RU2199492C2 - Device for continuous treatment of sea water at separation of desalinized water, hydrogen, oxygen, metals and other compounds; ion separator for separation of sea water into desalinized water, anolyte and catholyte by magnetic flux, separator-neutralizer for separation of hydrate envelope from ions and neutralization of electric charges and hydrogen generator - Google Patents

Abstract

FIELD: continuous treatment of sea water at separation of fresh water and raw resources. SUBSTANCE: device has ion separator, separator-neutralizer and hydrogen generator which are connected in series forming first production line. Second production line is formed by second separator- neutralizer, reactor-mixer and hydrogen generator working on desalinized water and alkali melt. Ion separator used for separation of sea water into desalinized water, catholyte and anolyte includes preliminary magnetizing section for performing magnetizing by annular magnetic field; this section is made in form of central pipe line connected with two pipe lines of lesser diameter through slits over diameter for separation of anolyte and catholyte. Separator-neutralizer used for separation of hydrate envelope from anions and cations and neutralization of electric charges on them includes branch pipes for introducing vaporous catholyte and anolyte, conical grates carrying positive and negative charges and neutralizer having metal spherical contact and molten lithium or sodium contact. Hydrogen generator has heat-insulated housing with reaction zone for interaction of molted lithium and water and reaction mass cooling system at separation of aqueous solution of lithium hydroxide and hydrogen. EFFECT: enhanced efficiency. 5 cl, 9 dwg, 1 tbl

Description

 This invention is a group of inventions that are combined into a single whole and aimed at obtaining raw materials from sea water due to the physicochemical processes to which sea water is subjected, moving continuously along two production lines.

 The main objective of this invention is the replacement of hydrocarbon fuel (gas, oil products, coal, peat) on environmentally friendly hydrogen fuel (pure hydrogen) on the entire planet Earth, as well as to provide fresh water for industry and agriculture, as well as raw materials for chemical and metallurgical industry.

 The technological process considered below does not have a complete analogue, since the literature does not contain a description of the technological process according to which a whole series of products mentioned above are immediately isolated from sea water in a single and continuous technological cycle.

 However, the technological process includes many technical solutions, based on which, when combined into a single technological process, this invention is created.

 1. The prior art device for the separation of sea water into catholyte, anolyte and desalted water by means of a magnetic field with a magnetic flux directed perpendicular to the movement of the water stream (SU 361981, 12/13/1972, C 02 F 1/48). However, our invention is structurally different from the invention.

 2. The prior art also knows a device for magnetizing water by a circular magnetic field, described by V. Klassen. "Magnetization of water systems", M.: Chemistry, 1985, p.157-158. This invention solves the problem only half, because does not divide water into anolyte - desalted water - catholyte.

 3. As you know, the interaction of molten lithium and water is accompanied by an explosion, in addition, molten lithium is a fire hazardous substance (Chemistry and Technology of Rare and Scattered Elements, K. A. Bolshakov, Part I, Textbook for High Schools, Moscow: Higher School, 1976, p. 8, 75).

 In the present invention, the technological process and the design of the hydrogen generator exclude the chemical reaction of hydrogen production in an explosive version.

 4. However, it is known that the conductivity of dielectrics, such as water vapor, sharply increases at high voltages and shock ionization begins (Brief Chemical Encyclopedia, M .: Soviet Encyclopedia, 1961, p. 1184). A voltage is applied to the grids of the separator-converter, which eliminates the appearance of impact ionization.

 5. The closest analogue to paragraph 4 of the hydrogen generator can be considered installation for the production of hydrogen by thermochemical decomposition of water containing a reaction zone and a heat exchanger (RU 204032, 01 J 37/00, 07.27.95, 110). This is a completely different process, and it cannot compete with the invention in question.

 The solution of this problem requires new high technologies that provide tremendous reaction rates between reaction components. This invention is based on four specially designed methods that provide high reaction rates between reactants, up to an instantaneous reaction rate — neutralization of electric charges on ions that do not have hydrated shells, with the formation of the target product.

 A special apparatus has been developed for each method, in which the corresponding physicochemical process takes place.

 The problem is solved in that the device for the continuous processing of sea water with the release of demineralized water, hydrogen, oxygen, metals and other compounds contains a series-connected ion separator for separating sea water by a magnetic field into demineralized water, anolyte and catholyte, a separator-neutralizer for separation of the hydration shell from anions and cations and neutralization of electric charges on them and a hydrogen generator to produce hydrogen by the interaction of molten lithium and water, which They form the first production line. The second separator-neutralizer, the reactor-mixer and the hydrogen generator operating on demineralized water and alkaline melt, connected in series, form the second production line.

 The ion separator for separating sea water into demineralized water, catholyte and anolyte contains a pipeline placed in a magnetic field, a section of preliminary magnetization of water by a circular magnetic field created by an electromagnet coil, equipped with a device for tangential water input. The separation section of pre-magnetized water by means of a magnetic field with a magnetic flux perpendicular to the direction of water movement is made in the form of a central pipeline, to which two pipes of a smaller diameter are connected through slots in diameter to output anolyte and catholyte.

 The separator-neutralizer, designed to separate the hydration shell from anions and cations and neutralize electric charges on them, contains a device for supplying high voltage direct current to conical grids, a separator equipped with two conical tubes for introducing vaporous catholyte and anolyte grids carrying, respectively, positive and negative charges, two dampers of the vapor velocity of anolyte and catholyte and two guide cylinders for input not containing a hydration shell of anions and cations in the converter, and a converter comprising a low voltage direct current generator and an external generator circuit, which includes a metal ball contact and a contact from molten lithium or sodium.

 The hydrogen generator contains a heat-insulating casing in which a reaction zone is provided for the interaction of molten lithium and water. The housing is also equipped with a cooling system for cooling the reaction mass with a coolant with the release of an aqueous solution of lithium hydroxide and hydrogen from it, pipes for the removal of hydrogen and an aqueous solution of lithium hydroxide. In addition, the generator has nozzles for introducing anolyte and catholyte into the annular space of the reaction zone and nozzles for withdrawing vaporous catholyte and anolyte, equipped with electric heaters.

SUMMARY OF THE INVENTION
A device for the continuous processing of sea water with the release of desalted water, hydrogen, oxygen, metals and other compounds from it is based on two technological processes, which include the following process steps.

 The first technological process.

Стадия 2. Пути использования анолита и католита, полученных после отделения из морской воды обессоленной воды.Stage I. Separation of sea water under the action of a magnetic field into three fractions: anolyte - demineralized water - catholyte,
consider the ongoing process on the example of LiCl
a) dissociation of LiCl in H ₂ O
LiCl -> Li ⁺ + Cl ^- (1)
b) the separation of sea water in the ion separator under the influence of a magnetic field takes place according to the following scheme:

Stage 2. Ways to use anolyte and catholyte obtained after separation of demineralized water from seawater.

Ways to use anolyte and catholyte are as follows:
a) the anolyte and catholyte are mixed after leaving the ion separator, and the mixed solution is sent back to the ocean, where it is diluted to the initial concentration of salts in the ocean;
b) the mixed solution according to paragraph (a) is sent to a landfill for the natural evaporation of water (for countries with a hot climate) in order to obtain natural sea salt and its further processing;
c) catholyte and anolyte are sent through separate pipelines for deep processing to chemical and metallurgical enterprises in order to obtain target products (individual metals, metal salts).

 Only desalted water is introduced into the first technological process, and hydrogen and oxygen are removed.

 Stage 3. Separation of an aqueous solution of LiOH into two fractions: anolyte and catholyte.

Reaction equation
LiOH -> Li ⁺ + OH ^- (4),
Li ⁺ + nН ₂ О -> Li ⁺ 6Н ₂ О + (n-6) Н ₂ О (5),
OH ^- + nH ₂ O -> OH ^- 6H ₂ O + (n-6) H ₂ O (6).

 Stage 4. Separation from the ions of the hydration shell.

Стадия 5. Нейтрализация электрических зарядов на ионах Li+ и ОН^- с образованием металлического лития, воды и кислорода.Reaction equation

Stage 5. Neutralization of electric charges on Li + and OH ^- ions with the formation of lithium metal, water and oxygen.

Стадия 6. Получение водорода и: водного раствора LiОН
Уравнение реакции
2Li + 2Н₂О --> Н₂ + 2LiОН (3).Reaction equation

Stage 6. Obtaining hydrogen and: an aqueous solution of LiOH
Reaction equation
2Li + 2H ₂ O -> H ₂ + 2LiOH (3).

 Stage 7. Cooling the reaction products using an absorption refrigeration machine.

 An absorption refrigeration machine is designed to recover heat generated by a chemical reaction between alkali metals Li, Na and water.

The thermal effect of this reaction is
2Li + 2Н ₂ О -> Н ₂ + 2LiОН + 484 kJ / mol (9, p. 248)
Stage 8. Purification filtration of alkaline solution.

For the continuous processing of sea water in the process described above, special devices have been developed:
- ion separator and industrial block of ion separators;
- a separator of cations and anions from the hydration shell and a neutralizer of electric charges on ions (separator-neutralizer);
- hydrogen generator;
- modernized absorption refrigeration machine;
- fractional separator.

 1. The ion separator and the industrial block of ion separators.

 Figure 1 is a diagram of an ion separator and a diagram of an industrial block of ion separators.

Note: on the sheets with the drawings of the figures, the text of the title of the invention is reduced to "Device for the continuous processing of sea water ..."
FIG. 1. The scheme of the ion separator and the circuit of the industrial block of ion separators.

 1 - ion separator; 2 - the first section or section of the preliminary magnetization of sea water; 3 - coil of an electromagnet; 4 - a second section or ion separation section; 5 - pipe for withdrawal of anolyte; 6 - yoke of an electromagnet; 7 - entrance slit for the passage of anions; 8 - pipe for the withdrawal of demineralized water; 9 - coil of an electromagnet; 10 - iron core of an electromagnet; 11 - entrance slit for the passage of cations; 12 - pipe for the withdrawal of catholyte; 13 is an industrial block of ion separators; 14 - protection against magnetic radiation; 15 - case; 16 - pipeline collecting anolyte; 17 - pipeline supplying demineralized water; 18 - pipeline collecting desalted water; 19 - pipe for removal of demineralized water; 20 - pipe for drainage of the anolyte; 21 - pipeline distributing seawater by ion separators; 22 - pipeline collecting catholyte; 23 - tangential input of sea water into the ion separator.

