WO2002066386A1

WO2002066386A1 - Process for selective refining of the di-hydrol polymer by temperature and pressure conditions below the critical point of water

Info

Publication number: WO2002066386A1
Application number: PCT/PT2001/000001
Authority: WO
Inventors: Mário Veríssimo HORTA LOPES; Nuno Manuel Carlos Fonseca Figueiredo
Original assignee: Aquarius Ventures International, Ltd.
Priority date: 2001-02-23
Filing date: 2001-02-23
Publication date: 2002-08-29

Abstract

The invention refers to a plant and to the various aspects of its construction and to a wet air oxidation process, initiated by infracritical water oxidation, induced by temperature and pressure conditions below the critical point of water, allowing the recovery of 70 to 80 % of the total water content in real effluents of an organic nature, and furthermore: (i) selective refining of reusable water by preselected patterns with or without chemical oxygen demand; (ii) extraction of over 99 % of organic and biological contaminants; (iii) extraction of over 99 % of inorganic contaminants. The invention establishes a relationship between the method of selective refining of di-Hydrol polymer in liquid phase by preselected patterns and the plant required for said purpose and its respective technical details. The raw material can be any real effluent of an organic nature with total concentration of solids between 1 and 12 %. The process consists of a superoxidation developed by a mechanism of infracritical water oxidation followed by wet air oxidation that develops a stabilized oxi-redox conditions, which regenerate the di-Hydrol polymer, optimized by adjusting and controlling the physical variables of the polar dielectric in liquid phase. The first chamber of the aquorefining plant's reactor establishes the critical parameters of the polydispersion pattern. These critical parameters are selected for infracritical conditions. The expanded and dilating materials, as well as the precipitates, that are derived from the oxidation process sequence, are extracted in the reactor's second chamber.

Description

PROCESS FOR SELECTIVE REFINING OF THE DI-HYDROL POLYMER BY TEMPERATURE AND PRESSURE CONDITIONS BELOW THE CRITICAL POINT OF WATER

Description

1. Problem identification

The permanent and daily conversion of drinkable water into contaminated water is significantly greater than the existing refining capacity of industrial and natural water treatment systems to convert it back for re-use. The consequences are a daily accumulation of irreversibly polluted water and also a permanent loss of usable water.

2. Problem solution in the state of the art

The current state of available technology proposes to solve the problem

referred to above in paragraph 1 by means of a large number of technical

solutions, involving a variety of procedures and processes. These

procedures have in common their inability to totally eliminate pollutants from

the effluents, only achieving a reduction of such pollutants. The continuous

drainage of these effluents into rivers, lakes or oceans causes an

accumulation of residual pollutants and thus does not solve the problem

referred to above in paragraph 1.

The biological or chemical oxidation of organic materials can be obtained by

the use of oxidation reagents. The use of these reagents is not very

advantageous as they are costly and can themselves produce pollutant

RECORD COPY byproducts, which, in turn, require appropriate treatment.

The aforementioned biological processes executed below the critical

temperature of water, although commonly used, are not efficient enough and

cannot achieve complete oxidation, as well as developing undesirable

byproducts. Moreover, biological agents cannot be used to oxidize organic

products that are toxic or difficult to oxidize.

The wet air oxidation process, executed at temperatures below the critical

temperature of water, which has been used to oxidize many organic

products, has not, however, been able to achieve complete oxidation and

produces byproducts that are detrimental to the oxidation process.

The various solutions for eliminating organic materials, namely, the known

techniques based on the use of water in supercritical conditions, are

generally solutions used in batch form (discontinuous process) using

temperatures above 647 K and pressures above 221x10⁵ Pa. The negative

consequences from these high pressure and temperature conditions are the

high cost of equipment, the high cost of the process and the risk of

corrosion. Additionally, these solutions do not adapt well to the objective of

regaining reusable water.

The known hydrothermal processes, such as supercritical water oxidation,

are used to fully oxidize the organic compounds. The critical temperature

and pressure of water which are, respectively, 647 K and 220.4x10⁵ Pa, may

substantially oxidize all of the organic matter in the reaction, releasing water, C0₂, N₂ and inorganic byproducts, such as metals and salts.

These processes are referred to in the following North American Patents.

