system to be aware of and to fully understand at this stage, but fortunately the fact that the fluid volume expands should render the system more easily achievable in practice.

Therefore, at this stage more fully discussing the effect of the heat energy also on the volume parameter of the fluid and how this will interrelate with the fluidity parameter. Which I will firstly do in the context of the preceding description in which fluid arrives at the nozzle for formation into a fluid jet, which to some extent will have to become added to on taking effect on volume into consideration since the discussion at that stage was based solely on a consideration of fluids of the same volume at the start and solely related to the fluidity variable of the fluid and s therefore, strictly as such would apply to fluids whose fluidity property alone is varying, as for example results from fluidity tests on paper where the mass per unit of volume is the same for fluids but where the fluids can vary vastly in their resultant fluidity property. This being in accordance with the viscosity equation: Viscosity = n(P1 - P2) r4t 8 V1 In which all the parameters will be constant for the same test equipment apart from time, t, for a given volume of flow. Therefore taking the reciprocal of the equation then: Fluidity = 8vl 4 z (P1- P2) r4t Fluidity = Constant t Wherein time to flow, t, is the only variable.

Or conversely for a given time of flow then fluid volume flow length would vary.

However, the micromass descriptionlat that stage will still apply to the air system under patent 2126963B 'Air power for propulsion' since in that system the volume of the air per unit of mass would remain the same when comparing a none-channelled system from front to rear with the system described in the patent. Moreover, the description up to that stage will still apply to the system under discussion, but with respect to a consideration of the fluidity parameter in isolation from incorporating into the description the accompanying effect of the heat energy on increasing the volume of the fluid.

There could in fact be a number of starting points from which one may try to consider the system, from a consideration of the faster moving molecules that will be present in the hot fluid which one may consider could become all aligned into the forward vector on formation of a fluid jet to thereby create a faster moving fluid jet of higher forward kinetic energy by an amount corresponding with the increased heat energy in the fluid. To views based on a consideration of the higher intermolecular distances between the molecules at higher temperature which then could become aligned into a longer fluid length on formation of the fluid jet. All the way through to a consideration of the effect on the fluidity parameter of the fluid, which could well be the last starting point that one would start considerations.However, whilst the first two views will apply to some extent, the former in particular when considering the addition of bonus energy from fluid streamlining and the latter when considering the basic length of fluid jet in unit time, it will in fact be the effect on the fluidity parameter that will be the central parameter of the system to consider both when considering the basic length of fluid jet attainable in unit time which will arise from the rate at which planes of the fluid will shear under a given applied pressure, and then when considering how easily the fluid molecules will further streamline all into the forward vector to give bonus energy.But having said that, it is necessary to consider the other two views in interrelation with the fluidity view, with the main one to consider at this stage being the volume view and in particular in the context of the micromass description.

Very simply it will mean that when the fluid arrives at the nozzle, either each microvolume will contain less mass or conversely a unit of micromass will occupy more volume. For the first part of this further description at least it is probably better to envisage the former view. Within each microvolume of the hot fluid there will be around 212 times less mass and therefore for one full unit of micromass 221 units of the microvolumes would have to pass along the fluid jet creating nozzle compared with one unit of microvolume containing one full unit of micro mass in the case of the cold fluid at ground state.Therefore, if the nozzle is the same CSA dimension in each case then for the same mass flow ratesand simply

od,2 ro to- LiolursjrSerence in the fluidsgthe fluid jet becoming formed from the hot fluid would be 212 times longer in unit time and if one then considers micro micromasses within the microvolumes then each micro micromass would be travelling 212 times faster in the hot fluid between exit from the nozzle and the impellors of the turbine.

Giving rise to 2.52 increase in kinetic energy compared with the base level of kinetic energy becoming produced via the cold fluid jet. However, for a hot fluid whose fluidity increases by 4.5 times then for the same sized equipment and in particular nozzle CSA the fluid jet would be 4.5 times faster in unit time for the same pressure head, in accordance with the viscosity equation:- 4 Viscosity = g ( P1 - P2) r t SVl Or for fluidity the reciprocal:: Fluidity = 8V1 err (P1-P2) r4t Wherein the volume parameter, v, will simply relate to a given volume of fluid regardless of how much fluid mass it actually contains for the comparison being carried out, i.e., that between cold and hot fluid where the fluidity of the latter becomes increased by 4.5 times on adding the heat and increasing temperature, with mean fluid velocity being given by the respective different fluid volumes divided by the same nozzle CSA.

In other words, relating to the fluid volume parameter, v, in the above equation, 4.5 micro volumes would pass along the nozzle in unit time, t, compared with one microvolume in the case of the cold fluid for the same pressure head, P1. But if 4.5 microvolumes are exiting from the nozzle in the case of the hot fluid then 1.8 full micromass units would be exiting in unit time and the pressure head would not be maintained, as can be gathered from a consideration of 1 full inicromass passing through the nozzle inside 21 microvolumes all in a row in series in the case of the hot fluid. Therefore inside 42 microvolumes passing through the nozzle there will be 1.8 units of the full micromasses, compared with 1 full micromass inside just one of the microvolumes in the case of the cold fluid at ground state, when the pressure would be maintained.

However, the pressure would still be maintained in the hot fluid system if the micromass flow rate can be reduced to one in unit time and the required kinetic energy of impact of 20 times would still be obtained if the velocity of that micromass is 4.5 times from nozzle to impellors.

Therefore firstly envisage the state of the fluid jet exiting from the nozzle of the same sized CSA when because the fluid has a 4.5 times higher fluidity it will be exiting from the nozzle at 4.5 times faster rate and the pressure head will be becoming lost. Now look at the fluid jet head on and reduce the CSA dimension of the nozzle until the pressure head is being maintained which will be at the point at which the mass flow rate becomes back at unity.

Thus one has reduced the CSA of the nozzle to achieve the mass flow rate of unity,

but now look at the side of the fluid jet and one can , that

travelling at 4.5 times faster speed from nozzle exit to impellor. In effect

simply blanked off apart of the mass flow rate in order to reduce to unity, with everything else remaining the same including the forward velocity of the fluid jet, or length of fluid jet coming out of the nozzle in unit time.In other words, each micro micromass in the initial fluid jet would initially be travelling with a 4.5 times faster velocity (until the pressure fell off) and therefore those that didnot become blanked off as one reduces the CSA nozzle dimension to cut the mass flow rate to unity

still be travelling at the 4.5 times faster speed. The sum of their kinetic energies of impact then being .52 times more. This aspect can be further understood if one considers the pressure exertion per micro unit area acting on the fluid and forcing it through the nozzle, which in the case of the larger nozzle would fall off because the mass flow would be too high.However, assuming we are at the beginning before the pressure falls off, then on reducing the nozzle CSA to achieve a mass flow rate of unity the pressure would thereby be maintained and the pressure exertion per micro unit area acting on the fluid and forcing it through the nozzle will still be the same as for the larger nozzle before the pressure began to fall off. Therefore the fluid passing through the reduced nozzle could still be doing so at the same linear flow rate speed as for the larger nozzle before the pressure fall off, i.e., at the linear flow rate speed of 4.5 times faster than the cold fluid.However,

the mass flow rate would have become reduced to unity and in

cassette pressure head would be maintained and therefore the fluid would continue to be forced through the smaller nozzle at the same linear flow rate speed of 4.5 times faster than the cold fluid, whilst in the case of the larger nozzle then the pressure would fall off and the linear flow rate speed would reduce by a prorata amount in accordance with the equation, to a point when the mass flow rate became unity in such a way. But of course then each micromass unit in the fluid would then also be travelling at pro rata slower speed and the resultant kinetic energy of impact of the fluid jet for the flow of mass unity would be correspondingly less.However, by simply reducing the nozzle CSA by a factor of 1.8, i.e., almost by half, for the system of the hot fluid then one could be achieving a mass flow rate of one in unit time, and a fluid jet velocity sti(l at the 4.5 times faster linear flow rate speed and possessing a kinetic energy of impact some 20 times higher than the same system based upon cold fluid at ground state and in this case necessarily having to use a nozzle which is 1.8 in its CSA dimension to maintain the pressure head, which will solely depend upon the mass flow rate being maintained constant at unity in the manner described.

8V1 Fluidity = Tr (P-P2)r4t Firstly considering the initial system before reduction of the GSA nozzle dimension. At that stage the fluidity value on the LHS will be 4.5 times more for the hot fluid and all the equipment dimensions would be constant where 1 would be the length of the nozzle and r the radius of its GSA. Now if considering one unit of time then the variable would be volume of fluid, V, passing through the nozzle in the unit of time. Which would be 4.5 times more for the hot fluid that has a 4.5 times higher fluidity value. Remember that of this 4.5 times faster volume flow the accompanying effect of the heat on the fluid volume parameter will account for 2.5 times more volume of fluid flow in the unit of time within which there would be 1 unit of mass.However, adding here that whilst the fluid volume has increased to be 2.5 times larger volume itzo,vIS still be the lower shearing energy property in the fluid thatwou enable the pressure head to force the larger volume of fluid through the nozzle with a linear flow rate speed of 4.5 times faster than the linear speed at which the same pressure head could force the cold fluid through its nozzle of appropriate GSA dimension to maintain the mass flow rate at unity and thereby the pressure head.However, whilst in the case of the hot fluid the linear flow rate speed of the fluid will be 4.5 times faster under the same pressure head, the effect of the increase in the initial volume of the fluid to 2.5 times larger for 1 unit mass of fluid will mean that the initial mass flow rate for a nozzle the same size as required for the cold fluid would only be 1.8 times more than unity which will be advantageous since the required reduction in the nozzle GSA would only be 1.8 times less, whilst if the densities of the fluids remained the same then the reduction would have to be by 4.5 times to maintain the mass flow rate at unity in the case of the hot fluid, which could then create more fluid to wall friction problems.Although this-could be a minimal aspect of the system with good fluid streamlining on entry to the nozzle, but would obviously become improved the less the required reduction in the nozzle CSA. However, it is an aspect that would have to be considered and allowed for, but here I am assuming that a good boundary layer could become created between the fluid flow

and the internal walls or the nozzle to minimise upon fluid to wally consiaerations and simply considering the other, main mechanics of the fluid flow in isolation from such effects on the system, which will be valid but then on adding fluid to wall friction effects as the fluid flows through the nozzle the effectCoLA\2 be to slow down the fluid flow by perhaps some 10% from the theoretical maximum under consideration here, and therefore in practice it would simply be a question of arranging the pre-conditions of the system such as to give a theoretical fluid jet velocity some 10% higher than desired in order that on flow through the nozzle the fluid jet would then exit at the actually desired velocity.

Thus I take the view that it is simpler to consider this aspect of the fluid flow mechanics as a separate entity in such a way, rather than trying to incorporate into the basic mechanics of the system. Therefore, returning to the main thread of the discussion here.

Thus the effect of the increase in the initial volume of the fluid per unit mass of fluid will mean that on reducing to nozzle GSA by 1.8 times compared with that required for the cold fluid to give a mass flow rate of unity, the actual volume of fluid flowing through the nozzle in unit time would become reduced by a corresponding amount, i.e., by 1.8 times from 4.5 units of volume

to 2.5 units of volume which would contain 1 mass unit andlstill be flowing at a 4.5 times faster linear flow speed than would the cold fluid through the necessarily larger nozzle GSA. Whilst if the density hadn't changed then the volume flow rate would have had to be reduced down to 4.5 times less for the hot fluid in order to maintain the mass flow rate at unity.

Therefore relating these changes to the fluidity equation. The fluidity value on the LHS will still be 4.5, but the volume, V, parameter on the RHS will be reduced by 1.8 times whilst the length of the nozzle, 1, and the pressure head P, will be the same, and time, t, will be unity. Therefore the reduction one makes to the radius, r, of the GSA nozzle would have to be such that the reduced, V, parameter divided by the reduced r4 parameter would remain the same in practice. Therefore, examining this aspect further as follows.

The basic equation relating the various parameters is given by: Fluidity = ~ 8V1 Tr(Pl - P2) r4t The lowering of the volume, V, parameter from the level associated with V=4.5 to that of V=2.5 will in fact in practice be associated with an r2 change from the larger r2 parameter of the larger nozzle GSA associated with the larger volume being represented by V=4.5 to the lower r2 parameter associated with the smaller nozzle GSA of the smaller volume represented by V=2.5, for a volume of fluid in which the length, 1, parameter is constant, which here I am regarding as a nozzle of constant length. This can be gathered from a consideration of the fact that volume, V, will then be given by Irr2 x 1.Therefore, with just these changes in mind one may hope that itwasv divided by r2 that was present in the equation since in practice on reducing the volume parameter from V=4.5 to V=2.5 the actual associated change in the radiuS parameter would be in the ratio of the respective r2 parameters. Therefore for all other parameters constant it would have to be the ratio V to r2 that maintained the constancy of the pre determined fluidity value on the LHS of the equation for the respective systems.Therefore, for the parameter relationship to give the same predetermined fluidity value on the LHS of the equation on changing from V=4.5 to V=2.5 then some other accompanying parameter changes would have to take place, which would have to boil down to V divided by r4 in practice and not V divided by r2 if one assumed the same values for the other parameters of the equation.

However, having deliberated thus over the system it will not in fact be correct to conclude that the fluid jet velocity would remain the same on reduction of the nozzle GSA because of the r4 relationship with volume flow in the basic fluidity equation, although there are aspects of the system that could render the former more possible. Therefore, I return to this aspect of the system after first discussing a method of operation of the system whereby it may not in fact be necessary to reduce the nozzle GSA to less than that which would be required for the cold fluid state. When the fluid jet velocity would not then need to become subject to the r4factor.

Thus, adding to the discussion at this point a potentially possible technique that has occurred to me during the course of deliberating over the foregoing aspects which may become useful to apply in the development of the system at some stage in the future, and which also seems to have some further equal and opposite similarity with existinq vapour svstems to PerhaPs indicate

that it may be a soundltechnique that could become useful.e} or further example, if for some reason one wished a fluid flow exiting from the nozzle of mass flow rate hiqher than unity which Perceivablv mav be desired in

future systems in order to thereby lower fluid to nozzle/CSA would otherwise have to be very small.On the other hand, the technique may not be feasible and, therefore, perhaps an apt analogy to draw

would be unwanted fluid friction against nozzle walls but nonetheless hopefully able to put up with a little. The anologuous friction here being how can one operate the system with more fluid flowing out of the nozzle than the compressor is pumping into the fluid flow at the other end of the system.

Supposing that for the hot fluid system of 4.5 times higher fluidity in the system under discussing one left the nozzle CSA dimension the same as one would apply for the cold fluid. Then if sustained in some way the mass flow would be of the order of 1.8 times too high in terms of the fluid mass coming out of the nozzle exit in unit time. Not because of a faster jet,

which would still bet4.5 times taster than the cold flUid in the same system, but because more parallel streamlines of the fluid would be exiting from the larger CSA nozzle in unit time.Although if the mass flow was not becoming sustained then the system would very quickly start to lose pressure and come to a new steady state in which the balance of pressure and fluid volume flow ratebecarneunity with respect to the fluid mass becoming pumped into the fluid flow by the compressor. Which can be gathered from a consideration of the basic fluidity equation, i.e., as the pressure falls off so the volume flow rate will decrease proportionately toanew steady state in which the mass flow rate becomes unity, and in which the balance of the equation becomes such as to still maintain the same fluidity value on the LHS of the equation. Thus as volume flow rate falls off so the fluid jet velocity will also fall off in still flowing through a nozzle of the same CSA.If one considers this aspect of the system in the context of the classic experiment of a barrel of water with holes at different heights through which the water would then be flowing under pressure heads of difference mgh value with the lowest flow exiting the fastest and the highest the slowest, then one can envisage part of the situation here as being similar.

Thus, under conditions of not sustaining the mass flow rate required for the larger nozzle CSA for the maintenance of the pressure head, whilst a new steady state would be arrived at where the mass flow rate became unity with respect to the output from the compressor, the micro-mass velocity would not then be the required 4.5 times faster as one full unit of fluid mass streams across to the turbine, cornprising as it would a higher proportion of the micromass in parallel rather than in series. Thus, on a consideration of the latter aspect one can envisage why in the future it may become desired to have nozzle system producing very long and thin fluid jets in unit time.

which obviously would require very accurate, straight, true and very smooth nozzle bores, perhaps in combination with an electro technique to induce an

effect, but which perhaps couldn't be achieved at today's level of progress and in any case would be systems of the future that may evolve out of the coarser systems that one would commence off with at the beginning of the technology, perhaps based upon R-21.

Thus the above would probably be the situation if one left the nozzle CSA at that required for the cold fluid and of the order of 1.8 times larger than that required for the hot fluid system. Although all sorts of other difficulties would probably become created on the lowering of pressure, for example, depending on the new temperature and pressure balance some fluid vapourisation could take place.However, supposing that one could maintain the pressure in some way then the fluid jet velocity would be maintained at the desired 4.5 times faster velocity and because the mass flow rate in unit time would be 1.8 times higher then one would in fact be producing 1.8 times more turbine energy in unit time

Now if at a normal level of operation the system would be just self-sustaining the compressor then one would be obtaining a surplus of energy in relation to the normal energy requirement of the compressor by the factor of 1.8 times to give 0.8 units of surplus energy in unit time, which therefore could become recycled to maintain the pressure to the rear of the nozzle back to the compressor in some way.

Perhaps in one way this could become achievable by placing some pistons along the side of the fluid flow from compressor outlet to the sub-system as required and facing into the fluid flow at right angles to the flow or angled into the direction of fluid flow as may be found desirable. Which when operated via the surplus 0.8 units of energy they had the effect of reducing the subsequent volume of fluid flow in such a way as to maintain the fluid pressure in the flow system from compressor to the nozzle of the sub-system.

Which however could only be a part of a way if at all since one would still be left with the main problem of 1.8 units of fluid mass leaving the nozzle exit for every 1 unit of mass becoming placed into the fluid flow by the compressor.

obviously the way would be to simply keep recycling the surplus liquid associated with the surplus energy via feeding the appropriate proportion from the liquid phase on the exhaust side of the subsystem directly back into the fluid flow at some point.Which would have to be after the removal of heat stage in the fluid flow circuit and obviously the liquid fluid would have to be placed back into the fluid flow at the same pressure and temperature of the fluid in the fluid flow prior to passing through the subsystem but after the heat removal stage. And obviously

the 0.8 units of surplus energy would be required to be used forXheatlng the fluid and for placing it back into the fluid flow

Such a method of operation wouldlposess some equal and opposite similarity with the normal refrigeration cycle based upon a refrigerant in which the vapour phase that becomes produced when the fluid thereof passes through the normal throttling device of such a process is recycled back directly into the compressor inlet, in contrast and in equal and opposite similarity.

Rather than being a part of the liquid phase that goes on to absorb heat and re-vapourise before then passing onto the compressor inlet.

alternatively in the process under discussion all the liquid phase after the sub-system could pass through a heat absorber of a correspondingly larger capacity with the larger amount of vapourised phase then passing onto a larger capacity compressor which would then be pumping fluid into the beginning of the fluid flow circuit by a correspondingly larger amount and at unity once again with that exiting from the larger nozzle.

All of which then simply amounting to a larger capacity process, and with all the energy being produced by the turbine of the sub-system then being required to sustain the larger capacity compressor.

there could be some advantage in operating such a system via the preceding method. Not least because it may be another route to bonus energy, since the energy required to place a proportionofthe liquid phase back into the fluid flow circuit after the heat removal staqe in the same fluid state could be less than the energy it produces, albeit at

15un11 However, some other heat energy may be available on site which may otherwise be wasted and which could become incorporated and harnessed in this way.

Moreover, one can envisage that it may prove possible to inject the recycled fluid in a streamlined manner by first pressurising to the required random pressure then entering the main fluid through streamlining nozzles inset into the sides of main fluid flow pipe, which if aimed at the nozzle entrance could conceivably aive a pressure boost since for this fraction of the fluid

it could be aireaayjpoiarisea into a ntgh toward dynamic pressure and a low static pressure, especially if in the liquid-vapour state, whilst the mass volume of the fluid would still be that required to maintain the pressure, but in a localised manner it may be an added technique that would give a higher effective pressure acting on other fluid actually entering the nozzle.

Such a technique would in fact havel~equal and opposite similarity with the main system of the IanclAB Process, Patent No. 2141179, and a further similarity with the Advanced version would be the concept of recycling a portion of the energy solely to render operable, which in the

achieved via the SE System of the work in further equal and opposite contrast.

However, perhaps the main equal and opposite similarity with the Advanced version will be that for that process the SE System would be essential, whilst for the main process herein the technique under discussion may not be as essentially required. Although a further more common usage could well be found in the area of relatively very small capacity processes where the nozzle bore requirement would otherwise be too small, e.g., in the harnessing of garden ground heat for example which could perhaps yield sufficient power for a house but where one couldn't go to a higher capacity process because there wouldn't be any further heat source. Or at least sufficient to keep the electric battery scooter running, etc. For collection of this order of small amounts of heat from the ground I refer readers to work by J.R.

Coulburn and J. Fearon of the Dept. of Mech. and Ind. Engineering, Queens University, Ashby Inst., Belfast, and to their paper 'Deep Ground Coil Evaporators for Heat Pumps', 1978.

reason why such a technique may become desirable to apply lies in the fluidity equation: Fluidity = 8V1 lr ( P1-P2 ) r4t From this equation it couldbeconcluded that if strictly applicable to the System in its present form then on reduction of the fluid volume from 4.5 units to 2.5 units, i.e., as required in order to establish a fluid flow of mass unity with respect to the compressor output, then the fluid jet velocity

local Icl notin fact remain at the 4.5 times faster velocity and as required to give the potential maximum energy yield. Although in the early micromass description I stated this could

be the case. However, this is an aspect thatWould be wrong since this would require the volume flow to be proportional to r2 and not to r4.Therefore, if the fluidity equation strictly applies without modification then the fluid jet velocity could become reduced as follows: V1 2.51 rl4 x 1 2.51 r1 x V2 4.52 4 r2 .328-for 1.8 CSA x = 0.182 r = .65 Therefore CSA = 1.327 Therefore fluid jet velocity could become reduced from the 4.5 times faster to 3.4 times faster.

At this pre practical stage perhaps even knowledgeable experts such as

Author or tne text book fluid Mechanics l.e.;lFranx M. wnite, Irir, COuldnC sav what the relationshis is likelv to be for this specific svstem. Which

is really { removed from the type of fluid flow that the basic fluidity equation is said to apply to, i.e., as for example becomes described under the text book 'Elementary Rheology' by G.W. Scott Blair, 1969, on page 14

to 15, wherein the r4 relationship lsl assoclatee with cold fluid flows flowing through long narrow straight cylindrical glass tubes. Which under Professor White's book becomes described as a parabolic flow, to which the basic fluidity equation in fact strictly applies and refers to the velocity distribution from a maximum along the central axis to in fact stationary fluid flow in contact with the glass walls.

Thus the system under discussion could be more towards an r2 relationship for a number of reasons. Firstly the fluid would be hot and could be close to its liquid-vapour state. Secondly it would be accelerating through the nozzle to a maximum fluid jet velocity at the nozzle outlet. Thus when these differences are compounded together they could give rise to further fluid streamlining beyond that which would normally take place and especially so if in combination with a special streamlining nozzle', to give at least an r3 relationship, to result in a reduc tion to 4 times faster fluid jet velocity.

Or, the system could well function as in the earlier micromass description with the fluid jet velocity remaining at 4.5 times faster, but obviously the colder and further into the liquid phase the initial fluid state then the more towards r4 the relationship would become.

However, to the rescue could be the foregoing technique since one could remain with the nozzle CSA the same as that required for the cold fluid to give the 4.5 times faster fluid jet velocity and then recycle the surplus fluid and energy hoping the recycling efficiency would be good enough. But the first aim would be to try to achieve a fluid volume relationship with r to the two rather than r to the four. When a modified fluidity equation may become: Fluidity = 8V1 (?) v (Pl-P2)r2t And if so quantification of the system could become simplified for practical application purposes. Or even if it would simply be a case of using the correct r-power relationship between r4 and r2 in the same basic equation, albeit perhaps unlikely basing on the derivation of the equation.However, a volume relationship with r2would require a full square face to the fluid jet flow, which is sometimes achievable with gas flows and in particular air flows over the body and wings of modes of transport, etc., ref:- 'Mechanics of Flight' by A.C. Kermode, page 55/6, where it can be seen that full velocity of the air flow can be achieved as little as a millimetre from the surface over which the air flows. However, this is an aspect of fluid flows determined by their viscosity property and the viscosity of the fluid would still be of the order of 5 times higher than in an air

rlow1in the

eX19' ype at systemslwhen in the Critical Point region state where the liquid behaves as a vapour.However, since it could be behaving as a vapour at suchastage in the process, and since the fluid flow will be accelerating along a streamlining converging nozzle directly from the high random pressure state P1 to the low external pressure, P2, then the flow could be better than parabolic having a relationship with r4 and could

be expected to at least have a relationship with r3. Then of course there may be techniques that one could apply to improve upon this aspect, e.g., use of an ionised fluid in combination with electra forces forcing the fluid away from the nozzle walls (?),

Thus

wod rz pbrh n correct to say that the fluid flow velocity is not fLAttj determined by the fluid viscosity, but rather if the fluid sticks to the walls of the fluid flow pipe then the viscosity property of the fluid will come into play and into the equation and determine the velocity distribution of the fluid flow across its face, from the worst case of a parabolic profile to the best case of a fully square profile, i.e., full velocity across the whole face of the fluid flow.But even in the case of the air flow the fluid velocity falls off to stationary close to the surface over which the air flows, albeit in such a case being at full potential velocity across most of the profile of the fluid flow velocity distribution because adjacent streamlines of the air flow are not held back to the same extent by the stationary layer of fluid on the surface of the body over which the air is flowing. In turn because of the low viscosity of air, or

high fluidity.

Therefore, it follows that if a system can be devised in which the fluid flow doesn't actually come into contact with the nozzle walls, e.g., via the above electro approach, then at such a stage in the process the viscosity of the situation would become overridden to some extent and fluid would not become held back from the maximum velocity along the central longitudinal

axis of the fluid flow ab% stationary fluid 'stuck' to the nozzle walls' through the interconnecting viscosity property between layers of the fluid, and all

the tiuld riow couldltlow along at the rull maximum velocity as tor the air flow but better since the velocity wouldn't even fall off at the very edges of the fluid flow.

It also follows that perhaps applying a material for the nozzle to which the fluid could not 'stick' because of the natural electro repulsion properties between the respective substances one to another could potentially be a means

improve upon these aspects of the system. As water to polyester glass fibre water shoots for example. Unless the fluid flow becomes held stationary at the interface due to phenomeno other than electro affinity, Of course, another component is the smoothness/roughness of the surface and a Pre- requisite would be smoothness at the interface before then trying to create a stand-off effect via electro repulsion forces. Which however could over ride lack of smoothness to some extent. However, recapping on probable reality at this stage.

Basing on the basic fluidity equation the following will apply: Vhot Fluidity hot = thot Vcold Fluidity cold = tcold In a system where all the other parameters are constant.

Therefore: Hot fluid fluidity - 4.5 ~ V For unit Cold fluid fluidity 1 1 i- time Therefore, the volume flow per second will be 4.5 higher for the hot fluid than for the cold fluid where the fluidity relationship is in the ratio of 4.5 to 1 and, therefore, the respective fluid jet velocities should be in this ratio through the same nozzle exit CSA. However, this flow would have to become reduced to 2.5 volume units via appropriate reduction of the nozzle exit CSA, which would unfortunately reduce the fluid jet velocity to 3.4 times faster for parabolic flowing, therefore, an r4 relationship 3 with volume flow strictly applying. Bu;L it is likely that at least an r3

relationship with volume flow couldjapplytJwhen the fluid zet velocity would become 4 times faster. Which, however, would still reduce the kinetic energy of the fluid jet per unit mass of fluid by some 20%, which remember

would probably be only just bordering an being able to impart the energy required.

However, to the rescue could be the foregoing technique of recycling fluid, and/or techniques to sr)So improve upon the basic parabolic nature of basic fluid flow. However, it is increasingly seeming likely that in the beginning at least one would try to apply the liquid recycling technique, which in fact could conceivably give increasing advantage with increasing size of nozzle CSA in combination with increasing quantity of recycling fluid? Thus, this could be another area where one may potentially be able to acquire bonus energy, albeit it perhaps being one of the main problematic areas potentially detracting from process efficiency.Yet on the other hand it could be a struggle where potential defeat could quickly be turned into a potential victory, not just by the fluid recycling technique but conceivable techniques to try to square the face of the forming fluid jet could not only reduce upon the level of detraction but could conceivably also be a source of bonus energy. Because if one can achieve a total stand-off for long enough via electro techniques then perhaps in the forming of the fluid jet flow one could achieve a fully square face on the fluid jet from which one would obtain a higher fluidity value relationship with respect to the cold fluid fluidity.

Which in effect would constitute a streamlining advantage.

whilst its early days, it can

be

that the viscosity equation that Poiseuilles evolved in 1840 will still hold for the system under discussion and at the high pressures and temperatures of the system after taking all the parameter changes into account when it could perhaps be thought that the enthalpy addition to the pressure parameter would require the derivation/evolution of a new equation to relate all the various parameters of the system. Albeit perhaps requiring of some modification/extension, which I in fact carry out later on in ensuing discussions.However, still in the context of the discussion at this early stage in the evolution of my thinking on this process, it is progressively seeming likely that one could indeed

regard the heat energy asl a separate entity and simply as though an additive that one may add to change the internal properties of the fluid which then responds differently under the separate entity of a given constant pressure.

In this case the additive heat increasing the volume parameter of the fluid and lowering the shearing energy requirement between adjacent molecular planes in the fluid, i.e., having these two main internal effects on the fluid. WhreaS normally the addition of an additive usually decreases the fluidity of the base fluid, e.g., as when dissolving paper in cuprammanium hydroxide. However, the basic equation should be found to still fully apply to the system under discussion in which the fluidity of the base fluid, i.e., the,cold,fluid, decreases on

addition of the additive, i.e., heat. However,1 under perhaps being the operative word. Which then becomes a fluid that responds differently under the separate parameter of the external pressure acting on the fluid.But the equation and the parameters it contains seeming to fully define the system in a comparison between hot and cold fluid in the system under a constant pressure head. Which presumably would still be the case if the,external pressure head were to vary.

In one

therefore whilst1 the pressure parameter has become a pressureenthalpy parameter, the effect of the additive heat is the enthalpy component which becomes manifest in the basic equation as lowering of shearing energy between molecules to increase the fluidity of the fluid combined with an increase in the volume of the fluid which becomes accounted for in the volume parameter of the basic equation. Just as any normal additive addition could.The pressure component then being a separate entity and still remaining the same pressure parameter in the basic equation just as for a normal additive. Which I, therefore, think will be a correct view of the system, the pressure parameter remaining the same and the fluid simply responding differently under a given applied pressure dependent upon how much heat it contains with the differences the heat makes becoming fully accounted for in the basic equation as lowering of shearing energy, ie, viscosity value, on the LHS, and as increase in volume on the RHS.

However, when one gets down to some of the very nitty-gritty of the system, as for example in the aforementioned text book by Dr Pryde, there could perhaps be some deviation from the basic equation in relation to the volume parameter to length parameter of the equation for the hot fluid when compared with the same parameter relation :ship in the system of the cold fluid. Which however could probably be fully factored for in and/or fully accounted for by the basic equation. This in addition to the basic difference that adding the drawing force of the partial vacuum system and streamlining the fluid will make to the basic equation which I deal with later on herein and also involving the addition of a factor to the basic equation which I have termed the x vector herein.On a related aspect, I think that it is better to view the system from the point of view of the fluidity of the fluid rather than in terms of viscosity as normally the case for fluid flow mechanics since after all the effect the heat addition to the cold fluid is simply to make it more fluid and flow more easily under a given applied pressure compared with the same pressure becoming applied to the cold fluid. Which, therefore would mean viewing the basic equation, i.e., the basic parameter relationship effecting fluid flow, upside down since fluidity is simply the reciprocal of viscosity when related to the equation and therefore is just as relatable. Which in turn would be in keeping with the additive of heat lowering viscosity rather- than effecting an increase when the equation then usually becomes related to viscosity.Thus, it follows that I'm a great believer in sticking to the basic paramater relationship affecting systems wherever and whenever possible, which of course are a part of the basic laws, order, simplicity and perfection of the Universe of which our Planet and the systems thereof are no small part. Or perhaps more apt to say should thereby be no small part. Thus one would expect all the systems and processes of the final Kingdom of God on our Planet, of which the current system under discussion could form a main part, to fall into such a category and it is progressively seeming likely that this could indeed be the case. And indeed as simple as the system may seem to some on a cursory viewing. To then and thereby become more at one with God and the Universe to its further extremities. Or perhaps more apt to say their furthest extremities, as the case may be.Wherein we are all supposed to be a part. Um.

Then if one were to determine the reduction in required shearing energy in absolute terms based on the equation and then relate to number of molecules being sheared and then to the total number of molecules in the fluid jet, then the simple arithmetic sum of the reduction in shearing energy as determined via such a route may directly equate to the gain in the energy of the fluid jet

oFthe hot fluid under a given applied pressure and moreso / more tnan tne cold fluid under the same pressure, which will remain more in the random pressure state on flow, if not wholly so, but of coursethe stronger Van der Waal forces that will exist inside the cold fluid will hold the fluid together and it will virtually be simply as though a solid mass in all directions in comparison.

Whilst in the case of the hot fluid flow the much looser Van der Waal bonding therein in combination with the shearing energy effect and the faster fluid flow on flow under a given applied pressure will all combine together to cause all the initially randomly moving molecules therein to all become more aligned into the forward vector, and indeed in a further but of course fully interrelated view of the system from a different perspective it will be this effect that will enable the higher level of the kinetic energy of the randomly moving molecules on addition of the heat to in fact become harnessable by an amount corresponding with the heat addition to the fluid, which is an effect that will occur naturally on flow in the normal fluidity test and give rise to the higher fluidity value of the fluid in such testing. However, whether further streamling would be achievable under a high pressure in combination with correct streamlining shaping to the nozzle entry would probably have to be ascertained in practice, although the viscosity/fluidity property of a fluid is said to be independant of pressure up to high pressure of the order of 100 ATS and beyond. Thus a test carried out under a lower pressure but the same temperature would still give the same fluidity property value within a few per cent.

Perhaps also I should mention at this point that I / m

self-taught in such areas of science and technology, particularly fluid mechanics, and, therefore, I'm not sure whether my ralrly simple views and treatment would be the same as anybody else's in such fields. Not only the main treatment herein in relation to Poiseuille's fluidity of fluids equation relating the parameters involved but also for further example my view and treatment of the Bernoulli's Theorem as could alternatively become applied to the system and which I concentrate on in more detail in my earlier writing on the system entitled 'Throttle Energy Conversion'.Simply being a view in which one first considers the fluid in a random state before the nozzle exerting a similar pressure in all directions including in the rear vectors, but determinable via the value KE=l2mv2 for the fluid jet which,in turn,would be the forward dynamic pressure component of Bernoulli's equation defining and quantifying the parameters of a fluid flow that becomes polarised into one possessing a high forward dynamic pressure and a low static pressure from the random state via externally applied forces,with that part of the fluid which is becoming forced along the entrytothe nozzle and then through the nozzle under the random pressure then becoming polarised into a fluid jet possessing a high forward dynamic pressure and a low static pressure, which I sometimes refer to as the side vector pressure of the fluid flow which it would be for all practical purposes. The sum of the two pressures re.m.ining a constant related to the initial random pressure. Then when a partial vacuum becomes applied to draw the fluid further then the further streamliningthatwill then and thereby take place will take the static or side pressure of the fluid jet below lATS. and the forward dynamic pressure will become increased upon by a pro-rata amount and by an amount equivalent to the power of the partial vacuum, and in this way this component of the applied forces will become added to the power of the fluid jet.Which when one considers that the mass flow rate has to still remain at unity then this may be the only way that the power of the partial vacuum could become added, as opposed to drawing the fluid en mass to flow at a faster rate. Although if one then reduced the nozzle CSA further to achieve a mass flow rate of unity once more, then I guess the micro-masses within the mass flow would be travelling faster and give a higher kinetic energy by an amount equivalent to the power of the partial vacuum.

Thus another in-situ example of the self-teaching nature of this work as I go along as it were, for which I apologise to those in the various fields concerned and ask others not to take me too seriously and/or too literally as the case may be, but pioneer forward at the front as it were and trust that the establishment will be able to wrap around me and my work. As intended at least anyway.

actually, the increase power of the fluid jet due to adding a suction force tv the applied force of the pressure head could be due to a combination of both effects simultaneously and it may become important to discern the difference between the two effects in this system and others, e.g., my air powered transport :ation system, but I leave my earlier discussion on this question as is for now, which I in fact confirm as probably being almost correct in ensuing deliberations. Thus, for the work herein it is of more interest, and perhaps as applicable, to relate the fluid mechanicsofthe system directly to the basic fluidity equation.

Via which, for example, one could probably acquire an' absolute value for the parameter fluid jet length in unit time, i.e., its velocity,which one could then directly apply to determine the l2mv2 value of the fluid jet, which of course in turn is the energy value of the forward dynamic pressure component of the Bernoulli's equation/theorem. However, I should perhaps add that I think my work via the Bernoulli's Equation will be as equally important as that herein.

Thus via such a route basing on the basic fluidity equation one should be able to determine the parameter fluid jet velocity v, for a liquid flow system in which the effects of both pressure and enthalpy content have to be fully considered, and not just the pressure head as in hydro power harnessing based upon cold water for example, when one can more simply and straightforwardly equate the potential energy value of the water pressure head, i.e., its normal mgh value, to the kinetic energy, i.e.,: mgh = lmvl energy of fluid jet produced under the pressure head of energy value mgh.

Iten fluid jet velocity, at times herein referred to as the linear flow velocity and fluid jet length in unit time, is more simply given by:

Thus, in the system under discussion perhaps all that would be required to calculate the same data for this new system would be the fluidity value of the fluid at the working temperature and pressure of the system, together with volume data for the fluid at the states being considered.Whilst perhaps via a different route to the same energy amount but through the same basic equation and parameter relationship of the equation and of the system, (the two progressively seeming particularly synonymous for the system as though tailor made for each other) it may prove possible to sum all the reductions in shearing energy in absolute shearing energy terms in order to identify and quantify the energy that one could acquire from the fluid in the system, which would also be a practical route to the determination of the Van der Waal bonding energy and the effect of heat and pressure on this energy in the fluid.Thus perhaps the latter route could be said to be via an ,internal lagrangian description through the equation to the energy quanitification, whilst the former route in contrast could perhaps be said to be via a euler ian description route through the same equation to the same energy quantity (Ref: Fluid Mechanics, Frank M. White. 1979 Daae 11. wherein it Plan type tht ehsF rhsnnP

ii' viscosityjf6r liquids is but few per cent up to 100 ATS. on aae 29

j relationship with temperature

upon a more accurate, expanded, version of the general equation).However, the whole of these aspects would require deeper treatment probably involving practical experimentation and therefore progressing on at this more general stage, although later in ensueing discussion I do commence attempts into such directions, e.g., fluid jet velocity quanitification and related nozzle CSA requirement. However, this is getting ahead of the more general discussion, which

on with as follows.

Thus, now relating the increase in the volume parameter to the early micro-mass description of the system.

the main practical difference on interrelating the accompanying effect of the heat additive on the fluid volume parameter into the description will be that the nozzle CSA dimension will only have to become reduced by 1.8 times instead of the 4.5 times that would have to be the case for fluids that remain the same in volume for a 4.5 fold increase in fluidity for the passage of unity mass in total. With all other aspects of the description basically reflaininq the same. Although the surface area of impact

would be larger/because the fluid Det would be or higher cross-sectional area but the micro-mass in each 2.5 times larger micro volume would be the same and therefore the impact energy per micro-mass would be the same.Obviously the advantage of only having to become reduced by 1.8 times will be when one brings into the equation frictional losses against the inside surface of the nozzle, and therefore in turn this will be the main advantage of the accompanying increase in the volume of the fluid. Otherwise had a 4.5 times reduction in the nozzle CSA been required for the system to operate under the conditions demanded by the hot fluid then perhaps more difficulty would be experienced in practice. Although in larger scale,ihe process the more fluid one could pass through one nozzle, and perhaps especially so in the simple fluid jet impulse turbine arrangement and therefore perhaps this aspect would not have presented too much of a problem.

However, to acquire an energy advantage from the hot fluids higher potential for further streamlining beyond that which one could achieve with the cold fluid at ground state then this would involve reduction down to an even less nozzle CSA dimension and therefore the increased volume advantage will become even moreso of an advantage. Although streamlining of the fluid will be the way to overcome much of the surface frictional losses anyway. Therefore, if one is successful in glining a streamlining advantage then one should accompanyingly be being successful in reducing the surface frictional losses against the inside surfaces of the nozzles.

Of course, to override all such considerations to some extent will be the aforementioned technique of fluid recycling, which in fact is a technique that grows as the ensuing discussion evolves to finally finish as a central main feature of the process.

Thus, progressing the basic discussion further.

Firstly repeating more fully the preceding exercise in which I conclude that on reduction of the nozzle CSA, to in such a way give a mass flow rate of unity, the velocity of the fluid jet may in fact become reduced from the required level of 4.5 times to 3.36 times faster when relating to the velocity of the cold state reference fluid of fluidity value 4.5 times less than the hot fluid being considered due to the r to the four element in the system. Which if so would reduce the initial kinetic energy of the fluid jet to 11.3 times from the required level of 20 times as when related to the normal mgh level that would be yielded by the cold state reference fluid.Which in turn would be disastrous since the 20 times level may only just eventually be capable of fully sustaining the compressor, e.g., as at a probable/possible 50% combined conversion and energy recycling efficiency level. However, the very r to the four element that could potentially bring about a downturn in the process to lower levels of potential horizons could also potentially bring about an upturn in the potential fortunes of the process taking it and them to higher levels of potential and horizons, since conversely if by recycling fluid this enables one to increase upon the nozzle radius dimension then by the same token the nett energy output may become improved upon rather than perhaps disastrously impaired due to having to reduce the nozzle CSA instead.However, in the event of the latter there could in fact be a further saving grace, this being that for hot fluid in the liquid vapour state at least there would very probably be the potential to be able to 'super' streamline the fluid jet in comparison to the level of streamlining achieved in the cold state reference fluid under normal conditions and then would take place under the conditions of a normal fluidity test on the hot fluid. Here making a distinction between normal laminar parabolic flow as would be obtained in the latter and further 'super' streamlined flow as should be achievable under the special conditions of acceleration of hot fluid in the liquid vapour state under and from a relatively very high pressure to a low pressure through an appropriately internally shaped nozzle.To in turn and thereby impart additional energy to the fluid jet becoming created and such that the energy of the fluid jet still exits from the nozzle at the 20 times energy level even after reduction of the nozzle CSA to that required for a mass flow rate of unity. To in effect thereby overcome the r to the four element in the system, and in the process perhaps giving rise to r to the thin effect and practice. However, this is an aspect I deal with more fully later on in the discussion and here seperately trying to determine whether it may prove possible to apply the r to the four element for the good of the system and in fact then and thereby bring about an upturn rather than a downturn in the potential horizons and fortunes of the process.

Thus, firstly repeating the preceding exercise but more specifically with in mind trying to determine whether the above could be expected to prove the case in practice, which if so would then potentially render the preceding concept of recycling fluid of far more central importance in the further development of the process.

Thus: Fluidity = 8V1 JIT(Pl-P2)r t If one considers that the parameters of the system remain the same then for the hot fluid of 4.5 times higher fluidity value the volume flow rate, v, must be 4.5 times higher in unit time, which in turn would then give a 4.5 times fluid jet velocity on passing through a nozzle of the same radius, r, parameter, assuming the mass flow is being sustained. Thus under such conditions the whole of the fluid jet mass would have a velocity of 4.5 times faster, but the mass flowing from the nozzle would be 1 x 4.5/2.5 = 1 x 1.8 = 1.8 times higher than the mass flowing from the compressor at the beginning of the fluid flow.

However, the point being and to grasp at this stage in the discussion is that the 1 mass unit flowing from the nozzle associated with the 1 mass unit flowing from the compressor would possess the required velocity of 4.5 times faster under such conditions of operation, which in turn would yield the 20 times energy level as related to the normal mgh energy level of cold state reference fluid, which in turn could Dotentiallv fullv sustain the comDressor. To

leave remaining the energy yield associated with 0.8 mass units/in unit time for continuously recycling 0.8 mass units in unit time.Which obviously may still fall somewhat short after allowing for energy conversion and recycling inefficiencies and, therefore, one next stage is to determine whether increasing the nozzle CSA radius involving the continuous recycling of more fluid mass in unit time could be expected to be a way to improve upon the nett energy balance of the system at this stage. Remember all we are trying to do is to minimise our losses resulting from the r to the four element in the system and perhaps in the process turn it to our advantage, not conjure up energy from nowhere and out of thin air as it were.However, still at this stage, if one then reduces the nozzle CSA to give the volume flow rate of 2.5 volume units from 4.5 volume units, in unit time as required to in this way maintain a mass flow

of unity, the radius dimension would have to become reduced asXfollowrbasing on the basic fluidity equation for normal laminar parabolic flow; Thus, up to this stage we are assuming parabolic flow will apply to the cold fluid then to the hot fluid and then on reduction of the nozzle CSA for the hot fluid.

Later I will explain how this could probably be deemed to be wholly the case for and at the point of fluid leaving the main bulk of the fluid and entering the nozzle and for the first stages thereafter, albeit perhaps the hot fluid then becoming additionally streamlined. Embodied within theory in which I postulate that perhaps at such a stage in the system one should regard the relevant length parameters in the basic fluidity equation in a comparison between the hot and cold state reference fluid as being different because hot fluid in the liquid vapour state would be bound to go on to become far more streamlined than could cold state fluid close to its solidifying point and therefore in a state far more bound by internal Van de Waal forces, even if super streamlining is not achieved and/or not achievable because of beingtoobound by internal Van der Waal forces. Which in turn and alone could be an aspect of the system that could potentially cause the hot fluid jet velocity to be in the ratio of the fluidity values between the hot and cold state fluid after the reduction of the nozzle CSA

the fluid volume flow rate of 2.5 volume units in unit time and when the mass flow rates in the respective systems would then be the same. But remember requiring the foregoing difference between the fluid states for this to prove the case, i.e., one becoming far more streamlined than the other with respect to the alignment of fluid molecules within the fluid on flow. You see the 2.5 volume units of the hot fluid containing 1 mass unit could then potentially become 4.5 units in the length dimension on flow of an initial 2.5 fluid volumes initially fully cubic in shape, whilst 1 cubic volume of cold state reference fluid similarly containing 1 mass unit would not nor could elongate in such a way on flow because of being too bound by much stronger internal Van der Waal forces in comparison. Which then could in effect redress the loss due to the r to the four element in the system on nozzle CSA reduction, either wholly or to some extent. However here considering the r to the four element in isolation from other effects which may or may not be applicable and prove to be the case in practice.

Thus, here assuming that normal laminar parabolic flow applies throughout and that the relevant length parameters applicable in the equation will be the same throughout then basing on the fluidity equation for normal laminar parabolic flow the following will apply to the hot fluid on reduction of the nozzle CSA to reduce the volume flow rate from 4.5 to 2.5 volume units. Here remembering that this comparison is simply between the same hot fluid at different nozzle CSAs and also that the pre determined fluidity value for the hot fluid will remain the same on the LHS of the equation.

Thus

two equations for the different nozzle CSAs

8x4.5x1 8x2.5x1 (P1 - P2)r4largext lf (P1-P2 )r-4smallst 4.5 = 2.5 r4 large r4 small On this occasion basing on a CSA of 1.0 for the larger volume flow of 4.5 volume units which would then relate moreso to the values in the earlier micromass description of the system.

Then for a CSA equal to 1 r will equal 0.564 and r to the four will be equal to

this time for the larger volume fluid flow. Therefore: 4.5 2.5 O.lûl = rCsmall r4small = 2.5 X 0.101 = 0.0561 4.5 r small = 0.487 TT r2small = 0.744 Since the mean fluid jet velocity under whatever the conditions of the actual velocity profile of the fluid flow must always be given by the volume of fluid that has flowed in unit time divided by the CSA of the aperture through which the fluid volume has flowed in this case the nozzle CSA at exit, assuming the fluid flow is at least touching all around the internal sides of the nozzle exit aperture, which it would/must be if no stand-in effect were becoming induced via electro effects, etc.Thus, the two fluid jet velocities will compare as follows For the large nozzle CSA: Velocity = V = 4.5 = 4.5 CSA 1 For the smaller nozzle CSA: Velocity = V = 2.5 = 3.36 CSA 0.744 In other words the nozzle CSA has been reduced to give the flow rate of 2.5 volume units and a mass flow rate of unity with respect to the compressor mass flow output, but at such a required nozzle CSA it is larger than would be required to maintain the linear forward velocity of the volume of fluid flowing out of the nozzle at the level of 4.5 velocity units i.e., at a level of 4.5 fluid jet length in unit time to express in such a way for the better understanding of the later discussion.

Now if I repeat the above exercise hypothetically assuming that an r2relationship applies then it will be more clearly seen that in such a case the fluid jet velocity must remain the same. Thus: 4.5 = 2.5 r21arge r2small 4.5 = 2.5 0.318 r2 r2 small = 2.5 x 0.318 = 0.177 4.5

Therefore, the smaller nozzle CSA would/be 0.555 and the fluid jet velocity would then = 2.5/0.555 = 4.5, i.e., remain the same. Which, however, would perhaps be conditions only almost fully achievable for some gas flows, e.g., an air flow where the fluidity is relatively high and the streamlined fluid layers very rapidly approach full fluid flow velocity from the edge of the fluid flow. For example, as illustrated in the text book 'Mechanics of Flight' by A.C. Kermode, pages 55/56.Although a fluid in the system herein in the liquid vapour state, e.g., as becomes described in the further text book biblography being referred to 'Fluid Mechanics' by Professor Frank M. White, 1979, Chap 1 page 4 lines 4 to 7, could potentially be induced to approach an r to the two relationship. Or at least to having an r to the three relationship. Which of course are fluid flows not to be confused with others that may also have a fully square profile but in their case due to the fluid being too viscous. However, here for the purposes of this particular exercise we are considering a situation in which the basic equation for normal laminar parabolic flow could apply and that there would then unfortunately be an r to the four relationship existing with fluid volume flow.Which in turn would unfortunately reduce the mean fluid jet velocity from the value of 4.5 to 3.36 velocity units on reduction of nozzle CSA to give a volume flow rate of 2.5 volume units and therefore and thereby a mass flow rate of unity with that at the compressor outlet which in turn would ensure that the pressure would be maintained from compressor outlet to subsystem nozzle outlet, and indeed the required conditions of constant pressure cooling.

If one considers parabolic flow then one can see why this would be so since if one envisages the edge velocity to be stationary andthevelocity profile to be parabolic for both fluid flows then one can envisage that the parabolic flow with the smaller CSA will possess a higher ratio of the slower moving fluid to the faster moving fluid along the central axis of the fluid flow, and therefore the lower will become the mean fluid jet velocity the lower the nozzle CSA.

Therefore, this is potentially a somewhat unfortunate aspect of the system as evolved to date since it will mean that on reduction of the nozzle CSA to give a mass flow rate of unity for the hot fluid with respect to the fluid mass flow rate from the compressor then the fluid jet velocity would not remain in the ratio of the fluidity values between the hot and cold state reference fluid.

Which in turn would mean that the required quantity of energy may not be obtained basing on the earlier work.

commenting that it follows from the discussion so far that the fact that one would obtain fluid jet velocities in this ratio for a system in which one could leave the nozzle CSA the same would not arise from extra streamlining advantage per unit mass of fluid flow, but rather because the r to the four reducing element would not then become manifest in the system. However, one would expect to be able to

induce / streamllnlng advantage in this particular system, as in earlier and later discussion, which if so would then be a further way to improve upon the energy yield.However, to what extent such extra streamlining could be achieved over and above that which would undoubtedly be associated with a normal fluidity value of and on hot fluid in the liquid-vapour state would probably have to be fully ascertained in practice, but in later discussion I 'guess' that one may potentially be able to achieve some improvement via inducing extra streamlining basing on current knowledge in the fluid streamlining field.

However, for the particular facet of the system under discussion here it is perhaps easier to be more definitive at this theoretical pre practical stage of the work. Therefore, now trying to determine how much one may be able to overcome the possible r to the four element in the system, and if so potentially detracting from the fluidjet velocity, via the large nozzle CSA and recycling of fluid method, and indeed whether one could perhaps potentially go even further to perhaps capitalise upon this element in the system for the further benefit of the system.

Of course, as a pre-requisite in such considerations one would not expect to be able to acquire anything for nothing in compliance with the laws of conservation of mass and energy. However, the r to the four element would already be a part of the fluid flow giving rise to the normal fluidity value of the fluid flow since by definition the fluidity value of the IHS of the equation is inversely proportional to r to the four on the RHS thereof. Therefore, the r to the four element would already be detracting from the velocity of the fluid flow.Thus, one would expect there to be scope for improvement via inducing additional streamlining, but here it is being considered that perhaps by increasing upon the nozzle CSA even further with recycling of correspondingly more fluid one could achieve a further way to perhaps improve upon the nett energy balance of the system since the r to the four element could then be detracting even less from the fluid flow velocity relative to that of the cold state reference fluid.which would then be flowina throuah

a

nozzle/in comparison for the flow of 1 mass unit in unit time

relative to the compressor output mass flow rateS Therefore, carrying out the preceding exercise for an increase in the nozzle CSA to 1.5 times larger as follows, instead of the reduction that is required to give a flow of 1 mass unit, when the cold state reference fluid would require the nozzle cSA before such reduction for the flow through of 1 mass unit in unit time.

For a nozzle CSA 1.5 times larger then the comparative radius dimension would 4 become 0.69 and the r parameter 0.227 Therefore, the following would apply:4.5 large = V(even)larger 0.101 large 0.227 = 4.5 large x 0.227 larger 0.101 large = 10.1 volume units The mean fluid jet velocity would again be given by volume flow divided by nozzle CSA: = 10.1 = 10.1 = 6.75 velocity units lTr2 1.496 Therefore, from the above it can be seen that the mean fluid jet velocity of the larger volume of mass flowing from the larger nozzle would become 6.75 velocity units. Thus, increasing upon the required level of 4.5 velocity units by a factor of 1.5 which, as one night expe:6 is in the same ratio as the nozzle CSA increase.Therefore, the 1 unit of fluid mass flow associated with the compressor output and a part of the larger fluid flow would now also possess the higher mean velocity value. However, the total fluid mass flowing from the nozzle would now be 10.1 divided by 2.5 = 4 mass units and therefore 3 mass units would now have to become continuously recycled from the level of 0.8 mass units associated with the nozzle CSA remaining the same relative to that required for the cold state reference fluid and the fluid flow then being just 4.5 volume units in unit time, which in turn and in contrast would be just 2 volume units over the volume flow for unity with the compressor output containing the 0.8 mass units therefore required to be continuously recycled.

While with regard to the energy, the fluid jet velocity would have become increased to 6.75 velocity units which in turn would become an increase of 6.752 = 45 times the energy per 1 unit of mass of fluid flow in comparison to that of the cold state reference fluid flow, thus increasing upon the preceding level from the value of 20 times the energy level per unit of mass for a system in which one maintained the nozzle CSA the same as that required for the cold state fluid.

Therefore, the total energy of thefluid jet would be 4 units of mass x 45 = 180 times the energy, but with 3 fluid mass units to become continuously recycled. However, the energy required to recycle the mass would very probably be the whole ofthe energy becoming produced by the recycling mass, although this is an unknown and in the preceding exercise the equivalent energy quantity would be the level of 20 times the energy of the cold state reference fluid per 1 unit of recycling mass. However, the difference in this current system is that 3 units of mass would be becomina continuouslv recvcled in unit time.

Therefore, would this require an energy level of 3 x 45 times or/still/3 x 20 times. I think one would definitely have to assume the former at this prepractical stage, and in relation to this a salient aspect to grasp is that although the fluid jet velocity is able to become increased from the level of 4.5 to 6.75 velocity units we are nonetheless still considering the same unit of time with respect to the flow of the 4 mass units. In other words, because the fluid jet velocity is able to be 1.5 times faster would not mean that the 4 mass units would flow through the system at a 1.5 times faster rate than the 1.8 mass units in the preceding exercise. But rather that the nozzle CSA is now able to be in a smaller ratio with the flowing mass because of a reduced r to the four element, causing the micromasses within the mass to flow faster.Or conversely, a nozzle CSA 1.5 times larger would allow the larger volume of fluid to flow through at a faster rate with respect to the micromasses in the larger volume of fluid because of the reduced r to the four element when associated with a larger fluid volume flow, which in total would still pass through the nozzle in unit time. Therefore, if each total mass is passing through the system in the same unit of time then perhaps the recycling energy would still be at the level of 3 x 20 times the energy quantity as related to the flow of 1 mass unit of cold state fluid in unittime. However, I must emphasise that it would seem far more likely that the energy yield due to the recycling mass would be the quantity that was required tocontinuously recycle the mass. Perhaps to say the least inferring that at least there would also be recycling inefficiencies to make up.On the other hand, when one considers the fluid jet energy equation: KE = Q mv2 then in the micromass description micromasses cause to flow faster could yield more energy whilst transferring the same total mass in unit time. However, one obviously couldn't acquire an ever increasing spiral of power yield in unit time, and therefore there must be a limiting factor or factors, but maybe with an optimum peak position at some point which however if so would probably be fairly close to the lower end of the possible range of this potentially possible technique. However, I have to admit that this particular aspect has got me more than somewhat mystified at this pre practical stage at the moment the deeper I look into it.Since the higher the volume of fluid then the faster could / would the fluid jet velocity be and, therefore, the more the energy each unit mass of fluid flowing in unit time would yield.

But the energy required to return each mass of fluid against the constant pressure head all the time could remain the same. You see, the time taken to transfer the total mass from the nozzle to the impellors would remain the same but the larger the nozzle then the even larger the volume of fluid that could flow in unit time, i.e., 4.5 volume units for the nozzle CSA at lsand 10.1 volume units for the nozzle CSA at 1.5, thus the volume units increase by 2.24 times whilst the nozzle CSA only increases by .1.5 times. Which will mean that for the larger volume of fluid to flow from nozzle exit to impellers in unit time then the fluid jet flow would have to have a faster linear velocity than the smaller volume of fluid transferring in unit time.Which in turn would mean that each mass in unit time should iinpart more energy to the impellors of the turbine in the case of the units of mass travelling in the larger volume flow.

One could understand the logic if the faster velocity for the larger volume flow gave rise to the time taken for the total volume to flow becoming correspondingly reduced since then the recycling energy would have to be correspondingly more. But the whole idea of the concept depends upon maintaining the time to flow the same and thereby maintain a constant pressure head. In other words to have the lot flow out in unit time no matter how much there is to go through thenozzle in unit time. Therefore, perhaps I'm on to something here.

yet to come is also the considered strong potential for a streamlining advantage over and above the normal level. Furthermore, the aspect under discussion here is but one potential further source of bonus energy and not really the basic one that I'm tryingtoget to in this particular part of the discussion.Therefore, for the purposes of this exercise and to arrive

at the basic potential source of bonus energy that I'mltrying to get to here I intend to assume that perhaps an optimum peak position would exist, perhaps when the fluid jet velocity is at 45 resulting from the nozzle being 1.5 times larger than the conditions necessary for unity with the output from the compressor, but that at the optimum position the surplus energy yield would then only just be that required for recycling the associated surplus fluid and perhaps still falling short by the recycling inefficiencies. Which then leaves the 1 unit of mass flowing from the compressor to consider, regarding which these considerations were first concerned and embodied within which lies the basic potential source of bonus energy that I'm trying to reach.

Thus, at this stage capturing the basic essence of the source of the bonus energy that I'm endeavouring to determine at this stage. Increasing upon the nozzle CSA enables a faster fluid jet for the volume of fluid necessarily having to flow through the nozzle in order to maintain the pressure head of the compressor output. However, it is being assumed at this pre-practical stage that at some optimum position all the energy produced by the surplus mass would be required to recycle the fluid mass, and even then may fall short by the recycling inefficiency factors in the system.Thus, the bonus energy source would be to provide for any short fall in energy here, and should arise from the fact that since the increased volume of fluid containing 4 mass units would be flowing out of the nozzle in the same time as the hot and cold reference systems then the 1 mass unit flowing along the pipeline from the compressor would still be doing so at the same rate, and of course necessarily so in order to maintain the pressure head pressure the same. Which in turn will mean that the energy input requirement to the compressor will remain the same, i.e., at the 20 times level of energy

around 50% of this initial energy level.However, the point being that this 1 unit of mass would be responsible for 45 parts of the total of 4 x 45 = 180 parts comprising the total energy of the fluid jet, and whilst the fluid mass recycling energy requirement may be fully 3 x 45 = 135 parts of the energysthat required for the compressor should be still at the 20 parts level. To leave available 25 parts to make up for any shortfall in the recycling energy. Which in turn would then enable the recycling efficiency level to be: 135 x 100% = 84% 135 + 25 This then the basic source of the bonus energy that I initially had in mind as potentially being possible before becoming a little thrown by the more mystifying element creeping in, which I think is still sound despite the latter aspect.And if so would mean that the 20 times initial energy level required for the compressor would become far more possible to achieve and not become reduced to an out of court level, i.e., to the level of 11.3 times initial energy level. Which of course is the whole objective of these deliberations somewhere beyond the horizon of the future. Thus it will be a question of whether we've cracked it yet or should look deeper, but whatever with the potential for a streamlining advantage yet to consider and yet to deliberate over.However, here carrying out a further exercise for double the nozzle CSA as follows: For a nozzle CSA 2 times larger then the comparative radius dimension would become 0.8 and the r to the four parameter .0g41. Therefore: 45 = V 0.101 0.41 V = 4.5 x 0.41 = 18.27 volume units 0.101 Therefore, the mean fluid jet velocity in this case would become: 18.27 = 18.27 = 9.1 velocity units 7T r2 2.01 Therefore, the fluid mass flow rate would now be 18.27/2.5 = 7.3 times higher requiring of 6.3 mass units to become continuously recycled. While the fluid 2 jet energy would now be at a level of 9.1 = 83 times higher per unit of mass for 7.3 times higher mass to give a total of 606 times higher energy level.

Of which 6.3 x 83 = 523 parts of the energy would be required to recycle the now 6.3 units of surplus mass, again assuming that all the energy yield of the surplus mass would be required for thfs even though it is now an even larger energy amount. 20 parts of the energy would still be required for the compressor.

To leave remaining 606 - (523 + 20) = 63 parts to aid with the recycling of the 6.3 parts of the mass. To in turn enable a recycling efficiency level of: 523 x 100% = 89% (523 + 63) Thus, no improvement upon the preceding level of 84% for a nozzle 1.5 times larger and a fluid jet energy level of 45. Which would seem to indicate that with respect to this source of bonus energy at least then there would indeed be an optimum peak somewhere between a nozzle CSA of 1 to 2 times increase. Perhaps close to a nozzle 1.5 times larger than would be required if the system were 100% efficient throughout, and giving an optimum fluid jet energy level at the 45 times level.

Thus, it could perhaps be said by some that this process is probably just about beginning to now have some level of achievement in sight of light on the horizon, but more than this I think it is moreso beginning to emerge that the process will perhaps be achievable in the fullness of time and therefore will probably be worth striving to achieve. However, there is obviously a long way to go yet and notwithstanding earlier comment, the preceding exercise should not be regarded as being at all definitive, quantified or absolute but simply a simple emperical exercise perhaps usefully pointing the way to one approach to PerhaPs overcoming the r to the four element in the svstem in anv further practical

development of the process.And perhaps also an approach to,urther bonus

energy, although the latter wouldn' seem possible. Thus still something of a mystery with yet a lot of unanswered questions still requiring to be answered since obviously the system couldn't go on gaining-a seemingly ever increasing spiral of nett energy without putting anything in. Perhaps ending up with too much all too hot to handle. So is it all simply a delusion, or an allusion, or all a joke, or could there at least be some truth lying therein, but if so is there a limit and if so what is the limit and what are the limiting factors? Just a few of the unanswered questions yet to be answered on this one in this case. Or more apt to say, further fathom.At this stage could probably be said that there is at least hope of overcoming the r to the four element already existing in the system and which of course we don't want to add to but minimise as much as possible whilst making as much capital out of the phenomena as possible.

Actually I think that within the concept or concepts of this approach may lay more than hope. Basically the hope will lie in the probable fact that the slower moving mass all around the periphery of the fluid jet will decrease in proportion to the faster moving mass at the core of the fluid jet with increasing nozzle cSA and fluid volume flow. As further confirmation of this under the text book 'Introduction to Fluid Mechanics' bv Henke, Pase 146, Fig 14-2 dealing with

the standard view of laminarlfluid flow it states that under laminar flow conditions the mean velocity will be one half the maximum velocity along the central axis of the fluid flow. Therefore, the smaller the fluid flow CSA then the more the surrounding slow moving fluid will be placing a drag on the velocity of the fluid along the central axis of the fluid flow, and conversely the larger the CSA then the further away will be the central fluid and therefore the less the influence and drag on this fluid by the surrounding necessarily slow moving fluid and therefore the higher will be its velocity and therefore the higher will be the mean velocity of the fluid flow. Or more correct to say, the higher can be the mean velocity of the fluid flow for a given pressure head, providing someway can be devised to maintain the pressure head, etc. Which is where I came in on this one and, therefore, now progressing on a little further.

For now ignoring the more mystifying element embodied in the foregoing treatment, which in any case one may only be able to get to the bottom of on deeper, practical, treatment.

Of course, the success or otherwise of the fluidmass recycling technique will depend upon whether there is sufficient surplus energy available to recycle this part of the mass whilst still leaving sufficient for the compressor input requirement in the processing of the other proportion of the fluid passing around the larger circuit of the process comprising the heat collection,compressor and turbogenerating stages the overall process.Whilst the foregoing exercise would seem to indicate that on the one hand this may be just achievable via this technique and on the other hand, perhaps having bags of surplus energy to play with, the former view definitely being favoured at this pre-practical stage, there could be yet an additional technique that could be added to the basic technique in order to then and thereby improve upon the basic performance and energy balance of the subsystem as follows.

The fluid mass to be recycled would required both re-heating and re-pressurising via the energy available for recycling in order to be rendered back in a state fit to be placed back into thefluidflowing towards the nozzle after the heat removal stage.

Therefore, a way to achieve this could be to first compress surrounding air with the recycle energy and re-heat the fluid with the heat of compre 55ion produced to just the required temperature whilst simultaneously pressurising the fluid to the required pressure via the expansion enerav of cool comPressed

air rrom tne precealng/cycle. à in tne process ana as a rurtner Donus leave remainina verv cold exhaust air for the two PS and CS functions. i.e.. RainMakina.

Refrigeration and Cold Store functions. But Lirstly1 couja be a way to increase upon the level of the initial recycling energy since under my PA No. 8728601 which went before, calculations show that the expansion energy of the cool compressed air would be some 60% of the initial energy and of course the value of the heat of compressionenergywould be the same as the initial energy in heat energy terms. Therefore the initial energy would become increased to 1.6 times before inefficiencies, now in the form of both heat and mechanical energy.However, the pressurising energy could fall short in becoming reduced

a way to improve upon this would be to add some of the heat of compression energy to the otherwise adiabatic expansion of the cool compressed air as and if found required. To leave the remaining heat of compression for re heating the fluid as required.With yet a further way to further bonus energy being tO render the expansion of the cool compressed air an isothermal expansion to ground temperature via appropriate application of surrounding

natural neat sources rnus pernaps via tne asaltlon or tne above tecnnique there would then be sufficient energy yield at the normal level of fluid recycling, i.e., the 0.8 units of mass level that would be associated with having the nozzle CSA the same as that required for the cold state fluid reference system.

But an advantage of recycling more fluid at this stage would be that one would obtain more cold exhaust air in the process for the 2Rs and CS functions.

Thus beina a staae in the Drocess enablina the Introduction of compressed air

and removal of heat of compression for such purposes. Perhapslthe process improving upon the energy balance of the sub system by further minimising the r to the four element

All of which however is perhaps getting too far ahead of the practical phase since the sub-system may be found to function satisfactorily in the first place on reduction of the nozzle CSA instead to give a mass flow rate of unity with respect to the output flow rate from the compressor and especially so if some 'super' fluid streamlining can also be achieved as the fluid flows through the nozzle.Then, if not in the first place on reduction of the nozzle CSA,

the fluid jet velocityt ldl I'in'the direct ratio of the fluidity values of the hot and cold state reference fluid and therefore having an initial energy value 20 times that of the cold state fluid. Which should then be a quantity of fluid jet energy that equates to the pressure-enthalpy content of the fluid, as attempted to demonstrate in the earlier work, and which in turn should just yeild sufficient energy to fully sustain the compressor. Thus, if this is found to be achievable for this system then the foregoing combination of techniques involving recycling of fluid could become a further approach to bonus energy in and by the system.It follows that a combination of super streamlining coupled with the fluid recycling technique could uLtimately prove the better way to maximise upon the energy yield of the sub-system.

Continued General Discussion: As discussed in preceding discussion a further main way that it may prove possible to increase upon the energy yield at and by the nozzle stage is by inducing very streamlined fluid flow beyond that which would normally be obtained in normal parabolic laminar fluid flow to which the fluidity values relate. However, at this pre-practical stage it's somewhat difficult to know whether a streamlining advantage could be obtained and therefore in ensueing discussion I discuss some of the more relevant basics of the system in an attempt to determine the probability of such a potential possibility.However, I should perhaps point out again that I have not been formally trained in

such fields of science and technology andPi/1more based upon a lifetime's experience and work at the 'mill' and original work in my own head based on the basics,as indeed the whole of the work, and therefore no doubt fluid mechanic experts fully engrossed in their particular field would subsequently be far more able to deliberate over such aspects of the system.

However, my treatment may at least serve to give some further useful insight into the svstem and could perhaps be a valid approach, or at least a starting

point to a valid approach. Of course there arezevolutions from the starting point

in current application and another approach from a different starting point could probably be via theBernoulli's Equation, e.g., as given under, the text book 'Fluid Mechanics' by Frank M. White page 159 to 162, but more generally in the form: po = p + 12,OV2 + pgZ

I'm not fully at one with this equation as treated and discussed in some of the text books, and at this stage would simply prefer to regard the equation as quantifying certain parameters of the system in a different way.

Namely an expression which on one side of the equation represents the parts of the sum of the applied forces, i.e., the random pressure energy plus any potential head energy, giving rise to a polarised fluid flow pressure on flow comprising the forward dynamic pressure 2mv2 and the side or static pressure of the fluid flow.Then on the addition of vacuum energy this becoming added to the side of the equation representing the applied forces in an appropriate manner, which in turn would give rise to a higher -21mv2 energy level

Equation-3-74 and 3-75 on page 175 of Professor White's book would seem to be points of unity, and moreover on page 368 under equation 6-124 he expresses the basic Bernoulli's equation in the way that I view the meaning of the theorem, i.e.,:: p + lpV2 = Po Where the quantities on the LHS of the equation are simply the separate parts of the polarised pressures comprising the static/side vector exertion pressure, P, and the forward dynamic pressure i2pv2. The sum of which then equallinq the energy of the uniform, - random, pressure, Po, which gave rise

to tne rlula rlow/now possessing a align rorwara aynamle pressure ana a correspondingly low side vector exertion pressure instead of the uniform, random, pressure. As in a Pitot tube.Where the value 2 V2, or 12my2 to express differently, will represent the impact pressure and that exerting in the side vector, i.e., p, will be a part of the po energy that will not nor could become transferred to the turbine,

that part of the Po energy that the quantity 2lpV2 or l2mv2 represent. Which of course makes sense, but I have to say that I became somewhat confused for a little while when I first approached the present day treatment of the basic Bernoullis Theorem. In part in order to incorporate the addition of vacuum energy into the basic equation of the theorem.