 The ion separator is designed to separate sea water under the influence of a magnetic field into three fractions: anolyte - demineralized water - catholyte.

 The ion separator is a pipe placed in a magnetic field, and additionally contains a section of water pre-magnetization with a circular magnetic field created by an electromagnet coil, equipped with a device for tangential input of water, and a section for separation of pre-magnetized water through a magnetic field with a magnetic flux perpendicular to the direction of water movement is made in the form of a central pipeline, to which two smaller pipes are connected through slots in diameter Diameter for the withdrawal of anolyte and catholyte.

 The principle of operation of the first section.

 In the inlet pipe 23 (Fig. 1), seawater with a salt concentration of 3.5 wt.% Is tangentially supplied. Then, upon dissociation of 3.5% salt, 3.5% of cations and 3.5% of anions will be formed (as applied to monovalent metals).

 When a water stream flows in turbulent mode, it crosses the magnetic lines of force created by the solenoid. Moreover, as shown in (I, pp. 47-50, 58), the electrodynamic motion of ions in a magnetic field leads to the appearance of microvortices in the magnetic field, which leads to microturbulation of the system and, as a consequence of this phenomenon, the ion concentration near the walls of the pipeline increases , which leads to density heterogeneity in the stream (in the middle of the stream, the density is less than that of the pipe wall).

 An increase in the residence time of the flux in a magnetic field leads to a decrease in the central part of the ion flux and their concentration in the transition layer existing between the laminar and turbulent motions in the pipeline flow.

Thus, the flow of magnetized sea water leaving the section of preliminary magnetization of sea water and then entering the section for separating sea water into anolyte - desalted water - catholyte has, in terms of circle area (section G-D of FIG. 1), a non-uniform structure:
- the bulk of the ions (cations and anions) are grouped in the hydrodynamic boundary layer of the turbulent flow, i.e. near the inner surface of the pipeline, as a result of this, the concentration of ions in the surface layer increases to 17.5% (according to calculation), while ions move together with the flow in one direction (1, p. 4);
- in the central part of the stream, the ion content is minimal, because most of the ions are moved to the inner wall of the pipeline due to the combined action of the turbulent flow, magnetic field and microvortices.

 The total concentration of ions upon leaving the first section in the total volume remains unchanged, but increases near the inner wall of the pipeline.

 The principle of operation of the second section.

 The second section of the ion separator is based on the principle of separation of opposite charges in a conductor moving perpendicular to the magnetic flux (this is exactly what happens in electric generators). The theory of this process is given in (2, pp. 140-142).

 In the ion separator, the role of the metal conductor is played by a pre-magnetized electrolyte (sea water), which moves between the two poles of the second magnet (see Fig. 1) perpendicular to its magnetic flux and intersects it, which leads to the separation of ions in different directions, i.e. . negative ions will move to the left, positive ions to the right.

 Since the ions leaving the stream from the first section are located near the inner surface of the pipeline, in the section the stream will represent a circular ring (see sections G-D and B-B of Fig. 1), on the periphery of which there are ions, and in the central parts of the ring are demineralized water. Under these conditions, due to the combined action of the turbulent magnetic field flux and microvortices in the second section of the ion separator, it will be easier to separate the ions in a narrow zone near the inner wall of the pipeline and direct them according to their electric charge into the corresponding slots 7 and 11.

 There is no magnetic field in the side tubes 5 and 12 of the ion separator, therefore, the ions that entered the side tubes are not able to exit and can be carried out from the ion separator to the corresponding process devices. The concentration of cations and anions at the exit from the ion separator is 17.5%, respectively.

For industrial purposes, the 10 ion separators discussed above are combined into an ion separator block, as shown in FIG. Then the performance of one block of ion separators will be
80 • 10 = 800 t / h of demineralized water,
where 80 is the performance of one ion separator per hour.

 2. Separator of cations and anions from the hydration shell and a neutralizer of electric charges on ions (separator-converter).

 The process of separation from the ions of the hydration shell is carried out in the apparatus - separator of cations and anions from the hydration shell, combined with a neutralizer of electric charges on the ions.

 Figure 2 shows the separator-neutralizer.

 FIG. 2. Separator-converter: 24 - separator-converter; 25 is a schematic diagram of an apparatus for supplying a high voltage direct current to conical grids 40 and 48; 26 - voltage regulator; 27 - step-up transformer; 28 - high voltage rectifier; 29 - colonizing electrode; 30 - precipitation electrode; 31 - ionizer; 32 - input and output of high voltage to the grid with a positive charge; 33 - pipe for introducing vaporous catholyte; 34 - pipe for input vaporous anolyte; 35 - input and output of high voltage to the grid with a negative charge; 36 - heat-insulating housing of the separator-converter; 37 - a quencher of the speed of steam (catholyte) entering the apparatus; 38 - nozzle; 39 - contact ring for removing and supplying a positive charge from the grid to the ionization precipitation electrode; 40 - grid, carrying a positive electric charge; 41 - a directing cylinder (in the form of a cylindrical grid carrying a positive electric charge); 42 - a protective housing; 43 - a contact ring for supplying a positive electric charge to the grid of the cation separator from a high-voltage rectifier; 44 - installation site; 45 - funnel for directing steam into an absorption refrigeration machine; 46 - a protective housing; 47 - a directing cylinder (in the form of a cylindrical grid carrying an electric charge); 48 - grid carrying a negative electric charge; 49 - a contact ring for removing from the grid and supplying a negative electric charge to the corona electrode of the ionizer; 50 - receiver of steam passing through the grid; 51 - nozzle; 52 - a damper for the speed of steam (anolyte) entering the apparatus; 53 - a contact ring for supplying a negative electric charge to the grid of the separator of anions from the high-voltage rectifier; 54 and 55 - nozzles for the input and output from the heat exchanger of chilled and heated water; 56 - pipe for oxygen removal; 57 - pipe for condensate discharge; 58 - heat exchanger; 59 - a pipe for introducing a vapor-gas (oxygen + water vapor) mixture into a heat exchanger; 60 - ball electrode; 61 - low voltage direct current generator; 62 - pipe for the removal of steam into an absorption refrigeration machine; 63 - electrolytic bath: 64 - pipe for the removal of molten lithium; 65 is a pump for supplying molten lithium to a hydrogen generator; 66 - pipe for removal of molten lithium.

 The separator-neutralizer is designed to separate the hydration shell from anions and cations and neutralize electric charges on them to produce lithium metal, oxygen and reaction water.

Separator-neutralizer is a system that includes
1. Installation for supplying direct current of high voltage to the conical mesh separator of cations and anions from the hydration shell.

 2. The separator of cations and anions from the hydration shell, ie apparatus for producing cations and anions.

3. The converter of electric charges on cations and anions, ie obtaining the target products Li, O ₂ and H ₂ O, including a low voltage direct current generator.

 1. Installation for supplying direct current of high voltage to the conical mesh separator of cations and anions from the hydration shell.

 This setup is designed to create a high electric field strength on conical grids that can repel a charge of the same name located on a cation or anion, i.e. This field repels cations or anions from the nets, respectively, but water vapor passes through the nets.

 The basis for the installation is the AF-90-200 unit, designed for cleaning gases from impurities on an industrial scale.

 This unit has a maximum voltage of 90,000 V and a rated current of the secondary winding of the transformer 200 mA (8, p. 742). The circuit is shown in figure 2.

The installation is based on the principle of electric gas purification (4, p. 251-255), but the following change was made to it:
- a continuous stream of purified gas moving in the field of positive and negative charges on the corona and precipitation electrodes undergoes ionization, as described in (4, p. 251-255), here we use an inert gas Ar argon with an ionization potential of 15.755 eV according to the reaction Ar ⁰ -> Ar ⁺ (14, p. 250).

 - inert gas is in a closed volume, i.e. in a hermetically sealed container.

 The principle of operation of the installation (see figure 2).

Using a voltage regulator 26, a step-up transformer 27, a high-voltage transformer 28, a high-voltage direct current of 90,000 V and a current of 200 mA are supplied to the corona electrode 29 and the precipitation electrode 30 located in the ionizer 31. As a result of this, a “corona” arises between the corona and precipitation electrodes. When an "corona" in an airtight cylinder of the ionizer 31 is ionized rarefied gas Ar and wherein the formed electrons and positively charged cations of Ar ^+, the electric field positively charged cations of Ar ⁺ will move toward the discharge electrode and to neutralize it, and the negatively charged electrons will move to the precipitating electrode and also neutralize on it. As a result of gas ionization Ar, an external electric circuit is closed and an electric current flows along the entire circuit. In this case, a positive "+" electric charge arises on the conical grid 40, and a negative "-" electric charge on the conical grid 48.

 2. The separator of cations and anions from the hydration shell, ie apparatus for producing cations and anions.

The separator of cations and anions from the hydration shell (abbreviated as the separator) is designed to receive cations and anions bearing an electric charge (Li ⁺ and OH ^- ), and their subsequent supply to the neutralizer of electric charges on ions.

 The principle of operation of the separator is as follows.

For normal operation of the ion separator from the hydration shell, the following must first be observed:
- if the catholyte or anolyte vapor is fed inside the conical grids 40 and 48 directly from the hydrogen generator, then part of the catholyte or anolyte vapor, having a high incoming flow rate (P = 10 ⁶ Pa, T = 472 K), the cone of the grid and the paired ions will not be released from the hydration shell and enter the guide cylinders 41 and 47 and then into the neutralizer, where water vapor enters into a chemical reaction with the formed Li, and this is a premature reaction and cannot be allowed. When a vaporous anolyte passes through, OH ^- ion will not be formed from some part of the anolyte, which will lead to adverse reactions on the spherical electrode, but this is not desirable. There is only one way out - to quench the speed of the catholyte and anolyte entering the separator to a minimum, i.e. to the speed of steam passage through the grid and the steam entering the steam receiver 50. The steam speed can be adjusted by its condensation rate in the heat exchanger of the absorption refrigeration machine, where the steam from the receiver 50 goes to a further technological cycle - a constant resolution must be maintained in the system, which is formed due to condensation steam on the cold wall of the heat exchanger in an absorption refrigeration machine.

 The process itself proceeds as follows.