5,558,783 Sep., 1996 McGuiness 210/761

5,560,822 Oct., 1996 Bond, et al. 210/181

5,674,382 Oct., 1997 Chapman 210/96.1

5,676,737 Oct., 1997 Whitlock 95/90

5,690,898 Nov., 1997 Barnes, et al. 423/210

5,723,045 Mar., 1998 Daman 210/175

5,804,066 Sep., 1998 Mueggenburg, et al. 210/177

5,888,389 Mar., 1999 Griffith, et al. 210/175

5,888,403 Mar., 1999 Hayashi 210/695

5,932,111 Aug. ,1999 Christensen, et al. 210/748

6,001 ,243 Dec, 1999 Eller, et al. 210/96.1

6,010,632 Jan.,2000 Ross, et al. 210/759

6,030,587 Feb. ,2000 Haroldsen, et al. 422/228

6,051 ,145 Apr.,2000 Griffith, et al. 210/761

6,054,057 Apr.,2000 Hazlebeck, et al. 210/761

6,056,883 May, 2000 Bond, et al. 210/721

These processes differ substantially from the present invention because the

range of temperatures and pressures used in the above processes are

considerably higher than those used in the process to which this invention

refers. 3. Invention description and fundamentals.

The invention establishes the combination of a wet air oxidation process, at

low vacuum conditions, which takes place in the second chamber reactor,

with an infracritical oxidation at temperatures below the infracritical point of

water, which takes place in the first chamber reactor, allowing the recovery

of 75 to 80% of the total liquid mass. This process is achieved by

maintaining constant the pre-selected pattern of the di-Hydrol polymer.

The Infracritical Water Oxidation reactor allows the operator to control and

adjust the infracritical water intervals at a constant pressure achieving

spontaneous superoxidation between 328 and 368 K at constant speed and

pressure of the pre-selected polydispersion at the shear stress. The photon

beam, of a specific wavelength, projected at the moment of repulsive

electrostatic stress, after the shear stress, onto the pulverized liquid stream

containing dissolved complex organic matter, inside of the first chamber of

the reactor, provokes spontaneous and short-lived first order half-reactions.

In order to sustain the oxidation potential, a specific dose of an oxidant is

added, supplying paramagnetic oxygen, thereby maintaining the irreversible

nature of the reaction, in which the high oxidation potential has an

accentuated reducing effect on the di-Hydrol polymer.

The reactor permits the operator to adjust the cinematic control of the auto-

regeneration process of the "clusters" of di-Hydrol polymer (coherent

electrostatic superposition), at low vacuum, obtaining pre-selected refinement of the dielectric equipotential, within varying electrical potential,

selected between 0.3 and 0.4V of oxi-redox potential.

The oxi-redox neutralization, in a oxygen saturated medium, induces an

electrical flow charge, reducing the volume density of polarization and

increasing the superficial density of the charge in the polar dielectric of the

aqueous solution, due to a combination of the oxygenation cone (enriched

by a dynamic flow of micro-bubbles) and the photon beam of a specific

wavelength, during the dispersive phase inside of the second chamber of

the reactor.

The effect of the apparent electrical neutrality, after the influence of

intermediate short-lived superoxydes, accelerates the precipitation of salts

and the separation of the colloidal structures, achieving the elimination of

over 99% of the di-Hydrol polymer contaminants.

The peripheral procedures that follow these phased reactions consist of salt

filtration, extraction of gas and foam and the cleaning or burning of gases

produced during the process.

The fundamentals of the invention are as follows:

Inside each isobaric cycle of energy preservation, under wet air oxidation

conditions, the thermal variation induces a mechanism of self-oxidation di-

Hydrol, which establishes electric equipotential nano-condensators

(clustering), with limited electric capacity to produce variables in the pattern

of tri-, di- and mono-Hydrol, consequently conditioning the dynamic characteristics of the dimerous medium (liquid phase).

During the incremental increase of temperature, inside the isobaric cycle of

energy conservation, below the critical point of vaporization and at a

constant pressure, spontaneous variations in the quantum states occur in

the Hydrol connections of an electrostatic nature, in overlapping

compressive conditions. These conditions are fundamental for the dimerous

medium to function as a nano-condensator), by electric overcharge of the

condensator, the intensity and frequency of which expresses the relation

between the relative mass and energy flow of the polar dielectric.

The periodical state of "short circuit" sets off electronic quantum jumps,

producing spontaneous quantitative differences in the relative proportions of

the tri-, di- and mono-Hydrol patterns per mol, allowing efficient free energy

absorption and, simultaneously, establishing a tendency to apparent oxy-

redox electric neutrality.