We are of course used to Po just giving rise to the ground state level of energy i.e., the mgh level of energy that the pressure head represents, when the fluid could be simply regarded as a mass in forward motion possessing the level of kinetic energy of forward motion given by 9mv2 that any mass would of the same weight travelling at the same speed.It therefore follows from this that the low side vector pressure that will exist when a fluid jet based on cold fluid is flowing will not necessarily arise because the molecules inside the fluid have become all aligned into the forward vector and therefore now exerting all their kinetic energy of translational motion in the forward vector, as in the case of a vapour flow, but because the internal Van der Waal bonding will be holding the molecules internally almost as though in the rigid structure of a solid mass. Similarly as in the case of a solid mass the pressure exerted by the fluid mass will only be in the direction of fluid flow. In other words the fluid flow will simply then become a medium through which the separate entity of the pressure head acting on the fluid, in this case the compressed vapour phase, can become transferred to the front of the fluid flow.In contrastwhilst the fluid is still in the random state then the separate entity of the pressure head acting on the fluid with no outlet will become distributed in all random directions through pressure 'distribution' forces, ie, molecular bombardments in all random directions and against all sides of the fluid containment with equal force, but then when an outlet is created for the fluid, then for the fluid that flows through the outlet all the pressure distribution forces will disappear (because then there would be no reaction forces off the sides of the containment vessel for the fluid flowing out of the exit) and all the pressure exertion by this fluid will be by the front face of the flowing fluid.Here there will probably be some equal and opposite similarity with the reaction force as for example becomes explained in the Mcgraw-Hill Encyclopeadia under Propulsion Principle, for more explanation another time.

The same as the above will be true to say on the addition of heat up to certain stages but then there will be differences and/or potential differences. The main difference being that it should then become progressively increasingly possible to streamline the translational motions of the molecules inside the fluid, initially in random motion in the x, y, and z planes, all into the x forward vector. Which in the case of the cold state fluid would remain

more I in their initial random motion state. Then when the heat and pressure are such that the fluid is in the liquid-vapour state perhaps full alignment of the molecules could be achieved.Indeed as the temperature and pressure approached the liquid-vapour state then perhaps it would become more necessary to streamline the molecules via special nozzle shaping internally because equally the molecules could become more prone to flying off the side vectors when the impulse fluid jet being created leaves the confines of the nozzle walls. It also follows from this that as the fluid changes from the fully liquid state to the liquid-vapour state on increased heat and pressure giving rise to increased loosening of the internal Van der Waal bonding then there could be a transition stage at which point it becomes fully necessary to fully streamline the fluid in order to maintain a low side vector pressure and a correspondingly high forward dynamic pressure.

in contrast to the fluid mass being held together by much stronger internal Van-der-Waal bonding on flow as in the case of the cold state fluid. However, this aspect should present no difficulty since such streamlining is achieved in the vapour phase where there is no Van-der-Waal bonding and on the contrary where repulsion forces of expansion exist between molecules, whilst in contrast in the liquid to liquid-vapour phase Van-der-Waal bonding will remain existing to some extent as the fluid approaches and enters the liquid-vapour phase.

However at this pre-practical stage it's a little difficult to fully speculate on the likely situation, but I draw such aspects to attention for the sake of better preparation for the practical stage.

qt this early stage it is of more interest and perhaps more relevant to continue on applying the basic fluidity equation, certainly it contains and relates most of the parameters that one may require for the practical application of the process, which is the purpose of it all and what everything is for in the end. Probably moreso than the Bernoulli's Theorem, which as far as I understand simply states that the sum of the applied energies on a system will remain constant on fluid flow, when of course they will be in a different form.

Thus, herein remaining with the application of the basic fluidity equation and then followed by some simple evolutions from the basic equation as may be more specifically applicable to this particular system. However, firstly the following discussion commences off in a more random general manner on related general themes of the process and then streamlines more specifically onto the theme of streamlining. Followed then by a section dealing more specifically with the application of the basic fluidity equation.

An aspect of the system will be that it will probably be important to have the fluid in the drum in a fully random state, by which I mean that all the fluid molecules therein would be travelling in all random directions under and with their translational kinetic energy of motions. For example as depicted under Fig. 37 on paqe 41 of the Open Universitv S101 Unit 8 course book.

blnce/unaer sucn conaltlonstne random pressure created by the random motions of the fluid molecules would then and thereby be maintained all the way back down the fluid flow to the compressor outlet, which in turn would be conditions that would enable constant pressure cooling during the heat removal stage of the porcess which may involve a stage of more rapid condensation of vapour phase to liquid phase as in a normal refrigeration cycle. However, the constant pressure would still be maintained under theSe type of conditions, as indeed in a normal refrigeration cycle.As for example becomes described in the text book 'Principles of Refrigeration' 2nd Edition, S1 Version by Roy J Dossat, page 109, Fig 6-15 appertaining and more specifically here the part thereof from D to E to E1 to A to A1 which becomes discussed on page 112

Basically the only difference between tnat circuit ana tne one unaer alscusslon for that part of the circuit is that on passing from point A1 to B the fluid in the text book circuit passes through a throttling device to lower temperature and pressure via the technique of flashing off a vapour phase, as explained in the text book, whilstin the system under discussion the fluid is being formed into a fluid jet at the equivalent stage A1 which then streamlines on to drive a turbine at the equivalent of stage B, to in this alternative way lower the pressure and temperature of the fluid whilst imparting energy to the turbine in the process by an amount which could potentially fully sustain the compressor stage of the circuit, i.e., the equipment between stage C1 and D. But apart from that difference and the fact that one would probably compress to a much higher pressure and thereby probably have the fluid in the liquid-vapour state above the Critical state at the stage of forming the fluid jet which in turn should render the fluid in a state better able to yield streamlining advantage, there would be little else different in these parts of the circuit.However, the other main difference will of course be that the heat that becomes removed from the equivalent of stage D, i.e., compressor outlet, to the equivalent of stage A1, i.e., prior to the sub-system stage, will become applied in a turbogenerator for generating power. The exhaust vapour from which then passing on to the heat collection unit, i.e., the equivalent of stage B to Cl in the text book circuit. To there become condensed before passing back to the turbogenerator for the next cycle of this fluid whilst in the process transferring the latent heat of the exhaust vapour back into the heat collection circuit and in turn in the process reducing upon the amount of fresh heat collection required each cycle for a given power output from the turbogenerator.Thus in such a manner of operation being dependant upon whether the sub-system will yield a level of energy approaching that required to sustain the compressor, but apart from that all other facets of the process are currently working in similar ways in existing processes and systems as shown by the text book example to which I have referred.

Furthermore, and to digress a little further from the themeofstreamlining, during my research via standard text book bibliography very recently whilst searching for subject matter on fluid streamlining I came across a text book in which the very concept that I am proposing here becomes theoretically suggested to a certain degree as a possible area for development into and for the future.

This being the text book 'Thermo fluid Mechanics', by Pefley and Murray on pages 270-71 thereof in relation to a similar refrigeration circuit as that discussed in the preceding on page 109 of Dossat. Where the Authors in fact suggest that it should be possible to replace the throttling device of the circuit with a turbine device. (To digress further, in the introduction to this section on page 268 the Authors also express their perception of the importance of the refrigeration of food in and for the advancement of civilisation, with which I am in complete accord basingonmy own personal experience and observations in parts of the World such as Djibouti However, here discussing the Authors views on the possibility for replacing the normal throttle device by a turbine harnessing system of some description.They state that the system would then essentiallv be the reverse of a normal turboaeneratina process. but that the

ylela rrom tne turbine m tne reverse cycle woula only Centre energy require to pump the liquid phase back into the vapour generator of the turbogenerating process. Which they state will be of. the order of 1% of the turbine outrut

tram the latter process, which in turn would be the level of energy required for the compressor in the reverse cycle.And fran this they conclude that the turbineyieldin the reverse cycle, i.e., as that under discussion, would only be 1% of the energy required for the compressor. At which one canmences to become somewhat disaroointed and one's eureka feelinas start to turn into

a pit at aespalr with the tnrougnt of several years endeavours in total/ontwmch so much hope for the future had been pinned turning out to have all been a waste of time after all. However, when one examines the work in the text book more deeply then one finds that the theoretical soundness of the work herein all but becomes fully endorsed, as follows.

The 1% level that the Authors state would in fact be correct for the water-steam system to which they are referring and would represent the normal mgh level of potential head enerav of the cold state fluid. i.e.. that to Dart the cold lianid phase back into the steam generator

VJOU {J/btehat which would be obtainable in the reverse cycle. The basic relationship with respect to this aspect being the ratio between the expansion energy yield of a given quantity of compressed vapour and the potential head energy that such a pressure would represent in terms of height of liquid. Therefore, firstly rechecking this for the main system example herein based upon R-21.Referring to the P-E diagram for this system on Fig. 2, for the reverse cycle one can see that the expansion energy to ground level would be of the order of 120 KJ/KG. Whilst to compare with this value the potential head energy expressed in terms of height of liquid that the pressure of COATS being considered would represent, which in turn would be the pumping in energy requirement for the cold liquid phase when being placed back into the vapour generator of the reverse cycle and which in turn would be the turbine energy yield of the cold state fluid in the process being considered, would be given as follows; P.E. = mgh ft. poundals/sec.

= weight x h in ft. pounds/sec = 2.2 lbs - i.e., 1 KG x (100 x 33.4) - i.e., the height, h that 100 ATS. represents* = 7348 Ft. pounds/sec.

= lOKJ/sec. for the flaw of each KG.

Thus, according to this value for every 1 KG of fluid vapour that expands through the turbine per second 120 KJ of ersersg would become produced, whilst the energy required to pump the cold liquid phase back into the vapour generator against the pressure of 100 ATS. would be lOUs for each KG of fluid required to become pumped back into the system per second, i.e, as the fluid becomes consumed per second so the fluid will require to be replenished at the same rate per second and the energy output to input will be in the ratio of 120 KJ/KG to lOKJ/KG of fluid throughput. Thus for this system the latter expressed as a percentage of the former would give a value of 8.33% however a possible source of error could be as follows.In arriving at the value of lOKJ/KG in the earlier work I deliberately didn't include in the calculation the difference in density between water and liquid R-21, i.e., 1 .Ogm/cc for water compared with 1.366 gm/cc for R-21, since I didn't think it would be correct so to do but here I had better explain this aspect further. On a cursory consideration it could be thought that the height, h, parameter required to be placed into the equation would be required to be less per lATS because of the higher density of R-21 liquid and not the standard value of 33.4 ft per 1ATS. as related to water, and as in fact applied in the above calculation in arriving at the value of 1OKJ/KG. And more specifically, be in the ratio of their densities.If so then the value of lOKJ/KG would become 7.32 KJ/KG.

Which in turn, whilst not totally knocking the process on the head in the way that a 1% level would, would nonetheless be a significant reduction and lower the potential for the process albeit still retaining some considerable potential.

However, I don't think the latter view of the system and the value derived from such a view would in fact be correct.

Consider if you will the vertical drum description with 100 ATS. of vapour pressure acting down on the heavier liquid phase of R-21 in its fully cold reference state, which we will imagine is a system state brought about by the removal of the heat at the heat removal stage of the process all the way down to the ground state of the cold state reference fluid under constant pressure cooling conditions to where iust the mgh energy value of the pressure head would be

obtained, i.e., from D to H on Fig. zl, as in fact in a normal refrigerant rerrlgeration cycle, e.g., as that on page 109 of Dossat. Thus, if one visualises such a system then if anything the heavier fluid would add to the normal level of output relative to basing upon water because one would still have 100 ATS.

of vapour pressure continuously acting down on the liquid phase, which if a system based upon water would be calculated to represent a potential head height of 33.4ft. for every 1 ATS. of the pressure. Therefore, the fact that the densities of both the liquid and vapour phases of R-21 are higher than water and steam respectively would not make any difference to the mgh value that the 100 ATS. of vapour pressure acting down on the liquid phase represented and if anything could add to the potential energy mgh value via the effect of gravity acting on the heavier liquid phase which in turn would be equivalent to an additional quantity of mgh energy, with the total then being the sum of the two mgh energy values.To reiterate and emphasise the main aspect, a lOOATS. of vapour pressure would still be acting down on the heavier liquid, each 1 ATS. of which still being equivalent to 33.4 ft of water, which in turn would therefore be the correct height to place into the potential energy equation for this system even though the liquid phase would be heavier itself of which one would only require 33.4 x 1/1.366 = 24.45 ft to give a potential energy height equivalent to 1 ATS. fior 14-21.

However if the drum was in the horizontal position then one can imagine that the force of gravity could perhaps drag the heavier liquid down as the fluid jet flows to the turbine, to perhaps detract from the impulse force in the forward vector, albeit very unlikely for a fast flowing jet.

Thus, whilst for the vertical drum system at least the pressure head energy and therefore the energy yield could well be higher than the value of lOKJ/KG, because remember the licuid phase would become produced about halfwav alone

tne cooling stage/temperature arop, ana therefore cauia potentlally/aoo quite a height of heavy liquid potential energy under the vapour pressure of 100 ATS at this early stage I have based on the value of lOKJ/KG for this parameter of the system. Then from this value the ratio of compressor input to turbine yield becomes that of 120 KJ/KG to lOKJ/KG, i.e., the latter 8.33% of the farmer.

However. there is still the fact that the Authors of the text book state a level

or tne oraer or la ror me adore value, DUt more speclrlcallylul relatlon to the reverse cycle for the pumping in energy for the liquid phase in comparison to the turbine energy yield of the subsequent vapour phase expansion. Which in fact would be true to say for the water-steam system that the Authors are considering.If one studies Table 12--1 given on page 250 of the text book in ccibination with the third diagram given under Fig 12-2 on page 248, i.e., the P-E diagram for the system, then one can compute that H2 - H1 will equal 165.8 - 161.2 = 4.6 Btu/lbm, which would be the pumping in energy requirement for the cold liquid phase against the steam pressure of 1500 psia, i.e., roughly 100 ATS. Then that H3 - H4 will equal 1814.2 - 1143.3 = 670.9 Btu/lbm, which

would represent the output/ trom the pressurised steam at H3 expanding and finishing at H4. Therefore, basing on these values then for this system the pumping in energy requirement would only be 0.69% of the turbine energy yield level.

However, the process that I am discussing is not a water-steam based system but rather an R-21 based system and therefore, whilst the equivalent pumping in energy for the latter system would in fact be the same or similar, a very different ratio will exist between the input and output energies of the reverse turbogenerating cycle per KG of fluid throughput because whilst the pumping in energy will be the same or similar the energy yield per 1KG of expanding vapour will be of the order of 10 times less, (an aspect which becomes discussed under my PA 8728601), and therefore the ratio of pumping in energy to output energy will be of the order of 10 times higher for this system. More definitively, lXT/KG = 0.4299 Btu/lb. Therefore expressed in such terms the preceding values for the water-steam system would be 10.7 KJ/KG pumping in energy yielding 1560 KJ/KG of steam expansion energy. While for the R-21 based system the equivalent pumping in energy would be the calculated value of lOKJ/KG, which therefore is the first aspect that becomes confirmed by the work in the text book, but then each 1 KG of liquid phase becoming pumped in would only yield 120 KJ/KG of vapour expansion energy and therefore the equivalent ratio would become lOKG/JG to 120 KJ/KG to give a value of 8.33% for the former in relation to the latter, which for the water-steam based system was the value of 0.69% for the equivalent ratio in that system.

Thus, the value of lOKJ/KG for the mgh potential energy level of the cold state reference fluid would seem to become confirmed by the work in the text book, a value on which I have based the whole of the work herein to date which therefore is also becoming to be confirmed by the work in the text book.

And a further potential source for bonus energy has become revealed thus far, i.e., that of the height of condensed liquid phase adding to the 100 ATS. pressure before the sub-system stage. However, this cross-check on my work up to this stage only goes as far as confirming the potential of the system for acquiring the normal mgh energy level of the 100 ATS. pressure head and as would be yielded ỳ the cold state reference fluid, although in so doing also serving as two very good second opinions on the soundness of the basic concept at least.

herein I am mainly concentrating on the hot fluid method of operation but in fact it is not intended to depend solely on this method of operation and following under a subsection entitled 'Other possible Methods of Operation' I propose that a further approach could be to remove as much heat as possible to bring about constant pressure cooling of the fluid all the way down to ground state then obtain from this fluid the normal mgh energy value of the pressure head, to in turn be the output from the process.Because via such a method of operation the energy that one could generate from the maximised quantity of removed heat, from D to

H on Fig is, via a normal turtenerator should be sufficient to continuously fully sustain the compressor stage of the process, i.e., the energy input required from B/C to D on Fig 2, at a 40% one-pass heat conversion efficiency level. And especially so if becoming converted via a low Bpt. turbogenerating fluid, e.g., R-ll of Bpt 240C and as becomes discussed under my PA 8728601.However, a 40% conversion level for the removed heat from D to H would be 124 KJ/KG and the compressor input from B/C to D would be 120 KJ/KG, whilst the turbine yield from the sub-system would be lOKJ/KG. Therefore, whilst on a cursory examination one may think that this way round of operating the process would be bound to at least yield the normal mgh energy level that would be associated with the sub-system the process may in fact be bordering on reality, and even if it did yield the sub-system mgh energy fully for output supply it would be some 3 times lesser an amount of energy than potentially yeildable by the hot fluid method of operation. Which again on a cursory consideration seems an impossible level of improvement but not when expressed in absolute terms, i.e., the hot fluid method yielding 30 KJ/KG for output supply in comparison.Thus again bordering but now there would be 20 KJ/KG of energy yield that could become recycled back into the system before this way round of operation would yield the low level of 10 KJ/KG for output supply. Thus it may seem as though I am splitting hairs here but the extra 10 KJ/KG in the total of 310 KJ/KG energy from D to H would tip the balance and make all the difference, one could even say a world of difference. But for the world to obtain this bonus then it would be expected that they would have to achieve bonus energy in the process, hence my deliberations to try to push the process across the borderline region and well into the output region via endeavouring to determine various potential sources in the process where bonus energy may be obtainable.Because one would also expect that if the process can be pushed well into the output region then its potential usefulness would become rapidly increased upon, and especially if and as one of the final process types of Kingdom Come on Earth. A very apt anology being that of 20 shillings and sixpence expenditure in the pound, hell, whilst 19 shillings and sixpence expenditure in the pound can and does lead to heaven on Earth. However, pressing on with the discussion on the text book work.

h'hilstthe foregoing confirming conclusions have been arrived at based upon the Authors example treatment of a water-steam system on page 250 of their text book and basing on which the Authors state the level of 1% for the pumping in energy yield and corresponding turbine yield of the reverse cycle, their actual calculation example for a system in which they replace the normal throttling device with a turbine on pages 270-271 is in fact in relation to a refrigeration cycle based upon the refrigerant R-22. Therefore, examining this example further.

Firstly, from the example and the description text on page 270 it can be gathered that the Authors in fact assume that the whole of the enerqv from the H1' will

become converted into turbinelon replacement of the normal throttling device with a normal turbine arrangement. In other words, that on forming a fluid jet with the fluid at stage H4 on the P-E diagram the whole of the P-E down to ground state at H1' on the saturated liquid line will become converted into turbine energy with the fluid therefore finishing in the fully liquid phase and no vapour flashing taking place giving the further advantage that a lesser amount of total fluid would then be required to circulate around the refrigeration cycle.Thus in this example and on which they base their estimations the Authors assume that the fluid state on ilrwrting energy to the turbine\rlou(d fully follow the saturated liquid line on the P-E diagram. However, the Authors of the text book go on to conclude that a highly efficient turbine must be developed before it could successfully replace the normal throttling valve. Thus, I will endorse this view by stating my view that the energy yield on fully following the saturated liquid line, which in fact will represent the normal curve of the normal cooling curve as later became5further discussed, is likely to represent the potential maximum energy yield from the system and among other aspects would require an efficient turbine to fully acquire.The amount of energy from H1 to H1' is given as H4 - H1' = 34.62 - 33.71 = 0.91 Btu/lb. Which in their calculation then represents the potential energy yield from the turbine substitute in the cycle of the process. WhiUfthe energy required for the compressor input is given as H3 - H2 = 118.2 - 107.24 = 11.0 Btu/lb. Therefore in this very example it can in fact be seen that the potential for turbine yield to the compressor input requirement would be in the ratio of 0.91 to 11.0 Btu/lb, i.e., now at a level of 8.27% for the former expressed as a percentage of the latter. Which again is in good agreement with my example cycle on Fig 2 herein in relation to a cycle based upon R-21.When close to the equivalent ratio will be the calculated value of 10 KJ/KG for the normal energy yield to be expected from the cold state reference fluid, i.e., the yield from H to A, to the compressor input requirement from state B/C to D of around 120 KJ/KG. Which expressed as the equivalent percentage becomes 8.33% and therefore is in some good agreement with the energy balance of the cycle in the text book example. Which therefore can be regarded as a further very good second opinion cross check for confirming much of the work becoming evolved, postulated and proposed herein.However, the work under the text book does not really verify the energy yield that could be expected to be obtained on the use of comparatively very hot fluid, and moreso relates to and therefore moreso confirms the method based upon cooler fluids, although I imagine that the Authors would still assume that on the use of hotter fluids they would still follow the normal cooling curve on imparting their energy to a suitable turbine.

On examining the calculation on page 271 further one can see that the turbine yield, i.e., that fran H4 to H1' = 0.91 Btu/lb, expressed as a percentage of the heat absorbed i.e., that from H1' to H2 = 107.24 - 33.71 = 73.53 Btu/lb, will be 1.23% energy yield to the heat energy required to be absorbed to yield such an amount of energy. Which would be the case if the heat energy that one could remove from H3 to H4, i.e., a total of 83.6 Btu/lb, would be sufficient to generate sufficient power to continuously drive the compressor of the cycle via a turbogenerator based upon an appropriate fluid.Since in this cycle the compressor input requirement from H2 to H3 will be 11.OBtu/lb then one would in fact expect to be able to obtain such an amount of drive energy from a maximum heat energy quantity of 83.6 Btu/lb because the thrbogenerator one-pass efficiency would only have to be 13% if all the heat energy were harnessable. Which will be rendered far more possible by the fact the exhaust vapour of the turbogenerator could and would be fed to the heat collection unit for condensation back to the liquid phase ready for the next cycle of the process wherein the refrigerant would be at a

temperature of -6.7 C if the same cycle, aepicteo on pages 270/271 of the text book.Therefore a relatively very low Bpt. fluid could be used in the turbogenerating process in comparison to a water-steam based process for maximised harnessing of the heat energy from H3 to H4 on the P-E diagram on Fig 12-15(c) page 270, and one would still be able to condense the exhaust vapour readily even if the condensation temperature of the exhaust vapour is below OOC, which we will assume exhausts at 1ATS. but obviously one should also be able to readily add condensation vacuum energy. In fact very readily because the cold refrigerant fluid could be applied in the normal cooling tube method, i.e., as the method depicted on Fig 71 page 203 of, 'Heat Engines and Applied Heat' by F. Metcalfe for example.

Thus perhaps R-114 of normal Bpt. 3.770C could be applied as the fluid in the turbogenerating process which should then enable the harnessing of at least 50% of the heat energy from H3 to H4 and if 40% one pass conversion efficiency is achieved then the energy yield would be: 83.6 x 0.5 x 0.4 = 16.72 Btu/lb With only 11.0 Btu/lb being required for the compressor input. Therefore the efficiency for this stage of the process need only be 66%. All of which therefore could be very much within the realms of possibility, to leave remaining the energy yield from the turbine substitute in this cycle for output supply, i.e., the quantity of 0.91 Btu/lb. Which may seem a small amount against the heat collection each cycle, i.e., the heat energy from H1' to H2, 73.53 Btu/lb, which expressed as a percentage would be 1.24%.However, when one takes into account the recycled latent heat from the exhaust vapour of the turbogenerating process then expressed against the fresh heat input requirement each cycle the equivalent percentage efficiency value would become approximately;- 0.91 x 100 = 1.88% 73.53 - (83.6 x 0.5 x 0.6) Which is still somewhat low, but these estimations are based upon only 50% of the heat energy from H3 to H4 becoming harnessable whilst 80% could well be feasible via use of the correct BPt.fluid in the turbogenerating process.

And especially so because if one looks at table 12-2 on page 271 and the second column of figures thereof dealing with temperature in conjunction with the P-E diagram Fig 12-15(c) on page 270 and also the fourth column of energy values then one will be able to gather that the temperature of the heat beconing removed will carmence at 1r0O F but then wont be required to lower all the way down to ground state as the heat becomes removed but will soon reach 800F then remain at this temperature all the way to state H4 due to the bulk of the heat being in the form of latent heat of condensation. This then is a very important aspect to be aware of and could well render 40% of 80% conversion of all the heat energy from H3 to H4 being very possible.Which if so would not only reduce further upon the fresh heat input required each cycle but a surplus of energy could be obtained over and above that required for the compressor to add to the yield from the turbine substitute for output supply and on both counts substantially improve upon the low level of 1.88% efficiency for this process.Thus, calculating for 40% of 80% conversion as follows: The amount of energy rendered available for the compressor would become : - 83.6 x 0.8 x 0.4 = 26.75 Btu/lb Whilst that required for the compressor would still be:- = 11 Btu/lb Which at 70% recycle efficiency would leave remaining : - 11 Btu/lb to add to the 0.91 Btu/lb becoming produced by the sub-system, giving a total of l2Btu/lb for output supply.Whilst the fresh heat input requirement each cycle would become reduced to: 73.53 - (83.6 x 0.8 x 0.6) = 40 Btu/lb Therefore, for a process based upon R-22 and operating exactly the same cycle as that depicted on Fig 12-15 (c) the output efficiency expressed in relation to the fresh heat input requirement each cycle could become: - 12 x 100 = 30% 40 In fact basing on this example calculation the sub-system needn't yield any energy for the system to be very worthwhile since it only represents sane 8% of the output anyway, and the above output efficiency level would only become reduced to 27.5% even if the sub-system didn't yield any energy.

Can all this be true I ask myself? Perhaps, and if so I may have got onto a wrong track in endeavouring to operate the system with hot fluid at a high pressure at or around the Critical Region since what the process could boil down to in this text book example is simply generating turbine power with the heat energy from H3 to H4 using half for powering the compressor and half for output supply, without even needing to bother about any energy yield at the equivalent of the subsystem stage in the cycle and still achieve an output supply as high as could be achieved via other methods of operation.Thus it follows that in this cycle one could perhaps go back to the use of a normal throttling valve to depressurise the liquid although obviously one may as well obtain the value of the P-E energy as turbine energy to give the further advantage. So can all this be true I ask myself again? On further consideratior probably only partially since firstly the heat transference in such a system is likely to be closer to 7096 at a maximum and secondly at a maximum temperature of 1100F,, i.e., 430C, one wouldn't be able to achieve 40% conversion efficiency via R-114 and one probably couldn't apply a turbogenerator fluid with a much lower Bpt. to endeavour to improve upon the one-pass conversion efficiency.

Or if one went down this road then the exhaust vapour would soon have to be at elevated pressure for condensation to be achieved and therefore the amount of energy transferred would be less by such an amount and one wouldn't then be able to add condensation vacuum energy. In the absence of full data, since the critical temperature for R-114 is 145.70C then a 10% one-pass efficiency even with added condensation vacuum energy is really the maximum yield that one should expect, and with respect to this aspect I refer readers to my work related to Fig 11 under my PA 8728601. Therefore carrying out the foregoing expercise for a conversion rate of 10% of 70% of the heat energy from H3 to H4, which would be realistic for the starting estimation for a process based on this particular cycle, but obviously would be improvable upon in a number of ways.

The quantity of energy rendered available for the compressor would be:- 83.6 x 0.7 x 0.1 = 5.8 Btu/lb Whilst the compressor would still require 11 Btu/lb and the subsystem would still only be yielding 0.91 Btu/lb. Therefore, now in possible reality the process would not work at all and we have therefore gone from an all time high to an all time low in the space of one little simple calculation. Which is almost more than I can take. However, there of course is still the reality of the much hotter fluid method of operation, and of course this would be one of the ways, indeed perhaps the only real way to try to improve upon the R-22 system. Thus one would compress the fluid further so that H3 on Fig.

12 - 15 (c) rose up tbeRHS of the P-E diagram until the optimum point was reached for this particular process. Whilst herein and at this early stage I don't intend to carry out a detailed examination of this aspect, although one will be required later, the optimum position may be as high as the Critical Point level or higher, or even a little lower. Perhaps even moreso now at the Point of Maximum leaning Over Backwards, i.e., at the PSB Point, referring to any exercise under Fig. 11, PA 8728601. Although perhaps just a little higher up in this case which would be in keeping with the equal and opposite similarity factors of the work.In any eventthesensitivity of the optimum position is likely to be as critical as shown in the exercise on that process, in equal and opposite similarity and therefore one could expect equal levels of improvement in relation to this aspect of the system. Ranging from say conversion efficiencies of 10% of 70% of the heat to 40% of 80% of the heat.

To then in turn give rise to the overall process ranging from impossible to around a main of 30% efficiency output to fresh heat input. But I hope readers and mare specifically experts in the various fields concerned will agree that this could be a very realistic estimation of expected performance basing on the work herein.

Therefore, whilst I nearly began to conclude, now with mixed feeling of exuberance and exasperation in contrast to despair, that perhaps one need not endeavour further than the very example process given under the text book based upon R-22 it would in fact be necessary to strive to achieve the optimum position for the process and this in turn may necessarily take the operating conditions into the Critical stage region and to much hotter fluid, higher pressure, conditions. Therefore, I of course intend to complete and present my planned work on this process.

Perhaps needless to say the particular text book being referred to here was in fact one of the last that I looked at whilst and for working on this project, which I obtained from Edinburgh's Central Public Library towards the end of April '88 and until that day had never seen the text book before. Which I additionally inform because this text book also refers to a system very similar to that of the ARC cycle in my PA 8728601 on page 259 and which I briefly garment on in passing.

Thus, the example system in the above text book based upon R-22 is now moreso beginning to confirm the soundness and feasibility of the process concept under discussion herein, but of course the system theorised upon in the text book is not based upon very hot fluid at the sub-system turbine stage but becomes a condensed liquid phase at 800F, i.e., 26.70C, under a saturated vapour pressure of 11 ATS. passing to depressurised colder liquid at 200F, i.e., - 6.70C, at 4 ATS. on the exhaust side of the turbine in this particular refrigeration cycle, having transferred the difference in P-E energy to the turbine.However in the ground state of the cycle being 4 ATS. then to some extent this work also confirms the soundness and feasibility of the proposed method of operation for very low Bpt fluids, the example herein being that based upon R-13 operating under an elevated ground state pressure of 20ATS., which in turn could give rise to bonus energy becoming more readily achievable in the ways discussed herein.

Thus the Authors example is not based upon hot fluid, but nonetheless they assume that on the transference of energy from the fluid to the turbine the fluid state will depressurise and cool along the normal cooling curve and impart an amount of energy equivalent to H4 - Hill, and therefore the Authors would presumably assume, as I, that the fluid would still follow the normal cooling curve for the system if commencing with very hot and highly pressurised fluid at above the Critical State region on the P-E diagram, Fig. 12-15(c).

When this particular system based upon R-22 may then also be found to give a better energy balance in the 20-30g6 efficiency region when relating to the fresh heat intake each cycle, and therefore obviously more detailed work is required on such aspects than I propose to carry out herein, nor could at this stage in the absence of all the necessary data and P-E diagrams, etc.

Thus suffice it to say that the text book example and the work and treatment therein under pages 270-71 coupled with that under pages 246-250 would seem to all but confirm at least the soundness and feasibility of all the work that I have undertaken and conducted herein, although not fully for systems based upon very hot and highly pressurised fluids. However I think sufficiently, and intentionally so, at least with respect to very good second opinions on the theoretical soundness of the work via extremely eminent people in their fields and professions, if not yet in practice. These being the Authors of the text book i.e., Professor Richard Kramer Pefley and Associate Professor Robert Ian Murray University of Santa Clara Stateside, 1966.

Obviously I haven' t had an opportunity to study the remainder of this text book in any depth and as previously stated the main reason for my search through text book material on this particular occasion was in fact to try to find subject matter on fluid streamlining at a molecular alignment level and this text book deals with this topic to some extent under Chapters 5 and 6 mainly which I will refer to again in the ensueing discussion dealing with this aspect of the system, e.g., Fig. 6-7 (a) on page 115, which corresponds to the stage in the process where the fluid leaves the drum and enters the nozzle.

However, I haven't yet cane across any material relating to the practical harnessing of the P-E energy of hot liquids under high pressures, which in fact is a system type that occurs in other parts of the work that I have undertaken and am contbrcting, e.g., The Lift System of the work. Moreover, as the Authors of this text book state in their preface, the field of 'Thermofluit" Mechanics' is a relatively new emerging field uniting together the much longer estabished fields of Therrrynamics and Fluid Mechanics, which could be said to be precisely that which the work herein endeavours to achieve. Thus it follows that this process in particular could play a central major role in this

ene 53 fluid in the future, although most of the work that I have undertaken and am conducting would in fact also form a part of this particular newly emerging scientific and technological field.Thus, I propose to complete my early stage work on the hot fluid method of operation, whilst pointing out that perhaps the colder fluid method in which one has the sub-system yield as the output from the process with the compressor becoming sustained by the turbogenerating energy yield from a maximised amount of removed heat and any surplus energy at this stage adding to the output energy, would be at least the forerunner if not remaining the main method, which I discuss further in the later sub-section dealing with other methods of operation.

Moreover, perhaps the forerunner could be based upon the very cycle in the aforementioned text book on page 270/71 in the ways discussed and applying R-22 in canbination with a suitable turbogenerator fluid, e.g., R-114. Which would then be in keeping with the Catch-22 situation having been caught.

However, undoubtedly the hot fluid, high pressure, method of operation would give the highest overall energy balance in the fullness of time, to then give all the higher potential applications discussed in the final section of the work herein. Thus I think that I am correct in having opted for operation of the system with hot fluid at and under a high pressure at or above the critical region. Not only because this would render the fluid prior to the sub-system in the liquid-vapour state and therefore probably more able to impart energy with a higher transference efficiency, but also because this would then render the temperature of the heat removed sufficiently above that at which thesround state of the turbogenerating process would necessarily have to be.To then in turn enable the heat to be converted at the maximised level of 40% efficiency with respect to the one-pass efficiency, which would be necessary in order to raise the energy balance of the overall process into the surplus region, and undoubtedly potentially could in my opinion. But perhaps requiring of a low B.pt. fluid in the turbogenerating process in order so to do, e.g., R-ll as in PA 8728601.

An aspect that I have realised whilst carrying out these particular deliberations is that when harnessing the normal potential energy of the pressure head via cold state fluid giving just the mgh energy yield associated with the pressure head I think the liquid must lose some accompanying temperature heat along with loss of the pressure head basing on a P-E diagram picture of such a system.

However, I'm not sure and those with practical experience in the hydropower field could obviously be more definite about such aspects, but if so then for water the temperature drop could be around 50C and for such fluids as R-21 and R-22 around 100C for the energy yeild level of 1OKJ/KG accompanying a pressure head loss of lOOATS. However, obviously I can't deliberate on every aspect of the system too deeply at this more general stage and therefore now progressing on with the discussion a little closer to the more specific objective of endeavouring to acquire a streamlining advantage in the process.

Streamlining Advantage coupled with more general discussion: Basing on the preceding deliberations with respect to pressure maintenance, for this further description I will visualise a fairly large CSA drum with therefore a large surface area drum base. Then a ccmparatively small CSA fluid jet creating nozzle protruding out from the centre of the driin base horizontally orientated, and initiallyanozzle entry similar in design to the Bellmsuth design given under Fig 6-7 on page 115 of the aforementioned text book and giving very minimised fluid flow resistance through the shaping of the nozzle entry at the actual point of entry of the fluid flow into the nozzle.

To be frank I am not in fact sure how to approach this section and at this late stage in one sense and early stage in another I don't propose to delve into text books too deeply in search of possible related subject matter, at this juncture anyway. However, I have in my mind an approach mainly basing on the basic fluidity equation coupled with a little more of my past experience, which however may not be correct, and/or only correct to a certain degree, and/or wholly correct. Thus it is possible that the following treatment could be deemed to be valid and correct and if so could potentially be the basis for a possible new approach to certain aspects of fluid mechanics and in particular departing from the Navier-Stokes Equation and related approaches, for example as becomes discussed in the text book 'Fluid Mechanics' by Frank M. White on pages 218 to 259, 'The Liquid State' by Dr. J.A.Pryde on pages 145 to 150, and 'Fluid Mechanics' by Shame under Chapters 8 and 9 for example.

All of which however, of course woody approaches that could become applied to the system at a later stage in the development of the process. But herein it is intended to substitute with a potentially possible less complex and simpler approach based upon the basic fluidity equation into which one incorporates an approach to potentially possible fluid extension on streamlining similar to the basic approach of the Shear Modulus, the Bulk Modulus and the Poisson's ratio, etc. That is, applying the type of treatment to this system that becomes discussed under the text book 'Concise Physics' by R.B. Morrison on pages 54 to 58 for example, incorporated into treatment by the basic fluidity equation, as becomes further elucidated upon in ensueing discussion.Thus, the fact that it may be intended that I should be instrumental in laying the foundation for such an approach to the system is really the reason why at this juncture I simply propose to evolve the approach that I have in my mind to evolve, but it should be bourne in mind that it may only be partially correct if at all and that I have had no formal training in fluid mechanics. However, as an additional pointer James R.Crompton Bros the PaperMakers for whom I used to work could perhaps also place two and two together and ccxne up with four here rather than five, since there I conducted R & on long fibre material involving fluidity testing at the research stage and then later modulus testing at the early further development stage, in passing also coming up with nit creation in the laboratory via vortex simulation, hopefully all eventually leading to nit free and improved long fibre papers and advancements in non woven fabrics nit free.However, should my work and treatment of herein receive the general thumbs down treatment all round then in the further way that I intend to approach the continuance of more of my early stage general development treatment herein, which could perhaps be deemed analogous with BGS energy, it should at least be useful in unveiling the system further even if incorrectly, and in any case should perhaps be viewed as the first stages of simply coranencing to dig some of the initial trenches for the foundations of a possible new alternative approach to the new type of system under discussion herein, which perhaps would be deemed to be more practically orientated as indeed the whole of my research and development stage on my concepts under discussion herein.

On the other hand, perhaps it is the case that Navier and Stokes, as Poiseuille's also of the 19th Century enlightenment period, intentionally evolved a more complex approach to fluid flow mechanics to that of Poiseuille's of 1840 with some degree of rivalry in mind which perhaps has given rise to an incorrect lead to those that followed. Whatever, my feelings are for Poiseuille's and His equation.

A further relevant aspect and dimension being the fact that I perhaps more so than others believe in the natural order of basic relationships of parameters as evolved during the creation and evolution of an ordered Universe and our World therein and of course necessary in order to maintain the steady state of such order. Then and thereby in the final happy steady state, of which Mankind progressively becomes involved, all laws governing all order and containing parameters as happy as they can be with all other parameters. Of course when Mean first commences to harmonise with Nature then all parameters do not usually carrnence off being fully happy with each other and it usually takes some time for a harmonious and happy steady state relationship to eventually evolve. So it is between Men and Machines and the laws of Nature governing the parameters of the concepts, materials, flaws, masses, and fluids that Man endeavours to apply in his Machines. But as those Machines became closer to the ideal happy state within their environment and Nature so the relationships of the parameters concerned and governing Man' S machines,should in theory become closer to the basic parameter relationship laws of Nature once again.

I suppose in a sense I have the same relationship with and feelings for science and technology that real doctors have with their fields of science and towards their patients. After all, science and technology should ultimately all be directed towards the good health of the Planet and the people thereon, which of course includes all the more luxury items thereof. Scme of which are as essential for good health and the maintenance of good health as the basics these days. However and therefore pressing on.

One such law of Nature being the discovery by Poiseuille's in 1840 of the relationship of parameters governing parabolic fluid flow in a pipe. Which therefore may not seem all that applicable to the system under discussion an a cursory consideration. However, I hope to show in the following exercise that it could be, but perhaps the more immediate usefullness of this exercise will be at least to reveal the system further. As for laying the groundwork for a new approach it is probably more true to say that I am probably resurrecting a potentially possible old approach for application in5anew system.However, it follows fran the foregoing thoughts that all things should eventually approach simplicity once again and not ever progressively increasing complexity, although probably inevitably after reaching a peak of complexity in the uphill struggle, which is probably where the peoples of the world are at the present time in general in all things including Man' s entanglements with Nature and Nature's Laws. Assuming this then it is probably right to now aim for simplicity once again as in the following exercise for example, which in a further analogy hopefully could became regarded as a Bellmouth entry stage to one's nozzle.

Not that I have any real objections to more complex approaches, nor indeed could, nor that they are beyond me with the reservation that I am only at

one withlsense, but I have simply taken the simple view that if they are not really necessary for the practical application of a process nor for the practical progress of the process and in general then why bother with them, to leave my brain and time free for the more inventive, general and such entrepreneurally spirited aspects. Perhaps for such flora to become added at a later stage.

That required for practical application and practical advancement and progress being that which everything should be forand boil down to in the end of course.

Whilst in equal and opposite contrast in Dr. Pryde' s text book on the Liquid State for example some approaches are said to have no solution. However, I'd better continue on with that which I have in hand.

The basic thesis that I intend to evolve and deliberate upon here is in fact very simple and sunarisable as follows.

A basic premise is that for fluid jet energy to be yielded by an amount which is equivalent to the kinetic energy content of the fluid then it would obviously be better and more achievable if the initially random kinetic energy content became all streamlined into the forward vector during the fluid jet creation stage. Then a further premise being that in contrast the cold state reference fluid will only yield the potential energy that the pressure,head represents

although in the process some Kinetic

'become trans ferredt Which however could possibly correspond with the kinetic energy already facing in the forward vector of the random state of the fluid.In which case one could still assume that in contrast the cold state reference fluid will remain fully in the random state and not become nor be as streamlinable in the forward vector in the

same way oue to the higher internal Vanwcler Waal tanning teing to'retrain the random structure of the cold liquid on flow. Then one would expect the cold liquid to simply be as a mass with respect to transference of energy and since the cold fluid imparts the energy that an equivalent weight would fall from the height that the pressure represents then one can assume that the cold fluid retains in the random state in such a system where this is the case.

Whil in the case of very hot fluid at or above the Critical region where the liquid behaves as though a vapour and where, therefore, there wouldn't be any effective bonding between molecules at such a stage in such a state then the molecules of the fluid are bound to be far more alignable all into the forward vector. Which is that which I mean by the term streamlining.

Now if during the fluid jet creation stage one can bring about a high level of fluid streamlininq over and above that which normal lv takes place on normal

riula; ana to wmcn a normal rlulalty value relates, tnen tne rlula Jet velocity will be higher and be capable of imparting more energy to the turbine than would the fluid jet velocity associated with the normal fluidity value.

However, from the preceding work on the fluidity equation giving rise to the fluid recycling technique we know that for a nozzle CSA the same as that required for the cold fluid for a mass flow rate of unity with the canpressor, then the fluid jet velocity associated with the normal fluidity value would be that required to give fluid jet energy equivalent to the P-E content of

the system. However,; one wouicn.t expect mucn molecular streamlining to be associated with the normal fluidity value and more specifically all the kinetic energy content to become all facing in the forward vector to give a normal fluidity value and yet the velocity of the fluid jet associated with the normal fluidity value for such a nozzle CSA would equate to the P-E content of the system.Following I will be using the classical description of cylindrical elements of fluid becaning forced forward by the pressure head from the drum into the nozzle and if one considers the system in this light at this stage then one can offer an explanation for the foregoing as follows. Because the fluidity value of the fluid is 4.5 times higher than that of the cold state reference fluid then this in practice will mean that the pressure head will be able to force cylindrical elements of the fluid forward from theirbonding with the bulk of the fluid in the drum at a 4.5 times faster rate than in the case of the same sized cylindrical elements of the cold state reference fluid.In other words the bonding forces around the outer surface area of the cylindrical elements of fluid in the case of the hot fluid will be less and such as to cause the cvlindrical elements to be

forced forward at a 4.5 times faster rate under the same pressure and throuah

the same sized nozzle.Which therefore is a mechanism that/haXlittle if anything to do with rrolecular streamlining to achieve fluid jet energy equivalent to the kinetic energy content of the fluid. But of course the mass flow rate in such a case would be 1.8 times higher than mass flow rate unity with the compressor and therefore the fluid jet energy level will be being fully achieved as a result of the r to the four advantage factor that will be present for such a nozzle CSA, 1.8 times larger than that required for a mass flow rate of unity. Now if we reduce the nozzle CSA to give a mass flow rate of unity then we know from the preceding exercise that the normal fluid jet velocity associated with the normal fluidity value is likely to become reduced to 3.36 times velocity units. But remember so far this has little if anything to do with the potential for additionally being able to achieve a high level of molecular streamlining during the fluid jet creation stage according to the above theorising in relation to cylindrical elements. The view here being that of the drag factor of a higher level of slower velocity fluid surroundinc and associated with the narrower cylindrical elements of fluid becoming increased upon with narrowing cylindrical elements as in earlier discussion, but it is also helpful to keep in mind here the nozzle blanking off description which will apply but with the above increasing drag factor associated with the r to the four element the more one blanks off the narrow the nozzle and therefore the cylindrical elements.In other words, the aspect to also have in mind and be aware of is that the velocity would remain at the 4.5 times velocity level on reducing the nozzle CSA but for the associated increasing r to the four drag factor surrounding the cylindrical elements of fluid the more one blanks off the CSA of the nozzle.

Therefore it follows that if a high level of molecular streamlining can be achieved during the fluid jet creation stage then this could boost the fluid jet velocity back up to the 4.5 times level fry'that of 3.36 times on reduction of the nozzle CSA to give a mass flow rate of unitv. And indeed could rotentiallv

similarity improve upon the fluid jet energy for the1 system in which one/ nstee the nozzle CSA the same as that required for the cold state reference fluid.

It is perhaps notw4coincidence that according to an earlier exercise that I have carried out

I determined that if one took a cube of fluid and aligned all the kinetic energy therein, i.e.,-all the molecular translational motions, from all the y and z vectors so that they added to those already facing in the forward x vector then the cube of fluid would effectively become a longer and thinner cuboid shape 1.73 times longer in the length direction at the pro rata expense of CSA in the y and z planes of the fluid cuboid.

which for the purposes of these particular deliberations I will round up to 1.8 times.

the same factor associated with the nozzle reduction to qive a mass flow of unity, or conversely and more relevant here the same as

the nozzle increase that wculd/be required from that required to just give a mass flow rate of unity with the compressor to achieve a fluid jet velocity of the required energy value resulting from the then reduced r to the four element in the fluid jet flow.Remeniber the fluid jet would be raring to go forward if it wasn't being held back and that with a larger CSA nozzle then it wouldn't beocme retarded quite so much The conclusion therefore being that commencing with a nozzle CSA that gave a mass flow rate of unity with the compressor then there could be tWD main and basic ways to improve upon the fluid jet velocity, which with such a nozzle CSA is likely to become reduced from that required of 4.5 to 3.36 times velocity units, and then by a canbination of both.

(i) One being by remaining with the same nozzle CSA but inducing further streamlining irrrto the fluid flow when the same flow rate of mass will extend further into the forward vector, which will then have the effect of accelerating the velocity of micro masses of the fluid to a higher velocity. A way to visualise this is to consider the cube of random fluid entering the nozzle and then extending in the length direction to became a longer and narrower cuboid shape containing the same mass then, whilst the mass flow rate would remain the same, the fluid jet length created in unit time from each unit of mass would be longer, i.e., the velocity of the fluid jet would be higher.

Via this means the probable lraxiirnwn increase in velocity being bythefactor of the order of 1.73 times, (or exactly 1.73 times?). And of course it is in relation to this particular specific aspect of the system that one may be able to apply an approach similar to that of the

as related to the similar extension of materials under an applied pressure.

A further view here is to first consider the fact that the heat content will increase the fluid volume by 2.5 times per unit of mass in comparison to the cold state reference fluid, which in the random state in the drum could therefore be visualised to be a cube 2.5 times larger than a cube containing the same mass of the cold fluid. Then the view that when they flow through their respective nozzles giving a mass flow rate of unity with the compressor the cold cube will remain in the random state, whilst the hot cube could have the potential to extend into a cuboid by the factor of 1.73 and in the length dimension then became 2.5 x 1.73 = 4.325 comparative length units in unit time and, therefore, thereby very nearly achieving the desired velocity of 4.5 times when in comparison to the cold state reference fluid.Which is a view that captures the essence of the potentially possible source for obtaining a streamlining advantage in the system when in comparison with the cold state reference fluid. From which one cculd conclude that it may just be possible to achieve the desired velocity of 4.5 times under the conditions of the reduced nozzle CSA and giving a volume flow rate of 2.5 volume units in unit time containing 1 mass unit, in comparison to a volume flow rate of 1 volume unit in unit time containing 1 mass unit in the case of the cold state reference

tiula necessarily passing tnrougn a 1.d llmesnozzle CSA under the same pressure head.Of course the increase in the fluid volume alone under the effect of the heat content would qive rise to and be responsible for 2.5 times velocity

mcrease when#comparison to tne cola state rererence rule, sul casing uWn the preceding we know that the normal velocity where the nozzle CSA has been reduced to give a volume flow rate of 2.5 volume units wouldinfact be 3.36

times velocity units, wnicn 1 tneorlse/wmcl remain ar; 43 times velocity

for the increase in the r to the four element in the system.

Thus I think the correct view is that of the rate of escape of cylindrical elements in continuation from the mass of the fluid in the drum, and that part and parcel of this will be the fact that the hot fluid containing an equivalent mass will be 2.5 times larger which in turn will be a part of that which gives rise to the velocity increase.

(ii) Then the second method being to increase upon nozzle CSA to reduce upon the r to the four drag factor on the fluid jet flow, which would improve upon the fluid jet velocity to the required level when the nozzle CSA became the same as that required for the cold state reference fluid, which would be a CSA increase by a factor of 1.8 times giving rise to an increase in the fluid jet velocity from 3.36 to 4.5 times velocity units but now the volume flow rate would be 4.5 times containing 1.8 times the mass and therefore 0.8 times the mass would have to become continuously recycled in this method.

(iii) Then a third method being by a combination of both (i) and (ii). As could be achievable via adding the Partial Vacuum Technique to the Fluid Recycling Technique.

Thus in the foregoing view one could perhaps consider the cylindrical elements as bullets of a given mass in continuation which then possess higher energy

when shearing#and flowing 4.5 times rasher as according to the kinetic energy equation KE = 3suv2. All of which however raises the question of whether one should in fact consider that the actual molecules inside the hot fluid become any more aligned into the forward vector on flow than for the cold state reference fluid under the normal conditions of the normal tests giving rise to the respective fluidity values for the respective fluids.

give more likelihood that a streamlining advantage could potentially be acquired when and on relating to such values.

It also follows from the above view of the system comprising cylindrical elements becoming forced forward in continuation that view and approach basinq on

multiples or tne ground state mgn energy"converg to 5 nv energy or tne corresponding cylindrical elements in continuation,for the cold state reference fluid will probably be a valid approach and of course simply stems from the fact that the cylindrical elements will shear and escape at a 4.5 times faster velocity for a fluid of 4.5 times higher fluidity property under the same pressure head force.In accordance with the definition of a unit of fluidity, i.e., a reciprocal poises a poise being the force in dynes acting on the CSA of the fluid flow required to maintain a difference of velocity of lcm/second between layers of 1cm2 in area along the direction of the fluid flow and 1cm apart. In the text book being referred to, i.e., 'Physics for ONC Courses' by Edwards, pages 42-43, it therein also states more explicitly for the aspect of the system under discussion that for the same values of layer area and distance apart the difference in velocity between layers is directly proportional to the force acting.Or conversely one could conclude that if a fluid has a 4.5 times higher fluidity property then for the fluids in the same system under the same force the latter fluid would shear and flow at a 4.5 times faster rate. Which of course also follows from the basic fluidity equation, i.e.,:: Fluidity = 8V1 TF (P1 - P2)r4t Thus for the fluids in the same system under the same pressure then the fluidity property will be directly proportional to fluid volume flow which in turn will be directly proportional to fluid velocity, which in turn will be given by Vt r2 for the mean velocity, which is really that which we are concerned with here and be the value that one would place in the equation

in order to qive the enerav of impact of the fluid flow/iet. It therefore

follows that for the same system one could perhaps substitutefluld iet velocity for V/Ttr2 in the basic equation to give:: Fluidity = 8 x Velocity x 1 (P1-P2 )r2t

in turn one could perhaps substitute

velocity value, i.e.,: Fluidity

Then in turn one could substitute the fluidity value for the term containing temperature, i.e.,

However, with further regard to the above I think the formula used will only serve as a rough guide but probably far more and adequate accuracy would be obtained via the formula given on page 29 of the aforementioned text book by Frank M. White, ie,:

loge visc. = a + b # To # + C # To # visc.0 T T Where visc.0 is a known viscosity at a known absolute temperature To, usually 2730K.

All of which, however, is getting a little ahead of the evolution of this possible approach to the system, but one can begin to see the possible potential for the practical usefulness of the approach, perhaps particularly as a route to determinina required nozzle radius for a fluid of a particular known temoerature

and energy ofiimpact valueXsimply by reference to the P-E diagram for the fluid, without necessarily needing to pre-know the fluidity value of the fluid at any given temperature or the fluid jet velocity.Of course the P-E energy of impact value before the mulling of the punch effect due to fluid contraction on impact and cooling would be the relevant value to place in such an energy equation at this pre-impact stage of the system. However, at this stage returning to the more primary discussion

the streamlining advantage potential.

This in fact would probably not be as much as so far indicated since the determined 1.73 times factor relates to the whole of the kinetic energy all becoming fully aligned into the forward vector, and under the same exercise I determine that when the fluid is flowing into a normal pressure of I ATS. then the maxirrurn level of streamlining achievable will only be 5/6ths of the way to being fully in the forward vector, with full aliqnment only being achievable when the fluid is flowing into a zero ATS.

vacuum. Which in turn would result in the extension of the cube/only being by a factor of 1.29.Therefore if one then applies this factor to the value of 3.36 times velocity, then the potential improvement could be to a level of 4.33 times for a fluid flowing into a normal ground state pressure of 1 ATS. Thus again almost just reaching the required level of 4.5 times velocity units but again just falling short and just out of reach. . As would seem to be always the case with any endeavour of this nature. But on the other hand perhaps just good enough in this case. Then if one is also managing to achieve and apply the partial vacuum creation technique in combination then correspondingly higher factors up to a maximum of 1.73 may be achievable, to give a potential trixirum improvement from 3.36 times to 5.8 times. Then potentially able to surpass the 4.5 times level by quite a degree.Remember, no matter how many techniques to bonus energy we may combine and apply simultaneous' in the system we only need the nett energy balance to be such that the fluid jet velocity per unit mass of fluid is at the 4.5 times velocity level for , Ii

the compressor to then probably be fully sustainable by the energy

by the sub-system. To leave remaining all the energy being produced by the turbogenerating process for output supply. However the r to the four factor could come into play again and similar reduce upon the streamlining advantage potentially possible to achieve in the system and,in line with the mean velocity being half the central maximum velocity could, therefore, similarly become reduced by half.Which if so would then reduce the potentially possible improvement levels due to achieving molecular streamlining to factors of 1.145 for a fluid jet flowing into normal 1 ATS., and 1.365 for a fluid jet flowing into zero ATS. pressure. Tag the 3.36 times velocity value to 3.85 times and 4.56 times respectively. Which could perhaps just be underestimates but nonetheless probably realistic levels of potentially possible improvement levels by such a means. HoWe\/er, , it follows that perhaps the approach possessing the more immediate hope will be that of capitalising on the r to the four element, i.e., reducing upon the r to four element, coupled with recycling of fluid. Then endeavouring to achieve a streamlining advantage in combination with this more basic method. Any extra energy being achieved via streamlining the fluid further than would normally be associated with normal laminar fluid flow and the normal fluidity value then being a further potential source of bonus energy to make up for any shortfall in the oversized nozzle approach. This perhaps being the better way to regard, view and combine these two facets of the system at this stage, although perhaps I 'm diminishing the importance of trying to acquire a streamlining advantage at this stage too much.On the other hand, if and when the partial vacu technique ever becomes combined then perhaps only then could significant levels of a streamlining advantage be acquirXeable. Indeed on a cursory consideration one would probably be correct in thinking that almost certainly a further applied force would have to become added, such as a partial vacuum drawing on the fluid flow, before one would improve upon the fluid jet velocity beyond that which would be expected to be associated with the applied force of the pressure head.Which I suppose is that which I really believe at this stage and certainly in relation to cold fluid, but for hot fluid in the liquid-vapour state with very loosened Van der Waal bonding and therefore in contrast very amenable to molecular orientating, streamlining forth immediately from a high random pressure of 100 ATS. through an appropriately shaped converging nozzle,then I'm not so sure and it would seem to me that quite a high degree of molecular streamlining could be achieved which would not normally be associated with normal laminar fluid flow and a normal fluidity value.Of course the fluidity value in terms of volume of fluid flow would remain the same, but it could prove possible to extend the fluid flow further into the x dimension than would normally be the case in normal laminar fluid flow even if the only applied force remains that of just the random pressure head to the rear and forcing the fluid through the nozzle from the rear.Thus, if such additional streamlining where achievable then it would require an associated reduction in the nozzle CSA at exit than would be required for normal parabolic laminar flow of the same fluid under the same pressure, which would then reduce the radius parameter in the fluidity equation: Fluidity = 8V1 AT (Pl-P2)r4t

nd therefore1 the r to the four and r to the two parameters of the system, which in turn would give the higher velocity flow of a given mass of fluid on the flow of a given mass fluid in unit time, i.e., simply due to the mass initially comprising molecular translational motions in all random motions, ;;e, up, down, sideways and backwards, becoming mass with all the random molecular motions becoming more aligned into the forward vector than would normally be the case on normal parabolic laminar flow of the same fluid under the same pressure. However, whilst the volume flow and volume parameter in the equation would therefore remain the same this would not give rise to a higher fluidity value necessarily having to be on the lilS of the equation, which

remain the same pre determined property of the fluid,

0neV' that . on rear me IS; run Iha , it l length parameter would now be longer when in - comparison with that which would be associated with normal flow wherein a given mass didn't undergo the same extension in the forward vector on flow.

And also when in comparison to the cold state reference fluid which wouldn't undergo any forward alignment of molecules at all in comparison on the flow of a given mass of fluid. It therefore follows that when in comparison to the cold state reference fluid the length of a unit mass of fluid and therefore

the lengtn parameter m tne case equation could De appreclaDly longer wnen viewed in this light with the radius parameter becoming correspondingly reduced in the equation in accordance with the mass of fluid becoming longer and thinner.

Perhaps to give an r to the three relationship when in canparison to the cold state reference fluid relating to the preceding discussion on this aspect resulting from a canbination of the fluidity property of the fluid being 4.5 times higher and only 5 times less than the gas air and induced streamlining via a specially shaped nozzle as the fluid bursts forth through the nozzle from the train bulk of the fluid.In which case then the fluid jet velocity could perhaps become the value of 4 times higher when in relation to the cold state reference fluid even after reduction of the nozzle CSA to give a 2.5 volume unit flow rate containing 1 mass unit from the probable level of 3.36 times velocity units, which would then be approaching the good enough level.

However, the discussion so far on the above aspects is still at a somewhat hazy stage and becomes further clarified in ensuing discussion.

Again I can only hazard a guess buL applying the equal and opposite factor the appropriate internal nozzle shaping could be as follows. If in longitudinal cross-section one likens a venturi shaping of vapour flows to be as though two halves of adjacent tear drop shapes at the broad end and at the appropriate distance apart with the vapour flowing towards and between the broad ends of the tear drop shapes, e.g., 'Heat Engines and Applied Heat' by F. Metcalfe page 224 Fig 75(b), then the relevant equal and opposite would be to turn the tear drop shapes around so that the fluid in the liquid to liquid-vapour state flowed towards their sharp end and between two halves that gradually converged until the final nozzle CSA was reached. Thus, if the slope of the converging sides was as for a tear drop shaping then they would be at a gradient of around 1 in 4.5 along the longitudinal axis and the length of the nozzle from drum base to nozzle exit would be 4.5 for every 1 unit of nozzle exit diameter.

Remember that in contrast to the equivalent vapour system no fluid expansion would be simultaneously taking place but one would similarly be trying to induce the translational motions of all the molecules in the fluid to all line up into the forward x vector from the fully random state where the translational motions would initially be travelling in all random directions, e.g., as shown in the OU. Course Book S101 Unit 8 Fig 37. Therefore, in contrast this type of internal nozzle shaping would seem correct for achieving such fluid mechanics.Full molecular streamlining would not normally take place on normal laminar fluid flow and therefore there should exist the potential to streamline further which in turn would give a higher fluid jet velocity and therefore a higher energy yield, which one would expect if in the process of the formation of the fluid jet the molecular translational motions making up the fluids as a random matrix of paper fibres, all become simultaneously streamlined into the forward direction as far as can possibly be achieved.

Additionally, one would perhaps expect this particular facet of the advancing front of science and technology, i.e., fluid streamlining, to play a role in such a new and advanced system applying fluid flow, when the higher the temperature and pressure the more advantage one could perhaps expect to be able to induce. However, the maximmm potential even with the addition of an applied vacuum of zero ATS. is likely to be only of the order of 1.73 times the normal velocity.Which however are Velocity Factors that I have determined from my own fairly simple exercise under the aforementioned earlier writing on this process applying my own derivation version of a shear mocukisapproach at that stage, but nonetheless it

approach and may be correct for this particular system.

Thus the view here is one of cylindrical elements of fluid becoming forced forward into the specially shaped, gradually converging, nozzle by the pressure to the rear at their normal rate for the pressure, all joined up of course, which would give the normal fluid velocity for the pressure head, but then additionally as the fluid flows through the specially shaped nozzle the fluid molecules form into streamlines and successive cubes of fluid extend forward into longer and thinner cuboid shapes to give a higher velocity than would normally be associated with the pressure head and the fluid flowing through a normal nozzle, e.g., of the Bellmouth design.

To add further to the imagination and the visualising of the above fluid mechanics, I refer readers to a number of diagrams and photographs in the bibliograph.

Firstly to the photographs given under the Mcgraw-Hill Encyclopaedia of S & T under Boundary-layer flow on page 20 Fig. 5. Then to the diagram in the same bibliograph under Fluid Flow on page 184, again Fig. 5. Then to the photographs of streamlines given in 'Fluid Mechanics' by Frank. M. White under Fig. 1.14(a) page 44; Fig 6.3(a) and (b) on page 308; and Fig. 7.21 on page 441. If one considers these photographs and diagrams and associated

diagrams and description then in particular) the first set of photographs under the Mcgraw-Hill Encyclopaedia one could perhaps conclude that Fig 5(b) to (c) would be the average photograph that would apply to normal laminar fluid flow but with the potential to become as Fig (a) to (b).When one can guesstimate that the order of improvement achievable could be as indicated by the preceding velocity increase factors. Moreover, looking at the diagrams and photographs referred to one imagines that it could be as though stretching out a web of polymer chains or a matrix of paper fibres to be longer and thinner, as in the tensile testing of such materials for example. Hence, the view that it may be possible to apply a simplified approach to this aspect of the system based upon a consideration of

with simplicity of approach and the application of further basic parameter relationship laws in mind.

It states in all the bibliograph that pressure has little if any effect on the fluidity value of a fluid which is solely temperature dependent, but perhaps operating under a high pressure of the order of 100 ATS. could make the difference that the further streamlining may become more achievable in canbination with an appropriately internally shaped nozzle. At least when relating to normal laminar fluid flow to which a normal fluidity value applies at the same temperature st not necessarily at the same high pressure.

Thus in the ensueing exercise in which I continue on with the dressing of the system with the basic fluidity equation I mainly hope to show that a streamlining advantage under the above conditions and as discussed in the preceding may be achievable, but the exercise will also serve to further reveal some of thebasic.mechanics of the system in an early stage fairly simplified and rudimentary manner and view of the system.

IHE POTENTLAL FOR APPLYING THE BASIC FLUIDITY EQUATION To THE SYSTEM AND EXDING UPON THE BASIC EQUATION VIA THE INCORPORATION OF A SHEAR MODULUS FACTOR FOR STREt'tINED FLUID FLOW Firstly if one considers the classical description that is generally given in most text books when discussing Poisedille ' s Equation in the context 9f the drum and nozzle description being considered here then one could well conclude that this was the perfect system to which the perfect basic relationships of parameters should apply.Which generally states that the relationship of parameters, ie, the basic equation, is concerned with a cylindrical element of fluid of length, 1, and radipus, r, becoming forced forward from surrounding stationary fluid but being held back by the bonding resistance of the bonds with the surrounding stationary fluid, under the power of apressure difference/drop from P1 to P2 across the cylindrical length of fluid.For example, as becomes discussed in the text books 'viscosity and it's Measurement' by Dinsdale and Moore, page 14, and in 'Physics for ONC Courses' by Edwards, page 44, amongst others of those being mentioned, with a very explicit and useful diagram being given in the latter text book which occurs again perhaps even more explicity in the context of the system under discussion in the text book 'Introduction to Fluid Mechanics' by Henke, page 146, Fig. 14.2, with a further relevant and useful depiction being given under the text book 'Essentials of Engineering Fluid Mechanics' 2nd Ed. by Rueben M. Olson, page 220 Fig. 10-1 (a) and page 149, Fig. 7-5. Thus I have these types of views of the fluid flow in mind when discussing this aspect of the system and therefore they will be of similar usefulness to readers.

Such views can in fact be visualised to be the mechanics of the fluid being considered here as a cylindrical element of fluid becomes forced forward from the bulk of the relative stationary fluid in the drum into the nozzle under the force of the pressure drop across the nozzle. However this will be a stage in the process where the fluid is in the process of forrring a fluid flow whilst the basic equation is traditionally applied to a fluid flow after the final fluid flow has been established, which in the system under discussion would be more precisely at the nozzle exit. On the other hand, the equation is more precisely concerned with fluid becoming forced forward by the pressure drop against the bonding restraints of surrounding stationary fluid, eg,as becomes explained at the top of page 14 of the first text book reference mentioned. Therefore, if one first considers the fluid as it leaves the main bulk of fluid in the drum and enters the nozzle these would be the conditions and. the fact .. .

that the fluidj then form a parabolic profile1 would acutally be that to which the equation applies. For example, if one looks at Fig. 10-1 (a) on page 220 of the fourth text book reference then the application of the basic equation to the system would in fact apply and relate to the finally formed parabolic fluid flow profile because this will be the velocity profile of the finally formed fluid jet in the case of the cold state reference fluid at least and in the absence of any additional streamlining being achieved.Then in the case of hot fluid through a specially shaped streamlining nozzle the velocity profile could approach becoming more square and especially so if under the influence of the additional drawing force of the partial vacuum technique. Thus, it will be theorised following that the velocity profile would probably range from being fully parabolic at a minimum to being fully square at a maximum and also that it should be possible to simply apply a modulus factor in the basic equation as related to parabolic flow for any increase in mean velocity beyond that associated with parabolic flow due to any of the influences, as will become clearer in ensuing discussion.

However, perhaps the better way to a further and better understanding of

such aspects is t Uj yu through the derivation of the basic Poiseuille's Equation, mainly as outlined in the first text book reference, with discussion on the relevant aspects.Aimed firstly at determining whether or not the basic equation should be fully applicable to the system, but then also for the purpose of discussing further the potential for incorporating into the basic equation a modulus approach to possible fluid extension on streamlining in the case of hot fluid when in comparison to the cold state reference fluid. Which I do following with apologies to Dinsdale and Moore for borrowing their derivation format for the purpose of this exercise.

Derivation of the Basic Poiseuille's Equation: Consider the forces acting on a cylindrical element of length, 1, and radius, r. That due to the viscous resistance of the surrounding liquid is: Farce F x the outer longitudinal area of the cylindrical element = F x: rl.

Thus from this it can be seen that the equation is concerned with forcing a cylindrical element of fluid forward specifically against the bonding resistance, F, of surrounding fluid which is considered to be stationary relative to the cylindrical element becoming forced forward. Thus from this point of view the equation would seem to be applicable to the system as the fluid flow becomes forced forward against the bonding resistance of the fluid in the drum, which in turn could be deemed to be stationary relative to the fluid becoming forced forward and especially so in this case where the main bulk of the fluid has necessarily to be exerting the same pressure in all random directions,as in previous discussion.

Then there is the force due to the applied pressure, P, acting on the cylindrical element and forcing it forward in a telescopic manner to finally form a parabolic velocity profile against the bonding resistance of the surrounding fluid. Which is given by the applied pressure, P, ie, the applied force per unit area acting on the end surface area of the cylindrical element and forcing it forward, times the total end surface area of the cylindrical element, ie: Tlr2 P Which will then give the total applied force acting on the end of the cylindrical element and forcing it forward against the.total bonding force holding it back and acting over all the longitudinal surface area of the cylindrical element of fluid.

Thus these two forces can be equated as follows: F x -2Trr 1 = rP F = Pr Newtonian behaviour requires that: F ID Where D will give the velocity gradient from the central longitudinal axis of the finally formed fluid flow to the stationary surrounding fluid in the drum. Thus on substituting this expression into the parameter relationships it can be seen that they will in fact apply to the finally formed fluid flow because as the fluid flow telescopes forward into and through the nozzle it will do so from stationary surrounding fluid in the drum and, therefore, in such a way that the finally formed fluid flow will have a parabolic profile, at least in the case of cold state reference fluid and in the absence of additional streamlining influences, in accordance with the parameter relationship becoming derived.Thus: D = - Sv 6r The negative sign is added since velocity, V, from the central axis decreases as distance, r, from the central axis increases, and D is considered positive. Therefore substituting: - q dv = Pr dr 2l dv = - Pr dr 2q( From this it can be seen that the shearing stress-and rate of shear are directly proportional to r and will therefore be zero along the longitudinal central axis of the cylindrical element.

On integration of the above expression traditionally when applied to finally formed fluid flow in a pipe the conditions are used that the velocity will be zero at the walls of the pipe. Whilst here it is similarly being considered that the velocity of the final layer of fluid surrounding the cvlindrical element will be zero. but initiallv this will be as in contact

with the surrounding fluid? - Thus the same conditions are used and more specifically that at the surface area contact of the cylindrical element with the surrounding fluid the radius, r, will equal a and the velocity of the final layer of surrounding fluid will be zero.To give: V : P (a - r) m7 Which is an expression that shows that the velocitv distribution profile

across the final state of the cylindrical elementlforced forward will be parabolic and therefore this relationship of parameters will in fact apply to the final effect of the pressure forcing the cylindrical element of fluid forward from the main bulk of the fluid and therefore in turn will relate to the finally formed fluid flow in the nozzle. For examplesto the final state of the fluid flow under Fig. 10-1 (a) on page 220 of the text book reference by Olson. That is, in the absence of further streamlining due to the possible streamlining influences.The further point to make ~~~~ ~~~ here is that in such a finål fluid flow state the expression considers that the final layer of fluid surrounding the cylindrical element and in contact with the surrounds will have a velocity of zero. Which would seem to imply that one need not further consider any resistance to fluid flow due to contact with the nozzle walls assuming they are smooth allowing laminar flow and not subsequently creating turbulence.