 From a hydrogen generator (see Fig. 3), vaporous catholyte and anolyte with a temperature of 473 K are supplied to the separator through different pipelines to the nozzles 33 and 34, respectively. Next, the steam is divided into two equal parts and enters the spray nozzles 38 and 51 and from of them into the vapor velocity damper 37 and 52. The steam jet is additionally sprayed by nozzles onto a multitude of tiny jets, thereby increasing the collision area of two steam jets having the same energy. In a collision, the velocity of both flows is extinguished to the optimum value, i.e. up to the steam passage through conical grids 40 and 48 to the cold grid of the heat exchanger in an absorption refrigeration machine.

 Due to the rarefaction obtained by condensation of water vapor, vaporous catholyte or anolyte, respectively, from the inside of the cone mesh rushes through the mesh cells 40 or 48 to the steam receiver 50, and from it through the pipe 62 to the heat exchanger of the absorption refrigeration machine (see Fig. 4) where the steam condenses and the condensate flows again like water into the production cycle.

The positive electric charge on the entire surface of the grid 40 and the negative electric charge on the grid 48 do not interact with water vapor, which is an insulator, and therefore steam passes freely through the grid, and cations, for example Li ⁺ , due to the high temperature of 473 K and a pressure of 10 ⁶ Pa Being already without a hydration shell, having approached a grid having a positively charged electric field, they repel the Li ⁺ cation to the center of the cone-shaped grid, because charges of the same name repel each other, but at the same time, with the cations moving toward the center of the conical network, they move down to the negatively charged electrode (molten lithium, through which electric current flows), because opposite charges are attracted to each other. Cations or anions exist only in a high voltage electric field under vacuum.

Аналогично проходит процесс на ионе

Нейтрализация электрических зарядов на ионах и является продолжением стадии 4, проводимой в аппарате-отделителе катионов и анионов от гидратной оболочки, совмещенном с нейтрализатором электрических зарядов на ионах (см. фиг.2).At the exit from the conical grid, Li ⁺ cations are concentrated in a cationic beam due to the circular action of a high-voltage electric field, enter the guiding cylinder, and then continuously fall on the molten lithium through which electric current flows, in the form of a cationic beam, i.e. electrons, due to which the reaction occurs

The process on the ion proceeds similarly.

The neutralization of electric charges on ions and is a continuation of stage 4, carried out in the apparatus separating cations and anions from the hydration shell, combined with a neutralizer of electric charges on ions (see figure 2).

 The process of neutralizing electric charges takes place in a neutralizer, which is the third component of the apparatus - the separator of cations and anions from the hydration shell.

The converter is designed for instantaneous electrochemical reactions with ions, for example with Li ⁺ and OH ^- .

The converter is a system consisting of a low voltage direct current generator 61 and an external part of the generator circuit, which includes
- metal ball contact 60;
- contact 63 of molten lithium;
- a guide cylinder 47 for supplying a Li ⁺ ion to the contact;
- a guide cylinder 60 for supplying OH ^- ion to the contact;
- heat exchanger 58 for cooling O ₂ and vapor H ₂ O;
a pump 65 for transferring molten lithium to a hydrogen generator.

 It can be seen from the scheme described above that the process taking place in the converter is not an electrolysis process, because there is no electrolyte, and therefore, there is no movement of ions along the external circuit of the generator through the electrolyte. This is the process of neutralizing an electrically charged particle, which occurs due to the recoil by the anion and the addition of electrons by the cation, i.e. there is an interionic transfer of electrons from anions to cations, while the anion is oxidized, and the cation is reduced.

 The principle of operation of the converter (according to the scheme of figure 2).

 When neutralizing electric charges on cations and anions, the principle of inter-ion transfer of electrons from the anion to the cation is carried out through the external circuit of the direct current generator 61 (in short - the generator).

 We consider the essence of this principle in reactions (9) and (10).

Согласно реакции (9) на восстановление четырех катионов лития Li⁺ требуется

Таким образом, при совместном проведении реакций (9) и (10) имеется полный баланс по электронам, т.е. четыре электрона освобождаются по реакции (10) и четыре электрона расходуется на проведение реакция (9).According to reaction (10), during the oxidation of four OH hydroxides ^- О ₂ and Н ₂ О are formed and are released

According to reaction (9), the reduction of four lithium cations Li ⁺ requires

Thus, when carrying out reactions (9) and (10) together, there is a complete electron balance, i.e. four electrons are released by reaction (10) and four electrons are spent on carrying out reaction (9).

 Technically, this issue is solved as follows.

 A ball contact 60 is connected to the external circuit of the generator 61, at which reaction (10) takes place.

 In order for reaction (10) to take place on the ball contact 60, it is necessary to continuously remove electrons, which can randomly flow off the ball contact 60 from the ball contact 60 in all directions. This cannot be allowed. Therefore, an electric current generated by a direct current generator with a strict direction of movement of electrons from the “+” terminal to the terminal “-” of the external circuit of the direct current generator flows through the ball contact 60. The electrons generated by the generator “carry away” the electrons obtained when the reaction (10) passes through terminal 60.

Thus, to the electrons formed by the generator 61 in the amount of Q ₁ and flowing along the internal and external circuits of the generator, in addition to the contact 60, the electrons formed by the reaction (10) in the amount of Q _{2 are} “poured” into the external circuit.

The total number of electrons flowing in the external circuit after contact 60 will be equal to Q ₁ + Q ₂ . This number of electrons, due to the direction of electron movement created by the generator in the external and internal circuits (from "+" to "-"), will also flow in this direction, it cannot be otherwise.

Electrons, having reached contact 63 in the amount of Q ₁ + Q ₂ , enter into reaction (9), for the conduct of which electrons in the amount of Q ₂ will be consumed, and the law of conservation of energy and mass will be observed.

The electrons remaining after the passage of contact 63 in the amount of Q ₁ pass through the clamp “-” of the generator back into the internal circuit and the cycle begins.

Contact 63 is a molten lithium bath through which electric current flows, i.e. electrons. The recovered Li ⁺ cation transforms into a lithium atom and immediately melts. As molten lithium accumulates, it is removed from the bath.

From the above it follows that the DC generator 61 is a carrier of electrons from reaction (10) to reaction (9). The reaction products O ₂ and H ₂ O through the pipe 59 and the heat exchanger 56 are removed from the Converter:
- oxygen to the compressor station;
- water for a repeated cycle.

 In this process, only a direct current generator 61 operates from an external energy source, providing the direction of motion of the electrons obtained by reaction (10).

 3. Hydrogen generator.

 Figure 3 presents a diagram of a hydrogen generator.

 Figure 3. Hydrogen generator diagram: 67 - hydrogen generator for the first production line, operating on lithium metal; 68 - pipe for the output of vaporous catholyte with a given temperature; 69 - pipe for outputting anolyte with a given temperature; 70 - heat-insulating casing of a hydrogen generator; 71 - a septum (two pieces) separates the catholyte from the anolyte in the annulus of the reaction zone; 72 - ring feeder of a hydrogen generator (condensate + demineralized water); 73 - nozzle; 74 - pipeline for supplying a reagent (water or molten lithium) to the nozzle; 75 - molten lithium distributor for nozzles; 76 — trajectory of the theoretical atomization by nozzles of water or molten lithium; 77 - reaction zone; 78 - ring feeder of a hydrogen generator with molten lithium; 79 - pipe for introducing anolyte into the annulus of the reaction zone; 80 - a zone of cooling of reaction products; 81 - heat exchanger; 82 - pipeline for the removal of hydrogen; 83 - pipe for draining an aqueous solution of LiOH; 84 - two nozzles for introducing cold coolant; 85 - pipe for the output of the heated coolant; 86 - pipe for introducing catholyte into the annulus of the reaction zone; 87 - pipe for introducing molten lithium into an annular feeder; 88 - nozzle water distributor; 89 - pipe for introducing water into the annular feeder; 90 - electric heater of catholyte vapor to a predetermined temperature; 91 - electric heater of anolyte vapor to a predetermined temperature.

A hydrogen generator is designed to produce hydrogen according to reaction (3):
2Li + 2H ₂ O -> H ₂ + 2LiOH (3).

 Alkaline or alkaline earth metals react with water in a heterogeneous phase.

If the process is carried out in a heterogeneous system between reagents located in different phases, then the reaction is carried out at the interface. Then the number of reaction acts does not refer to a unit volume, but to a unit surface and the dimension w (reaction rate) is measured as mol / s • cm ² . An example of such reactions can be the combustion processes of many solids in a gaseous oxidizing medium (O ₂ , Cl ₂ , etc.) or the action of water on active metals (6, p.205-206).

 From this it follows that in order to create a high reaction rate (3), it is necessary to create a large surface near molten lithium and water introduced into the reaction zone.

 How this issue is resolved is shown below.

The hydrogen generator is
1. The reaction chamber 77, cooled by catholyte and anolyte. Here, lithium interacts with water by reaction (3). Due to the heat of reaction and the electric heaters 90 and 91, the catholyte and anolyte are evaporated and are directed to a ion separator from the hydration shell with a temperature of 473 K and a pressure of 10 ⁶ Pa to produce ions (stage 4).

 2. The cooling zone of the reaction products, where on the heat exchangers 81 cooled by cold water, the reaction products are cooled to a temperature of 373 K.

3. The density of saturated water vapor is 0.5977 g / l (at 100 ^° C and 1 atm) (see 8, p. 607); hydrogen density 0.0899 g / l (at 0 ^° С and 1 atm) (see 8, p. 620); hydrogen is 7 times lighter than water vapor (0.5977: 0.0899 = 7), so it will easily be separated from water vapor and condensate and go into line 82.

 4. Hydrogen will also easily separate from the LiON aqueous solution and will be discharged from the hydrogen generator via line 82.

 5. The alkaline solution through the nozzle 83 is sent to a centrifuge to separate the solid impurities, i.e. purification filtration is carried out.

 The principle of operation of the hydrogen generator is as follows.

The eighteen nozzles 73 are supplied simultaneously
- in 9 nozzles molten lithium from stage 5;
- in 9 nozzles water (condensate and demineralized water) from stages 7 and 1.

Due to the increased pressure during the supply of liquids to the nozzles, the liquids twist in the nozzles and at the exit from the nozzle lithium and water are sprayed into tiny drops, which, moving towards each other and colliding, instantly react with each other (Li and Н ₂ О) , thus forming, according to reaction (3), hydrogen and lithium hydroxide.

 Due to the thermal effect of the reaction, unreacted water is converted to steam.

The excess heat remaining after heating the catholyte and anolyte is taken from the reaction zone 77 in the heat exchangers 81. Water cooled to +1 ^° C flows in the pipes of the heat exchanger ^. The heated coolant in the form of steam is melted through the pipe 85 into an absorption refrigeration machine to obtain the cold necessary for conducting the process.