The energetic and molecular rearrangement in the dimerous medium,

resulting from the spontaneous electronic quantum jumps, define an

infracritical interval with specific expression in the ratio between the relative

mass (in mols) and the free charge flow in the polar dielectric.

In the infracritical interval, the mechanism of self-induced water regeneration

is characterized by: re-nucleation of free polarization charges, duplication of

the characteristics of oxygen of a paramagnetic nature and recombine the

Hydrol patterns in the ratio between the internal energy and a volume mass at a given moment.

Each isobaric of water conditions the magnitude and frequency of the

mechanism of self-induced regeneration, based on auto-oxidation of a

paramagnetic nature, which can greatly reduce the Hydrol polymer, with

capacity to increase the quantity of mols and to fix the free energy, followed

by an oxi-redox neutralization with capacity to vary the relative proportions of

the patterns.

The process of refining the di-Hydrol polymer must be induced, due to the

binary character of the infracritical interval, expressed in the dimeric matrix

of liquid, that does not allow a random variation of combinations by function,

equivalent to the most complex systems, inherent in the continuous process

of auto-regeneration. Hence, the di-Hydrol polymer remains active, due to

the limitations and induced inter-relational dynamic of the dimeric matrix, in

other words, its dependency on the character and frequency of external

stimuli.

In the continuous process of refining the di-Hydrol polymer, the

superoxidation is efficient in the elimination of dissolved organic specimens,

and the neutralization is efficient in the precipitation of dissolved inorganic

specimens at low temperature.

The invention permits the recombining of the molecular structure of water,

and simultaneously eliminating therefrom, all the contaminants that are

present and recalibrating the regeneration levels, with or without chemical oxygen demands, according to the requirements of industrial, municipal and

domestic applications. The method applied in this invention avoids the

accumulation of contaminated water and makes it possible to decentralize

local recovery operations.

The process in this invention has the following advantages: maintaining

conditions of low risk of corrosion and incrustation in the equipment;

reducing operational costs, when compared with supercritical oxidation;

eliminating the dissolved organic matter in the water, derived from the

effluents used as raw material in the process, and eliminating biological

activity; destroying the simple and complex organic chains in gas phase,

that are then reused as an alternate fuel; refining the di-Hydrol pattern and

allowing the recovery of the total liquid mass in the range of 70 to 80 per

cent.

A description of the invention, with reference to the attached drawings, is

given as follows:

Fig.1 represents the general diagram of the aquorefining plant

Fig.2 represents the mechanism for hydrolyzed polymerizing of the liquid

phase, through coordination complexes in aqueous solution, and the system

for filtering and pre-heating the effluent.

Fig.3 represents the first chamber of the reactor, which is the oxidation

chamber of water in infracritical conditions, integrating the back-pressure

regulating mechanism. Fig .4 represents the mechanisms for adding, mixing and accelerating the

reaction of the oxidant of a paramagnetic nature.

Fig.5 represents the second chamber of the reactor, which is the chamber

of wet air oxidation integrated in the cooling circuits, the control of the

hardness of the water by removal of salts and conduction of concentrated

foams and gases to the extraction system.

Fig.6 represents the feedback circuit for modeling water.

Fig.7 represents the aquorefiner reactor as a whole.

The present invention consists of a sequential process of oxidations,

beginning with the influx 1 of real effluent, through an effluent filter 2, with

discharge regulated by on/off valve 3; using a pump of medium pressure

with regulated valve 4, for pumping said liquid effluent through a heat

exchanger 5, in order to pre-heat said liquid effluent between 325 and 375

K; the effluent then passes, with pressure controlled between 10x10⁵ and

15x10⁵ Pa, to a polymerizing device 6, for polymerizing hydrolyzed

coordination complexes of the effluent, with an injection of 2 to 4% in weight

of steam between 410 to 450 K, achieved by control device 7; removing

gases and foams through a modulated valve 8. In order to regulate the flow

of extraction of the polymerizing device, there is a modulated valve 9, as

well as a medium pressure pump 10 for pumping the polydispersion

obtained in the polydispersion device, at a pressure between 30x10⁵ and the 60x10⁵ Pa. The pumped flow will then cross an electromagnetic field

produced by a coil device system 11, powered by an electric current in the

range of 2 to 5 V, to polarize the polydispersion. This polydispersion is

projected, with constant pressure and velocity between 70 and 100 m/s, on

a pre-heated target through an induction coil 14, producing micropolarized

polydispersion inside of the first chamber of the reactor 13. Next, a radiation

source device 12, with wavelengths between 1.6x10^"7 and 3.8x10^"7 m, is

used to bombard, with a beam of ionizing radiation, the micropolarized

polydispersion in the said first chamber of the reactor 13, where the

infracritical water oxidation took place. The resulting gases are conducted to

a backpressure device, with gases and foams extracted by a three-way

valve 16, controlled by adequate sensors, composed of a backpressure

regulator 15 and a modulated valve 17, controlled by adequate sensors.

