Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
  • B01J8/10—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by stirrers or by rotary drums or rotary receptacles or endless belts
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F28—HEAT EXCHANGE IN GENERAL
  • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
  • F28D11/00—Heat-exchange apparatus employing moving conduits
  • F28D11/02—Heat-exchange apparatus employing moving conduits the movement being rotary, e.g. performed by a drum or roller
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F28—HEAT EXCHANGE IN GENERAL
  • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
  • F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
  • F28F13/02—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by influencing fluid boundary
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/18—Details relating to the spatial orientation of the reactor
  • B01J2219/182—Details relating to the spatial orientation of the reactor horizontal

Definitions

• This invention relates to fluid flow apparatus wherein boundary layer fluid flow influences the function of the apparatus.
• a known technique for reducing the boundary layer thickness is to drive the fluid through the heat exchanger at a velocity too high for streamline flow or to provide appendages, dimples or other structures close to the separating wall which increase turbulence.
• a method of producing fluid flow within a fluid containing apparatus comprising the step of putting the fluid in an artificially accelerated frame of reference whereby the artificially generated inertial force of acceleration acts on density variations in said fluid to produce flow of the fluid.
• the inertial force acts on density variations in boundary layers of said fluid to case fluid flow thereat.
• the invention is particularly applicable to situations wherein heat exchange across the boundary layer needs to occur.
• apparatus for producing fluid flow comprising a fluid containing portion and means for applying an artificial acceleration to said portion whereby the artificially generated inertial force of acceleration acts on density variations in said fluid to produce flow of the fluid.
• the inertial force of acceleration acts differentially on what may be thermally produced density gradients within the fluid to produce fluid flow.
• the fluid containing portion has a selected surface and the inertial force acts on density variations in fluid boundary layers at said selected surface to cause fluid flow thereat.
• the apparatus applies particularly to the boundary layer that contains the non-turbulent flow regime and situations wherein heat exchange across the boundary layer needs to occur.
• the invention is effective since thermally produced density gradients become differential force gradients when accelerated (assuming a negative gradient for density against temperature) . Consequently, any slight variation in temperature within a boundary layer is translated to a force gradient which produces fluid flow.
• the accelerating frame of reference can be provided by a continuous rotation or by an oscillation about a fixed point.
• the apparatus has a further fluid containing portion, said selected surface providing a thermal contact between said portions whereby said inertial force acts on density variations in fluid boundary layers at said selected surface to cause fluid flow thereat.
• the first mentioned fluid containing portion defines a generally cylindrical shape rotatable about the cylinder axis. This is a particularly convenient shape for manufacture and application of the inertial force.
• said first mentioned portion comprises a plurality of axially aligned channel elements radially spaced from the axis. This too is simple and convenient to manufacture.
• the channel elements can then have heat exchanging elements for said selected surface to provide thermal contact with said further fluid containing portion.
• This construction further aids passage of heat between the respective fluid containing portions.
• said further fluid containing portion is defined " by the region substantially inwards from the perimeter of the channel elements so that for example the second portion can effectively be open to air to produce a simple and effective way of passing heat to or from the air without the requirement of a physical structure for the further fluid containing portion.
• said further fluid containing portion comprises an inner cylindrically shaped vessel, and an outer cylindrically shaped vessel is coaxially provided therewith to define said first mentioned fluid containing portion between said vessels. This is particularly useful for passage of heat between liquid to liquid.
• a plurality of walls are provided for rotation around an axis to define a plurality of closed channel elements as said first mentioned and further fluid containing portions with the walls defining said selected surface.
• selected ones of the elements define said first mentioned fluid containing portion and the remaining elements define said further fluid containing portion. Indeed, it is easier if alternate ones of said channel elements define said selected channel elements.
• the channel elements have a predetermined length which may be greater than zero and less than the diameter of said cylindrical shape.
• a simple construction of the apparatus arises where the walls extend between coaxially provided inner and outer cylindrically shaped vessels.