 Let us determine how many times hydrogen is diluted with water vapor in a hydrogen generator. (Conventionally, we do the calculation without being brought to normal conditions).

1. The amount of hydrogen that is obtained from 14 kg of Li according to reaction (3) -22400 m ^{3 of} hydrogen (see material calculation).

2. During the evaporation of 18 g of H ₂ O, 22.4 liters of water vapor are formed, then in terms of t-mol we get
18 t-mol - 22400 m ³ pair
295 t mol - x
x = 367111 m ^{3 of} water vapor.

Dilution of hydrogen with water vapor in a hydrogen generator will be
367111: 22400 = 16.4 times.

 Thus, when hydrogen is diluted with water vapor 16.4 times, the possibility of a hydrogen explosion in the hydrogen generator is excluded.

 The nozzle 73 is a nozzle with a continuous spray cone (10, p. 77), it is used in cases where it is necessary to fully cover a certain surface and it is preferable to have a more uniform distribution of drops.

 The diameter of the outlet of these nozzles is 0.5-50 mm, and the productivity is 0.04-750 l / min.

 4. Upgraded absorption refrigeration machine.

 The reaction heat can be removed by cooling the reaction mass with water from the reservoir. But the water consumption will be huge and, in addition, the ambient temperature will change.

 The most suitable for cooling the reaction mass is the use of an absorption refrigeration machine, where almost all the heat released from the hydrogen generator is absorbed by the absorption machine to generate cold and ammonia from the aqueous ammonia solution.

 Figure 4 shows a diagram of a modernized absorption machine.

 FIG. 4. The scheme of the modernized absorption refrigeration machine: 92 - absorption refrigeration machine; 93 - a generator for evaporating a strong aqueous ammonia solution; 94 - capacitor; 95 - throttle valve; 96 - evaporator; 97 - pipe for the discharge of chilled water into the heat exchanger of a hydrogen generator; 98 - an absorber; 99 - throttle valve; 100 - heat exchanger; 101 - pump; 102 - condensate distributor; 103 - a pump for supplying condensate to the evaporator for cooling; 104 - a pump for supplying condensate to a hydrogen generator; 105 - pipe for condensate discharge to a hydrogen generator; 106 - pipe for introducing steam from the heat exchanger of the hydrogen generator; 107 - pipe for introducing steam coming from the ion separator from the hydration shell.

 The modernized absorption refrigeration machine is designed to remove heat from the hydrogen production reaction in a hydrogen generator and is as follows.

 Generator 93 (Fig. 4) serves to evaporate a strong aqueous ammonia solution - the following modernization is made here.

As the heat carrier for the evaporation of ammonia, steam is used coming from the heat exchanger 106 of the hydrogen generator (Fig. 3) and steam from the ion separator (Fig. 2). Condensate formed after heat exchange in an absorption machine is sent in appropriate amounts to a hydrogen generator to conduct a hydrogen production reaction, then in the evaporator 96 the condensate is cooled to about +1 ^o C and the cooled water is sent to a hydrogen generator heat exchanger 106 to remove heat from the reaction mass, t. e. water along this circuit goes through a closed cycle without leaving the absorption machine.

 The condenser 94, the throttling valves 95 and 99, the evaporator 96, the absorber 98, the pump 101, and the heat exchanger 100 have not been upgraded as part of the machine circuit.

 The basic principle of operation of a modernized absorption machine is the principle of operation taken from (5, p. 213) and (11, p. 411).

Gaseous ammonia (~ 95% NH ₃ ) released from the aqueous ammonia solution in generator 93 (12, p. 429 and 11, p. 411) at a high pressure of ≈10 ⁶ Pa (10 ata) and a temperature of 383 K enters the condenser 94, where it condenses, giving off heat Q to the cooling water. Liquefied ammonia at P = 10 ⁶ Pa and T = 298 K passes the throttling valve 95 and evaporates in the evaporator 96, absorbing heat at a low temperature level T ₀ from the condensate, and the condensate cooled to a temperature of +1 ^o C is sent through the pipe 97 to the pipe 84 a hydrogen generator to the heat exchanger 106. After the evaporator, gaseous ammonia with T = 253 K (-20 ^o C) and a pressure of P = 1.17 • 10 ⁵ Pa (1.2 ata) is sent to the absorber 98 and upon cooling (removal of heat of dissolution) absorbed by water with the formation of a highly concentrated solution (~ 50% NH ₃ ). The resulting solution is pumped by the pump 101 through the heat exchanger 100 to the generator 98. In the generator 93 due to the heating by water vapor (supply of heat of evaporation) coming through the nozzles 106 and 107 respectively from the heat exchanger of the hydrogen generator and from the ion separator from the hydration shell, most of the ammonia evaporates and in the form of gas it enters condenser 94, the depleted aqueous ammonia solution (~ 20% NH ₃ ) leaves the generator 93 through the heat exchanger 100 and the throttle valve 99 into the absorber 98, where it is again concentrated to ~ 50% as a result of gas absorption ammonia and is sent to the generator 93 for a second cycle.

 5. Fractional separator.

 Figure 5 presents a diagram of the fractional separator.

Figure 5. Fractional separator: 108 - fractional separator; 109 - pipe for loading sludge; 110 - turbine mixer, equipped with a gearbox and a special mechanism for raising and lowering the mixer: a) the mixer in the position of sedimentation of particles; b) a mixer in the position of suspension of particles; 111 - level of suspension of polymetallic conglomerate; 112 - shutter; 113 - shutter; 114 - drain pipe; 115 - valve; 116 - pipeline for draining the suspension of Ca (OH) ₂ sump; 117 - valve; 118 - pipe for filling demineralized water from bottom to top into the fractional separator; 119 - pipe for draining a suspension of polymetallic conglomerate into the sump; 120 - valve; 121 is a pipeline for directing a suspension of polymetallic conglomerate into the sump; 122 - pipeline for directing the suspension of Mg (OH) ₂ in the sump; 123 - valve; 124 - drain pipe; 125 - shutter; 126 - pipeline for draining water; 127 - valve; 128 - drain pipe.

 The theory of the process of fractional separation of solid particles is given in stage 15.

Fractional separator designed
- to separate a suspension of polymetallic conglomerate in demineralized water into three fractions:
suspension fraction Ca (OH) ₂ ;
a suspension fraction of Mg (OH) ₂ + Al (OH) ₃ (as a micro mixture);
a suspension fraction of the remaining compounds included in the polymetallic conglomerate;
- separation of the separated fractions from each other.

 The fractional separator is a column with a diameter of 2 meters and a height of ~ 65 meters, in which, based on the Stokes law, particles are separated according to their density and diameter.

 The principle of operation of the fractional separator.

 The fractional separator through the nozzle 118 is filled with demineralized water about 2 meters above the axis of the damper 112, after which the damper 112, 113 and 125 from a vertical position (relative to the plane of the damper) are translated into horizontal.

 Through the nozzle 109, the slurry is loaded into the upper part of the separator, which comes from the centrifuge from stage 13 in an amount equal to the three-hour operation of the hydrogen generator.

 The turbine agitator 110 is turned on, and the shutters 112, 113 and 125 are moved from horizontal to vertical, by which the slurry and demineralized water are transferred to the slurry.

 The turbine mixer 110 is turned off, and the shutters 112, 113 and 125 are moved from horizontal to vertical, after which particles of a polymetallic conglomerate in suspension in water are lowered by gravity.

 After 2 hours, the flaps 112, 113 and 125 are moved from a vertical to a horizontal position.

In 2 hours, particles of Ca (OH) ₂ and Al (OH) ₃ fall down the pipe by 42.24 meters and 54.72 meters, respectively, particles of heavier compounds in 2 hours of deposition will go from 87.84 meters to 709 ,2 meters. However, their lowering stops after the passage of the shutter 125, where particles accumulate at the pipe 11.

Installing dampers from the upper connector of the splitter housing cover:
- damper 112 - by 2.5 meters;
- shutter 113 - by 51 meters;
- shutter 125 - at 55 meters;
- the lower housing connector is installed at 55 m.

 After installing the dampers in a horizontal position, the dampers 115, 120 and 127 open, and the suspension divided by fractions is sent to the intermediate containers.

 Since the suspension fraction of the remaining hydroxides of metals and metals in terms of metals together weigh only ~ 24 kg, they are collected in a single collection in the form of powder at the bottom of the fractional separator from several separation processes, then the valve 120 is opened and the entire fraction is sent to an intermediate tank . From intermediate containers, suspensions of individual fractions are sent to centrifuges.

 The demineralized water centrate is sent to the drainage channel for demineralized water for further use, and the sludge (sediment) for further processing to stage 16.

 The list of figures and drawings and other materials.

 Figure 1. Ion separator and industrial ion separator unit.

 The diagram explains the ion separation device and the process of separation of sea water in a magnetic field into three fractions: anolyte - salt water - catholyte, and a diagram of the industrial block of ion separators is shown.

 FIG. 2. Separator of cations and anions from the hydration shell and a neutralizer of electric charges on ions (separator-converter).

A combined scheme of separating the hydration shell from hydrated cations and anions and neutralizing the electric charge on cations and anions is shown in order to obtain the target products Li, O ₂ and H ₂ O.

 Figure 3. Hydrogen generator.

 The diagram shows how the process of producing hydrogen in a large volume during the interaction of molten lithium and water supplied to the reaction zone in the form of microdrops is organized, and how the heat of the reaction of interaction between lithium and water is removed.

 Figure 4. Upgraded absorption refrigeration machine.

 The diagram shows what modernization was done in a typical absorption refrigeration machine and how heat is taken from the separator-converter and the hydrogen generator.

 Figure 5. Fractional separator.

 Based on the Stokes law, a process for the separation of polymetallic conglomerate into separate fractions was developed, and a fractional separator was created on the basis of this process.

 The figures related to the section "Information confirming the possibility of carrying out the invention."

 FIG. 6. The first production line for the production of demineralized water, hydrogen and oxygen.

 The diagram shows the sequence of equipment and the movement of material flows when receiving demineralized water, hydrogen and oxygen using lithium technology.

 FIG. 7. Scheme of a technological line for the extraction of cations and anions from sea water and their processing into target products.

 The diagram shows the sequence of arrangement of equipment and the movement of material flows with the processing of cations and anions extracted from sea water into target products.

