WO2024205452A1 - Plasma arc electrolytic centrifugal conversion method and device - Google Patents

Abstract

The invention relates to metallurgy and can be used for processing ores, hydrocarbon material and waste, with the subsequent separation, reduction and refining of any metals and non-metals to obtain hydrocarbons and chemical products for the generation of electrical, chemical and thermal energy. A process for generating electrical energy and heat is combined with a process for processing a substance and delivering a substance to an energy consumer in the form of a liquid energy carrier, thus forming a closed system for processing a substance and producing energy. The reduction and dissociation of metals and non-metals is accelerated by the fact of carrying out reaction, separation, synthesis and energy generation simultaneously. The process chains taking place in all of the production sections contained in the production loop and the consumption loop are interlinked. The claimed device is used as a waste processing plant where an arrangement for processing industrial and domestic waste operates in the same way as an arrangement for processing common ores and hydrocarbons. The process of producing energy combined with the production of energy carriers, oil and gas refining and a metallurgical process makes it possible, by virtue of the bombardment of chemical substances with plasma particles, to reduce energy consumption by comparison with the amount of energy required to carry out such processes separately.

Description

METHOD AND DEVICE FOR PLASMA-ARC ELECTROLYTIC CENTRIFUGAL CONVERSION

The proposed invention relates to the field of energy-chemical-metallurgical production and can be used for processing ore, hydrocarbon raw materials and waste with subsequent separation, recovery and refining of any metals and non-metals to obtain hydrocarbons and chemical products, for generating electricity, chemical and thermal energy, as well as for the production, transportation and storage of energy carriers.

[1] The first analogue of the proposed invention is a method patented in the USA (patent US4363832). This method allows for the creation of a metal tube with an oxide ceramic coating on the inner surface in a form (crucible) from the products of the self-propagating high-temperature synthesis reaction. This method uses a centrifugal force field with an acceleration of approximately 69g.

[2] As a second analogue of the proposed invention, a method of ore-thermal smelting of slags and reduction of metals is adopted. To separate the oxides of titanium, iron and other impurity elements included in the composition of titanium concentrates, reducing ore-thermal electric smelting of these concentrates is used on a large industrial scale, as a result of which the majority of iron oxides are reduced to metal, and titanium oxides and some impurity elements pass into slag.

[3] As a third analogue of the proposed invention, a method for carbothermic reduction of metals from oxide raw materials, using a melting plasma torch, is adopted. This is a reverse polarity plasma torch, where the electric arc is closed on the melt of the metal reduced from the oxide raw materials.

[4] The fourth analogue is the reverse polarity melting method developed at the E. O. Paton Electric Welding Institute. The peculiarity of the method is that two power sources are used. One power source is for continuously maintaining the pilot arc burning between the internal electrode, which is the cathode, and the plasma torch nozzle, which is the anode, the other source is used to power the main arc burning between the anode and the metal being melted, which is the cathode. Using the nozzle as the anode for the main arc eliminates the influence of the reverse polarity current of the main arc on the internal cathode, thereby This ensures its good durability, and its small diameter ensures stable burning of the pilot arc at currents of 2–5 A.

At low plasma-forming gas consumption (0.2–0.8 l/min), the anode spot of the main arc is located inside the nozzle channel, and compression of the arc column in its open section and near the cathode is ensured by a protective gas, just as during melting at direct polarity.

[5] The Cambridge process of direct electrochemical reduction of TiO2 in molten CaCh is adopted as the fifth analogue of the invention. The titanium reduction reaction is carried out at 950°C in a closed electrolyzer filled with inert gas on a cathode made of solid TiO2, while the oxidation of oxygen anions occurs on a graphite anode with the release of CO2.