The volume of liquid Flowing in unit time between radius r and r + dr will be 3nor v dr, wherenr v is the surface area of a cylindrical element in which the length parameter has become replaced by length in unit time, ie, velocity, v. Which on integration through the radius parameter, r, from r = o along the central axis to r = a at the final surface ofthe cylindrical element will give the volume of the fluid flow, ie, give the sum of all the annular sheaths of fluid from the centre. Thus the volume flow will be given by:

Substituting for velociyt, v, by the previous expression to give:

) = Err dr V : r (a2 ( a - r ) dr 4qL Jo IT Pa = 1T Pa in unit time a

4 =nPa t in time t 8 C) L (1 =ffP a t Fluidity = BVL B Vl.

It also follows from the above that the mean velocity will be given by fluid volume flow in unit time divided by the CSA of the cylindrical element. Although this aspect also follows very simply from the fact that the volume of fluid one collects in unit time must have flowed out of the nozzle exit at a velocity qiven by volume/CSA in order to have delivered the given volume in unit time.

Thus, thereby becomes derived the Poiseuille's Equation. Nice and neat isn't it. Certainly it would seem that it may apply admirably to the new system under discussion as I hope has been demonstrated by the foregoing exercise.However, I don't intend to be definite on this aspect at this pre-practical stage since there is obviously a difference between this system and normal parabolic fluid flow in a pipe to which the basic equation was oriqinally and is traditionally applied. Having said that the

flcX lsa (luidfÁLuflowedSthrough the pipework and/or the drum in a normal manner albeit in a more random manner and probably, therefore, the basic equation would in fact be as and/or more applicable at the nozzle stage where the fluid would become intrinsically more streamlined, ie, as the fluid state to which the basic equation is said to more strictly apply. When then and there one could imagine the calibration marks of a fluidity test to be.Therefore, for the discussion here I propose to continue to assume that the basic equation may in fact apply in the ways discussed and yet to be discussed.

EXTENDING UPON w BASIC FLUIDITY EQUATION FOR APPLIG4BILITY TO STREAMLINED FLUID FLOW VIA THE INCORPORATION OF A SHEAR MODULUS EXTENSION FACIOR PARAMETER: ThLXstheisnow the question of incorporating into the equation the effect of streamlining the fluid via a modulus approach.Since the volume/mass flow rate will remain the same with simply the molecular translational motions therein becoming more to fully aligned all into the x forward vector from the y and z planes then the only effect in practice will be that a given volume of fluid on entry to the nozzle wiz become longer and correspondingly narrower as the volume of fluid flows through and exists from the nozzle, by an amount of the order of the preceding discussed factors, eg, perhaps increases in the mean velocity by some 15 would be possible simply via an appropriately shaped converging nozzle when in comparison to the fluid jet velocity that one should obtain via a normal Bellmouth type, which in turn should/would give the normal velocity associated with the fluidity

property of the fluid, ie. in the absence of an extra applied forcereg, as may be creatable via the partial vacuum creation technqiue. When the potential maxium increase could be around 73 ,0 but pechzlps around3 OSOL 85S,35) increase in mean fluid jet velocity by such a technique would ever be the

maxyum achievable. Which, however, whilst just making the difference could make all the difference. An analogy with respect to the latter being the wind blowing in the opposite direction on a very small pressure increase and drop in the opposite direction such that the pressure gradient becomes in the opposite direction.

Therefore, if a given volume of fluid simply becomes longer and narrower when in comparison to the fluid flow through a normal Bellmouth nozzle the parameters of which being those which one would normally place in the RHS of the fluidity equation, then only the length and radius parameter would become affected and in practice of course it would simply be a question of reducing the nozzle CSA smaller which in turn would result in a smaller r to the four parameter in the fluidity equation. However,ifthe fluidity property and value of the fluid on the LHS of the equation remains the same one would also have to decrease upon the comparative length parameter in the equation in order to maintain the balance of the equation under the two sets of conditions.But the new mean fluid jet velocity would still be given by the same fluid volume flow, ie, the V parameter in the equation, divided by the new and smaller value for the CSA of the nozzle exit, ie, 7r rX new. However, when one came to apply the equation to the system and more specifically to the normal fluidity property and value of the fluid then the length parameter would become a parameter, or more correct to say would have to become a parameter, to which one took into account a modulus extension factor in the case of a system in which one was achieving streamlining beyond the normal level associated with normal parabolic fluid flaw in a normal pipe.However, there is a confusing aspect since if the cylindrical element is becoming longer and narrower in camparison to the normal cylindrical.element throught a Bellmouth nozzle then one could first consider that the length parameter would have to be increased in camparison by the factor of the extension, but of course this would not maintain the balance of the equation.Therefore, some subsequently considered incorrect initial thinking on this aspect was that since the basic relationship of parameter is concerned with the cylindrical element of fluid becoming pushed forward from the bulk of the fluid in the drum then at such a stage the length of the cylindrical element could in one view be regarded as being shorter in the case of a fluid which subsequently went on to be deformed into the length direction on flow through a converging nozzle in comparison to flow of the same fluid in unit time through a normal Bellmouth nozzle because the fluid flowing out of the nozzle exit in unit time in the case of the converging nozzle would be a shorter and fatter cylindrical volume of fluid at the beginning larger end of the nozzle than the same volume of fluid flowing through a straight Bellmouth nozzle in unit time, albeit flowing on to be a longer and narrower cylindrical volume of fluid on flow through the converging nozzle, but after the stage of actually shearing from the surrounding stationary fluid in the drum where the given volume flow of fluid in unit time would occupy a shorter and fatter volume in direct contact with the surrounding fluid in the drum.Therefore, assuming the foregoing is a incorrect view too it

be the,longitudinal surface area of this shorter length

volume of fluid thatj De applicable in the equatton, which in turn would require the final length of the volume of fluid to be reduced by the factor that it has become deformed into the length direction, which in turn would then be the applicable dimension for the system with respect to the area of the bonding forces with surrounding fluid that has to be overcome by the applied force for every unit volume of fluid passing through the system.ThUs at the nozzle exit as far as this part of the basic relationship of parameters is concerned the dimension of a given length of fluid would not in fact b as at the nozzle exit, but the shorter and fatter dimension as at excape of the fluid form the surrounding fluid in the drum. Whereas for the normal system through a normal Bellmouth nozzle where further fluid extension would not be achieveable then the comparative length dimension would be as at nozzle exit.

A further aspect then being that in order to maintain the balance of the equation the decrease in the r to the four parameter would also have

to oe tne same1ractor tnat one appiieo to tne iengtn paramter ror tne flow of a given unit volume of fluid. Therefore, would one in fact expect the elongation of the fluid element to boil down to a factor which became the same as the r4 reduction. For this. if one considers the

volume of fluid in the y plane that becomes1 displaced to become fluid volume that adds to the lenath dimension of the fluid flow and similarly

the volume of fluid in the z plane that simultaneously becomes/dispfaced to also become fluid volume that adds to the length dimension of the fluid flow, then there would be involved two equal volumes offluid one in the y plane and one in the z plane that become added to the x dimension of the fluid flow.Without carrying out full calculations here, but bearing in mind that the original volume will be given by frll, then one can see that when the two displaced volumes compound together the factor extension of the length of the fluid could in fact boil down to the same if one looks again at the basic equation, ie:: Fluidity = ~ l 8VL 1T(P1,- P2) r 4 t One can see that the complexity of additional streamlining and that of the addition of the partial technique may be possible to become incorporated into the basic equation very simply by reducing the length 4 parameter by the same factor that the r4 parameter would become reduced when in comparison to the normal system through a normal Bellmouth nozzle which in turn would give the normal levels of fluid jet velocity as determined in preceding exercises, with the higher mean velocity of the streamlined flow still being given by the V, the volume flow which would still be the same, divided by rrrz where r would now be smaller and therefore the mean velocity would be correspondingly higher.With the factor one reduced the comparative length paramter by, ie, the level of the 4 r reduction, in fact in practice being the factor increase in the length dimension of the fluid volume on streamlining when in comparison to the normal fluid flow through a normal Bellmouth nozzle - which in turn should give the normal levels of fluid jet velocity as determined in preceding exercises.

However. one doesn't acquire anything for nothinq in this World and

LE 1U ELt: E LU EiU 1 1y further the conditions of the derivation of the equation to determine whether via a specially and appropriately shaped nozzle one could in fact expect to be able to achieve fluid extension/deformation by thereby being able to induce extra fluid alignment in the streAmlines of fluid becoming formed in the fluid as the fluid telescopes forward through

the specially shapedjrram the random pressure,(ie, isontropic pressure to place in present terminology), and state in the drum

that which would occur on flow through a normal Bellmouth nozzle which in turn should give the normal levels of fluid jet velocity.For these deliberations firstly considering the reverse tear drop converging nozzle shaping in comparison to a normal Bellmouth type

giving the normal levels of expected velocity. Thus, when one considers the former shaping in comparison to the latter in the context of the derivation of the equation then one can envisage that the end surface area over which the pressure would then be exerting would in fact be appreciably larger than that of the cylindrical element of fluid that finally exits from the nozzle.Therefore, firstly if one considers this element of fluid hypothetically extending back to the entrance of the converging nozzle

as though hypothetically inside auellmoutn nozzle then one can see that the'force nD rP of the

half of the derivation and acting on the end surface area of the cylindrical element and giving rise to it's shearing from the bulk of the fluid at the rate determined by the fluidity property of the fluid would in fact now also be acting on surrounding fluid at the entry of the fluid to the exit nozzle in this hypothetical view.Of course only fluid equivalent to the cylindrical element of fluid would actually pass through the nozzle exit. However, one shouldn't think of this as though, therefore, fluid competing to flow out of the nozzle exit, but rather that an element volume of the fluid flow on entry to the nozzle will fully fill the entry to the nozzle in disc shape, which initially will contain molecules travelling within the fluid in a fairly random manner. Then as the disc of fluid volume flows forward through the converging nozzle that it changes shape into a progressively longer and narrower disc shape with fluid in the y and z planes becoming displaced into the forward x plane.When according to the preceding theorising the extension in the x plate will be by a factor by which r4 the the r parameter would be progressively decreasing,

The above, therefore, the view of the system that one should have in practice, and from this view and that of the hypothetical view I think one can see that under such conditions extra applied pressure would in fact be being exerted onto the fluid flowing through the nozzle from solely the applied energy of the pressure head source above that which would be associated with a normal Bellmouth nozzle and which in turn should give the normal level of fluid jet velocity associated with the fluidity property of the fluid.Thus, one can see that by progressing to a specially shaped coverging nozzle there could/would in fact be extra applied energy from the source of the pressure head which could give rise to the same pressure head energy being able to induce the extra fluid streamlining giving rise to a higher fluid jet velocity when in comparison to the fluid jet velocity that would be obtained through a normal Bellmouth nozzle.In

otner woras, tnere woula oe moreytne pressure neaa energy acting on tne

fluid flowinq throuqh and out of the nozzle thin would nor could act on the

fluid1 flowing through a normal Bellmouth design in the direction of flow,~ WKCh in turn should give the normal fluid velocity that one would expect from a fluid of a certain fluidity property.Thus, one indeed may expect to be able to achieve a higher fluid jet velocity via an appropriately shaped nozzle on the application of just the pressure head energy without necessarily having to add a further applied source of energy, (erg, that of the partial vacuum technique), when relating to normal conditions.

However, the addition of extra applied energy would obviously improve upon the level of streamlining and factor increase achievable.

However, to achieve such an advantage the internal shaping of the nozzle will be all important and may be anything from a normal shaped venturi entry to a nozzle with a very shallow converging angle from entry to exit, eg, at entry being the diameter of a volume of random fluid and at exit beign the reduced diameter of the streamlined fluid. In between which would be the reverse tear drop converging shaping.

With further regard to such aspects of the sytem I refer to the text book 'Mechanics of Flight' by A.C. Kermode, pages 66 to 67. Where it similarly states in the 7th line from the bottom of page 66 that the exact shaping of a venturi tube is all important to the success or otherwise of inducing a faster flowing air flow through the venturi tube. Then on Fig 2.21 on page 67 a diagram is given of an air flow speeding up as it flows along the convergence of a venturi shaping, becoming a maximised velocity at the narrowest point of the convergence of the walls of the venturi tube. Thus, it will be a similar type of effect that would be hoped to be achieved in the system under discussion.If one looks at this diagram at the beginning stage of the formation of the final streamlines before entry to the venturi shaping proper then one can see that the streamlines indicated fan out towards the beginning and that those on

the edge of the flow indicated point1as muh in the y vector as they do in the x vector, and similar for a cross section in the horizontal plane they would point as much in the z plane as they do in the x vector, whilst those along the central axis are indicated as already pointing in the x plane, ie, the desired direction of flow for all the streamlines.

Therefore at this stage the translational motions of the molecules in the fluid could be regarded as being in a random state to a larger extent even though the diagram may give the impression that the fluid starts off already fairly streamlined. However, when one considers the fact that an enormous number of molecular collisions will be taking place over very short distances in the x, y and z planes of the order of 1 um (ref:-'Fluid Mechanics' by Frank. M. White, page 20.) then one can moreso envisage that the fluid state would still be comprised of molecular collisions tending to produce the random state at the beginning stage. Then as the fluid flows towards and through the special converging flow path of the venturi shaping quite a good analogous description would again be that of the log flow description.Initially one can imagine the logs in a unit mass or volume of logs to be knocking each other in all random directions then as they become channelled along the converging flow path progressively and increasingly beginning to knock each other just into the direction of flow. Until the logs finish all lined up in neat rows of streamlines all pointing in the direction of flow and having got into such a state from the random state by progressively pushing each other forward into the direction of flow rather than in other directions as when in the random state. Thus, as such a process takes place the velocity of the fluid flow will increase for the flow of a given mass of logs past a given point in unit time involving the log flow becoming longer and narrower.However, only if the converging shaping is correct for the type of fluid since if one tries to overdo things then the logs would keep knocking each other into the random state and if insufficiently done than the random state would not become as streamlined as potentially possible. It follows that the required optimum shaping for the system under discussion could change with fluid temperature and pressure. On the other hand and not,withzstanding my earlier thinking with respect to this aspect the optimum shaping could be that of the venturi shaping. However, the higher the temperature and pressure then probably the higher the level of streamling advantage that could be achievable over and above the normal level.Which also follows if one considers the extension of the fluid in terms of a Rigidity Modulus property of the fluid, since the hotter the fluid then the less rigidly would be being held the fluid molecules by the internal Van der Waal bandingqand the higher the pressure then the higher would be the level of extra force acting on the end of the fluid entering and passing through the specially shaped converging nozzle.

A further aspect to consider is that of pressure loss at nozzle entry, but it can be gathered from the text book 'Thermofluid Mechanics' by Pefley and Murray that for a Bellmouth nozzle this would only be of the order of 4 Ó and therefore for an applied pressure of 100 ATS this would mean that the effective and applicable pressure parameter to place into the basic equation would become reduced to 96ATS. It also follows that for the specially shaped nozzle then this pressure loss factor could be less. reducina the effective and aoolicable Pressure to say

97-99 ATS.It also follows from r,neEexample- or the Bellmouth system that one need not then consider any further loss of pressure effects due to fluid to nozzle wall friction as the fluid flows through the nozzle, which in turn also follows from the fact that one has already considered that the edge velocity of the fluid flow through the nozzle to be zero in arriving at the mean fluid jet velocity.

Similarly, for the similar small percentage pressure loss that is normally associated with constant pressure cabling due to fluid flow friction work en-route to the stage equivalent to that of the nozzle it should similarly be simply a question of reducing further the effective and applicable pressure parameter in the basic equation by the percentage loss due to this fluid mechanics effect. Perhaps with the total pressure loss being of the order of 10, ó for the system envisaged, reducing the initial pressure of 100 ATS to 90 ATS for the effective and applicable pressure that one should place in the relationship of parameters for the system.

Of course, so far it is not fully certain that the basic relationship of paramters could be applied to the system in the ways being discussed and then be wholly correct on so doing. However, on further thinking and considering this aspect in the context of a normal Bellmouth nozzle, eg, as the diagram in the text book 'Thermofluid Mechanics' page 115, Fig 6-7 (a), then it would seem to me that if one considered the normal calibrations of a normal fluidity test to be at the any of such a nozzle, the distance between which for the purposes of this exercise and for comparative purposes let us consider to be the length of 1 unit of normal volume and/or the length of 1 unit of normal mass of fluid flowing through the calibration marks in unit time, then the system would in fact be in full compliance with all the requirements of a normal fluidity test which gives rise to the normal fluidity value, ie, at such a stage the fluid jet flow would have fully established the final parabolic flow profile and accompanyingly the level of laminar flow that would normally be associated with the fluid flow under a normal fluidity test would by then have become fully established on flowing from the more random/isontropic state in the drum, and of course the fluid flow would be being subjected to a constant and continuance pressure head. Furthermore such a nozzle would be very much akin to the normal cylindrical tube through which most fluidity tests are carried out.

It therefore follows that if one considered the system in this light then the basic parameters of the basic equation should indeed be applicable to the system if based upon a Bellmouth nozzle with correction of the pressure for effective pressure loss as may be found in practice. Thus, it further follows that firstly for such a system one should be able to directly relate the fluidity values of cold state reference to those of hot value as the reduction in the r4 parameter on the fluid volume becoming longer and narrower.Therefore, if one assumes this to be the case then fluid in the ways discussed, ie, mainly to render it possible to calculate that the fluid jet velocity of the hot fluid through the same system would be higher than the cold fluid in the direct ratio of their normal fluidity values, and then from this that the energy value of the hot fluid jet would therefore. be in the ratio of their fluiditv values snared as

in the

stagelwork. Then secondly that the range of evolutions from the basic equation discussed in the preceding. exercise should be fully applicable.However, a little more complexity creeps in when one then progresses on to streamlining the fluid via a specially shaped nozzle, but this probably need not involve a lot of extra complexity incorporated into the basic equation, although on my further thinking on these aspects of the system I have in fact concluded that the early stage thinking in the foregoing in relation to this particular aspect is not wholly correct which, however, on this occasion I will leave as is and rectify my thinking at this stage, hopefully to approach closer to a wholly correct level.

Firstly, the fact is that in a comparison between the same fluid through a Bellmouth nozzle and a specially shaped nozzle the initial volume of fluid shearing and becoming forced forward into the nozzle from the surrounding drum in unit time should in fact probably be regarded as being the same in both cases with respect to the surface area over which the shearing is taking place. Because it is only subsequently on the flow of the volume of fluid through the specially shaped nozzle that the volume of fluid will become longer and thinner in comparison to the same volume entering and flowing through a Bellmouth nozzle.In other words, for the same volume of fluid flowing from the drum into and through the nozzle of whatever type in unit time, ie, as the situation being considered in this comparison, then one should probably regard the bonding forces with the surrounding fluid to be overcome to be to same for both the types of nozzles being considered here for calculation purposes. Which in fact becomes obvious when one considers that even though the longitudinal dimension is less the CSA dimension of the cylindrical disc will be pro-rata larger and, therefore, the outer surface area of fluid in contact with the surrounding fluid will in fact probably be the same. Therefore, the half of the derivation involving the bonding force, ie, Fx2 rl, would in fact probably be the same in both cases notwithstanding the earlier thinking. However, the point being that in the case of the converging nozzle commencing as it would with a larger CSA at entry then the pressure head energy would be acting over this larger surface area which, therefore, could alone in theory be a source of a little bonus energy that could alone induce a little additional streamlining beyond that associated with flow through a straight Bellmouth nozzle and giving the normal level of velocity.Then the difference being that now when the longer and thinner volume of fluid flows through the graduation marks still in unit time it will be doing so at a faster velocitv bv an amount eaual to the increase in the lenoth of the fluid

volume,remember at thel reduction of fluid volume in the CSA dimension in order for the same volume and mass of fluid to flow through the same calibration marks in unit time.Yes, but if one achieves extra streamlining

via means of a specially shapedlwlll this necessarily mean that the fluid volume will become longer and thinner requiring of a reduced nozzle CSA exit when in comparison with the same volume of fluid passing through aBellmouth nozzle? Well the only point in trying to induce extra streamlining via a specially shaped nozzle would be to increase upon the velocity of the flow of a given volume or mass of fluid in unit time.

Therefore, if the forward mean velocity does become increased by the order of the factors discussed in the preceding exercise and the same volume of fluid becomes collected in unit time on exit from the nozzle then the nozzle CSA at exit must be required to be reduced because this would be given by the same volume of fluid divided by the increased mean velocity.

Therefore, the questions, now are what will be the changes to all the parameters in the basic fluidity equation on streamlining, and more specifically how will the various changes relate to one another in the balance of the basic relationship of parameters, and will the overall balance remain the same or change to? It follows from the foregoing that the required reduction in the nozzle exit GSA for the streamlined fluid will in fact be directly related to the increase in the mean fluid jet velocity, or more descriptively in the context of this discussion, directly related to the increase in the length of a given volume on mass of fluid flowing in unit time through the calibration marks or past one calibration mark, or indeed flowing out of the nozzle exit in unit time.Which therefore will mean that since GSA is given by lv r then the increase in the length of a unit volume or mass of fluid will be by the same ratio that the r to the two parameter of the system becomes reduced by, and not in fact the r to the four parameter. Hdwever, the basic equation would of course still possess the r to the four paramter, but an streamlining the increase in the length parameter would only involve a corresponding reduction in r to the two of the full r to the four parameter, ie. in the basic equa tion: - Fluidity = 8 VL 1T (P1 - P2) r 4 t

thejparameter,twould become increased by a certain factor on streamlining which would entail a reduced nozzle exit GSA, which in turn would 4 involve a reduced r value. Therefore so far the balanceof the equation is becoming such that the length parameter may become increased by a factor, with the r to the four parameter becoming reduced by the square of the same factor, which if so would upset the balance of the relationship of parameters beyond that which could reasonably be expected.Therefore, firstly I think that as far as the values that should be placed in the basic equation are concerned on streamlining then, even though at nozzle exit a given volume or mass of fluid will be longer by the factor increase, the length of the volume of fluid as it is initially on being forced forward from the surrounding fluid should be the comparative lenath parameter that should be placed into the equation. Which 6hould

rdarcA 1albeehme, as in foregoing discussionXand not reduced by the factor as in the earlier preceding discussion, although bear these two views in mind for further deliberations following but at this stage assuming that the comparative length parameter would be the same.In which case then so far we have the r to the four parameter becoming reduced by the square of the factor that the length of the fluid becomes increased by the time it gets to the nozzle exit but which we are not going to multiply the length parameter by for the foregoing stated reasons.

However, yet to consider is the fact that in the case of the specially shaped nozzle it will in fact commence with a larger GSA surface area over which the pressure will be exerting on the fluid in the direction of the fluid flow. Of course the extra surface area of pressure would probably not equate directly to the actual physical increase in the GSA of the nozzle entry, not least because some of the extra pressure exertion would be as much in the other two vectors at right angles to the direction flow as actually in the direction of flow. Nonetheless, when in the comparison with the straight Bellmouth nozzle entry the effective and applicable pressure exertion in the direction of flow for a given volume or mass throughput of fluid would be over a larger GSA surface area of fluid 2 flow.Which in turn would mean that the end surface area parameter, t r P, in the derivation of the basic equation would be larger in comparison, or more correct to say the r part, with the pressure, P, ie, farce, eg, lbs per unit areasremaining the same. Now it won't in fact be necessary to have to directly determine the quantity of the increase in the effective surface area of pressure,lVr , acting in the direction of flow although one probably could via some fairly complex and lengthy vector calculations.

However, the fact will be that with a Rigidity ModulUs view of the system then it can be concluded from the example discussion on the modulus properties of substances in the text book 'Concise Physics' by R.B. Morrison, pages 53 to 59, that the increase caused in the length of a given volume of fluid via the displacement of fluid volumefngthe y and z planes at right angles to the length direction will be by the same direct proportion that the effective applied pressure causing the deformation or displacement of the fluid is effectively increased by, which in turn causes the increase in the length of the fluid at the expense of fluid in the GSA dimension when in comparison to the same volume of fluid passing through a normal Bellmouth nozzle under the same pressure head.

Such a conclusion can probably very simply confirmed as follows. Referring again to the basic fluidity equation:- Fluidity = 8 5 (tP1- P2) r t For the normal flow created by the pressure head through a normal Bellmouth system then it can be seen that the fluid volume flow will be directly proportional to the pressure head because the basic equation should apply directly to such a system. Then from this it can be concluded that the mean velocitv of the fluid jet in beina volume divided bv < r will be

directly proportionallhead, as one would expect.Now since fluid velocity could be regarded as fluid jet length in unit time thenit can be said that the normal fluid jet length in unit time will be directly proportional to the pressure head. If now the same pressure head becomes effectively exerted over a larger and surface area then the increase in the fluid jet length in unit time which thereby becomes created will probably be by the same amount that the pressure exertion area in the X vector effectively becomes increased by via the special entry shaped nozzle becuase the fluid still has the same fluidity property, which in this context could be regarded as a rigidity property. Therefore since the normal fluid jet length will be proportional to the normal area of pressure exertion in the x vector, on increasing this effective area one would expect the fluid jet length in unit time to increase in the same proportion that the effective area of pressure exertion becomes increased by. Then from this it follows that one really needn't know the effective increase in the pressure exertion area, because instead one could calculate the increase in the fluid jet velocity on streamlining compared with flow through a normal Bellmouth nozzle and this increase would then be by the same proportion that one could conclude that the effective area of pressure exertion becomes increased by.

Therefore, just to reiterate the main aspect here, the effective rr r P parameter of the derivation must become increased because it is that which is giving rise to the extra streamlining as in combination with a specially shaped nozzle, without which the extra streamlining would not take place and of course wouldn't, therefore, be possible via a normal Bellmouth nozzle because such a nozzle wouldn't possess the entry shaping whereby a higher area of effective pressure would be able to be exerted onto the fluid flowing into and through the nozzle which, however, would give the normal level of fluid flow velocity one would expect to obtain from a fluid of a certain fluidity property ie, as those in the preceding exercises.This also follows from the fact that if a Bellmouth nozzle could be deemed to be the conditions of normal fluidity tests, then the calculations based on the values of such tests should be fully applicable to a system of the same conditions as those of the fluidity tests, eg, as would be the case for a Bellmouth nozzle system. Now continuing on with the preceding thread of thought.

Therefore, on streamlining, the increase caused in the length of a unit volume of fluid compared with flow of the same volume of fluid through a Bellmouth nozzle will be a direct measure in terms of a proporiton that the effective area of exertion of pressure P should be deemed to become increased by.Therefore, once again referring to the basic relationship of parameters that will be applicable to flow through a Bellmouth nozzle ie: fluidity = 8VL g (Pq - P2) r 4 t On adding the complexity of streamlining through say a venturi shaped entry we now have the following delightful situation:: (i) The total volume, V, (and mass) flow in unit time would be the same (ii) The length of a given volume of fluid flow would become increased by a certain factor determined by the level of extra streamlining, or fluid deformation, or modulus extension, achieved which I will term the x factor associated with the streamlining in keeping with the length dimension of such systems normally being regarded as the x dimension, and which I will further regard as being the increased length divided by the original length although there could of course be several ways of expressing.However, up to this stage we are neither going to multiply nor divide the length parameter by the x factor because we are considering that the part of the equation involving the length parameter ie, the outer surface area of the cylindrical element of fluid becoming forced forward, 2real, will only be concerned with the length of the cylindrical element as related to the surrounding fluid and the bondingtherewfiith, and not with the subsequent

length after streamlinino. The increase in the effective area of pressure

exertion on tne other side or tne derivation, being that which brings the extra streamlining about against the internal rigidity of the fluid uncler the Van der Waal bonding therein.Therefore, this part of the process, ie, the extra of the streamlining, will not be concerned with the extra area of pressure exertion having to overcome any extra surface area of bondina resistance with the surroundina fluid. Rather theextra

area or pressure exertion will oe only concerned wltnss tne internal rigidity within the cylindrical element of fluid as in the modulus views and when in comparison to the flow of the same fluid volume through a normal Bellmouth nozzle.

(iii) Then on the bottom line the extent by which the length of the fluid actually increases will be by the same factor increase that one would have to multiply the pressure parameter by, not because the pressure as force per unit area would increase which would remain the same value, but rather because the effective area over which the oressure exerts will

Decome increased oy tnel ractor. altnougn in anotner view one copula consider that the farce, eg, lbs of fluid, per unit area in unit time will become increased upon by the factor

Thus, so far the balance of the equation is such

that we have t\?e Frri - assoce parameterhs on the bottom line multiplied by ontz-tactor ,/lwith then just the r to the four parameter to consider.

(iv) Well embodied within r to the four on the bottom line will be two r to the two terms simply by virtue of the fact that r to the four can be broken down to r to the two times r to the two. Now know that the actual increase in the length of the fluid will be the decrease in the nozzle GSA at exit. Therefore, it can be concluded that since r to the two of the system would become reduced by the x-factor then the r to the four parameter will be reduced by one x-factor times another x-factor.

Now one of thse x-factor reductions would become counterbalanced by the x-factor increase in the pressure parameter. To leave remaining on the bottom line one x-factor reduction on the bottom line with the top line remaining the same in the case of the streamlined fluid through the specially shaped nozzle when in comparison to the flow of the fluid through a normal Bellmouth nozzle, which in turn should give the normal levels of fluid jet velocity.Therefore expressing the equation for the streamlined flow in terms of the basic relationship of parameters that would apply and be required for a Bellmouth nozzle systems, as follows: - Fluidity value = 8VL streamlined flow #(P1 - P2) x (x-factor) x r4 Bellmouth xt ( x-factor )^ Which could then be reWritten as:: Fluidity value = 8VL x (xfactor) streamlined flow #(P1-P2) x r4 Bellmouth xt ReildraWngfin practice for the streamlined flow then the r parameter would be less than that for the Bellmouth flow, and more specifically for the same volume flow in unit time then the CSA parameter of the nozzle exit would become reduced by the X-factor and therefore the r to the four parameter of the basic equation would become reduced by the x-factor squared. However, the rewritten, reduced, form of the equation is in a form which one can readily relate to since the fluidity value on the LHS of the equation for the streamlined flow can readily be seen to simply become a value equal to the normal fluidity value times the xc-factor, as one would probably expect. On the other hand, one could alternatively consider that the fluidity value of the fluidity property of the fluid should remain a constant value in being a pre determined property of the fluid. However, I don't now think that this would be a correct view since the special molecular collisions one induces into the fluid via the specially shaped nozzle would in effect increase upon the fluidity of the fluid in literal terms. In any case the volume flow in unit time would still remain the same and the difference would simply be due to that volume of fluid becoming longer and thinner on flow by an amount equal to the factor proportion, with the further difference then being that the same volume of fluid then becomes forced through a smaller nozzle exit to give a faster fluid jet velocity.The increased mean fluid jet velocity being given by: Volume in unit time GSA of streamlined nozzle exit Where the CSA of the streamlined nozzle exit will be aiven by: The Bellmouth nozzle exit CSA

d;iled b tlmesl the factor,

Thus, it follows that the range of evolutions from the basic equation could equally as readily become applied to the relationship of parameters for the streamlined flow in a number of forms.For example,

in It first expression in the foregoing,substituting fluid jet velocity for Volume divided by nozzle exit CSA as given above, as follows: Fluidity value = 8L x Fluid jet velocity streamlined flow (P1- P24 (factor) x e Bellmouth xt (x factor) 8L x Fluid jet velocity (P1 - P2)x r;Bellmouth xt Where the fluidity value for the streamlined flow equals Normal Fluidity Value tBellmouthW times the factor for the streamlined flows

Therefore, substituting by the relationship that the normal fluidity value has with temperature, as follows: Viscosity = 1 Fluidity Viscosity = a 2.718

(re-Mcgraw Hill Encylopaedia) (under Viscosity) Fluidity = 1 a 2.718

Fluidity x x-factor = x-factor increase (b/RT) a 2.718 Therefore: x factor increase = 8VL x (c factor increase) (b/RT) t (P1 - P2) x r4 Bellmouth x t a 2.718 Where the X factors will cancel and L and t can be regarded as 1, to give

1 = 8V 4 (b/RT) T1 (P1 - P2) x r a 71e Bellmouth Thenfor the expression containing the fluid jet velocity one could substitute by the energy term:- velocity

as follows::

1 = x xT baT IBellmouth a 2.718 (P1 - P2) x rl Bellmouth =8FE M (P1 - P2) x rX streamlined x X factor increase factor increase = 8 x2E a 2.718 (P1 - P2) r streamlined RT 2 Thus from the latter ex pression it would again be a simple matter to substitute actual data from off a P-E diagram for the fluid.

However, my aim herein is not to go too deeply nor too far into such potentially possible evolution from the basic equation/equations, but simply to propose the basic treatment as a possible approach to the practical application, development, advancement and progress of the process, which at this early stage may or may not be found wholly correct. Therefore the first requirement would be to have the approach and treatment thoroughly examined and scrutinsed by the appropriate experts in the field, but if deemedcorrect then I think the higher degree of simplicity of the approach could lead to higher degress of progress. However, I'm not that confident and therefore returning to one of the further main aspects of this discussion, ie, that of gaining an energy advantage via streamlining the fluid through a specially shaped nozzle.

Based on the foregoing discussions then one could well conclude that undoubtedly one should be able to gain an energy advantage in such a way. However, the all important factor will be the rigidity or otherwise of the fluid. Thus one wouldn't expect to be able to gain an advantage in such a way via cold fluid and probably only when the fluid is above the Critical Point in the liquid-vapour state may it prove possible, and even under such conditions there are obviously doubts in my mind at this pre-practical stage. However, having expressed such reservations, it would certainly seem potentially possible that some improvement would be possible via trying to induce some further streamlining into the fluid via a specially internally shaped nozzle,

of a venturi entry type, given hot fluid under a high pressure to play with above the Critical Point region.When it could well prove possible to improve the 3.36 times velocity value of the preceding exercise

associated with reduction of the nozzle GSA in the first place to give a fluid flow rate of 2.5 volumes unit containing 1 mass unit as related to the compressor outpout,by the full factor of 1.29 discussed in the preceding exercise. To then give a velocity value of 4.33 times that of the cold state reference fluid, which in turn would then just fall short of the 4.5 times really desired. The factor of 1029 of the preceding exercise

in being the increase in the length dimension of a fluid volume under the speical streamlining conditions would of course be the X factor of this current exercise.Moreover, it follows that the nozzle GSA at exit would have to become further reduced to accomodate the longer, thinner, fluid on streamlining which would be given by the normal GSA level times the x factor as a reduction.

It also follows that the same factor improvement could also be obtained under the conditions where one leaves the nozzle GSA as that required for the cold state reference fluid qivinq iust the normal mgh energy value of

the pressure head/involving recycling of a proportion ot fluid. When the

velocity value of 4.5 times the cold state reference fluid would become 5.8 times, to potentially give quite a surplus of energy in this way to make up for fluid recycling inefficiencies and energy lasses. Remember the mass flow would remain the same providing the nozzle GSA was reduced to accomodate the longer and thinner streamlined fluid which would be given by the normal GSA that would be required for the cold state reference fluid reduced by the factor of 1.29 which in turn would again be the L factor for the system.This then would perhaps be the better starting point for the initial development of the process, involving simultaneous application of the fluid recycling technique and streamlining advantage acquisition with the fluid in the liquid-vapour state above the Critical Point region and if R-21 then let us say 100 ATS at

Of course,

addition of a further applied energy source and more specifically the partial vacuum technique applying a drawing,force on the fluid flow then one would expect to gain an advantage in such a way and by such a means far mores, but with further regard to the foregoing it should be rememebered that such considerations and estimations are based upon reflation to normal fluidity values which in turn should relate directly to flow through a Bellmouth design of nozzle, and therefore one might expect to be able to improve upon fluid jet energy values via progressing to the specially shaped nozzles when relating to flow through a Bellmouth design even in the absence of the further applied force of the partial vacuum. The fluid jet velocity times values of 4.5 and 3.36 in the foregoing being those which should be obtained through a normal Bellmouth entry design of nozzle.

However, if one were also able to simultaneously add the technique of a partial vacuum application too then x factors of the order of-1.4 to 1.5 to give fluid jet velocity times values of 6.3 to 6.75 could perhaps be achievable. When one may then be verging on a surplus of energy at the sub-system stage, although perhaps thisstage of the overall process would then become just self-sustaining. To leave all the energy produced at the turbogenerating stage for output. Undoubtedly I think that such an achievement in the development of the process would be just achievable, if indeed not more than achievable once all the various techniques to Bonus Energy, ie, BE, have been perfected and become simultaneously incorporated.

However, an aspect not yet included in the foregoing treatment and approach to the system is the fact that whilst the stated factor improvements in the level of the basic fluid jet velocity will be of the order estimated.

the energy yield will not become increased by tne/ amounts even though the energy yield will

be a function of the fluid jet velocity squared.

However,

to createjincreased fluid jet velocity the cross-sectional area of the fluid flow will become correspondingly reduced with the nett effect being that the X factor increase will also apply directly to the energy increase.However, let me leave the derivation of this aspect to my work under my earlier writing on this process, hoping that readers will be prepared to take my word for this herein and at this stage in the presentation of the whole work and indeed let me leave the full correct and proper inclusion of this aspect in the work herein until a later time.

As one would expect the part of the earlier work dealing with thiS aspect is part and parcel of the work therein dealing with the derivation of the lengths to which a cube could extend into a cuboid on streamlining flow via the fluid flow mechanics mechanism of alignment of the translational molecular(notions therein into the forward vector. Which I derive via a simple straight forward modulus treatment approach but I think possibly a correct approach for the fluid flow system with sufficient accuracy. At least for incompressible liquid phase flow.

this could be an area where a different approach to the extension factors could be carried out

diFE t wNenti MdklMd aCt5 zJ 2 al 1nsre of wSdenmed value 0? Iç739 taL eewnefAC6 aR f X , but then I think one could still apply thejderived extension factors and associated CSA reductions

in tne Dasic riuiaity equation ln/ tne ~same way as being aiscussea ana evolved to give the streamlined fluidity equation, although again these are aspects that Xfitl require verification.Thus again I hope that readers will accept the extension factors stated in this discussion as probably being sufficiently correct at this early stage, which could also be termed the X-factor as an abbreviated, scientific, form of extension.

factor in the traditional scientific mould.

the incorporation into the basic equation of the addition of partial vacuum energy would probably also be a fairly simple and straight forward matter which in essence would probably simply continue on from the incorporation of a streamlining advantage down to ground state as via just the pressure head applied energy in combination with a specially shaped nozzle. That is, a cube of fluid on passing through the nozzle would

become an even longer and narrower cuboid shape to give a higher x-factor of say 1.4 to 1.5 if one assumes that my estimations of 1.73 for the potential maximum for such a system to be correct, ie, as in my earlier writing in relation to this process. Which in turn would require a nozzle exit GSA given by that required for the Bellmouth system

the now larger X factor.Then the higher fluid jet

velocity would be given by thevolume flow divided by the now even smaller nozzle exit GSA. In general it follows from the latter relationship of parameters that the fluid jet velocity woula also be given by the fluid jet velocity that would be given by the Bellmouth system multiplied by the x-factor increase.

However, the system would not yet be fully quantified because the value of P2 in the basic equation would now be lower and therefore if one firstly considered the partial vacuum technique becoming applied to the

- Bellmouth system then the differencelin such a case would be tnat tne volume flow would increase by a directly proportional amount for flow through the sane system where the nozzle GSA remained the same in a comparison between the system with and without the partial vacuum technique.

Which would then either require the nozzle GSA to be reduced to give the desired volume flow once again, or more simply a correspondingly higher quantity of fluid could become recylced. Therefore, when incorporating the addition of the partial vacuum technique into the basic equation one would first have to take these aspects into acocunt as for the Bellmouth system, simply involving a higher volume, V, parameter in direct propotion with the increase in the pressure drop from P1 to P2 across the nozzle for a system where one remained with the same nozzle GSA and recycled more fluid as required, ie, increased by the amount of the increase in the volume flow.Then on progressing to a streamlining nozzle from the Bellmouth nozzle the subsequent quantification and treatment should be exactly the same as in the foregoing involving a higher x factor

depending upon whether a higher level of streamlining becomes achievable under the application of the extra drawing force on the fluid jet flow, which so far I have been assuming would be the case, ie, as in the brief description of the creation and application of the partial vacuum techniqe herein and as in the earlier writing. Indeed in the earlier discussions I have theroised that this would have to be the case for one to acquire any benefit from the extra applied energy source in terms of extra available energy yield, and indeed for the technique to be able to become created and continuously applied in the self-sustaining manner. However,rny thinking an these aspects may not wholly strictly be correct so far because the volume flow could increase under the application of the partial vacuum which alone would be an effect that would transfer energy from the partial vacuum to the fluid flow where it would become manifest as a faster fluid jet velocity-given by the increased volume flow divided by the same nozzle exit GSA. However, referring to the basic fluidity equation once again:: Fluidity = 8V1 n (P1 - P2)r 4 t From this it can be concluded that if P1 is a 100 ATS. and P2 is normally 1ATS down to normal ground state which would normally be the case in the absence of the partial vacuum technique, then the creation and application of a partial vacuum of say 0.5 ATS would in fact only increase the volume flow by 0.5 per cent and in turn the fluid jet velocity by 0.5 per cent. Which, therefore, would be an effect that would be responsible for a very small fraction of extra energy yield compared with the extra energy that one would obtain in a vapour system where the level of the partial vacuum was the levelof the applied condensation vacuum.Which in turn is the level of extra energy that one would hope to be able to obtain in this system for the application of the same level of partial vacuum to the fluid flow, and indeed should be on applying the equal and opposite factor. However, basing on the basic fluidity equation then the only way that such levels of energy could become transferred from the partial vacuum to the fluid flow would indeed be via inducing higher levels of streamlining such that the flow of a given cube of flow becomes an even longer and narrower cuboid on flow through a specially shaped converging streamlining nozzle.- To then and thereby give a higher fluid jet velocity for the passage of a given volume or mass of fluid by an amount given by the normal Bellmouth system fluid jet velocity multiplied by the now even higher c factor of the order of say 1.4 to 1.5.

While for flow throuqh a normal Bellmouth nozzle in the presence of

applied partial vacuum energy by the same amount then1theonly energy that could become transferred would be that resulting from the increased fluid volume flow thereby caused . And of course any extra fluid volume having to become recycled would require to consume more energy in so

doing, although the fluid mass thatltravel around the larger circuit to the compressor would also be at the higher fluid jet velocity caused by the increased volume flow effect. An effect, however, which is so small that it could almost be ignored although for operation at lower P1 pressures it would become more significant.However, since the operation of the pressure is likely to be at high pressures at and above the Critical Point region then undoubtedly the main way that the energy could become transferred would be by inducing a given volume or mass of fluid flow to become longer and narrower ofl flow thorugh a specially shaped converging streamlining nozzle, probably of the venturi entry design although not necessarily for the reasons given in preceding discussion.

for the partial vacuum technique to become created and continously sustained and applied then in the first place this would require the fluid jet on importing energy to become cooled down to a level where the vapour pressure of the resultant cooled fluid was

below 1ATS to give and self-sustain a partial vacuum effect.

system may be particualr conducive to this because of the internal contraction and cooling effect that takes place by the fluid on kinetic energy becoming transferred from ti fluid, ie, one can envisage that a good initial head-on-impact of the fluid jet with the impellers of n suitable turbine could result in nuite an intensive shnrk rnnlinn

effect in the fluid at the /impact because remember the transferred kinetic energy would not have to be by an amount which when subtracted from the kinetic energy in the fluid alone reduced the temperature of the fluid since simultaneously the fluid would be contracting to render the kinetic energy remaining more rigid with stronger Van der Weal bonding and therefore also at a lower temperature.Therefore, if the,,initial

impact is such that a maximised amount of kinetic energylbecomes transferred then the accompanying contraction of the fluid could well be an effect that would bring about supercooling of the resultant fluid to a fluid temperature below the ground state of the process, eg, for the example based on R-21 > íS would be

depressurisation down to 1ATS,

if depressurisation of the fluid was down to the pressure of the partial vacuum then the associated temperature

be that which was thermadynanically associated with the reduced pressure, so that the

reduced pressure would then by~ sustalned in being created by the SVP of the fluid cooled below the normal ground state of the process. In other wards, if depressurisation took place down to 1ATS. then the temperature of the fluid should also be at that thermodynamically associated with the liquid at 1ATS. on the SVP liquid line of the fluids P-E diagram. But if depressurisation took place down to a pressure below 1ATS, eg, to 0.5 ATS. then similarly the associated fluid temperature should be at the lower temperature value thermodynamically assoicated with the pressure of 0.5 ATS on the SVP liquid line of the fluids P-E diagram, assuming the fluid follows the normal cooling curves on contraction and cooling which is likely to be the case. Part and parcel of which could be a shock cooling effect bringing about some supercooling to a lower temperature and associated SVP than would otherwise be achieved, should the initial fluid jet impact be very hard or more correct to say, very well aligned in the first place before striking the impellors of the turbine to then be in a state which can then strike the impellors of the turbine head on very hard on exit from the nozzle.

However, it follows from the preceding disucssion that the extra energy of the partial vacuum could only become transferred via a fluid mechanics mechanism of inducing extra streamlining so that a given cube becomes even longer and narrower on flow through the special nozzle. But the point is this, if the energy does become transferred in such a way and then this additional energy becomes transferred from the fluid to the turbine then the fluid must finish minus the extra amount of transferred kinetic energy and therefore must finish at a lower temperature associated with the less content of kinetic energy, which in turn must have a SVP lower than that of the fluid if just transferring kinetic energy down to the normal ground state of 1ATS. pressure.

And if the fluid must finish in such a state then it would be possible to continuously create and aPPly the partial vacuum to the fluid

jet flow because it could be't'the SVP of the cooled fluid. Moreover, in later discussion the process as could become linked to an Air ARC cycle for the heat source becomes discussed with the yielding of very cold exhaust air in the process. In the event of which a small fraction of the very cold exhaust air could become applied to help maintain the exhaust fluid of the sub-system cold so that it's SVP was that of a partial vacuum which could then in turn be the pressure, P2, continouously acting on the exit side of the sub-system turbine.Which conceivably could also be assistance providable via similar heat exchange to the water flow from which one may be extracting heat in the case of some systems operating in appropriate temperature ranges. However, here just considering the system without such potentially possible assistance.

Thus, the transference of the energy of the partial vacuum will probably be required to be via inducing extra streamlining but then if this is achieved in the first instance then the extra energy must become transferred and the resultant fluid must become cooler and the SVP it creates must become lower, which could be the continous pressure on the exit side of the turbine. Althougiperhaps it would creep slowly back up in the first instance by a mechanism of the partial vacuum becoming at a slightly higher pressure each time which in turn induced less streamlining and cooling, which in turn created a slightly higher SVP than before, etc.

Which however, could be countered by applying an evacuation pump to the isolated chamber in order to maintain the same SVP pressure as before, and which in turn should consume only a fraction of the extra energy becorring yielded, eg, equivalent to the partial vacuum energy between say 0.5 and 0.55 ATS whilst the extra energy becoming yielded would be that represented by the partial vacuum energy between 0.5 and 1ATS.

Application of the Partial Vacuum Technique with assisted Cooling: In half part at least it is in fact a very similar technique to that of the condensation vacuum technique as applied to normal vapour system but with the difference that one hopes that the fluid would cool itself.

However, perhaps this is not very realistic and perhaps it would require the assistance of cold exhaust air or a cold water flow to help with the cooling down of the fluid when on the exit side of the turbine so that its SVP then became that of a partial vacuum. In the methods of operation evolved for the combining of the process with the Air ARC cycle as the heat provision source there are some methods involving internal stages of cool air expansion and, therefore, it could be via one of these stages that in the process became applied to help cool the fluid on the exit side of the sub-system rather than consuming a proportion of the final cold exhaust air capacity for such a purpose.Although the energy advantages gain should far outweigh the loss in such capacity since the extra energy achievable should then give a fully self-sustaining subsystem - compressor cycle, with the overall process then able to yield more output energy and accompanying very. cold exhaust air capacity in the

first place. In this

processlthe source of the energy1 in fact

Visibly be the enthalpy energy contained in air from ground state to the very cold temperature of the final very cold exhaust air.

Therefore undoubtedly I think that the above way could probably definitely be a way that one could add partial vacuum energy to the normal output yield of the sub-system. Whilst via a cold water flow it may not be possible to operate the system in the necessary temperature range that

would be required, bLllt ït may not be that realistic to hope and expect

tnat tne rlula coulaicoDl itseir. un tne otner nana, since/ir tne partial vacuum energy could only become transferred by inducing extra streamlining of the fluid, i.e. higher levels of forward alignment of the kinetic energy of molecular translational motions in the fluid and such that on impact they transfer more of their initial random kinetic energy of motion, i.e.

more of that which also gives rise to the heat and temperature left remaining in the fluid after imparting energy, then on imparting the extra kinetic energy associated with the extra streamlining, which would be the only point of applying the technique in the first place, the resultant fluid could become at a temperature below that of the normal ground state of the process.

More General Discussion, cont'd.

Thus, one way or another it should be possible to reduce the temperature of the resultant fluid on the exit side of the sub-system turbine such that it has a low SVP and such that the pressure of the low SVP becomes a partial vacuum source of applied energy acting on the fluid jet flow, and if a partial vacuum source of additional applied energy drawing on

tne riuia rlow Decomes acaea ro tne pressure neaci tnen one1expect to oe able to transfer that applied energy to the fluid jet flow. But by how much? i.e. by the very small amount that the increase in the volume flow would make or by the very much larger amount that inducing a longer and narrower fluid flow would make to the fluid jet velocity and energy yield.

Perhaps this question could not be wholly answered on this theoretical side of the practical work, although it is an aspect that mav be possible

to more definitely predict basing jupon current knowledge ana tneory m tne appropriate fields concerned. Certainly if the fluid mechanics mechanism for transferring the energy could become via inducing extra streamlining

longer and narrower unit volume or mass of fluid flow, then the extra energy increase associated with the partial vacuum could then and thereby become of the same order of energy increase that would become achieved in a vapour system for the same level of condensation partial vacuum pressure creation.Moreover, whilst the addition of a condensation vacuum to such systems is usually thought of in terms of creating further vapour expansion energy adding onto the end of the normal level of expansion, if considered in terms of pre-expansion of the vapour flow in the nozzle before the turbine as achieved in and by some vapour nozzle and turbine designs, e.g. a Curtis Turbine, then the fluid mechanics of the mechanism by which the vacuum energy becomes transferred would in fact be similar.

It therefore follows that the work under my earlier writing in relation to this process could perhaps contain aspects of further importance, since therein I concentrated to a larger extent on trying to apply and quantify the partial vacuum technique. However, I don't intend to confuse this current writing on the process with the earlier writing at this stage, since I think the current writing is encompassing the concept of the process and the other main basic nitty-gritty thereof fairly well andp2r)nafsbetter than I managed to achieve in and by the earlier writing.

Although some would perhaps deem the latter to be at a higher degree of complexity, whilst I think that I have passed through to a clearer and simpler view and approach to the process, and indeed to views and approaches that are probably more wholly correct. However, having said that some of the relevant nitty-gritty not really captured in this writing so far but far more so in the earlier writing is the fact that when one bases on a Bernoulli's Theorem approach it can more readily be seen that if the partial vacuum energy becomes added to the energy of the fluid je flow, then the static/side pressure of the fluid jet flow should/would become the low pressure of the partial vacuum with the forward dynamic pressure becoming correspondingly increased in accordance with Bernoulli's Theorem.Moreover, it could also be concluded that if the pressure exerting in the side vector becomes the low pressure of the applied partial vacuum, then the fluid molecules must have become more aligned into the forward rector precisely in order for the side pressure to become as low as that of the applied partial vacuum vacuum,

in turn would result in the forward dynamic pressure becoming correspondingly higher in accordance with Bernoulli's Theorem.

Then from this it could be concluded that if in a Bernoulli's Theorem view of the system

the partial vacuum energy would become transferred to andlmanifest in the fluid flow such as to create a static/side pressure equal to that of the applied partial vacuum (in accordance with Bernoulli's Theorem?), then this must result from higher levels of streamlining of the fluid molecules into the forward x vector. Then in turn it could then be concluded from this that the fluid mechanics mechanism for transferring the partial vacuum energy must be via inducing extra streamlining, whichever view and approach one is applying to the system.Therefore, for the practical development of the process then I think one should assume that this will be the fluid mechanics mechanism at this stage, until perhaps proven otherwise, and calculate and design accordingly along the lines being discussed herein.

If the mechanism is fully or mainly via inducing a higher degree of streamlining, i.e. the creation of a longer and narrower cuboid from a given cube of fluid mass flowing into the nozzle, then obviously the hotter the fluid the more likely such inducement would be possible and again probably being most possible when the fluid is above the Critical Point region in the liquid-vapour state, since colder fluid would be more rigid and may only be able to partially respond to the extra applied force of the partial vacuum and, of course, in the comparison with the condensation vacuum system the fluid thereof is already in the vapour state at the stage the energy becomes applied, i.e. at the vapour extra expansion or extra pre-expansion stage.However, if the temperature of the initial fluid is at or above the Critical Temperature for the fluid then the more cooling it would have to undergo to render at a temperature below that associated with 1 ATS. on transferring its kinetic energy content to the turbine, but the fluid would be in a state more conducive to the transference of higher levels of kinetic energy and for the supercooling/shock cooling effect to be achieved. Thus, the BGS Energy is in fact probably better able to be acquired when operating the system in the high pressure, hot fluid, Critical Point region of the State Diagram rather than close to ground level in the first place..

A further aspect in relation to inducing the streamlining advantage in generalbut perhaps in particular if and when one is attempting to induce the higher degree of streamlining as probably required to be associated with the application of the partial vacuum in order to transfer the energy equivalent thereof to the fluid jet, could be that the potential for the streamlining advantage may prove to be improvable upon by the development and application of nozzle fluid stand in techniques because whilst the edge velocity of the fluid flow will be zero when and as the fluid jet flow leaves the bulk of the surrounding fluid in the drum it would obviously be helpful if the fluid flow didn't subsequently adhere to the sides of the nozzle from the point of view of inducing the additional streamlining.In the absence of such potentially possible techniques, then perhaps the system could only approach the potential

maximum x factor for the fluid and applied forces, e . gw / as the 50% estimat ions in the preceding, whilst in the presence of such techniques then perhaps one could achieve closer to the potential maximum for the system.

But, of course, it would then be a question of finding the optimum energy balance if the stand in technique consumed energy. Whether one would achieve a full square face or an even more pointed rat or weasel face to the fluid flow profile on application of such techniques would probably only be fully determinable in practice.However, perhaps the profile would progressively and increasingly become a square-faced profile as the fluid jet flow flowed along such a streamlining nozzle because a fluid mechanics aspect of the system will be that the dragging of the fluid flow to zero velocity around the edges of the flow will be an effect that will progressively and increasingly also drag the fluid molecules therein into a more random state and into y and z vector orientations in the planes of fluid from the centre of the fluid jet flow of maximum X vector velocity to the edges of the flow of zero X vector velocity. Therefore, it follows that it will be in fluid surrounding the centre and progressively increasingly towards the edge of the fluid wherein most of the improvements could potentially be made in the forward alignment of the actual molecules inside the fluid flow.Which if so then in theory if fully achieved the fluid jet flow could finish up with a square profile and the mean fluid jet velocity could become doubled. For example, the fluid jet velocity of 4.5 times in preceding discussion could potentially become 9 times, which in turn would give double the fluid jet energy in the comparison where the required level is 20 times and would still be so, since remember the fluid jet energy will also become increased by the same factor that the fluid jet velocity becomes increased by.

Thus it follows that even the more marginal imDrovements to the fluid jet

flow velocitv via inducin additional streamlining , becoming square

times improvements in terms of the energy yield would7give quite substantial overall energy balance improvements.For example, if in the system where the nozzle CSA is left at that through which 4.5 volume units would flow in unit time and requiring of 2.0 volume units to become recycled, which remember would be given by a Bellmouth system, one applied the streamlining advantage via use of an appropriately shaped nozzle to give an x factor improvement of 1.2, then the fluid jet energy and probably associated energy yield would therefore become increased by 20%, which would then be extra energy available to overcome shortfalls and inefficiencies.

Thus, there would now be a surplus of 20% energy associated with the energy yield from the 1 unit of mass passing around the larger circuit to the aid with the recycling of the other 0.8 mass units, which remember would also be yielding its recycling energy but obviously not fully when one takes into account energy shortfalls and inefficiencies, etc. as in preceding discussion.Thus, based on this example coupled with the foregoing deliberations, exercises and estimations, then I think that it would be agreed that it would be very realistic to consider that the sub-system - compressor cycle could become rendered fully self-sustaining via a combination and simultaneous application of the fluid recycling technique and the fluid streamlining technique via a specially shaped nozzle in combination with the partial vacuum technique, since an x factor of 1.2 is fairly small compared with the possible maximum of 1.73.

And particularly so if the partial vacuum technique proves to be reasonably successful, and then moreso if the initial energy yield is becoming improved upon via the air compression technique discussed in the preceding, which of course is a technique that could be applied to the whole of the energy yield, i.e. not only to improve upon the energy required to recycle the surplus fluid but also the energy required to sustain the compressor.And remember in this case too the source of the energy improvement will be very visible because the exhaust air from the system of the technique will be very cold and suitable for refrigeration and rainmaking and, therefore, again the source of the energy improvement will be the whole of the enthalpy energy contained in air from normal temperature to the very cold temperature, which of course is quite a considerable amount of enthalpy energy that will add to the initial turbine energy yield imparted by the fluid jet.

the'sub-system

stage one would have consumed all the fluid jet energy of the subsystem, which alone could be just sufficient, and the enthalpy energy lost from the air from normal temperature to its very cold exhaust temperature will also have been consumed by the same systems that the fluid jet energy becomes used for, which must be so because after the sub-system stage the system would be minus the fluid jet energy plus the enthalpy energy of the air with this combined energy only becoming used up by the systems to which the fluid jet energy alone would otherwise become applied. However, this is only clearly visibly the case for the air compression technique as applied to the fluid recycling technique since for this system the appropriate portion of the turbine energy, i.e.

as associated with the mass of fluid becoming recycled, would first compress air and the heat of compression thereof would then be used to heat the fluid being recycled and the resultant cool compressed air would be used to pressurise the fluid to the required pressure for entry back into the fluid flow system. Therefore at the end of such a system one would have consumed the appropriate proportion of the fluid jet energy and the exhaust air from the pressurisinn Drocess would be very cold and

therefore the combined energy of the fluid jetlpius the enthalpy energy of the air must have all gone into effecting the recycling of the fluid.

In other words, the appropriate portion of the fluid jet energy would have/must have become added to by the enthalpy energy in the air used for effecting the recycling of the fluid, because at the start of this process one would have the fluid jet energy and the air would contain its enthalpy energy and at the end of the process the system would be minus both of these amounts of energy which, therefore, must have all become consumed in recycling the fluid. All of which then makes some sense with respect to the calculations on the air compression system carried out under my PA. 8728601.

However, when one then considers the application of the air compression technique to the portion of the turbine energy required to sustain the compressor in order to render this portion similarly improved upon then one could again come into the realms of Van der Waal's invisible energy since in this case after first compressing air with the appropriate portion of the turbine energy, the heat of compression would have to become placed back into the cooled compressed air expansion as the system under by PA 8720291, ie, as the means by which the energy yield could potentially become improved upon in this case. But then in contrast the exhaust air could finish back at normal temperature with, therefore, no apparent source of energy addition to the initial turbine energy.Although in the overall process there may be other ways to apply the technique to again finish up with very cold exhaust air from an adiabatic expansion of the cooled compressed air, when

there would then be a visible source ot the energy1 improvement with the bonus of more very cold exhaust air for said purposes. For example, the heat of compression energy could be applied in the turbogenerating process to add to the normal level of heat applied from the process at this stage, to then in turn produce more turbine energy which could become used to add to the cool compressed air expansion energy driving the compressor.

ich1 could be rendered an isothermal expansion via heat trom another natural surce, e.g. water flow, when again one would be left with a visible source of the energy improvement, iet a colder water flow.

With further regard to the invisible energy source, I think that my discussion on this aspect under PA 8720291 and 8728601 will be correct as far as it goes, but I think that I will have to have another think because based upon present day and age knowledge and thinking one couldn't finish with a nett energy gain where there was no source for that energy on the energy loss side of the energy balance equation. This is not to say that the work under the above PAs is defunct, since at the least both of these processes should be able to convert fresh heat input energy from another source, e.g. gas, with approaching a 100% efficiency compared with today's levels of 40%.

However, more than this, probably it would be found in practice that the exhaust air from the processes did, in fact, lose some degrees of heat compared with the temperature of intake, to then be a visible source of energy for a potentially possible surplus energy yield from both these processes. However,

not as much as the calculations indicate in the case of the process under PA 8728601. But, having said that, I don't know for certain one way or the other at this stage; can anybody say for certain at this pre-practical stage with their hand on their heart.

it would only require the exhaust air to exhaust at -50 C from the ARC cycle of the

process for the full amount of surplus energy yield to be as calculated because this would then be slightly less than the amount of enthalpy energy cntained in air between normal intake temperature and minus 500C. and it is conceivable that placing back the heat of condensation of the process into the air expansion could render the ARC cycle fully self-sustaining whilst only raising the temperature of the air expansion to -500C, although the results of the calculations show a somewhat different picture, taking the discussion into somewhat barmier reaches.

While in the case of the process under PA 8720291 then for the much smaller order of surplus energy yields estimated the intake air would only be required to exhaust around 5"C lower than at intake for the estimated surplus energy yield to be less than that which would be lost from the air on losing So of heat on passing through the process. Which, if and when placed in the context of such a discussion, would then seem very plausible and not so barmy after all.

All of which raises one of the main peripheral aspects of the work that I would like to comment on in relation to this aspect of the work, this being that I hone readers will nut un with the barmier aspects of the

workctich as thisXprobable example, notwtnstanang tne latter comment and discussion, because it is my contention that the central core of the work is wholly sane and sound and, indeed, the way forward with basic progress into the future for the purposes of the creation of higher levels of Civilisation aimed at the continuing general Ascent of Man in general on our Planet, and indeed as such a part of the basic foundation for the further and more World-wide creation of Heaven on Earth in accordance with the Lord's Prayer, i.e. for the creation of Kingdom Come on Earth as opposed to Hell. However, work which at my initial breaking-through stage occasionally verges across the border into the barmier reaches of science fiction around the edges of the work. And I contend not viceversa, although in the final analysis that's for others to judge, and/or the proof of this puddin' will be in the eating.

Thus, I think that the current process under discussion of the whole work is one which is particularly sane and sound and even at this early stage is probably more wholly correct than most and on the ball, as the saying goes, not least because of course in the case of this process there is a very visible source of the energy, e.g. and i.e., the heat energy contained in flowing waters or the enthalpy energy contained in air providing one finishes up with very cold exhaust air.Inferring that probably if one wished to achieve via just air all that discussed under PA 8728601, then probably one would have to progress to the process

under discussion

, / proDaDly in tne process unaer aiscussion tne air compression technique could also be applied to good effect at the subsystem stage, not only to improve upon the turbine energy but also to yield additional very cold exhaust air in the process for said purposes.

To draw an aptparallel with the system of the process under discussion, the application of this technique to the system is, therefore, probably one of those around the central core of the work which would potentially give rise to quite substantial improvements in the overall energy balance and, indeed, could even render the sub-svstem - compressor svstem in

energyland especially so it in combination with the other techniques.

Simply requiring of bags of air compression equipment to apply, but the more the better from the point of view of in the process making available cold store, refrigeration, and the Big R capacity. To add to that being yielded where the heat source is via the ARC cycle. However, returning to the further potentially possible technique that could be applied at the sub-system stage, i.e. that of applying a nozzle fluid stand-in technique. If indeed such a technique would be possible to devise in the first place, which will probably be the case in the fullness of time and I hope that I haven't deterred nor thrown cold water on the work through the foregoing pulling of the punch considerations and reservations.Because once started, then who can say at this stage where things

will lead to But I certainly think that Heaven blossoming/could be on the cards. Which are also comments that could apply to the application of the air compression technique to the sub-system in the ways discussed because with this and all the other techniques applied in combination to the sub-system, then one could well be in a surplus of energy situation at this stage in the overall process, when Heaven creation would then become more possible applying the latter-day doctrinal of Dickens, just under1 Hell, just over Heaven, or words to that effect.

Thus, I am now beginning to think more strongly that the fluid streamlining techniques in combination with a nozzle fluid stand-in technique could be a way to further very substantial energy yield improvements, as indeed could be expected since one would then be involving very much more advanced science and technology in the creation of the nozzle fluid stand-in effect. When perhaps almost a full square profile to the fluid flow would be achieved because the fluid on the edge of the fluid flow could conceivably reach the full velocity of the central fluid flow under such conditions and with the application of the partial vacuum technique in combination.Whilst in the presence of the latter but'the absence of a nozzle fluid stand-in technique then perhaps the fluid flow profile would become more pointed than the normal parabolic profile, with the edge velocity still remaining zero but the central velocity increasing to give a higher mean velocity, but not as high for the applied forces as would probably be the case in the presence of a nozzle fluid stand-in technique.

Although on deeper thought the profile would probably become somewhere between a parabolic and a square profile, with the central velocity remaining the same. Say half-way, to give an r to the three relationship and a mean fluid jet velocity of 6.75 times velocity from the value of 4.5 times to give an energy value of 30 times from the value of 20 times, which could be just possible because whilst one would not expect the addition of the partial vacuum technique alone to induce such an increase it should be remembered that the 20 times level would be given by the normal Bellmouth nozzle and therefore one would also have the extra given by the special entry shaped nozzle alone inducing the higher fluid jet velocity.

Moreover, if the nozzle fluid stand-in technique is via an electromagnetic field method, then it would seem potentially possible that this could additionally be an approach to variable nozzle internal shaping and nozzle exit CSA via varying the longitudinal shape of the electromagnetic field profile.

With further regard to the foregoing, the fluid mechanics mechanism that will probably apply to this system is now perhaps clearer and one which is now moreso seeming to be highly conducive to having the modulus approach applied. Firstly consider if you will Fig. 40(a) on page 56 of the text-book 'Concise Physics' by R.B. Morrison, and, more specifically, half the diagram encompassed by AA1Q. Then consider if you will the Bellmouth fluid flow profile hypothetically being represented by ABA, then the streamlined flow moving to PQP.From this view one can conclude that as the central fluid flow moves from B to Q, so the fluid flow would become narrower in direct proportion with point A moving to point P and point A1 to P1, for a system where all the extension would be taking place in one direction and BQ would be XBQ. With this type of view in mind, now consider the fluid flow as it would probably be in practice, i.e. with the central velocity remaining the same and instead the fluid on either side increasing in velocity and catching up with the central velocity. Then in combination with this, imagine' playing tents withasheet, when as one pushes up the central pole with one's knees the sheet sides move in towards the centre.Now imagine that the central pole Js erected and that the sheet tent in end on view cross-section has a parabolic profile. Then place one's hands on either side of the knee in the centre underneath the sheet and stroke across towards the

edges AS the sheet becomes raised on either side, so the edges of the sheet will move in closer towards the centre in direct proportion. In reality in the case of the profile of the fluid jet flow, which here we are imagining to be horizontal, the profile would move from a parabolic shape for the Bellmouth flow through infinite successive stages to a full square-faced profile when the width would halve and the fluid jet length or velocity double , as becomes further elucidated upon following.However, still considering the system in the context ofthe sheet tent analogy, and again initially the end-on parabolic view representing the Bellmouth flow. Now imagine that you are lying face upwards under the sheet tent along the centre pole and place one's clenched fists up to come into contact with the underside of the sheet halfway towards the edges of the sheet on either side. Then quickly open one's clenched fist to cause one's fingers to fully straighten rapidly upwards on either side of the centre at the maximum height. Then the sheet would move upwards on either side toapproach the maximum central height and the edges of the sheet would move inwards towards the centre in direct proportion.

So one can imagine that the more random molecules on either side of the

g~4Iudz ata mas a a onDsrtWeamlining would progressively straighten out moreso into the straight forward X vector and cause the fluid flow profile to become squarer and the fluid flow to become narrower in direct proportion. A further analogy being that of randomly orientated logs in a log flow becoming more aligned, which here would take place on either side of an already aligned central log flow travelling at a faster velocity than the forward velocity of the logs on either side, which, however, when fully similarly aligned into the t vector would give the same X vector velocity and the log flow would become proportionately narrower.

Thus whilst the system is a little different than that on the stated fg.40(a) diagram ,with the extension taking place between AB and BA1

remaining the same, A would still move to P and A to P in direct pronortion and the principle would be the same.Remember also that whilst

the fluid flow would become narrower in tfl? above way tne,ena-on area or

pressure exertion would)be effec~tively larger than for the comparative

Bellmouth flow

extra extension of the fluid in direct proportion, and also that the system under discussion would be in three dimensions as the cube on Fig.41 which, in turn, is similar to the cube view given in fluid mechanic text-books.

Thus, I think the foregoing must be what the fluid mechanics mechanism of this system would be in practice on effecting the streamlining advantage because the central flow in the Bellmouth flow would probably be at a maximised state of alignment with scope for just the more random fluid on either side to become more streamlined than it would be in the Bellmouth flow, but perhaps with the potential for the fluid flow velocity to become doubled in such a way in the somewhat unlikely event of the fluid flow velocity profile becoming fully square at a maximum.

Therefore, with this view of the mechanics of the fluid flow and approach to its quanitification the potential maximum improvement would be a full

square profile, pernaps/acnievabie via the nozzle fluid stand-in technique in combination with the others. Since the mean fluid jet velocity of the parabolic flow is half the central maximum velocity, and since when the flow profile is fully square the whole of the fluid flow will be at the maximum velocity of the central flow, then the mean velocity of the square profile flow will be twice that of the parabolic flow.Then since the velocity of the square flow will be given by that of the parabolic flow times the c factor, the X > factor for the fully square flow would be two,2,i.e. the mean fluid jet length in unit time would double. Which in turn would require the nozzle exit CSA to be halved, and the square flow would have an r to the two relationship with volume flow. However, according to my exercise in my earlier writing, the x factor couldn't be more than 1.73, although this was in the context of just considering the application of the vacuum drawing energy and, therefore, I suppose that the potential maximum x factor for the svstem could be 2 as. related to a

Bellmouth flow.Having said that, the actual maximum/is likely to be of the order of 1.5 to give the foregoing estimated improvements for this value of x factor.