 FIG. 8. Plant for the production of demineralized water, hydrogen and oxygen using lithium technology.

 The diagram shows the location of the first three production lines for producing demineralized water, hydrogen and oxygen using lithium technology and shows the ways of using catholyte and anolyte.

 Fig.9. Catholyte and anolyte processing plant.

 The diagram shows the location of the second processing lines and additional equipment and production facilities for the complete processing of catholyte and anolyte to target products.

 The first production line for the production of demineralized water, hydrogen and oxygen.

 Figure 6 presents a diagram of a first production line.

FIG. 6. Scheme of the first production line for the production of demineralized water, hydrogen, and oxygen: 13 - industrial block of ion separators; 16 - pipe for output anolyte; 19 - pipe for removal of demineralized water; 20 - pipe for removal of catholyte; 21 - pipe for entering into the industrial unit 13 separators of ions of sea water; 24 - separator-neutralizer; 33 - pipe for introducing vaporous catholyte; 34 - pipe for input vaporous anolyte; 40 - grid, carrying a positive electric charge; 48 - grid carrying a negative electric charge; 56 - pipe for oxygen removal; 57 - pipe for condensate drainage (reaction water); 62 - pipe for the removal of steam into the absorption machine; 66 - pipe for removal of molten lithium; 67 - hydrogen generator; 68 - pipe for the output of vaporous catholyte with a given temperature; 69 - pipe for outputting a vaporous anolyte with a given temperature; 79 - pipe for introducing anolyte into the annulus; 82 - pipe for the removal of hydrogen; 83 - pipe for draining an aqueous solution of LiOH; 84 - two nozzles (on both sides) for entering cold coolant; 85 - pipe for the output of the heated coolant; 86 - pipe for introducing catholyte into the annulus; 87 - pipe for introducing molten lithium; 89 - pipe for entering demineralized water into the annular feeder; 97 - pipe for the withdrawal of cold water from the absorption refrigeration machine and feeding it through the pipe 84 for a second cycle; 105 - pipe for condensate discharge to a hydrogen generator; 106 - pipe for introducing steam from the heat exchanger of the hydrogen generator; 107 - pipe for introducing steam entering
from the separator-converter; 129 - the second ion separator, dividing LiOH solution into anolyte and catholyte; 130 - pipe for entering the filtered LiOH solution; 131 - a pipe for outputting the anolyte with its direction into the pipe 79 of the hydrogen generator; 132 - pipe for output catholyte with its direction in the pipe 86 of a hydrogen generator; 133 - gas holder for oxygen; 135 - a mixer for mixing condensate with demineralized water coming from the block 13 of the ion separator; 134 - mixer for mixing condensate with steam; 136 - centrifuge; 137 - pipe for the output of the filtered LiON solution; 138 - pipe for outputting sludge; 139 - gas holder for hydrogen; 140 - water body; 141 - filter intake; 142 - pump; 143 - pipeline for drainage of anolyte; 144 - pipeline for the removal of catholyte; 145 - mixer of anolyte and catholyte; 146 - a spray of a mixture of anolyte and catholyte in a pond.

 The first production line is designed to produce demineralized water, hydrogen and oxygen from seawater.

 The first production line is an engineering structure, the basis of which is unparalleled high-speed apparatus for the processing of sea water to target products: demineralized water, hydrogen and oxygen.

 The principle of operation of the first production line.

 From the reservoir 140 through the filter intake 141 by means of a pump 142, sea water is supplied through the pipe 21 to the industrial block 13 of ion separators, where sea water is divided into fractions: anolyte - demineralized water - catholyte. Desalted water through the pipe 19 enters the mixer 135, where the desalted water is mixed with condensate, which comes from the absorption refrigeration machine 92 and is sent through the pipe 89 to a hydrogen generator 67.

 The anolyte and catholyte from the industrial block 13 of the ion separators are sent via pipelines 143 and 144, respectively, to the second production line or through the mixer 145 and the atomizer 146 back to the reservoir 140.

Hydrogen generator 67 is the central apparatus into which all the main material streams participating in the production of hydrogen flow and the material streams departing from it, participating in the production of Li, O ₂ and reaction water.

 In the hydrogen generator through the nozzles 89 and 87 (Fig.6), 18 nozzles simultaneously receive (according to the calculation) desalted water plus condensate (they are supplied from the industrial block of the ion separator 13 and absorption chiller 92), and the molten lithium from the neutralizer separator comes into tact 24. Nozzles of lithium and water are sprayed onto the smallest drops, creating a huge contact area between lithium and water.

 Under these conditions, the reaction of the interaction of lithium and water with the formation of hydrogen and an aqueous solution of LiOH, which are removed from the hydrogen generator 67 through the nozzles 82 and 83, respectively. Hydrogen through the pipe 82 is sent to the gas tank 139.

The reaction of lithium with water has a large thermal effect, equal to 484.9 kJ • mol ^-1 .

In a given operating mode, 969.8 million kJ of heat is released per hour in a hydrogen generator, which is removed by heat carriers, namely
- anolyte and catholyte, which are heated here to a temperature of 473 K;
- cold water, which is supplied with a temperature of 274 K;
- the heat goes to the evaporation of ammonia from a strong aqueous ammonia solution in an absorption refrigeration machine.

The vaporous anolyte and catholyte, heated to a temperature of 473 K, are sent through nozzles 64 and 68 to the separator-neutralizer 24 to obtain Li ⁺ and OH ^- ions, which carry positive and negative charges, respectively.

In the neutralizer, these charges on the ions are neutralized with the formation of Li, O ₂ and H ₂ O.

 Lithium in the molten state through the nozzles 66 and 87 is sent to the hydrogen generator for a second cycle, and oxygen through the nozzle 56 to the gas holder 133.

 The reaction water when receiving oxygen in the form of condensate is supplied to a hydrogen generator 67 through a pipe 57 and mixers 134 and 135 for a repeated cycle.

 Water vapor after separating it from the ions ("+" and "-") in the separator-neutralizer 24 and the water vapor in the hydrogen generator are supplied to the absorption machine 92 through pipes 107 m 106, respectively, to use their heat for evaporation of ammonia from a strong aqueous ammonia solution. Next, condensed water vapor in the form of condensate is supplied to the hydrogen generator for a repeated cycle (the supply is through the pipe 105, mixer 134, pipe 135 and pipe 89).

The heat is removed from the reaction as follows: cold water through the pipe 97 and pipe 84 enters the heat exchanger 81 (see Fig. 3) of the hydrogen generator, where due to the removal of the reaction heat, water in the heat exchanger tubes evaporates, and the steam through the pipe 85 and pipe 106 enters the absorption refrigeration machine 93 for the evaporation of ammonia from aqueous ammonia solution. Condensed vapor in the form of condensate through the condensate distributor 102 (Fig. 5) is sent to the evaporator 96, where it is cooled to a temperature of +1 ^o C and through the pipe 97 is sent to the hydrogen generator for a second cycle.

 The resulting LiON aqueous solution through the nozzle 83 enters a centrifuge 136, where the LiON aqueous solution is filtered off from possible solid impurities, then through the nozzles 137 and 130 the solution enters the second ion separator 129. Then, the LiON aqueous solution, divided into anolyte and catholyte, sent to a hydrogen generator for a second cycle of taking the heat of reaction from the reaction zone of the hydrogen generator.

 Anolyte through nozzles 131 and 79 enters the annulus of the reaction zone of the hydrogen generator.

 The annular space is divided by partitions into two parts for anolyte and catholyte.

 The catholyte through nozzles 132 and 86 enters the second half of the annulus of the reaction zone of the hydrogen generator.

 With the anolyte and catholyte entering the hydrogen generator from the second ion separator, a second cycle of work begins.

Thus, consideration of the scheme of the first production line showed that the material flows continuously, each in its own circuit, and lithium is not removed from the technological cycle, but is continuously circulated from one device to another in the form of Li, Li ⁺ or LiOH, respectively, of the process stage.

 Desalted water is continuously added to the technological process, which goes to the formation of hydrogen and oxygen, which are continuously discharged from the technological line.

Removing cations and anions from seawater and converting them into metal atoms and corresponding gases (H ₂ , O ₂ , Cl ₂ , Br ₂ , I ₂ , F ₂ , SO ₃ ).

The extraction of metal salts contained in it from sea water is carried out on the second processing line for the processing of sea water in the following stages:
Stage 9. Obtaining cations and anions that do not contain a hydration shell in the separator-neutralizer.

 Stage 10. Neutralization of electric charges on ions that do not contain a hydration shell, with the formation of target products.

 Stage 11. Separation of the gas mixture.

 Stage 12. Obtaining hydrogen by the interaction of an alkaline melt with water.

 Stage 13. Centrifugation of a suspension of alkaline solution.

Stage 14. The conversion of metal hydroxides (N ₂ , K, Li, Rb, Cs) in the halides, sulfates and carbonates of these metals.

Stage 15. Fractional separation of the suspension of polymetallic conglomerate into three fractions:
- fraction of hydroxide Ca (OH) ₂ ;
- fraction Mg (OH) ₂ and Al (OH) ₃ ;
- fraction of the remaining hydroxides of metals and individual metals.

Stage 16. Processing of Ca (OH) ₂ , Mg (OH) ₂ and the rest of the polymetallic conglomerate.

 Description of the stages of the process.

 Stage 9. Obtaining cations and anions that do not contain a hydration shell in a separator-neutralizer.

 The theoretical basis of this process is given above in stage 4. The process takes place in the apparatus of the separator-neutralizer (figure 2).

 Let us consider what electrochemical processes take place upon receipt of cations that do not contain a hydration shell.

The dry residue of sea salt contains 77.7% NaCl, i.e. NaCl is the basis of the salts contained in seawater. To simplify further calculations, we assume that all the cations contained in seawater are conditionally Na ⁺ cations, and the error in the approximate calculation will be quite acceptable for this type of calculation.

 Consider the processes occurring during the separation of ions from water, i.e. obtaining ions that do not contain a hydration shell.

Нагрев католита происходит в два приема
- предварительный нагрев на стадии 14 в реакторе-смесителе за счет теплоты растворения газов в воде и химических реакций (24-30);
- окончательный нагрев происходит на стадии 12 в генераторе водорода за счет тепла реакции получения водорода из натрия и воды.I. The separation of metal cations from water goes through two phases:
a) heating of catholyte (cations + water)
Catholyte

Catholicite heating occurs in two steps
- preliminary heating at stage 14 in the reactor-mixer due to the heat of dissolution of gases in water and chemical reactions (24-30);
- the final heating occurs at stage 12 in a hydrogen generator due to the heat of the reaction to produce hydrogen from sodium and water.