• Such walls are preferably formed by folding of sheet material to define the plurality of channels. They can be formed by channel elements which are formed from substantially the same shaped channel pieces. These pieces may be stacked in a cylindrical shape to define said first mentioned and further fluid containing portions. The performance of the heat passage across the selected surface is improved if said channel elements are corrugated.
• the walls are formed by a plurality of spaced axially located discs having means to interconnect intervening spaces to define said first mentioned and further fluid containing portions.
• the or each fluid containing portion incorporates a radial asymmetry to produce a pumping force, in use, along an axial direction.
• a radial asymmetry to produce a pumping force, in use, along an axial direction.
• the apparatus includes means to supply relatively cooler fluid to the further fluid containing portion and relatively hotter fluid to said first mentioned fluid containing portion.
• relatively cooler fluid to the further fluid containing portion and relatively hotter fluid to said first mentioned fluid containing portion.
• These can take the form of rotating sealed manifolds.
• the selected surface is provided with flute shapes or the like thereon.
• said apparatus comprises a heat exchanger with said selected surface providing heat exchange between the first mentioned and further fluid containing portions.
• the general performance and efficiency of heat exchange achieved can be better than hitherto known heat exchangers.
• the movement of the fluid away from the selected surface renders the apparatus of the present invention particularly applicable to a heat exchanger.
• a further static heat exchanger may be included wherein fluid to the first mentioned heat exchanger also passes through the static heat exchanger.
• said apparatus comprises a chemical reactor with said selected surface being provided with a catalytic surface.
• the movement of the fluid away from the selected surface renders the apparatus of the present invention particularly applicable to a chemical reactor.
• said selected surface is permeable to reactant to be catalysed.
• reactant can pass between the respective fluid containing portions so as to provide a supply of un-reacted material to the selected surface.
• the means for applying an artificial acceleration to said portion(s) to generate an artificial inertial force of acceleration preferably comprises means to rotate or oscillate said portion(s) .
• apparatus for producing fluid flow comprising a plurality of walls for rotation around an axis to define a plurality of closed channel elements wherein the elements incorporate a radial asymmetry to produce a pumping force on the fluid, in use, along the axis.
• Such a construction functions to give an efficient pumping action.
• Figure 1 illustrates the forces that act on a fluid volume element within an accelerating frame of reference
• Figure 2 illustrates a sectional view of a heat exchanger embodying the present invention taken along the axial line II-II of figure 3,
• Figure 3 illustrates a cross-section of figure 2 taken along the line III-III
• Figure 4 illustrates the view along the axis of another heat exchanger embodying the present invention
• Figure 5 illustrates the view along the axis of another heat exchanger embodying the present invention
• Figure 6 illustrates a sectional view of another heat exchanger embodying the present invention taken along the axis of rotation
• Figure 7 illustrates a sectional view of the heat exchanger 8 shown in figure 6 adjacent the inside wall as mounted
• Figure 8 illustrates a sectional view of the heat exchanger shown in figure 6 adjacent the outside wall as mounted
• FIG. 9 illustrates schematically the air flow through the heat exchanger channel elements A from inside to outside for bi-directional use
• FIG 10 illustrates schematically the air flow through the heat exchanger channel elements B from outside to inside for bi-directional use.
• FIG 11 illustrates schematically the air flow through the heat exchanger channel elements B from inside to outside for uni-directional use
• Figure 12 illustrates schematically the heat exchanger of figure 6 in combination with a static heat exchanger
• Figure 13 illustrates a section along the axis of an embodiment of the present invention as applied to a chemical reactor.
• a fluid volume element V lying on a circle 1 and within a frame of reference rotating about an axis 2 has an inertial force F acting thereon in response to local variations in density p(T) of the fluid, where the density is dependent on the temperature T of the fluid.
• F inertial force
• v is the local fluid velocity vector which varies in time.
• the action of the force F is to locally accelerate the fluid element to a radial velocity of v(r) .
• the velocity vector has three components, one angular v(0) , one axial v(z) , and one radial v(r) as shown in figure 1.
• cooler fluid having a relatively higher density will tend to move outwards from the axis 2.