[6] The sixth analogue of the invention is the production of hydrogen, carried out by the iron-steam method: Fe2CO3+CO3Fe2O3+CO2, Fe2O4+H2 "-" Fe2O3+H2O, due to a multi-stage transition, where the efficiency reaches 63%. [7] The iron-steam method has been used for many decades, where hydrogen is reduced by iron and its oxide:

_H2O + Fe = FeO + _H2 + 8.9 kcal (1)

H ₂ O + 3FeO = Fe ₃ O ₄ + H ₂ + 16.7 kcal (2)

At a temperature of 700 °C the process proceeds at a sufficient rate, reaching a hydrogen content of 63% in the first reaction and 41% in the second reaction. The steam is not fully utilized, and the sulfur compounds of the ore with the steam form hydrogen sulfide and other compounds. Iron sulfide, reacting with steam and hydrogen, forms hydrogen containing CO2, CO, CH and H2S.

[8] The seventh analogue of the invention is the Australian process for producing hydrogen, using iron ore through which natural gas is passed at a temperature of 600-1000°C, where the particle size of the ore is in the range of 0.1 h-10 mm, producing 2000 ^m3 of hydrogen, which requires 27 kg of iron ore. The ore, acting as a catalyst, is modified and becomes a more suitable product for recovery. A disadvantage of the Australian process is the need to remove carbon to restore the reactivity of the ore catalyst.

[9] The eighth analogue of the invention is liquid metal pyrolysis for hydrogen production, which was proposed by D. Tyrer in 1931. This is the pyrolysis of methane in molten iron, but the proposal did not reach practical testing. The latest work in this area describes the course of pyrolysis with a gas flow rate of 50 ml/min, where the hydrogen yield is 78%. To obtain hydrogen by this method, liquid lead or tin with the participation of solid particles (SiC; AhO; NiMo/AhOs) is used. Pyrolysis proceeds successfully in liquid magnesium at 700 °C, where the methane conversion reaches 30%. [10] At the University of California, an alloy of 27% Ni and 73% Bi was most successfully used as a catalyst for liquid metal pyrolysis, where nickel acts as a catalyst and bismuth as a solvent. The resulting catalyst is 50 times more effective than molten lead and 5 times more effective than platinum and nickel. [11] Liquid metal pyrolysis is possible with the participation of liquid tin or lead, where silicon carbide is present, allowing the process to be carried out until the complete decomposition of methane at a temperature of 600 to 900 °C.

[12] The ninth analogue of the invention is the autothermal conversion of synthesis gas production, which combines several reactions in one reactor: steam conversion of _CH4 + _H2O CO -I- _3H2AN = +206 kJ/mol; partial oxidation by oxygen _CH4 + ^/2 _O2 <-> CO + _2H2AN = -35.6 kJ/mol; carbon dioxide conversion of _CH4 + _CO2 ■ 2CO + _2H2AN = +247 kJ/mol.

[13] The tenth analogue of the invention is the steam-carbon dioxide conversion for the production of methanol, where a mixture of gases CH4, H2O, CO2 in a ratio of 1:3.3:0.24 is involved, turning into synthesis gas on a nickel catalyst at 860°.

[14] Hydrogen thermal power plants (HTPP) are adopted as the eleventh analogue of the invention; hydrogen combustion is used to implement the process of generating electricity.

[15] As the twelfth analogue of the invention, fuel cells are adopted that can generate up to 20 MW or more of electricity using hydrogen as fuel.

[6] As the thirteenth analogue of the invention, the steam-carbon conversion of hydrogen production is adopted, where the reaction of water vapor and carbon C + H2O = CO + H2 at 1000 °C takes place, producing water gas, which is then fed to the production of methanol.