It also follows from such a view of the fluid mechanics of the fluid flow that when considering mean velocity as fluid length in unit time then we are really considering the mean fluid length in unit time with the actual length of the central flow in fact remaining the same when the fluid length becomes increased by the L factor.One can then conclude from all of this that when harnessing the fluid jet flow only that kinetic energy in the forward x* vector, either fully or as a vector component, would/ could become harnessed as, indeed, one would expect to be the case in such a fluid flow system

Cow - ,,in

work it was determined that the 20 times level

of energy, represents the quantity ot energy that is present in the fluid so where does the extra energy come from and how on earth can it become doubled? Well, the extra energy will come from that which is present in the fluid from the normal ground state of the process all the way down to absolute zero.However, having said that, from such a view of the system the potential maximum increase in the energy yield of the fluid jet could only be of the order of 50%, which in fact will be the correct view and, therefore, a 50x increase in the energy yield will probably be a more correct estimation of the maximum energy increase potential. Moreover, whilst I'm fairly confident of my derivation of the probable fact that because the CSA of the fluid jet becomes decreased in direct proportion with the increase in extra fluid jet velocity thereby achieved, then the factor increase as applicable to fluid jet velocity will also be directly applicable to the forward kinetic energy value of the fluid in the x vector. However, this is an aspect that as yet requires confirming, although it is something that I go into in some depth under my earlier writing.Thus, I now really need extra time to combine the two works in order then to produce a complete and correct overall work and view of the system based on one approach to the system from the starting point of the Bernouillis Theorem coupled with a P-E diagram view and that herein based on the starting point of the fluidity equation similarly coupled with a P-E diagram view.

As rnr., > A zndiscussion herein, in the earlier work I derive that the

normal level screamllnlng in a fluid flow at normal ground level will be 5/6ths of the way to full alignment in the X direction of flow and that the final 1/6th of alignment, if achieved, would increase the fluid jet

velocity by a factor of 1.73, which then/becomes an energy factor increase because of a proportional decrease in the surface area of the transference of the energy at the turbine stage.Which at this stage perhaps renders my earlier micro-mass description a little lacking, although there too it will be correct as far as it applies to the actual energy yield

is an aspect that I

included in the discussion on the micro-mass description

Now relating such a view of the fluid flow to the present discussion it would become progressed to a view that the average level of alignment of the translational molecular motions in the fluid will be a 5/6th level of alignment with the potential level of improvement being the same,

probably the analogy of stroking the underside of a sheet tent from the centre to the edges will be a correct view, since probably the improvement in forward alignment would spread from the centre to the edges of the flow rather than vice-versa.Then when the additional forward alignment becomes transferred (remember it has been concluded that only that kinetic energy actually aligned into the direction of flow1 and vector components of s could actually become potential transferred to the turbine), the fluid will finish cooler than would otherwise be the case and if transferring energy beyond that associated with transference to the normal ground state of the process then the temperature of the final fluid would then be lower than the temperature of the normal ground level of the process, which in turn in terms of enthalpy heat energy will represent the quantity of increased energy that becomes transferred and indeed could become transferred.Because, of course, one cannot materialise energy out of thin air unless fully accounted for, e.g. as in the example under discussion.

It, therefore, follows from the above that any extra energy produced in such a way should really become accounted for by the energy that is represented by the power of the partial vacuum becoming additionally applied to induce the extra levels of forward alignment of the molecular kinetic energy of motion in the fluid flow, and that any extra energy yield due to improved forward alignment from the pressure head alone in combination with a special streamlining nozzle would be minimal in comparison, as in fact in preceding discussion.

Thus it follows from the above that the fluid jet would carry out its own internal cooling, because such cooling must equate to the level of increased energy yield. However, to prevent the vapour pressure creeping.

back up to destroy the partial vacuum pressure drawing the fluid, then there would be the two methods

some extra assistance to help maintain

the partial vacuum at a constant steady state level and/ofj'additional cooling of the final fluid on the exhaust side of the turbine to again and thereby maintain the steady state level of the applied partial vacuum.

Thus, drawing these aspects of the discussion on the process to some form of an interim ending. Firstly, I think that undoubtedly there would be scope to improve upon the energy yield of the system via inducing further forward alignment of the molecular motions in the fluid flow at the nozzle stage, but

most of such improvement would/could only arise

/ applfc tion of the partial vacuum technique.Then, secondly, it follows from this that perhaps one could achieve the required fluid iet

velocity and energy increase

the nozzle CSA to give a mass flow rate of unity with the compressor via inducing the streamlining advantage via a combination of nozzle shaping and partial vacuum drawing force creation without then the need for the fluid recycling technique and the associated extra equipment, cost and bulkiness. However, based on the velocity reduction to 3.36 times in comparison to the required level of 4.5 and basing on a probably maximum x factor of 1.5, then the energy of the fluid jet would become: 3.36 x 3.36 = 11.29 then times 1.5 s 16.9 times compared with the required level of: 4.5 x 4.5 t 20.25 times.

Therefore. very probably one would have to apply the fluid recycling

tecnnique, but or course one'sti & lappIy tne streamiining wecnnaques to thetrfullest extent in order to maximise upon the energy yield at the sub-system stage and perhaps place in a surplus situation. Since then at the probable maximum x factor of 1.5 the energy yield could become 20 x 1.5 - 30 times to give 50% over that required for the compressor and fluid recycling. However, perhaps the probable maximum factor of 1.5 would only be achievable with a fluid nozzle stand-in technique in combination, with a realistic x factor of say 1.3 being achievable when just the partial vacuum technique in combination with a streamlining shaped nozzle is applied.Which, however, would give 30% over the energy required, which in turn would make up for 70% efficiencies when recycling the energy to the compressor and fluid recycling system. Thus, perhaps at such a stage in the development of the process the sub-system could just become self-sustaining, with the addition of a nozzle fluid stand-in technique perhaps placing the sub-system in surplus but depending upon the energy balance and, therefore, natural techniques could give the better nett results, or to put it another way, naturally created nozzle fluid stand-in techniques could give the better overall result.Although not necessarily, since it will be the low side pressure of the fluid flow that an electromagnetic technique would be exerting against whilst the increased energy yield could be via the high

torward dynamic pressure not rully tnereby1cratea. Because all one would be doing would be reducing the r to the four drag factor and improving upon the streamlining effect and perhaps nozzle shaping.

If the process works at all and becomes cne of the next major advancements in means of energy provision to the Peoples on the Planet then the above estimations of likely attainable performances for the sub-system at each stage of development are probably about at the right order of correctness in my mainly fluidity expert-opinion, personal experience and en endeavours

perhaps erring a little on the conservative side.

Adding that I think the process will work and be one of the next major advancement in means of energy provision to the Peoples on the Planet in my more general expert opinion, amongst other possible applications for the sub-system, e.g. refrigeration.

Then, thirdly, the1 approach to the system as

herein could perhaps form the basis of a correct approach in as far as it goes to date, at least for the practical development and advancement of the process.

Thus a useful addition to this part of the discussion at this stage would be a skeleton summary and extension of the approach and treatment so far derived and evolved. However, I think the basis of the approach requires to be fully-checked and ratified first before going to such further lengths and thereby perhaps over-inflating the approach in the event of it being deemed incorrect on such further thought, either by myself and/or others at a later date.Therefore at this early stage in the evolution of the process I now propose to progress the discussion onto other and related aspects of the Drocess. However, adding that I

think that I've probably

the approach to the practical development of the process to a reasonable initial starting point when, of course, the treatment that one then applies to the sub-system and process in general will evolve over many decades and centuries to come. In one approach perhaps along the lines being suggested if found correct and applicable in practice. If not, then it has at least been a means by which I think I have probably arrived at a clear and correct descriptive view of the fluid mechanics fo the system, and thereby probably correct techniques that could potentially become applied to the system in order to maximise upon the energy yield.

As an example of the potential for further ongoing ideas and improvements, consider if you will the concept of pulsating impellors aimed at reducing the pulling of the punch effect by a mechanism in which the impellors expanded in unison with the fluid contraction. Perhaps achievable via hydraulic fluid pressure inside hollow impellors of a diaphragm construction oscillating between two pressures in unison. En route to the next impact site, the impellor contracting under lower hydraulic fluid pressure, then expanding again during impact under increasing pressure. Thus, perhaps a way to further BE. Um, perhaps not. Then what about; normal solid impellors vibrating in unison. Etc.

Modified Pelton lssheel Design: For this one could calculate what the new curvature design of the Pelton Wheel impellor had to be for a fluid that contracted in volume as it imparted energy in comparison to that required for water which doesn't contract in volume on imparting energy. Which in one approach could involve plotting points around the curvature for the water-based system then determining where the equivalent points would be for a fluid that contracted on flowing around a new, correspondingly, contracted curvature.

Thus, as the fluid flow begins to flow around the curvature it will impart some energy of forward motion but slow down at a faster rate than would be the case for a water or hydraulic oil flou in normal systems for the transference of the same amount of energy, because they would not simultaneously contract. Thus, one can envisage that the curvature required would more rapidly curve around the bend for the fluid that contracted.

Thus, as the fluid flow begins to round the bend it will impart some energy of forward motion and slow down at a faster rate than would nor

maily be the case in normal systems, which one1 envisage would require the bend to be of a smaller size in comparison to that required for a water jet processing the same initial kinetic energy of forward motion.

Perhaps again in the ratio of the fluid density beforeandafter in comparison to the size required for the water-based svstem. Although

to tasce into account1 tne streamlined nature or tne not fluid rlow at the beginning and then its gradual change to the cold random state as it flows around the curve and imparts its energy, taken perhaps a better ratio would be the ratio of fluid length of 1 mass of fluid before and after. When the ratio would not be the values of 2.5 to 1, i.e. as for the density parameter, but rather 4.5 to 1 as for the fluid length parameter, which would also be in the ratio of the respective fluidities of the fluids before and after. Thus, as a starting point one Could determine the size of impellor required if the initial fluid jet were water then as above Actually one can envisage that a new shape of curvature would also be required, because one would want the large size at the beginning and the small size at the end, with the range of sizes

in between progressively/en route from the large size to the small size,which would be the large size multiplied by 1 over 4.5. Therefore I can envisage a method of superimposing a progression of curves of existing curves between the large to the small size, which then gave the curve required for the new system by a process of joining up all the curves in a tangential manner to form a new smooth curve.The. datum point of superimposing would probably be the central point of each curve, as in the x, y and z axis of such curves, with the last part of the smallest curve forming the last part of the required curve and the first part of the largest curve forming the first part of the required curve, etc. Which, in my considered opinion, could then give the curve required for the system. To give a starting point. But obviously one could perhaps be able to determine the curve via a mathematical route at the start, and if not at the start then undoubtedly a formula would be worked out subsequently in the ongoing development of the process. But there will be two mathematical approaches to the same curve, one fairly straightforward via calculation, and one very complex via obscure formulae.And my considered opinion is that it is the former way that would be the correct way forward into the future, and there then to be able to achieve higher things.

Then of course there would be the relationship between the fluid jet velocity and the radial turbine speed to consider in combination, which with such a curvature design obtained in such a way could, in fact. be the same as that reauired for the arrest curve related to

the initial fluid jet velocity. However, perhaps,one would sub-cool the initial fluid a little further than required at the start to further ensure that the fluid remained fully in the liquid phase on going around the bend, but after the initial fluid jet initially strikes the impellors then the fluid jet velocity to turbine radial speed could cease to matter as the fluid flowed around the curve, to finish with zero velocity with respect to the surrounds. Thus the ratio could still be 2 to 1 for the initial fluid jet velocity to the required radial speed for such a fluid jet.It probably being a case of either correct the curve design or change the radial speed in a progressive manner and not both, and obviously the latter would not be possible. However, when trying to improve upon design in an impulse jet - turbine method, then probably higher rewards would be obtained from the starting point of the turbine blade design of, for example, the type of turbine employed in diesel-hydraulic locomotives, since the impellor cups oFa Pelton Wheel would not really be a good starting point from which to eventually achieve a precise design for the fluid flow. But in a turbine blade method then the approach to the required new design compared with that required for hydraulic fluid could be similar, and it is considered that from such a starting point ,then one could probably achieve a precise design.Moreover, this type of impellor blade would be more conducive to initial head-on impact followed by fluid drawing via a partial vacuum on the exit side.

Whilst in the use ot a Reaction Turbine, then perhaps all one would require is knowledge of the science involved in order to determine better optimum conditions, more simply in combination with the correct nozzle exit CSAs. However, progressing on with other related aspects of the system at this more general stage.

But firstly stating, after giving consideration to all the aspects deliberated upon herein, that one would probably apply the impulse jet-modified Pelton Wheel system in the method of operation discussed herein in which one had a higher ground vapour pressure inside the isolation chamber of the sub-system, eg, the 25 ATS. as discussed in relation to the possible process based upon R-13, and in which one would hope to be able to achieve some bonus energy by being able to sweep aside the vapour away from the immediate vicinity of the turbine iinpellors in order then to be able to harness fluid pressure energy to a lower pressure than the 25 ATS. of the immediate external environ;nent, eg, to 1 ATS., for the expenditure of less energy in so doing.Which in turn could be the better apply in Ships for the various stated reasons discussed herein, eg, to better facilitate for variable sea heat temperature.

Whilst for the addition of partial vacuum energy to the energy yield at the subsystem stage in the ways discussed herein then firstly one would probably apply the method based upon fluid jets pointing downwards and passing through a rotating blade of the type applied in hydraulic fluid turbines, eg, as in diesel-hydraulic locomotives, since via such a method one should be able to very effectively apply the partial vacuum technique in being present in the isolation chamber and acting as it would directly on the underside of the rotating blade drawing the fluid through the channels thereof, ie, as depicted on Fig. 1D.

Then perhaps progressing onto a reaction turbine of the design depicted on Fig. 1 in both the above systems. Or perhaps one would try this way first in both the above systems.

GENERAL DISCUSSION CONTINUED: STREAMLINING: It follows from the foregoing that maximising upon the streamlining potential of the system via the three techniques of: A) Internal nozzle shaping, firstly at entry to the nozzle.

B) Application of the Partial Vacuum technique as creatable via the low SVP of liquid phase fluid that is caused to become substan tially cooler than the normal ground state of the process which would have an associated SVP of normal 1 ATS above the resultant liquid phase. Either by internal cooling alone or internal cool ing plus the aid of some external cooling, e.g. as could be achievable via cold exhaust air production in the process.

C) The application of a nozzle fluid stand-in technique whereby the fluid flow on leaving the main bulk of the fluid and entering the specially shaped nozzle is caused by some technique or other, either naturally in-built into the system or created with further external assistance, not to then go on to naturally adhere to the sides of the nozzle internal walls but become repelled away in order that the fluid could then potentially become caused to be streamlined to its fullest potential.When the transference of kinetic energy from the fluid would be higher and therefore the energy yield would be higher and the resultant fluid liquid phase exit from the turbine would be correspondingly colder, which in turn would therefore possess a lower SVP as would be associated with the colder temperature of the exhaust liquid phase, which in turn would sustain the higher level of streamlining, ad infinitum would be one of the main development routes to take in the ongoing development of the process.

Then, coupled with these techniques would be the rendering of the fluid at an optimum state of temperature and pressure most conducive to enabling the fluid to become streamlined to its fullest potential,as the initial basics, but then one can imagine that there may be additives that one could add to certain fluids to render them more streamlineable, i.e. not to thereby create further streamlining potential but to render the fluid more conducive to achieving the predetermined maximum streamlining potential. Which would b'e a further and separate secondary technique to add to the mpre basic ones, although it could conceivably be in combination with a nozzle fluid stand-in technique as a simultaneous effect.

Since the creation of the heat of compression is likely to be to a high temperature in the first place for the purposes of the generation of power at the turbogenerating stage of the process, then the compression pressure creating the heat of compression is likely to be required to be to a high pressure in the first place. Then it will be a question of leaving sufficient heat remaining in the fluid at the turbogenerating stage in order that a maximised streamlining advantage could then be achieved. Which, remember, will largely arise from the transference of the partial vacuum energy into the fluid jet flow as induced further forward alignment of the translational molecular motions of the kinetic energy in the fluid flow.Which in turn could only take place if the kinetic energy is sufficiently loosened from its cold state Van der Waal bonding as to be able to respond and become further aligned. Otherwise one imagines that the cold state fluid may only yield extra energy equivalent to that which the extra volume flow would yieldRkthen as the temperature of the fluid increases one can imagine that this minimal basic level of energy increase would become progressively and increasingly added to by the streamlining alignment fluid flow mechanism until at some stage one was achieving the potential maximum from the streamlining.Which obviously would be a finite amount and be when the parabolic flow profile becomes a full square profile, when in descriptive theory the fluid flow velocity would become doubled because the mean velocity of parabolic flow is half the maximum central velocity (ref: Fluid Mechanics by Henke, page 146, Fig.

14-2) and for a square profile all the fluid would attain the velocity of the central maximum velocity of the parabolic flow, when the nozzle exit CSA would become halved for the same volume flow travelling at twice the velocity. However, according to my shear modulus exercise the maximum potential increase would be by the factor of 1.73. Therefore, via these two separate views of the fluid mechanics of the system one arrives

at slightly different results and, therefore "1S one of the areas of the work that requires some further thought.When comparing against the normal fluid flow through a normal Bellmouth nozzle,when the normal fluidity value and basic fluidity equation would apply as in the foregoing approach and treatment to the quantification of the system, then Iperipstend to favour the view that the fluid flow velocity could potentially be doubled as an absolute maximum and literally so since this would necessitate forward alignment of the kinetic energy in the fluid flow all the way down to absolute zero in terms of the heat involved, when a full square profile would then be achieved.However, this obviously would not be realistic in practice and in any case could only be to the level represented by the partial vacuum, which in one form could be expressed in terms of its temperature, but more specifically if one looks at the P-E diagram for the system then it would be the equivalent of the enthalpy energy on the horizontal axis of the diagram from the normal ground state to the fluid state thereon at the lower vapour pressure and temeprature of the partial vacuum. Which however could be rendered at a lower temperature and associated SVP partial vacuum with the aid of very cold exhaust air that may be becoming produced in the process.

Thus, the estimate of 1.5 times potential maximum would still be the realistic value and, of course, it will probably make no difference to the foregoing treatment how the x factor of the Streamlined Fluidity Equation as it is found to be in practice could or should become derived in theory. Although from the point of view of the ongoing development, improvement and perfection of the system then it would obviously be better if one was aware of the precise fluid mechanics mechanisms taking place inside and surrounding the fluid flow, e.g. the view that improved forward alignment on streamlining and taking place under the influence of the partial vacuum would in practice be as though the laminar flow streamlines to either side of the central streamline would become more forward aligned to approach the velocity of the central streamline already at a maximum of forward alignment and therefore velocity, etc.

With further regard to the above, it is of interest to refer to the diagrams of fluid flow under Professor White's text-book on fluid mechanics on page 330. Where, on Fig.6-ll(a), a diagram of normal laminar parabolic flow is given which will represent that which would probably be obtained on and after flow through a Bellmouth nozzle.Then on adding the further streamlining influences of a specially shaped nozzle in combination with the partial vacuum technique, the foregoing theory postulates that the streamlines to either side fo the central streamline would not be as forward aligned as the central streamline in the normal parabolic flow, but could become so under the additional streamlining influences to a theoretical maximum represented by a full square profile flow of twice the velocity and half the CSA, with all the flow at U max, i.e. not to be confused with the square profile of Fig.6-ll(b), although one could visualise this to be the type of profile that could become achieved in practice at the higher velocity of U max. in the laminar flow.For a full square profile then the volume flow would have an r to the two relationship and not an r to the four as in normal parabolic flow, by which I mean that volume flow would then change in direct proportion with nozzle exit CSA and not just velocity. But in practice perhaps just the equivalent of an r to the three relationship would be possible. If one considers the diameter of the GSA of the normal parabolic fluid flow to be 1, then the full square profile of half the CSA would have a diameter of zero point 707 and would correspond with an x factor of 2 in the Streamlined Fluidity Equation. While if a maximum x factor of 1.8 was actually achievable in practice, then the diameter of the fluid jet would become zero point 747.But in reality perhaps only barely achievable and then probably only when in combination with both the partial vacuum technique and a nozzle fluid stand-in technique to repel the fluid flow away from the internal sides of the nozzle and an x-factor of 1.5 would probably be a closer estimate. However, in this way also drawing the distinction between normal laminar flow of a parabolic profile flow, which hitherto is usually spoken of as streamlined flow, and what I will start to refer to as super streamlined fluid flow involving an x-factor in the conversion of the basic fluidity equation to the Streamlined Fluidity Equation in the manner under discussion. When for an x-factor of 1.5 in the straight-forward direction the nozzle diameter required would be zero point 816, which isprobably where we may get up to with this lot eventually involving just an 18% decrease in flow diameter at nozzle exit to give a 50% increase in nozzle fluid jet power.

However, a nozzle diame~ter reduction of 10% probably seems more reasonable which would correspond with an x-factor of just 1.23 to give a 23% increase in the nozzle fluid jet power.

All of which brings the discussion to further related aspects of the system which I will progress onto whilst feeling that the foregoing deliberations probably still leave a lot to be desired, which however could become progressively and increasingly added to in an Appendix Section, at least this is one of my current intentions.

Vapourisation: One oF the further related aspects being that of the avoidance of fractional/flash vapourisation taking place as could potentially occur either as the fluid jet leaves the confines of the nozzle exit and enters the low pressure environment that will exist between nozzle exit and turbine impellors and/or at the point of impact of the fluid jet with the impellors of the turbine. Of course this is one of the areas where the use of a reaction turbine of the type depicted on Fig.1 could improve the system by virtue of the fact that the potential possibility of such vapourisation taking place, and if so detracting from the energy yieldable, would become removed because the fluid would be under the confines of such a turbine and, more specifically, under the pressure therein during the period of the transference of the energy.However, here remaining with the discussion in relation to an impulse fluid jet system, although again making mention of the fact that in the earlier writing I moreso concentrate therein on the use of such a reaction turbine in the system, In relation to this possible failing of the impulse fluid jet systems, which in fact perhaps has more good aspects than failings, one of the main ways to overcome this potential failing will in fact be to operate the system above the Critical Point'region at a higher pressure and temperature in combination with super-streamlining the fluid jet on its creation in the nozzle,because under such conditions then the fluid state would not possess any latent heat and therefore couldn't flash fluid en route from the nozzle exit to the impellors, and once there would impart its kinetic energy of impact before it had a chance to become flashed fluid.However, if operating the system below the Critical Point region then the fluid d would be in the liquid phase at the start of the operation with the possibility that some of the fluid could flash off into a vapour phase en route to the impellors to detract from the kinetic energy of impact. If so, then one way to overcome this could be to sub-cool the liquid so that its initial starting state is well past the saturated liquid line into the liquid phase.

However, if one now changes to a Bernoulli's Theorem view of the system then as far as the pressure of the fluid jet is concerned one will become nnoreso aware of the fact that the initial random pressure of the fluid will become polarised into a high forward dynamic pressure and a low static pressure since this theorem will quantify the fluid jet as follows: Prandom = Pstatic + F MV2 Therefore, if the energy represented by the expression 15 MV2 equates to the energy contained in the initial fluid down to the grdund state pressure of the system, then one could conclude that on the creation of the fluid jet the static pressure should in fact become that of the ground state pressure of the system, i.e.P2 in the fluidity equation, which in turn would be the pressure exertion of the fluid jet in the side vectors. In which case then perhaps one wouldn't in fact expect any flash vapourisation to take place from off the surface of the fluid jet en route to the impellors because the outward pressure exertion by the fluid molecules contained in the fluid into the side vectors would already be as low as the external pressure surrounding the fluid jet.However, if the associated static temperature of the fluid jet was higher than the temperature associated with the low pressure when in the SVP equilibrium state then perhaps some flash vapoursation would take place as in a normal system under such conditions until the vapour pressure acting on the fluid becomes such as to suppress any further vapourisation from liquid phase now at a lower temperature in the establishing of the SVP equilibrium state. Thus far in my endeavours, extensive as they are, I have in fact only got as far as determining the static temperature of a perfect gas flow.Which, however, will be an exercise of interest to carry out here because in the process it will give a worked example of the foregoing approach to the system via the fluidity equation in part, and should be of approximate accuracy for a fluid jet flow in the liquid-vapour state and/or highlight an area of the system of probably some primary importance where there is yet work to be carried out.

Thus for a perfect gas: CpT + d VZ s Cp To As given under Professor White's text-book, page 521.

Where To is the temperature of the random molecules.

T - the temperature exhibited by the fluid molecules inside the fluid flow, at right angles to the direction of flow between the stream lines and on the outside of the fluid flow (I think?). But perhaps the mean temperature for parabolic flow in the light of the preceding discussion, with the temperature gradient being higher on the edge of flow than at the centre. Whilst in the case of a square profile that would become created on the formation of a perfect gas flow then the temperature would be expected to be the same across the full width of the fluid flow.

V - the mean velocity of the fluid flow.

Therefore: V T = To - Cp For V units of feet per second and T in OR then Cp will be in BG units.

Therefore: Cp = &gamma; R &gamma;-1 Where 2 = Cp/Cv and for the purposes of this exercise will be approximated to 1.25.

Thus, for a fluid at a random temperature of 18O0C: Cp = 1.25x672 = 3360 in BG units 0.25 Preliminary Calculation Example: Determining the velocity of the streamlined fluid jet via the fluidity equation as follows: Firstly for the cold state reference fluid: mgh = h MVZ V ft/sec. = j2gh

for a random pressure of lOOATS.

= 463 ft/second.

Then secondly, for a hot fluid of 4.5 times the fluidity value of the cold state reference fluid, as in the example under discussion, then the fluid flow velocity through a Bellmouth nozzle of the same nozzle exit CSA will be: 463 x 4.5 = 2084 ft/sec.

Then thirdly, changing from the above nozzle to a streamlining nozzle, which I will assume for the sake of this exercise is creating a fluid jet flow with an x factor of 1.3 in the Streamlined Fluidity Equation assuming that the system is achieving the addition of some early

stage partial vacuum energy, in the absence of which the x factor may become around say 10X. Thus the fluid jet velocity would become: 2084 x 1.3 = 2709 ft/sec.

Which out of interest compares with steam fluid jet velocities of typically 3300 ft/sec. in normal steam turbogeneration, whilst an x factor of 1.5 would give the same order of fluid jet velocity..

Then fourthly, from the velocity value of 2709 ft/sec. can be deter mined the required nozzle CSA dimension at exit for the streamlining system for any desired capacity of fluid volume flow by simply dividing volume flow in cubic feet per second by the velocity in feet per second to give the required nozzle exit CSA in units of square feet initially.

Then, fifthly, two parts in every 4.5 parts of the volume flow, i.e.

44.5%, would require to be recycled back into the fluid flow at nozzle entry via the fluid recycling technique, whilst the other 55.5% travelled on around the larger heat-absorbing cycle of the process.

Then sixthly, now applying in the relationship: T = To - V2 Cp 2709 = 672 3360 = 672 R - 1092 R = -233 K Then seventhly, probably back to the drawing board on the latter result, However, I think one can conclude from the latter result that the static temperature of the fluid jet is in fact likely to become at least that which would be associated with the low static pressure of the fluid jet if 150an SVP equilibrialised state, as one would probably expect, which in turn is likely to be the pressure of the external environment.

Therefore from this point of view too one would not expect any flash vapourisation to take place off the surface of the liquid jet, even if as in the pre-random state it would vapourise if placed under the low surrounding pressure. At least during the stage between the nozzle exit and impellors. Apart from the fact that there is the probably as yet unknown of a static temperature gradient from the centre to the edge and increasing towards the edge. If one considers further the situation of the edge velocity being regarded as zero, then in + The preliminary calculation thus far still contains a known initial basic error which becomes explained and corrected on pages 342 - 350.

practice this must mean that the fluid molecules immediately around the outer surface of the fluid jet would be pointing towards the side at right angles to the direction of flow because the edge fluid will, of course, also flow from nozzle exit to imDellors. As one would exoect.because

these fluid molecules are deemed to betas whenbonded to adjacent1 fluid in the side vector at right angles to the direction of flow, which in practice as the fluid jet travels across the gap with the edge molecules on board too could be deemed to have been left standing facing out to sea on either side as it were rather than facing in the direction the ship was travelling.And as such,even though on board,not contributing anything to the power of the fluid jet on its impact with the impellors of the turbine apart from the proportion of the cold state.reference fluid jet power that

they, represent simply as cold masses. Whilst tne molecules OI tne central streamline in having the highest velocity of the fluid flow velocity profile must be at a maximum level of forward alignment for the system.

Therefore, if the fluid molecules on the edge ofthe fluid jet flow are pointing in the sideways vector on exit from the nozzle exit

the temperature and probably static pressure being higher with the external environment being at a lower vapour pressure and temperature, then obviously this could give rise to problems and quite a substantial amount of vapourisation could take place off the surface of the fluid jet by the time it reaches the impellors of the turbine. Which, however, is perhaps an academic view in the context of this system because if one is operating the system above the Critical Point,with the fluid at the start in the liquid-vapour state and containing no latent heat, then the fluid jet

would te susceptible to erosion via a fluid flashing mechanism off the surface of the fluid jet between the gap, and probably similarly when on impact with the impellors of the turbine providing the kinetic energy of the fluid jet become efficiently and rapidly transferred. Although obviously it would be important to super streamline the fluid jet on its creation as much as possible to avoid fluid molecules flying off at a tangent into the surrounding low pressure atmosphere prevailing in the gap and acting on the surrounds of the fluid jet flow.But in this respect such a system should be no more difficult than found for steam generation and indeed could be better because in such a system the individual fluid molecules are fully separated from each and repelling each other and moving further apart as the steam expands in the nozzle, whilst for the system under discussion the fluid would have some characteristics of the liquid phase and the tendency of the molecules therein would be the exact opposite, at least to tend to moreso keep each other in line better on streamlining.

However, in the case of a starting fluid already in the liquid phase then perhaps some erosion of the fluid jet could take place in. the gap and on impact with the impellors of the turbine whilst under the low vapour pressure of the surrounding environment and because of being under a low pressure. Although if the static temperature of the edge fluid of the fluid jet does become at the temperature that would be associated with the surrounding low pressure environment in an SVP equilibrium, as the

early calculations would seem to indicate may be the case, and the static presure exertion in the side vector became that of the low pressure environment, then I don't think that any such flash vapourisation could take place even though if on subjecting the pre-random fluid state to the low vapour pressure and temperature then the fluid would flash off in the normal way, i.e. until the vapour pressure had become built up to a level which suppressed any further vapourisation in an equilibrialised stateconsuming the heat of the liquid phase to provide the latent heat for the vapourisation which therefore would simultaneously cool down to be and give the temperature of the equilibrialised state.However, when the fluid polarises into a fluid jet it could well be that the static conditions of temperature and pressure of the fluid jet are as the surrounding environment and therefore already become in a state necessary to be in equilibrium with the surrounding atmosphere during the creation of the fluid jet whilst still within the confines of the fluid jet creating nozzle, which in the context of a throttling device route to the establishing of such an equilibrialised state could be regarded as a

to the establishing of such an equilibrialised state.

However, the only question now being whether or not a static temperature and pressure gradient will exist and such that the surface molecules would be prone to vapourisation in the gap and on impact with the impellors of the turbine. If as the cold state reference fluid on the edge of the fluid jet flow then again probably not, but if left jostling about in a heated agitated manner with some vigour in all side vector random directions, then perhaps so.Obviously further streamlining could help but then the external environment would be at a lower vapour pressure to give rise to the further streamlining in the first place and, therefore, in such a case one would probably turn to the approach to the system based upon a reaction turbine of the type depicted on Fig. 1 because the energy of the fluid would become transferred to the turbine whilst still within the confines of the turbine.However, how much of

the heat energy, two add to that of thelmgh- ground level energy of the pressure head,would become transferred in such a turbine would ultimately have to be determined in practice, but it may be found that one may only acquire an increase equivalent to the increase in the fluid volume that the additional heat energy makes plus any streamlining that one can induce into the fluid flow as it flows along the exit leg of such a turbine, which however could be high to give an energy yield equal to that which one could theoretically acquire via the impulse jet system if only fluid jet erosion did not take place in the gap.In other words1 and for the purposes here basing on the values of the main example herein, the heat content in the fluid would cause the fluid to expand to 2.5 times the volume and therefore whilst in the random state one could expect to acquire at least this order of increase in energy due to the heat addition, but then if on the exit leg of such a turbine one can fully streamline the fluid from the random state to the level of laminar flow

streamlining and thefl1super streamlining that one could achieve before the turbine in the case of the impulse jet system, then probably the same levels of energy could become obtained.In relation to this aspect of such a system the log description is quite good via which one can visualise the logs pushing the turbine backwards at a faster rate as they straighten out along the exit leg than otherwise would/could be the case if the random fluid simply flopped out of a normal non-streamlining exit of such a turbine, when just the 2.5 times level of energy increase associated with the volume increase may be only that to be expected.

It therefore follows that probably those fluids with a very high fluidity even at ground state and below could be more conducive to this approach, eg, R-13.

because the lower fluidity fluids, eg, R-21, would obviously stiffen up moreso and not be as alignable at such a stage. However, later in the continuation of the preliminary calculation example it will become shown that probably the nozzle bore in the use of R-13 will be required to be very much smaller than for the lower fluidity fluids which could necessitate far more accurate precision tooling, but depending upon the size of the fluid volume flow possible through each nozzle bore. It follows, that the final legs on the reaction turbine would have to be shaped as the streamlining nozzles for the impulse jet stream.

With further regard to the above approach to the system via a reaction

turbine, I think that I may be correct in having arrived at a1 conclusi on that recent advances in Pratt and jitney aerojet engines aimed at achieving extra fuel cost savings must depend upon a similar mechanism of extra forward alignment to create a higher thrust reaction force for the flow of a given mass of fluid, in this case induced by partial vacuum rear wake zone forces in combination with the drawing force creatable via surrounding streamlining air? Therefore, such a recent facet of the advancing front of science and technology could perhaps be expected to occur again at the beginning and at the forefront of the new technology under discussion to advance this facet of science and technology further and potentially leading to all manner of Craft where one needn't bother about trying to achieve fuel cost savings because there wouldn't be any.

However, this may be partly academic in the case of the main process type under discussion herein because perhaps every time in the operation of the sub-system one could operate the system with the starting fluid already above the Critical Point region when such considerations of possible vapourisation in the gap and on impact would not be necessary for the aforegoing stated reasons.However, there may be occasions when one would wish to operate the systems with the starting fluid already in the liquid phase. ror example when perhaps incorporating the sub-system into the Intermediary Brierley Process, i.e. the IBP-O, to help convert it into the Advanced Brierley Process, i.e. the ABP-O, via the replacement of the elaborate condensation system thereof, then one would probably want to operate the system with hot fluid already in the liquid phase at the beginning of the sub-system stage when it may, therefore, be necessary to turn to the use of a reaction turbine for the aforegoing stated reasons.On the other hand, perhaps not depending upon how much side vector vapourisation during the time the fluid jet is in the gap and on impact takes place under the impulse jet method under the desired conditions of operation. i'hich, however, again may be academic because I'm not yet fully sure whether even the Advanced Brierley Process would add to or detract further from the overall energy balance of systems of the work in comparison to the alternative use of more conventional approaches in similar system arrangements, which again may ultimately only be determinable in practice, although it may be possible to predict in advance.

Certainly I think rne j-coulA be an approach to fully self-sustaining very cold exhaust air production for Rain-Making, Refrigeration, Cold Store and generally cooling the place down, but whether one could get even a trickle of surplus energy yield for output supply, or indeed whether one would instead have to have a continuous trickle of energy input even for such applications, I'm not sure, but this could be the borderline situation of the Advanced Brierley Process. However, having said that, I now think that the process would

be capable of producing quite a surplus of energy when combined with the ARC cycle and simultaneously yielding very cold exhaust air for the above purposes, since the compressor~ - sub-system arrangement under discussion herein would be used to apply to the exhaust vapour from the main turbine - SE system arrangement and would be able to condense the vapour phase back to the liquid phase for recycling back into the ABP-O, whilst at the same time recycling much of the latent heat of condensation back into the fluid becoming heated to effect the vapour generation in the ABP-O. If all the latent heat became recycled then the conversion efficiency of the heat of compression from the ARC to which the ABP-O would be combined in one method of operation as the fresh heat input source would approach 100% conversion efficiency, with the ARC cycle only requiring 40% of this energy to be rendered fully sustained. However, as in combination with the compressor-sub-system arrangement, then

around 50% of the latent heat would become recycled for the next cycle, to leave just 10% of the heat of compression as turbine energy for output suttlv after making uD the then shortfall

in the ARG cycle.Thus again thejsource ot the energy would be that m the air from NTP down to the very cold temperature of the exhaust air, and the compressor-sub-system arrangement would simply be a means to condense the turbogenerator fluid back to the liquid phase for the next cycle, whilst at the same time effecting the recycling of a large proportion of the latent heat energy that otherwise becomes discarded in current processes. Thus the system wouldn't be adding any extra energy, but simply effecting these two functions.Then the other main addition to the process would be the SE system to the rear of the turbine in an arrangement where the extra drawing force on the turbogenerator fluid thereby created would help draw the vapour flow further to improve upon the multi-stage vapourisation system and the extra energy yielded of the drawing force would become recycled to continuously operate the SE system.

Thus the compressor-sub-system arrangement could probably be applied in the above way, not just in combination with the ABP-O but also in more conventional turbogenerating processes to similarly effect the condensation of the exhaust vapour for the next cycle of the process whilst at the same time effecting the recycling of the latent heat which is an aspect dealt with more fully in a part of the work that, for now, I have entitled the Process-P range of processes. However, again maximising upon the energy yield of the sub-system will be all-important and probably the main way of achieving this will be via the partial vacuum technique under discussion. Thus, returning to the preceding threads of this discussion.

The use of a reaction turbine of the type depicted on Fig.l, coupled with hot liquid fluid flow, is in fact another area of the deliberations in my earlier writing in relation to the sub-system and therefore this part of this discussion could be regarded as another dovetail joint in the early stage combining of the two works. Therein, I in fact theorize that since the partial vacuum pressure if created would be acting directly on the exit nozzle of such a turbine, then perhaps it could induce the additional streamlining of the fluid in and along the exit leg of the turbine with improved efficiency, as via the log description mechanism.

Which raises the question of whether one could in fact induce the streamlining advantage potential into a system based upon an impulse jet method.

For example, in an impulse jet - Pelton Wheel type of system, then whilst the system could be in an isolation chamber in which the vapour pressure therein could be low vapour pressure well below 1 ATS. associated with cold liquid phase fluid, would that alone enable/cause the fluid jet to become streamlined to the level that could potentially be associated with the low vapour pressure, or would the extra drawing force of the partial vacuum have to become applied more directly to the front face of the fluid flow? If so, then the better impulse jet system for applying the partial vacuum technique could be that of downward pointing jets into a single rotating blade, with the low vapour pressure of the liquid phase immediately on the underside of the rotating blade and acting directly on the fluid channels through the rotating blade above, with the cold liquid phase dropping to the bottom of the isolation chamber housing the system and in turn giving rise to the low vapour pressure above it and beneath the rotating turbine blade. Which, in turn, should draw the fluid jet on its actual formation in the streamlining nozzle to the higher level of streamlining associated with the applied partial vacuum at the nozzle stages rather than all take place subsequently in the channels of the rotating bladevvia a pulling or drawing force chain reaction mechanism back along the lines of streamlining molecules.The equivalent in steam powered systems would be that of pre-expansion nozzles in which the power of the condensation vacuum becomes transmitted into the fluid jet on its formation in the nozzles ahead of the turbine impellors themselves and there becoming manifest as a low static pressure and a correspondingly high forward dynamic pressure, i.e. a fluid jet of correspondingly higher mean forward velocity. Thus, similarly the formed fluid jet prepossessing the extra power associated with the extra applied energy of the vacuum before impact into the impellors of the turbine. Which I think is achieved in steam turbines known as Curtis Turbines, although this is an aspect that really requires further verification.

However, from a different view of the system under discussion and perhaps a correct view then one could perhaps conclude that the potential level of extra streamlining could perhaps be equally as achievable via the impulse jet - Pelton Wheel type of system, because in this view one considers that a certain level of streamlining would be achievable simply as associated with the ground state of the system, which for this part of the process and this aspect of the system would be the conditions inside the isolation chamber.Thus if the environment in the isolation chamber was comprised of fluid saturated vapour pressure well below 1 ATS. and at the associated cold temperature of the SVP, then fluid streamlining as associated with these ground state conditions should be possible,' and beyond a lesser level ofstreamlining that would be possible if the environment was at normal 1 ATS. and the higher temperature associated with an SVP of 1 ATS, which in the earlier writing I derive and postulate would be streamlining 5/6th of the way to full alignment with just 1/6th of the way to go, but a 1/6th that could add 73% extra fluid jet energy and representing the enthalpy energy in the fluid from normal ground state down to absolute zero.

Deliberating on this aspect from a slightly different viewpoint.

It the normal ground state of the process was 1 ATS. and'jassociated SV? temperature then in the absence of any additionally applied force one would only expect to achieve a certain level of streamlining as associated with the normal ground state and as would yield the energy quantity down to the normal ground state.Then on transference of said amount of kinetic energy the resultant fluid at ground state would still contain its ground level of kinetic energy giving rise to its associated ground temperature and a ground level of random motion of molecules in the fluid.

wnich1would be kinetic energy and random motion tnereor tnat potentially could additionally have become transferred to result in a colder fluid at the end containing less kinetic energy of less random motion closer to absolute zero if only one could have pre-streamlined the kinetic energy moreso on the creation of the initial fluid let. But iust as in the ex

pansion ot gases beyond tne level associates wltn 1 A5,11t is not tne so termed drawing or suction power of the partial vacuum below 1 ATS. that causes the gas to expand further, but rather that the pressure of 1 ATS prevents the gas expanding any further than the expansion to 1 ATS which it would otherwise do to whatever level the external pressure would not

So in the case of the system under discussion under an external pressure of 1 ATS. streamlining would only be achievable to a level in which the molecular randomness that would be present in the random fluid at 1ATS.

and normal temperature was still remaining in the streamlined fluid jet.

However, if the external ground state conditions are at a lower pressure and associated temperature then it follows that streamlining to a higher level should ensue in which the molecular randomness left remaining in the streamlined fluid flow is that associated with the lower ground state conditions. However, this again is an aspect that may only be fully determinable at the practical development stage of the work and perhaps the partial vacuum technique would not be achievable via an impulse jet - PeltonWheel arrangement, but it should be achievable via the other arrangement of fluid jets acting down on a rotating blade with the partial vacuum beneath and more directly drawing the fluid through the blade channels and nozzle. Or perhaps two rotating blades, one beneath the other.The fact that the fluid would become in the liquid phase if not fully in the liquid phase at the start should again be helpful in such a fluid drawing mechanism because as the fluid cools and contracts and becomes more fully in the liquid phase then the Van der Waal bonding therein will become stronger, which should be a mechanism that helps draw the following fluid in the nozzle to the level of streamlining that could potentially be associated with the partial vacuum becomtnqapplied,

oerhapslmoreso than in a pre-expansion nozzle ot a vapour system.

It follows from the above view of the system, that a fluid in the liquidvapour state would again be better from this point of view.

It/follows that one could probably determine the x factor associated with a specific partial vacuum from P-E diagram data because the energy equivalent on the P-E diagram representing the energy increase that should be inducable under the extra of the applied partial vacuum would be givenbyt-(the enthalpy energy equivalent down to normal lATS. pressure, which would represent the normal level) plus (the enthalpy energy from lATS. down to the actual pressure and SVP temperature of the partial vacuum some way beyond, below and to the left of the normal finishing state conditions above and further to the right\ divided by the normal

energy level ,Although perhaps such a value would only give the partial vacuum component of the x-factor as applicable in the now two Fluiditv

Equations, with the tstreamlinlng nozzle component having to become added but bearing in mind that the enthalpy energy down to the finish state of the fluid would be all the energy that could become transferred.Therefore, if the nozzle component was, say, 1.1 and the value derived in the above way 1.2, then I don't think that one could conclude that the combined x-factor would be 1.3, but rather that it would still be 1.2 as given by the actual energy ratios and, therefore, probably the attainment of the normal energy level would require the streamlining nozzle component to fully attain.But as far as application in the Fluidity Equations are concerned in the approach and treatment via reference firstly to cold state reference fluid and then, secondly, via comparing flow through a Bellmouth and Streamlining nozzle, then perhaps the relevant factor to apply would be the combined factor of 1.3 However, some further thinking is required here involving substitution with the energy value in the evolutions from the basic equations, which I and/or others will carry out at a later date and add as an Appendix. A further more practical route to the x-factor will be to divide the nozzle CSA required for flow through a Bellmouth by the nozzle CSA required for the streamlined flow for a given fluid volume flow in unit time.However, it would be helpful to be able to pre-determine the value from P-E diagram data in the way discussed to then be able to place in the treatment involving the Streamlined Fluidity Equation in order then to determine the required system conditions for practical application, as in the foregoing worked example. Here reiterating that whilst I may seem to be going to some lengths to try to achieve Bonus Energy, Ithink that this would be particularly important in this process via one means or another because otherwise the energy balance of the overall process may be just selfsustaining with no nett output and perhaps the main way will prove to be via the application of the partial vacuum technique but, of course, there would also be the further ways discussed.Perhaps in practice one would find that the impulse jet - Pelton Wheel system had a maximum energy balance involving recycling half of the energy of the turbogenerator to make up a shortfall in the compressor-sub-system cycle, leaving the other half for output supply, since in such a system it may be found that one could not in fact achieve the self-sustaining partial vacuum technique.

Then in ongoing development becoming closer to the desired goal of a fully self-sustaining compressor-sub-system cycle via progress to the rotating blade method when the partial vacuum technique should be more likely to be able to achieve. Which similarly may prove the case on branching off onto the use of a reaction turbine of the type depicted on Fig.1 of special design involving a long exit leg of special internal streamlining design amongst other aspects of the special design.Then progress to a nozzle fluid stand-in technique could potentially be found to improve such systems even further.

probably to a maximum xfactor of 1.5 which

in isolation may seem barely worth striving

to achieve, woula in fact represent a 50% increase in the energy yield at the sub-system stage to render its cycle with the compressor perhaps just in surplus, with all the energy produced at the turbogenerator stage

available for output supply.Then when such a stage is reached in the ongoing development of the process, perhaps the creatlon then of Super Heaven on Earth would be within sight and reach on this side of the Horizon of the FutureZ6utwhilst still at the Pelton Wheel stage then perhaps just ordinary or normal Heaven on Earth would be achievable. However, I personally take the view that until at least such a stage is reached in the advancing front of science and technology on Earth then many places on Earth are currently suffering Hell on Earth and/or Wilderness on Earth when otherwise they could probably cross the border and aspire towards and reach

ordinary Heaven on Earth.

Thus on the P-E diagram the quantity of around 50 KJ/KG representing the energy of the partial vacuum added to the much larger amount of energy down to normal ground state of around 200 KJ/KG may barely seem worth going to extreme lengths to achieve, because the level of 200 KJ/KG should be sufficient, but if it made the above difference to life on Earth then of course it would be more than worth striving to achieve, which will probably be the case.

However, returning to first principles once more in relation to the partial vacuum technique. For its sustained application I am assuming that if the cold liquid phase in the bottom of the isolation chamber was colder than the temperature that would produce and sustain an SVP environment of lATS, then it would produce a lower vapour pressure environment in the isolation chamber, which would be the SVP pressure of the fluid at the lower temperature, which would be continuously sustained at the lower vapour pressure via the internal cooling of the fluid and added external cooling probably via very cold exhaust air. Some of which could be becoming produced in the fluid recycling technqiue that could/would be simultaneously being carried out.Therefore, am I right? Could this potentially be the situation if such a system arrangement could be achieved? Obviously, one would first have to evacuate the isolation chamber of air by external means, but then if the fluid exiting from the nozzle was cold with a low associated saturated vapour pressure then surely this would be the pressure of the environment in the isolation, i.e. sealed chamber, above the liquid phase in the steady state of the process. Of course, the cold liquid phase would flow on to become re-heated in the next stage of the process, but such heating could

conduct back through the liquid flow

couldn't

Fa as t flowing liquid flow in the opposite direction.However, an aspect would be that the potential head height of the liquid phase would have to be such as to make up for the low vapour pressure above the liquid phase on this side of what could be regarded as a manometer arrangement for the purposes of this particular descriptionain order that the vapour pressure on the other side could be at lATS. which, however, as potential head height would only be the value of 33.4 feet for a full lATS. if water and 24.5 ft. for a full lATS. if R-21 of density 1.366 g/cc.Which may sound as though one is trying to get something for very little in comparison, but the

small increased volume tlow that the lower F2 volumelin the Bellmouth Fluidity Equaticn, would equate to the energy value represented b the above potential head. Whilst the higher energy amount really comes from the streamlining achieved via special nozzle internal shaping, particularly at entry, but will require the low pressure and temperature external environment on the exhaust side to achieve by the amount of and allowed by the external environment. But again another question mark at this pre-practical stage.However, with a view in mind that the final 1/6th of alignment from therandom state would be that associated with the below ground state alignment and if fully achieved would increase the energy yield by an x-factor of 1.73 then I think one can begin to appreciate the potential source of the higher energy yield potential. The volume flow increase equating to the increase pressure difference across the nozzle, but accompanyingly it should prove possible to streamline the fluid further to a lower ground state of lesser randomness and as that of the partial vacuum applied force.Or in a Bernoullis Theorem view of the fluid flow, if the static/side pressure of the fluid jet flow became that of the external partial vacuum pressure of the external environment as it could potentially do on good fluid streamlining, then the fluid flow must be more forward aligned to give the lower static pressure and the forward

dynamic pressure ot the tluid tlow must1 become correspondingly increased by an amount which must be due tothe extra forward alignment of the fluid in the x-vector, which in turn must give rise to a maximum potential xfactor of the value of 1.73. With a factor of 1.5, therefore, expected to be achievable for very low partial vacuum pressures.In other words, therefore, if the low static pressure in the fluid flow managed to become that of the applied partial vacuum, then the corresponding increase in the energy yielding forward dynamic pressure of the fluid flow must become increased according to the amount of the above factors and, indeed, accor- ding to the amount of energy that the partial vacuum represents on a P-E diagram.

I I think I will be correct in thinking that it will be via the further streamlining forward.aliRnment mechanism that the latter

would potentially be achievableh

one o'uld expect to be able to

add the extra P-E energy represented by the partial vacuum, i.e. be the mechanism by which the energy equivalent represented by the partial vacuum on a P-E diagram could only become added to the normal level down to ground state lATS, if at all.But if this does become an advancing front of science and technology of and for the future, then I would expect fluid streamlining to play an important role in the science and technology and, therefore, from this point of view the main way that this could be the case could be via the partial vacuum technique, and of course there

a

equal similarity with the application of the condensation vacuum technique to vapour-based turbine systems.

While ifthe static pressure remained as the normal level at lATS. then this would indicate that no further forward alignment had been achieved and one would then expect to acquire just the volume flow increase assocaited with the increased pressure drop. However, again a further area requiring of further thinking.

With the manometer description still in mind, it can be seen that an advantageous aspect of the process will be that alternatively one could allow the SVP in the isolation chamber to build up to a higher level than lATS. with the fluid jet energy and turbine yield being less and as represented via depresurisation to the higher pressure rather than all the way down to normal ground state, because the vapour pressure on the other side of the manometer leg could be to the higher pressure which in turn would require an equal amount of less compression energy. Since the lesser yield of energy could be easier to achieve, and since one woudl then have built-in extra flexibility in range of operation, then perhaps this would be the better way, e.g. as discussed via R-13 at a ground state pressure of 25ATS. but variable. But one may not then be able to achieve the same level of extra Bonus Energy. However, the reverse may be true and it could well prove easier to reduce from 2ATS.

to lATS., simply via the application of the SVP isolation chamber technique as coupled with further internal and external cooling in the higher pressure range, but then the potential head height of liquid phase that one would then require would be the equivalent of 25ATS., i.e. 640 ft. of R-13. Further pie in the sky perhaps? However, there would probably be applications in which the choice of fluid and/or method of operation was predetermined by other factors, e.g. when in combination with a turbogenerator as the exhaust vapour condensation and latent heat recycling system then I don't think one could

system in such a way as to gain such an energy advantage in the first place but one could still apply the partial vacuum technique to achieve

a higher level of heat conversion, with theji'luid1becoming reheated back to ground level via the natural environment en route back to the turbogenerating process, etc. All the time trying to ensure that there is a visible source of the energy.

An Introduction to The Mountain Technique to BE: With further regard to the pre-seeding method of operation, firstly clearly stating and thereby clarifying the difference between: A. The above method of operation in which the BE may become achievable via thereby being able to harness energy via the sub-system all the way down to lATS. and below and achieving BE advantage by virtue of the vapourising vapour being able to vapourise at a higher pressure than lATS. on the other side of the manometer like system arrangement, and: B.That in which the high vapour pressure, of 25ATS in this example, is also in the isolation chamber of the sub-system but may become possible to be swept aside just in the immediate vicinity of the turbine exit by some means to thereby again enable harnessing of the pressure energy all the way down to lATS. and perhaps below with BE advantage being gained by virtue of the vapour to the compressor on the other side of the manometer like arrangement of the heat collection unit again already being at the pressure of 25ATS. before entering the compressor.

Method A above is that which I am now beginning to refer to as the Mountain Technique for reasons which will become obvious if not already.

However, from the outset stating that there is yet an unknown in the technique embodied within the fact that the vapourising vapour would of course have to rise through the height of the liquid phase leg on the other side of the manometer like arrangement of the heat collection unit. Which so far I have been considering it may be able to do under its own 'steam' as the apt saying is. However, later on in ensuing deliberations on page 3 y I conclude that one would either have to place in some pumping energy, or alternatively and more likely lose some of the pre-pressure vapour pressure, of 25ATS. in this example, en route of the rising vapour to the higher level fo the system. Which however, I theorise may only be the flow work required, which in turn one could regard as equivalent to 10% of the pressure energy.Thus if allowed to thereby lose pressure on rising then by the time the vapour at 25ATS. reaches the top of the system arrangement it could have become reduced to 22.5ATS. However, I'm not fully certain about this aspect at this theoretical, pre-practical stage, and the loss from the BE potential could be higher, but at this stage I refer readers to my later deliberations on page367 where the above are my conclusions at this stage but readers will be able to draw their own conclusions.

I also refer readers to the P-E diagram for the system based on R-21 on Fig.2 where I have indicated the potential for this source of BE by which it can be clearly seen that in such a way one could substantially reduce upon the subsequent compression energy input requirement whilst still attaining the same pressure and heat of compression temperature.

However, the vapour would actually vapourise on the saturated vapour line and I think a little subsequent superheating of the rising vapour before it enters into the compression stage, i.e. to take the initial vapour state further to the right in equal and opposite contrast to sub-cooling, would also be very beneficial.

To digress the discussion a little on the same P-E diagram I have indicated the BE potential via Method B above where E to F would be the equivalent of harnessing down to 25ATS. and E to A the equivalent of harnessing down to lATS. if the vapour pressure could be swept aside to enable the latter, but remember here the BE potential would be subject to the fluid contraction effect to lower the apparent amount by say 50Z. However, returning to the method under discussion here.

Thus at this early stage I intend to continue assuming that this method could prhaps be a further route to quite substantial BE whilst remaining with reservations since it is not yet certain how much energy would become consumed in effecting the rise of the vapourising vapour to the higher level of the system arrangement.

In the later discussion I also raise the potential problem of freezing which would be applicable considerations if the method was being applied in depths of water but if the method is being achieved by means of a Mountain giving the higher level of the system then the heat source could be via the ARC process in the valley below rather than via water when there wouldn't need to be any water freezing problems to consider.

Moreover, via such a means one would have much more flexibility in temperature range of application in contrast to necessarily being tied to the natural temperature of natural flowing waters. Which in turn would enable the use of higher Bpt. refrigerants in the method.

Thus, I think the latter way is a modus operandi that I seem to be gradually homing in on in my deliberations and certainly a modus operandi which I now intend to shift these discussions here to and concentrate upon more specifically. For a number of reasons, but basically because one would also wish to be able to apply the partial vacuum technique on the other side of the process circuitory and at this prepractical stage I'm not sure how successful this could be achieved when basing on a very low Bpt refrigerants such as R-13 for example.While if basing on R-21 for example then one would be able to apply the partial vacuum technique in the normal manner being discussed herein in the other, separate, part of the process circuitory and one could in fact re-vapourise the fluid at say 800C to give a starting pressure of 25ATS., i.e. as indicated on Fig.2, because the initial heat of com tression fo the ARC cycle would be of the order of 3000C on com

pression t/lOATS. in the compression half of the ARC cycle.Thus if vapourising at 25ATS. then the heat would become removed to 800C instead of to 9 C if vapourising to lATS, which in turn may not make all that much difference to the functioning of the ARC and may in fact improve upon it in the overall energy balance of the process, but one would be gaining the BE advantage indicated on Fig.2 on the application of the Mountain Technique in the process circuitory in the process leg on the other side of the manometer like system arrangement on the other side of the heat collection unit. Which for a likely normal compression input requirement of 140KJ/KG would reduce the energy input requirement to 1OOKJ/KG which in turn could then be at the sub-system self-sustaining level just on the application of the Mountain Technique, to leave remaining all that being produced by the turbogenerator for other usage.However, in this process based upon the ARC as the heat source in the valley below then much of the power would have to become consumed in making up the shortfall in the ARC cycle, although there would also be the BE of the partial vacuum technique and the BE of the fluid recycling technique via the air compression technique, i.e. as becomes depicted on Fig.7, which when all added up together may give an overall energy balance for the process in which the shortfalls in the compressor - sub-system cycle and in the ARC cycle become made up via all the BE becoming created, to leave remaining all the power from the turbogenerator for output supply. And in the process yielding bags of cold exhaust air for Cold Store, Deep Freeze, RainMaking, and in the Mountain Technique, Snow and Rain to form streams to in turn form a River or a Lake in the lush green Valley below.Thus thereby the Process becomes ideal for application at Mount Sinai the objective. All running on thin air and remember in this process there would be a visible source for the energy, firstly the cold exhaust air of the ARC cycle as indicated on Fig.6, and secondly the cold exhaust air of the fluid recycling technique as indicated on Fig.7.

However, to improve even further on the overall energy balance and particularly in a spot such as the Sinai Desert would be the possibility of applying solar radiation either directly to the air expansion of the two air processes and/or via a solar pond technique. But of course at the expense of RainMaking capacity but perhaps to still leave Deep Freeze and Cold Store capacity. Thus perhaps the air ARC cycle in the valley could be rendered almost self-sustaining in such a way but leaving the exhaust air still suitable for DF and CS in and through the orchard growing ventures in and through the lush green valley.

While leaving the exhaust air from the fluid recycling technique at the higher level of the system arrangement, i.e. on top of the Mountain, still as cold as can possibly be achieved for the humid air precipitation purposes and in turn Rain, Snow, River and Lake creation.

In the above manner, therefore, it is my belief that the Holy Land described under Deuteronomy, Chapter 8, verse 15, is intended to become converted into the type of Holy Land described by God The Eternal under Deuteronomy,'Chapter 8, verses 7 - 11, and to the Holy Land flowing with Milk and Honey discussed by God The Eternal under Joshua, Chapter 5, verse 6.

An aspect of the addition of Solar Heating will be that the temperature of the air expansion in the ARC cycle would only have to be maintained at ground temperature during the expansion to render the ARC cycle fully self-sustaining, as calculated under PA.8728601, but of course still requiring to be of the required energy quantity and therefore perhaps this part would be best achieved via the Solar Pond approach.

However, an aspect ofthe overall process may be that one needn't in fact go to the lengths of such an extra addition to the process, as I hope is clear in the foregoing discussion. .On the other hand, the basic heat source for the process could be solely via Solar Pond in such a place instead of via the ARC cycle, when one could similarly achieve vapourisation temperatures of 80"C and thereby achieve the Mountain Technique to BE of the order indicated on Fig.2 herein, as can be gathered from the paper being referred to herein in relation to Solar Ponds,i.e. reference 32 at the rear. When one wouldn't then have the problem of making up a shortfall in an ARC cycle but when one would lose the extra potential capacity for Cold Store and Deep Freeze and indeed Air Conditioning.Therefore, perhaps one would apply the combination of these two techniques because such extra capacities obtained in such a way would be ideal to really turn the Hot Lands into idealic places flowing with Milk and Honey.

Of course, if such a project is based upon the ARC cycle then again it would be a question of optimising between all the various parameters involved, and in particular here the vapourising temperature and pressure between on the one hand Mountain Technique BE advantage and on the other, ARC cycle sustaining efficiency, in the overall energy balance of the process.

Deliberating further upon the system arrangement depicted on Fig. 6 showing the process combined with an ARC process as the heat source, in addition to the arrangement shown in which the latent heat from the exhaust fluid from the turbogenerating process becomes recycled as heat source for the next cycle and to thereby reduce the capacity of ARC process required to achieve a given level of total heat input each cycle, there would in fact be the alternative method of operation possible discussed under PA. 8728601 in which the latent heat becomes absorbed into the expanding air of the ARC cycle and in this way helping to render the ARC cycle fully self-sustaining whilst perhaps stillleaving the exhaust air at a sufficiently cool temperature for the 3 functions of CS, DF, and AC.Thus it again will be a question of determining which way is the better approach to the process for the particular application and functions desired. However, to be more certain of the success of such a project I think at this stage it would be better to think in terms of adding some Solar Pond heat in combination, albeit probably more as a make-up heat source rather than the main heat source in such a project.

But having said that some detailed calculations would have to be carried out on the various approaches to the project before making a final decision on the better system arrangement. Which I will refer to as the Mount Sinai Project wherever it be applied.

Of course, there is the yet unknown of whether or not the Mountain Technique route to BE would in practice yield any BE, which will probably solely depend upon whether the vapourising vapour at the pressure of 25ATS. will rise to the higher level of the system arrangement simply for the expense of 10% flow work, although to be really successful perhaps also depending upon whether some superheating of the vapour can be achieved en route up the Mountain side to the compressor at the higher level. Which at a place like Mount Sinai could perhaps be achieved via Solar heat, although with environmental impact in mind I envisage one could blast a cavern in the Mountain to house the bulk of the process with the vapour rising up piping through the Mountain to the higher level, as in the Welsh Hydro electrical storage scheme.

However, an aspect and an advantage of much of the overall work that I am conducting is that facets such as the Mountain Technique to BE, whilst fairly complicated to test for as part and parcel of the overall process involved and as yet undeveloped, could quite easily and readily become tested for as separate facets. Then having tested for all the various facets it simply being a question of placing them all together to produce the whole process if found successful as separate facets.

For the system based upon R-21 as depicted on Fig.2 then the height of liquid phase required acting down on the heat absorbing unit at the lower level of the system to enable the fluid to vapourise under a pressure of 25ATS. vapour pressure on the other side of the manometer like arrangement would be: lATS. ' 34 ft. H20 25 ft. R-21 at 1.366 g/cc.

Therefore: 25ATS = 25 x 25 = 625 ft.

Which is a system arrangement that could reduce the compressor input requirement by some 30% whilst the yield from the sub-system could still be all the way down to lATS. with the partial vacuum technique to BE still able to be fully applied without being affected by the route to BE on the other side of the process, although requiring of a further 25 ft. of liquid phase leg so to do to make up for the loss of lATS pressure in the isolation chamber fo the sub-system acting down on the side of the manometer arrangement. The Planet is beginning to sound like a laboratory and is probably intended so to be.

In the overall process there will be 3 sources of Below Ground State Energy, i.e. that of the partial vacuum technique, that of the condensation vacuum addition to the turbogenerator output, and that of the air in the fluid recycling technique, without which the process probably wound't be successful, with then perhaps the addition of the Mountain Technique taking things well over the top.

The application of the Mountain Technique couialm fact render the subsystem/compressor cycle self-sustaining which could only require the input requirement to become reduced from the level of 140 KJ/KG to 100 KJ/KG as in discussion in various places herein, and indeed render the compressor requirement more likely to be fully sustainable in the alternative method of operation in which the turbogenerator power is used to sustain the compressor stage. Thus again it will be a question of which way round gives the better overall energy balance. However, having said that I think in the fullness or time the addition of partial vacuum energy to the sub-system will ultimately give the better energy balance but the alternative method could be an easier starter to achieve in the first place.

Of course, in the application of the Mountain Technique the use of other refrigerants would be possible of different temperature properties. For example Ammonia of normal Bpt. -340C at lATS. and Rev of normal Bpt -300C at lATS., both of which would enable some BE via such a technique when basing on the natural heat in natural waters as the heat source, and would both probably be in a temperature range where the partial

vacuum technique would still be as successful as for/ higher Bpt re frigerants. However, at this juncture I propose to simply remain with the discussion as in the foregoing in relation to the use of R-21 in the application of the Mountain Technique whilst commenting thus in relation to the potential use of other refrigerants.In any case I think that the use of R-21 could be fairly ideal for obtaining all the various routes to BE in the one process if the heat source is via the ARC cycle, or via Solar Pond, or via a combination of both.

The more I think about the Mountain Technique and more specifically about the uncertain part thereof of the vapour rising to the higher level in the way described in the later discussion in my mind's eye the more I convince myself that the only energy that would become consumed would indeed be just that of flow work as the vapour travels through the pipe, which of course could be auite a large diameter to reduce upon flow work losses. Because

remember tne vapour would flood into the compressor on the intake stroke and one can envisage all the vapour just 'utching' up the pipe by a corresponding amount on each intake stroke as further vapour at the pressure of 25AT5. enters at the pipe at the lower level, simply under the Van der Waal forces of repulsion acting between all the molecules of the vapour.In contrast to the liquid phase where such forces are not present in such a manner. With then just losses due to normal levels of flow work to consider the same as associated with flow through a horizontal pipe. However, I could be wrong so far since the column of vapour would obviously weigh something which would be acting down on the vapourising vapour but in the density of R-21 at 25ATS. and 800C only being of the order of O.25g/cc compared with liquid R-21 at 1.366 g/cc then to the 625 feet of vapour column would only be some 18% of the weight of liquid R-21 in the same column. Therefore, this may only reduce the potential BE by a similar amount which when added to flow work losses could become a 25% to 30% reduction in the potential BE.

While if the vapour column weight was the full weight of the liquid phase column then one probably wouldn't expect to be able to obtain any BE via such a means but in it being very much lighter and just 18% of the corresponding liquid weight then perhaps so. However, I still remain with my reservations because the flow of mass in unit time would of course still have to be the same for continuity of the cycle, which hwoever may be that which the system of the vapourising vapour at the lower level and the simultaneously intake of vapour at the higher level by an equal amount into a space which would otherwise be fully depleted amount, is able to achieve.

However, on thinking further the latter part of the foregoing deliberations probably won't be a correct way to consider the system because the pressure of 25ATS. acting down would itself and alone fully repre-

sent the weight or the fluid acting down on the fluid vapourisingy, and the fluid in vapourising at 800C and a vapour pressure of 25ATS., or more correct to say in the context of this system in vapourising at 800C will do so at a saturated vapour pressure of 25ATS., and it will be the very act of the vapour becoming generated at 25ATS. under the elevated temperature of 80"C which would be that which would overcome the pressure of 25ATS. acting down on the vapourising vapour.However, the vapour would then have to rise up the large diameter pipe to the higher level of the system but the mechanics of vapour removal at the top and fresh generation of vapour overcoming the pressure of 25ATS, acting down would be that which would push the vapour upward by the very definition of overcoming by pressure, with then only flow work to further overcome, i.e. the friction of the flow work against the pipe walls presenting a little resistance to the vapour becoming pushed upward by the fresh vapour becoming generated, which would only be equivalent to a small fraction of the energy represented by the pressure of 25ATS., e.g. 10%.

Or to place in even simpler envisionable terms, the vapour becoming generated at 25ATS, will overcome the pressure of 25ATS. acting down and simply lift the whole of the vapour, which can be envisaged to be simply as a block of vapour inside the large diameter pipe, upward en bloc at the rate space becomes made available to do this as the vapour becomes removed at the top, just the same as it would a much smaller volume weight but still equivalent to 25ATS. or 352 Ibs/square inch acting down on the vapourising vapour, but in the case of the block of vapour with the resistance of flow work presented via the friction against. the piping walls to further overcome, which would be better to

berimDlv as loss of 10% pressure at the other end, i.e. at the top

as the vapour becomes pushed upward. Then one/becoming further enhanced by the fact that the vapour would be becoming drawn off into an otherwise depleted space at the top of the block of vapour at the same rate it's vapourising, or more correct to say,vapourising at the rate it's being allowed to by the rate it's being drawn into the compressor intake at the top which otherwise would be depleted of vapour and, therefore, in a sense would draw the vapour in as though a vacuum pulling on the vapour and drawing it upward.

Thus, it now becomes possible to envisage the system here very simply as a very, very tall vapour generator of the type used in normal turbogenerators but very much taller, eg, 600 ft. instead of 60 ft. - which may be the height of existing vapour generators in Nuclear Power generation for example. For further example, as that discussed under my PA 8728601,(Fig. 13 appertaining) However, the system in the case here being one in which the vapour take-off is at the top of a very much taller vapour section and into a compressor intake.

Which in the example here will be at a rate which will maintain the pressure of 25 ATS. inside the vapour column section which in turn will maintain the vapourisation of the liquid phase refrigerant at a temperature of 800C and at a pressure of 25 ATS. since this will be the steady-state of the equilibrium set up for this system (in the absence of accurate data). In other words, if the vapour pressure above the vapourising liquid phase is 25 ATS. then the latter will vapourise at a pressure of 25 ATS. and at the associated temperature of 800C, and at a rate at which the vapour is becoming removed at the top.And I don't think it will make any difference to this normal mechanics what height the vapour section above the vapourising vapour apart from flow work subsequently detracting from the pressure of 25 ATS. as the vapour becomes pushed upwards under the action of removal of the vapour at the top and fresh generation of vapour at the bottom of the system, which should simply have the effect of causing the vapour pressure to become reduced by some 10% at the top of the column of flowing vapour.

However, I again stand to be corrected by my Noble Fellows. It also follows, that a way to achieve the desired level of superheating could be as discussed under PA 8728601 when and if basing the system here on ARC Heating.

In which case, therefore, I would seem to be back at my original thinking on the feasibility of this particular route to BE. However perhaps still something of a question-mark on this technique at this stage but if found to be a sound technique in some initial practical experimentation then I certainly think that it is a technqiue that should become part and parcel of the process if possible to be applied at the desired site of usage.However, obviously there would be many applications where this particular technique would not be possible to apply because one wouldn't be able to establish the two levels of the system arrangement, e.g. in a ship application and probably at many industrial sites, in contrast to applying the process to enhance the ecology of regions of the Planet when it should invariably be possible to apply mountains, cliffs, ravines and gorges, etc. in combination with the process in such a way in order to thereby achieve BE via such a means. If I'm right that is. And perhaps even more purpose built towers and/or dual purpose built towers as under Genesis, Chapter 11, vs.4 and 5, if only 500 ft. or so of height is required.

Indeed, if one considers further the method of operation in which a maximised quantity of heat becomes removed from the compressed vapour and used for the generation of power via a normal turbogenerator which in turn becomes used to fully sustain the vapour compression then by reducing the compression energy requirement via the Mountain Technique one could well render this part of the process possible to achieve simply via such a means. To leave remaining the cooled liquid fluid under pressure with the energy of which being able to be harnessed as in normal hydropower harnessing.Which would then be fully available for output supply if firstly the operation of the compressor was rendered fully sustained in the above manner and secondly the heat source was via for example the heat contained in natural flowing waters or a heat source such as a Solar Pond, i.e. where no produced energy has to become consumed to make up any energy shortfalls in process equipment. Obviously an ideal site for such a method of operation would be deep, fast flowing, rivers flowing through a gorge with high cliff faces on either side or a site such as Victoria or Niagara Falls where one could apply the height of the water fall as the two levels of the process system.