• adjacent channels are provided in thermal contact and both are rotated about an axis
• two separate paths can be followed in space by the fluid streams bringing heat to or taking heat from the thermal contact.
• One path is a spiral path, in which the fluid is given initial angular momentum, followed by a helical path in which the fluid has constant angular momentum.
• a similar path is followed by the second fluid stream but the two streams may be parallel or anti- parallel in adjacent channels.
• the vectors of angular velocity v(0) and axial velocity v(z) are orthogonal to the force F vector and so have zero product. This means that the force F can be made arbitrarily large without incurring additional viscous power losses from the velocity of the bulk fluid. Only the relatively small component of the fluid velocity v(r) in the radial direction caused by the force F has a finite vector product with the vector F.
• the majority of the energy dissipated by the action of the force F is therefore restricted to the region near the interface between the fluid streams.
• the effect of this force is to drive fluid at a higher temperature, relative to the surrounding fluid, in a direction opposite to that of the force thereby causing relative motion of the fluid adjacent to the interface.
• the action of the force F is to continuously destroy by fluid mixing any density variations in the fluid.
• the inertial force F acting on a volume element in a rotating frame of reference is directed therefore in the + or - radial direction.
• the orientation of the interface relative to the direction of the force F is important.
• the maximum effect is where the interface is perpendicular to the force.
• An intermediate effect is where the interface is parallel with the force separating two streams running parallel.
• a heat exchanger is located in a wall having an inner surface 20 and an outer surface 21.
• the heat exchanger comprises a plurality of elongate channels 8 which are closed along their length and are mounted in a cylindrically shaped housing 5. Separate channels are defined in this example by walls 3.
• the left ends (as viewed in figure 2) of alternate channels 8, labelled A in figure 3, have an end section 22 of the axially outer portion of the channel cut out to open exclusively to a radially outer manifold 6 which has one or more outlet grilles 9.
• the left ends (as viewed in figure 2) of alternate channels 8, labelled B in figure 3, have an axially inward corner or angle section 23 cut off to open to 11 a radially inner area portion 24 which opens to the outside of the wall by means of one or more grilles 25.
• the right end of the heat exchanger (as viewed in figure 2) is similar to the left end.
• the ends of alternate channels labelled A in figure 3 have an axially inward corner or angle section 23' cut off to open to a radially inward area portion 24' which opens to the inside of the wall between a front cover 26.
• the right ends of alternate channels, labelled B in figure 3 have an end section 22' of the axially outer portion of the channel cut our to open exclusively to a radially outer manifold 6' which has one or more grilles 9• . It will be apparent that the construction of the end manifolds channel ends can take many forms.
• a first communication way is formed along the channels A via region 24', manifold 6 and grilles 9. This is indicated by a dot and dash line in the figure.
• a second communication way is formed along the channels B via grilles 25, region 24, manifold 6• and grilles 9 ⁇ . This is indicated by a line of crosses in the figure. It will be apparent that the respective end manifolds are adapted to prevent leakage of air therebetween. Furthermore, it will be apparent that the flow of air through channels A and B do not cross and are kept separate on each side of the heat exchanger.
• the housing and channels A and B are mounted via radial spokes 11 to a motor 12 rotatably provided on a fixed mounting shaft 14.
• the end manifolds are connected to the housing 5 which is fixedly mounted via spokes 13 to the mounting shaft 14.
• a wall 27 prevents passage of air along the inner region bounded by the channels 8.
• the channels A and B are formed so that the action of rotation causes air to be pumped into the channels along the respective communication ways described above.
• the housing channels 8 are rotated and relatively hotter air enters through the front cover 26 into the region 24* and passes along channels A to exit to the outside the wall through grilles 9.
• Relatively cooler air enters through grilles 25 to region 24 and passes along channels B in contra flow to exit through grilles 9' .
• heat from channel A is transferred or passed across the wall to channel B. In channel B this higher than average temperature air at the wall surface with a relatively lower density is driven inwards towards the axis 2.