2. Рассмотрим процессы, проходящие при получении анионов, не содержащих гидратной оболочки.b) separation of the cation from saturated steam

2. Consider the processes that take place upon receipt of anions that do not contain a hydration shell.

Нагрев анолита, как и католита, происходит в два приема на стадиях 14 и 12.We also assume that all anions are conditionally Cl ^- anions. The separation of anions from water takes place in two phases:
a) heating anolyte (anions + water)
Anolyte

Anolyte, like catholyte, is heated in two stages at stages 14 and 12.

Стадия 10. Нейтрализация электрических зарядов на ионах с образованием целевых продуктов.b) separation of the anion from saturated vapor:

Stage 10. Neutralization of electric charges on ions with the formation of target products.

This process takes place in the separator-neutralizer (figure 2) simultaneously in two directions:
1 - reduction of cations;
2 - oxidation of anions.

М²⁺ + 2е^- --> М (двухвалентный) (12)
М³⁺ + 3е^- --> М (трехвалентный) (13)
где М - металл и его катион.a) reactions occurring during the reduction of cations at contact 63 (Fig. 2), consisting of molten sodium (formerly lithium)

M ²⁺ + 2e ^- -> M (divalent) (12)
M ³⁺ + 3e ^- -> M (trivalent) (13)
where M is a metal and its cation.

 Metallic sodium and potassium with many metals form alloys of various compositions that are soluble in excess molten sodium (24). Metals that do not form alloys with sodium and potassium will be in the sodium melt in the form of a suspension.

 At stage 10 obtained: alkaline molten metal, which includes all the metals shown in the table.

 b) reactions occurring during the oxidation of anions at the spherical contact 60 (Fig. 2).

Образовавшаяся на контакте 60 смесь газов (температура 473 К) направляется в цех по разделению газовой смеси.

The gas mixture formed at terminal 60 (temperature 473 K) is sent to the gas mixture separation workshop.

 Stage 11. Separation of the gas mixture.

The gas mixture contains Cl ₂ , Br ₂ , J ₂ , F ₂ , SO ₃ , CO ₂ , O ₂ . According to the request of the industry, a certain part of the gas mixture is separated from the total volume of the gas mixture through the distribution panel and subjected to fractional separation according to (4, p. 750). Fractional separation products are sent to consumers or used locally.

 The remaining undivided gas mixture is sent to stage 14 to the reactor-mixer for the conversion of metal hydroxides (NaOH, KOH, LiOH, RbOH, CsOH) into chlorides, bromides, iodides, fluorides, sulfates and carbonates in appropriate quantities.

 Stage 12. Obtaining hydrogen by the interaction of an alkaline melt with water.

 From stage 10 to stage 12, the alkaline metal melt enters the hydrogen generator.

At this stage, the following reactions proceed:
a) reactions leading to the formation of hydrogen and water-soluble alkaline compounds:
2Na + 2 H ₂ O -> H ₂ + NaOH
NaOH -> Na ⁺ + OH ^- (21)
Similarly, sodium undergoes reactions with K and My, Li, Rb, Cs;
b) reactions leading to the formation of hydrogen and a water-insoluble polymetallic conglomerate.

With bivalent and trivalent metals forming water-insoluble or slightly soluble metal hydroxides, reactions take place, for example
Mg + 2H ₂ O -> H ₂ + Mg (OH) ₂ (22)
2Al + 6H ₂ O -> 3H ₂ + Al (OH) ₃ (23)
The following metal hydroxides belong to this group: Al, Ba, Fe (II), Fe (III), Y, Ca, Co, Mg, Mn, Cu, Ni, Pb, Sr, La, Ra, Sc, U.

 A number of the metals indicated below do not react with water and do not form metal hydroxides and include metals Sr, Ga, Au, Mo, As, Sn, Hg, Se, Ag, Th, Cr, Si, V, Zn.

 Thus, all the metal hydroxides and individual metals listed in paragraph “b” (not reacting with water) make up the so-called “polymetallic conglomerate”, i.e. water-insoluble mixture of all elements included in the table with the exception of alkali metals. These metals, together with metal hydroxides, are washed off the walls of the reactor with steam and an alkaline solution, and the resulting suspension, together with water vapor and hydrogen, is sent to heat exchanger 81 (Fig. 3), where water vapor condenses and is separated from hydrogen.

 The condensate is an alkaline solution of Na, K, Li, Rb, Cs, which also includes a polymetallic conglomerate and, after cooling in the heat exchanger 81, the condensate suspension is sent to stage 13 "Centrifugation of the alkaline solution suspension".

 Hydrogen, having passed the heat exchanger 81 (Fig. 3), cooled by cold water, is sent to the hydrogen compressor station 200 (Fig. 8).

 Stage 13. Centrifugation of a suspension of alkaline solution.

An alkaline suspension containing a polymetallic conglomerate is fed to the stage. The centrifugation process is ongoing, and at the same time
- sludge (polymetallic conglomerate) is sent to fractional separator 103 (Fig. 5), where the polymetallic conglomerate is mixed with desalted water to form a suspension and subsequent separation of the resulting suspension into fractions depending on the density of the metal or metal hydroxide and particle size;
- the centrate (alkaline solution) from the centrifuge 178 (Fig.7) is sent in two lines
a) to stage 14;
b) to the distribution panel 188 (Fig. 7) and from it to the central point 214 (Fig. 9) of the distribution of material flows.

By order of the industry, a certain part of the alkaline solution is taken and sent to workshop 228 (Fig. 9) to separate NaOH from KOH and obtain concentrated solutions of NaOH and KOH, as well as solid KOH and NaOH. RbOH, LiOH, CsOH are not released from the solution, because the content in sea water of Rb, Li and Cs in terms of metal is 1.5 • 10 ^-5 - 2 • 10 ^-7 % (weight), i.e. very small amount.

 Stage 14. Transfer of metal hydroxides (Na. K, Li, Rb, Cs) to the halides, sulfates and carbonates of these metals.

As a result of physico-chemical effects on the anolyte and catholyte obtained
- hydrogen - is used as a target product for its intended purpose (mainly for the reduction of metal hydroxides);
- polymetallic conglomerate - used as raw materials for chemical and metallurgical plants to obtain target products from it;
- a mixture of gases (Cl ₂ , Br ₂ , J ₂ , F ₂ , SO ₃ , O ₂ , CO ₂ ) - industry will use only a smaller part of the total amount of gases obtained, most of these gases are not used and their disposal is required;
- alkaline metal solution (Na, K, Li, Rb, Cs) - the industry will also use a smaller portion of the total alkaline solution obtained, most of this solution will not be used and their disposal is required;
- a mixture of gases (Cl ₂ , Br ₂ , J ₂ , F ₂ , SO ₃ , O ₂ , CO ₂ ) and an alkaline solution of metals (Na, K, Li, Rb, Cs) obtained during the physicochemical process, leave on the surface in huge quantities is impractical, because ecological disaster may occur, therefore, a mixture of gases and an alkaline metal solution must be converted to salts, which are the basis of sea water, such as: NaCl, NaBr, NaJ, NaF, Na ₂ SO ₄ , Na ₂ CO ₃ and, accordingly, K, Li, Rb , Cs, for this, the alkaline solution and the gas mixture are sent to the reactor-mixer apparatus 147 (Fig. 7) and the mixture obtained there is poured into the ocean through a ~ 1 km long pipeline and with many small holes along the length of the pipeline, which is perpendicular to the sea current at the bottom of the ocean, leading to a gradual restoration w salt concentration in sea ocean.

 Consider the chemical processes according to which you can complete the task.

хлорноватистая кислота легко разлагается
НClО --> HXL + 1/2 O₂ (25)
на чем основано белящее и дезинфицирующее действия хлора в присутствии воды.I. When chlorine is dissolved in water, hydrolysis occurs with the formation of hypochlorous acid

hypochlorous acid easily decomposes
HClO -> HXL + 1/2 O ₂ (25)
what is the basis of the whitening and disinfecting effect of chlorine in the presence of water.

2. Released HCl interacts with NaOH by reaction
NaOH + HCl -> NaCl + H ₂ O (26)
A similar reaction takes place with hydroxides K, Li, Rb, Cs.

3. Sulfuric anhydride SO ₃ , dissolving in water, forms sulfuric acid
SO ₃ + H ₂ O -> H ₂ SO ₄ (27)
4. Sulfuric acid reacts with NaOH
2NaOH + H ₂ SO ₄ -> Na ₂ SO ₄ + 2H ₂ O (28)
a similar reaction occurs with the hydroxides K, Li, Rb, Cs.

6. Угольная кислота реагирует с NaOH
Н₂СО₃ + NaОН --> Na₂СО₃ + 2Н₂О (30)
аналогично идет реакция и с гидроксидами K, Li, Rb, Cs.5. Coal anhydride CO ₂ reacts with water by reaction (12, p. 314)

6. Carbonic acid reacts with NaOH
H ₂ CO ₃ + NaOH -> Na ₂ CO ₃ + 2H ₂ O (30)
a similar reaction occurs with the hydroxides K, Li, Rb, Cs.

 Thus, chemical reactions (24-30) show that the interaction of an alkaline solution and a mixture of gases produces salts contained in sea water, but without salts that make up the poly-conglomerate of metals.

Таким образом, океан сам приводит неравновесную систему в ионное равновесие, т.е. количество катионов равно количеству анионов с соблюдением и электрического равновесия по зарядам, т.е. количество положительных зарядов равно количеству отрицательных зарядов.It should be noted
- due to the fact that the polymetallic conglomerate is removed from the process, there will always be an excess of the number of anions in the outgoing sea water compared to the number of cations. As a result of this, a slightly-weakly acidic solution of sea water will be supplied to the ocean from the mixing reactor 147 (Fig. 7);
- the final neutralization of this solution will occur with a large dilution of the seawater effluent directly in the waters of the oceans and the interaction of free acids with CaCO ₃ (shell rock) located in microscopic organisms of the oceans, for example
2НCl + CaCO ₃ -> CaCl ₂ + Н ₂ CO ₃ (31)

Thus, the ocean itself brings the nonequilibrium system into ionic equilibrium, i.e. the number of cations is equal to the number of anions in compliance with the electrical equilibrium in charges, i.e. the number of positive charges is equal to the number of negative charges.