Which as an immediate starter would be the simplest, easiest and perhaps most certain way to apply the process but of course requiring of the Mountain Technique to be verified in practice. And if based on natural heat of water then of course requiring of a suitable refrigerant with appropriate temperature properties different than those of R-21, e.g.R-12 or Ammonia, via which, however, one wouldn't be able to achieve the same advantage if natural heat is the heat source and probably one would have to go to the use of a very low Bpt refrigerant such as R-13 or perhaps R-13B1 of somewhat higher N.Bpt. at -580C,

Of course, in such a fairly straightforward operation oFthe process one wouldn't achieve the same levels of power output and functionality as potentially possible to be achieved in the fullness of time in the further methods being discussed herein but it would be a fairly straightforward bridge,not too far removed from some existing systems, to the more complex methods of operation and even in this simple method one could produce very cold exhaust air for the various functions of Rain, Snow, River, DF and CS, simply by using a proportion of the power yield to compress air then removal of the heat of compression via the heat absorbing equipment with the added advantage of thereby reducing a little the amount of fresh heat to be absorbed each cycle, then simply expansion of the constant pressure cooled air in a turbine to gain back a high proportion of the power used to compressed the air in the first place whilst at the same time additionally yielding some cold exhaust air for the various additional functions. However, the feasibility of the Mountain Technique to BE is far from certain at this stage and all the other various techniques and ways to apply the process could vastly accelerate the improvement, development and widespread implementation of the process and therefore now continuing on with discussion on other various aspects, as follows.

Method B discussed at the start of this section on the Mountain Technique could possibly become applied in situations where a system height would not be possible, e.g. in the Engine room of the Ship, which would also have the advantage in such an application of it being possible to build into such a technique variation in temperature range of use to accommodate for changing sea temperatures. Perhaps to thereby achieve a similar level of BE as via the Mountain Technique since obviously there would be limiting factors to the application of the latter, e.g.

when the flow work becomes more than the further advantage being gained, etc. However, in a ship's application one should still'be able to achieve the system height required for the application of the partial vacuum technique, which would be just 30 ft. or so, i.e. the height of liquid phase equivalent to the lATS, or so of depleted pressure inside the isolation chamber of the sub-system, which in any case could alternatively be achieved via consuming a little of the energy. Therefore, at this stage continuing on with the discussion more specifically in relation to the application of the Partial Vacuum Technique, as follows.

Continued Discussion on the Partial Vacuum Technique to BE: Firstly somewhat belatedly giving some data at hand in relation to the application of the partial vacuum technique as extractable from the tables 'Thermodynamic and Transport Properties of Fluids' by Rogers and Mayhew, and more specifically in relation to the application of R-12 as on page 13 thereof since similar data on R-21 is not yet at hand and in any case one could well apply R-12 of N.Bpt -30 C as a fluid which could extract natural heat from natural flowing waters and in so doing give some potential for the Mountain Technique route to BE as well as perhaps still being in a suitable temperature range for achieving the full application of the Partial Vacuum Technique to BE.

The refrigerant Ammonia of N.Bpt -340C would also be in the same potential category. Perhaps the Colorado River, Grand Canyon, Flagstaff, Arizona, The Republic of the United States of America, would be a further suitable place to eventually apply the process in the fullness of time with this type of approach to the process in mind,where Solar Pond and Direct Solar heating would also be possible.

The extracted data being as follows: From Normal lATS. to Below Ground State Pressure & Temp.

TOC :- -300C -400C -500C -600C -100 c Associated SVP :- lATS 0.64ATS 0.39ATS 0.23ATS O.O1ATS Thus from this data it can be seen that in the case of R-12, effecting further fluid cooling by just 300C beyond the normal level of fluid cooling that would take place on transferring and harnessing energy down to a fluid pressure of just lATS. would give a partial vacuum pressure of 0.23ATS, which basing on the P-E data for R-12 could give an x-factor of around 1.3 in the manner discussed to give a 30% increase in the energy yield at the sub-system stage and then continuous self-sustaining of the partial vacuum pressure in the manner discussed, albeit perhaps requiring of a little assistance in one or both of the ways discussed and obviously could become improved upon substantially at no extra cost in energy consumption if the method is via the application of very cold exhaust air becoming produced in the process.

Whilst I don't have similar P-E data for R-21 I think the amount of cooling to achieve a certain saturated vapour pressure inside the isolation chamber would be similar but with the difference and advantage being that the fluid on transferring energy down to lATS. would become at an associated pressure of 90C (hopefully) with the further cooling by just 300C then taking the fluid temperature to just -200C, which obviously is a temperature that could be achieved quite readily via the application of very cold exhaust air. However, if the fluid jet is yielding more energy then it must be transferring more kinetic energy so to do and, therefore, it must be becoming colder and, therefore, it must create its own low SVP in the isolation chamber.However, the fundamental question being will it work in the first place, i.e. even if there is a very low pressure in the isolation chamber, which in the case of the use of R-21 at least could well be rendered almost zero with the aid of cold exhaust air, will this necessarily draw the fluid jet so that it yields more energy by an amount equivalent to the vacuum, i.e. as can be determined off a P-E diagram by looking at the enthalpy content at lATS. on the saturated liquid line and then at the enthalpy content at the SVP in the isolation chamber, e.g. O.1ATS, then by subtracting the latter value from the former.

Thus in the case of R-12 this can be seen to be about a further 40KJ/ KG on 140 KJ/KG for an SVP of O.1ATS., i.e. an increase of 25 to 30%, if again commencing with fluid just to the left of the Critical Temperature. To give an x-factor of 1.25 to 1.3 for the system. However, the question still remains will this be feasible? Well I think the only way that it will is by causing the fluid to become more forward aligned, which obviously will require hot fluid able to be so in the first place, then a good, long, streamlining nozzle, then a high pressure to ensure that the hot fluid becomes streamlined to its fullest potential on tt's flow through the long streamlining nozzle.At this stage probably the better context to place this part of the system in is the Bernoulli's Equation, which in a very simple view will be as follows. If the fluid jet becomes streamlined in the above manner to such an extent that the static or side pressure becomes'that of the partial vacuum pressure in the isolation chamber then the forward dynamic pressure of the fluid jet must have become increased by a corresponding amount, which in turn must transfer a higher energy amount to the turbine by a corresponding amount, which in turn must lower the temperature of the exhaust fluid further to create its own low SVP in the isolation chamber, etc., ad infinitum.Then if in conjunction with this view one considers that the final 1/6th of further streamlining adds 73% to the forward dynamic pressure energy, at least according to my exercise in my earlier writing on the process, then the foregoing would seem more possible. Thus, now feasibility really boils down to whether or not one could expect that the static Xorside pressure of the fluid jet could become that of the low pressure on the exhaust side of the turbine in the isolation chamber in such a system under such conditions.Given hot fluid in or above the Critical Region where the Van der Waal bonding between molecules will be virtually non-existent, and a good, high pressure and a good, long, streamlining nozzle, then I personally think that one could achieve the above, and especially in view of existing pre-expansion nozzle systems in vapour systems where similar levels of pre forward alignment in fluid jet flow must be achieved, e.g. as in a Curtis Turbine. However, in the latter system a condensation vacuum is becoming applied which could perhaps be deemed to have stronger drawing power than simply a partial or full vacuum, but on the other hand it has to deal with an expanding vapour during the formation of the prefluid jet and one could deem that a fluid to the left in the liquid phase could be drawn easier. However, as with the Mountain Technique there is left remaining the element of doubt at this pre-practical stage and I leave readers to ponder such aspects further, but obviously it would be a better process if both work well and both are becoming applied simultaneously in the same process. Indeed the process may not be very successful at all if neither of these potential routes to BE are found not to give BE in practice. Although there is still the Higher Ground Pressure Method involving obtaining BE via sweeping vapour pressure aside inside the isolation chamber just in the immediate vicinity of the turbine impellor sites, which could become as main a way to BE as any of the other methods put together, as the apt saying is, I can but press on with my evolving discussion on the process.

As for the energy advantage technique perhaps potentially achievable via the dubious means of reducing the r to the four element in the fluid flow in the fluid recycling technique by increasing further upon the nozzle GSA beyond that required for the cold state reference fluid, I think enough has been said and at this point in the discussion since I seem to have passed a peak at the moment where I am now going around the circuit of the discussion in ever-diminishing circles to no more advantage, I propose to link onto some of my earlier previously written material, comemcning with some earlier deliberations with respect to some of the foregoing deliberations, hoping that readers won't mind or notice the join too much but in any case the discussion quickly progresses onto other early stage deliberations on various other related aspects of the process, some of which may not yet be wholly correct at this stage but at least they will be useful in again further highlighting primary parts of the various facets of the process, the correctness or otherwise of some of the deliberations again perhaps not being fully known by anyone on Earth at the present time. But no doubt over the next Millenium of deliberations on this advancing front of science and technology by those that follow things will become clearer during the practical phase. I merely aim to get the ball rolling somewhere close to the jack.

General Discussion, cont'd.

Thus maximised streamlining should prove to be one of the ways to overcome the possibility of some fractional vapourisation taking place in the impulse jet - impulse turbine method of operation, either on exit of the hot fluid jet from the nozzle into the surrounding lower pressure atmosphere and/or at the point of impact of the fluid jet with the impellors of the turbine. Since if one streamlined the fluid jet as much as possible then the static pressure and temperature of the fluid jet could become as low as the conditions of the surrounding atmosphere in accordance with Bernoulli's Theorem governing fluid jet flow, and if the static conditions of the fluid jet were the same as those of the surrounding atmosphere to which it is exposed around its surface, then the prevailing static thermodynamic equilibrium would not be required to adjust to the surrounds.Pressure in practice s, of course, bombardment of molecules over a unit of area with a force as represented by the level of pressure, e.g. lATS of pressure being equivalent to 14.5 lbs.of exertion of fluid per square inch as under the force of gravity. Therefore, with respect to the static pressure of the fluid jet flow and, m;vre speciftca'ly, the pressure exertion in the side vc!ctcrs into the surrou;;lting atmosphere it would perhaps be more correct to say that this would be comprised of side vector components of molecules primarily travelling in the forward vector, notwithstanding the preceding view that perhaps the molecules in the outer annular sheath of the fluid flow would in fact be still in a random state bombarding in all random directions

then1 to a lesser extent towards the centre or the tluid tlow until at the centre they are fully aligned into the forward vector. Obviously the less streamlined the flow then probably the more the latter will be true and the more streamlined the flow becomes then the more the former will become the fluid flow state.Therefore if the fluid starts in the liquid phase and contains a high quantity of heat then it could obviously be important to streamline the fluid jet as much as possible in order to minimise/avoid flash vapourisation off its surface on exit from the confines of the nozzle into the surrounding low pressure atmosphere. But perhaps the liquid phase couldn't become sufficiently streamlined to fully avoid such flash vapourisation, although unlike cold water jets the fluid would be closer to its Bpt. than Fpt. to perhaps render the fluid sufficiently streamlinable and such that the outer surface pressure andtemperature conditions of the fluid jet became sufficiently low to avoid flash vapourisation on exit from the nozzle.Obviously, super smooth internal nozzle walls would be very helpful in achieving the desired level of streamlining in the fluid and on the edges of the fluid flow, coupled with the internal shaping of the nozzle and whilst it probably would not be possible to apply an external electro technique to create a fluid stand-in effect in the beginning this could perhaps be achieved in part by using a material for the nozzle that has no affinity for the fluid flowing through the nozzle with as high a builtin repulsion value as possible.

Whilst in contrast to the static pressures the forward dynamic pressure of the fluid jet flow will become higher than the random pressure and therefore still be at a pressure higher than that required to maintain the fluid in the liquid phase. Therefore, with respect to these aspects it would probably only be the outer annular sheaths of the fluid jet that could be vulnerable to flash vapourisation on exit from the nozzle in the case of a fluid in the liquid phase containing a high quantity of heat, but of course this would detract substantially from the power of impact of the fluid jet and once the fluid jet started to go, then perhaps it would be rendered useless.Therefore, one would wish to optimise the conditions so that no vapourisation at all took place, with a further damaging effect being that it would destroy a partial vacuum environment if trying to be applied.

When the fluid jet impacts into the impellors of the turbine then the rate of transference of fluid pressure coupled with the rate of cooling and contraction of the fluid will be required to be such that the fluid remains in the liquid phase. Here will be another equal and opposite similarity with the harnessing of a vapour jet which would depressurise down the constant entropy line at maximum efficiency of the transference of the kinetic energy of the vapour jet, but if not efficiently transferred then the vapour jet would depressurise with heat energy left remaining in the vapour that could otherwise have become transferred under more efficient transference. Whereas in the case of a fluid jet on the liquid side of the P-E diagram of state the equivalent line to the constant entropy line will be the normal cooling curve for the liquid and it will be a question of whether all the surplus kinetic energy on cooling will all become transferred to the turbine efficiently, or whether some will be left remaining in the fluid, resulting in flash vapourisation taking place as in a normal throttling device. Thus, there would be these two competing mechanisms, but since the fluid jet will impact with the impellors of the turbine then it is likely that the energy would become transferred before becoming extracted into a latent heat energy mode, with all the fluid depressurising along the liquid phase cooling curve for the fluid and none becoming flashed off in the fluid cooling process.However it must be remembered that even if the fluid jet starts off above the Critical Point region in the liquidvapour state on transferring energy it will progressively become in the true liquid phase on depressurising down its cooling curve. Thus, on the one hand, one would probably wish to commence off with the fluid as far towards the vapour phase as possible in order to achieve improved streamlining, whilst on the other hand one would probably wish to pre sub-cool to as far as possible in order to avoid the cooling curve for the system being very close to or actually on the saturated liquid line for the fluid when obviously some vapour fraction would become produced unless the transference of the kinetic energy of the fluid jet was super efficient.Whilst if the fluid commences off sub-cooled to a lower temperature and such that the cooling curve for the fluid is rendered some way to the left of the saturated liquid line, then the liquid fluid could absorb some inefficiency in the transference of the kinetic energy before a vapour fraction became produced, which in turn would also have the benefit of not destroying a partial vacuum environment. However, the related aspect being that perhaps in order to apply the partial vacuum technique successfully in the first place then one would have to achieve as much streamlining as possible at the fluid jet creation stage, which in turn could require the fluid to be in a state above the Critical Point region and as far to the vapour phase as possible.A view which in fact is opposite to some of my earlier thinking in which I consider that to apply the partial vacuum technique then perhaps it would be better to start with the fluid in a state some way down the P-E diagram fully in the liquid phase because then the fluid wouldn't have as far to depressurise before entering the below ground state region and gaining the extra energy thereof in the energy balance with the compressor input requirement.However, since the energy equivalent of the partial vacuum is only likely to become transferred via inducing extra forward alignment involving the static pressure of the fluid jet on its creation becoming that of the partial vacuum with a corresponding increase taking place in the forward dynamic pressure of the fluid jet, then probably the fluid would have to be in a commencing state as close to the vapour state as possible, with then very much further to depressurise and cool but probably the fluid state would enter into the below ground state region with more success.But providing the kinetic energy of impact becomes transferred efficiently and rapidly, otherwise a vapour fraction would become produced at this stage to both detract from the energy that could otherwise become transferred and also destroy the partial vacuum environment that otherwise would be creatable. Thus a hell of an optimum line to walk here, but if walked successfully then one should achieve the highest rewards for one's endeavours. Obviously the design of the impellors will probably be all-important and radial speed in relation to fluid jet speed, etc. for the efficient impartation of the kinetic energy of the fluid jet to the turbine.On the other hand, one may find that a full frontal, blunter impact gives good results as in combination with the contraction of the fluid that will take place on cooling, giving rise to a softening of the fluid jet impact' as the impact takes place, i.e. with the initial forward velocity of the fluid jet initially being appreciably higher than the radial speed of the turbine.

All of which, however, is a further area of the work requiring of further and deeper study and thought and at this stage returning to the discussion on the cooling curves, which will probably be the curves the fluid could follow if achieving maximised energy transference efficiency whilst, and in so doing, remaining fully in the liquid phase on depresurisation without the formation of a vapour fraction being necessary in achieving the latter.

For this further discussion, firstly referring to the cooling curves given under liquifaction of gases on page 732 of the McGraw-Hill Encyclopaedia of Science and Technology where one will find a Temperature-Entropy diagram on Fig.2 showing some cooling curves for a gas starting at different temperatures and pressures. However, this diagram may not be all that useful to this discussion if at all, since it is the P-E diagram that is really required, which I don't think can be deduced from the T-S diagram.For example, from the T-S diagram one could gain the impression that the cooling line always progressively goes further to the left of the saturated liquid line on cooling, whilst for the same curves on a P-E diagram of the system then I think that for a reversible cooling process at least the line of the cooling must follow the saturated liquid line if commencing on the latter state line, e.g. at point C on the T-S diagram, and I think that wherever the fluid state may commence on a P-E diagram the fluid state would probably always finish on the saturated liquid line on a P-E diagram because this would be the state that represented the final equilibrium at the end of the transference of the kinetic energy between the liquid phase and the saturated vapour pressure of the fluid vapour acting on the liquid phase.

Unless the fluid became additionally cooled by some external means towards the end of the energy transference, e.g. via cold exhaust air.

May I also comment in passing that P-E diagrams, P-V diagrams and Triple Point diagrams are the main diagrams on the fluid state that I personally like at the depth I wish to study the fluid state, perhaps because they are closer to the truth of the matter as it were.

Thus, for the purposes of this further discussion I intend to assume the foregoing for cooling curves on a P-E diagram, although with the further thinking that perhaps if a very streamlined fluid jet became created from fluid on the saturated liquid line towards or at the Critical Point, then perhaps in the beginning stages of the transference of the kinetic energy of the fluid jet two the impellors of a turbine via a good initial impact the cooling curve of the fluid may 'shoot' a little further to the left of the saturated line in a more horizontal downward curve than that of the saturated liquid line, then curve down more steeply towards the final point, still the left, on the saturated liquid line. Rather like a slim handle on the side of some silver cupsr upside down.Thus, these are the P-E diagram views of the system that I will have in my mind during ensuing discussion but they may not be wholly correct. Therefore, at the start of this discussion stating that there is an important aspect of the process that I wish to bring into the discussion which I don't wish to become confused with any incorrectness that I may discuss in relation to the fluid state P-E diagrams and I ask readers to bear this in mind.

Should the cooling line initially 'shoot' a little to the left of the saturated liquid line for a fluid commencing in the latter state, then this would be advantageous from the point of view of avoiding fractional vapourisation taking place during the transference of the fluid jet energy, but towards the end of the energy transference and the accompanying fluid depressurisation, cooling, contraction and re-randomisation then this would become an increasing danger as the fluid state and the conditions it was under approaches the saturated liquid line. When the application of cold exhaust air may become beneficial to the overall system. However, I think it probably more likely that the fluid state would follow the saturated liquid line on transference of the energy when commencing on the saturated liquid line rather than initially going further to the left, but of course the closer towards the Critical Point then the more horizontal the initial downward curve would be in following the saturated liquid line, still indicating that there would be a concentration of energy transference in the initial stages if simply following the saturated liquid line without going further to the left.

But probably it would be more correct to say that this would be the line the fluid state could potentially follow for maximised efficient transference of the fluid jet energy. Thus in this respect, thereby, being in similarity with vapour expansion systems following the constant entropy fluid state for maximum kinetic energy, i.e. heat, transference, and in fact in equal but opposite similarity, because in this case it is not the constant entropy line that the fluid state follows on cooling but the saturated liquid line. Therefore, since it is unlikely that one would ever achieve such energy transference then some heat energy would probably become in excess in the fluid state for the conditions of the fluid state to result in some fractional vapourisation taking place during and at the end of the energy transference stage.There

fore, should one wish to avoid such vapourisation raKlng { as one probably would if one wished to apply the partial vacuum technique, then one would pre sub-cool the fluid to some way to the left of the saturated liquid line, adding the sub-cool heat to that becoming converted in the turbogenerating process. However, the fluid state would then probably head for a final fluid state on the saturated liquid line from the sub-cooled starting point on transference of the fluid jet energy and therefore the same susceptibility to some fractional vapourisation taking place towards the end of the energy transference would still exist.Moreover, since the fluid state may not then be in as streamlinable an initial state, then the transference of the energy could be less efficient to perhaps inevitably more likely leave remaining a surplus of kinetic (heat) energy in the fluid for the depressurisation rate and final pressure of the fluid to then and thereby result in some fractional vaDourisation taking Dlace.Thus. notwith

standing some1 earlier discussion perhaps sub-cooling would not be the full answer to avoid fractional vapourisation taking place, although probably still at the fluid jet creation stage and its emergence from the nozzle exit

bouse tn r the the/less streamlinability

of,sub-cooled fluid due to the stronger internal Van der Waal bonding that would then and thereby exist within the fluid deeper in the liquid phase could lower the energy transference efficiency of the fluid jet to the impellors of the turbine which, in turn, could give rise to the heat content of the fluid becoming in excess for the depressurisation of the fluid state.However, the further to the left the sub-cooling then the more excess heat that could become accommodated in the liquid phase of the fluid between the maximum potential cooling line for the system and the saturated liquid line before then crossing over the border to the right into the fractional vapourisation danger regionshanone

to maintain the partial vacuum potential of the system.

It follows, therefore, that one would probably strive to achieve an optimum starting fluid state between the opposing forces of streamlinability and sub-cooling and obviously such a fluid state could be arrived at by operating with the pressure of the system above the Critical Pressure for the fluid and then constant pressure cooling some way to the left of the Critical Temperature of the fluid, i.e.

as discussed in relation to the use of R-21 and as depicted on Fig.2 herein. Thus, I still remain with my earlier discussion with respect to this aspect of the system, and for R-21 one may sub-cool to say 1500C to 1700C, depending upon the efficiency of the energy transference but obviously operating at a temperature of:: ONE HUNDRED AND EIGHTY

for this fluidlmay be out of the question, although it the pressure is appreciably higher than the Critical Point pressure then there would be quite a gap between the saturated liquid line and even a straight line to the final fluid state on the saturated liquid line to enable the fluid to contain an appreciable excess of untransferred kinetic energy for much of depressurisation, but of course towards the end one would probably have to try to remove the excess heat if one wished to avoid fractional vapourisation. Although if the line curves to the left like the saturated liquid line,as would probably be the case, then it could potentially only be very close towards the end that one would have to remove any untransferred heat energy but depending upon the energy transference efficiency of the system.

It follows, therefore, that the energy transference efficiency would be an important aspect of the system for more reasons than one and this could be one of the main areas of the process left remaining that could potentially present some further difficulty. If

If the energy transference efficiency is poor resulting from the turbine design being poor then, depending upon the level of sub-cooling,heat energy could soon become in excess for the depressurising pressure of the fluid state with the fluid state then crossing over the border to the right, producing unwanted fractional vapourisation at the cost of wanted energy and one's sub-system turbine equipment disappearing in clouds of vapour.

Of course, in order to achieve the partial vacuum technique then it will be important not to cross over the border to the right even at the end of the energy transference process, although obviously if the fluid state crossed over the border right at the end then the less fluid vapour that would have to become continuously removed by an external means in order to maintain the desired steady state partial vacuum vapour pressure in the isolation chamber of this technique, and viceversa.

A further way to deal with the above potentially problematic aspect of the system will be to apply very cold exhaust air that could potentially be becoming produced in the process, which could not only be applied to avoid the vapourisation in the latter stages, but also to cool the exhaust liquid phase on exhaust from the turbine down to a much lower temperature than would be achieved by itself. To in turn

produce an associated saturated vapour pressure in the isolation chamber of the system to a much lower partial vacuum pressure than could otherwise be achieved, to in turn be more effective in increasing upon the extra of the x-factor energy yield.Obviously, therefore, this could be a very good approach to the system which wouldn't have the cost of external energy addition if the very cold exhaust air production was part and parcel of the overall process which it would be if a by-product of the fluid recycling technique being simultaneously applied. The application of cold exhaust air to the end of the energy transference

stage to the turbine to carry away any damaging surplus heatlaimed 'aU preventing the fluid state crossing the border to the right to result in unwanted fractional vapourisation taking place is perhaps the de-resistance in the equal and opposite similarities with the vapour

expansion-turbine systems since inlsuch systems heat sometimes becomes added towards the end of the expansion energy transference stage in order to avoid the opposite of fluid fractional condensation taking place at such a vital stage in the process and in such a case involving the fluid crossing the state border to the left of the saturated vapour line into the other extreme of the intermediary fluid state region of the liquid-vapour mixtures.

It follows, therefore, that it would now moreso seem that the better and even intended approach to the system would be to apply the partial vacuum technique in an isolated chamber and in combination with this simultaneously apply the fluid recycling technique and in combination with the latter technique the compression of bags of air technique to effect the recycling of the fluid if for no other reason than to produce very cold exhaust air for the more successful functioning of the partial vacuum technique, which in such a way could approach a more complete vacuum effect because a very cool fluid temperature could then and thereby be reached at which the fluid had an extremely low associated saturated vapour pressure than could otherwise be achieved.

Although the foregoing table of SVP values look quite promising with respect to the latter aspect but obviously removal of a further lO0C to 200C could give an appreciable improvement.

Thus perhaps thiswould always be the way that one would design and operate the sub-system via one large combined unit now involving the required quantity of bags of air compression equipment to thereby always have available on hand very cool air as a part of this isolated part of the process and totally separate from the rest of the process, although with the potential to become combined in some way if desired, in order to thereby always be able to achieve firstly the better operation of the sub-system and secondly the better Operation of an interconnected partial vacuum system, perhaps at times achieving a complete vacuum effect. Even at times when the heat absorption in the next stage of the process at the start of the next cycle is from a source other than via an interconnected main heat source ARC cycle, e.g. natural flowing waters.Moreover, on Earth at least there would always be air available in abundant replenishability on site and the remaining capacity of the very cold exhaust air could invariably always find application as a by-product for refrigeration, cold-store, air conditioning and, of course, for the Big R purpose. Or, if the remainder of the cold exhaust air is not required then it could always become exhausted back into the general atmosphere after carrying out its function of cooling the liquid phase of the fluid on exit from the sub-system into the isolation chamber for the better operation of the partial vacuum technique.

A function which alone could justify this method of recycling the surplus fluid over and above that in unity with the compressor of the main outer circuit comrpessing the new vapour of the refrigerant resulting from subsequent fresh heat absorption in the next stage of the cycle of the process. But in addition to the above further functions for the cold exhaust air there would also be the probability that application of the air compression technique for the recycling of the surplus fluid would add to the overall energy balance of the process by the amount of enthalpy energy that becomes extracted from the air and added to the process in the process.

Indeed, like all ideas thismethod for the recycling of the fluid is now beginning to grow moreso and it now seems to me that this would be an alternative,but probably simultaneously applied,way to increase upon the energy yield of the sub-system to that of applying the partial vacuum technique to induce extra fluid streamlining and an increased fluid jet velocity for the flow of a given mass of fluid. Probably to yield an equal or higher amount of extra energy at the sub-system stage. You see, the amount of energy required to repressurise the fluid required to

be recycled would only be equivalent to the mgh value of the coldfluid, but with the heating of the fluid to the required temperature for recycling probably consuming all the heat of compression yield of the air compression.Therefore, should this prove the case then there would be a higher proportion of the compressed air energy left remaining from the application of the technique that would be available to go on to help with the compression of the vapour in the sub-system - vapour compression cycle. If one estimates that the total initial compressed air energy would be say 50% of the initial surplus turbine energy and that 20% of this is required to repressurise the surplus cold fluid which simultaneously absorbs all the heat of compression yield, then there would still be 40Z of the surplus turbine energy yield in the form of cooled compressed air energy available to add to the turbine energy being used for the vapour compression part of the cycle.The extra energy then visibly being the lost enthalpy energy from the air on its exhaust as very cold exhaust from the process, i.e. it would be normal temperature on intake into the system of the process and say -1500C on its exhaust with the extra energy added to the system being the equivalent of the enthalpy energy contained in air between normal temperature and -1500C.

Thus it follows that in this alternative way the normal energy yield dcwn to ground state from the sub-system could become increased upon by the same order of factors as discussed in relation to the addition of the partial vacuum technique without the latter technique necessarily being required to be added, but of course if both techniques are becoming applied simultaneously then one should be able to achieve double the energy factor increases. Therefore, perhaps the main basic ways to improve upon the energy yield will boil down to the application of these two techniques, perhaps coupled with the 'above ground' pressure technique if possible to apply in the situation of the process and indeed if it is a method that will yield any bonus energy.

Considering the air compression technique in combination with the fluid recycling technique further, one can therefore envisage that the system arrangement could be one in which the heat of compression from adiabatically compressed air first becomes fully heat exchanged into the cold liquid phase to be recycled raising its temperature back up to that desired for re-entry back into the system, which could be to a higher temperature than the fluid comingfrom the vapour compression circuit to then potentially add a little to the energy output in this way. Which would be carried out under conditions of constant pressure cooling with respect to the compressed air pressure, i.e. as in the Brayton Air Refrigeration Cycle, re McGraw-Hill Encyclopaedia under 'Refrigeration', page 464.To leave remaining cooled compressed air still at the compression pressure, a part of which then being used to repressurise the re-heated fluid for re-entry back into thesystem, with the remaining cooled compressed air then going on to aid with the vapour compression part of this cycle. Yielding cold exhaust air in the process.

Thus, such a system arrangement would have some similarity with the process type under PA. 8720291.

Probably the quantity of extra energy made available for the vapour compression part of the cycle in this way being potentially of the order of 20 - 40% of the total vapour compression energy requirement, i.e. of the same order as adding the partial vacuum technique could potentially achieve.

As for the potentially possible way via the mysterious r to the four element that crept in towards the end of the preceding discussion on the fluid recycling techniquetand more specifically on nozzle enlargement, I don't take too seriously at this pre-practical stage and can probably be explained away as follows. If one opens up the nozzle to be larger then very much more fluid from the compressor would want to flood out of the enlarged nozzle in the absence of the fluid recycling technique and, therefore, on the application of the latter technique it would probably prove necessary to apply extra energy via the re cycling fluid on its re-entry back into the fluid flow to simply hold back the flood of fluid that would otherwise take place in the presence of the larger nozzle outlet.However, this is not to rule out the possibility that via design one may be able to acquire an energy advant age due to such a phenomena. Whereas I think that the application of the air compression technique for the recycling of the surplus fluid is a real way to BE production at the sub-system stage on the application of the fluid recycling technique. Perhaps alone able to yield sufficient Bonus Energy to make up the energy shortfall in the cycle that would exist in operating down to normal ground state.

Then additionally there is the potential possibility that the applica tion of the air compression technique to the whole of the sub-system turbine energy, including that required for the vapour compression, could increase upon the energy via the means described under the process type under PA. 8720291, but if so then the system enters into the region of invisible internal Van der Waal energy which is perhaps better not to be relied upon at this stage.

The heat absorption part of the cycle could of course still be from any source with probably a main one becoming via the natural heat in natural flowing waters, when such a process if applying the air compression technique in combination with the surplus fluid recycling technique would in effect be a Combined Water and Air-based Plant. However, the heat source could potentially be via the Air ARC cycle which if so could be more convenient in that the heat source would be available any time day or night to anyone in free and abundantly replenishable availability, with the added bonus that such a method of operation could at least double upon the very cold exhaust air capacity for the Big R purposes, etc.However, it is a method of operation that will depend even moreso on the overall energy balance achievable since to add to the potential shortfall in the sub-system energy there will also be the shortfall in the Air ARC cycle to make-up, which wcs4ld SQ by around 30 to 40x of the required air compression energy. Which, however, could prove possible by similarly applying one or a number of additional techniques to the ARC cycle, one of them being via a technique that I have termed the MAC Heat Processor, standing for Multi Air Compression Heat Processor which I discuss further in a following section.

Cooling via the application of very cold exhaust air: The manner of applying the very cold exhaust air to the cooling of the liquid Dhase exhaust fluid from the sub-svstem turbine could be verv

simply via a cooling tube menoaisimiiar in operation to the cooling

tube technique1in the condensation vacuum technique for vapour systems.

for the impulse fluid jet system may only be applicable to the method in which fluid jets pass down through rotating turbine blade(s) when the cooling tubes through which would be pumped the very cold exhaust air could firstly pass through the liquid phase of the fluid as it cascades down immediately underneath the rotating blades and then also through the layer of liquid phase at the bottom of the liquid phase.

Not to condense the fluid back to the liquid phase as in adding condensation vacuum energy to the vapour turbine systems, but simply to cool the liquid phase to a temperature at which it has a very low vapour pressure, which in turn would then be the partial vacuum pressure in the steady state of the process in the isolation chamber, which would be sealed all around and house the necessary parts of the sub-system with just the fluid flow outlet beneath the layer of liquid at the bottom of the chamber as the only outlet from the chamber. The cold fluid then flowing onto the next stage of heat absorption but firstly could become aPPlied for refrigeration en route on site, whilst the very

cold exhaust air could becomelfurther afield for the stated purposes.

Which should be still very cold because, remember, for the fluid to transfer the energy equivalent of the partial vacuum then it must itself lose the equivalent kinetic energy which itmust do by the fluid mechanics mechanism described, i.e. by the fluid molecules becoming more aligned into the forward vector on streamlining under the influence of the partial vacuum than could otherwise be the case in the absence of the partial vacuum as the ground state for this part of the process. Therefore, hardly any further heat should be required to be removed from the exhaust liquid fluid in order to maintain the low temperature required to maintain the low saturated vapour pressure of the cold liquid phase in the isolation chamber.Whilst I don't have precise data, the normal ground state temperature for R-21 is 90C when the liquid phase at such a temperature could create a SVP of normal lATS. in the isolation chamber, but if the exhaust liquid phase was, say, -2O0C due to transferring more energy from a more aligned fluid flow under the influence of the extra drawing force on the fluid jet creation of the partial vacuum, then the associated SVP in the isolation chamber would be around 0.3 ATS., which should almost self-sustain itself in the above way.

Similarly for a lower exhaust temperature and associated SVP.lwhas,with the aid of very cold exhaust air then perhaps almost a zero pressure vacuum would be maintainable in the isolation chamber. It follows from the discussion on such aspects that in one view of the overall energy balance of the overall balance that the BGS energy yield here would be that which enables a surplus output from the process even though the BGS energy itself would become consumed internally, and without the addition of which a surplus not being possible.

With further regard to the cooling of the exhaust fluid and having deliberated as in the foregoing thus far, it may be that one could allow the fluid to cross over the border into the fractional vapourisation region at or towards the end of the energy transference stage in order to perhaps gain the benefit of some volume maintenance and a pressure boost according to the effect described on page 147 of the text book 'Concise Physics' by R.B. Morrison. Then very quickly cool and condense the fluid via the application of the cold exhaust air, which would per

naps'1 become comprised ot a homogeneous mixture of say 90 - 70% liquid fraction and a 10 - 30% vapour fraction if and on crossing over the line to the right.As such the fluid would still largely behave as though a liquid with all the vapour fraction initially entrapped in the liquid phase and if the cold exhaust air then becomes quickly applied immediately on exhaust of the fluid mixture all the vapour should instantly become condensed back to the liquid phase, with the partial vacuum system then continuing to function in the same manner as that described in the foregoing. Thus, an aspect that could become experimented with on the development of the process and, of course, is a technique that could still be applied if and on crossing over the border in the BGS region of the P-E diagram.

The manner of compression of the air by the sub-system turbine energy could obviously be via several designs of air compression equipment but rather than a multiplicity of small units it could obviously be more efficient just to have onelarge unit or two reciprocating units compressing the whole air required in one operation, which in one design could be cuboid in shape with the turbine energy becoming transmitted to each of the four corners of the cuboid(s) in sub-divided equal amounts and simply effecting up and down motion of the lid(s) of the cuboid(s) with the air entering on the upstroke and adiabatic compression of the air on the downstroke.The advantage of such a system being that the air would be always plentifully fed to the cuboids by Nature anywhere on the Planet at any time of the day or night, albeit exhausting very much colder than it entered and therefore from the latter point of view the further afield the cold exhaust air becomes fed away from the actual industrial site of the process then the better.

CONTINUED DISCUSSION ON THE COMPARISON WITH THE COOLING CURVES: Now discussing the cooling curve, ABC, lower down the T-S Diagram, Fig.

2, in the encyclopaedia in order to further compare the difference between the existing process with that under discussion.

For the purposes of this comparison consider that in both processes the fluids commence in the same state at point A and then undergo the same constant pressure cooling to point C. The process in the encyclopaedia would in fact be the same as that under discussion with respect to the constant pressure cooling stage to point C with1 in thot cases con densation also taking place between point B and C as a part and parcel of the cooling.However, once at point C then the processes differ since in the process in the encyclopaedia the pressure under which the fluid is being held and maintaining it fully in the liquid phase for the temperature of the liquid phase becomes released with the fluid then flashing off a vapour fraction to adjust to the new low pressure environment of the normal atmosphere of lATS. and establish a new temperature - SVP equilibrium as associated with a pressure of lATS., involving the extraction of heat energy, i.e. kinetic energy, from the liquid itself for the latent heat of the vapour fraction. Thereby the liquid in this process becomes cooled by an amount equivalent to the amount of kinetic energy that has had to become transferred into the vapour fraction in the establishing of the lower pressure SVP at lATS.

Thus this process will be an adiabatic process in the sense that no external heat becomes used to effect the fluid vapourisation and no heat would become lost to the external surrounds. An additional way to view this process is to consider that once placed into the lower pressure environment of lATS. of the normal atmosphere and no longer under the higher pressure of the constant pressure cooling stage, then the liquid contains too much heat for the pressure that it is being held under and therefore loses heat in the way described until a new temperature - SVP equilibrium has been established.The quantity of heat removed from the liquid phase in the production of the vapour fraction will be either equivalent from E to D or E to D1, depending upon whether a valve is used and whilst I'm not sure, the extra heat removal on the use of a valve would probably boil down to being due to extra streamlining of the fluid taking place in the valve, whilst without a valve then the cooling would be that associated with a lower level of streamling or forward alignment of the fluid molecules, in turn as associated with the random state level of fluid forward alignment, i.e. none.Thus, the latter cooling would take place under the reversible conditions of the random state, whilst fluid flow as created via flow through a valve would undergo some polarisation in pressure from the random state into a high forward dynamic pressure and a low static pressure with the final conditions then becoming established in an irreversible manner to a lower temperature.Therefore, from this it could well be concluded that a streamlined fluid jet commencing with fluid on the saturated liquid line would curve across some way to the left of the line in the initial stages of the transference of the energy of the forward dynamic pressure of the fluid jet,then curve downwards more steeply towards the final random equilibrium state on the saturated liquid line, rather than follow the saturated liquid line all the way which could be the line just for a fluid all the time in the random state when transferring the energy of the pressure head. If so, then this would improve upon the risk of vapourisation taking place during the transference of the energy as in preceding discussion.The more streamlinable the fluid and the more streamlining actually achieved then the more advantage that could become derived from this aspect,and the lower down the P-E diagram andi or the more sub-cooled the fluid then the closer to the random state would the fluid in the fluid jet remain and the less the curving over to the left and the less the advantage derived, etc.

Thus, in the comparison with the process in the encyclopaedia, the fluid at the equivalent of point C would instead become streamlined into a fluid jet under the force of the constant pressure head when the random kinetic energy content of the fluid would become streamlined into the forward vector to some extent or other, which obviously would probably be possible to achieve to higher levels for fluid in the liquid-vapour state above or at the Critical Point for the fluid. When operating the process in such a higher pressure region then, of course, the same amount of heat could become removed from the equivalent of point A to point C for the turbogenerating part of the process, but during this heat removal stage a sudden phase change would not take place. i.e. as that from B to C.

On formation of the fluid jet it would then impact into the impellors of a sutiable turbine, just as theorised possible so to do in the text book 'Thermofluid Mechanics' by Pefley and Murray, 1966, on pages 270-1.

Whereupon the forward dynamic pressure of the fluid jet would become transferred to the turbine and the fluid would lose a corresponding amount of kinetic energy, depressurise, and cool. However, as in the preceding discussion, one of the difficulties will lie in avoiding the competing mechanism of flash vapourisation and particularly in the case of the system conditions under discussion, where the fluid comemnces as fully condensed liquid phase and is in a state right on the saturated liquid line.Thus, having regard to preceding deliberations one can imagine that in the case of the system commencing at point C at least the outer annular sheaths of the fluid jet would flash off immediately on the emergence of the fluid jet from the nozzle, resulting in the whole of the more immediate equipment disappearing in a cloud of vapour before the fluid jet even got to the impellors of the turbine, of either a Rolls Royce rotating blade type or a more run of the mill Pelton Wheel type. In this respect, therefore, the part of the fluid concerned would be as existing systems, e.g. as that discussed in the encyclopaedia.

In this event then sub-cooling the fluid to shift it from that of point C further to the left and more fully into the. liquid phase at the start could obviously be found helpful, but of course the more the pre-subcooling then the less streamlinable would be the fluid, etc. However, for the purposes of the ensuing discussion remaining with the fluid at point C and assuming no such flash vapourisation takes place which in any case may not take place if the static pressure and temperature of the fluid jet became that of the external environment on its formation which it could well do, but obviously would depend on very good fluid streamlining being achieved in the formation of the fluid jet with as little turbulence as possible becoming created at the edges in the outer sheath of fluid as the fluid jet flows past the internal nozzle walls.

Thus assuming no vapourisation takes place then the whole of the fluid jet will impact into the impellors of the turbine, transfer its kinetic energy and depressurise, and as it cools and contracts the P-E line of the fluid state commencing at point C may curve over to the left then curve down more steeply towards the final equilibrium on the saturated liquid line, either at the normal ground state of lATS. or at the lower BGS pressure of the partial vacuum technique if becoming applied. which, if so, would give a P-E diagram for the system which appeared to be upside down in relation to the T-S diagram in initially curving over rapidly to the left and then gradually converging towards the saturated liquid line along a steeper incline.Or alternatively, the P-E line of the fluid state may follow the saturated liquid line from point C for transference of the potential maximum energy,butnotwithstanding some earlier discussion, perhaps some curving over to the left would occur the higher up the P-E diagram the initial fluid state and the more streamlinable the fluid jet to give a slim handle on the side of the P-E diagram. However, now bringing the discussion to the more important aspect7in a primary sense,that I wish to discuss here which I don't think I will in fact totally resolve at this stage in these deliberations, but the confusion of which should not become confused with the confusion so far although of course all the confusion is intrinsically interrelated.This being the question of the pulling of the punch of impact effect due to equally rapid and simultaneous fluid contraction taking place as the fluid impacts into the impellors of the turbine and transfers its energy of impact. Now if a fluid jet became created from fluid at say the Critical Point for the sake of descriptive convenience, then imparted energy to a turbine down to say normal ground of lATS. pressure, then the enthalpy energy that one could read off from the horizontal axis of a P-E diagram between these two points would be the energy difference between these two fluid states in enthalpy energy equivalent,and indeed would be the amount of energy that would become transferred into a vapour fraction under a normal flashing process.However, according to theorising to date, on the one hand the energy that would normally become flashed off in a vapour fraction would be that which instead would become transferred to the turbine, which in turn would be represented by the above quantity of enthalpy energy, whilst on the other hand, my theorising to date is that the initial energy of the fluid jet, which in this example would be represented by the enthalpy value on the horizontal axis of the P-E diagram corresponding with the Critical Point, would become reduced to around 40% for this example due to the fluid contraction effect additionally detracting from the velocity of the fluid jet as it impacts its energy adding to the normal loss of fluid jet velocity due to the transference of kinetic energy of the forward motion of the fluid jet.But if this proves the case then in a normal P-E diagram energy balance for the cycle of the process there would be a considerable amount of energy missing between the Critical Point state and the ground state totally unaccounted for,wtri)st for the flashing process then the energy balance on the P-E diagram would fully account for all the energy involved, but if the energy that normally transfers into a vapour fraction on transference to a turbine instead becomes appreciably reduced then to date there would be a gap in the energy of the P-E diagram energy balance.

But, of course, one cannot have energy unaccounted for or more apt to say unaccountable for, which in this case would be mysterious disappearance of energy in contrast to themysterious materialising of energy annarentlv from nowhere in the case of the process under PA. 8728601.

Therefore. in relation to this aspeci; of the workjintroducing a new

Dotentiallv possible concept ofthe overall energy balance between tne two separate processes

o saHLS - on tejbalance, before now progressing on with the normal discussion at this stage.

Firstly, on further consideration and notwithstanding the postulating thus far on this question, it is perhaps more likely that the energy of the fluid jet would become detracted from by the mean of the fluid volume contraction and not by the full, final fluid volume contraction, if at all.

However, with respect to the latter question, it is contraction that would not take place by the cold state reference fluid which therefore would be expected to be able to potentially impart the full d MV2 energy value of the fluid jetas one would calculate before impact, on impact. Similarly aS for a solid object with a certain h MV2 kinetic energy value of forward motion.Therefore for -a fluid or solid object that contracted on impact then I think the 3E MV2 energy value that one would calculate based on the velocity of the fluid jet or object before impact would, in fact, become detracted from on impact by the contraction effect on impact, but perhaps by an amount proportional to the mean of the volume contraction rather than by an amount proportional to the final level of volume contraction.

Because, of course, the fluid would only reduce in volume after the initial impact and/or on the initial impact, i.e. simultaneously. Obviously, there are similarities with crash resistant systems absorbing the energy of crash impact and, indeed, with the mechanism of springs, mechanical buffers, boxing gloves and the like.To leave remaining the question: by how much would the initial energy of the fluid jet become detracted from by the fluid contraction effect? If, as in the example herein based upon R-21, the fluid volume contracts to 40% of the initial volume finally, then the fluid jet energy may not become reduced to the level of 40% of the initial energy value but rather to 70%, i.e. the mean of the volume contraction from 100% to 40%, which may be a level of reduction that relates better to possibly an advanced P-E diagram picture of the energy balance as will be further discussed. Should the 70% level be found to be the case in practice, then obviously the process could become appreciably less border-line than hitherto considered with respect to the subsystem energy yield being able to sustain the compressor. Although when transference, conversion, recycling and further transference and conversion inefficiencies become applied, then the process could still be as border-line as hitherto considered. Therefore, all the techniques to Bonus Energy that I have evolved and deliberated upon would perhaps still be necessary and, in any case, would usefully add to the overall energy balance of the process, even if not as essentially required as first considered? On the other hand, the energy may become reduced by an amount related to the full fluid volume contraction, i.e. to the 40% level, as first considered, when my deliberations to Bonus Energy would then be more worth while.One way to this could be via a train-buffer

parallel, and more specifically via applying the equationltne effect the contraction of the buffer has on reducing the impact of the train, considering that the buffer is the fluid and that one is impacting the impellors into the fluid as in wind tunnel reverse experiments, etc. A train at full velocity would probably plough through to the platform with the buffers just lowering the impact by å certain amount in such a case and, therefore, similarly one would expect the energy of the impact of the fluid jet to become reduced by a certain amount. The energy of impact of the train would become reduced by the quantity of strain energy that could become stored in the springs of the platform buffers.If the former is more than the latter, then the train would plough through to the platform. Similarly, it is being considered herein that Van der Waal forces inside the fluid, which could perhaps be considered to be spring forces in one sense, get a tighter grip on a proportion of the energy rendering it'non-transferable, which could therefore perhaps be equated to stored strain energy in springs of buffers removing a proportion of the energy of impact of a train on train impact. However, the removal of energy in such a way is not to date a normal feature of P-E diagrams as far as aware, but I think could quite readily become so if the above is found to be a part of the mechanics of the system in practice. However, unfortunately a part of this aspect is embodied within a part of normal P-E diagrams that I don't fully understand as yet.This being that all such diagrams for refrigerant fluids seem to commence with zero enthalpy content being at -400C. But most of the freezing points of such fluids are well below -400C and for R-21 is -1350C. Therefore, I think it follows that there must in fact be quite a high quantity of enthalpy energy in the liquid phase at the temperature value of -400C because, by definition, one would be able to remove heat energy from the fluid all the way down to its freezing point temperature and, indeed, all the way down to absolute zero of -2730C, which would then include the latent heat of fusion, when the fluid would then truly contain zero enthalpy energy.Therefore, by definition, the fluid must contain enthalpy energy at -400C and not zero enthalpy energy, yet P-E diagram for the refrigerants all seem to commence with zero enthalpy along the horizontal axis being at -400C.

However, it is tnis 1energy that it is being postulated would be that which the energy of the fluid jet becomes reduced by as it cools and contracts, which is really the re-encapturing and restricting of translational molecular motion by a progressively increasing amount by the Van der Waal forces in the fluid as the fluid cools and contracts under strengthening Van der Waal bonding therein, which they are not able to do when heat and pressure is added and therefore for fluid at the Critical Point the Van der Waal forces in the fluid would not be and could not be holding onto energy of molecular translational motion in the above manner.

But as the fluid transfers energy, then not only will the fluid jet energy become less by the energy transferred but the energy remaining to be transferred will be less than it was initially in the fluid jet. All of which would seem to be the same phenomena as discussed with respect to the downgrading of energy in my discussion in relation to the process under PA 8728601 on page 112 thereof. But equal and opposite in the sense that in that process one would be able to try to strive to avoid the loss of energy due to this phenomena whilst in the case of the process herein, all the energy would inevitably go to Van der Waal rather than become transferred before it gets an opportunity so to do. In other words, the

fluid would be lett remaining with enthalpy energy that Van der Waal recaptures via fluid contraction.Which in fact could be a level of energy that equates closer to the 40% level of reduction as first considered, rather than the lower reduction to the 70% level as subsequently considered may in fact be the case in reality.

Now in the vapour flashing process the reason why the initial energy amount on transferring into a vapour fraction instead does not become reduced is because the Van der Waal forces would not exert on the transferred energy via the above mechanism of fluid contraction because the vapour fraction would not contract and indeed would expand on depressurisation to give further equal and opposite similarity. But the liquid phase fraction of such a process would and in exactly the same way as for the process under discussion. Therefore, when there is no vapour fraction and all the fluid remains in the liquid phase, then the energy that would have normally become transferred into a vapour fraction and then there not become subjected to the fluid contraction effect on the energy would now be energy that would also become subjected to the fluid contraction effect reducing the energy quantity.However, this is an aspect not yet fully clear both in terms of the precise mechanics involved and in the quantification of the amount of the energy that would be involved, although on the latter question I think that I am now perhaps tending to favour the 40% rather than the 70% level because, whilst it will probably be the mean of the relevant parameter that will be the correct value to apply, this will probably be arrived at as follows. The first relevant parameter involved will be the effect that the internal contraction of the fluid under strengthening Van der Waal bonding has on the velocity of the fluid and it will be the mean of this effect during the transference of the whole energy that will be correct to apply.But then to express in terms of an energy value the mean reduction in velocity determined in the above manner would become squared in accordance with the energy equation KE = h MV2. Therefore, whilst the mean reduction in fluid volume during the transference of the energy could well represent the mean reduction in velocity due to the fluid contraction effect since the fluid would be contracting in all three dimensions, this mean reduction value would then become squared in order to give the mean reduction in energy due to the contraction effect.

Which of course would not then be the reduction to the tonal volume but a reduction value of the same order arrived at in the above different but probably correct manner, e.g. for a mean velocity reduction of 70% then the mean energy reduction would be 49%. Therefore, perhaps somewhat better than the 40% level first considered but probably no higher than 49% and therefore still closer to the 40% level than the 70% level. However, this will be an area of the system that will require some accurate mathematics to fully determine, which I don't intend to carry out at this more general stage but may conduct later.Suffice it to say here that the initial fluid jet energy is likely to become reduced to between 40%

to 50% of the initial value with respect to the amount otlenergy that could potentially become transferred to the turbine of the sub-system due to the fluid contraction effect during the transference of the energy, with the other 50-60% of the energy becoming rendered non-transferable energy as the fluid contracts which I think will be an amount of energy that will equate to the enthalpy energy left remaining in the liquid phase all the way down to absolute zero and in this way the energy balance of the turbine-compression cycle becoming balanced. Remember if the initial fluid jet energy did not become reduced, then the process would be extremely easy to achieve because the energy could be almost double that required for the compressor and I think that one of the main aspects that

channelled my mind into thinking that the energy would become detracted from by as much as first considered is the fact that otherwise the process would be so very easy to achieve and if this proved the case, then surely it would already be in operation and therefore it had to become borderline and just under, which it does when one considers the likely effect of the simultaneous'fluid contraction on the energy yield.It is not that the energy disappears as such in an inexplicable manner, but that the contraction effect caused by the drawing together of the atoms in the molecules of the fluid on cooling would render a proportion of the energy non-transferable in the process in a mechanism which could be likened to a pulling of the punch effect or re-absorption of released strain energy e.g. as in illegal golf swings, which I think must then be equivalent to the amount of enthalpy energy left remaining in the cool, contracted fluid all the way down to absolute zero, although not directly in the normal sense of becoming transferred from one energy state to another, but rather that the energy left remaining will equal the Van der Waal energy involved effecting the contraction of the fluid, although I don't quite see why this should necessarily be so at this stage.Then on the addition of heat and pressure the'Van der Waal forces would not be able to hold onto the energy of the translational motion of the molecules in the fluid by the same amount.

With further regard to the latter aspect, if one considers the reverse of the mechanism to that which will take place under fluid contraction, i.e.

under fluid contraction the mean velocity of molecules in the fluid will probably become reduced proportionately but the enthalpy energy that they represent would therefore be reduced in proportion to the square of the mean velocity and therefore to the mean fluid contraction. However, I think a more linear relationship exists between mean fluid contraction and enthalpy content which, in turn, would have a bearing on the amount the energy would become reduced by on fluid contractionsperhaps bringing the level back closer to the 70Z level. Therefore, this is a whole area of the system requiring of further deliberations and treatment. However, the relationship is not fully linear and given reductions in percentage volume change will progressively represent less amounts of enthalpy energy change. And then vice-versa.However, since this is an aspect not yet fully clear I will progress the discussion onto other related aspects.

Thus, here making mention again of the possibility that because Van der Waal forces may cause energy to apparently disappear in this process by an amount somewhere between the 40% to 70Z reduction levels, then perhaps in the other processes under PA. 8720291 and 8728601, those same Van der Waal forces can create an equal amount of energy in the equal but opposite way discussed under that work.

At perhaps the Apex of science and technology in these fields and there perhaps evolving some of the final processes for the final Coming Kingdom on Earth that will serve Mankind for as long as He lives on Earth in a culmination of all such work to date in the Alternative Struggle to Freedom in real terma by Mankind on behalf of Mankind, then I do not rule out such a concept in balancing energy at such an Apex, whilst at this stage thinking that such thinking is perhaps somewhat over the border into the barmy thinking region. However, should the above prove the case then perhaps gas heating would not be required at all to make up any shortfalls in energy in the various processes of the work because perhaps there may not be any in such processes.I leave readers with this final thought, is it the case that the overall balance can be restored via one totally separate process in the case of the remission of sins by Jesus Christ on behalf of the sins of others? Enough of this nonsense and progressing on, although before doing so just one final thought on the topic, is for example the Body of Christ on Earth in reality comprised of totally seperate processes, or is it regarded all as one Body by the Powers beyond at least and in reality all dependant upon the efforts of others.

High Fluidity Fluids coupled with a correction to the preliminary calculation example: The next topic planned for further discussion in this somewhat rambling discussion is further deliberation on what is likely to be the situation when employing refrigerant fluids of very high fluidity value as at the ground state of the process in comparison with known experience with water in normal hydropower systems. For example, and firstly, in R-21 having a viscosity value of 0.34 cp at NTP compared with water of 1 cp at NTP, what difference would this make if R-21 at NTP substituted for water at NTP in a normal hydropower system.Referring to the basic fluidity equation, i.e.: 8V1 Fluidity s f (P1-P2)r4t For all other parameters oFthe system being equal then the volume flow rate and, therefore, the velocity of the fluid jet would be 1/.34 - 3 times higher at the exit from the nozzle stage than the water-based fluid jet. And, therefore, would probably produce 9 times more energy in accordance with the energy equation KE = MV, if this was all that was involved. However, if the volume flow rate increased then the mass flow rate would increase and one would soon lose the constant pressure head, assuming that the rate of replenishment of the pressure head is the same in both case which would have to be the case for the comparison.Therefore if this were the situation then one would have to reduce the nozzle CSA to give the volume flow required to maintain the pressure head and probably the energy yields would then become the same. Thus, determining the required nozzle CSA reduction, as follows.

Basing on the basic equation, the comparison would be: For water:- For R-21: V V 1 = - 3 = - r4 r4 Therefore for V to be the same in both cases: 3 1 - for R-21 would have to equal - for water.

r4 r4 Assuming r s 1 for water then r for R-21 would be: r4 = 1/3 = 0.333 r2 = 1/3 = 0.577 r = 0.76 Therefore, the nozzle exit CSA for water would be: r2 1 3.142 And for R-21: r2 s 3.142 x 0.762 - 1.815 Therefore, for the same volume flows now the respective mean velocities of the fluid jets would be 3.142/1.815 - 1.73 times higher in the case of that based on R-21 through the reduced nozzle CSA, whilst the mass flow rates would be the same. Therefore on applying the energy equation KE - F MV2 one may consider that one would still obtain more energy in the case of the system based on R-21. However, because the nozzle CSA is reduced the surface area of impact will be exactly correspondingly reduced and therefore this will mean that the energy yields would, in fact, be the same in this type of system. On the other hand, one could consider the energy yield would be higher by the amount indicated by the increased velocity which, in being 1.73 times higher, would indicate a 3 times increase in energy yield which, in turn, would be the square root of the 9 times higher energy yield. But this could not be so, because a pressure head has a certain energy value and the fluid would be really simply a medium for harnessing the constant energy value of the constant pressure head, whether it be water or R-21, that is being used as the energy-harnessing medium.Therefore, in such a comparison in such a system then I think it would be found that the reduced surface area of impact would exactly compensate and render the energy yields the same whether the pressure head be harnessed via water or R-21. At this stage remembering that up to this stage we are just considering the comparison between cold state systems.

Which is a conclusion that really has its origins in the law of transmission of pressure and it will only be the conditions of the system that will differ for the transmission of the same energy value of a given pressure head determined by the different fluidity values of the different energy transferring fluid medium. The Law of Transmission of Pressure in this context I think would simply state that force times surface area of the transmission of the energy will remain a constant,

a given

pressure head the1 will be different for different fluids of different fluidity value as the energy transferring mediumi tthe law of transmission of pressure in this context

state that force times area in the transmission of the energy of the pressure will remain a constant.Therefore if the force of impact increases and the area of impact reduces by the same amount, then the pressure energy transmitted would remain the same.

of course stand to be corrected by my noble fellows.

However, assuming this interpretation of the Law to be correct for this system in such a comparison within the system, then if the force of impact increases, i.e. as given by the force equation KE t MV2, but the area of impact reduces by a corresponding amount, then the actual pressure energy transmitted would remain the same. Thus and thereby the energy yields would remain the same.

It therefore follows that this would have to be an aspect that would have to become built into the beginning of the preceding worked example, since whilst the mgh value of the pressure head would remain the same and be the energy value transmitted by whatever fluid was being used to transmit the energy, the manner of transmitting that energy would not be directly given by the relationship: mgh s F in the case of a liquid with a different fluidity value than water. In the case of normal hydropower harnessing, then these two equations become directly equated in order to first determine the velocity of the water required to transmit the mgh energy value of the pressure head, and then

from this one/determine the nozzle CSA required for a desired water volume flow by dividing the latter by the determined velocity.However, for a fluid with a different fluidity value then from the basic fluidity equation I think one would first have to determine the different nozzle CSA required for the higher fluidity fluid to give the same mass flow rate under the same pressure head, then incorporate this difference between the two systems into the above expression as becomes applied for hydropower harnessing.

Perhaps the better approach to this initial aspect of the worked example would be to first substitute the volume, V, parameter by mass divided by fluid density, since we are concerned with maintaining the mass flow rate the same. In which case the basic equation would become: 8ml Fluidity = #(P1-P2)r4t x density Then in the comparison between water and R-21 for 1 unit mass to flow through 1 unit length in unit time under the same pressure head, i.e. as would be required for the same mass flow rate from the same pressure head in both cases, then the only system condition variable will be that of the parameter r to the four on the bottom line. However, both the fluidity value and now the fluid density will be different for different fluids.

The fluidity value of R-21 being 3 times higher than water at normal state and its density is 1.366 compared with 1 for water at normal state. Therefore, substituting these different values and equating the two respective resultant equations as follows: Fluidity R-21 x density fluid x r to the four R-21 = Fluidity water x density water x r to the four water.

Both the fluidity and density of water can be taken as 1 and when they are the following will apply: Fluidity R-21 x density fluid x r to the four R-21 r r to the four for water.

4 Fluidity R-21 s r water 4 r R-21 x density (for water g 1) 4 4 r R-21 s r water Fluidity R-21 x density R-21 Therefore, from this expression one can determine the nozzle radius, r, required for the system based upon R-21 to give a mass flow rate the same as for the water system. Then from this the nozzle CSA and from this one would obtain the fluid jet velocity by dividing the volume flow, V, by the nozzle GSA. Thus, basing on r = 1 for water: r4 R-21 = 1 = 1 3x1.366 4.1 r4 R21 = 0.244 0.703 2 Then CSA R-21 s r w 1.553 2 CSA water - r - 3.142 However, the volume V flow rate in the case of R-21 will be less than for water in the ratio of the respective densities.Therefore, the velocity ratio of the respective fluids would be as follows: For water 1 s 0.318 3.142 For R-21 1 s 1 density R-21 x 1.553 1.336x1.553 = 0.47 Thus for R-21 the velcoity of the fluid would be 1.48 times higher than for the same mass flow rate under the same pressure rate, which I will round to 1.5 times higher. Requiring of a nozzle GSA 2.02 times less, which I will round to 2 times less.Therefore, referring again to the expression: mgh s F MV 2 If one places in this expression the value of 1.48 times higher velocity, the KE value of the fluid jet becomes 2.19 times higher, but of course the mgh value remains the same and, therefore, now it's a question of concluding what would be the required addition to the above expression for water for this system based upon a fluid of a different fluidity value and I think one can conclude that it would become evolved to the following expression: : mgh s F MV2 x CSA for R-21 CSA for water Thus confirming my earlier conclusion that the constant pressure head would equate toFforce x area over which the force becomes applied, in a comaprison between two fluids requiring of different conditions to transmit the power, i.e. energy in unit time, of the constant pressure head, which in turn would be in compliance with the Laws governing Science and more specifically here the Law governing the transmission of pressure.

It therefore follows that which would be required to be built into the preceding worked example would be: mgh = h M'72 x GSA for fluid CSA for water However, since one would only know the mgh value of the potential pressure head at the beginning of such an applied calculation, then one would have to arrive at the other values via the foregoing treatment.

All of which, however, could be still off the beam but at least it's some kind of a starting point for the practical development of the process. However, assuming to be correct then the treatment should be the same as in the preceding worked example once past the foregoing initial hurdle.

Now, where does this aspect of the system leave preceding descriptions herein? Well, I think basically sound but is an aspect that would have to be considered further and perhaps become built-in better on a further run through the work

However, deliberating on this aspect here a little, I think that the preceding descriptions will all be correct as discussed, apart from the fact that in a comparison with water in the system one would be commencing with a smaller nozzle GSA and a correspondingly faster fluid jet than would be the case if water was in the system under the same pressure head. And in the case of R-21 then the nozzle GSA required would be half that which would be required for water and the fluid jet velocity would be twice as high.But the important aspect being that the energy becoming transmitted would be the same and that of the mgh value of the pressure head, simply that the higher fluidity fluid would require these different conditions than would be required for water to transmit the same energy in unit time from the same pressure head. Then on heating the fluid the descriptions will be as discussed, firstly that in relation to the nozzle GSA remaining the same and then that in relation to reducing the nozzle CSA to give a mass flow rate of unity for the hot fluid.Hopefully without confusing the discussion further, this

will in fact occur again in a separate context, namely on streamlining the fluid jet when the area of impact for the same mass flow will become reduced

lt lti tb / the x-factor increase in velocity

the increase in energy and not an increase related to the square of the increase in velocity.

It is in fact quite easy to show that this will be the same as reducing the energy that one would obtain via the MV expression for the increased

velocity in the ratio of the reduced CSA, i.e.1 the energy one would 0bjvn

will equal the energy one Could compute for the increased velocity x the ratio of the reduction in nozzle CSA.

The latter beingldirect

the law of transmission of pressure and as discussed in the foregoing.

The above aspect is also part and parcel of one of the exercises in my earlier writing where it becomes shown that the above will be the case on streamlining a given mass of fluid.

Thus, in the case of the descriptions in relation to the use of R-21, one would commence with a nozzle CSA half that required for water to transmit the same pressure head, but then on heating to the Critical Point the velocitv of the fluid jet would become faster bv the 4.5 times factor to

give an energy increase of 20 times but then/the Smass flow' rate would become too high in the ratio of 4.5 volumes to 2.5 volumes and one would either have to recycle the surplus fluid or reduce the nozzle CSA, then to this one could add the streamlining advantage, etc., etc., all as in the preceding descriptions and worked example based on those descriptions.

Again hopefully not to confuse but to clarify further, for the description in which the nozzle CSA becomes reduced to give a mass flow rate of unity for the same fluidity fluid then the energy value in such a case would remain directly related to the square of the velocity without having to take into consideration the reduced area of impact, because in such a case one is also reducing the mass by a proportional amount, this being the reason for reducing the nozzle CSA, and therefore the reduction in the mass will be equal to the reduction in the nozzle CSA in the first place or, conversely, the higher nozzle CSA will have a correspondingly higher mass flow rate. Thus it is only when the mass flow rate is the same that one would have to consider associated changes in surface area of impact.

Firstly as discussed in the foregoing for fluids of different fluidity values requiring of different nozzle CSAs to transmit the same energy in unit time as via the same mass flow rate in unit time. Then secondly when on streamlining the fluid further the same mass flow rate will flow through a correspondingly reduced nozzle CSA.

With further regard to a certain aspect of the descriptions, I caught part of an O.U. programme the other night dealing with Fluid Mechanics (22nd June 1988), and whilst there in relation to a comparison between turbulent and laminar flow it would seem to me that embodied within this comparison was confirmation that on applying the extra applied energy of the partial vacuum to the fluid system

under discussion it would be the velocityj in iaminar fluid flow that would increase to approach that of the central velocity and more specifically in the manner of the sheet tent description.

It perhaps also became confirmed that on changing from a normal Bellmouth nozzle to a specially shaped streamlining nozzle, then one could potentially

some advantage due to the fluid flow becoming more forward aligned in so doing. One can envisage that on entry and flow through a Bellmouth nozzle then the fluid molecules in the entering fluid would tend to become/ remain more scattered in random directions and not become as aligned as for the same fluid entering and flowing through an appropriately shaped streamlining nozzle.

Thus I amlin some accord with the OU's version of interpreting certain aspects.

An aspect which perhaps becomes raised by the foregoing deliberations is that it probably follows that if the rate of replenishment of the pressure head could keep up with a faster volume flow at the turbine end of the system as would be possible on the use of a higher fluidity fluid in comparison with water, e.g. R-21, then the system may in fact be capable of yielding more energy than the same system based on water for everything else being equal. However, if the replenishment rate of the pressure head was similarly faster for the system based on water, then because the fluid velocity would be slower for a given pressure head, the pressure head in such a case would build up to a higher level and probably the energy yields would again become the same in this manner.

For the process under discussion the flow rate determining steps of the process will probably be the rate of vapourisation and the rate of compression of the vapour and therefore obviously one couldn't have the fluid .speeding around its closed-cycle circuit any faster than becomes determined by the slowest of these stages in the circuit of the process, but if one could increase upon the circulating flow rate of the fluid around its closed-cycle circuit then this could be a further way to BE. Which would probably be achievable via one of the methods of operation in which the liquid phase of the refrigerant has an appreciable lower temperature than the heat source to then increase upon the temperature gradient and therefore upon the rate of heat flow from heat source into the refrigerant at the vapourisation stage.However, the compression energy input requirement would be correspondingly faster and therefore there would be no gain with respect to this part of the in creased energy production in unit time, but for any surplus energy produc tion at the sub-system stage over and above that required to sustain the it compressor, then perhaps the overall power yield,1,energy production in

unit time, coula become improved upon m sucn a way, whlch wouldlconstitute a further way to BE.

In preceding discussion it has become concluded that perhaps operating the process with the fluid R-13 could be the better approach using a ground state of 20 ATS for the process, since this would then give one flexibility with respect to heat source temperature. However, for the sake of this advantage one could be increasing upon potential nozzle difficulties magnified many-fold because it follows from the foregoing discussion that for a fluid with such a high fluidity, i.e. 60 times higher than water and 20 times higher than R-21, then the required nozzle CSA for a given pressure head would be very small in comparison, although to overcome such difficulties there would be the potential for increasing upon the fluid recycling technique.Since this would involve the recycling of by far the higher proportion of the total fluid in such a case, then this could potentially lead to some BE via the reducing r to the four element on increasing nozzle CSA over and above that required for a mass flow rate of unity or just above. Thus, notwithstanding the foregoing doubt, perhaps one would be able to apply R-13 successfully in the process in order to obtain the extra flexibility in the potentially possible range of operation, but also to consider would be the comparative energy advantage that could be obtained below the normal ground state of the process, which in such a case would involve sweeping aside the external vapour pressure immediately on the exit side of the turbine as in preceding discussion.

Which, however, may not be as successfully achievable as the application of the partial vacuum technique when in contrast one needn't sweep aside the external vapour pressure because in such a case it would be the very inherent absence of external vapour pressure in the first place that would be giving rise to the BE.However, a further thought has just this minute struck me, i.e. as an alternative to sweeping aside the external vapour pressure and/or additional to the latter technique, perhaps it would prove possible in practice to apply very cold exhaust air from the fluid recycling technique to the external vapour pressure zone immediately on the exit side of the turbine system in order to continuously precipitate as raindrops the external vapour pressure immediately on the exit side of the turbine and thereby create a very low pressure in the zone immediately on the exit side of the turbine in comparison to the normal level for the process of 20 ATS. Which, however, could literally be a nout inside thought because, of course, the external vapour pressure would immediately if not instantly rush into the zone becoming depleted of vapour pressure in such a way.But would it if in combinaktion with a technique to sweep aside the external vapour pressure? Thus a further facet that one could play around

with toachieve BE after developing the basic system which alone could be good enough. However, of the two approaches as via R-21 or R-13 respectively, I don't know at this stage which I would recommend as the better starting point for the development of the process, although probably the safer bet would be the approach via R-21 for use in warmer waters, then progressing on to the higher ground state pressure approach as achievable via R-13 or some other fluid for use in colder waters with the flexibility to be used over a range of water temperatures, which would be a particularly useful advantage for use of the process for the provision of ship's power when the waters may commence off hot or cold at the start of a journey but then could change to hotter or colder as one progressed on the journey as the case may be, requiring the heat absorption equipment to become dipped into waters of changing temperature as one journeyed on, e.g. as from the English Channel to the Equator and then progressing on from the Equator into the Southern Polar region. However, I propose now to progress on with the discussion and

picking up the discussion thread of

a point at which I discuss a little about the normal throttling process, which is lacking in the discussion so far.

Discussion on the normal throttling process: There are in fact a number of scientific descriptions of this process in a number of the text books covering this type of subject matter. However, I will add to these by placing the process in my plain man's poor man's guide to scientific processes and systems terms. Or detract, as the case may be deemed to be.

For this I will refer' to the diagram of a throttling device given on page 22 of 'Refrigeration and Air Conditioning' by W.F. Stoecker, in combina

tion with huts description or the process,andlas given under the PlcGraw- Hill Encyclopaedia in relation to the process discussed in the preceding.