• the air is cooled by conduction through the wall to the air in channel B. As this air cools, it becomes a lower than average temperature and hence higher than average density so that it is driven outwards from the axis 2. As the relatively hotter or cooler air is carried away from the wall during the process of heat transfer, air which has not been relatively heated or cooled in drawn to the wall surface.
• the inertial force F acts on temperature induced local density variations to rapidly take heated or cooled air from the boundary layer of the wall 3 resulting in bulk mixing with air in the respective channels.
• Flutes (not shown) can be provided on the wall surface so as to enhance heat transfer rates. Consequently, enhanced transfer by the breakdown or reduction of the non-turbulent boundary region by the use of the inertially driven differential force is particularly important in attaining the efficient heat transfer described herein.
• the release of heat at the surface of wall 3 results in rapid removal of the heated air in channels B from the surface 13 through the action of the aforementioned inertial forces driving the fluid towards the axis 2 of rotation. This results in bulk mixing with the bulk fluid in the channels B and the flow of un-heated air to the wall surface.
• the bulk of the air in channels A is cooled or temperature controlled by conduction through the walls 3 to the relatively cooler air passing through channels B.
• the surface of the walls are self cleaning because debris or the like which would normally case fouling are driven to the axially outer or inner surfaces of the channels 8 depending on their relative densities.
• a simple pumping action of the fluid can be produced by introducing an overall geometrical asymmetry in the radial direction between the respective ports of the channels A and B.
• the asymmetry is such that the air leaves the heat exchanger structure at a larger radius than it enters the structure.
• the angular momentum of the air as it passes through the heat exchanger is conserved.
• the axial length of the heat exchanger and so the thermal efficiency of the system can be increased indefinitely without effect on the angular momentum.
• the integration of the pump action also eliminates the fluid turbulence created at the interfaces between separate pumping elements and the heat exchange structure used in a conventional system. Eliminating this source of fluid turbulence increases the mechanical efficiency of mass transfer through the exchanger system and reduces the noise generated by turbulence in the fluids.
• a heat exchange effect can be produced between the aforementioned contra flows in channels A and B.
• the walls defining the channels A and B are preferably formed from thin films of plastics or metal with the channels uniformly distributed around the axis 2. 14
• the channels A and B with the present invention can take many forms.
• the channels A can be formed by mounting tubes in the intervening space between inner and outer skins with the remaining space defining channels B.
• the channels can be formed by making a series of folds in a sheet or foil of metal, paper of the like. The sheet is then inserted in the intervening space between the inner and outer skins with the radially outer end of each fold attached to the outer skin and the radially inner end of each fold attached to the inner skin.
• each fold defines a wall 3 between adjacent channels.
• the channels 8 can also take many forms of practical shape, for example they can be in honeycomb form as in a car radiator.
• the channels have a corrugated form which corrugations are not too deep to impair the self cleaning.
• the walls 3 separating adjacent channels can be made from two slightly different tapered stamped plates which are stacked into a cylinder to form the heat exchanger, end ducts and pumping effect in a simple manner.
• the air inlets are angled with respect to the axis to give a larger cross- sectional area and both inlets and outlets can be strengthened by overlap of material.
• Directional control of the air flows within the channels formed by these plates can be achieved by moulding the plates or by inserts. Either internal or external rotor motors can be used.
• the channels walls can be identical in form and stacked around the axis 2.
• the channels can therefore be produced in a number of different ways essentially restricted by the ways that thin sheets or foils can be manipulated. They can be rolled, folded, twisted or left flat and can be deformed by pressing or the like. It is possible, amongst other ways, to have the walls defining the channels as planes running along the axis 2 and intersecting it, a series of discs aligned on the axis 15 perpendicular thereto with interconnection by means of holes in the discs which are open/sealed to alternate discs, or cylinders parallel to the axis.
• the aforementioned inertial force ensures that the boundary layer is substantially reduced or effectively destroyed leading to improved heat transfer between the air flows.
• Baffles can be introduced at the ends of the channels or within the end manifolds so as to provide a radial temperature gradient within each channel.