 This process is carried out in a mixing reactor, which is designed to convert metal hydroxides (Na, K, Li, Rb, Cs) into the halides, sulfates and carbonates of these metals.

 The mixing reactor is a hydrogen generator (described above), but instead of hydrogen, oxygen released by reaction (25) enters the pipeline to remove hydrogen.

 The principle of operation of the reactor-mixer, see above.

 The oxygen formed according to reaction (25) is discharged from the mixer reactor through the pipeline 198 (Fig. 8) and sent to the oxygen compressor station 203 (Fig. 8), the cooled brine through the pipe goes to the ocean.

 The second production line for the extraction of cations and anions from sea water and their processing into target products.

 A second production line is included in the process, see FIG. 7.

7. Diagram of a technological line for the extraction of cations and anions from sea water and their processing into target products: 147 - reactor-mixer; 148 - pipe for the output of the heated anolyte; 149 - pipe for output heated catholyte; 150 - pipe for entering an alkaline solution; 151 - pipe for entering cold catholyte; 152 - pipeline for the removal of oxygen; 153 - pipe for the removal of oxygen to an oxygen compressor station; 154 - pipe for entering cold coolant; 155 - pipe for the discharge of saline into the ocean; 156 - pipe for removing the hot fluid; 157 - pipe for entering cold anolyte; 158 - pipe for introducing a mixture of gases; 159 - hydrogen generator; works on an alkaline melt; 160 - pipe for outputting anolyte vapor; 161 - pipe for the withdrawal of steam catholyte; 162 - pipe for introducing condensate; 163 - pipe for input alkaline sodium melt; 164 - pipe for entering heated catholyte; 165 - pipe for the removal of hydrogen; 166 - pipe for the removal of hydrogen in a hydrogen compressor station; 167 - pipe for entering cold coolant; 168 - pipe for the withdrawal of alkaline solution; 169 - pipe for the withdrawal of hot coolant; 170 - pipe for entering a heated anolyte; 171 - separator-neutralizer, operates on an alkaline melt; 172 - pipe for introducing a pair of catholyte; 173 - pipe for introducing anolyte vapor; 174 - pipe for the removal of a mixture of gases sent to neutralization in the reactor-mixer; 175 - pipe for the removal of gases directed to fractional separation; 176 - pipe for the removal of steam from the anolyte and catholyte in the absorption refrigeration machine; 177 - pipe for removal of alkaline melt; 178 - a centrifuge; 179 - pipe for entering an alkaline solution; 180 - pipe for the output of sludge (sludge); 181 - pipe for the removal of alkaline solution; 182 - absorption refrigeration machine; 183 - pipe for the removal of cold coolant (+1 ^o C); 184 - pipe for entering a hot fluid; 185 - pipe for condensate discharge and its supply to the hydrogen generator; 186 - pipe for introducing superheated steam from the separator-converter; 187 - mixer; 188 - distribution panel; 189 - pipe for receiving hydrogen; 190 - pipe for receiving a mixture of gases for separation; 191 - pipe for receiving oxygen; 192 - pipe for receiving alkaline solution sent for separation; 193 - pipe for receiving sludge polymetallic conglomerate for fractional separation; 194 — A pump for supplying saline back to the ocean.

 The second production line is designed for the processing of sea water and the allocation of target products from it: metals and their salts, hydrogen and oxygen. This line is an engineering complex consisting of a highly efficient technological process and a new type of apparatus providing high speeds of the process.

 The principle of operation of the technological line is as follows.

 From the ion separator 13 (Fig. 7) to the reactor-mixer 147 (Fig. 7) for preheating, catholyte and anolyte are separately supplied to the annular spaces through the nozzles 157 and 151, respectively. Due to the heat of reaction, the catholyte and acolyte, being heated, cool the reaction mass in the reactor-mixer. The heated catholyte and anolyte through the nozzles 148 and 149 are sent to the hydrogen generator 159 and through the nozzles 170 and 164 enter the annulus of the hydrogen generator. Due to the heat of reaction, catholyte and anolyte pass into steam. The vaporous catholyte and anolyte are sent through nozzles 160 and 161 to a separator-neutralizer 171. Through a nozzle 172, catholyte pairs enter the cation separator from the hydration shell, i.e. obtaining cations carrying a positive electric charge. In the converter, the cation is reduced by an electron and passes into a neutral metal atom and, in the form of an alkaline melt, passes through a nozzle 177 and 163 to a hydrogen generator 159. Here the alkaline melt reacts with water to produce hydrogen and a polymetallic conglomerate. Hydrogen through the pipe 166 and pipe 189 enters the distribution panel 188 and then to the destination.

 The suspension of the alkaline solution and the polymetallic conglomerate through the nozzle 168 is sent to a centrifuge 178. The slurry of the polymetallic conglomerate is sent to the nozzle 193 of the distribution panel 188 and then to the destination.

The alkaline solution through the pipe 181 is divided into two streams:
- through the nozzle 181 and the distribution panel 188 with a click, the solution is sent to separation by components;
- the alkaline solution through the pipe 150 is sent to the mixer reactor, where the reaction of converting the alkaline solution and gas mixture into alkali metal salts, the aqueous solution of which is sent back to the ocean by pump 194, is carried out.

Anolyte vapor through the pipe 173 enters the separator of anions from the hydration shell, i.e. obtaining anions bearing a negative electric charge. In the catalyst, the anion is oxidized to free gas molecules, for example, Cl ₂ , Br ₂ , SO ₃ , etc. The resulting gases are divided into two streams
- through the pipe 174, the gas mixture is sent to the reactor-mixer through the pipe 158 to interact with the alkaline solution sprayed by the nozzles; oxygen formed after reactions 18 and 19 in the separator-neutralizer enters the reactor-mixer 147 and does not participate in further reactions, and it is discharged through line 152 and pipe 153 to the distribution panel 188, and then through pipe 192 as intended;
- alkaline solution through the pipe 155 using the pump 194 is sent back to the ocean.

Thus, in the considered technological line, catholyte and anolyte introduced into it are obtained
- hydrogen;
- oxygen;
- alkaline solution;
- a mixture of gases;
- polymetallic conglomerate.

 Hydrogen and oxygen are immediately used as target products, and the alkaline solution, gas mixture, and polymetallic conglomerate are subjected to further processing in order to isolate target products from them.

 Plant for the production of demineralized water, hydrogen and oxygen using lithium technology.

As calculations have shown, in the processing of 1 km ³ (10 ⁹ tons) of sea water with a content of 3.5% of salts, 965000000 tons of demineralized water is formed (at 100% processing) and 1200898496000 m ^{3 of} hydrogen and 600449248000 m ^{3 of} oxygen can be obtained from it.

From the material balance it is known that one hydrogen generator produces 22,400 m ^{3 of} hydrogen per hour.

Let us determine how much hydrogen generators need to be installed to produce 120089849600 m ^{3 of} hydrogen per year.

1. 22400 • 24 = 537600 m ^{3 of} hydrogen per day
2. 537600 • 350 = 188160000 m ^{3 of} hydrogen per year (we will take 350 working days a year, 15 days - scheduled preventive maintenance)
3. 1200898498000: 188160000 = 6382.32 hydrogen generators needed
4. we will accept that 200 plants of such will be established in Russia, then one plant must be installed
6362.32: 200 = 31.91≈32 hydrogen generators,
those. At one plant, 32 production lines need to be installed.

 On Fig shows a diagram of a plant for the processing of sea water to produce demineralized water, hydrogen and oxygen using lithium technology.

 7. The scheme of the plant for producing demineralized water, hydrogen and oxygen using lithium technology.

 I - XXXII - desalinated water processing lines; 140 - a reservoir with sea water; 141 - seawater intake; 13 is a block of ion separators; 146 - separator into small streams of concentrated (17.5 wt.%) Solution, outgoing sea water up to 1000 meters long (used only when catholyte and anolyte are not processed); 196 - channel for removal of demineralized water; 197 - a demineralized water intake; 198 - a pipeline for supplying oxygen to a compressor station; 199 - pipe for supplying hydrogen to the main pipeline; 200 - hydrogen compressor station; 201 - a pipeline for supplying hydrogen to a compressor station; 202 - pipe for supplying oxygen to the main pipeline; 203 - oxygen compressor station.

The seawater processing plant is designed to produce demineralized water, hydrogen, oxygen, anolyte and catholyte. The plant is a
- three blocks of ion separators to obtain desalted water;
- a drainage channel for removal of demineralized water;
- 32 production lines for the production of hydrogen and oxygen;
- two compressor stations for the purification, cooling and injection of hydrogen and oxygen into main pipelines.

 And all this is combined into a single continuous technological cycle.

 The principle of operation of the sea water processing plant is as follows.

 From the reservoir 140 through the intakes 144 sea water is supplied to three blocks of ion separators 13, where sea water is divided into three fractions: anolyte - demineralized water - catholyte. Desalted water in the amount of 2400 tons per hour (from three blocks of ion separators) is sent to channel 196 to drain the desalted water.

Anolyte and catholyte are sent in two directions
a) are mixed (see stage 2) and squeezed out in thin streams into the ocean through the holes of the separator 4;
b) are sent (if there is a need for them) via pipelines 143 and 144 to the anolyte and catholyte processing plant.

 Desalted water flowing through the outlet channel 196, with the help of intakes 197 is supplied to the hydrogen generator of the production line to produce hydrogen and oxygen. 36 tons of demineralized water per hour are consumed to produce hydrogen and oxygen in one production line. 1152 tons of demineralized water per hour are supplied to 32 production lines. The rest of 2400-1152 = 1248 tons per hour is supplied for industrial needs, for example, anolyte and catholyte processing plant or irrigation of farmland and development of desert lands. If there is no need for demineralized water for agricultural production, then one block of ion separators is turned off.

 Hydrogen and oxygen obtained on production lines through pipelines 198 and 201, respectively, are supplied to compressor stations 200 and 203, where gas is cleaned, dried, and injected into main pipelines.

 Anolyte and catholyte processing plant.

 Figure 9 shows a diagram of anolyte and catholyte processing plant.