In the latter process, fluid was taken to state C, which in being at a state just on the liquid line is a state when any release of pressure under which the liquid is being held and maintaining the fluid just but

fully in liquid state would1 result in a proportion of the liquid phase vapourising because at the lower pressure the pressure would not then be sufficient to hold the fluid fully in the liquid phase.Or to place in more scientific terms, under the lower pressure the thermodynamic equilibrium of the fluid state on adjusting to the new lower pressure would involve the production of a vapour fraction until the vapour pressure under which the liquid was being held was again sufficient to maintain the liquid phase in the liquid phase for the new lower temperature that was becoming created as heat left the liquid phase and entered the latent heat energy mode of the vapour fraction becoming produced.Thus and thereby the fluid will also cool as the pressure becomes released and a vapour fraction becomes produced, which will be the same temperature throughout both the liquid and vapour phases because when heat energy enters the latent heat energy mode of the vapour fraction becoming produced it will no longer become manifest as temperature, i.e. as kinetic energy in the form of translational motion of molecules in all random directions before any streamlining. Thus, vapourisation would continue as required to maintain the new thermodynamic equilibrium for the lowering pressure and the accompanying lowering temperature.And if the lowering of the pressure was all the way down to normal 1 ATS, then one would finish with a fluid whose vapour fraction was at a vapour pressure of 1 ATS. and both the liquid and vapour fractions would be at the new, lower boiling point temperature associated with the lower vapour pressure of 1 ATS. acting on the liquid phase. And the vapour fraction of the whole fluid would be whatever the proportion had to be to establish the new thermodynamic equilibrium under 1 ATS. of vapour pressure. Of course, lother heat was allowed to enter into the system during the process then the new thermodynamic equilibrium that became established would be somewhat different. However, here we are simply concerned with the adiabatic process and therefore not to digress onto such aspects at this stage whilst bearing this potential of the system in mind.

Thus, in the process under the McGraw-Hill Encyclopaedia in essence the fluid is allowed to adjust to a vapour pressure of 1 ATS. acting on the fluid, which in turn is the external pressure of the surrounding normal air atmosphere acting on the fluid, and which in turn is why the new thermodynamic equilibrium will adjust to this pressure if simply allowed to vapourise into the normal atmosphere. This description then goes on to say that in practice in this process the fluid is passed through a valve into the atmosphere. Now if at this point we turn to the diagram of the throttling device given under Stoecker and imagine this system to be at point C.In effect the aperture of the restriction can be regarded as the valve in the above process, but then on the other side of what is in effect the valve there then being in effect a continuation of the pipework to confine the fluid liquid-vapour mixture and thereby to effect a continuation of the fluid flow to the next stage in the process. In other words, if one first envisages the pipework to initially be full of air at 1 ATS, then the liquid under vapour pressure to the rear and maintaining the fluid fully in the liquid phase at this stage f lowtngalong the pipework to the restriction, the first part of the fluid will pass through the restriction and undergo the process described above, which in turn will then become the fluid in the pipework beyond the restriction pushing out the air.

But as far as further portions of the fluid passing through the restrictions are concerned it will still be a pressure of 1 ATS. on the other

side of the restriction that the fluid is then being subjected to and1 which it will have to thermodynamically adjust to. Whereas on the

side of the restriction the fluid will continually be being maintained under the vapour pressure of the compressed vapour at the other end of the liquid phase flow and acting on the liquid phase at that end of the fluid flow.

And the size of the aperture would have to be whatever it had to be in order to maintain the mass flow rate at unity to in turn maintain the pressure. Thereby, the fluid mass flow rate velocity remains constant and the fluid continues on along the continuation of the pipework at the same mass flow rate velocity, i.e. there will also be a continuation of the same fluid velocity with respect to its mass flow rate. It also follows that it could be concluded that the normal dimensions of the aperture of the restriction of normal throttling devices would in fact, in general, be the basic dimension of the CSA of the nozzles in the system under discussion for comparable systems.Thus, it can further be concluded that the only basic difference will be that in place of the normal restriction of a throttling device will be a nozzle of the same basic CSA dimension and which will instead streamline the fluid liquid flow into a fluid jet. Therefore on the emergence of the fluid jet from the exit of the nozzle why will it not be the same as the same fluid in a comparable system going through the aperture of the corresponding throttling device aperture as it enters into thesurrounding atmosphere of lower pressures, e.g. normal air pressure of 1 ATS en route to the impellors of the turbine.Very simply, the answer being because the fluid will have been pre-streamlined into a jet on its emergence from the exit of the nozzle, which will strike the impellors of the turbine and impart all its kinetic energy to the turbine before it thermodynamically re-adjusts to the lower pressure of the surrounding atmosphere, when it will

thereby finish at the pressure of the surrounding pressure and will not be required to adjust further to the surrounding pressure under which it then subsequently becomes subjected to. And the

amount of kinetic energy transferred to the turbine will be the amount of kinetic energy, i.e. heat energy, that would otherwise have to pass into a vapour phase in the normal throttling process. Thus the fluid should also remain fully in the liquid phase at the end of the turbine stage.The desired state for the next stage in all such processes and systems.

Thus, because the fluid will become streamlined into a fluid jet it won't disperse into all random directions on emergence from the nozzle as would the same fluid passing through the aperture of a throttling device. However, having regard to my deliberations over this aspect of the system I think one would either commence with fluid at or above the Critical Pressure in order that the fluid would not be susceptible to such vapourisation, or sub-cool the fluid to well to the left of the saturated liquid line in order to prevent such vapourisation taking place.

An aspect of such streamlining through a specially shaped streamlining nozzle with very smooth internal side walls will be that the fluid friction against the internal walls of the nozzle will be very minimal, leading to very little pressure loss due to such effects. While in contrast on the same fluid passing through the aperture of the throttling device, fluid friction against the internal wall of the aperture will be quite high.

However, it will not be the fluid friction as such that will lower the pressure, but the fact that the fluid will become scattered in all random directions on the other side of the aperture where the prevailing pressure will always be at the low pressure that the fluid is being lowered to.

Thus on the initial side of the aperture the fluid will be continuously being held under the compressor pressure, but on flow through to the prevailing conditions on the other side of the aperture the fluid will become subjected to the low pressure of the system when instantaneous, contained, vapourisation will take place to the low pressure in the steady state of the system flow.

DEVELOPMENT PROGRAMME: Finally, before progressing onto the next planned sections for this writing on the process and whilst leaving open to further discussion which turbine approach to the sub-system and method of operation would be the better starting point for the process following I include a little preliminary summation in relation to such aspects.

The potential turbine systems having been discussed herein being: 1) Impulse Jet - Pelton Wheel 2) Downward pointing impulse jets - rotating blade or blades 3) Reaction Turbine fo the type depicted on Fig.1.

In conjunction with choice of refrigerant fluid and method of operation.

For example: 1. R-21; impulse jet - Pelton Wheel; without BGS energy addition.

2. R-21 downward pointing impulse jets - rotating blade: with BGS energy addition underneath.

3. R-21; reaction turbine; with BGS energy addition.

4. R-21 reaction turbine without BGS energy addition.

5. R-13 higher ground pressure method of operation; impulse jet Pelton Wheel trying to sweep aside the vapour pressure.

6. R-13; higher ground pressure method of operation reaction tur bine; trying to sweep aside the vapour pressure.

7. Use of other refrigerants in the above methods, e.g. R-12, R-114, Ammonia, or any of those given in the list under Dossat, etc.

8. The additional methods of operation discussed in the following section.

It follows that in a development programme one could spend some time arriving at the better approach or approaches for particular applications. However, as starting points I would probably recommend methods 2 and 5 above at this stage, and of these, 2. Which, however, may require some fairly precise persevering and precision engineering to achieve the optimum design for the impellors of the rotating blade under the conditions of contracting fluid, which if so would be a further equal and opposite aspect,in this case as in relation to the work of Parsons on Expansion Turbines, ref: 'Power Production' by Thirring, 1956, pages 62/63.However, it should also follow that the process should be worthwhile so persevering, but perhaps method 5 would be the easier starter to get fully turned on to the probable potential for the process

in the first place:, I perhaps in contrast just involving redesigning the impellors of the Pelton Wheel in the comparatively easy manner discussed.

It also follows that the required designs of impellors could be different 4 for different operating conditions giving rise to different fluid states having different levels and rates of contraction. Therefore, it would obviously be better to determine the optimum fluid state and then design the impellors specifically for the optimum fluid state. Thus, an estimate at this stage for the likely optimum fluid state for the use of R-21 in method 2 above is compression to 100ATS and removal of heat to 1600C but in the beginning would perhaps be better to remove to 1500C.

However, 1800C may be the ultimate goal in the use of R-21 in the system for the stated reasons but alas may never be quite achievable for the stated reasons. Optimum conditions for the system based upon R-13 would probably be similar, although I would require more data than at hand at the moment to estimate more accurately.However, having recommended thus there is of course the perhaps less certain unknown at this stage of the use of a reaction turbine of the type depicted on Fig.1, which could be applied in both the above methods in the ways discussed and conceivably could potentially prove to be as good or better, not least because it.may prove easier to roduce the optimum turbine design

use ot which in tact worming the larger part or my deliberations in my earlier writing on this process. Therefore, perhaps the better starting point approach would be to set two development programmes in motion in parallel, viz: A. One dealing with both the foregoing recommended, 2 and 5, methods based upon an impulse jet approach, and B.The other dealing with same two processes based upon the reaction turbine approaches, i.e. methods 3 and 6.

In both programmes that based upon the higher ground pressure method of

operationjinitially being aimed at ships propulsion power, ana tnat based union the addition of BGS energy, i.e. with instead a partial vacuum

inside the isolation cnamber or tne sub-system,1initic.Ily Teing aimed at the creation of a stationary plant complex extracting heat from flowing waters and perhaps producing both power and cold exhaust air for output supply.Then constant ongoing reviews of the programmes to better determine the better approaches as this becomes clearer on the practical trial and error testing of the various methods, which could well include change of refrigerant and/or change of optimum conditions as well as determining the better basic systems to apply and the better design for the better systems. For example, it could become necessary to change from R-13 to some other refrigerant with a lower fluidity property but retaining some of the other desired properties to some level, albeit perhaps to a lesser level, and refrigerants in this category would for example be: R-22 of Fluidity 0.23 at 250C; N.Bpt.-40.750C; C.P.49ATS; C.T. 960C R-13B1 " 0.15 " , " -57.750C; " 39ATS; " 670C.

And on further consideration of the comparative properties probably the use of R-13B1 would be a better starting point than R-13 in the higher ground rpessure method of operation. Therefore, R-13 B1, instead perhaps. Whilst in the case of the process based upon R-21, for the use of this refrigerant in this process having as it has a Bpt. of 90C at lATS., I initially had in mind application in the warmer Countries of, for example, Africa, the Middle East, the Sub-Continent, the Far East, the Southern States of the USA., Mexico, Central America, the northern Countries of South America, the Australian Outback, etc., where the waters are at around 200C all year round and where a vast export potential exists, to satisfy crying needs in some cases.However, for the northern Countries of Europe, Canada, the Northern States of the USA and Russia, the Polar Regions, etc., then the choice of refrigerant could perhaps be one with a lower Bpt., e.g. Butane of N.Bpt + 0.40C, or R-12 of N.Bpt -300C, or Ammonia of N.Bpt -340C. Although not necessarily because if the partial vacuum technique is becoming applied and BGS energy is becoming extracted from the fluid taking its temperature down to the level of say -200C, then at such a temperature the refrigerant could become applied in the colder waters of say 50C to 100C, which would be temperatures that could still generate the vapour at lATS., or perhaps just below if generating below 90C to subtract from the nett energy balance a little by virtue fo then requiring slightly more compression energy input.Hence, perhaps one would opt for a lower Bpt refrigerant in the first place, with a further strong possibility being R-114 of N.Bpt.+3.770C. Which could in fact be the better choice of refrigerant for the warmer waters too, although not necessarily. Etc.

Therefore, to some extent it would depend upon what the development programme was being primarily aimed towards, e.g. internal or external markets or both, but perhaps one could develop a general purpose model in the first place based upon R-114 that would be suitable for most waters in the World, then become more specific for specific applications in a second phase.

With further regard to the latter, one would also have to consider whether any of the additional methods could become applied at the intended site of application of those discussed under 2 and 3 in the following section dealing with other possible methods of application.

Then one would have to consider further whether the use of Ammonia would be preferable in not being a fluorocarbon. However, my views on this question are firstly that in a process which is dependent upon its closed-cycle nature to function successfully then there should be no such worries and secondly if the fluorocarbons become excluded from use then the potential for the process could become less although the use of a fairly wide range of other fluids would still be possible, e.g.

butane.

Then in addition to the probably main heat source of natural heat in natural waters there would be the use of other heat sources to consider and probably particularly as providable via the ARC process.

Then application of the process for RainMaking purposes and Weather Control, and for refrigeration and Cold Store, to add to solely Power Production.

C. In addition, and within the overall programme, a third development programme could be set in motion in parallel based on the first method discussed following under other possible methods of operation.

Obviously a main part of such development programmes would consist of some initial experimentation to test the soundness or otherwise of the main routes to BE, the starting point main ones probably being: 1. The Partial Vacuum Technique 2. The Fluid Recycling Technique via the Air Compression Technique 3. That under 2 coupled with increase in the r parameter to reduce upon the r to the four element 4. The Mountain Technique. Which alternatively could be referred to as the Deep Water Technique if obtaining the two levels of the system in such a way and harnessing the natural heat in natural waters.

Which is a technique that could be applied in combination with all the above three techniques.

5. The Higher Ground Pressure method of operation.

6. The Fluid Stand-In Technique via electro effects, which would probably be a subsequent addition to.improve upon the application of the Partial Vacuum Technique

It follows from deliberations to date that it would probably require at least one technique to BE to be reasonably successful for the process itself to be equally reasonably successful.

Perhaps the easiest of the routes to BE to initially test for separately would be the Mountain Technique, which alone could render the process in the very viable category.

Therefore, perhaps one development programme could commence at a site with a Mountain or cliff face, (which I suppose could be a quarry face), available on site for testing for this technique, with perhaps heat provision via the ARC cycle primarily in mind although not necessarily.

And on.-therconsideration of all such aspects perhaps initially it would be better to in the first place establish one of those nice Government establishments way out in the Country somewhere where there is a nice deep river flowing rapidly through a deep gorge with high cliffs on either side and/or perhaps a waterfall, with everything being tested for under the one roof but with separate teams specialising in the separate facets of the process under discussion in the traditional British manner. A type of site where there should also be a reasonable level of humidity in the air in the summer months for testing the Rain Making Technology.

How one should progress from such a position to the Market Place with a successful process or processes having in such a way become developed will have to be a matter for further thought but it is my opinion that more higher scientists of His Excellencies quality should be prevailing at the top in Big Business. However, we all have our part to play in such a process.

The heat source in such a site could probably be via fast flowing river but perhaps it is intended to be via the ARC cycle in such a smallish application and one which would also ahve the advantage of not being at all vulnerable to the whims of Nature, whilst a smallish river could be vulnerable, either to drying up and/or freezing. If both the Mountain Technique and the Fluid Recycling via the Air Compression Technique are becoming applied then perhaps just via the BE from these two techniques there would be surplus energy at the sub-system stage to provide for the make-up energy to the ARC cycle, which are techniques that are perhaps most certain at this stage and both of which could yield appreciable quantities of BE. Then in ongoing development one could add and/or progressively improve upon the Partial Vacuum Technique.Which, however, could be added in the first instance together with cold exhaust air cooling from the Fluid Recycling Technique even if it didn't work very well in the beginning which may be the case since it would probably be a facet of the system that one would have to strive further at the practical stage to fully achieve the system's fullest potential. Then later further development here could involve the addition of an electro Fluid Stand-In Technique.As a last resort there would also be the use of gas heating to render the air expansion side of the ARC cycle isothermal and thereby the ARC cycle fully selfsustaining, but probably this would not be required with this process type on successful application of all the routes to BE. HowOvenR this would be an aspect that would become fully ascertained during the practical development stage of the first process of this particular type.

Of course, if the heat source was via the water heat in a river then there wouldn't be any energy shortfall to have to make up here in the first place.

However, an advantage of basing on the ARC is that there would be further cold to very cold exhaust air capacity, which could either become applied for more SnowMaking all year round and/or for Refrigeration for the fisheries industries and supermarket stores and shelves, etc., and for these purposes could perhaps become piped into Glasgow from the Fort William site.

A further way to make up the shortfall in the ARC cycle could in fact prove to be via the heat in natural flowing waters and obviously the application of a fast flowing river to the process in this alternative way would have advantages as well as disadvantages, viz: i) Firstly the process could still continue to function in the absence of the river water flow.

ii) A smaller quantity of water flow would probably be required.

iii) One would have the advantage of the exhaust air controll able to any temperature.

iv) The heat source would have the advantage of being free and abundant and available to anyone anywhere on the Planet with exports in mind.

v) The air expansion temperature of the ARC cycle need only be maintained at ground temperature via the water flow at the temperature of the water flow or below for the ARC cycle to probably become rendered fully self-sustaining.

vi) The method would be readily replaceable by some other form of heating, e.g. recycled waste heat from the Aluminium Smelting Process and/or gas heating, without the rest of the process becoming affected.

vii) However, there could be water freezing problems to overcome and especially if one wished cold exhaust air controlled to 'a deep freeze temperature of say 20CC, whilst cold-store at 1 or 20C could be better achieved.

However, it follows that with such industry as the Aluminium Smelting Process on site then a better way to provide a proportion of or all the heat for the ARC cycle shortfall dependant upon capacity would be via recycled waste heat from the Smelting Process and probably this is the point I'm intended to arrive at and therefore I'll curtail this discussion at this stage. Other than to remind readers that the latent heat in the exhaust vapour of the turbogenerating process would also be becoming recycled either into the air expansion of the ARC cycle or to reduce the capacity of ARC cycle required in the first place.

Therefore quite a lot of further thought on the detail of such a project coupled with detailed calculations along the lines of those I carried out under PA. 8728601 is still required here in order to best determine the better way forward in the further development of this project.

Other Possible Methods of Operation: 1. The main other method of operation that I wish to emphasis under this headir.g is that of maximising upon the heat removal from the fluid after the compression stage under the conditions of constant pressure cooling and then the use of this heat to generate turbine power in a normal turbogenerating process, with the use of this power to continuously drive the vapour compression system. To leave remaining the cold state mgh level of energy in the fluid flow for harnessing via the sub-system which would then be the power for output supply assuming the power from the turbogenerating process is sufficient to continuously drive the vapour compression system.

Basing on the data on the P-E diagram on Fig.2 herein, the latter could just be the case and perhaps especially so if the removed heat become harnessed by a turbogenerating process of the type discussed under PA 8728601 based on R-11. since via such a process the heat could become removed

and harnessed India lower temperature range. However, this is not to say that harnessing the heat via a normal steam turbogenerating process would not be equally as successful. Whilst at this stage I had intended to carry out some further detailed estimations to better determine the feasibility of this method of operation, it is another aspect of the work that I propose to leave until a later date.

2. A further method which I wish to emphasise under this heading is that of having the heat collection unit of the process under a considerable depth of water, e.g. on the sea bed with the process on the surface, since such a system arrangement would then and thereby enable one to have a considerable height of the liquid phase of the fluid acting down on the inlet side of the heat collection unit.Which would then in effect constitute a large pressure acting down on fluid in the heat collection unit on the inlet side, which in turn would enable vapourisation of the fluid to the same pressure on the exit side, which in turn would then be the starting point for the vapour compression process. whit the sub-system half of the cycle could harness the fluid pressure all the way down to normal 1 ATS. and perhaps below since it would be still possible to apply the partial vacuum technique under such a method of operation. Thus in such a method one would be obtaining BE by virtue of the compression energy input becoming reduced in comparison to the energy one could obtain via the turbine of the compressor-turbine cycle.

and perhaps more intended, to obtain the same source of

BE one could have the process on the top of a mountain/with the heat collection unit in a river valley below. When cold exhaust air from the fluid recycling system could become directly applied for Rain-Making on the appropriate and required side ofthe mountain range. If the process was at a 1000 ft., which would be very possible in such a system arrangement, then the effective pressure acting down on the inlet side of the heat collection via the liquid phase of the fluid would be equivalent to

30AT5. pressure, which could thenZbe the pressure of vapourisation of the fluid.When the vapour compression side of the cycle would then be from

30ATS. to say lO0ATS, whilst the turbine side of the cycle wouldlbe able to harness the pressure energy from l0OATS. to lATS. and below.

However, difficulties may lie in choice of a suitable fluid with the required temperature range because the 30 ATS of vapour pressure would have to become generated at the temperature of the river flow whilst harnessing the energy of such a fluid down to 1 ATS and below would result in the liquid phase on exit from the turbine of the cycle becoming at a very cold temperature in comparison and indeed necessarily so for harnessing down to 1 ATS.Otherwise vapour pressure would become generated on the exit side of the turbine and one

then be able to harness the pressure energy all the way down to 1 ATSr. However, and assuming

the above would be possible, then the1 difficulty would be one ot the very cold liquid phase freezing the water, but if a very fast flowing river then this could overcome such a difficulty. jrHowever, perhaps such an approach to BE could be combined with the R-13 Higher Pressure Range method approach to BE.

A further bonus of such a method of operation would be that one could apply the very cold liquid phase for refrigeration purposes en route to the heat collection unit below.

However, having deliberated thus on this method of operation potentially able to give rise to bonus energy it is in fact not yet fully sound because of course the vapourising vapour from the heat collection unit at the lower level of the system arrangement will be required to rise to the higher level of the system which I have been considering it may potentially be able to do under its own steam as the apt saying is.

For example, if the vapour was at lATS. and at a density less than air then the vapour should certainly be able to rise to the higher level unaided. However, in the system under discussion the latter may not be the case and if not then any energy that one had to place into the system in order to assist the rise of the vapour flow to the higher level at the rate required would subtract from the BE that one could potentially be obtaining. Thus, if energy had to be placed in at this stage in the circuit then it would be a question of whether in the nett energy balance of this cycle BE became produced. Thus considering these aspects further as follows.One could either have the vapour rise at the pressure of vapourisation, e.g. at the 30ATS. spoken of in the foregoing, or firstly one could compress to the level of 1OOATS. in the

valley. In both cases1 having 4 column of the vapour/vapour flow up to the higher level of the system. Thus, firstly imagine the former system arrangement. Then imagine the intake stroke by the compressor at the top and in-rushing vapour at 30ATS., in conjunction with vapoursation of the fluid at the bottom level.My original thinking on this was that if one first considers the piping carrying the vapour to the higher level simply as a container full of vapour at 30ATS., then one would consider that the pressure of 30ATS. would be exerting in all random directions and be exactly the same at the bottom as at the top. In which case then the pressure acting down on the vapourising fluid would be 30ATS. and be independent of the height of the column of vapour above, and if this was the case then the vapour could indeed vapourise at 30ATS. at the bottom and the rate of vapourisation would be at the rate of removal of vapour at the top by the compressor providing the heat flow into the heat collection unit was at a sufficiently fast rate and calculations show that the latter could so be.However, the vapourising vapour would of course have to travel from the bottom level to the top level up the piping, but probably the only energy required would be that required to overcome flow work which would be equivalent to around a 10% loss in the pressure in such a svstem. because the Dracti-

Cal view here could be that it would be the same as travelling /a horizontal pipe. However, a question mark on this aspect at this theoretical stage. But if so then the potential level of BE would only become reduced by the same level, i.e. by 10%. In addition, in such a system arrangement one could also be obtaining the maximum potential level of BE via the partial vacuum method and when the two BEs are added together then one could well be becoming in a just surplus energy situation at the sub-system stage to add to the output from the turbogenerating process. However, a further method of operation and aspects thereof to deliberate upon further at a later date. For example, it would probably be necessary to apply the technique of applying very cold exhaust air to the liquid at the top of the column of liquid phase and in this way help to prevent fluid vapourisation off the surface of the column of liquid phase.To then enable the depressurisation to take place to lATS. and below, even though the liquid may otherwise be exiting at a temperature which would have a higher saturated vapour pressure associated and acting on the exit side of the turbine in the use of a fluid such as R-13 which would have to undergo cooling to -800C in the sub-system just to achieve a SVP of lATS. in the isolation chamber of the system.

Continuing on parts of the foregoingthinking,a further concept will be one of Rivermaking on suitable Mountains where hot humid air rises up over the Mountain range from the seaside but as it contacts the cold air over the Mountain may only become partially condensed to cloud formation.

However, if one is on top of the Mountain with a process combined with the ARC then one could fully precipitate the water vapour in the air and cause it to run down the other side of the Mountain as small streams which would then combine together in the valley below to form a river meandering through the valley where there was no river or perhaps a dried up river or the streams may form a lake in the valley below which that is perhaps more likely and which could be kept permanently topped up in such a way whilst using the accompanying power production to pump the water in the lake further afield as desired and as required, all on thin air. With permanent Rainbows on the Mountainside taboo. A bonus then being that one could thereby also reduce rainy weather along the valley.Then similarly for snow and the creation of Ski slopes coupled with the storage of water via such means.

3. A further idea then being that one could in fact apply the Mountain to give a potential head of the liquid phase of the fluid after it exits from the sub-system and harness the energy of the potential head in the valley below before then passing through the heat collection unit to revapourise and rise up to the top of the Mountain once again, which it should be capable of doing under its own steam either as vapourised, i.e.

at the pressure of vapourisation, or after compression to 100AT5. This would be the source of this Bonus Energy, i.e. if the energy one acquired from the potential head of the liquid phase on the downside was substantially more than any extra energy input required to raise the vapour phase to the top of the Mountain once again for the next cycle. Assuming the vapour on vapourisation was at lATS., as it could be in the use of R-21 in such a system, then perhaps one would have to place a pump on the vapour line in order to get the vapour to the top of the Mountain at the rate required, but I think the pumping energy required could be less than the potential energy of the liquid phase head. Then from this concept several other potential possibilities spring to my mind.

However, a potential head height equivalent to 1OOATS. would only give

the 1OKJs level of energy,, and such a height for R-21 liquid phase would be around 3000 ft. Therefore, in the process under discussion probably the use of the liquid phase potential head to give the system as described in relation to8-13 could give rise to substantially higher levels of Bonus Energy, i.e. as the system described under 2 in the foregoing.

General Discussion: Thus, the foregoing sums up most of the basics on the process under aiscussion, all of which could be Much Ado About Nothing. Certainly it is probable that one may only just be able to render the Compressor Sub-system cycle fully self-sustaining after application of all the various techniques to BE in combination. Therefore, in one sense one could say much ado about nothing with regard to this system. However, the point being that if the sub-system cycle can be rendered fully selfsustaining then the main process becomes very possible, which if only yielding 20KJs of energy for every 200KJs of fresh heat absorbed each cycle will still be very worth while as the work under the following section will show.Which, however, basis on somewhat higher energy yields in relation to the fresh heat input bearing in mind that the latent heat from the turbogenerating process can readily become recycled as absorbed heat each cycle. Thus, the work under the following section basis on two levels, i.e. 1KJ output for every 7 KJs and 3.5 KJs of freshly absorbed heat, i.e. 14% and 28% efficiency in relation to the freshly absorbed heat each cycle respectively, and considers that the 28% level of efficiency will be that achieved when the compressor - subsystem cycle is rendered just self-sustaining.

When the process would then certainly not be much ado about nothing nor one that disappears to nothing in ever decreasing cycles, as the work

under the following section willlshow where the potential tor the process and the compressor - sub-system becomes further explored.

Thus, at such levels of efficiency it will be possible to harness the low grade heat of the Planet contained in abundance in the sea; in the rivers; in the Earth; on the Earth; in the air; in near and far space; on the Moon; on the Planets, which hitherto would not be as possible and all importantly in the context of business, not as cheaply, viably,and reliably, although the present methods to harness solar radiation via solar cells goes some way towares achieving such objectives, Hnwver. I hone to show under the following section that the way for

the human race to achieve such a goal ould1be better, via tne method being discussed herein

Furthermore, on the advent of the Nuclear Power Age there was much talk about the start of a Golden Age, which however in the event hasn't really come to pass as based upon Nuclear Power. However, such raised hopes can now probably stay raised since in my personal view the process discussed herein has the potential to be the basis for such an Age, as I hope to show under the following section. But in contrast the Golden Age that I have in my mind is really the creation of a Walt Disney type of World ae probably possible to be achieved based upon all the processes and systems that I have evolved. However, probably the process under discussion would be the founding basis for such an Age, with the other processes and systems then creating all the surrounding superstructure of the Walt Disney civilisation founded upon the process.

This now being my view, notwithstanding the work under preceding Patent Applications Nos. 8720291 and 8728601 which could perhaps similarly form the basis for such an Age but in my view now not as well. Although of course those processes would be a part of the foundation and the superstructure of the Age but probably not the central basis of the foundation which I think would be formed more so by the process under discussion.

At this stage, the main source of heat for the process that I have had in mind is that of natural heat in natural flowing waters, 9.g. rivers, and the tidal flows of the seas and oceans. And particularly tidal flows for very large scale production of power on the Planet. However, this then progresses onto the concept of Power Ships, as becomes discussed in the following section, and it will probably be debatable which would be the better approach at the outset although in the beginning of such an Age perhaps one would still base on fixed processes with the tidal waters flowing through, but not necessarily.However, to a large extent the approach and to what extent would depend upon the success or otherwise of initial prototype models, but one can envisage that one could progress with the practical implementation of the work very rapidly in the way that the Nuclear Age became established but this time really leading to the creation then of a truly Golden Age without end in which free and abundant power would be available to anyone any

where on the Planet night and day, forever and a day, which would 1give rise toal? pollution and via which one could control the weather and the temperature of the Planet, which I think are intended advancements within the infrastructure of our Civilisations on the Planet and in keeping with Mankind taking the reins and control of His destiny. In any event, this may be an aspect that will necessarily have to be carried out in the near future in view of the climatic changes that are reported to be taking place at the present time, and probably it is not coincidence that I am coinciding with such ailments of Nature as the counteracting force to make Nature better once again and in the process found a truly Golden Age leading to the creation of a World

Whilst the natural heat contained in~ natural waters would probably be the main source of heat for the process, there would of course be other sources but perhaps not with the same potential for very large scale power production.However among other sources for large scale production would be the idea of Solar Ponds, some details of which can be found in the paper entitled 'A Solar Pond Power Plant' by Yehuda L.Bronicki, of Ormat Turbines Ltd., Yavne, Israel, IEEE? Spectrum 1981, The advantage of such a concept linked to the process under discussion over theirexisting application would be that the steady state heat temperature level could be lower whilst achieving maximised heat conversion efficiency because7of course,the collected heat would subsequently become upgraded to the optimum temperature via the compressor-sub-system cycle. Which in fact would be one way to view the process, i.e. a system comprised of the compressor-sub-system cycle which is able to upgrade low grade heat in order that it can become harnessed via a turbogenerating process.

However, it follows that perhaps one needn't go to the lengths of solar pond construction since this process could equally well collect direct solar radiation via direct absorption into pipes carrying the heat absorbing, vapourising,refrigerant. Thus one can envisage the pipes simply laid side by side on the desert sand of appropriate black body, heat absorbing, finish and material, e.g. large copper piping painted matt black.

Then a further way would be to bury the pipes in the sand a little beneath the surface, and in connection with such an approach I refer readers to the paper entitled 'Deep Ground Coil Evaporators for Heat Pumps', Applied Energy, 1978, by J.R. Goulburn and J. Fearon, of Queens University, Belfast.

However, such approaches could be fairly limited in capacity potential in comparison to the method via the natural heat contained in natural flowing waters but a further and comparable large scale heat source could be via linking to the ARC cycle, which could in fact become one of the main ways to produce very cold exhaust air in the process for large scale Rain-Making and weather control in the way that finally becomes evolved in the following section and involving the addition of a MAC Heat Processor, i.e. Multi Air Compression Heat Processor, by ever increasing

number or stages/ror ever increasing very cold exhaust air and accompanying power production.The intended inference being that perhaps via natural flowing waters would be the way to principal( power, and via the ARC cycle would be the way to primarily very cold exhaust air for Rain Making which alone could be quite lucrative but obviously better if the process also yielded some remaining surplus power for use beyond the process. However, large scale Rain-Making capacity could also be achieved via the heat source of natural waters, which however may not be as convenient for use in the interior of deserts, when one can envisage that one could commence a plant complex in the centre of a desert based upon air compression and then add increasing stages for increasing production and development of the desert all around, perhaps from the fairly small beginnings of an Oasis Development in the centre of the desert in the first place.

However, having envisaged thus perhaps the basic way to such development will still be via pumping water and desalinating if and when required, but obviously this will depend upon how successful the Rain-Making technology turns out to be in the fullness of time. And obviously one good approach to this technology will be via the development of Rain New Towns along the coastlines of appropriate Countries, as discussed under PA 8728601.

Additionally, in the ensuing a method of desalinisation becomes evolved in which all the heats of compressions from the Process as linked to an ARC cycle and MAC Heat Processor first becomes used to boil water for the production of steam which then becomes condensed for the production of pure water, with the heat of condensation then being that which is applied in the next stage of the process rather than the heat of compression. Which however could still be the same amount of heat but in the process having raised and condensed steam en route of the heat to the next stage in the process. Thus, in the fullness of time this could become a main way to apply the process to give a Big D, Big R and probably Big P capacity via the one Plant complex.However, now progressing on to the next section in which I explore in more detail the potential for the process with in mind the view that perhaps the process could become the central foundation for a new Golden Age to be as but replacugthe Nuclear Power foundation in this respect and perhaps in a better way than could be achieved just via the other processes of the whole work under evolution.

PROCESS CONCEPTS - THE POTENTIAL: These cover the following potential processes and concepts: 1. Harnessing the heat of natural flowing waters via: Tidal Plants Sea Plants River Plants 2. Mill Plants 3. Power Bridges 4. Ships Propulsion Power 5. Power Ships 6. Air Passage Heat harnessing for Road, Rail, Sky and Aircraft propulsion power 7. Solar Pond Plants 8. Direct Solar Earth Plants 9. Direct Solar Space Plants 10. Concentrated Solar Plants 11. Moon Plants 12. Space Craft Solar Plants.

13. The Process combined with the ARC Cycle to give the following Earth Plants A. Power PlantsfA.P. Plant B. Rain Making, Refrigeration and Cold Store Plant. A RR & CS Plant.

C. Power, Rain Making, Refrigeration and Cold Store Plant A PRR & CS Plant D. Power, Rain Making, Refrigeration, Cold Store and Desalinisation Plant.

A PRR, CS and Big D Plant.

14. Similar Plants to those under 13 via other heat sources, mainly natural water heat.

15. Grount Heat Plants 16. Wind Heat Plants 17. Static Air Plant 18. Static Water Plant 19. Water Pump Plant.

Not necessarily discussed in the order listed, and not all discussed in any detail at this more general stage 1. Process to harness the natural heat contained in natural flowing waters Probably the main process at this stage.

Fig. 4.

To illustrate the concept and potential for this process I have carried out a schematic diagram on Fig. 4 illustrating a simple floating platform, 1, concept moored in natural flowing waters, 2, with the heat collector unit, 3, fixed to the underside of the platform and submerged in the water flow below, and the process equipment required for converting the collected low grade into high grade usable energy on the topside of the floating platform. Which I will refer to in the 'further discussion of the process but obviously probably the main way of applying this process to harness the heat contained in the natural flowing waters on the Planet could be via fixed structures in the fullness of time.

However, the floating platform approach would be a good starting point for a prototype model and development of the process. Moreover, it would be a convenient operation to be able to construct such process types in the ship and oil rig yards back at base then simply float them to all corners of the Planet to desired sites, having a sea cruise in the bargain for one's endeavours.

Thus, as implied it is considered that the process could be applied for very large scale production of power and therefore I intend to carry out a process concept for a 1000 Mater capacity plant in relation to the floating platform model, but perhaps such large capacity plant would be fixed structures in practice with floating platform models up to lesser capacities, e.g., of the order of lKW to 100 MWh. However, the following model will demonstrate how feasible very large scale power production would be via the process as well as demonstrating the moored platform concept and potential.

Process Model - 1000 Mhr Plant For the cycle of the process basing on that depicted on Fig. 2. and assuming that the turbogenerating plant of the process is achieving the normal level of 40% one pass heat conversion efficiency for the heat becoming removed between stages D to E of the cycle. Then for two views of this particular process assuming : - (i) That the subsequent energy yield from the sub-system of the process i.e., that from E to A of the energy cycle, is just sufficient to sustain the compression energy input requirement of the compressor stage, i.e., that required for stage B/C to D. To leave remaining all the power yield from the turbogenerating plant of the process for output supply.

ii) That half the energy yield from the turbogenerating plant of the process has to become used internally to make up a short fall in the energy required for the compressor. To leave remaining half the power output from the turbogenerating plant of the process for output supply.

Then for the purposes of the models basing on a speed of 5 mph for the natural flowing waters. Which however, would probably be more the speed of prime sites where there is a particular fast flow or current of flowing waters, and obviously it would be this type of site that one would preferably select if available.However, more general speeds more simply associated with the general flow of the sea are of the order of 1 mph and therefore for application in such sites the process bulk in relation to the submerged heat collection unit would probably have to be five times larger than becomes estimated following for the more specicific conditions being considered, but it follows that by simply increasing on the dimensions of the submerged heat collection unit it should be possible to apply the process almost anywhere in any sea or ocean and perhaps especially in and amongst islands and along fiordal type coasts where the tidal flows of the seas tend to flow faster between closer land masses. And therefore. some data is included followinq to

demonstrate such a potential for the process.However, ? returning to the more specific model under discussion, as follows.

(i) Firstly considering the model in which the sub-system just sustains the compressor.

A Plant having a 1000 MWhr output from the turbogenerating part of the process at a 40% one pass heat conversion efficiency level and where the sub-system energy yield is just sustaining the compressor stage would be required to absorb the following amount of heat in the submerged heat collection unit, 3, basing on the energy cycle depicted on Fig. 2.

On that cycle the amount of absorbed heat from A to B/C is approximately 240 KJ/KG of R-21.

Whilst the total amount of heat removed from stages D to E is approximately 133 KJ/KG of R-21. Which if converted at an efficiency level of 40% would yeild approximately 50 KJ/KG of R-21 for external supply.

Therefore, for such a cycle the ratio of absorbed heat, i.e., collected low grade heat from the natural flowing waters, will be 240 KJ/KG to 50 KJ/KG, i.e., in a ratio of approximately 5 to 1. However, whilst perhaps not necessary in this particular application the process would invariably become operated with the latent heat of condensation from the turbogenerating stage of the process becoming recycled via absorbtion into the refrigerant prior to becoming piped through the main part of the heat collection unit. Which if 60% of the 133 KJ/KG would be 80 KJ/KG and at 80% recycling efficiency 65 KJ/KG. Which when subtracted from the level of 240 KJ/KG would leave 175 KJ/KG of fresh heat input to become absorbed by the heat collection unit submerged in the water flow.

Therefore, if the output supply from the Plant is required to be 1000 MWhr then the heat collection unit would have to absorb an amount of heat in the ratio 175 to 50 KJ/KG, i.e., the equivalent of 3500 MWhr of heat from the natural flowing water and such a Plant would have a 20% output efficiency level with respect to the total amount of heat being absorbed each cycle and 28% in relation to the fresh heat input, which of course is the more meaningful efficiency value of the process.

3500 MWhr = 3500,000 KWhr 1 KWhr = 1 KJ/second Therefore the heat collection unit would be required to collect and deliver the absorbed heat at a rate of 3500,000 KJ per second.

Therefore it is now a question of determining what size the heat collection unit would have to be to collect such an amount of heat from the flowing waters flowing past the heat collection unit at a speed of 5 mph.

The way that I propose to approach this estimation calculation is to first assume that the heat collection unit will extract 5 C of heat from the flowing waters as the water flows through an open bank of pipework of appropriate design and arrangement comprising the heat collection unit from front to rear, and that every 10 ft long section of the unit will extract 0,250C of the total of 50C of heat each successive lOft section of the submerged unit. Which, when basing on feasible heat collection unit designs and the thermal conductivity through pipework, should be very feasible and a very feasible rate of heat extraction for water flowing through the unit at 5 mph.Even though the pipework arrangement carrying the heat absorbing refrigerant,

probably

comprised of pipework arranged in either the length or cross direction of the water flow although not necessarily, would have to be fairly open and probably quite a lot of attention would have to be paid in design to achieving smooth fluid flow through the arrangement of pipework in order to enable the water flow to flow in a fairly unrestricted fashion through the heat collection unit.

The reason for basing on a 50C temperature drop over 200 ft. (61M) of heat collection unit firstly being that such a rate and quantity of heat extraction should be very feasible over such a longish length of heat exchange unit, as following calculations will show for present day materials, even if the arrangement of the pipework has to be very open, and especially so due to the fact that the refrigerant running through the heat exchange pipework will not increase in temperature on absorbing heat but will simply absorb heat into its latent heat energy mode and gradually change phase from a liquid to a vapour whilst still remaining at the initial low temperature of entry.Which however in the case of the use of R-21 will be quite high for some waters at 9 C although if only 50C is being extracted from the waters then they could be at a temperature of 14-15 C. However, British waters for example can become appreciably colder down to temperatures of the order of 50C minimum in colder wintertimes, although in summer they can be higher than 15 C. Nonetheless for such waters then the process may have to be based upon a lower Bpt refrigerant such as R-114 of Bpt 3.770C, or Butane of Bpt. 0.40C. A useful table of current refrigerants and their Bpts can be found in the text book 'Principles of Refrigeration' by Roy. J. Dossat pages 380-2.

Thus it follows that the use of Butane may be ideal for British Waters since it would just avoid freezing the water itself whilst having as a low a Bpt as possible, and probably sufficiently low to enable 50C heat extraction all year round from many natural flowing water sites in and around Britain. Moreover it is feasible that if the water flow is sufficiently rapid then refrigerants with lower Bpts below OOC could be applied whilst still avoiding freezing of the water flow. But to override all such considerations with respect to choice of refrigerant at least could be the fact that it may be possible to devise a process in which one can have sensitive control, perhaps in an ongoing manner, over the temperature of the liquid phase after the subsystem stage via control over the vapour pressure above the liquid phase.

Conceivably over a range in the use of any refrigerant making it possible to select from a choice and not necessarily as dictated by the temperature of the heat source, which obviously would also be very advantageous if one wished to use the process in different waters of different temperatures, e.g, as would be desirable for Ships, and/or where the waters range in temperature throughout the course of a year.From temperatures associated with pressures below 1 ATS., e.g., as on the application of the partial vacuum technique, which could then render the use of R-21 possible in the colder waters in and around Britain, to temperatures associated with saturated vapour pressures above 1 ATS. which could then render the lower Bpt. refrigerants possible because such a method of operation could bring the liquid phase temperature up closer to 0 C and as required to be as low as possible whilst avoiding freezing the water itself. Thus perhaps one could select the best refrigerant from the point of view of the operation of the sub-system and then control the liquid phase temperature as required in such ways.

Thus, the second reason for basing on 50C temperature extraction being that such a level of extraction should be within the range of both the process and most potential water flow sites.

However, the waters around Africa, India and the Middle East for example and to name but a few places on the Planet, are all year round around 200C and above, and it is application in such waters that I have mainly had in mind when basing the process on R-21, where the skies are blue and sunny and the shores are sandy and golden all year round too. Thus for such waters then the use of R-21 in the process would be very feasible and probably ideal, and the removal of just 50C from the water would be well within the range of the refrigerant at the normal 1 ATS. ground state pressure method of operation, and indeed would represent but a drop in the ocean, as far as removing heat from the sea is concerned, as the following estimations will show.

Thus it follows that for such a rate of heat extraction and total quantity of heat extracted, i.e., that represented by 50C, then the total length of

the heat collection unit would be just 200 ft (61M) and any/every part of the water flowing from front to rear of the unit at a speed of 5 mph would pass through a distance of 7.3ft of the unit in 1 second and take 27 seconds to emerge from the rear of the unit and then go on its way with the remainder of the water flow, initially 50C less in temperature than when it entered the unit and than the surrounding water flow. But the waters would soon blend and the Sun would be beating down on the waters all day long during the day.Moreover a probable slight reduction in water vapour vapourisation from off the subsequent surface of the slightly colder surface water could itself compensate for the heat loss, and render the climate slightly less clammy and more bearable in the process.

Thus, if the flow of water is flowing through the unit at a speed of 7.3 ft every second and the unit absorbs 0.250C of heat every 10 ft section of flow through the unit, then 1 second of flow will transfer 0.183 C every 7.3 ft section of the unit. And by the time the water flow has flowed through 27 of such sections then it will have become cooled by 0.183 x 27 = 50C, and therefore if initially entering at 200C then it will exit at 150C and remember the refrigerant temperature would be remaining at the temperature of 9 C if and as associated with a normal pressure of 1 ATS. existing above both sides of the liquid phase, which should be a method of operation readily achievable. Therefore a good temperature gradient would be maintained throughout this heat exchange operation of the process.But of course for' even absorption of heat along the whole unit then some method would have to be applied in order to achieve this because heat would flow down a temperature gradient of 200C to 90C at around twice the speed it would flow down a gradient of 150C to 90C and, therefore, although one could have such a changing rate of heat flow, for the purposes of the following description it will be assumed a method is being applied to even out the flow rate, e.g., perhaps through appropriate reduction in the thickness of the walls of the pipework carrying the heat absorbing refrigerant.

Basing on the preceding estimated values the total amount of heat required to be absorbed will be: 3,500,000 KJ/second And, therefore, the amount of heat that is required to be absorbed by the first 7.3ft section of the unit in one second will be: 3,500,000 x 7.3 = 127,750 KJ/second 200 Meanwhile in each of the following 26 successive 7.3 ft sections of the unit the collection unit will be absorbing the same amount of heat each second to give the total of 3,500,000 KJ/second, albeit the water flow itself cooling from 200C to 150C as it flows through the unit but assuming the absorption rate has been evened out in some way and remember the absorbing refriqerant

in the pipework of the unit will at 9 OC throughout.

Therefore, now it is a question of determining what the width and depth the heat collection unit would have to be submerged in the flowing waters in order to be able to absorb such a quantity of heat for a 1000 MWhr output Plant. As follows:1 calorie of heat is contained in l0C of 1 gram of water.

Therefore:4.18 Joules of heat are contained in 10C of 1 gram of water 453 grams = llb 1 cubic foot of water weighs 62.3 lbs Therefore:1 cubic foot of flowing water will contain: 62.3 x 453 x 4.18 = 118KJ per 1 C of heat contained therein.

Therefore, every 1 cubic foot of water flowing through the first 7.3 ft of the unit in 1 second will transfer: 0.183 C x 118KJ = 21.6KJ Whilst at the same time in the same second exactly the same will be taking place in the following 26 x 7.3 ft sections of the unit, albeit the water itself gradually cooling.

Therefore, for the total requirement of 127,750 KJ to become absorbed in the first 7.3 ft section of the unit, there will be required to flow through this length the following total number of cubic feet of water: 127,750KJ = 21.6 KJ 5914 cubic feet If one then divides this volume quantity by the length dimension then one would obtain the width x depth dimension, which would be: 5914 57934 = 810 square feet.

If one then opts for a depth of 20ft for the submerged unit in the flowing waters then the width of the unit would have to be: just 40ft All of which seems somewhat incredible and all too ridiculous for a 1000 MWhr Plant requiring a submerged volume space of just: 200 ft long 40 ft wide 20 ft deep Submerged in flowing waters and only removing 5 C from the drop of water flowing through the unit. Not even the size of a Supertanker and if expressed in metres seems even more incredible, i.e., 61 Metres long 12.2 Metres wide 6.1 Metres deep Therefore, have I made a mistake. Perhaps I should have calculated with another 7.3 ft section on the end of the unit, which however would make very little difference but perhaps it would be better to base on 1 foot of flow, as follows and to cross check.

1 foot of flow will take 1/7.3 seconds The total amount of heat required to be exchanged in 1/7.3 seconds will be: 3,500,000 = 479452 KJs 7.3 Therefore every one foot of flow will be required to transfer the following amount of heat: 479452 200 = 2397 KJS But in flowing through just 1 foot of flow then the temperature exchanged per 1 foot unit will be: 5 0 250 = 0.025 C Which will represent a quantity of heat, as follows: 62.3 x 453 x 4.18 x 0.025 = 2.95 KJs Therefore there will be required to flow through each 1 ft section of the unit in 1/7.3 seconds the following volume of water: 2397 = 812 cubic feet 2.95 Since the length dimension will be 1 foot then the area of the width x depth of the volume of water will be:: 812 = 812 square feet If one then opts for a depth of 20 ft then the width of the unit will be required to be: just 40 feet Thus the calculation would seem correct. Therefore, I will progress on the discussion with these dimensions in mind, whilst still being somewhat amazed and so much so that I would wish for someone to check through this work because of course I have been known to be wrong in the past, albeit moreso in the beginning of the evolution of processes and systems.

Returning to the view of 27 x 7.3 ft sections of the system in 1 second of flow It will of course be the case that every drop of water, say each 1 gram drop, will be required to lose the heat, which for a 7.3 ft section of the unit and for the flow of just 1 gm of water along the section taking just 1 second will be the heat associated with the loss of just 0.1830C from the water from say 200C to 19.817 C, i.e., just 0.765 Joules of heat per gram drop.

Which is an infinitesimal amount of heat compared with the total quantity becoming transferred, but in terms of heat exchange units would represent quite a large infinitesimal drop of the water flow at 1 full cubic centimetre.

Therefore, even if the pipework arrangement had to be quite open to enable unrestricted flow one would expect there nonetheless to be some appreciable direct contact between pipework and water flow, with good heat conduction through the remainder down large temperature gradients. To at least give the infinitesimal heat transference on average throughout the mass of the water flow.Then an even more realistic and feasible view is obtained if one considers that all each drop of water has to lose is 50C of temperature on flowing through the full 200ft of the heat exchange collection unit, and as long as the average temperature in the water flowing out of the unit is 50C less than its initial temperature on entry after flowing through 200 ft of a unit at a constant temperature some 10 C less and wherein is present an absorbing substance that will literally suck the heat into itself, then the required quantity of heat must have become transferred to the refrigerant even if there is some variation in the rate and quanitity of heat transference from each gram drop of the flowing water.

However, thereisprobably an error so far and that is that some of the natural water flow would become pushed around the sides of the unit and wouldn't all be able to flow through the unit. If by the full amount the volume of the pipework carrying the refrigerant occupies then perhaps only half the volume of water would be able to flow through the unit, which would then render it a 500 MWhr Plant. Or conversely, if the unit was just twice as wide or twice as deep then it would become a 1000 MWr Plant once again.

Thus it follows that the pipework carrying the refrigerant could occupy a full half of the volume of the heat collection unit and the dimensions for a 1000 MWhr could become just: 1000 MWhr:- 61 Metres long 24 Metres wide 6.1 Metres deep.

After allowing for half the water flow volume becoming pushed around the sides of the unit and/or to and out of the sides of the unit during flow, etc.

Moreover, it follows that for a 2000 Mh'hr Plant the dimensions would simply have to be doubled again to: 2000 MWhr:- 61 Metres long 48 Metres wide 6.1 Metres deep.

Then if too deep for the available depth of waters one could simply double the width and halve the depth for the same capacity process. Or conversely, one could keep the width the same as for the 1000 MWhr Plant and double the depth. Or a combination of both, as found suitable for the particular flow of water.

Thus, obviously at this pre practical stage it would be more realistic to base on half the volume occupied by the submerged heat collection unit becoming occupied by the pipework arrangement carrying the refrigerant in turn causing an accompanying reduction in the effective water volume flow to a half. To which the above, later, dimensions would then apply.

It follows therefore that a 4000 MWhr Plant could require just the following dimensions with respect to the submerged heat collection unit: 4000 :- - 61 Metres long in the direction of flow 50 Metres wide across the flow 12 Metres deep.

After doubling the volume to allow for the effects of the heat collecting pipework.

And obviously there would be room above to house the Plant required to convert the collected heat.

However there may not be many sites where one could plant such a large unit in such fast flowing waters, and for rnany sites then it would probably be better to think in terms of quartering rather than quadrupling to say 250 MWhr Plants if in busy estuaries on the one hand, or if in narrowish rivers on the other.When the dimensions would become the following on allowing for half the water volume flow becoming pushed to the side of the unit: 250 MWhr:- 61 Metres long in the direction of river flow 6 Metres wide 6.1 Metres deep Or, if too deep then: 61 Metres long 8.1 Metres wide 4.5 Metres deep Whilst for the larger capacity Plants one could think in terms of 1 mph

riowing water1 sites, rive times tne aimension in eitner tne width or aeptn dimension, or between the two dimensions, but also then in terms of the vaster expanse of the seas between offshore islands and the like. For example between the Isle of Wight and the Mainland.When much of the extra volume could probably be in the depth direction, perhaps even forming part of the support for a bridge from mainland to island all the way to the sea bed.

This then being the basis for the concept being referred to as a Power Bridge. Other similar sites for similar idea consideration being across the Channel from Dover to Calais and from Mull of Kintyre to Northern Ireland less than just 15 miles, which is a Power Bridge site that could provide much of the power requirements for Northern Ireland and the West Coast as well as giving the benefits of a bridge. Moreover, such Power Bridges could have wind generators blade tip to blade tip all the way along each side of the exposed part of the bridge to break the wind and protect the bridge, as well as adding to the Power output of the Power Bridge. Stood off from the sides of the bridge on shafts as found required to achieve optimum wind breaking and power production.Basing on the premise that if the power of the wind is given to the wind generator then it must produce power and couldn't then go on to damage the very long bridge.

However, lowering ambitions and horizons somewhat and considering the heat collection dimension requirement for a 4000 MWhr Plant for just a 1mph flowing water site, again basing on double the volume for half the volume of flow available, as follows: 4000 MWhr/lmph flowing water site: Since such sites could be way out to sea in comparison then the units could be much deeper in the depth dimension to achieve the fives times volume require :ment.Therefore the dimensions could be: 4000 MWh:- 61 Metres in the direction of flow 60 Metres in the width direction 50 Metres in the depth direction In comparison I note from the Guardian report 24 March 1988 that 25err100 ft high wind generator turbines capable of just 7.5 to 12.5 MWhr would occupy rather more than 1 square mile of space and that output comparable with Sizewell B power station as above would require a land area of some 200 square miles.

Whilst the above sea site would perhaps also be comparable with the land area occupied by Sizewell B nuclear power plant

of course would have the advantage in operating on an infinitely renewable, infinitely abundant, infinitely free, infinitely constant, infinitely reliable, and relatively safe in use heat source. Available to anyone anywhere on the Plant within the limitations of the heat source but remember the above estimation relates to 1 mph sea flows, which should be generally available in most seas close in to a Country's coast line.

Then an advantage of such a relatively small site off shore for such a relatively large quantity of power production will be that the increased cost of an off shore operation would not in fact be that high, with the added bonus of and necessity for saving the land on such a small island as Britain for example.

While sites further afield could be in the Bab al Mandab passage at the foot of the Red Sea a between Djibouti and the Arab States of the Yemen, which could perhaps be an ideal site for the process under discussion based upon R-21 since the water there will be around 200C all year round and the flow speed of the water through this passage could well be in excess of 1 mph for most of the time.

Of course probably all sea sites and estuary sites will be comprised of a flow in one directionfior half the time and then flow in the exact opposite direction for the other half of the time and in this respect such sites wouldn't be constant and especially at the time of the turn around of the direction of flow. However, the flow speeds, directions of flow and turn around times are now fully recorded for most seas and estuaries, and in this respect they would be constant and reliable sites. And of course the advantage of the heat collection unit would be that it could easily be designed for and be very conducive to water flowing through in both directions in an alternating manner.Thus it is a convenient and apt stage in the discussion to pursue this aspect further and include some data on the general speeds of some general sea flows around the coast of Britain.

Bearing in mind that we would like at least 1 mph' as constant and as reliable as possible. However since 1 mph is approximately 1.5 ft per second then perhaps a desirable minimum could be regarded as lft per sec, i.e., 0.68 mph.

The following data has been compiled from Admiralty Tidal Stream Charts.

1. Tidal flow rates between Mull of Kintyre and Northern Ireland Repeating over a 12 hour Period of 2 x 6 hourly alternating tidal flows: Mean Neap Rate Mean Spring Rate South Easterly Direction 1 hr 50 m before HW Ullapool 0.8 mph 1.5 mph 50 m 2.3 mph 4.14 mph 10 m after gN Ullapool 2.88 mph 5.18 mph 1 hr 10 m 2.76 mph 4.95 mph 2hr lOm 2.1 mph 3.8 mph 3hr lOm 0.92 mph 1.73 mph North Westerly Direction 4hr lOm after HW Ullapool 0.46 mph 0.91 mph 5hr lOm 1.84 mph 3.33 mph 6hr 15m before HW Ullapool 2.65 mph 4.95 mph 5hr 15m 3.00 mph 5.3 mph 4hr 15m 2.5 mph 4.48 mph 3hr 15m 1.38 mph 2.53 mph South Easterly Direction 2hr 15m before HW Ullapool 0.23 mph 0.46 mph lhr 50m Repeating Repeating Thus it can be seen that for the slow neap tidal flows the sea flow rate will be over 2mph for good 3 hour periods in the mid of each of the 6 hour alternating tide periods reaching a maximum of around 3mph in each tide period, but reduces to a minimum of 0.46 mph on the turn around from a south-easterly to a northwesterly direction and to a further minimum of 0.23 mph on the turn around back from a north-westerly to a south-easterly direction.

While for the fast spring tide it can be seen that the sea flow rate speeds will ; be approximately twice as fast throughout.

Thus while the neap tidal flows should be satisfactory the faster spring tide flow rates would obviously be better. However, there is quite a variation throughout, albeit it will probably be a fairly constant and fairly predictable variation day in day out, year in year out, century in century out. But it follows that such a source of heat for the power generating process would be best geared to a national grid system of electricity provision.

2. English Channel Midway between Dover and Calais Repeating over a 12 hour period of 2 x 6 hourly alternating tidal flows: Mean Neap Rate Mean Spring Rate South-Westerly Direction 6 hr before HW Dover 1.27 mph 2.3 mph 5hr 1.96 mph 3.45 mph 4hr 2.07 mph 3.8 mph 3hr 1.84 mph 3.22 mph 2hr 0.8 mph 1.5 mph North-Easterly Direction lhr before HW Dover 0.69 mph 1.15 mph High Water Dover 1.27 mph 2.18 mph lhr after HW Dover 1.96 mph 3.45 mph 2hr after HW Dover 1.96 mph 3.56 mph 3hr after HW Dover 1.49 mph 2.76 mph 4hr after HW Dover 0.8 mph 1.38 mph South-Westerly Direction' 5hr after HW Dover 0.46 mph 0.92 mph 6hr after HW Dover 0.92 mph 1.61 mph In this case it can be seen that for the slow neap tidal flow the sea flow rate will be from 1 mph reaching to a maximum of 2mph for most of the time in each of the two 6 hourly alternating tidal flow periods, but reducing to a minimum of 0.69 mph over a two hour period on the turn around from a south-westerly to a north-easterly direction, and to a further minimum of 0.46 mph over a similar 2 hr period on the turn around back from a north-easterly to a south-westerly direction. While the spring tidal flow rates will again be approximately twice as fast throughout.

Thus, while the overall tidal flow rates for this site are approximately three quarters of the corresponding tidal flows for the preceding site between Mull of Kintyre and Northern Ireland throughout, there could be less variation between maxima and minima and therefore more constancy through longer periods, and therefore perhaps there would also be more predictability. Although in contrast the chart for this site does indicate quite a degree of variation across the Channel, but for any specific site the above could apply.

3. Off Great Yarmouth Repeating over a 12 hour period of 2 x 6 hourly alternating tidal flows: Mean Neap Rate Mean Spring Rate Southerly Direction 6hr before HW Dover Turn around with very little flow 5hr 1.5 mph 2.65 mph 4hr 2.18 mph 3.9 mph 3hr 1.84 mph 3.22 mph 2hr 1.38 mph 2.53 mph lhr 0.8 mph 1.38 mph High Water Dover Turn around with very little flow lhr after HW Dover 0.8 mph 1.5 mph 2hr 1.84 mph 3.22 mph 3hr 1.95 mph 3.45 mph 4hr 1.72 mph 3.1 mph Shr 1.0 mph 1.84 mph 6hr Turn around with very little flow Again quite a degree of constancy over 4 hour periods in each of the 6 hourly tidal flows.

4. Off the Cote de la Hague Repeating over a 12 hour period of 2 x 6 hourly alternating tidal flows: Mean Neap Rate Mean Spring Rate North-Easterly Direction 6hr before HW Dover 1.5 mph 3.7 mph 5hr 2.5 mph 6.21 mph 4hr ' 4.6 mph 11.15 mph 3hr 4.25 mph 10.35 mph 2hr 3.45 mph 8.3 mph lhr 0.92 mph 2.3 mph South-Westerly Direction High Water Dover 1.15 mph 2.88 mph lhr after H-N Dover 1.5 mph 3.56 mph 2hr 3.1 mph 7.5 mph 3hr 3.68 mph 9.0 mph 4hr 2.64 mph 6.55 mph 5hr 0.5 mph 1.15 mph North-Easterly Direction 6 hr after how Dover 1.38 mph 3.45 mph Thus, it can be seen that this site has the fastest tidal flow rates of those compiled, but also the widest variation between maxima and minima.However, such sites would have the advantage of not crowding the estuaries and rivers where similar fast flow rates may exist and as such, therefore, perhaps become tempting sites for the process. Nonetheless, river and estuary sites would obviously be more convenient and less expensive to apply and obviously would be the first choice of site type for first applying the process. Moreover, for off-shore sea sites one would obviously select specific sites where there is known to be a good tidal current as constant as possible over as long periods as possible in each of the alternating tidal flows, but the foregoing compilation of data should serve to give some indication of the types of conditions that one may find at such selected specific off shore sites. The main question at this stage being whether such conditions would be suitable for applying the process.I think undoubtedly if the process is geared to a national grid set up, with the output becoming evened out over several such processes and/or by associated methods of storing and releasing the power. Although at this point in time and having viewed the off shore seas from the end of piers and the like I find it a little difficult to actually believe in these types of off shore water flows and envisage them flowing through the heat collection unit at such flow speeds. In contrast to a river flow for example which is far easier to believe in and envisage flowing through the type of heat collection unit discussed, all the time in one direction at a fairly constant speed, albeit probably not as predictable.However, perhaps this is because one sees such flows relative to stationary banks on either side and if the Admiralty Charts state such water flow speeds for off shore sites then thev must of course be correct and.therefore.

it should re possible to apply

1to tne process must as one could a river flow albeit having to facilitate for alternating flow every 6 hour period of tidal flows. Which the process is ideally conducive to being able to do.

How one would actually facilitate for the ongoing variation over the 6 hour periods would be a matter for further more detailed deliberations, but in one way it would probably be achievable by basing on a multiplicity of systems comprising compressor/turbogenerator/sub-system, and then varying the number in operation at any one time in unison with varying collected heat which should be pre predictable. Or facilitating for the slowest flow rate of the longest periods, and shutting down during the tide turn around periods, e.g., 4 hours on, 2 hours off, 4 hours on, 2 hours off, day in, day out, year in, year out, forever ad infinitum, as long as the Sun keeps shining and the Earth keeps gently swaying rocking from side to side. The Sun at least will keep on shining for at least 2 million years before showing signs of any solar radiation diminishment.

Thus, it would probably be better to harness the heat closer to the surface of seas and due to the Sun rather than water heat in currents adjacent to the Earth's crust.

Now turning to data on river and estuary flows. At the present time I am not in fact in possession of much of this type of data. However, I have a little data on the Firth of Forth which I give following.

The fastest flow speeds for this water system is said to be at a point just above Alloa, where the flow is in fact still an alternating tidal flow With the turn around point taking place some 6 KM beyond Stirling. At high tide the flow at the fastest point just above Alloa is said to be 6.56 ft/sec, i.e., 4.47 mph and ranges from 0 mph at the turn around point to the maximum of 4.47 mph flow speed then back to 0 mph each 6 hour alternating period. The width of the river at this point is approximately 1/3 KM and is approximately 3 - 8 Metres in depth.

Therefore, whilst one may consider such sites would be more ideal, some of the off shore sites could in fact be betterand from all the standpoints,eg,flow speed, constancy of flow speed, pre-predictability of flow speeds, depth of water flow available, minimum cluttering of water ways, perhaps temperature level and its pre-predictable constancy.

To round off this general data review at this stage following I give some data obtained on average surface sea temperatures between 1904 and 1954 around the British Isles: Feb-coldest Aug.-warmest West of Ireland - Atlantic 9-lloC 14-160C Irish Sea 5- 80C 13-160C North Sea 5- 80C 13-160C Severn Estuary 6- 80C 15-160C Thames Estuary 60C 170C Thus, some of the temperatures in the waters around Britain become quite cold in the winter months, but probably one would be able to rely on being able to still extract at least 4 C during the coldest month at the particular site selected, and perhaps the full 50C when one takes into consideration the depression of the freezing point of salty sea water.

Other possible sea sites would be in the pathway of fast running tidal currents deep down in the sea, when an advantage of such sites would be that of perhaps being able to apply the potential head value of the liquid phase from the surface where the sub-system would be down to the actual heat collected deep in the depths of the sea. Thus in the use of the refrigerant R-13 for example it would seem possible that one could harness energy in the sub-system all the way down to normal lATS. Then applying the potential head of the liquid phase to give the equivalent of the desired ground state of 20 ATS. in the use of this refrigerant on the entry side to the heat collector in order that one could then vapourise at 20ATS.

vapour pressure on the exit side of the heat collector. Although if such a method of operation proved possible then the liquid phase would become very cold and to the temperature associated with 1 ATS. pressure, i.e., -81.40C, and therefore it would be necessary to thermally insulate to avoid premature vapourisation until the liquid reached a position with the equivalent of 2SATS.

liquid pressure above. Then the vapour produced on contact with the water flow would pass along the heat collector and exit on the other side. But obviously there may be a water freezing problem and therefore it would be a question of optimising pressure and temperatures with water flow speed, etc. However, it could prove a way to acquire a quite substantial level of bonus energy, if at all possible in the first place but/this stage I'm not too sure whether or not the concept is sound in principle. The depth of R-13 liquid to give the equivalent of 25ATS. pressure above would be approximately 850 ft. Then there would be the possibility of the use of other refrigerants which could perhaps be more suitable for acquiring bonus energy via such a means.For example, refrigerant R-12 of Bpt -30 C at lATS, since at such a temperature the potential water freezing problem would be less. Remember one would still only be extracting 4 - 50C from the water which itself wouldn't be a level and rate of extraction that would freeze the water flow, but one could obviously form an ice layer on the heat collection unit. Although the refrigerant would be trying to reach the temperature of the water flow and should have fully done so by the time it exits from the unit. Therefore perhaps such a method could operate with a steady state ice layer over the collection unit, which could also protect the unit.

However, the bonus energy one could obtain in such a way in the use of R-12 would probably only be of the order of 5%, whilst the use of R-13 in such a way could give a level of 2r% bonus energy. But in comparison the depth required for R-12 would only be around 125ft. Before then passing through the depth of the heat collection unit.

Moreover, iE one is applying the partial vacuum technique to add to the output of the sub-system then it would perhaps be necessary to apply this liquid phase potential head technique in order to be able to apply the partial vacuum technique in the first place. However, in contrast the height of the liquid potential head would only have to be the equivalent of lATS. vapour pressure, i.e., around 25 ft. Aaain. before then Dassina throuah the depth of the heat collector

But in contrast I think could give up to a 50% energy advantage,1andas in normal power generation based on steam and vapours where partial vacuum energy becomes added in the form of a condensation vacuum.However, again all aspects that would require practical trials and in this case the 25ft of potential head requirement could be simply achieved by elevating the sub-system and associated equipment to 25ft above the water level if one wished the heat collection unit to be close to the water surface, bearing in mind that the compressed vapour on exit from the compressor could perhaps become freely elevated to such a height without any extra energy input requirement or very little and without impairing the functioning of the process. Thus, perhaps also another source in the system for acquiring bonus energy advantage

Additionally, there would of course be actual river sites, and one envisages that it could be a feasible proposition to add the process downstream from existing hydropower schemes.Such a process could also be ideal for applying relatively small capacity processes in rivers and streams simply to produce power needs for small industry, cottage industry, small holding sites, market garden sites, and for normal domestic purposes, etc. For application at home, abroad, and all over the Planet in such a way. When 1 - 20 KW units would be very small in comparison. For example for a stream or river flowing at typically 5ft per second and extraction of the value of 0.250C over just a lOft long heat collection unit, then for a 1OKW unit the width and depth dimensions would have to be as follows: 1OKW = lOKJ/second For the heat to be absorbed I will firstly base on double the 3.5 to 1 ratio, i.e., 7 to 1, to allow for half the energy perhaps having to become consumed internally to make up a shortfall in the sub-system.

Thus the unit will be required to absorb 70KJ/second The unit would extract 0.250C over its full length in two seconds, and it would require to extract 140 KJs in two seconds.

1 cubic foot of water will contain: 118 KJ per 10C 30 KJ per 0.250C 15 K3 per 0.1250C In 1 second of flow from half the unit there will be required to be collected 35 KJs. While each cubic foot of water flow would be transferring 15KJs over half the unit's length in 1 second. Therefore there will be required to flow a total of 2S cubic feet of water from which 35 KJs of heat would become extracted. Meanwhile a further 35KJs would be becoming extracted from the preceding 2Ji cubic foot volume flowing on through the second half of the unit. Therefore the width and depth dimension would only be: 2.33 = 0.467 square ft.

-5 = 67 square inches If one bases on a depth of 6 inches then the width of the unit would only be required to be 12 inches. If one then doubled the depth to allow for the pipework carrying the refrigerant then the dimensions of the submerged heat collection unit would be just: 10 KW Unit 10 ft long or 5 ft long 1 ft wide 2 ft wide 1 ft deep 1 ft deep Which again seems ludicrously small.

Therefore cross checking, as follows.

10 ft x lft x 0.5 ft = 5.0 cubic feet of water.

Such a volume of water would contain: 4.18 J per gram per C.

62.3 lbs of water are contained in 1 cubic foot of water.

Therefore 5.0 cubic feet of water would contain: 62.3 x 453 x 4.18 x 5.0 = 590 1000 - 90 KJs per I C = 147 KJs per 0.2QC Since the 5.0 cubic feet of water would flow through the unit in 2 seconds then 147/2 = 70 KJs would be becoming extracted in 1 second.

70 KJ/s = 70 KWS And therefore at a 7 to 1 efficiency level the unit would be producing 10 KWs of power capacity for output supply. Thus the calculated dimensions would seem correct However, for such a small unit then one would perhaps moreso come up against

and therefore the technique devised to overcome such difficulties may moreso have to become applied than for very large capacity Plants able to have very large fluid flows through the sub-system in the first place.

Basing on the foregoing estimations giving below a table of possible heat collection unit dimension for 10 KW to 1 SY capacity Plants.

For River Flow application basing on a flow speed of 5ft per second, i.e., 3.42 mph, and a heat extraction rate of 0.25 C per lOft length of unit.

Submerged Heat Collection Unit Dlmensions,E G: Length Width Depth 1OKW - lOcu. ft. 5ft x 2ft x lft 20KW - 20CU. ft lOft x 2ft x lft 40KW - 40cu. ft. lOft x 2ft x 2ft 80KW - 80cu. ft. lOft x 4ft x 2ft 100KW - lOOcu. ft. lOft x 5ft x 2ft 500KW - 500cu. ft. 20ft x lOft x 2.5ft 1MW - 1000cu. ft 20ft x lOft x 5ft The relationship 1 KW is given by 1 cubic foot of heat collection unit is very convenient and cross checks as follows.