• the inertial force causes thermal differentiation of the air throughout the volume of the channels with the air of higher temperature or lower density moving in a direction opposite to the inertial force vector. This internal process of thermal differentiation is useful because it allows air inlets and outlets to the exchanger to be positioned so as to minimise mixing between air streams or volumes of significantly different temperature, an effect know as thermal shunting.
• the manifolds at each end can be adapted such that the heat exchanger acts as a one way fan.
• the channels in the embodiment above can have a wide range of lengths down to almost zero length where the function is primarily as a bi-directional fan.
• the distributer comprises a plurality of radial channels 42 connecting at their periphery tb respective axially parallel heat exchange channels 43.
• the other ends of the heat exchange channels 43 towards the port 40 are connected by further radial channels 44 to an outlet port 45.
• Each heat exchange channel has mounted thereon a large number of heat exchange fins 46 which may in reality comprise annular discs continuous around the axis 2 with each channel 43 intersecting the disc.
• the entire heat exchanger is rotated by means (not shown) and appropriate rotating seals 50 and 51 are provided respectively at the ports 40 and 45.
• the heat exchanger In operation, the heat exchanger is rotated and hot liquid passes through the inlet port 40 to the distributer 41 and on to the exchange channels 43. There, heat is exchanged with air so that the relatively hotter air travels towards larger radii and eventually leaves the exchanger.
• the now cooler liquid at the outlet port 45 passes to a chamber 47 containing a rotating impeller 48 to increase the remaining angular momentum of the arriving liquid prior to exit through an outlet 49.
• a liquid to liquid heat exchanger comprising an inner cylindrically shaped vessel 30, an intermediate cylindrically shaped vessel 61 and an outer cylindrically shaped vessel 31. At one end there is provided a manifold 62 having an inlet 63 for feeding relatively hotter liquid to the space 64 between the vessels 31 and 61. 17
• This liquid leaves via an outlet 65 provided in a manifold 66 at the other end of the vessels.
• the manifold 66 includes a inlet 67 for cooler liquid to be fed to the space 68 between the vessels 30 and 61 and this liquid leaves via an outlet 69 provided in the other manifold 62.
• Appropriate seals 70 are provided for the manifolds.
• the vessels rotate about a common axis 2 by means not shown.
• the heat exchange occurs through the surface of vessel 61.
• the radial spaces of the vessels connecting to the spaces 64 and 68 include radial fins 71 which are fixed within the vessels.
• FIG. 6 where components common to figure 2 and 3 bear the same reference numeral, there is shown a further embodiment of the present invention in which the heat exchanger described in figures 2 and 3 is adapted to operate with filtering and can be bi-directional or unidirectional.
• This embodiment is similar to figure 2 except that ducting is provided below the heat exchanger.
• the control 103 includes a rotatable knob 107 connected to a flap 104 which opens a grille 106 at the inside lower surface of duct Z and closes the connecting duct W thereby isolating duct Y from duct Z.
• a grille at the inside upper surface of duct Y opens and the grilles 9' are closed.
• a duct 105 connecting to manifold 6 » now connects to duct Y.
• the channels B function to suck air in through grille 106, along duct Z, accelerated along channels B and pass out to duct 105 and duct Y instead of out through grilles 9'. Consequently, channels B extract air in the same direction as that of channels A.
• the passage of air in this case is schematically shown by the solid lime in figure 11.
• a catalytic reactor 83 comprises a closed outer cylindrically shaped vessel 84 mounted for rotation (by means not shown) about an axis 2.
• the inwardl facing surface of the vessel is coated with a catalyst 86.
• a coaxially mounted inner cylindrically shaped vessel 85 is mounted internally of the vessel 84 for rotation about the axis 2 (by means not shown) .
• an inlet port 89 mounted on the axis and having an internal outlet port 90.
• the ports 89 and 90 are connected to open into the inner vessel 85 with the outlet port 90 having a cup-shaped member 91 to ensure that fluid from the inlet port does not travel straight to the outlet port.