FIG. 9. Scheme of the anolyte and catholyte processing plant: 208 - production line for the extraction of cations and anions from sea water; 214 - neutral console distribution of material flows; 215 - a pipeline for supplying hydrogen to a hydrogen compressor station; 216 - workshop for the separation of a mixture of gases; 222 - pipe for outputting an undivided gas mixture; 223 - pipe for entering an undivided mixture of gases directed to other purposes; 224 - a pipe for introducing an undivided alkaline solution; 225 - reactor-mixer; 226 - pipe for entering an undivided gas mixture; 227 - pipe for draining saline back into the ocean; 228 - workshop for the separation of alkaline solution; 229 - a pipe for introducing an undivided alkaline solution; 230 - a pipe for outputting an undivided alkaline solution; 231, 232, 233, 234 - nozzles for outputting the separated fractions of an alkaline solution; 235 - a pipeline for supplying oxygen to an oxygen compressor station; 236 - screw feeder for feeding a polymetallic conglomerate; 237 - fractional separator of polymetallic conglomerate; 238 - an intermediate container for collecting polymetallic conglomerate (without Ca (OH) ₂ and Mg (OH) ₂ ); 239 - an intermediate container for collecting Mg (OH) ₂ ; 240 - an intermediate tank for collecting water; 241 - an intermediate container for collecting Ca (OH) ₂ ; 242 - fractional separator for re-separation of fractions of a polymetallic conglomerate; 243 - workshop for the production of salts of Ca and Mg; 244 — reduction furnace Ca (OH) ₂ ; 245 - reducing furnace Mg (OH) ₂ ; 246 - reduction furnace multimetallic conglomerate.

The anolyte and catholyte processing plant is designed to obtain the following target products due to the electrochemical and chemical reactions to which the anolyte and catholyte undergo:
- hydrogen;
- oxygen;
- metals contained in sea water;
- gas mixtures (Cl ₂ , Br ₂ , J ₂ , F ₂ , SO ₃ and CO ₂ );
- alkaline solution (NaOH + KOH + impurities);
- individual compounds from an alkaline solution.

 The presence of a large amount of alkaline solution allows the organization of the production of soluble glass (liquid glass) and acid-resistant cement based on it for the manufacture of large-diameter reinforced concrete pipes for pumping demineralized water from the coast to the mainland, where plants for the production of hydrogen and oxygen are installed.

 The plant for the processing of anolyte and catholyte is a group of physico-chemical industries, combined into one whole production.

The structure of the plant (Fig. 9) includes three production lines for the extraction of cations and anions from sea water and the production of processing cations and anions, which includes
- Central console flow distribution 214;
- workshop for the separation of a mixture of gases 216;
- reactor-mixer 225;
- shop for the separation of alkaline solution 228;
- three fractional separators 237;
- fractional separator for re-separation of fractions of the polymetallic conglomerate 242;
- a workshop for the production of other Ca and Mg 243 salts from Ca (OH) ₂ and Mg (OH) ₂ ;
- reduction furnaces 244, 245, 246.

 Hydrogen obtained after reactions 11, 12 and 13, through a separator of hydrogen streams 247 is directed to a hydrogen reduction furnace, and an excess of hydrogen is sent to a hydrogen compressor station.

 Oxygen obtained by reaction 25 is separated from the gas mixture and sent via pipeline 235 to an oxygen compressor station.

 The principle of the plant for processing anolyte and catholyte.

 From three production lines (Fig. 7), the resulting products are sent to the central console for the distribution of material flows 214 (Fig. 9), where the flows of the same name are collected and removed from the pipes: 209 - hydrogen; 210 - a mixture of gases for separation, 211 - oxygen; 212 - alkaline solution (a mixture of NaOH and KOH and trace elements LiOH, RbOH, CsOH); 213 - polymetallic conglomerate.

 By order of the industry, the gas mixture is sent to workshop 216 for gas separation (through pipe 223), where due to the cooling of the gas mixture in the heat exchangers with a refrigerant, fractional separation of the gas mixture occurs. A certain amount of individual gases is taken and sent to the customer. The remaining undivided portion of the gas mixture is sent to the reactor-mixer 225, where the alkaline solution interacts with the gases according to reactions 14-20. The resulting saline solution, representing halogens, sulfates and carbonates of Na and K, merges back into the ocean.

 Also, by order of the industry, the alkaline solution is sent through pipe 212 to workshop 228, where a certain part of the solution is divided into NaOH and KOH, and concentrated (40%) solutions of NaOH and KOH and solid NaOH and KOH are obtained from them. The remainder of the undivided alkaline solution is sent to the reactor-mixer 225 for reactions in it (14-20).

 A polymetallic conglomerate in the form of sludge (sediment) from a centrifuge through a nozzle 213 is fed by screw feeders to the fractional separators 237. A portion of the polymetallic conglomerate in the amount of three-hour production from one production line is loaded into each fractional separator, because the total time for the suspension separation process is three hours, and three fractional separators included in the production line will provide a semi-continuous process for the separation of polymetallic conglomerate.

In fractional separator 237, Ca (OH) ₂ , Mg (OH) ₂ fractions are separated from the suspension, and the fraction from the mixture of other metal hydroxides, individual metals and water is sent to intermediate containers 238, 239, 240 and 241.

Part of Ca (OH) ₂ and Mg (OH) ₂ goes to workshop 243 to obtain salts of Ca and Mg. Most of Ca (OH) ₂ and Mg (OH) ₂ goes to reduction furnaces 244, 245 to reduce metal hydroxides with hydrogen to individual metals Ca and Mg, and for Ca, in addition, also to CaH ₂ .

 The polymetallic conglomerate and individual metals accumulated in the intermediate tanks are sent by a screw feeder to the fractional separator, where the individual metals are separated from the metal hydroxides, which are collected in an intermediate tank and sent to the reduction furnace 246. From there, the metal powders are sent to a concentration plant for the final separation of metal powders by the method flotation on individual metals.

 Thus, the device developed and described above for the continuous processing of sea water can actually fulfill the main objective of the invention - to replace hydrocarbon fuel with environmentally friendly hydrogen fuel (pure hydrogen) and provide the world's population with demineralized water and raw materials for the chemical and metallurgical industries.

 Soluble glass production.

 Soluble glass - colorless or slightly colored green or yellow transparent hardened melt, consisting of alkaline silicates.

Gross soluble glass formula:
R ₂ O • mSiO ₂ ,
where: R ₂ O-Na ₂ O or K ₂ O;
m is the number of SiO ₂ molecules.

 Soluble glass is obtained by fusing a mixture of quartz sand with soda or sodium sulfate and coal in continuously operating glass melting furnaces using a technology similar to industrial insoluble glass. The resulting melt is called "silicate - block", and acid-resistant cement is obtained from it (3, p. 1037).

 In our case, the most acceptable is the method of obtaining soluble glass by processing amorphous silica with concentrated solutions of caustic alkalis in rotating autoclaves (3, p. 1037).

 Concentrated alkali solutions are obtained in workshop 228, Fig. 9.

The general production scheme is as follows:
nNaOH (KOH) + mSiO ₂ • R ₂ O -> mSiO ₂ -> acid-resistant cement -> reinforced concrete pipes and other products.

 The use of an alkaline solution according to the above scheme will ensure the pumping of demineralized water to specified regions of Russia without the use of metal pipes.

Literature
1. Sokolsky Yu.M. Magnetized water: truth and fiction. L .: Chemistry, 1990.

 2. Lomonosov V. Yu., Polivanov K.M., Mikhailov O.P. Electrical Engineering M .: Energoizdat, 1990.

 3. Dickerson R., Gray G., Haight J. Basic laws of chemistry, Vol. 2, ed. The World, 1982.

 4. Kasatkin A.G. The main processes and apparatuses of chemical technology M .: Chemistry, 1971.

 5. Planovsky A.N., Nikolaev P.I. Processes and devices of chemical and petrochemical technology. M .: Chemistry, 1972.

 6. Pavlov N.N. Theoretical foundations of general chemistry. M .: Higher school, 1978.

 7. Brief chemical encyclopedia. V.4, M .: Soviet Encyclopedia, 1965.

 8. Brief chemical encyclopedia. V.1, M .: Soviet Encyclopedia, 1961.

 9. Properties of inorganic compounds. Handbook, L .: Chemistry, 1983.

 10. Perry J. Chemical Engineering Handbook. V.2, L .: Chemistry, 1969.

 11. Chernobyl II, Bondar A.G. and other Machines and apparatus for chemical production. M .: Mashgiz, 1961.

  12. Brief chemical encyclopedia, V.5, M .: Soviet encyclopedia, 1967.

Claims (4)

 1. A device for the continuous processing of sea water with the release of demineralized water, hydrogen, oxygen, metals and other compounds, containing a series-connected ion separator for separating sea water by a magnetic field into demineralized water, anolyte and catholyte, a separator-neutralizer for separating the hydration shell from anions and cations and neutralization of electric charges on them, and a hydrogen generator to produce hydrogen by the interaction of molten lithium and water, forming the first technological line ju, and serially connected to a second separator-converter, a reactor-mixer and a hydrogen generator operating on demineralized water and alkaline melt, forming a second production line.  2. An ion separator for separating sea water into demineralized water, catholyte and anolyte containing a pipe placed in a magnetic field, characterized in that the device further comprises a section for preliminary magnetization of water by a circular magnetic field created by an electromagnet coil, and equipped with a device for tangential water input and the separation section of pre-magnetized water by means of a magnetic field with a magnetic flux perpendicular to the direction of water movement is made in the form of a central Nogo pipeline, through which slit the diameter of the two smaller diameter conduit connected to the output of the anolyte and catholyte.  3. A separator-neutralizer designed to separate the hydration shell from anions and cations and neutralize electric charges on them, comprising a device for supplying high voltage direct current to conical grids, a separator equipped with nozzles for introducing vaporous catholyte and anolyte, two conical grids carrying positive and negative charges, respectively, two dampers of the anolyte and catholyte vapor velocity, and two guide cylinders for explosives but not containing the hydrate shell of anions and cations in the catalyst, and the catalyst comprising a low voltage DC generator and an external oscillator circuit that includes a metallic ball contact and the contact of the molten lithium or sodium.  4. A hydrogen generator containing a reaction zone and a heat exchanger, characterized in that the generator contains a heat-insulating casing in which a reaction zone for the interaction of molten lithium and water is provided with a cooling system for cooling the reaction mixture with a coolant with the release of an aqueous solution of lithium hydroxide and hydrogen from it, nozzles for the removal of hydrogen and an aqueous solution of lithium hydroxide, in addition, the generator has nozzles for introducing anolyte and catholyte into the annulus of the reaction zone and nozzles in the output of vaporous catholyte and anolyte, equipped with electric heaters.

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