[16] As the fourteenth analogue of the invention, a method for obtaining various compounds of a substance by a flow of elementary particles is adopted, which include, for example, radiation-thermal cracking of heavy oils, the method of electron-beam processing of high-molecular compounds, the “Petrobeam” method, radiation-wave cracking (RWC), the method of ultra-high-frequency (UHF) irradiation of a substance, including the Ranque vortex effect. [17] The irradiation method also includes the process obtaining methanol from natural gas under the action of laser radiation, where photochemical processes operate. The stage of methane activation with oxygen followed by dissociation of the carbon-hydrogen bond is 230 kJ / mol, and the conversion of methane with a hydroxyl radical is 23 kJ / mol, which is an order of magnitude less and occurs under the action of laser irradiation. Processing of hydrocarbon raw materials irradiated with a flow of elementary particles allows an order of magnitude reduction in energy costs compared to thermal methods. Modern physicochemical methods of processing heavy oil confirm the effectiveness of using radiation wave radiation to separate interatomic and molecular bonds of a substance. A directed flow of elementary particles causes ionization of any medium, including gases, liquids or minerals, which leads to a change in the structure and properties of the substance. In the molecules of heated raw materials, the bonds are broken due to resonant vibrations, where lightweight molecules are formed at the output. The use of irradiation of matter with the Ranque vortex effect allows energy costs to be reduced by approximately an order of magnitude, compared to thermal technologies.

[18] The Boudoir reaction is accepted as the fifteenth analogue, which allows carbon dioxide and graphite to be produced from carbon monoxide at a given temperature according to the reaction 2CO -> CO2 + C. This reaction is exothermic at all temperatures and allows the amount of gas phase of a substance to be reduced in various production processes.

[19] The sixteenth analog is heat pumps, which are used in thermal power plant circuits, where water is considered the best coolant. A high-temperature heat pump based on the ANR “RASO” project was created on water. [20] Heat pumps are used to transfer thermal energy from a less heated environment to a more heated one, which are increasingly used in thermal power plants.

[21], [22] The seventeenth analog is the closed-loop Stirling engine, which is used to perform work, for example, as a pump for pumping a substance or for generating electrical energy. The operation of the Stirling engine is provided by heat pipes, which can be used with any source of thermal energy. Due to this, the system with the Stirling engine becomes multi-fuel. The principle of operation of heat pipes is the transfer of heat, located in a closed space, by a substance with a phase transition.

[17] As an eighteenth analog, a technology for producing methanol from natural gas under the influence of laser radiation is presented. The technology is based on photochemical processes are used that allow energy costs to be reduced by an order of magnitude during the activation of methane by molecular oxygen, due to the hydroxyl radical.

[23] The nineteenth analog is a magnesium production process where the furnace consists of a reactor, an intermediate chamber, and a condensation chamber, and heating is provided by resistance elements. The charge is loaded into the reactor through a sluice gate, where magnesium reduction occurs in a hydrogen atmosphere at 1600 °C and a pressure of 3 kPa. The residue from the reduction is discharged from the reactor through a grate and a sluice gate. Magnesium vapor enters the intermediate condenser, cooling to 900 °C for filtration through a falling layer of powder from the charge, on which impurities condense. Next, magnesium vapor enters the condensation chamber, where at 650 °C it condenses into liquid on the cold inner walls of pipes connected to a vacuum system. The pipes are alternately heated to melt the deposited magnesium crystals, which flow into a crucible placed in an electric furnace. The total energy consumption for the production of magnesium using this method, taking into account the production of ferrosilicon, reaches 18 kW h/kg.

[24] The twentieth analogue adopted is the method of electrothermal reduction of aluminum, which is more promising than electrolysis, since it consumes two and a half times less electricity. [25] The process of electrolytic reduction of aluminum consumes 15 kW h (57.6 MJ) of electricity per kilogram of aluminum produced, while with electrothermal reduction the costs are 6 kW h (22.5 MJ). [26] An effective option is the process of aluminum reduction in plasma with natural gas, where with carbothermic reduction, the yield of aluminum approaches 100%.

[27] A similar technical solution, the prototype of which is the method according to Russian patent No. 2524036, where the liquid phase of the metal, entering the crucible, is heated in an oxidizing or reducing atmosphere, while chemical reactions occur in the melt and the reaction products are separated by density, leaving the reaction zone in different directions under the action of centrifugal and gravitational forces, and the base metal crystallizes into an ingot on the inside of the crucible. Light impurities are forced out to the surface of the melt. To remove them, the ingot is turned over and poured out together with the melt, heavy impurities go to the periphery of the ingot, from which they are subsequently removed by various methods.