1 cubic ft. of water contains 118 KJs per 10C From 1 cubic ft. of water in 1 second will be becoming extracted: 0.125 C = 14.75 KJs per 0.1250 C - which will be the amount of temperature extracted from 1 cubic foot of water per second. And from all the 1 cubic feet of flowing in the unit in 1 second.

If one then bases on the ratio of 1 to 7 absorbed/becoming converted for output supply then the value would be 2KJs per cubic ft per second, i.e., 2KW per cubic ft. However the heat collection unit dimensions have yet to be doubled to allow for the volume and effects of the heat absorbing pipework in the unit.

the relationship will become 1 KW per cubic ft of unit. Enough power to keep 10 x 100 watt bulbs continuously on all the time shedding light all around where there may be darkness. Or to continuously keep a small 1 KW water pump pumping water all around all the time where there may be dryness at around 15 gallons per minute, i.e., 900 gallons per hour and capable of pumping to a head of up to 16ft in the process.

Then when one builds the capacity up to lrNshr the heat collection unit dimensions perhaps seem more believable, and the dimensions required for lFENhr would perhaps be the limit capacity for most smallish rivers from one site.

Additionally if one wanted to set up on or close to the beach then there would seem the potential for individual in-shore off-shore sites for these order of power production simply via means of the flow of the tide going in and out? Water Pump Plant: A further concept at this stage would seem to be the potential for producing the power to run water pumps from the heat that one could extract from the water that was continuously pumped, ad infinitum, which would then be a pump that could be placed at either end of the water flow. Obtaining cool water in the process and perhaps a refrigeration and/or cold store facility via pre application of the cold liquid phase of the process as it exits from the sub-system and en route to collecting further heat from the water flow ad infinitum.Obviously, therefore, such a process if possible and sufficiently inexpensive to manufacture could be ideal for some Third World situations, as indeed would application of small units in rivers and streams and in the tidal flows of their local coastal waters and estuaries.

Water Pump and Power Plant: Progressing further, it follows that the process as a water pump could not only convert sufficient energy to power.the water pump but could well be capable of producing a surplus of energy via the collected heat from the water flow, at least for the needs of a market garden and the like. Perhaps to give even cooler water if extracting at say the 50C level. 10C of which should be ample to keep the water continuously flowing, with the other 4 C then being surplus power for the other needs of the venture.However, it would be better to be a venture where the water was required to be continuously running all the time on a fairly large scale, and just one such venture would be agricultural ventures in arid and desert lands of the type where water is continuously sprayed over the growing areas via stand pipe sprays.

Whilst for a venture such as a Paper Mill then 50C of heat could become extracted from the water throughput through the mill, which would invariably range between lO0C to 150C throughout the course of a year even in the colder climates. If my memory serves me correctly the water throughput of such a Mill is around a 2i million gallons per 24 hr day per paper machine. Although with new water conservation measures and new water recycling systems this could now have become improved to say 1/4 million galls. per 24 hr day per paper machine. Therefore, basing on a million gallons per 24hrs for a 4 paper machine Mill. The amount of water throughput per second would be: 11.6 gallons per second = 1.86 cubic ft of water.

1 cubic foot contains 118 KJ per 1 C Therefore: 1.86 cubic feet will contain: 118 x 1.86 x 50C = 1097 KJ per 50C Which would be the extraction rate per second. Thus the total energy production would be: 1097 KJ/sec = 1000KW = lENhr Whilst the total energy requirement of the 4 paper machine mill could be up to 100 MWhr. Therefore, probably not a suitable method via such a means for such an application and probably the only approach would be via a River Plant in the river from which the water was being taken for the Mill if the river was large enough.However, for solely growing ventures in the desert then it could be a feasible way, and indeed it could prove possible to purify and/or desalinate a proportion of the water in the process for drinking purposes via a boiling water/condensation of steam technique via an electric kettle element type of system, since all the heat input required would all be possible to recycle back into the heat collection unit. Firstly the 80 calories per gram required to raise from 200 to 1000C, then the 540 calories of latent heat per gram to convert from water to steam, which would all become recovered on condensing and cooling via the heat collection unit.However, since the process only converts a smaller proportion of the absorbed heat each cycle, then in this particular process concept where the heat is coming from the water being pumped probably just Sw of the total pumped water could become treated in this way, and closer towards 5% if one still wanted a surplus of power for uses other than the water pump.

However, these are very general estimations and is an example of where more detailed calculations would be required to fully ascertain the potentials for this particular process concept. However, for smaller applications in particular it should be remembered that the process would comprise quite a number of expensive items of fairly complex equipment, although perhaps no more complex than say a car in total, or the sum of a number of domestic appliances and/or electrical goods, e.g., fridge plus vacuum cleaner plus washing machine plus car engine, etc., to try to place in some perspective.Nonetheless, for smaller applications where there may be no commercial venture involved or one which is not very lucrative then another process type may be less complex and less expensive in the fullness of time, albeit perhaps not as easily and at as little cost in energy giving the accompanying functionalities of refrigeration and cold store capacities, e.g., the process type under PA 872 0291 Wi) Basing on half the power production having to become consumed internally to make up a short fall in the sub-system energy requirement, coupled with continued discussion Under such conditions then it would simply be a case of doubling on the volume flows and required heat collection unit dimensions in either the width or the depth dimension, or via a combination of both, in relation to the preceding estimated values for a given capacity of Plant.Thus the heat collection unit for a 1000 MWhr Tidal Plant would become the following dimensions for exampe:- 1000 b5shr- 61 Metres long 48 Metres wide 6.1 Metres deep Where the width dimension has been doubled from 24 Metres. Remember the dimensions are already doubled to allow for the volume and effects of the pipework carrying .

the refrigerant, which in fact is probably an overestimation but it is better to err on the larger size at this stage with respect to this aspect.

However, the conditons under this heading were in fact allowed for in the preceding estimations for the smaller capacity River Plants.

Therefore, I don't propose to give further dimensions here for this method of operation. Which however could perhaps be the conditions in the beginning of the development of the process before the sub-system becomes perfected and, therefore, they should be considered with more than just passing comment but one can see that the process would still be very worthwhile and a viable proposition in all the methods of applying the process that have been discussed so far even if half the energy produced by the turbogenerating process has to become used internally to make up a short fall in the sub-system/compressor cycle of the process Perhaps especially in the case of the River Plants where such a method of operation was in fact considered and thus with the potential to become substantially improved.While in the case of the Tidal and Sea Plants then these may seem rather long at least in being based upon 200 ft in length, but in relation to the length of a ship and in the open seas or widening estuaries at least then I don't think so. However, at this point in the discussion considering this aspect further.

The length dimension of the heat collection unit: Firstly it should be bourne in mind that when just 50C is desired to be extracted from the water then one wouldn't increase upon the length dimension to increase capacity or to allow for the above conditions, although for the river units where just 0.250C became extracted over the lOft long unit then it would be possible to extract further heat via longer units as indeed for the 500 KW and 1MW River Plants in the preceding. However, a further aspect to be aware of is that the 50C heat could become transferred over a shorter distance of heat collection unit than a 200ft long unit and could well be transferable over a lOOft or even a 50ft unit.While the width and depth dimensions could remain the same for a given capacity unit but with each gram of water 'captured' by the frontal surface area of the unit then going on to transfer the same quantity of heat as for the longer unitbutover a shorter length of heat collection unit.Therefore whilst the total temperature tobeextracted would be a fixed amount, the heat collection unit to extract the heat could be shorter and this parameter will depend upon a number of factors but basically the rate of extraction possible as determined by the rate at which heat can conduct, firstly through the walls of the pipework carrying the refrigerant, then the total surface area of this pipework that would be possible in the unit, coupled with the rate the heat can transfer through water and all coupled with the speed and volume of water flow possible to flow through the unit.At the present time the metal that would be used would probably be Delta Metal of composition Cu55, Zn 40, (Al,Fe,Mn)5, which has a strength approaching that of steel and has great resistance to corrosion by sea water and currently becomes applied for Ships propellors and the like, ref; General and Organic Chemistry by P.J. Durrant, page 567. However, this metal should also have one of the higher thermal conduction properties of the more traditional materials to further add to its ideal nature for this application. Perhaps being a little more expensive in the first place butifthe process then and thereby lasts for 100 years without ongoing fuel costs then any extra expense due to such aspects would be worthwhile. The thermal conductivity of the metal will be approximately: 3 Joules per square cm. per cm. length per C per sec.

Therefore, here giving an approximate calculation to determine the thickness the walls of the heat absorbing pipework would have to be, i.e., the length parameter in the above value, to allow the rate of heat transference required.

And for this basing on the calculation for the original 1000 MWhr Sea Plant Unit, but assuming that it becomes a 500 MWhr unit due havingtouse half the power output internally, which however won't make any difference to the following calculation.

Thus, that unit had to absorb a total of 3,500,000 KJ/second, and the total volume of the unit was: 200 ft long 80 ft wide 20 ft deep Of course I can only guess at what amount of heat absorbing pipework would be possible and its total heat absorbing surface area within the above volume, but the path of the water flow would have to be fairly clear and any pipework in the way would have to allow smooth flow of water between by appropriate design shaping of pipe CSA, here thinking in terms of horizontal Pipes across

the path of the water flow.Therefore with these aspects in mind 11base the calculation on just one pipe horizontally across the water flow of 3 inch diameter (if it was round) in 1 and every square foot of the surface area of the sides of the unit running from one side to another, suitably staggered for the best flow of water. Such a volume of pipework would in fact represent appreciably less than half the total volume in total, but its better to have erred on the larger size and the water flow rate could become slowed down to some extent even with such an open arrangement of pipework.

Then the total heat absorbing surface area would be: 200 x 20 x 80 x /err0.125 = 251360 square ft.

Now its a question of calculating the thickness of the pipework that would enable such a flow rate of heat through such a heat absorbing surface area.

Thus applying the heat conduction equation as follows: Q per sec = KA (T1 - T2) - Ternperature Gradient across, 1.

pipe thickness, 1, = 3 x 251360 x 929 x say 5 C average 3,500,000,000 = 1.0 cms which is of around the correct order-and as such confirms my original calculations on which I based the earlier work and also, therefore, the estimation that the heat collection unit will be capable of extracting 0.25 C from the water flow every lOft length distance of the unit through which the water is flowing whilst still having a sufficiently open arrangement of pipework to enable smooth flow of the water through the unit.However, this would obviously be an area where better heat conducting materials would enable the extraction of a given quantity of heat over a shorter distance of heat absorption unit and where better design arrangement could improve upon the heat absorbing surface area to volume ratio to again enable shorter units for the absorption of a certain amount of heat and desired total temperature drop, although the design arrangement discussed could be fairly ideal. Nonetheless one can see thattheunits could become shorter,. and indeed simply by halving the piping thickness then one could half the required length of the unit. Which would be tempting, but if made to last for a century in the strong currents of salty sea water and with the creatures therein then the thicker the better.However, encrustation would lower the heat conduction rate and therefore it would be debatable whether or not it would be better to have a system of periodic replacement of thinner pipes. 2000 in total if half the thickness enabling half the length of collection unit. Indeed half the thickness, i.e., 0.5 cms may be suitable in the first place for very long lasting units, but throughout I've tended to err towards the worst conditions in order to give the system areas for vast improvement while showing that even the process under the worst conditions would still be satisfactory.Thus, when one considers the thickness of modern copper based pans, or the old copper kettles, and the rigours of very high temperatures that they have to withstand in comparison over long periods yet able to last for decades, then perhaps thinner guage pipes would withstand the flow of water for some 10 decades or more bearing in mind that the pipework would not be load bearing. And perhaps especially so in the case of River Plants.

However, an aspect is that the temperature gradient from water to absorbing pipes will gradually lessen by 50C in the case of the Sea Plants, but by only 0.250C in the case of the River Plants per lOft. length of heat collection unit.

Therefore, particularly in the case of the very long Sea Plants it will be necessary to take this aspect into account and from the heat conduction equation it can be seen that this parameter will make a large difference from the front to the rear of the unit if the water is reducing by 50C whilst the heat absorbing part of the equation, T2, will be remaining the same throughout. For example, in cooler waters then the gradient could well become reduced to 10C and the pipewall thickness in the preceding calculation would become a fifth to 0.2 cms, which obviously would be too thin.Nonetheless, it would obviously be one approach to evening out the heat absorption rate, i.e., simply via gradually reducing the pipe wall thickness as required, and for the earlier views of the Sea Plants and the estimations based on those views it was assumed that some such way had been devised to even out the heat conduction rate along the heat collection unit to give the even temperature extraction rate of 0.25 C every lOft length of the unit. Although, for warmer waters which may corn;nence at 200C and reduce to 15 C, with the pipes remaining at 90C throughout, then the required reduction rate in pipewall thickness would only be to around half their original thickness, which would then render this particular approach more feasible with today's materials.However, a further problem will of course be that if the process is dependent upon 2-way alternating tidal flows then if such an approach was adopted then one would perhaps have to revolve the heat collection unit around in the way of some swing bridges and railway engine turntables and the like, although there could be a system of changing/moving the pipes around during the tide turn around period which could perhaps be more easily facilitated for if the pipes were vertical.Which may be required to be carried out anyway in order to change special pipe shaping around to be facing into flow in the opposite direction, although with such an open pipework arrangement then perhaps fully circular CSA pipes would suffice and just give sufficient turbulence for optimum mixing and transference of heat from every drop of the water. Which would also be a desired design for the following further approach to evening out the heat transference rate.

Where there is a broad margin of temperature then a further approach would be to increase upon the vapour pressure at the start then gradually lower back down again to gradually lower the absorbing temperature to the level of 9 C and in such a way maintain a temperature gradient of 5 C throughout for the same thickness of pipewalls throughout. Then at the tide turn around start with the higher vapour pressure at the other end of the heat collection unit.

However, for cooler waters such an approach may not be possible because the lower temperature of 90C to the water temperature may only be the desired 50C temperature gradient in the first place. However, yet a further approach would be to alter surface area of heat absorption, then change/move the pipes around during the tide turn around period, but this could obviously interfere with the design arrangement for optimum water flow through the unit, which is likely to be best with a constant number of pipes throughout. Therefore perhaps a gradual reduction in pipewall thickness would be a better approach, and obviously~ the use of new materials with much higher heat conducting properties could render such an approach more feasible and indeed lead to shorter heat collection units for a given heat absorption.

Thus itis possible that one could apply some other technique to even out the heat absorption rate than changing pipe wall thickness and it is possible pipewall thickness could be half than applied herein. In which case then the length dimension in all the foregoing estimations of heat collection unit size would be half, with the width and depth dimensions remaining the same.

Although a further aspect to bear in mind is that the pipework arrangement would be fairly open to allow good flow of water through the unit and therefore the actual water to pipework contact may be lowish for the system and the heat conduction rate through water is slowish, and therefore perhaps at this stage one should in any case err on the longer side to allow for these aspects of the system. Thus, even for half the wall thickness the unit may still have to be the length dimensions applied. But having said that this would be an area for improvement, perhaps to achieve half the length dimension simply via a combination of a less wall thickness than applied herein, design shaping, design arrangement, and best method of operation.But then with even more potential via the develop ment and use of a material possessing a higher heat conduction property, when an improvement in the heat conduction value from 3 to 9 Joules could potentially enable the same heat transference over a third the length of unit.

Of course,one need not bother about evening out the rate of heat absorption and simply live with a variation in the rate of vapour production via pipes of the same thickness and giving the same surface area throughout, but for cooler waters this would mean that as the temperature gradient diminished to 10C then for the same wall thickness and piping surface area the vapour production would also diminish by a directly proportional amount. Although not necessarily since yet a further way would be to use piping with changing heat conduction property. Thus, there would be several possible approaches, but all something of a mute aspect in the early stages and therefore progressing on but obviously it would be better to have some ideas on the general direction with regard to such aspects of the process in advance.

Methods of Operation - general discussion continued: While the 4 hours on-2 hours off method of operation may sound a reasonable approach the start up and shut down procedures would have to be very readily and quickly achievable, which would seem feasible in the fullness of time.

However, a different approach would be to facilitate for the ongoing variations in production over a 12 hour period with the constancy and reliability of the repeating 12 hour period. Which via,and from the point of view of storage of the energy in order to facilitate for an output supply as desired, may be fairly readily achievable by a method in which one evacuated underwater tanks with the energy that became produced by the process as and when the energy becomes produced. Then simple harnessing of the potential head energy of water as it is allowed to flow back into the tanks through hydro turbines set in the top of the tanks, as desired in contrast.In such a method of operation one could in fact gain the advantage of high tide levels by evacuating the tanks at low tide then harnessing at high tide, which to some extent could be in unison with the high tide period in any 12 hour period since high tide will take place at the high tide turn around stage. Moreover, one could increase upon or decrease upon the rate of harnessing of the potential head of water simply by changing the capacity of the hydropower turbine. Thus, for example, one could evacuate the tanks with a relative trickle of energy over a 12 hour period, and then subsequently harness over a 1 hour period during high tide.The advantage of the high tide could double the energy and if the trickle of variable energy represented an average of say 100 Mshr then the power yield one acquired over the 1 hour period could be 12 times doubled equals 2400 MWhr. However, in such a case only for 1 hour every 12 hour period. Or if over a 2 hour period then 1200 Ruhr for 2 hours every 12 hour period, etc. Then if one had Tidal Plants all aground Britain, one could probably feed a constant supply to a National Grid because while the tide is up on the west coast it is down on the east coast, and vice-versa, etc.Thus, it is progressively seeming to be a method of power production best suited to a national approach of planned harmonising in with the sea tides surrounding a Country and supply to a national grid, although not necessarily the only approach of course. For example, one or two very long Power Bridges appropriately sited in combination with some such storage technique could provide all a Country's power needs from here to Kingdom Come. For example, one from Dover to Calais and one from Mull of Kintyre to Northern Ireland to also harmonise with the developing plan for Europeans to add to the present Channel tunnel plan, and could become road highway bridges.

Perhaps also accommodating for cyclists and pedestrians on a different level with the attractions of a pier all the way across. Similarly from the Rock to North Africa, and from Djibouti to the Yemen joining Africa to the Arab States across the Bab al Mandab Passage. In the process providing much of the power needs for Djibouti and for part of the Yemen which could readily be turned into Rain if desired simply by compressing air, then removing the heat of compression to generate electricity in the normal way, e.g., as discussed under my PA 8728601, then application of the cooled compressed air to generate further electricity and in the process yield very cold exhaust air for RainMaking purposes. Thus in such a method of operation one could finish with at least the same amount of power and a very large RainMaking and Refrigeration capacity.But of course for extra Plant and the capital costs thereof in the first place, but then all running on the freely available sea heat, which the Sun would keep replenished and a drop of 5 C for the relatively small amount of water involved would barely be felt by the other factors. If and when it ever did then a further-method of operation would be to compress air with the initial energy, place the heat of compression back into the sea, then generate power with the constant pressure cooled compressed air and apply the cold exhaust air for RainMaking and Refrigeration. And if the heat of compression was placed into the sea upstream ahead of the heat collection unit then the process would keep recycling the same heat.However, the heat of compression could just as well be placed directly back into the heat collection unit along with the recycling heat of condensation from the turbogenerating process. When the process would then be becoming close to the process as combinable with an air ARC cycle instead of the heat source being via the heat of a natural water flow.

But a way to render the latter combined process type fully self-sustaining could be to make up any short fall in energy via the heat of flowing waters or perhaps via direct solar heat, or indirect solar heat via a solar pond approach.

Yet a further way being to use the first amount of cooled compressed air to first compress further air to yeild more heat of compression. Then use the second quantity of cooled compressed air for generating power and there would in fact then be two amounts of very cold exhaust air for the RainMaking and Refrigeration purposes. However, progressing on these potential possibilities for the basic process under a following section dealing with the process as co;nbinable with the air ARC cycle.

While for the process placed in the Bab al Mandals Passage for example one can see that a further potential method of operation would be to compress air with the initially produced energy, then generate electricity on site with the heat of compression, then distribute the cool compressed air around a Country as though a gas pipeline and at the desired sites of usage generate electricity and apply the cold exhaust air for rainmaking and refrigeration. And if in conjunction with the equivalent of gas storage holders around a Country then this would be a further approach to dealing with variable production. Furthermore one could double the energy output from the cool compressed air by rendering an isothermal expansion to ground state temperature via use of available natural heat, e.g., solar pond heat, albeit at the expense of RainMaking capacity but perhaps still retaining Refrigeration and Cold Store capacity. Moreover, for many uses, e.g., water pump, one could apply the compressed air directly without needing to first generate electrical power. But again this modus operandi would be more for a co-ordinated National Plan, which is not all that appealing a proposition in the evolving British climate of business but would probably be so for many of the African nations for example, necessarily leaning towards more communal approaches to the construction of their societies.Thus such Countries could opt for a National Grid of cool compressed air instead of an electrical grid, comprising the equivalent of gas holders all over their country becoming fed by one or two large power generating sites via the process based on sea heat and/or ARC heat where electricity could also be produced onsite via heat of compression and where concentrations of power consuming industry could be sited. While in the agricultural parts of the Country then cool compressed air could become supplied, which could provide power, refrigeration and rainmaking capacity.

Thus for the hotter Third World Nations prone to drought and famine I think the above approach makes sense and could be one of the better ways forward into the future for them, gradually leading them towards control over their weather and climate and rain and rainbows at the touch of a button. With tall nodding chimneys issueing forth cold, clean, air all over their agricultural lands creating the gentle rain and coloured rainbows for them. All from power produced for them via the sea heat flowing to and fro through the Bab al Mandals Passage. All in all year round Sun and Blue Skies with unlimited land, Arabia, Persia, Oman, the Persian Gulf to the East and further to the East Bombay and Mangolore, to the north Egypt the Pyramids and the Pharoahs and a little further to the north the Mediterranean, while to the south the Cape of Good Hope.

All around golden sandy beaches under all year round Sun and Blue Skies with the warm gentle waters gently lapping on the golden shores all around. As a cake mix, just add water, removing salt to taste as desired and as required.

100 MWh Plant Meanwhile closer to home a new era in Mills could become created, obtaining power from fast flowing, natural waters. All lined up along the banks of rivers and estuaries, each dipping their equipment into the waters in some appropriate staggered fashion. Probably in such cases the refrigerant collecting the heat would become pumped to and from the waters with the actual Power Plant in the Mill.

Assuming the Mill required 100 MWhr of power and the flowing waters were travelling at 5 mph then the approximate dimensions of the required heat collection unit would be: 100 MWhr = 100,000 KJ/second Which at the conversion efficiency of 28% becomes: 350,000 KJ/second Assuming the unit for such an application will be 100 ft. Then for water flowing at 7.3 ft per second each 7.3ft section will be required to absorb 25550 KJ of the total heat per second. 1 cubic foot of water will contain 21KJ per 0.183 C which will still regard to be the temperature extraction over a 7.3 ft section of the unit. Therefore the volume of water flowing through the 7.3ft sections will be required to be 1217 cubic feet. Therefore the front surface area will be 167 square feet. Assuming the unit is 20ft wide then the depth would be 8.3ft.If one then doubles the volume the required dimension of the heat collection unit would be approximately: For example:100 ft long extracting just 2.50C of heat.

30ft wide llft deep And double again if the River waters were flowing at just 2.5 mph.

Thus really quite a small unit for Mills consuming 100 MWhr and used to paying around 10 million per annum for their power.

Moreover, there are many wide and deep rivers around the Continents of the World which peacefully and surely meander gently and slowly to the sea all year round.

And when they are and do then their speed would probably be closer to 2.5 mph which may then require a unit twice the size, which however, in this case could be all in the length direction since twice the length would double upon the extracted heat to the value of just 50C.

Ships Propulsion Power & Power Ships

It follows that instead of the water flowing through a stationary heat collection unit, if the heat collection unit was attached to the underside of a ship then it could travel through the water and similar collect heat for generating power for powering the ship.

A medium sized ship is around; - 300 ft long 50 ft wide (40ft deep) Travels at a speed of around 16 mph, and consumes around 3Thr of power. Whilst such dimensions would be the capacity of 1-2000 MW'hr Pants based on the preceding estimations. Thus it also follows that one could also have Power Ships, approp riately travelling to and fro capable of producing any amount of power but only consuming a very small fraction themselves. All the process equipment could be on board, but how to get the power to the national grid whilst steaming through the waters around a Country? Hawever, if possible then this could obviously be a better approach than fixed processes in tidal flows.Advantages would be one-way water flows and constant speeds. One can envisage that the Power Ships could circulate around undersea tanks evacuating them of water on a rota basis, in some way. Which could perhaps be achieved by first compressing air, producing power on board with the heat of compression which could be stored on board in some way and then evacuating the tanks with the cooled compressed air. All of which however doesn't seem a very modern, Space Age, way and perhaps not possible anyway. Therefore the waycouldbe via Energy Beam to Shore Collection Dish.

In the process pioneering such technology for Space Power Grids where the Earth power line grid approach would not be possible.

Which, however, may also not be possible but

via conversion of powerful laser beams back to normal power in some way. But perhaps it would be better to have the Energy Collection Unit out at sea on the horizon sky line, so that if one missed the beam would travel harmlessly on into space. Then from the fixed conversion station out at sea feeding power to shore in more normal ways.

However, how? would be a matter for further thinking, but undoubtedly the concept of Power Ships perhaps seems a better proposition than fixed Plants sited in natural flowing waters. At least when it comes to trying to harness the heat energy in the seas, although the concept of fixed stations would still apply and be better for River Plants. Moreover, if some easy, convenient, and inexpensive means were possible for the transmission to shore of the vast quantities of power that could reliably be produced in such a way then I think this could be one of the better final ultimate approaches to the provision of large scale power to national Power Grids.Having many advantageous aspects that one would wish and hope for in the application of the process based on natural water heat, e.g., reliability, constancy, one way flow, but with the disadvantaoes of rough weather

to contend with and1 how to transmit the energy to land. Perhaps after all is said and done the simplest way would be to have a hold full of battery storage capacity. Then several hour long cruises to fill up the battery store followed by discharging into the grid at suitable fixed stations around the coastline of a Country, ad infinitum. With as many of the Power Ships operating the coastline stations as required for the amount of Power desired to be produced in such a way.However, returning the discussion to power for ships propulsion and firstly estimating the size of heat collection unit required for 5MWhr of power production at a ship's speed of 5 mph.

5hr= 5,000 KJ/second Which at the 28% efficiency level would be 17857 KJ/second Assuming the unit is just 40ft long then for a ship travelling at 7.3 ft per second each 7.3ft section will be required to absorb 3259Mof the total heat per second. 1 cubic foot of water will contain 21KJ per 0.1830C which is still being considered would be the temperature extraction over a 7.3ft section of the unit. Therefore the volume of water flowing through the 73ft sections per second will be required to be 155 cubic ft. Therefore the front surface area will be 21 square ft. Therefore on doubling the size of the unit it will be required to be just; - 40ft long extracting just 10C 7ft wide 6ft deep Which is a size of unit that should fit nicely into a central recess in the bow hull of a ship in place of a part of the usual pointed shaping. Or alternatively side stabilisers could also function as the heat collection unit. Or the heat could simply flow through the ship's hull to vapourise refrigerant fluid flowing through a layer adjacent to the ship's hull. Which could perhaps be a better approach from the point of view of retaining the original shaping of the ship's hull and not adding to it's water resistance.However, the latter need not be too much of a consideration since one could simply have a larger capacity process to allow for the extra power required to overcome any extra water resistance.

Then for start-up one could charge a battery store via surplus energy during crusing times at 15 knots. For example, as the battery store that accompanies the Rolls-Royce 25 M' Gas Turbine Generators reference SK30, which occupy comparatively small space.

Thus, I think one of the above ways would be a very good reliable way to power ships freely via the natural resources on site, in the same vein as wind powered sailing ships in the latter respect but very much more reliably and now more dependent upon mankind's engine process rather than the reliability of the natural power source which in this propulsion system would be very constant and very reliable in contrast to wind power, even in rough weather unless the Ship is lifted clean out of the water. Therefore, perhaps an improved way would be to have the heat collection unit nestled in the hull in some way which when out to sea becomes lowered to a good depth via telescopic hydraulic rams, acting as a stabiliser in the process if broad and long but with little depth.However, a problem area would be changing sea temperature and perhaps the better way to approach this would be to select a refrigerant whose normal Bpt is around the OOC level, e.g., butane at 0.40C, then vary the actual vapourisation temperature via controlling the pressure of vapourisation, to in turn enable a constant temperature gradient for waters which may change from 5eC to 200C during the course of travelling around the waters of the World.

Use of the Process for powering a road vehicle, train, sky or aircraft This would be similar in concept to ship's power but instead of extracting heat from water the heat would become extracted from the air of the vehicle's on rushing air passage. Firstly estimating the potential for powering a train by such a means, which would have the large capacity of a train engine for the process.

To maximise upon the extractable heat from the trains air passage and minimise upon the air resistance to forward motion then probably one would capture, channel and streamline all the on rushing air passage to a heat collection unit mounted on the top of and to the rear of the front engine wherein would be housed the remainder of the process. For minimal air resistance the unit could again be comprised of suitabley shaped pipework carrying the heat absorbing refrigerant in its cross-sectional shaping, although some turbulence creation may be necessary to extract sufficient heat.

Assuming the heat collection unit extracts 5 C from the air flow as it flows from front to rear of the unit, then the total amount of energy extracted per second for a train travelling at 50mph would be as follows; - Assuming the front surface area of the train is 9ft x 9ft = 81 square feet, then the total amount of air flowing through the collection unit for a train travelling at 50mph, i.e., 73ft/second, will be 73 x 81 = 5913 cubic feet per second.

The heat capacity of air at 15 C = 1KJ per KG per C Density of air = 1.2 KG per cubic metre 5913 1.2 Therefore the weight of air = 35.31 x = 201KG Therefore extracting 50 will give: 1 x 201 x 5 = 1005 EJ/second = 1 Mhr Which at a 28% conversion level would yield 0.28 D1hr, and half this quantity in the method of operation where half the initially produced power becomes used internally to make up a short fall in the sub-system-compressor cycle, i.e., 0.14MWhr. Since a normal train consumes 2-3MWhr then the process would probably not be suitable for normal trains.

However, for road transport where the air passage air could be about half but the power needs much less e.g., 60HP equivalent to 45KWhr = 0.045MWhr, then even at the 14% level of output the power produced could well be of the required order, i.e., half of 0.14 Shr being 0.07Mh'hr which could still be twice the power requirements for the vehicle.

The process for such an application would of course have to be fully closed-cycle with respect to both fluids in the process, but is and moreover is achieved in an ideal manner, with the exhaust steam or vapour from the turbogenerating part of the process able to be readily condensed via the liquid phase of the heat absorbing fluid and in the process reducing the amount of fresh heat input requirement Moreover, the cold liquid phase of the heat absorbing refrigerant could provide cold-store and deep freeze transport, which would also apply to the application of the process in Ships.

Thus for road transportation at least the application of the process to provide propilsion power from air passage heat could be more than just a possibility and as such perhaps a future way to power road transport.

Whilst in the case of Sky and Air Craft perhaps a better way would be to have the refrigerant flowing beneath the outer skin of the normal aerodynamic shape of Aircraft in order not to interfere with the latter whilst at the same time creating sufficient power for the powering of the Aircraft. Then mankind would really be achieving 'Around The World on Something'. However, calculations indicate that probably one would have to try to apply the whole fusilage and wing surface area to be able to absorb sufficient heat energy from the air flow flowing over the body and wings of the plane.But conceivably this should be possible and probably the better approach would be to wrap pipework all around

all the body of the whole plane, with then a normal outer aerodynamic sKm,-l l to and fro heat exchange piping through both wings. When the total heat absorbed may yield sufficient power the plane via conversion into power that could drive propellors, in turn via the process at the 14 and 28% levels of conversion efficiency.

For example, considering a square metre of on-rushing air passing around the nose of the plane then along and spreading out all over its fusilage, and that such an amount of air is that which the heat absorbing system can extract 50C of heat from as it flows from the front to the rear of the plane. Then assuming a plane speed of just 200 mph for this exercise.

The air would be flowing at a rate of 300 cubic metres per second and becoming cooled by 5eC.

The heat capacity of air at 150C per KG per OC Density of air = 1.2 KG per M3 Therefore the weight of air = 360 KG.

Therefore extracting 50C will yield: 1 x 360 x 5 = 1800 KJ/second = 1800 KWhr At 28% output = 500 KWhr At 14% output = 250 KWhr However, such a plane could require 250-500 KWhr of power basing on known data.

Nonetheless perhaps just more than just a possibility in the fullness of time, and especially so when one considers that there then wouldn't be the weight of any fuel, although there would be the weight of the process and its fluids and that of battery storage for take off which together may be comparable weight.

However the larger the fusilage then the more the heat absorbing surface area and the better for passenger comfort. Moreover, the safer the plane from fire hazard in the absence of fuel. Furthermore, if the fluids in the process are flourocarbon refrigerants, as would likely be the case, e.g:i) Refrigerant-21 or perhaps more likely one of lower Bpt for this application, e.g., R-114 of Bpt 3.70C, for the fluid in the sub-system - heat collection compressor circuit.

And:ii) Refrigerant-ll of normal Bpt 240C in the turbogenerating circuit.

Then they would ín fact act as fire extinguishers in the case of a fire. Thus the whole plane would be encased in fire extinguisher fluid and the helical flow pipe system surrounding the plane would/could afford scme appreciable crash impact resistance. However I'm not sure where one would put the windows. Perhaps instead the plane could be fitted with closed-circuit TV giving panaramic views of the surrounding scenes on a large screen for everyone to see, not just those by the windows.

An additional aspect being that this would be another system of the work where the prevailing forces tend towards largeness rather than diminishment of capacity in order to achieve cost savings, which of course is a good aspect from the point of view of passenger contort. In contrast to the current tends due to the current prevailing forces of streamlining and drag reduction, etc.

The Process Combined with the Air ARC Cycle

As stated in preceding discussion, one main alternative source of heat for the process would be via the heat of compression of the air ARC cycle - i.e., as discussed under PA 8728601, and it would be a question of whether such a process could produce surplus power, and if not whether such a process would be worthwhile anyway simply for very cold exhaust production for the two RS and CS functions, i.e., Rainnaking, Refrigeration and Cold Store, but without sufficient energy left for the P function.Very probably it would in many of the arid dry hot lands of the World since such a process would be able to take in say 10% of the hot air of a Country, up to say a 1000 ft, and create Rain in the other 90%, down through say a l000ft, forever and a day, providing sufficient cold air for unlimited cold store and refrigeration facilities for their produce en route in the process. All on Thin Air. However, for such a project one would require quite extensive plant, and therefore firstly trying to determine at this stage the potential for some accompanying power production, with in mind smaller processes for individual farming ventures and the like possessing a PRR and CS capacity.

I will assume that the ARC cycle will fall short in its energy requirement by

40% as under PA 8728601,/firstly assume that the subsystem cycle will just selfsustain itself.

Referring to the energy cycle for the process based on R-21 on Fig 2, the heat of compression from the ARC cycle i.e., the heat source for the process,will all become absorbed by the liquid phase of the refrigerant in the process which if based on R-21 would all take place at a temperature of 90C. The vapour produced will then become fed to the compressor of the process and then heat removed with which to generate power. The power will be produced and the exhaust vapour from the turbogenerating process will become recycled to the heat absorbing liquid phase. Therefore, how much power would have to be being produced to sustain the short fall in the ARC cycle and for a surplus, and would such a level of power generation be possible whilst still leaving sufficient energy in the fluid for the subsystem to sustain the compressor.

Basing on the preceding estimations in relation to the energy cycle of R-21, Fig 2, the recycling latent heat between D to E will be around 65KJ/KG of the total of 240 KJ/KG becaning absorbed each cycle basing once recycling efficiency of 60% recycling heat, which would then reduce the heat that is to be supplied by the ARC cycle to 175 KG/KG. Since the heat of compression will be in the heat energy terms the turbine mechanical energy input requirement to the air compression stage of the ARC cycle, then the 40% shortfall will be 40% of 175 = 70 KJ/KG. However, at 40% power production then the power yield would be just 50 KJ/KG, with the sub-system just sustaining itself.Therefore, as one might expect at such a technology apex, the process could fall short in the beginning.

But apart from perfecting the various systems in the process so that the process would then yield a surplus of energy by just the desired amount no doubt, there is the technique of producing further heat via compressing further air and therefore examining whether via such a means some surplus energy may be expected to be achievable, albeit having the disadvantage of requiring more air compressing equipnent.

The first power yield from the turbogenerating plant could be used to compress further air, which would yield heat of compression equivalent to itself i.e., 50KJ/KG. This would then become recycled to the heat collection unit and say.

dOKJ/KG would be effective. This would then reduce the ARC cycle required capacity further to 175-40 = 135KJ/KG. 40% of which would be 54KJ/KG. Therefore, would the power yield from the second air compression be sufficient to sustain the 54KJ/KG and leave a surplus. Since the original turbogenerating energy was only 50KJ/KG, then the answer would be no. However a further technique that could be applied would be to render the second air expansion isothermal which would double the amount of energy, which should then be sufficient and in being renderable isothermal simply by maintaining the expansion at ground temperature then the heat required could be provided by the natural surrounds. Meanwhile all the ARC cycle air would be being rendered very cold exhaust air suitable for RainMaking and the liquid phase of the process could be applied for a CS function en route to the heat collection stage. Whilst the surplus power yield could then be of the order of 25 KJ/KG, i.e., as though the yield from the basic process was at the 10% level.

The above therefore would be a way to produce a PRR and CS Plant which ran on Thin Air, but requiring of an appreciable quantity of natural heat on site.

Which could be via a solar pond technique, and again I refer readers to the two papers being mentioned herein and which I further record at the end. The way that one would apply the solar pond heat would probably be via pumping the hot brine solution around the air expansion turbine in the manner discussed under PA 8728601.

However why not simply pump water and desalinate if requiring desalinisation and/or purification. Well I simply have in mind being able to go into the desert with a process, plonking it down anywhere and creating oasis style, paradisic living, with minimum of hassles and potential harassment.

However, a solar pond would be a bit of a hassle and therefore a further way could be to compress yet a further amount of air with the second amount of compressed air and the heat of compression from this compression could be placed into the air expansion carrying out the third air compression, to say double upon the energy value of the resultant third amount of cool compressed air. Although I will estimate just 40 x 1.7 = 68 KJ/KG. Which, therefore, could leave a surplus of energy after making up the 54 KJ/KG required for the original ARC cycle.

And moreover would yield further cold exhaust air to add to that from the ARC cycle, and since this would essentially be a Rairt'aaking Process then the more air that became compressed to yield cold exhaust air the better and therefore this approach could be one of the better ways to a PRR and CS Plant running on Thin Air, with only air compression being additionally required. However, perhaps for a rich man to play with rather than normal farmers and normal farming ventures, although it would be an approach for a Nation as a whole to apply in a National Plan to produce Rain over large areas of land whilst cooling their climate a little, and perhaps warming ours by virtue of removing water vapour

tnat may otherwise precipitate over Britain as itlmet the Arctic air travelling south.

Thus it follows that given the total quantity of Plant that would be required for a Country to control its climate and weather via such a means then quite a substantial amount of power in total could become produced in the processes.

However, perhaps one for a rich man's Nation rather than for a poor Third World Nation. Initially, at least, with overcoming the American drought problems perhaps being a more ideal scenario and reason for developing such technology to such levels in the first place. However, an open aspect at this stage.

Considering further the third air cwression with the second amount of cool compressed air, in one view the energy yield on recycling the heat of compression back into the second air expansion may barely be sufficient to make up the energy shortfall in the original ARC cycle and yield a small surplus per process, but in another view I could have underestimated the energy yield since when the heat of compression from the first cycle becomes recycled this could nearly double upon the energy yield which would then go on to increase upon the heat of compression and with this increased amount of heat of compression it will in turn give rise to an even higher energy, and so on. But there will be a limit because the second amount of air will be a finite amount and there will be limit to the quanitity of heat the air could absorb.But remember the amount to the barely sufficient level will only take the temperature to ground level, which should then be capable of absorbing further heat to at least double the barely sufficient level. To then give a surplus for output supply of around 50iGJ/KG when related to the foregoing estimations. Thus, this could then really be the way to produce a PRR and CS Plant running on Thin Air forever and a day and only additionally requiring of air compression equipment. But of course more detailed calculations would now be required to confirm, although not at this more general stage of course.

Hopefully not to confuse, further, commenting that the system between the second air expansion and third air comperession would be similar in principle to the process type discussed under PA 8720291. But different in that in the system under discussion the first energy of the turbogenerator would be that which was continuously compressing the second amount of air, which on removal of its own heat of compression then goes on to compress the third amount of air, having the heat of compression of the latter placed into the air expansion. While in the aforementioned process it would be the equivalent of the third air expansion with its own heat of compression placed back into the air expansion that would be powering the equivalent of the third air compression.Thus in the process under discussion there is the extra of the first energy from the turbogenerator commencing the line of two further air compressions linked to the turboger.erating part of the process,in addition to that of the ARC cycle to which the process is linked as the principle heat source.

Thus, the foregoing manner of operation of the process is progressively seeming to be a very plausible way of achieving one of the goals, i.e., that of the PRR and CS Plant running simply on thin air and requiring only plant equipnent.

As opposed to requiring another resource such as solar heat, ground heat, water flow heat, water flow for condensation purposes, or the inconvenience and capital cost of a cooling tower. Although the latter in cornbination with the process under PA 8728601 and as discussed therein would be a further approach.However, in contrast the process under discussion would only require simply

air compression equipment again. Of course, we come back to the question why not simply pump water and purify or desalinate if required, but I'm envisaging a future of perhaps the human race being able to control the weather of the Planet moreso, and especially so and/or simply on a localised basis over targeted regions of a country where there may be a highish atmospheric humidity but where Nature doesn' t normally send any cold air along to precipitate these days, but perhaps in the past when such regions invariably use to be forested. Deuteronomy Chap 20 V 19. Such high humidity levels exist all around the coasts of Africa, the Countries of the Middle East, India, Australia, South America, Central America, etc., and indeed between the tropics in general.Simply resulting from the Sun beating down on the surrounding Seas all day long evaporating, and in the process desalinating, sea water.

Which however, apart from in their rainy seasons, generally remains as unprecipitated water vapour in the atmosphere until it travels either north or south and meets the colder polar airs travelling in the opposite directions. Usually precipitating over Manchester, so in that respect Manchester acquires some of the good work of the hot Sun of the tropics. However, how far inland such high humidity levels extend over arid and desert lands I'm not sure at this stage. Thus, with such a project it would be better to commence fairly modestly on the coast of a Country with vast potential for this type of develop'ment and see what develops in the fullness of time.One region of very high humidity that I have been subjected to in my life where the land is desert and arid and where a PRR and CS Plant would raise their Civilisation level no end is Djibouti, and another being along the desert road from Port Said to Cairo. However, I think the Rain Twwn approach as discussed under PA 8728601 would be one of the better ways forward for such development and for the human races to take into the future as they determine and mould their own future destiny via the leadership of their respective Governments with the help of others of course, in true Christian Spirit as it were.And therefore the first way forward may be via the PRR, CS and Big D Plants discussed under the above PA, although to the process under discussion could also become added a desalinisation, i.e., a Big D, capacity. Which could be achieved by using a proportion of the power to boil sea water via an electric element, as in electric kettle, then condensing the steam produced via the cold liquid phase of the refrigerant of the process to further add to the absorbed heat from sources other than the ARC cycle and thereby further improve upon the overall energy of balance of the process. Since the latent heat of water is 540 cals per gram at the phase change from liquid to steam at 100C then one would recycle most of the energy if all the latent heat of condensation became placed back into the process then the heat of the water liquid phase produced back down to ground state, as it could very readily be. Not only via the heat absorbing refrigerant of the process but also via one of the expanding air stages, which would probably best be the second air expansion although not necessarily. Thus in such ways one could achieve a PRR, CS and Big D. Plant via the process under discussion and perhaps in a better and more convenient way, although not necessarily.

Therefore, really what is required now are more calculations around the three main approaches to Rain Towns and a detailed costing of a Plant of sufficient capacity for a Rain Town in parallel with some practical experimentation on the processes, bearing in mind that they won 't need to be perfected in the beginning but could become so over the next blillenium. The three main approaches for a Cote de la Rain Town via plant with the capacities PRR, CS and Big D being: - 1) Via the process under PA 8728601 and via the ways therein discussed.

2) Via the process herein under discussion as combined with an ARC cycle and further air compression equipment via the ways being discussed.

3) Via the process herein under discussion as combinable with natural flowing water heat and the various approaches discussed.

Obviously all with further and/or additional variations possible, and more detailed calculations should point towards the better ways more accurately,coupled with some experimentation in parallel to test some of the basic fundamentals on which the processes depend. Which however are only a few, but probably it would be more realistic to think in terms of a further 10 year programme to achieve a stage of actually having a Rain Tawn in operation via one or other or a combination of the three main approaches under discussion. Following which they would no doubt mushroom all over the Planet, but in any case such a programne with such a goal would in the process bring into operation a large slice of the technology with many other applications in many other fields, e.g., as for Mills.And especially so if the aim was for a blockbusting PRR, CS and Big D Plant. When in the fullness of time just one spin-off could be that Big D Plants could generally become a main means of water provision to national water grids. However, returning to the main topic under thlsparticular heading, i.e., that of producing a Power, RainMaking, Refrigeration and Cold Store Plant running on nothing but and requiring nothing but Thin Air at the Plant site, although hopefully also with a reasonably high humidity level in the surrounding atmosphere and hanging over the surrounding growing fields.The finally concluded potentially better approach via combining the process under discussion with an ARC cycle and further air compression equipment linked to the turbogenerating part of the process may have become a little confused and therefore, briefly recapping on the general arrangement concept since I think it could become an important way. As follows : - 1. Firstly the process would be combined with an air ARC cycle, the heat of compression of which being the heat source for the process.

2. The power from the turbogenerating part of the process would then be used to compress further air. In the preceding I then placed the heat of compression produced into the heat absorbing refrigerant in order to reduce upon the ARC cycle capacity and therefore on its 40% shortfall. However, the energy of the resultant cooled compressed air from this air compression was estimated to still be barely sufficient to make-up the short-fall in the smaller ARC cycle, and certainly without leaving a surplus of power remaining for output supply.

3. Therefore, the above cooled compressed air became used to compress a second quantity of air and the heat of compression produced became recycled back into the air expansion of the first quantity of cooled air, which should at least double the energy of the first quantity of cooled compressed air and therefore also of the second quantity of cooled compressed air. Which should then be sufficient to make up the short fall in the ARC cycle whilst leaving some over for output supply.

4. In such a method of operation, whilst the ARC cycle would be reduced by about 33g6 and therefore also the cold exhaust air yield from the ARC cycle, there would be a further large supply of cold exhaust air becoming produced on the expansion of the above second quantity of cool compressed air in this method of operation.

Therefore, whilst there could be other ways round of recycling the further quantities of heat of compression back into the process to improve upon its energy balance and output, e.g., all the further produced heat of compression could be placed into the ARC cycle itself to render isothermal and therefore self-sustaining as under PA 8728601, I think the above way could be the better approach to achieving the full range of a PRR, CS and Big D Plant.Not only because it would probably yield more very cold exhaust air since in the foregoing method of operation that from the ARC cycle itself would become destroyed, but also because placing the heat of compression from the second air compression back into itself via placing into the expansion of the first additional air expansion should prove a technique that should in itself improve upon the overall energy balance of the process which one wouldnt gain the additional benefit of if the initially produced second heat of compression was placed into the ARC cycle instead of into the expansion of the first additional quantity of air to then and thereby improve upon the second air compression energy yield. Therefore, to hammer this method of operation home a little more since it may prove an important method.

This Process is initially combined with an ARC cycle for heat provision. Then the turbogenerating part of the process is linked to a line of two further air compressions, in the above referred to as the additional first and second air compressions. The heat of compression from the first is used to reduce the ARC cycle capacity further, but the heat of compression from the second is continuous recycled around the line of the two additional air compressions linked to the initial turbogenerator power, and this should then prove a way to produce sufficient power to make up the short-fall in the ARC cycle and leave a surplus for output supply perhaps at around the 10% level when relating to the preceding estimations.

But of course this is based on a process where it is being assumed that the su > system-compressor cycle would be just self-sustaining. Which however could well be the case because these estimations are also based on a process where the fluid to the sbsystem wc)uld still be in a high energy state, i.e., as in state E on Fig. 2. However, obviously there could be many variations and one to boost the power could again be that of rendering the expansion of some of the cool compressed air isothermal by use of surrounding natural heat, as required and/or desired. Moreover, I may have fallen short since if one placed a third air compression after the line of two air compressions linked to the turbogenerating process, then the increased power yield of the second air expansion could alone produce sufficient heat of compression in the third air compression which when placed into the ARC cycle just rendered it fully selfsustaining, but one would be left with the whole of the cooled compressed air from the third air compression for power production for output supply and the cold exhaust air produced for RainMaking. Perhaps some of the Power becoming used for a Big D operation, all of which should be recoupable by placing the heat into the ARC cycle which would convert heat back to power with approaching 100% efficiency. Etc., etc., etc., ad infinitum until the end of time. Enough of everything to keep everybody busy and happy over any one and every 70 year lifespan from here to Eternity.

Thus, perhaps the basis of one of the better ways to create RainMaking capacity from nothing but fairly average Plant and Thin Air, and fairly readily yielding the bonuses of power, refrigeration, cold store and Big D capacities in the same process.

a little more since it therefore may be important.

The system of a line of air compressions in which the cooled compressed air from one goes on to compress a further amount of air next in line I have referred to in the work as a Multi Air Compression Heat Processor or a MAC Heat Processor for short. Therefore the basic general arrangement concept for the Plant would be the Process combined with the ARC cycle and the turbogenerating part combined to a MAC Heat Processor which so far would have 3 stages. But then what if one kept on adding a further stage in combination with recycling the heat of compression produced back into the air expansion of the preceding air compression that is bringing about the next in line air compression.If one didn 't recycle the heat of compression back into the preceding line of air expansion one would obtain diminishing returns at each stage in the MAC Heat Processor. But if one does then one should obtain increasing returns at each stage. Which don't have to be all that increased each stage to soon build up sufficient power for the needs of the process and for output supply. Therefore, we can perhaps now contemplate also being able to make up a short fall in the sub-system energy by such a means. But of course more air compression equipment would be required with each extra stage one added to the MAC Heat Processor.However, I really do think now that this could be the way and progressively increasingly so, when the Power and Very Cold Exhaust capacities from the Plant Complex would now be more from the last stage in the MAC Heat Processor, rather than from the initial ARC cycle and/or the initial turbogenerating stage. Thus, a little like roses growing on one but I think sufficiently now and sufficiently in the right directions to progress on to a further stage of more detailed calculations, perhaps leading to practical working models of the process in this manner of operation.Then in ongoing development the more perfected the various systems of the overall process and Plant complex becomes the less air compression equipment required, but in the beginning then it follows that even if the sub system energy falls short by half the process could still be rendered successful by adding further stages to the MAC Heat Processor comprising more air compressic each stage. And all the time whilst trying to make sufficient power for the process and a surplus one would probably be increasing upon the very cold exhaust air yield from the process for the two RS and CS functions.While a Big D capacity could perhaps be added for very little consumption of power in the overall energy balance of the process if indeed any since a further way to a Big D capacity would be to boil sea water with one of the heat compression yields at lATS and 100 C, i.e., simply to produce steam which when condensed becomes pure, clean, water. Then place the heat of condensation and heat down to normal temperature into the same stage of the process where the initial heat of compression was destined, which should be the same amount of heat and therefore a Big D capacity would have become added for nothing but some water boiling equipment.

It follows that the whole Plant Complex could become one Giant Big D Plant applying all the heats of compressions, wherever they may be destined, first in such a way. Then applying the heat of condensation and temperature down to ground state of the resultant steam wherever the heat of compressions was destined for in the process.

This then would moreso justify a number of increasing stages of air compression equipment in the MAC Heat Processor line. Because the more air compressions then the more the total heat of compression yield from the Plant Complex and the bigger the Big D capacity of the Plant would becoxne. But remeiriber also the bigger would be becoming the RainMaking, Refrigeration and CS capacities and the more likely the Plant Complex would be yielding a surplus of power whilst fully sustaining the ARC and subsystem cycles.

Thus, one could regard the Plant Complex as a Big D Plant with most of the heat of compression becoming produced therein becoming usefully used for the Big D function, but then the heat going on to give all the other potential capacity.

And the bigger the Big D caoacity then the more likely the other potential capacities would be possible, and indeed the process in the first place.

Thus, again more of the 'Growing Roses Process, but I think to an even more very useful stage now. However, that seems like an end and, therefore, progressing on now.

The Process as corribinable with Direct Solar Heat It would of course be possible to apply direct solar radiation as the heat source for the process since matt black pipework acting as a black body solar heat absorber and carrying the heat absorbing refrigerant within could render the process very conducive to such a manner of heat provision. However, whilst the efficiency of the system could potentially be appreciably higher than as for current solar cells the process would nonetheless still require a very large surface area for very large power production and of course cloudless blue skies, and therefore I think this method would become Tnoreso one for application in Space.Although not necessarily, and perhaps especially if in combination with the method of concentrating the Sun's radiation onto a smaller area via mirrors in suitable sites, e.g., Arizona style canyons in the hot Sun from dawn to dusk with Mountain ranges on either side, which are similarly present in many of the hot arid Countries of the World.For example. as in the Abvsinian mountain ranaes in Abvsinia.

However, woula one nave to use expensive mirrors, or woula/a night gloss rerlecting white paint suffice on suitably shaped and sufficiently large surrounding boardings appropriately directing the Sun's rays onto a concentrated area in the green valley below. Remember, current mirror systems concentrate the solar radiation over a very small area to achieve very high temperatures i.e., 600-10000C.

Whilst here the absorbing refrigerant would be at 90C if R-21 throughout this stage and therefore one could apply the heat over a much larger surface area and achieving lower temperatures, albeit smaller surface area than one would require if just harnessing the solar radiation as it comes from the Sun. However, considering the possible efficiency and required surface area of heat absorbing unit for the latter method of harnessing the solar radiation in such places on Earth, whilst perhaps mainly having in mind this method for application in Space where via satellite mirrors one could similarly add the solar heat over a more concentrated area if for an orbiting Space Station and the like. Moreover, I am given to understand that the Moon can be very hot from Solar radiation during the day and very cool during the night and hence perhaps an approach suitable for Moon Development on a large scale.

The normal rate of Solar radiation as it comes is 1.41KW/M2, ref: - Encyclopaedia Britannica. Vol 20 p854, which presumably would be higher in Space since the above figure refers to the heat reaching the Earth, after some having been reflected and some having been absorbed by the atmosphere. Therefore for Space one could probably base on say 2KW/M2 in the absence of more accurate knowledge, and for convenience I will convert the value of 1.41 KiV/M2 to 1.31 KW per 10 square ft.

Based on preceding discussion this process could have an efficiency conversion rate of 20% with respect to the total heat being absorbed each cycle if the sub-system is fully self-sustaining. But if the latter is not the case then this efficiency value could become as low as 10% On the other hand, I think readers would agree that there could be the potential to improve to a maximum of say 30% via perfection of the various systems contained in the process.

However, initially there would of course be a way to improve upon this efficiency value, i.e., via the method of recycling the unused latent heat from the turbogenerating part of the process back into the absorbing refrigerant of the process, which should improve upon surface area required to give a certain output level and therefore let us see what the surface area would be for such a method of operation assuming the 20% level in the first place in co'mparison with the surface area that would be required for the same output via normal solar cells.

For this again considering the cycle for the process based upon R-21 as on Fig 2.

The 20% conversion level would yield 48 KJ/KG for every 240 KJ/KG of heat absorbed.

All of whichXhowevertwill not be provided by the solar radiation if the latent heat from the turbogenerating process is becoming recycled, as it would be, and as in the estimations in the preceding section would become reduced by 65KJ/KG to 175 KJ/KG. Therefore, one could base on an efficiency of 48 KJ/KG for every 175 KJ/KG of Solar radiation, i.e., an efficiency level of 27% Which then could have the potential to become improved to around 40% via perfection of the systems of the process. It follows therefore, that these are the estimations that would generally apply for the process combined with the other sources of heat.

Thus, basing on the value of 1.31 KW per 10 square ft., and an efficiency level of 27% conversion the heat absorbing surface area required for several capacity levels would be as follows.

10 KW - 286 square ft, e.g., 20ft x 14ft 100 KW - 2860 " " " 50ft x 57ft 1 MW - 28600 " " " '100ft x 286ft 10 MW - 286000 " " " 500ft x 572ft 100 MW - 2860000" " " 1500ft x1906ft

Thus the method could certainly potentially be a way to generate power for small capacity processes for domestic application and fo-r small farming and market garden ventures and the like. For example, one can envisage that the whole roof of a house in hot countries could be covered with the heat absorbing pipework carrying the refrigerant of the process, which in the process could keep the interior of the house cool since the latter would be under the temperature of 90C.

And the estimations would seem to indicate that one may be able to generate up to 100KW via such a means during the day which should be ample for the domestic and carnercial needs of say a small market garden and/or horticultural venture.

While the efficiency of solar cells are of the order of 10% and therefore the same surface area would only yield 37 KW in comparison. However, it would probably depend upon comparative cost and indeed on the lucrativeness of the commercial venture since such a process could be fairly expensive, albeit once installed then freely providing power. However an advantage would be that the heat absorbing refrigerant could be piped through a cold store at little extra cost, and refrigeratic could fairly readily be facilitated via using a small proportion of the power to make up the energy short fall in an air ARC cycle, the heat of compression of which could readily become removed via the heat absorbing refrigerant, which then and thereby would render the accessory of a small ARC cycle easy to apply for accompanying refrigeration and cold-store functions.An ARC cycle being an Air Refrigeration Cycle as applied in aircraft for example where the heat of compression can and does become removed via ram air. When in production such a process installation would possibly be around the 50,000 level as combined with a battery storage facility. Thus, beyond the reach of most, but for some fruit and vineyard ventures for example then such a method of application of the process could be an attractive proposition, especially with the cold store and refrigeration potentials for the process. But of course it would also depend upon how reliable the Sun source of heat was at the desired site of application.

While for poorer folk then I am hoping that the process under PA 8720291 could be the basis for units that could retail at 1000 per 1OKW capacity.

To give people the opportunity to more easily eam some of the World's wealth, re-recent Christian Ajct Bill Board advertisement - & April '88, and that of Cape Grapes around the same time to give a good example of what I have in mind The Process corribined with Wind Power: Whilst one perhaps wouldn't it follows that one could place the heat absorbing unit of the process in the pathway of winds and extract the heat from the natural flow of air similar in concept to extracting heat from natural flows of water.

When extracting 50C of heat from a wind travelling at 20 mph over a lOoft x lOoft surface area of the wind at the 27% efficiency level could yeild the following amount of power.

20 mph = 30 ft per sec Volume of air per sec.

= 30 x 100 x 100 = 300,000 cubic ft.

Heat capacity of air = 1 K7/KG/ C at NTP Density of air = 1.22 Kg/m3 at NTP Total wgt. of air per second = 3000,000 x 1.22 = 10365 KG 35.31 Heat extracted per second = 10365 x 1.50C = 51825 KJ/sec Converted at the 27% efficiency level = 13992 KJ/sec = 13992 Klthr 1. 1.4 .NStr Which compares with 300-500 KhMr capacity for the wind generators referred to in the Guardian 24th March '88 page 4, 100 ft in height and of 100 ft blade diameter.

Which in turn coincidentally is of the same order of difference obtained in the preceding in the comparison for Solar heat between the process and solar cells, i.e., around 3 times better with potential to become 5 times better. And if lO0C extraction was achievable via use of say Refrigerant R-114 of Bpt. 3.70C then these factors would be doubled in the case of wind heat, i.e., potentially 10 times better. However, the heat collection unit would also have to have some depth, although could be appreciably shorter than the Sea and River Units for 50C and 100C heat extraction because of the lower heat capacity of air in comparison to water and would probably be in this ratio, i.e., 4 times shorter due to the transference of a given quantity of heat reducing temperature by 4 times.

Which would be an aspect that could potentially be very much improved upon via use of a material with a far higher heat conductance, e.g., potentially an 8 times factor improvement based on known data. However, the unit would probably have to revolve in order to be able to face into variable direction wind.

Thus, perhaps a method of application to consider in the future but probably not a starting point for the initial development of the process, which should probably be Big D Plants with the added capacities of Power RainMaking, Refrigeration and Cold-Store; Ships propulsion; Power Ships; River Plants; Fixed Tidal flow Plants; Power Bridges; Road Transport propulsion; Earth Solar Plants; Space Solar Plants; Moon Plants; Space Craft Plants, etc.

Advanced Brierley Process: This is the Advanced version of the Intermediary Brierley Process under Patent No. 2141179 and possesses two main advancements, as follows: A. The system herein comprising the sub-system - compressor cycle which is placed after the turbine stage of the main process for the sole purpose of then being able to compress the exhaust vapour back up ,to a sufficient pressure in order that a high proportion of the latent heat contained therein becomes rendered recyclable back into the heating fluid in the way discussed under the Patent, whilst at the same time leaving sufficient heat in the condensing vapour so that when the fluid goes on to pass through the sub-system hopefully sufficient energy will be yielded to fully sustain the continuous operation of the compressor of the cycle, whilst the fluid itself will then exit from the subsystem stage as a cold liquid ready to commence the next cycle of the process in the turbogenerator. Of course, one doesn't get something for nothing, but remember that the general concept here will be that the sub-system - compressor cycle will continuously recycle its own energy of compression to sustain the continuous operation of the compressor, to leave remaining all the thereby upgraded latent heat energy of the exhaust vapour for recycling back into the heating fluid. In other words, in theory at least one shouldn't necessarily have to consume a high proportion of the latter energy for the operation of the compressor-sub-system cycle each cycle of the main process.Or, to put another way, the heat of compression energy that will add to the vapour on compression will also add to the heat energy already contained in the vapour by a corresponding amount, and the continuous recycling of the added compression energy by definition will be that amount required to become continuously recycled to fully sustain the continuous operation of the compressor - sub-system cycle. Which are observations that generally apply to the cycle in whatever process of operation. However, there is then the effect of fluid contraction to consider, probably giving rise to a pulling of the punch effect and thereby detracting from the energy yield at the sub-system turbine.

Therefore, again it will obviously be necessary to maximise upon the energy balance at the sub-system stage and at this distance from the main nitty-gritty herein it can more clearly be concluded that a main way to achieve this will be by adding the BGS energy contained in the fluid all the way down to Absolute Zero to the energy yield via the application of the partial vacuum technique. To result in the liquid phase probably exiting at a colder temperature than desired for placing back into the turbogenerating part of the process, but the advantage being that one could readily apply surrounding natural heat to bring the temperature of the fluid back up to normal temperature en route to the turbogenerator, and moreover one could in the process apply the cold liquid phase for refrigeration en route to the turbogenerator.

The further aspect being that a full vacuum equivalent to 1 ATS. in the

isolation chamber of the sub-system would only require 25 feet of height of liquid phase to give the equivalent of lATS. pressure acting on the fluid at the turbogenerator stage again, and if the turbogenerator is placed upright then one can see that one could readily facilitate for such a height of liquid phase in such a way. However, this is taking the discussion into the nitty-gritty of the ABP-O which becomes fully dealt with under the appropriate file of my work.

It follows that in this process it would be particularly important to maximise upon the energy yield at the sub-system stage, otherwise one would have to consume much of the energy yield from the turbine of the turbogenerator in driving the compressor and therefore in addition to the partial vacuum technique it will probably be particularly necessary to apply all the other techniques in combination in the case of this process, whilst this may not be absolutely necessary in the main process discussed herein, albeit obviously better so to do. The other techniques being: 1) Minimising upon the r to the four retardation by maximising upon nozzle enlargement in the application of the fluid re cycling technique.

2) Coupling the fluid recycling technique with the air com pression technique as the means of effecting the fluid re cycling.

3) Maximising upon fluid streamlining under the application of the partial vacuum technique by: a) Firstly, appropriate nozzle shaping, particularly at entry and thereafter.

b) Secondly, application of a fluid stand-in technique in the nozzle, either via natural forces or added forces.

Thus, in the above manner it should prove possible to recycle the latent heat energy of the exhaust vapour without having to consume the turbine energy of the main turbogenerator. This being the basic objective which, of course, doesn't involve the mysterious addition of energy to the system apparently from nowhere, but in being able to effect the recycling of the latent heat in such a manner rather than discarding from the process then the fresh heat input required each cycle will be that much less for the generation of the same power. Which will be particularly important for heat input via the ARC cycle, because one would then require less ARC cycle capacity and the shortfall thereof will be easier to make-up via the turbine energy of the turbogenerating process whilst still leaving some over for output supply.

B. However, even the Advanced version of the IBP-O will still not work properly until a further failing has been addressed, this being associated with the fractional vapourisation technique inside the main turbogenerator and to render fully workable in the manner discussed a further piece of equipment becomes added to the basic system in the Advanced version of the process. This being the addition of the Space Energy System of the work to the exhaust side of the turbine of the turbogenerator in order to better draw the vapour is ing fluid flow along the central flow, to in turn better create the desired low side pressures acting on the vapourising cavities of the fractional vapourising system.

The concept here being that the extra energy that the operation of the SE System will add to the turbine energy yield would become continuously recycled to maintain the continuous operation of the SE System, ad infinitum. Thus, again no energy gain but simply being a means to improve upon the working of the fractional vapourisation technique inside the turbogenerator in the first place. However, this again is nitty-gritty that becomes fully discussed under the ABP-O file of my work.

Application of the Sub-System - Compressor Cycle in Conventional Turbogenerating Processes: The Advanced Brierley Process, i.e. ABP-O, may in fact be purely academic, because I think one could apply the sub-system - compressor system to existing turbogenerating processes in a similar manner, the nitty-gritty of which becoming discussed in the Alternative - P file of my work. However, this may not be so and, on the contrary, this

of the work could follow a development route which progressed from the application of the sub-system - compressor system in existing conven tional turbogenerators to application as part and parcel of the ABP-O in pursuit of higher efficiency and compactness, etc., i.e. for all the normal reasons for progressing processes, perhaps also coupled with the important reason of achieving more fulfilling science.

Although with further respect to the latter aspect I think on Earth this could in part become shifted to gaining control over and manipulating the parameters of the Planet's weather via application of the technology with the shift into Space equally adding to such aspects.

Muof which may solely depend on the success or otherwise of the subsystem.

Therefore to round off the discussion, I pose the questions again, will it work and if so with what levels of expected success and how successful is it required to be in practice anyway? To answer the last question first.

If the sub-system only gave the mgh potential head energy value of the pressure head, which

ita at least be capable of yielding, then this could become the power output from the process with all the power yield from the turbogenerating part of the process beccming used to sustain the compressor, which it should at least be capable of doing. And especially so since under such conditions one would pre-remove as much heat as possible from the fluid flow to help render the fluid at ground state temperature and therefore in the liquid ground state so that it would behave simply as a normal liquid and just yield the normal ground state level of energy of the pressure head, i.e., its mgh energy value as in hydropower harnessing.But in removing such an amount of heat then one would be maximising upon the output from the turbogenerating part of the process.

Which could be maximised upon further by harnessing via use of a low Bpt fluid in the turbogenerator. For example Refrigerant -11 of Bpt 240C and as discussed under PA 8728601, which should be able to harness the heat all the way dawn to at least 1000C and probably lower to say 500C Then any remaining residual heat that may be desired to be removed before passing through the sub-system could all become removed via the refrigerant liquid phase of the process at the stage before it passes through the main heat collection unit associated with the main heat source of the process, along with the latent heat of condensation heat from the exhaust fluid of the turbogenerating part of the process, and to give somme similarity with the process under PA 8728601.Under such a method of operation then the turobgenerating energy yield Could be in excess of that to continually

sustain the compressor stage of the process but here' .{ conslaestnat it could just be sufficient,w ith the energy yield from the sub-system then able to become the energy output from the process.

The whole of the heat would have become removed from the main fluid of the process under constant pressure cooling conditions and therefore the fluid passing to the sub-system for all practical purposes would be a normal cold liquid in the normal liquid state under a constant pressure head, i.e., 100 ATS in the example under discussion. And as such should yield the normal level of potential head energy associated with the pressure head, i.e., its mgh energy equivalent.

Which should be an amount of energy some 15% of the preceding estimations where these were based upon the 20% leveland some 30% of the preceding estimations where these were based upon the 10% level of efficiency with respect to the total amount of heat being absorbed each cycle.

Therefore, it follows that the process ',,i'((work under such a method of operation and therefore should be capable of yielding at least the above estimated amounts of energy. Which in turn would still be a very viable level of energy output from the process and perhaps especially so if one considers this in relation to the Power Ship method of application. Albeit a 2000 MWhr Power Ship now becoming say a 350 'hr Power Ship, although with the higher level of latent heat that would then be becoming placed back into the system then for a given fresh heat collection unit size this comparison could well be to a 700 MWhr Power Ship.However, it follows that in the fullness of time it could become debatable which method of operation would yield the mst for output supply, since if all or most of the removed heat energy is able to become harnessed via use of a low Bpt fluid in the turbogenerating process at a fairly high level of one-pass efficiency i.e., as discussed under PA 8728601, then there could be a surplus of energy at this stage for output supply to add to that from the sub-system. And, therefore, the energy yield for output supply could become the same whichever way round one operated the process.

Furthermore, it follows, that the sub-system may not in fact be required to work after all since there could become sufficient energy left from the turbogenerating part of the process after sustaining the compressor stage for a worttthile output supply. All of which in turn perhaps poses the further question, have I approached the process in the wrong way to date? Perhaps, but via the way that I have approached the process to date I have evolved and examined the potential for harnessing the heat energy content of a hot liquid under a pressure head in my own way, which at the least may be useful background if one wished to harness residual heat left in the fluid after the turbogenerating stage rather than recycling back into the heat collection unit, and at the roost could in fact be the better way to maximise upon the total energy yield from the process potentially leading to a whole new field of applied technology with endless possibilities for the future. Which in fact is what I really think may be the case, at this stage anyway, as I hope I have managed to demonstrate)

to render the technology really successful then it would be necessary to maximise upon the nett energy yield from the basic process and probably the better way to achieve this would be via maximising upon the energy yield from the sub-system and such that the heat energy becomes harnessed all the way down to at least qround state with

at least a 40%1efficiency. Which I don't think would be possible via just the turbogenerating process.Then I hope I have demonstrated that in a number of ways it could be possible to improve upon the energy yield from the sub-system by applying one or other or a combination of the techniques to add bonus energy at this stage in the process. Slhílst in the first place to maximise upon the normal energy yield from the sub-system just down to norrnal ground state it may be necessary to corrrnence with the fluid in high and hot energy state E where the fluid would still be behaving as a vapour. Although not necessarily, but if so then the work herein would become more useful and be more applicable.

if one considers further the energy cycle on Fig 2 one can see that in fact for a turbogenerating process one-pass efficiency of 40% then the heat would have to become harnessed all the way down to around 30-400C for the energy yield to sustain the compressor, and therefore one would need at least the mgh energy value of the pressure head to give a surplus of energy for output supply because even if the turbogenerating part of the process harnessed an absolute maximum of the heat energy it may in fact only just be sufficient to fully sustain the compressor stage of the process which would still be compressing the same amount of vapour phase each cycle with the higher level of latent heat becaning recycled each cycle. Which would then leave at least the mgh energy value of the pressure * head, as would be given by a cold liquid, for output supply. Which then poses the question, why does the energy balance become very much improved upon via harnessing the energy of hot fluid in the sub-system at the expense of energy production via the turbogenerating process since surely this would be as broad as long wouldn' t it? I think this is simply because the heat energy should become harness all the way down to the ground state of the energy cycle if one managed to harness heat energy in the sub-system in addition to the normal

mgh energy that would be given by cold liquid. But then to achieve this it may prove necessary to canmence with the fluid in high,hot, state E. Then we are back to the work herein being more useful and more applicable.But I don't know and its difficult to come to firm conclusions on this aspect at this stage.