The monodispersion resulting from infracritical oxidation is then subjected to

the addition of the oxidant of paramagnetic nature, whose reaction is

prepared in a rapid mixing system 21 and polarized in an electromagnetic

field produce by a electromagnetic coil 22. This polarized monodispersion is

projected at constant pressure and velocity on to the heel of the second

chamber of the reactor 24, in parallel with compressed air stripping,

obtained from a compressor 23, at a pressure between the 5x10⁵ and the

7x10⁵ Pa and a temperature between 283 and 288 K, with a comparative flow between 1 to 2 % of the circulating stream. By the combined effect of

air stripping, with the micropolarized monodisperson flow in the heel of the

second chamber of the reactor 24 an oxigenation cone with micro-bubbles

and ascendant streams develop, by ultracavitation, which allow the capture

of the colloid stuctures extracted in the expansion chamber of gases, on low

vacuum, controlled by a modulated valve 32. This process takes place in

wet air oxidation conditions. Subsequently, the apparent electric

neutralization process is started, in which, in addition to the already

mentioned ascendant streams, descendant streams occur, dragging salts

by gravity, conducted through an electromagnetic field, produced by an

electromagnetic coil 34, powered by an electric current between 2 and 4 V,

which caused the inorganic particles to aggregate. Inside the oxygenation

cone, various streams are produced simultaneously, created by the

pressure differential between the internal and external surfaces of the wall of

oxigenation cone, which is being cooled by recycled water, producing

microvortices exposed to an external source of polarizing radiation 26, with

wavelengths of 4x10^"7 to 2x10^"2 m. The stability of neutralization is obtained

with a cooling, which results from the mixture of the recycled water streams,

supplied by valve 36, with the passage of the liquid mass as a whole

through the auxiliary cooling device 27, which is a part of a system

composed of a cooling tower 30, a water pump 31 and an on/off valve 29

controlled by adequate sensors, where the refined and filtered water is regulated by an on/off discharge valve 25, and also controlled by adequate

sensors. The refined water, controlled by the on/off valve 37, is added to the

oxidant of paramagnetic nature in the tank 18, the resulting mixture then

feeds a dosing pump 19, controlled by modulated valve 20, to be injected

under pressure into the fast mixing device 21.

The extraction of gases and foams, regulated by modulated valves 8, 17

and 32 controlled by adequate sensors, are drawn into a collector 33 which

feeds into a cyclone with a forced extraction system by vacuum pump or

high pressure fan 39, to separate solid matter from gases, conducting solids

to a container40.

The refined water, after passing through an electromagnetic field, produced

by an electromagnetic field 34, passes through a filter 35 and is recuperated

by modulated valve 38, controlled by adequate sensors.

CHEGADA EFLU 20°C 14 BDBINE INDliςao 29 VΛLVULA DN/DFF FILTRO 15 REGULADOR DE CONTRAPRESSSO 30 TDRRE DE ARREFECIMENTO V<SLULA ON/OFF 16 V4LVULA DE 3 VIAS 31 BDMBA <5GUA ARREFECIMENTO BOMBA 12.5 BAR + ViSLVULA DN/DFF 17 V4LVULA MDDULADA 32 ViSLVULA MDDULADA PERMUTADDR DE CALDR 18 TANQUE ADITIVα 33 CDLECTDR CΛMARA DE POLIMERIZAςaD 19 BDMBA DDSEADDRA 34 BDBINE ELECTRDMAGNέTICA A 1» CS ARA DD ITEM 6 20 V4LVULA MDDULADA 35 FILTRU B 2" CΛMARA DO ITEM 6 21 MISTURADOR R.SPIDD 36 V<SLVULA MDDULADA V<SLVULA MODULADA 22 BDBINE ELECTRGMAGNέTICA 37 VήLVULA DN/DFF V4LVULA MDDULADA 23 COMPRESSOR DE AR 38 V4LVULA MDDULADA V4LVULA MDDULADA 24 AQUDREFINADDR - 2* CβMARA DD REACTOR 39 CICLDNE & BDMBA VACUD 0 BOMBA 37 BAR 25 V LVULA ON/OFF 40 RECIPIENTE DE INERTES 1 BDBINE ELECTRDMAGNέTICA 26 SISTEMA DE REFINAζZO 2 FONTE RADIAQZD 27 PERMUTADDR 3 ICWD- 1* CβMARA DD REACTDR 28 FDNTE DE ALIMENTAQSD EXTERNA