The proposed invention solves the problems of recovery, refining and separation of chemical substances from ore, with the participation of hydrocarbons and related compounds, where using plasma-chemical reactions, electrolysis and cracking, allowing, with lower energy costs, to destroy the atomic-molecular bonds of these compounds and synthesize liquid fuels at the output, form a solid residue in the form of a disk, where metals and non-metals are separated by density throughout its volume, and also produce energy at power plants due to the hydrogen and oxygen released in the process, where the resulting heat is returned to production, and the produced substances and energy carrier go to the sales market and to the consumer at ambient temperature, while the necessary cooling of the condenser during energy production is ensured by a flow of water that preliminarily gives off excess heat to the reagents of the batch and a flow of carbon dioxide returned from the energy consumption circuit at ambient temperature, where carbon dioxide is then used in the production circuit for reprocessing. The process of processing the substance and generating energy takes place in a closed volume of the production circuit without emissions of thermal energy into the environment due to the transportation of the substance, where the manufactured industrial products remain inside the circuit and subsequently, before going beyond it, serve as accumulators of thermal energy. The proposed method solves the problem of significant reduction of losses during energy production and energy consumption, during processing of ore and hydrocarbons by combining these production areas into a single system and by supplementing thermocatalytic reactions with electrolysis and photochemical reactions occurring under the action of irradiation of the substance with electrons, ions, photons and other particles. The processes of catalytic separation and synthesis use ore as a constantly renewable catalyst, and the metallurgical processes occurring in parallel use hydrocarbons as reducing agents for metals from compounds of this ore. The combined process of energy production with the production of energy carriers, gas and oil refining and the metallurgy process allows, due to irradiation of the substance with plasma particles, to reduce energy consumption by at least an order of magnitude, compared to the energy required to carry out these processes separately.

In order to conserve the maximum amount of energy and prevent its loss to the environment, the process of energy production, processing of ore with hydrocarbons, production of energy carrier, as well as the process of energy consumption, are carried out simultaneously and are connected to each other. For this, all processes are contained in the space of two or more circuits and are connected by pipelines for the supply of energy carrier and the return of refrigerant. For processing the substance, a production circuit is used, which is connected by pipelines transmitting energy carrier and refrigerant, with the consumption circuit, where the energy carrier is consumed. Within the production circuit there are sections for energy production, crushing, preparation of substances, metallurgy, separation, and methanol synthesis, which are combined into a single system.

In the power generation section, two or more power plants are combined into a single system, allowing the generation of electricity from external sources and allowing operation on hydrogen produced within the circuit in order to achieve the highest possible stability in the process, energy production and material processing.

The proposed invention solves the problem of increasing the energy efficiency of equipment operation and expanding its technical capabilities for the separation, recovery and synthesis of chemical substances, by reducing energy costs, shortening the production cycle, combining various processes, reducing the dimensions of the equipment, increasing the speed and environmental friendliness of production.