• an outlet port 92 mounted on the axis 2 and having an internal inlet port 93.
• the port 93 is connected to open into the outer vessel 84 and the port 93 extends through the inner vessel 85 to open into the opposing end of the outer vessel 84. It will be appreciated that the respective ports are connected to the vessels 84 and 85 by means of rotating seals (not shown) .
• the reactor vessels 84 and 85 rotate and fluid reactants are supplied through port 93 and pass to the outer vessel 84 where they react at the surface of the catalyst 86. Heat is generated at the surface so that, as with the function of the heat exchanger above, this higher than 20 average temperature fluid with a relatively lower density is driven inwards towards the axis 2.
• the fluid is cooled by conduction through the vessel wall to a coolant supplied to the vessel 85 via the port 89. As the fluid cools in vessel 84, it becomes a lower than average temperature and hence higher than average density so that it is driven outwards from the axis 2 back towards the surface of the catalyst 86.
• coolant from the port 89 is heated at the vessel wall by conduction and the heated coolant of lower than average density travels towards the axis 2 and is removed by the port 90 via the cup-shaped member 91. Reacted fluid then passed to the outlet port 92.
• the inertial force F acts on temperature induced local density variations to rapidly take heated reactant fluid from the boundary layer of the active surface of the catalyst 86 to the boundary layer of the cooler surface of the inner vessel 85 resulting in bulk mixing with fluid in the outer vessel 84 and the flow of un- reacted fluid to the surface of the catalyst 86.
• Bulk reaction fluid is cooled or temperature controlled by conduction through the wall of the vessel 85.
• Flutes (not shown) can be provided on the inwardly facing surface of the vessel 84 which can also be coated with catalyst so as to enhance reaction rates. This advantage applies particularly since the transfer of heat to or from the fluid is the dominant mechanism for heat transfer at the catalyst surface. Consequently, enhanced transfer by the breakdown or reduction of the non-turbulent boundary region by the use of the inertially driven differential force is particularly important in attaining the efficient chemical reactor described herein.
• the chemical reactor above or a modified form thereof reacts to differences in temperature and, whether in heat 21 generating or heat consuming reactions, the reacted fluids containing the desired reaction products are carried away from the catalyst surface in the process of heat transfer, thus drawing un-reacted fluids to the catalyst surface.
• the heat exchanger embodiment of figures 2 and 3 can be adapted to function as a chemical reactor by coating both the internal walls of the channels 8 labelled A with a catalyst. Reactant fluid is then provided to the channels A and coolant is provided to the channels B. As regards the heat passage between the channels A and B, the function of such an apparatus when rotated is similar to that described with reference to figure 6.
• the surface of the catalyst is self cleaning because products and debris which would normally case fouling are driven towards or away from the axis depending on their relative densities.
• the manifold structures 6 and 6' can be adapted so that reactant fluid travels along one channel A and back along an adjacent channel A.
• coolant fluid can be fed and drained from the same manifold.
• the walls defining the channels 8 can be formed of a perforated wall which can be a tailored membrane or some other permeable material. Then, in use, a pressure differential is applied to ensure a higher pressure in the channels B relative to the channels A.
• reactants added to the coolant pass from the channels B into channels A to enhance the reaction rate.
• a reverse pressure could be applied so that reaction products pass into the coolant, with the coolant being recirculated to attain optimum enrichment of the reaction products.

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• Engineering & Computer Science (AREA)
• Physics & Mathematics (AREA)
• Thermal Sciences (AREA)
• Mechanical Engineering (AREA)
• General Engineering & Computer Science (AREA)
• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
• Nozzles (AREA)

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• 1991
  • 1991-02-13 CA CA002104020A patent/CA2104020A1/en not_active Abandoned
  • 1991-02-13 WO PCT/GB1991/000211 patent/WO1992014981A1/en not_active Application Discontinuation
  • 1991-02-13 AU AU72176/91A patent/AU657674B2/en not_active Ceased
  • 1991-02-13 EP EP91903395A patent/EP0588788A1/de not_active Ceased

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