• I VDI oxiooςα INΓRA-CKITTCA DA -GUA

INLET 14 INDUCTION COIL 29 CODLING REGULATOR VALVE FILTERS 15 BACKPRESSURE REGULATOR 30 CDDLING TOVER DN/DFF VALVE 16 3-WAY VALV!_ 31 CDDLING PUMP PUMP DF 12.5 BAR 17 MDDULATED VALVE 32 ON/DFF VALVE PRE HEATING 18 ADITIVE TANK 33 CDLLECTDR POLIMERIZATION CHAMBER 19 DDSIFIER PUMP 34 ELECTROMAGNETIC COIL A FIRST CHAMBER OF ITEM 6 20 MODULATED VALVE 35 FILTER B SECOND CHAMBER OF ITEM 6 21 MIXER 36 MDDULATED VALVE MODULATED VALVE 22 ELECTROMAGNETIC COIL 37 DN/DFF VALVE MODULATED VALVE 23 AIR COMPRESSOR 38 MODULATED VALVE MDDULATED VALVE 24 AQUDREFINING REACTOR 39 CYCLDNE & VACUUM PUMP PUMP DF 37 BAR 25 ON/OFF VALVE 40 INERTS RECEIVER ELECTROMAGNETIC CDIL 26 SOURCE OF RADIATIDN SOURCE DF RADIATION 27 CODLING ICVO REACTDR" 28 EXTERNAL ELECTRIC SDURCE

Claims

1. A method for transforming real effluents of an organic nature with

concentration of solids up to 12 % in the liquid phase, and a potential oxi-

redox with a range of 0.3 to 0.4 Volts, with or without a chemical oxygen

demand, characterized by the hydrolyzed polymerization of complexes of

coordination, by infracritical water oxidation with the addition of an

oxidant of paramagnetic nature, and by wet air oxidation with apparent

electric neutrality of the liquid phase, in order to achieve the preselective

refining of the di-Hydrol polymer in the liquid phase.

2. The method in claim 1 , wherein the polymerization of hydrolyzed

complexes of coordination is characterized by nucleations of an organic

nature, developing a hydrophilic polydispersion saturation, which is

obtained by sequential injections of steam.

3. The method in claim 1 , wherein the micropolarized polydispersion is

characterized by the dimensional reduction of nucleations of an organic

nature, caused by a change in the electric charge signal, obtained by the

repolarization, the acceleration, and the pressure and impact of the

polydispersion over a heated and fixed target.

4. The method in claim 1 , wherein the infracritical water oxidation is characterized by the development of first order half reactions, in temperatures ranging from 323 to 363 K, achieved by repolarization of the micropolarized polydiserpsion at the relaxation time of the particles, by electromagnetic wave effect.

5. The method in claim 1 , wherein the infracritical water oxidation, with the

addition of an oxidant of a paramagnetic nature, is characterized by the

concentration of dissolved oxygen, in a range of 5x10^'6 to 8x10^"6 Kg of

dissolved oxygen per Kg. of polydispersion and by the low concentration

of intermediate complexes which inhibit the oxidation process, producing

a monodispersion which is transformed into a polarized monodispersion

by the electromagnetic field effect.

6. The method in claim 1 , wherein the wet air oxidation, characterized by

the formation of an oxygenation cone with micro-bubbles, referred to as

ultracavitation, is obtained by the simultaneous effect of the injection of

compressed air and the injection of a polarized monodispersion (i.e. air

stripping conditions) at different pressures and temperatures, creating

ascendant streams of air and gas which transport electrically charged

colloid particles.

7. The method in claim 1 , wherein the wet air oxidation with an apparent

electric neutrality, is characterized by an oxi-redox stability, is obtained by

transporting the colloid structures via ascendant streams, and the salts

via descendant streams, for subsequent removal, and by maintaining the

magnetic stability of the paramagnetic nature of the electron spin marker

in the oxygen of the di-Hydrol polymer, attained by exposure to a specific

ionizing radiation.