However, it follows that the process purely for power production would still be very useful and very worthwhile even if the output from the process was only that of the normal mgh energy value of the pressure head as should be obtainable via the cold liquid phase. Which should at least be obtainable since surely a maximised yield from the turbogenerating part of the process would be expected to at least sustain the compressor stage of the process cycle, i.e., the energy input from B/C to D'. Therefore the process should at least be worth pursuing further for such a very possible and feasible method of operation yielding a very worthwhile amount of power.And especially so since the higher level of recycling latent heat from the turbogenerating process would be reducing further the required size of heat collection unit. Then from

and more certain position one could progress on to exploring the fuller potential of the process as discussed and outlined herein. Which in retrospect may not have been necessary to have fully gone into at this stage since I could have just pursued the foregoing more simplified~ method of operation more fully. On the other hand, it is probably better to have explored the potential for what is probably the final facet of the processes being evolved in the total work at this stage and as embodied within the work herein, i.e., that of harnessing the heat energy content of hot liquid phase under a pressure head.Which was really my original thinking when I first approached this particular process concept.

However, the work should now be combined with that under PA 8728601 in order to properly determine the potential for the more simplified approach involving maximised heat removal and maximised power generation via the turbogenerating stage of the process and as should be achievable via the application of a low Bpt fluid in the turbogenerating process, e.g., R-ll as applied in the aforementioned PA. Although in the final analysis probably only practical application will determine the better way to approach the process, which again formed a part of my initial thinking and that it would, therefore,be better to explore the potential for the sub-system at this stage and especially so since the system applied a little of my particular background experience i.e., that of fluidity testing on paper.

Thus, as a final comment and recoiTmendation, the process type would at the least

seem rejwortnwnile progressing to a practical development stage anc at the ZOst would seem the foundation for a whole new industrial, technological and scientific era leading to higher levels of civilisation being achievable in many of the basic and not so basic areas of our ascending civilisation here on the Planet. Who can say, perhaps leading to the creation of Heaven on Earth being more readily achievable in the ways that I have tried to indicate. Ref. 'The Lords Prayer'.

Other Bibliography referred to herein: 1. Principles of Physics, 1958, M. Nelkon.

2. Physics for ONC Courses, 1970, Edwards.

3. Principles of Refrigeration,. 1961, Roy J. Dossat.

4. Refrigeration and Air Conditioning, 1958, W.F. Stoecker.

5. Elementary Rheology, 1969, G.W. Scott Blair.

6. Viscosity and its Measurement, 1962, Dinsdale & Moore.

7. The Liquid State, 1966, J.A. Pryde.

8. Essentials of Engineering Fluid Mechanics, 2nd Ed, 1966, Reuben M.

Olson.

9. Introduction to Fluid Mechanics, 1966, Henke.

10. Thermofluid Mechanics, 1966, Pefley & Murray.

11. Aerodynamics - The Science of Air in Motion, 1963, John E. Allen.

12. Mechanics of Flight, 1972, A.C. Kermode.

13. Fluid Mechanics, 1979, Frank M. White.

14. Concise Physics, 1962, R.B. Morrison.

15. Heat Engines and Applied Heat, 1966, F. Metcalfe.

16. General and Inorganic Chemistry, 1959, P.J. Durrant.

17. How it Works - The Locomotive, 1968, Ladybird Books.

18. Roget's Thesaurus, of Synonyms and Antonyms, 1972, P.K. Roget & J.L.

Roget & S.R. Roget.

19. The Choice English Dictionary, Purnell.

20. The Mcgraw-Hill Encyclopeadia of Science & Technology.

21. Thermodynamic and Transport Properties of Fluids, S1 Units, 3rd Ed, 1981, G.F.C. Rogers & Y.R. Mayhew.

22. Thermodynamic Tables in S1 Units,.2nd Ed, 1972, R.W. Haywood.

23. Thermodynamic Properties of Fluids and Other Data, 1970, Y.R. Mayhew and G.F.C. Rogers.

24. Science and the Planet Earth II: Problems of Survival, The Open University, S101 Unit 32, Science: A Foundation Course, 1979.

25. 8 Energy 9 Light: Waves or Particles, The Open University, S101 Units 8 & 9, Science: A Foundation Course, 1979.

26. Admiralty Tidal Stream Atlas: NP 218: North Coast of Ireland West Coast of Scotland, 1983.

NP 251: North Sea Southern Portion, 1976.

NP 264: The Channel Islands and adjacent Coasts of France, 1977.

The Isle of Wight.

27. Logarithmic and Other Tables, For Schools, 1963, Frank Castle.

28. Handbook of Chemistry and Physics, 68th Ed, Weast.

In particular: Physical Properties of Fluorocarbon Refrigerants, E-32/3.

Viscosity: Water, F-39, Carbon Tetrachloride, F-41.

29. Pressure-Enthalpy Diagram For Refrigerant - 12, 1977, D.C. Hickson and F.R. Taylor.

30. Pressure-Enthalpy Diagram for Ammonia, 1978, D.C. Hickson and F.R Taylor.

31. Crudens Complete Concordance to the Old and New Testaments and the Apocrypha, 1737, A. Cruden.

32. A Solar Pond Power Plant, Ormat Turbines. Dead Sea Works, Israel. IEEE Spectrum, February 1981, Yehude L. Bronicki.

33. Deep Ground Coil Evaporators for Heat Pumps, Dept. of Mechanical and Industrial Engineering, Queens University, Ashby Institute, Belfast, Northern Ireland. Applied Energy, 1978, J.R. Goulburn and J. Fearon.

34. Biogeography An Ecological and Evolutionary Approach, by, C. Barry Cox & BR< Peter D. Moore. 1973 - 85, 4th Ed.

35. The GAlA Atlas of Planet Management, by, Norman Myers, 1985.

Combined Nozzle Systems.

This addition to the basic patent application is concerned with the fluid recycling technique coupled with the minimisation of the r to the four element in the system, as firstly becomes discussed on pages 132 to 144 of the original patent application, and more specifically is concerned with combined nozzle designs aimed at simultaneously maximising upon potential sources for increased energy yield at the sub-system stage via means of the fluid recycling technique. Extra drawings associated with this addition are given following under Figs 9 to 12.

The basic concept of the first design, which becomes depicted on Fig 9B, is one of placing a nozzle inside a nozzle with the recycling fluid flowing through the inside nozzle and within the combined concept there are a number of basic scientific principles involved and applied but the first basic aim of which being to facilitate for the return of the recycling fluid back into the fulid flow with as little resistance as possible and, therefore, requiring of minimised energy to recycle apart from the basic amount required to pressurise and heat the fluid to the conditions of the fluid flow into which it is being returned.Then if this is achievable via this design of combined nozzle system it should also prove possible to maximise upon any energy advantage that could potentially become achievable by increasing upon the quantity of the recycling fluid w jto thereby facilitate for increased nozzle CSA to in turn thereby minimise upon the r to the four drag element on the forming fluid jet and more specifically on it's linear velocityiheflinso doing one could also thereby maximise upon the resultant cold air capacity via such an additional route should the air compression technique be being used to recycle the fluid.

However, before discussing this combined nozzle and the principles thereof in more detail, at this point I will recap on the basic principles involved in this source of potentially possible route to BE since there are two basic aspects involved and it is important to clearly discern the two, with one aspect or view perhaps being more certain than the other at this stage as a potential source for some energy advantage.Moreover, this further discussion will help with the understanding of the basic principles of the combined nozzle systems

Thelbasic principle of the potential source of energy advantage via the fluid recycling technique and within which are embodied the two aspects arises from the fact that if one increases the fluid flow through the nozzle by means of continuously recycling surplus fluid over and above that continuously becoming fed from the compressor then the larger combined flow will be able to flow through the nozzle at a faster rate than could just that fluid becoming fed from the compressor for a mass flow rate through the nozzle at unity with the mass flow rate from the compressor.Thus, the principle being that a given mass flow from the compressor and then through the nozzle should be able to flow at a higher velocity through the nozzle when combined into a larger flow because it will then be associated with an r to the fourzeFlement which doesn't slow the fluid jet linear velocity down as much as the same element would if flowing alone and not inside the larger flow. And, therefore, the fluid flowing from the compressor should then and thereby possess higher kinetic energy of forward motion at the sub-system stage than it would otherwise do if flowing alone.

To demonstrate this, repeating here the exercises in which the nozzle CSA is first reduced to give a mass flow rate of unity with the compressor when flowing alone, then increased to a CSA 1.5 times that which would give the flow rate of 4.5 volume units for a larger combined flow comprising a proportion of continuously recycling fluid, as on pages 132/133 and 136 respectively of my original text.

Basing on a CSA of 1.0 for the volume flow of 4.5 volume units, then reducing the nozzle CSA to give the volume flow rate of 2.5 volume units to then and thereby give the mass flow rate through the nozzle at unity with that from the compressor which would be the conditions necessary to maintain the fluid flow pressure at that required to be maintained by the compressor.

Thus for a CSA equal to 1, r will equal 0.564 and r4=0.101, and the volume flow rate would be 4.5 volume units.

Therefore on reducing the nozzle CSA to give the required volume flow rate of 2.5 volume units and on equating the respective fluidity equations the following will apply:4.5 = 2.5 0.101 small r4small = 0.0561 r small = 0.487 nr2small = 0.744 Therefore, the forward linear velocity of this flow would then be given by:2.5 = 3.36 velocity units 0.744 - Whilst had the nozzle CSA been maintainable at 1 then the forward linear velocity would have been:4.5 = 4.5 velocity units Within which would have been the mass flow from the compressor and, therefore, we are beginning to see this potential source to BE.

However, 2 volume units containing 0.8 mass units with respect to that from the compressor would require to become continuously recycled in such a case.

Now increasing upon the nozzle CSA to 1.5 times.

For a nozzle CSA 1.5 times then the radius dimension would become O.69 and the r4parameter 0.227. Therefore, in this case the following would apply:4.5 = Vlarger 0.101 0.227 V larger = 10.1 volume units The mean fluid jet velocity would then be:10.1 = 10.1 = 6.75 velocity units mr X 1.496 Within which would be the 2.5 volume units of fluid flow from the compressor but now 7.6 volume units would be required to be continuously recycled containing 3 mass units compared with the 1 mass unit contained in the 2.5 volume units passing around the full circuit.

The kinetic energy of forward motion of the fluid jet before impact, and before the fluid contraction detracting effect, would be given by the equation: EV Therefore, one can see that this energy quantity would increase in direct proportion with increasing mass, and have a velocity squared relationship with increasing velocity.

Therefore, the higher the linear velocity of the fluid jet can be caused to become via such a means then the higher would be the energy yield per unit mass since the contraction effect should detract from the energy yield in similar proportion, eg, reduce to say 40% in both cases, and the mass required to be continuously recycled would be responsible for yielding it's own energy so to do.

Therefore, if the latter is achievable, which in part or wholly is hoped could be achieved via principles embodied within the combined nozzle concepts, then the other proportion of the mass would be producing more energy for input to the compressor than it could otherwise do if flowing through the nozzle alone. By what amount is a little difficult to estimate at this stage in the absence of precise knowledge in relation to the fluid contraction effect on energy yield, but suffice it to say it should be higher although perhaps not in the

ratio of the square of the velocity but couldlbe say 40% of such a ratio which. would then still be a high ratio. However, here I will base upon4tdirect relationship with velocity.Then basing on such a relationship the mass flow from the compressor could yield twice the energy when combined into the larger fluid flow than if one had to reduce the nozzle CSA to give a mass flow rate of unity with the compressor, ie, in the ratio of 6.75 to 3.36.

However, one wouldn't be able to recycle the surplus fluid with a 100 efficiency under normal circumstances, although in hydro storage schemes 90% efficiency is obtainable for the ratio of pumping energy input to elevate the water and the subsequent mgh energy output from the raised water.

Then, additionally there could be the fluid contraction effect detracting from the equivalent energy yield to take into account, which I failed to do properly in my original work. Therefore, one would almost certainly apply the air compression technique for the recycling of this fluid, although if the combined nozzle concepts do function as theorised may be possible then this may not necessarily be rulr but obviously could be applied to add further energy as a further source of BE. However, having said

toathe t,otal 1. , t haS rC'?w cre 1g kt: application of this technique may not give BE but just be a means by which the surplus fluid could be rendered wholly responsible for yielding it's own recycling energy.But the technique could give the bonus of very cold exhaust air for Rain Making and Refrigeration purposes. Moreover, one would wish very cold exhaust air to become yielded at and by this stage of the process for use in helping to create and maintain the vacuum of the Partial Vacuum Technique,~~~~ and the extra energy given to the system via the technique would very visibly be that contained in air from normal temperature to the very cold exhaust temperature.Nonetheless, a question mark here as to whether one would be able to add sufficient to the recycling energy via just this means, but if not one should be able to add further to the energy by rendering the otherwise adiabatic expansion of the cooled compressed air isothermal to double upon the expansion energy in such a way and remember for this the heat could be at the temperature of the environment and, therefore, should the process be extracting river or sea heat then it should be possible to apply more of the same heat source for this additional stage in the process.

But, of course, if the expansion is rendered isothermal then one would lose the Rain Making capacity and perhaps the Refrigeration although not necessarily and it would be even more possible to retain a Cold Store capacity.

Or it may be possible to render isothermal via applying otherwise waste heat at such a stage,etc.

Thus, perhaps the air compression technique could render the recycling energy fully sufficient when it may otherwise not be, although with respect to the latter thereare stilll3e principlesembodied within the combined nozzle concepts which could ensure the recycling energy was sufficient which I haven't yet discussed. However, continuing on with the discussion up to this stage.I think it would be reasonable to summate by stating that one is only endeavouring to render the sub-system-compressor system somewhere approaching a self-sustaining level in order for all or most of the energy yield from the other turbogeneratortobeavailable for output supply and for this one wouldn't really need to double upon the energy yield via the Sans anA principlesinvolved in the fluid recycling technique, albeit one perhaps could as shown by the preceding exercises.Then via a combination of all the techniques up to this stage, ie: (i) Increasing upon the fluid jet velocity via the fluid recycling technique which in comparison to the flow yielded by 4.5 volume units, giving possibly a just self-sustaining level assuming the 2 volumes of fluid to be recycled in such a case could be responsible for producing it's own energy so to do, could increase upon this energy amount by some 50%. Rather than otherwise having to detract from the energy if one had to reduce the nozzle GSA instead.

(ii) Addition of energy to the fluid recycling energy by an amount represented by that in air from normal to a very cold temperature.

(iii) Doubling upon the above energy under (ii) by rendering an isothermal expansion via addition of further environmental heat, again a very visible source for the energy addition. The energy under (ii) and (iii) together probably giving the equivalent of the original turbine energy but in the process also havi

a dCkd g/ tse equivalent in heat energy. Therefore after taking the fluid contraction detraction effect into account the energy required for recycling could be on the borderline even on adding (ii) and (iii) but perhaps not when one adds the surplus from (i), ie, that which would not then be required for the compressor input requirement.

(iv) Addition of the Partial Vacuum Technique which could increase upon energy yield by a further 50% but realistically by 20-30%.

When one would be able to raise the recycle part of the fluid back up to ground state via applying further of the environment heat before then raising to the pressure and temperature required via the air compression technique. And here one could also have further refrigeration capacity en route in-situ, whilst cold air could be piped further afield.

(v) Addition of the Mountain Technique which again could improve upon the energy balance anywhere from say 5-50%.

(vi) The higher pressure method of operation involving sweeping aside vapour.

(vii) Perhaps addition of the Fluid Stand-In Technique to the Partial Vacuum Technique.

Then it is my further considered opinion at this stage that one could perhaps thereby render the sub-system-compressor system self-sustaining, to leave all the energy yield from the other turboqenerator for output supply. But if not then a further technique that could be added would be that of the MAC Heat Processor

normal air compression technique being used to raise the recycle energy, firstly in order to increase upon the heat available for the heat input requirement and perhaps also to increase upon the energy available for repressurising, although for the latter one would almost certainly have to render the air expansions from one stage to the next in the MAC Heat Processor isothermal via adding further of the heat source heat.Perhaps to yield unlimited energy in such a manner since at each stage one may be able to increase upon the original turbine input energy still in the form of turbine energy via such a means, in addition to the heat energy also becoming produced each stage which itself could be used to generate more power as required. However, the process may yield just diminishing returns with respect to the turbine energy still in the form of turbine energy. However, it follows that this type of process as a process in it's own right could be all that is ever required. However progressing on with the current process under discussion.

Or a further and perhaps better method of operation could be to compress air with the energy from the other turbogenerator and add the heat of compression thereby produced the fluid recycling technique, when the proportion of the turbine yield from the sub-system available for recycling the surplus fluid together with this quantity of heat could be sufficient without having to go through the further air compression technique at this stage, although one could but one would probably have sufficient heat energy then and one would not wish to diminish the rotational turbine energy available.Then for output supply one would have a supply of cooled compressed air at or around normal temperature with which one could generate power, etc, the adiabatic expansion of which giving around 40% of the original turbine energy and the isothermal expansion probably around the same as the original turbine energy which again could probably be rendered isothermal via applying further of the natural heat source, but one may settle for the 40% level, in being far simpler and cheaper to acquire? And remember one would probably have fairly simply rendered the recycling energy sufficient via just this method of operation.

But if things still fell short there would be this potential in reserve. Moreover, one could extend upon the air compression technique at this stage also by adding several more stages to form the MAC Heat Processor. However, now progressing the discussion onto the second aspect of the fluid recycling technique combined with the combined nozzle technique which could lead to further BE and embodied within which could alone be a method by which the recycle energy produced by the recycling mass could be rendered sufficient unto itself, albeit perhaps better to be deemed doubtful at this pre-practical stage.

It follows from the preceding exercises in relation to nozzle CSA that if one increased upon the nozzle CSA even further involving the recycling of more fluid then one could thereby increase upon the fluid jet velocity even further. Which in turn would cause the kinetic energy of forward motion of the fluid jet to be even higher.Whilst in the original text, eg, as on page 137 lines 9 and 10, I inferred that perhaps this could give rise to a further source of increased energy advantage, ie, as distinct from that in relation to increasing the effective energy yield from the mass flowing from the compressor with the surplus mass being responsible for producing it's own recycling energy, I am in fact, and as implied by my added comnent in relation to plausibility, now more of the mind than perhaps inferred that the increased kinetic energy of forward motion of the surplus mass proportion would be all of that required to recycle the increased surplus mass bringing about the increase in kinetic energy because the

mass would still have to be recycled in unit time with respect to 1 unit of mass in 1 unit of time passing through the nozzle from the compressor.Which could still be alright since the surplus mass in the fluid jet Could at such a pre-impact stage possess sufficient energy of impact to yield sufficient extra turbine energy equal to the quantity that would be required to recycle itself in compliance with the laws of conservation of energy. However, and at this stage I am

considering the case where the fluid contraction effect may substantially reduce the pre-impact energy, which if so Could then also perhaps be in compliance with energy conservation laws since one would have increased the energy yeild of the mass flowing from the compressor quite substantially via the fluid recycling techniaue.

under certain conditions of combining the flows the contraction effect may not reduce upon the energy yield of the recycling fluid to the extent that it substantially reduces upon the energy required to recycle because it's pre-impact kinetic energy of forward motion could also become improved upon when as a part of the combined flowSdue to also becoming subjected to an improved r to the four element.Furthermore, on further thought one would probably more expect the recycling fluid to ostensibly yield it's own recycling energy, apart from inefficiences, in keeping with the laws of conservation of energy even if there was a substantial fluid contraction effect detracting from the pre-impact energy which, if so, would have to be correspondingly higher at such a stage. However, at this stage still considering that it may and/or that the shortfall in the recycling energy would be fairly substantial.

Whether one could apply the air compression technique stroke MAC Heat Processor to increase upon the reduced surplus energy sufficiently for recycling the fluid as in the preceding discussion would have to be ascertained but as implied above this may not be necessary so to do and perhaps especially when applying the technique embodied within the combined Nozzle concept, although probably one would apply both techniques because the air compression technique, perhaps extended to a MAC Heat Processor, would be a convenient way to yield heat for the required heating of the fluid whilst adding extra energy to the system and potentially retaining sufficient mechanical energy for the necessary pressurising of the energy which remember as a seperate component would only relate to the normal mgh value of the system. In the energy conservation law balance the extra energy that would and could thereby become added then equating to the increased energy yield being acquired via the fluid recycling technique which in turn would increase upon that available to fully sustain the compressor, ie, the objective. Which is energy that one couldn't add without the fluid recycling technique and perhaps the process wouldn't be possible without so doing, gaining some r to the four element advantage in the process, which is perhaps the better way round to look at the system up to this stage, although the energy could

transferred by virtue and means of a reduced r to the four drag force element on fluid jet velocity. With the system then and thereby coming into credit, etc, etc. In one view perhaps.However, whatever the view I think undoubtedly one of the main keys could be facilitating in the above way for the addition and conversion of a further quantity of natural heat source heat, eg, air and river or sea heat, to aid with this stage of the process, as distinct from that intended for output supply. Thus such a potentially possible way and associated view of the system perhaps adding up. But now we come to the technique that could be carried out inside the combined nozzle and which could potentially reduce upon the mechanical energy component required to pressurise and recycle the surplus fluid and is an advantage that may become increased upon with increasing surplus fluid recycling, although up to this stage one would probably tend to have the latter at an optimum minimum having regard to the foregoing discussions.

Thus now discussing the Combined Nozzle Systems in more detail, of which there are four basic designs with variations, but which all apply the same basic concepts, as follows.

A. Combined Nozzle - 1, Fig 9B: To recap, the basic concept of this first design, which becomes depicted on Fig 9B, is one of placing a nozzle inside a nozzle with the recycling fluid flowing through the inside nozzle.

The design concept has really been arrived at via a consideration of the system depicted on Fig 9A, which isn't a further design for possible use but simply a tear drop inside a nozzle serving no useful purpose other than to demonstrate the starting point for the Combined Nozzle system under Fig 9B. Thus it serves to show how a tear drop can be placed in the fluid flow from the compressor and fit snuggly into a nozzle, a tear drop shape being a shape of least resistance to fluid flow and indeed of minimal resistance. Then how by cutting it short at the end to an optimum length one can thereby create a Combined Nozzle of the type depicted on Fig 9Bnwhfchthe recycling fluid issues forth from the converted tear drop within the nozzle, with the fluid from the compressor still flowing around the now shortened and converted tear drop.

The main principle I had in mind when first designing this combined nozzle is the fact that if the fluid from the compressor is,being caused to smoothly streamline around the tear drop then theC,reercycling fluid on it's entry into the fluid flow from the compressor wouldn't have to'push'against the compressor pressure at all in order to get into the fluid flow and as would normally be the case if simply pumping the fluid into the fluid flow at some point before the nozzle stage and when one would expect the full amount of mechanical energy requirement to be required.Therefore, I think onecÇald gain some energy advantage by placing the recycling fluid in without having to pushagainst the compressor pressure in a comparison betweenthesetwo recycling energiesand since the former would be the normal level then the latter could be a reduced level of recycling energy compared to the normal level and with respect to the mechanical energy component thereof. Although perhaps only marginally bearing in mind that the pressure would only have to be the same for the recycling fluid to be able to combine, but perhaps a more substantial energy advantage could result as becomes discussed following.However, as stated, ~~~~ the fluid would of course still have to be at the pressure of the fluid flow, ie, as being created via the compressor, which would be achieved via the aperture size of the inside nozzle in the normal manner. Which of course would be a nozzle system that had it's own r to the four element but if for a flow three times the size of that which would otherwise be flowing through the nozzle then this could give r to the four advantage to the fluid flowing from the compressor on the combined flow through the combined nozzle. However, considering further the recycling energy advantage.

Should an energy advantage be obtainable in the foregoing manner then I think it could probably boil down to the fact that one would be returning the recycling fluid back into the fluid flow in a fully streamlined state and therefore the fluid mass one is returning will have a longer linear length in unit time of flow. Whilst in the normal system the same mass and equivalent dimension would be some 40% shorter because in the normal system the fluid would be still in the fully random state at the pumping in stage, albeit subsequently perhaps becoming as streamlined, but at cost of time and effort in comparison.

Then an accomDanvina advantaqe, or a component of the same advantage could arise from the fact

thátSide pressure of the fluid flow issuing forth from the inside nozzle would be very low, as in a water tap vacuum pump for example, and this could create a suction force to act on the fluid flowing from the compressor for an optimum design and conditions where the surrounding fluid at such a stage in the development of the fluid jet would otherwise perhaps be travelling at a

slower speed in the forward x-vector.Perhaps an apt analogous view here would be one of Freeway on-ramps on either side of a 3-lane freeway with the flow of cars on the freeway drawing the cars to a faster speed on either side which themselves have to flow faster to let in the cars on the on-ramps, or at least those ahead passing through the nozzle exit into the light of the Partial Vacuum Technique in the isolation chamber. A further system parallel would be that of a steam ejector vacuum pump. Certainly such an additional effect could help with the streamlining of the fluid flow from the compressor around the tear drop such that it presented no resistance at all to fluid flow, to leave the full advantage created by the forward dynamic pressure.The latter being a further and probably a better way of looking at this BE advantage in this case since one can see that the entry pressure on the front face of the fluid entering the fluid flow would be appreciably higher, ie, by some 40%, in the case of the polarised fluid having a high forward dynamic pressure at entry in comparison to the random pressure of the normal fluid and system at entry. For the same mass entering in the same time.

IVrawingaparallel witn the "propulsion via air power" project as under Patent 2126963B, as follows.

I think trying to reduce upon the r to the four drag factor via increase in fluid flow would be analogous, ie, not a direct parallel, to trying to reduce the drag forces on a vehicle. Then trying to obtain an energy advantage in the foregoing manner could be likened to applying the rear wake zone forces as distinct from simply trying to minimise upon them.Then an associated relatable parallel could be that this addition to my basic work could be likened to

my further deliberations contained in my correspondence to the Patent Office ot the 16th January 1986 in relation to the propulsion via air power project, which really contained my clearer breaking through thinking on that project after my thinking had crystallised and, therefore, perhaps the concept of the combined nozzles under discussion is a similar real breakthrough point on the further project under discussion herein. Although I think one would have to also add the air compression technique perhaps extended to a MAC Heat Processor to yield sufficient heat energy component, with the combined nozzle then making it more likely that there would be sufficient mechanical energy remaining.Which could be likened to progress from the SAT to the SEAT Process in the vehicle propulsion project, with the SE system of the latter being analogous to the Partial Vacuum Technique in the current process.

However, I think the system in the current process is still at the stage of an optimum minimum of recycling fluid probably being the goal essentially for the purpose of adding an optimum level of the energy of the air compression/MAC Heat Processor techniques to this stage of the system now with the aid of the combined nozzle technique, and perhaps only practice will reveal whether increasing advantage could be gained with and by increasing the quantity of recycling fluid.

Such an optimum minimum could be the level of 4.5 volume units involving the recycling of just 2 volume units or could be as high as the conditions on increasing nozzle CSA by 1.5 times ,ct;.

Such a minimum optimum would try to determine the optimum fluid recycling conditions between on the one hand, optimum fluid recycling for maximum further energy addition and maximum r to the four advantage with respect to the fluid from the compressor for maximum energy yield via this fluid, ie, as in relation to compressor input requirement, then on the other hand, minimum fluid recycling because of the short fall in the energy it produces to recycle itself. But somewhere there could be an optimum peak position which gave close to the self-sustaining energy balance. For example, such a peak optimum between all the factors and parameters involved could contain a point at which the fluid from the compressor was producing more energy than required for the compressor and at an optimum for helping to make up the shortfall in the recycling energy, etc.Which was one of the starting points for this train of thinking.

Thus, the above view of this route to BE really sums up the first aspect of this route that is perhaps more certain at this pre-practical stage. However, if we now progress to the second aspect it is conceivable that increasing fluid recycling would yield A' increasing energy advantage, or render the optimum peak between all the factors involved at a higher level than the minimum optimum of the- first view.Which, however, would depend upon one or other of the combined nozzle designs, as would the first view in order to minimise uson the short fall in the initial recycling enerav nroduction. However, the second vie

also iwX co nsiders the compressor pressure in the fluid flow and the Law of Transmission of this pressure.ThuG if one can place the recycle fluid into the fluid flow without having to pushtJp against the compressor pressure but then the compressor pressure becomes transmitted throughout the whole combined flow in accordance with the Law of transmission of pressure, then one would be graining the advantaqe of that pressure acting upon the fluid that didn 't have to "pay" for that pressure in the wav that it would have to in the normal system in which it had to

push'\Pagai nst the pressure when it would then and thereby become subjected to the compressor pressure.

Thus, the more fluid one can get into the compresssor fluid flow without having to pay the full price for the compressor pressure then perhaps the more would be the advantage gained, which then could be perceived as a maximised optimum in contrast to the minimised optimum of the first view. Although again there would be a peak at which the shortfalls started to overtake the gains.

However, the foregoing design of combined nozzle whilst gaining the advantage of not having to place the recycling fluid into the fluid without having to sush9aaainst the pressure of that fluid. flow, it may not

haveXbist potential to subsequently give the benefi

t0Jcm press ion pressure as could be transmitable throughout the combined flow because of the tear drop approach to the combined nozzle.

some of the following designs may be better from this point of view but before progressing onto these firstly stating that the distinction between the first and second aspect is

now becoming even more discernable in now

taking on the foregoing dimension, which may ultimately be the main dimension and indeed the main view since one may not get much energy advantage until the pressure of one of the flows adds to the pressure of the other flow, ie, gives a boost to the pressure at the point of combining the flows via a combined nozzle of a design which will give such an effect, albeit having commenced off this train of thinking in relation to the r to the four parameter.You see if one places the surplus mass into the fluid flow in the unit of time the 1 mass unit from the compressor flows through the svstem whilst holdina off the latter fluid

all the combined

må s s bnec omlNq subjectedto the compression pressure, then the effective pressure at nozzle exit could have been given a very substantial boost via a combined nozzle of the correct design which could well be the first design on thinking deeper.

effect, for the 1.5 CSA dimension and via the correct design of combined nozzle one could perhaps approach placing the 1 mass unit from the compressor into the 3 mass units of recycling fluid in unit time without having to increase upon nozzle CSA above that required for the 3 mass units. When the fluid jet length in unit time would become increased by some 30% and the increase in kinetic energy by some 100%, with this extra energy not being fully paid for, although one would lose the advantage of the r to the four element of a larger CSA flow, but perhaps not in a tit for tat relationship. However, again it would probably be a question of maximising for marginal benefits but which when all such marginal benefits are maximised upon they could give rise to a substantial quantity of BE when compared with the simple fluid flow in which one had to reduce the nozzle CSA to give the flow at unity with the compressor.

Therefore the foregoing view of this potential route to further BE, ie, as via combining recycling fluid via a specially designed combined nozzle, is probably now closer to the correct view with all the foregoing views probably only being partially correct. The apt analogy could be drawn with streamlining one's thoughts until they become more on the beam.Although, of course, not to abandon the original thinking in relation to the r to the four factor at this stage and it could well be that one could obtain a combination of both these potentially possible advantages since the combining of the flows via one or other of the Combined Nozzle designs/techniques thereof, could well simultaneously prove a means by which the r to the four element of the lesser flow becomes overcome, with the system effectively being subjected to the r to the four element associated with just the larger flow when otherwise the relevant rate determining factor would be dictated by the r to the four element of the lesser flow, etc. I also add that I am currently developing my thinking further in relation to the potential for the pressure boost which I am not yet including in my discussion on the system.

Relating all such aspects to the law of conservation of enerqy, here it is not a question of qaininq energy from nowhere but a case of simply improving upon the simple method,

one doesn't lose as much due to the r to the four element at a maximum level of detraction from in the simple system. Which is where I came in and, therefore, now progressing on and I think we a back at a minimum optimum of recycling fluid with respect to such aspects but of course this will also depend upon how readily one can add, and on how effective is adding, further quantities of the natural heat sources at this stage in the process to make up the shortfall in the recycling energy.If easy to add and very effective in so doing then one may wish to maximise for the cold exhaust air capacity, but remember if having to be rendered an isothermal expansion then this may not be very good.

Thus such aspects are not all necessarily as broad as long as the old saying is in certain old quarters, and one can finely optimise all the parameters involved and/or can be made involved, eg, as via the recycling fluid, for peak yields substantially above that which would be obtained via a simple straight forward system. And especially so through and via fine tuning of optimum design in the application of basic principles. But remember still all in aid of simply making the sub-system-compressor cycle fully self-sustaining when otherwise it would be lacking to the extent that it would render the process totally useless.

A further view of the difference between the two aspects embodied in this route to BE is that in the first view one could consider that one was minimising the drag forces on a vehicle in motion and such that the input energy causes more forward motion of the vehicle, after all a gallon of petrol has the same energy value whichever vehicle it is placed into but some of the same weight it could move a lot faster and/or a lot further than others. With the second aspect being analogous to the view that one attempts to actual apply the drag forces to aid with the forward motion so that area doesn't have to place as much energy into the same mass in the first place to move as fast and/or to move as far.And I think that the minimistation of the r to the four drag element in the fluid flow of the system under discussion will in the fullness of time be found to directly parallel the stages to the minimisation of drag and the perfection of design so to do in the history and evolution of the automobile, and now perhaps the application of to provide the power for, ie, as hoped to be achieved in the propulsion via air power project. And perhaps in the system under discussion we are also now up to the stage of the application of in a sense, albeit perhaps not the same sense.

However, now progressing the discussion onto the other combined nozzle designs and some more Figs.

Other Combined Nozzle Types: These are illustrated on Figs 10;

and are perhaps now self-explanatory. However, I will include a little further discussion on these further individual nozzle types, some of which may be more successful than other ways and some of which don't have a tear drop in the way of the fluid flow from the compressor inside the nozzle and in such cases perhaps the fluid from the compressor would i more conducive to giving the recycling fluid around the smaller, inner, circuit a pressure boost rather that vice-versa. Yes without having paid the full price for the pressure boost in mechanical terms but nonetheless having done so in mechanical and design terms. Thereby gaining the benefit of a pressure boost without needing to pay for it.

B. Reverse Combined Nozzle - 1, Fig 10: As implied this design of combined nozzle is the reverse of the foregoing design

in ,~he recycling fluid surrounds the fresh fluid coming from the compressorv and the principles involved would be similar. Again the entering fluid would not have to pushWPagainst the full random pressure of the compressor but would simply be pumped in as a flow surrounding the central flow from the compressor, as indicated. Therefore, perhaps the r to the four element of the system would be as that associated with the central flow with the surrounding fluid possessing that associated with the final nozzle exit.Thus, if the surrounding fluid is the lesser flow at an optimum minimum which alone would possess a higher r to the four drag factor then this could be one area of energy advantage in this system. Remember the internal edge of this flow at the point of combining could be adjacent to a very low side pressure as associated with the streamlining central flow, which would be flowing from 100 ATS to 1 ATS just across the length of the nozzle and be streamlining in so doing. Which if it doesn't have an actual drawing influence on the other flow should at least maintained the velocity of the inner edge of the flow moreso and, therefore, perhaps the foregoing view of the r to the four drag factors and advantages thereof will apply and be correct.However, the further view here could again be likened to cars flowing along on ramps on either side and combining with a 3 lane central freeway with perhaps forward pressure boost creation as the flows are caused to merge through subsequent converging nozzle design. When the system would still possess the r to the four drag factor as associated with the central flow if the final CSA of the nozzle exit is no narrower, but under such conditions one would have squeezed in the flows on either side and if the same mass is flowing out of the nozzle exit in unit time then each rnicromass in that mass would possess an appreciably higher velocity than if the CSA had to be correspondingly larger to accomodate the passage of the surrounding fluid combining with the central flow.Thus, in one view it may be a question of whether the static pressure of the inner flow would draw into itself the surrounding fluid converging into the inner flow. One only has to consider fluid flows through venturi systems to appreciate how this may take place to some extent with a similar shaped converging nozzle and with respect to the latter aspect I again point to the comment ofi page 66 of Kermode where it states that the creation of such effects are very much dependant upon exact shaping.

Thus, it follows that in such an approach to this system there may be a peak energy yield position between on the one hand, reduced r to the four drag factor as associated with a broader flow and on the other, increased pressure boost factor as associated with a narrower fluid flow for the flow of a given combined mass in unit time. Then if one adds the Fluid Stand-In technique one could maximise upon the pressure boost component. An aspect here being that in contrast to some old fashioned power getneerating systems the circulatory would be all fully closed-cycle and therefore very conducive to the addition of additives to the fluids to enhance such an effect.

C. Combined Nozzles- 2, Figs 11A, B and C:

TheXprinclple ot this type ot combined nozzle is that the recycling fluid would be pumped into the beginning of the nozzle as indicated on the diagrams and on flowing through the nozzle down the pressure drop of 100 ATS to 1 ATS,or below if the Partial Vacuum technique is becoming applied, across the length of the nozzle and forming streamlines in so doing,coLild in Design llA draw the fluid passing through the holes indicated along the sides of the inner pipe carrying the fluid from the compressor, which in this case would be a sealed pipe at the end. However, coupled with such a view is the fact that the compressor fluid would be under the pressure of 100 ATS, which would be forcing it through the holes. But in this case into the low side pressure of the other flow. Since the compressor fluid would possess the pressure energy of 100 ATS and contribute this to the combined flow then perhaps this would be a way to create the pressure boost effect discussed in relation to the analogy of a 3-lane freeway because via such a means it may also prove posible to place the compressor fluid into the other fluid flow without having to increase upon the CSA to accomodate the fluid for the passage of the same combined fluid in unit time. Or at least not as much as one would normally have to do.However, at this stage I think I have more faith and belief in the first two designs discussed, However, on progressing to Designs llB and C in the same category then such an approach could perhaps be better than Design 9B at least because both these designs are in the absence of the tear drop in the way of the fluid flow from the compressor and, therefore, they may be more conducive to the creation of a pressure boost effect on the combining of the two flows since this again becomes achieved without having to push up against the compressor pressure.

In Design liB to instead enable the entering fluid to force against the low side pressure of the forming fluid jet on combining, and already with a high forward dynamic pressure in further advantageous contrast, and in Designs liC very similarly and similarly as in Design 9B but with the flows the reverse way around. Whilst in the comparison of Designs llB and C with ilA then I think one can see from the diagrams that they would have the advantage in the flows there of all being caused to flow in the same direction before combining, and of the inner flow from the compressor not exerting any back pressure on the recycling fluid on combining.

D. Reverse Combined Nozzles- 2: Figs1;L4= and C: As implied this combined nozzle type is really the reverse of the foregoing with the flow from the compressor drawing in the recycle fluid becoming pumped in as indicated. When the recycle fluid would be pumped into the low side pressure of the forming fluid jet rather than against the full compressor pressure.

Again the central fluid flow would be streamlining along the nozzle across a pressure drop of 100 ATS to 1 ATS and/or below and the entering fluid would be doing so at a pressure of 100 ATS into the low side pressure of the forming central fluid jet. Therefore again one can envisage that one could therby achieve the Freeway Effect and, in turn, thereby achieve some energy advantage over the normal system, ie, via thereby creating a pressure boost in the forward vector and thereby in the forward dynamic pressure of the combined fluid jet finally flowing out of the nozzle exit, or to express a further and more relevant way, to thereby increase upon the linear forward velocitv of the final formed fluid iet for the flow of a riven combined mass in unit time.

the area of impact of the fluid would be less, but each micro mass of a given area of impact would be travelling faster and causing the turbine to rotate faster and therefore as far as the turbine is concerned the total area of impact of the total given number of micromasses in the same mass flowing in unit time would be the same. With further reqard to the latt

asM=ts ::erl I firsltq refer to the experimentat fun system Fseveral years ago ana snown as a 6.30pm local TV news item in which a man from and at Heriot Watt University was floating in a vertical stream of air flowing up a large tube and become raised to a higher level when in a section of the air flow that passed through a venturi like narrowed section in the vertical tube up which the flow of air was passing, indicating that the forward energy of the air flow had been caused to increase simply by creating the narrowed section in the air flow without placing in any further energy to the air flow, ie, simply through design. At the time confirming to me my propulsion by air power project in part.However, the principle involved m relation Lu the foregoing aspect is the same.

Secondly, I also draw the parallel with a particle bean weapon in which successive impacts of minute micro amounts of mass in unit time travelling at a very high speed would impart a far higher energy of impact in total than would the same total mass in unit time travelling at a much slower speed.

In these current one one can also envisage the mechnisms by which the pressure boost in the forward x-vector could become created 6y a consideration of a molecular collision view and how by correct angle of attack and correct design shaping molecules could become knocked towards the nozzle exit when otherwise they may remain travelling at a vector angle from the nozzle exit, and especially so the edge molecules of the central fluid flow, whichcoulin fact embody a further key to this approach to BE, ie, using the entering fluid to force the edge fluid of the central fluid flow to become pushed away from the sides and into the forward vector instead.

Of course a part of the entering fluid would then become stationary edge fluid, but the final combined effect could be one of a pressure boost in the forward vector compared with a normal system. Which must be the case if via such a technique one can cause the same combined mass to flow through a narrower CSA nozzle exit in unit time than in the normal system.

In relation to this and to the freeway analogy I also point out problems number 3.29 to 3.31 on pages 191/2 of Fluid Mechanics by Frank M White, where flows are being caused to combine in the normal manner in the first example and where the same analogy becomes used in a somewhat different context in the following two examples.

However, now progressing this discussion onto the further addition to this patent application. But firstly stating that having deliberated thus, at this pre practical stage I think it would be wiser to take the view that the Combined Nozzle approach could prove a way to better transfer the power of the Partial Vacuum Technique to the forming fluid jet than may perhaps be achievable. For example, in the system depicted on Fig. 1D. Whilst bearing in mind that it may be a way to BE in its own right having regard to the foregoing deliberations.

Bonus energy addition to the alternative method of operation discussed on page 365: To recap, this method of operation involves powering the compressor with the energy yield from the main turbogenerator and then harnessing the remaining mgh value of the cold fluid in the sub-system for output supply. When it was considered that one may be able to just aquire sufficient energy via the turbogenerator for fully sustaining the compressor, to leave remaining that from the sub-system for output supply. However, not necessarily and, therefore, this addition commences to explore the potential for adding BE techniques specifically to this method of operation which is exploration lacking in the originial patent application.

In this method of operation there should of course still be scope for adding the Partial Vacuum Technique to add extra energy yield to that of the basic amount just down to the ground state of IATS., which would then be additional output energy that could make up any shortfall in that becoming fed to the compressor from the turbogenerator. However, and on the one hand, in being rendered as close to ground temperature as possible, or even at depending upon the temperature range of the other fluid being used in the other turbogenerating system, then the fluid may not be as streamlinable for the purposes of facilitating for the conversion of the partial vacuum into harnessable energy.Although in the use of R-21 for example of BDt.90C, then the cooled temperature would still be close to the Bpt of the fluid on streamlining to lATS. and still be far removed from it's Fpt. Whilst in contrast if one were to try to apply the technique to a hydro system then one probably wouldn't gain any extra energy yield because the water would be very close to it's Fpt. and also be very hydrogen bonded in further contrast and, therefore, in a state wherein the molecules would probably be difficult to align into the forward vector beyond the "normal" level for the purposes of transferring additional BGS kinetic energy from the water to the turbine.

Whilst on the other hand, the fluid would be closer to the BGS region on the P-E diagram and, therefore, perhaps this aspect coupled with the fact that the fluid would be still close to it's Bpt at 1 ATS.

albeit now far removed from the liquid-vapour state in the critical point region of it's P-E diagram when such extra streamlining should be far better achievable, could result in some BGSEof the Partial Vacuum Technique still being able to become transferred and added to the basic energy yield just down to lATS.

However, having deliberated thus, since one would wish the turbogenerator energy yield to fully sustain the compressor then obviously if one could substantially reduce the compressor input requirement via the Mountain or Deep Sea techniques then such a goal would become appreciably more achievable, to then be more certain that all the output from the sub-system plus any BGSEaddition would be available for output supply. Then a further technique that could work equally as well in this method of operation could be that of working in a higher pressure range across the sub-system and sweeping aside vapour in the immediate vicinity of the nozzle exits.

Therefore, perhaps in view of the envisaged difficulties in relation to the hot fluid method of operation perhaps being more difficult to achieve, albeit once achieved then perhaps better, one would first approach the process with this alternative method of operation in mind but which would probably still require one or a number of techniques to BE to become added for the process to be successful and indeed perhaps in order for the process to yield any energy for output supply above that required internally. Since I evolved all such techniques during the course of deliberating upon the other method of operation perhaps I wouldn't have if just considering this part of the process in the light and context of current cold water hydro systems. Thus, the foregoing work could be at least useful in this respect.However, moreso than this, in becoming rendered at a cooled temperature then a further route to BE here in this alternative method of operation could be one of subsequently adding heat to the cooled fluid before passing through the sub-system to boost upon the energy yield. For example, heat at too low a temperature for the other turbogenerator system but at a sufficiently high temperature to become transferred to the fluid flowing to the sub-system, eg, between 300to 60 C, eg, the residual heat from the other turbogenerating system.

Then there would be scope to add the air compression technique to the process, which theoretically could again potentially add the energy contained in air from normal state to the very cold exhaust state to the turbine output(s) from the process, which would then be three, as well as yielding very cold air capacity.

Moreover, subsequent addition of heat could then and thereby also render the fluid more streamlinable and, therefore, probably the Partial Vacuum technique could thereby become rendered more successful pn application.

Additionally there would be the fluid recycling technique to consider, which in one sense could be perceived as not being as essentially required in this method of operation in which the other turbogenerator power is hoped to fully sustain the compressor and if achievable then whatever energy became produced at the sub-system would be for output supply and would not be required to be a specific amount for fully sustaining the compressor with.

On the other hand the colder fluid would be more viscous with the r to the four drag element at a maximum and, therefore, would be in a state that could undergo maximised improvement with respect to this element.

Moreover, the fluid contraction effect in the colder fluid would be less, if at all, and therefore the surplus mass would be more likely to yield it's own recycling energy (as in hydro storage schemes for example). Then recalling very effective vacuum creation via vacuum pumps based upon cold water tap flows in laboratories, the drawing and/or entraining advantages and/or pressure boost advantages that may be achievable as the two flows are caused to combine via one or other of the combined nozzle techniques could perhaps be better and more ideally achieved in this alternative method of operation.Perhaps particularly with a further dimension that could then be better incorporated, this being the more deliberate creation of differential pressures and temperatures between the two combining flows, ie, if the air compression technique is becoming applied to the recycling fluid then it's temperature could be higher but it's pressure could be lower which could render the fluid better able to receive firstly a drawing influence and then a pressure boost influence from the fluid flowing through from the compressor, eg, via combined Nozzle - 1. Which is perhaps an apt point to curtail this further discussion at this stage.

Suffice it for me to finish off by stating that at least this alternative method of operation with added bonus energy techniques should be pursued to the practical testing stage in my opinion.

Further discussion in relation to the Combined Nozzle Systems with particular regard to Combined Nozzle type 1: Fig 9 Ba: Combined Nozzle 1 Illustrating the On-Ramp to Freeway Description combined with a Snooker Description: Firstly deliberatingfurther upon why the Combined Nozzle approach could very probably be better than a single flow system through a simple single nozzle system, and again in this further discussion initially having in mind a fluid in the liquid-vapour state which, notwithstanding the foregoing discussion, could be found easy to apply and in so doing give a better energy balance than the cold system from the outset, eg, before perfection of turbine impellors, etc.Then in deliberating thus I will hopefully arrive at Further reasons why the Combined Nozzle approach is likely to be better than the single ssshe If one studies diagram Fig 9Ba then one could well think why should such a system give any better results than the simpler system in which the recycling fluid entered the fluid flow through the side wall of the flow system leading up to the nozzle with then just a single flow passing through a single nozzle, ie, as illustrated on Fig 9 Baa.

Well I think the advantage over the above system could probably be comprised of a number of interrelated aspects but basically because one can only go so far with the existing systems as achievable, defined, dictated and pre determined by just the parameters of the single fluid flow through a single nozzle, albeit of optimised shaping to give a peak flow velocity for the system.Whilst in the case of the Combined Nozzle then embodied within the energy advantage that is hoped will ensue from the manner of combining the flows in the ways discussed one in effect is adding further to the flow parameters that can become manipulated and optimised to probably give a higher flow velocity for the flow of a given amount of combined mass in unit time than cools otherwise become achieved. although at this Doint in time before any practical experimentation

In,tnt end to tend to consider that the Combined Nozzle approach will be a 'way to render the application of the Partial Vacuum Technique more effective in terms of transferring the extra energy that it represents to the fluid flow and then and thereby to the turbine. Whilst bearing in mind that I also think that it could well be a way to further BE in it's own right.

However, continuing the discussion in relation to further parameters to manipulate.

For example, if one considers the single flow system as it would be at point (a) in the combining of the fluid flows, then at such a stage in the development of the final fluid jet already comprising the combined fluids the randomly orientated molecules thereof would only just be beginning to align themselves into streamlines. Whilst in contrast in the Combined Nozzle system the central stream of molecules would be fully aligned, as would probably also the surrounding flow of molecules via their action of streamlining around the tear drop. At which point, in further contrast, the fluids would not yet be combined but held apart. With the further shaping of the nozzle in this case not being to streamline but rather to merge the already streamlined fluid flows by gently coaxing and squeezing them together.Although at the actual point of the merger some re-randomisation of and by certain molecules may take place as higher flyers at such a stage knock slower lower flyers at such a stage sideways, rather than push on as hoped to be achieved with the further shaping then also being to simultaneous re align as the merger is ~~~ taking place. But with the whole objective of it all being to thereby create a longer narrower and therefore more effective combined fluid flow per unit of combined mass flowing out of the nozzle exit in unit time than would otherwise be achievable via the normal system and as represented here by the system of Fig 9 Baa.Which is an aspect that would probably become enhanced via the simultaneous application of the Partial Vacuum Technique, or conversely, the Combined Nozzle approach could render the latter system far more efficient in terms of the energy it represents actually becoming efficiently transferred into the forming fluid jet in comparison to the efficiency of such transference that could otherwise be achievable, ie, becoming knocked along at the rear via the on-ramp to freeway or snooker mechanism as well as being drawn along from the front, to draw a further apt analogy(s), could render the drawing forces at the front infinitely more attractive in their drawing action.

Therefore, in relation to such a view I also refer to my earlier discussion in the original work where I deliberate upon the fact that the fluid jet on its creation could have the potential to become drawn to the extent that its static pressure could become that of the external environment in the isolation chamber when, if so, its forward dynamic pressure representing the impartable energy would have become increased by a corresponding amount, as in a pre expansion vapour turbine system on transferring the power of a condensation vacuum.And state that perhaps such a potential would be better achieved in practice, firstly, if the fluid state is in the liquid-vapour state at the stage of the formation of the fluid jet and, secondly, if the Combined Nozzle technique is also becoming applied to induce the type of action described above on the formation of the fluid jet. Thus, perhaps a further technique which would be particularly effective for solely this function, ie, to help with the transference of the power of the Partial Vacuum Technique to the fluid jet on its creation, in the system depicted on Fig. 1D and Fig. 7.

huts, as implied, a further parameter that could particularly become manipulated via pressure, temperature and optimum positioning and which in contrast is also fully pre determined in and by the single flow system, is one of creating a velocity difference between the two flows so that on combining one flow, eg, the central flow, could be caused to impact into the other flow in a way which could be not be achieved in the single flow system, Thus at stage (a) in the development of the fluid jet the surrounding flow could be caused to have the same randomness and velocity that it would have in the normal system at such a stage but with the difference that this fluid flow would then receive a mighty boot forward from the central flowing fluid at this early stage in the formation of the fluid jet which it would not nor could not receive in and via the normal system. Of course, one has Newton's Laws to consider but one really isn't trying to get something for nothing but rather by design cause the two flows to combine in such a manner that a given mass of the combined fluid fluid flowing in a given time finishes flowing as a longer and narrower fluid flow at the nozzle exit than could otherwise become achieved.An exercise here is to consider that as one increases velocity so kinetic energy of impact increases in a disproportionate squared relationship manner in accordance with the equation KE = 1/2MV; and therefore the faster the central fluid flow at point (a) then the much higher will be the energy of impact in the forward vector at such an early stage in the development of the final combined fluid jet, which would not be achievable flow mechanics in the normal single flow System. Moreover in such ways could one probably achieve an improved r to the four element in the finally created fluid jet at the finish than would otherwise be achievable via the simple single flow system of Fig 9 Baa. However, aspects to deliberate further upon in the future continuation of this project and it is probably better at this stage to remain with the view that in such ways one should be able to more effectively transfer the power of the Partial Vacuum Technique to the forming fluid jet than could otherwise be achieved.

Claims (54)

1. A process comprising:- (i) a liquid to vapour heat exchange unit through which passes a suitable fluid for becoming converted to it's vapour phase on absorption of surrounding heat on it's flow through said unit, (ii) a vapour compressing unit for adiabatically compressing the resultant vapour from the former unit, followed by, (iii) a further heat exchange unit for removing from (ii) under constant pressure cooling conditions the upgraded heat produced in said adiabatic compression for use subsequently or in-situ, followed by (iv) a special turbine unit in place of a noarmal throttle device for converting otherwise wasted pressure-enthalpy energy remaining in the fluid from (iii) and still under the constant pressure from the outlet of the compressing unit, into usable mechanical energy instead of allowing such energy to go to waste as in a normal throttle device, which in one main method of operation of the overall process could then become used to help or fully power the vapour compressing unit and thereby facilitate for a surplus of energy production for external use via that yielded by the process at stage (ii), although not exclusively; with the fluid from the exit of the special turbine unit then going on to the heat exchange unit under (i) above for a further cycle of the process, - which is principally aimed at the upgrading of low heat, eg, of the type and temperature contained in the waters or ground of the Planet, to a temperature suitable for electrical generation in a liquid to vapour turbogenerator via said means, although not exclusively.

2. A process as claimed in Claim 1 in which said heat exchange to said vapour turbogenerator could be in-situ directly to the latter.

3. A process as claimed in Claim 1 in which the heat of condensation from said liquid to vapour turbogenerator becomes placed into the liquid to vapour heat exchange unit under (i) at the start of the process to thereby effect the continuous recycling of said heat as well as rendering the process fully closed-cycle with respect to it's two fluid cycles.

4. A process as claimed in Claim 1 in which said special turbine unit is comprised of an impulse jet turbine of either the Pelton Wheel or rotating blade type.

5. A process as claimed in Claim 4 in which the rotor cups of said Pelton Wheel turbine are designed to have a reducing curvature to facilitate for contracting fluid.

6. A process as claimed in Claim 4 in which the fluid channels through said rotating blade are designed to reduce to facilitate for contracting fluid.

7. A process as claimed in Claim 1 in which said special turbine unit is comprised of a reaction turbine of the type in which several radially equidistant arms through which fluid under pressure flows are thus caused to rotate by the flow through force of said fluid under the pressure of said compressor around a central axis.

8. A process as claimed in Claims 4 and 7 in which said turbine is housed inside an isolation chamber where the only inlet to the chamber is the pipework carrying said fluid to said turbine therein and the only outlet is pipework at the base of said chamber carrying the fluid exiting from said turbine to the next stage of the process, ie, said heat exchange unit at the start of the next cycle of the process, and wherein a pressure can, therefore, exist which is the vapour pressure associated with the fluid on it's exit from said turbine and more specifically, as would be thermodynamically associated with the exit temperature of the fluid.

9. A system as claimed in Claim 8 in which said vapour pressure inside said isolation chamber is a low vacuum, pressure below lATS. due to the fluid exiting from said turbine at a low temperature for the fluid and, therefore, having associated with it a low saturated vapour pressure, the vacuum power of which adding to the forward dynamic pressure of the fluid jet in accordance with the Bernoullis Theorem and in a self sustaining manner via the action described, ie, the vacuum pressure inside said isolation chamber will add to the forward dynamic pressure of the fluid jet which, in turn, will become imparted to said turbine to lower the temperature of the fluid which, in turn, will then have associated with it a low saturated vapour pressure on exit from said turbine, which, in turn, will add to the forward dynamic pressure of the fluid beyond that associated with normal ground state pressure of lATS. which, in turn, will become imparted to the turbine etc, ad infinitum.

10. A process as claimed in Claim 9 in which said isolation chamber is facilitated for becoming evacuated at the start of the process to commence off said self-sustaining action thereafter.

11. A process as claimed in Claim 9 in which a coolant additionally becomes added to the system, such as a cold air flow or a cold water flow, to assist the self-sustaining fluid cooling action, similarly as in condensation vacuum systems of vapour turbines, and which could also become applied to commence off said self-sustaining action.

12. A system as claimed in Claim 9 in which said vapour pressure inside said isolation chamber is a self-sustaining high pressure above lATS. due to the fluid on exit from said turbine therein having an associated saturated vapour pressure above lATS., in turn, due to the fluid exiting from said turbine at a high temperature for the fluid.

13. A system as claimed in Claim 12 in which the rotating turbine inside said isolation chamber of either the impulse jet or reaction turbine type is, via appropriate design, caused to push away the vapour at said elevated pressure inside said isolation chamber from the immediate vicinity of the fluid jet exit(s) from the turbine in order that the fluid jet can impart energy to the turbine to a pressure below that of the surrounding vapour pressure and in this way gain an energy advantage over the energy required to compress the vapour from the pressure of the surrounding vapour pressure, assuming that through design said pushing aside of vapour can be achieved for less expenditure of energy than the advantage gained.

14. A system as claimed in Claim 13 in which a coolant such as cold air or cold water becomes suitably applied to aid with said depletion of vapour in the immediate vicinity of said turbine fluid jet exits.

15. A system as claimed in Claim 13 in which heat may subsequently be added via some appropriate means, eg, a water or air flow, in order to maintain the desired surrounding vapour pressure on said condensation of fluid in the immediate vicinity of said fluid jet exit(s).

16. A process as claimed in Claim 1 in which the nozzle(s) of said special turbine units under (iv) have internal walls that are shaped for maximised streamlining of the fluid jet(s) becoming created therein and thereby.

17. A process as claimed in Claim 1 in which an ionised fluid may be used in said process, or an ionised/ionising additive incorporated into the fluid, in combination with oppositely charged electro repulsion forces, either natural existing at the surface of the nozzle material or induced via electrical charge, acting to force said fluid away from said fluid jet creating nozzles under Claim 16 in order to try to aid with said shaping and streamlining of the fluid as it flows through said nozzle(s).

18. A process as claimed in Claim 1 in which an additive may be added to said fluid to alter it's normal, newtonian, flow behaviour for improving upon the streamlinability of the fluid as it flows through said nozzles under Claim 16.

19. A process as claimed in Claim 1 in which a surplus of said fluid is caused to flow through the fluid jet creating nozzles of said special turbine unit in relation to that exiting from the compressor outlet, which then becomes continuously recycled back into the fluid flow ahead of the inlet to the nozzle on exit from said turbine and en route becoming reheated and repressurised as required to enter back into the fluid flow and maintain the fluid pressure as required to be maintained by said compressor, with the turbine energy produced by this portion of the total fluid passing through said turbine directly equating to the amount so to do, for the purpose of trying to thereby gain some energy advantage over the energy yield from a fluid flow the same as that at said compressor outlet in one or several of a number of ways, eg, thereby facilitating for a nozzle radius larger than would be required for the smaller fluid flow as at the compressor outlet which could then have associated with it less drag on the fluid as it forms into a fluid jet in accordance with the relationship between the parameters of fluid flow in Poiseuille's equation, as well as facilitating for a larger fluid flow through said nozzles in such a manner which could prove helpful particularly for small capacity processes where it may prove difficult to produce the bore through said nozzles with minimised drag on the fluid flow.

20. A fluid recycling system as claimed in Claim 19 in which said reheating and repressurising becomes effected via using the energy from said turbine to first adiabatically compress air; with the heat of compression thereby produced then becoming used to reheat the fluid under conditions of constant pressure cooling with respect to the compressed air, and the resultant cooled compress air, as still at the pressure of the compression, then becoming used to repressurise the fluid and in the process yield a supply of very cold exhaust air as a bonus.

21. A system as claimed in Claim 20 in which said yield of cold exhaust air becomes applied in the process in the systems thereof under Claims 11 and 14 in the ways described.

22. A system as claimed in Claim 20 in which said yield of cold exhaust air becomes applied for refrigeration.

23. A system as claimed in Claim 20 in which said yield of cold exhaust air becomes applied for a cold store function.

24. A system as claimed in Claim 20 in which said yield of cold exhaust air becomes applied for moisture precipitation from a suitably humid atmosphere.

25. A system as claimed in Claim 20 in which heat becomes added to the air expansion on use of said cooled compressed air for said repressurising of the recycling fluid in order to convert an otherwise low energy yielding adiabatic expansion into a high energy yielding isothermal plus expansion, with such heat being possible to be provided via the low grade natural heat contained in the waters of the Earth for example, which should not only ensure that there is sufficient energy for the repressurisation but could also be a source of further energy gain.

26. A system as claimed in Claim 19 in which one endeavours to achieve a pressure boost advantage on the re-entry of the recycling fluid into the fluid flow.

27. A system as claimed in Claim 19 in which the recycling fluid enters the fluid flow at the turbine nozzle stage via a combined nozzle design, which attempts to maximise upon either (i) the advantage that may be achievable via minimising upon said drag on the fluid flow as it flows through the turbine nozzle(s), or (ii) maximise upon advantage that may be achievable through causing said pressure boost under Claim 26, or (iii) attempts to optimise for maximised advantage from a combination of the foregoing effects (i) and (ii).

28. A process as claimed in Claim 1 in which said vapour compression under (ii) and said removal of heat under (iii) is such that the thermodynamic state of the fluid on it's passage through said turbine unit under (iv) results in the fluid state passing beyond the saturated liquid line for the fluid into the vapourisation state in order to try to obtain an energy advantage via such a means by a pressure boost effect and/or a fluid volume maintenance effect for otherwise contracting fluid detracting from energy yield.

29. A system as claimed in Claim 28 in which any resultant vapour fraction at the exit from said turbine becomes condensed back to liquid phase via the appropriate application of a suitable coolant, eg, a cold air flow from the system under Claim 20 passing through cooling tubes.

30. A system as claimed in Claim 4 in which contraction of fluid on passage through said impulse Jet turbine is attempted to be counteracted via either expanding and contracting turbine impellors upon which the fluid jet impinges in unison, or via the vibration of said impellors in unison.

31. A process as claimed in Claim 1 in which in an alternative method of operation a maximised quantity of heat is removed at said stage under (iii) for the generation of a maximised quantity of mechanical energy, which then becomes used for the sustaining of said vapour compression under (ii), to leave remaining the energy yield from said special turbine unit under (iv) as that available for output supply.

32. A process as claimed in Claim 31 in which heat becomes added to the fluid after the heat removal stage under (iii) and before or during passage through said special turbine unit under (iv) in order to increase upon the energy yield at the latter stage, from any available heat source with one on-site example being residual heat in the fluid at said turbogenerating stage.

33. A process as claimed in Claim 1 in which the fluid on exit from said special turbine under (iv) becomes appleid for a refrigeration purpose before then passing onto the heat exchange unit under (i) at the start of a further cycle of the process.

34. A process as claimed in Claim 33 in which all the energy from both stage (iii) and (iv) under Claim 1 has to become used within the process to fully sustain the compressor under stage (ii), but can nonetheless become used for said refrigeration function via said means in a process based upon abundant and renewable heat sources such as the low grade heat contained in the waters of the Earth.

35. A process as claimed in Claim 1 in which all or a part of the heat yield under stage (iii) becomes applied directly as heat to render the process also a Heat Plant as distinct from just a Power Plant.

36. A process as claimed in Claim 1 in which the heat source for the heat into the process via the heat exchange under stage (i) is that of the heat contained in the air passage of a moving transportation system.

37. A process as claimed in Claim 1 in which the main or one of the heat sources is solar heat via a solar pond system or direct solar heating of the pipework carrying the fluid in said heat exchange unit under (i).

38. A process as claimed in Claim 1 in which the main or one of the heat sources for the process is via the self-sustaining air refrigeration cycle, which, however, would probably have a shortfall in energy to perhaps leave no surplus energy from the overall process for output supply, but such a process would still yield the very cold exhaust air from said air refrigeration cycle which could become applied for the three functions of refrigeration, water precipitation from the atmosphere, eg, rain or dew making and cold store, via a process based solely on an abundant, renewable and reliable source of energy, ie, 'fully selfsustaining' adiabatic compression of the air of the Planets atmosphere to yield the heat of compression thereof for input to the process, which in a normal air refrigeration cycle normally goes to waste, and in the process yield a supply of very cold exhaust air for said functions even if no power remains for output supply after use of that required by the process, when one could apply the process to grow energy in the form of biomass as well as for growing and storing food, etc, purely on air.

39. A process as claimed in Claim 38 in which any shortfall in energy in the air refrigeration cycle thereof is attempted to be made up via rendering the otherwise adiabatic expansion of air in the air refrigeration cycle of a higher energy yielding isothermal type or beyond by adding heat to the air expansion as it expands, which could again be the low grade heat of the Planet because for the otherwise adiabatic isothermal would give a finish temperature for the expanded air back at the temperature of the Planet air, eg, via a fast flowing water source or via a solar pond system or via direct solar heating, etc, but of course one would then lose the very cold air capacity although one could operate such a process so as to render the air refrigeration cycle just selfsustaining via such a means which could still leave the exhaust air suitable for some functions5 eg, refrigeration and cold store.

40. A process as claimed in Claim 38 in which the turbogenerator mechanical energy yield from the process itself becomes used to first compress air with the heat of compression generated in this air compression becoming added to render the air refrigeration cycle selfsustaining in the manner stated, to leave remaining cooled compressed air, which could then become applied directly as a power source or to generate electricity and in the process yield a supply of very cold exhaust air from this source for the stated functions even though the capacity of cold exhaust air would have been reduced in the air refrigeration cycle.

41. A system as claimed in Claim 40 in which said heat of compression instead becomes placed into the heat exchange unit of said process under stage (i) of Claim 1 in order to reduce upon the air refrigeration cycle capacity required and, therefore, the accompanying shortfall in energy, whilst at the same time making avaialble a capacity of cold exhaust air from the latter once again, albeit reduced.

42. A process as claimed in Claim 41 in which a second air compression stage becomes added to the first stage, which, in turn, was added to the turbogenerating stage, with the heat of compression from the first stage still becoming used to reduce upon the air refrigeration cycle via placing into said heat exchange unit, but with the heat of compression from the second air compression stage becoming placed into the air expansion of the first air compression stage, which should then yield a supply of cooled compressed air from the second stage of sufficient power capacity to make up the shortfall in the energy requirement of the reduced air refrigeration cycle as well as a surplus for output supply and in the process yield a supply of cold exhaust air at this stage for said functions.

42. A process as claimed in Claim 42 in which a third air compression stage becomes added to the first two stages, with the heat of compression from this stage becoming added to the air refrigeration cycle to render it fully self-sustaining by rendering the air expansion thereof isothermal, to leave all the cooled compressed air yield from the third stage for output supply and said functions.

43. A processas claimed in Claims 4-42 in which heat becomes added to the otherwise adiabatic air expansion of said cooled compressed air yield from the process in order to increase upon energy yield via such a means, with some sources of heat for such a purpose being as under Claim 39 and a further one being otherwise waste heat from factory processes, eg, the aluminium smelting process.

44. A process as claimed in Claim 1 in which any number of air compression stages become added to the turbogenerating stage of the process, with the heat of compression from each becoming placed into the air expansion stage of the preceding stage, apart from that from the first stage which becomes placed either into the heat exchange unit of the process under (i) in Claim 1 or into an air refrigeration cycle, or into itself.

45. A process as in Claims 42 and 44 in which the heat of compression quantities en route to their destinations in the process become applied for raising steam, with the steam then going on to the intended destinations and there becoming condensed back to water5 whilst in the process imparting almost the same heat to the intended recipient system, to in such a manner add a water purification and/or desalination plant capacity to the basic process.

46. A process as claimed in Claim 1 in which the output power yield from said turbogenerating stage becomes used to first compress air, with the heat of compression generated becoming used to generate power and the resultant cooled compressed air, still at the pressure of said compression, becoming used to generate further power and in the process yield a supply of very cold exhaust air for said functions, although further heat could become added to the air expansion as under Claim 39 to increase upon the power yield and reduce the cold exhaust air capacity.

47. A process as in Claim 46 in which the cooled compressed air becomes used to evacuate under water tanks for storage of the energy as harnessable hydropower via a suitable turbine at the top of the tanks and to in such a way be able to even out variable production, and also for the purpose of gaining an energy advantage via evacuating underwater tanks at low tide and harnessing the stored energy as hydropower at high tide, with a further possible source for energy advantage via such a system being that of rendering the otherwise adiabatic air expansion on the evacuation of the tanks of a higher energy capacity isothermal nature via surrounding and/or available heat.

48. A process as claimed in Claim 1 in which all or a portion of the output power yield becomes applied to boil water for water purification/desalinisation purposes via appropriate electrical element heating apparatus, with the raised steam becoming condensed via the heat exchange unit of the process under stage (i) of Claim 1, to in the process continuously recycle this portion of the energy yield of the process, or via some other available means, eg, at an air expansion stage to also thereby recycle the energy or via cold exhaust air or via a water flow.

49. A process as claimed in Claim 1 which attempts to obtain an energy advantage via placing the heat exhange unit of stage (i) at some depth beneath the surface of the water flow from which it is absorbing heat in order to thereby facilitate for a height of the liquid fluid on it's exit from the turbine unit of stage (iv) acting down upon the inlet to said heat exchange unit so that the fluid could then vapourise at a vapour pressure which corresponded with the pressure that the height of fluid represented given the choice of a suitable refrigerant so to do, eg, Refrigerant R-12 of Bpt-30 C could vapourise at SATS pressure for a water flow at normal temperature, which, in turn, would then reduce the compression energy input requirement by a pro-rata amount whilst one would still obtain the same energy yield at stages (iii) and (iv).

50. A process as claimed in Claim 49 in which said energy advantage is attempted to be achieved via use of an elevated site such as a mountain to facilitate for said height of fluid.

51. A process as claimed in Claim 1 in which the technique of Claim 49 is applied for the purposes of applying the vacuum technique of Claim 9, ie, to provide the desired fluid pressure for the inlet to the heat exchange unit of stage (i) which would otherwise be detracted from to the extent of the partial vacuum pressure in said isolation chamber.

52. A process as claimed in Claim 9 in which a piston or a diaphragm system may become applied in conjunction with said isolation chamber for sensitive control over the vapour pressure becoming created in the chamber via effecting volume change of the latter.

53. A process as claimed in Claim 1 in which the vapour on exit from said heat exchange unit under stage (i) becomes heated en route to said compression unit under stage (ii) with available heat direct solar heating, for the purposes of improving upon the overall energy balance of the process.

54. A process as claimed in Claim 1 in which the system arrangement as in Claim 49 and 50 becomes applied but instead one harnesses the potential head energy of the height of fluid via a suitable turbine at the foot of the height of fluid, when one wouldn't then be able to also obtain the energy advantage of Claims 49 and 50.