8. The method in claim 1 , wherein the wet air oxidation with an apparent electric neutrality sustained by the magnetic stability of the electron spin

marker of a paramagnetic nature in the oxygen of the di-Hydrol polymer,

is characterized by the oxi-redox irreversibility with or without chemical

oxygen demand, obtained by inducing the polarization of the di-Hydrol

polymer which rotates inside of the microvortices generated on the

external wall of the oxygenation cone.

9. An aquorefining plant for the purpose of executing the preselective

refining of the di-Hydrol polymer in the liquid phase, in accordance with

the method in claim 1 , is characterized by an apparatus for

polymerization and by a reactor with two chambers.

10. Apparatus for polymerization 6, according to claim 9, characterized by its

two chambers, for producing a calibrated polydispersion, wherein, in first

chamber 6A, the pressurized effluent is injected through a lyred injector,

promoting frictional energy, against a small curved shaped receiver,

followed by the addition of steam, with an ascendant discharge of the mix

against a heated target, to produce the expansion of gases and foams,

which will be separated from the liquid by a cylindrical perforated ferrule

and conducted to a forced extraction device; and a second chamber 6B

wherein, steam is added at the level of a low speed rotation turbine

blade, to develop a saturated concentration of the hydrophilic

polydispersion.

11. Reactor, according to claim 9, characterized by its two chambers.

12. Reactor, according to claim 11 , characterized by the fact of its first

chamber 13, where a regulated infracritical wet oxidation is generated,

being constituted by a high pressure injection device for injecting the

polarized polydispersion, which is obtained by the effect of an

electromagnetic field produced by the electromagnetic coil 11 against a

heated target by an induction coil 14, micropolarizing the polydispersion;

followed by a repolarization by the continuous bombardment of a

radiation beam produced by radiation source 12, which takes place in the

interior of the first chamber of reactor 13; the discharge of the gaseous

phase thus obtained will be drawn to the backpressure regulator 15,

conducting the liquid solution toward the fast mixer 21 , where the mixture

of the oxidant of a paramagnetic nature, dosed by dosing pump 19, is

optimized, and the resulting monodispersion is repolarized by

electromagnetic coil 22.

13. Reactor, according to claim 11 , characterized by the fact of its second

chamber 24, for obtaining a controlled neutrality, in liquid phase, of a

chemical separation of salts and the removal of colloids, being

constituted by an injection device 23, under air stripping conditions,

generating an oxygenation cone with microbubbles, which transports the

organic and biological materials for their subsequent removal, via an

ascendant stream, capturing the flow of free electric charges on the

surface of the electrodes in a closed circuit, at the level of the liquid surface, where said electrodes are powered by an external electric

source 28, generating, by means of vessels connected by U-tube in

backpressure on the oxygenation cone wall, microvortices that absorb

the polarizing radiation beam which is emitted counterflow by radiation

source 26; wherein, due to the gravity effect, the salts are drawn by the

descendant stream, receiving, at the same time, the flux of free charges

deriving from the electric flux 28 and developing an aggregation of

inorganic material in the electromagnetic field generated by the

electromagnetic coil 34; the microvortices receive, at the external wall of

the oxygenation cone, the cooled ascendant streams deriving from the

refined water 35 and, by contact, the Hydrol patterns, with a

predominance of di-Hydrol and parts of tri- and mono-Hydrol,

progressively stabilize the molecular structure of water.

14.Device, according with claim 10, characterized by its producing, in

continuous process, a polydispersion by steam oxygenation,

independently of the standard deviation of the raw-material used,

producing hydrolyzed complexes of coordination.

15.Device, according to claim 10, characterized by producing, in continuous

process, a spontaneous expansion of volatile matter and making, in

continuous process, a controlled extraction, lowering the tendency of

concentration in long chains and, simultaneously, the chemical oxygen

demand in the monodispersion.

16.Reactor, according to claim 11 , characterized by the fact of its first

chamber regulating the variation in the frequency and speed, creating the

requisite conditions for induced half reactions of first order and sustaining

the oxidization potential, with the continuous addition of an oxidant,

producing water and carbon dioxide.

17.Reactor, according to claim 11 , characterized by the fact of its second

chamber allowing the physical separation, continuously and

simultaneously, of floating matter (colloids) and precipitates (salts).

18.Reactor, according to claim 11 , characterized by the fact of its second

chamber allowing the recombination of tri-, di- and mono-hydrol in the

relative proportions per mol, according to the preselected pattern of the

refined water .