The set objectives are achieved by the fact that the plasma-arc electrolytic centrifugal converting (PAECC) method for the production of metals, non-metals and energy carriers consists in the fact that the reagents heated in the crucible, consisting of chemical compounds of metals of the ore, hydrocarbons and water, representing the charge, forming a falling stream and moving along the shaft, which is then melted due to the electric arc burning on the electrodes, forming a plasma, fed from the power plant, electromagnetic fields, irradiation with flows of elementary particles, electrolysis, dissociation and centrifugal forces of rotation under the action of a crucible turbine, a rectification column, condensation rods, sluice gates, as well as electromagnetic fields of the solenoid, are reduced in a certain volume to metals and slags, forming a board-shaped ingot, with the formation of chemical compounds in the form of gases, which are synthesized in the apparatus into hydrocarbon products, characterized in that, that before melting, large-sized ores and solid hydrocarbons are crushed in water to small particles and mixed, forming a charge, and liquid and gaseous hydrocarbons in stoichiometric composition are added to it before melting, entering the plasma combustion zone, where a melt bath is formed, in which chemical reactions of reduction occur due to carbon, hydrogen and carbon monoxide, which are enhanced by electrolysis, and the resulting gas compounds form a synthesis gas, from which methanol is synthesized in the apparatus, after the reduction of metals, the melt bath in a plasma flow is discharged in a continuous stream into a rotating crucible turbine, where the produced reagents, under the action of rotation in a high-gravity field, are separated by density, forming an ingot in the form of a disk, ensuring the separation of chemical substances throughout its volume, dividing them by density, where the reduced metal is displaced to the peripheral surface of the disk, and the slag is displaced to the center of rotation. The reagents of the charge enter the arc and plasma combustion zone through a horizontal shaft, simultaneously being replenished with the reaction products of the preceding melting, as well as gaseous and liquid hydrocarbons, where during movement they dissociate into soot carbon and hydrogen, which reacts with metal oxides and reduces them with the formation of carbon monoxide, which also produces reduction to carbon dioxide, and entering the melting zone, at the plasma combustion temperature, where the temperature exceeds two thousand degrees Celsius, the reduction of the metal from the compounds is carried out only due to carbon with the formation of carbon monoxide, where hydrogen creates a protective environment preventing the reverse reaction of oxidation of the reduced metal, forming, together with carbon monoxide, synthesis gas from which, at the outlet, the resulting gas mixture is pumped out of the melting zone and sent to the synthesis production section in the methanol apparatus, where the plasma, forming a melt from the reagents, initially burns above the mirror of the melt bath, and after the formation of a given volume of melt, the plasma with the electrode acting as an anode is immersed in the melt, allowing the process of electrolysis with a chemical reducing agent for metals and dissociation of compounds to be carried out, and then the drained melt is constantly irradiated with elementary particles of plasma, allowing the interatomic-molecular bonds of the substance to be destroyed with the least energy expenditure, the rupture of which is enhanced by the rotation of the melt in the turbine and the effect of a high-gravity field on its substance, where the effect of rupture of interatomic-molecular bonds is enhanced by the compression of the melt jet and plasma flow, the electromagnetic field of the solenoid, while an increase in the intensity of the electromagnetic field leads to compression of the plasma flow and an increase in temperature, which increases the speed of movement of atoms and molecules inside the melt and promotes more intense rupture of bonds, which transfers the substance to a supercritical high-temperature state, preventing it from evaporating, due to compression by the electromagnetic field, which is maintained in a supercritical high-temperature state and then, under the action of rotation, begins to expand and lose temperature under the action of the kinetic energy of rotation, and the chemical elements, due to different densities, begin to separate from each other, creating the effect of high-speed separation, where the denser substance is squeezed out to the periphery of the ingot, and the least dense substance to the center, while the process of zone purification of the melt occurs, where heavy metals crystallize into a skull on the outer diameter, and light slags are displaced into the melt on the inner diameter of the ingot, into the zone of heating of the melt by plasma. Transfer of the substance of the melt stream to the high-temperature state is carried out for a short period of time in the range of 0.1-НЗ.01 sec. to break the bonds, under the influence of the photoelectric effect created by the flow of elementary particles in the field of high gravity, which is similar to the Ranque effect, allowing to obtain simpler substances in composition from complex substances, with significantly lower energy costs, while the bonds are broken at some distance from the plasma torch electrodes, not allowing to affect the substance of the electrodes by the action of ultra-high temperatures, and to obtain ultra-high temperatures in the falling melt stream, which under normal conditions convert any substance into steam, possibly, in the zone around the stream, to increase the compression of the stream with an additional separate electromagnetic field, as well as to affect it with laser, electron beam, radioactive and ultra-high-frequency radiation. The process of metal reduction in the melt bath and obtaining non-metals is accelerated by dissociation of substances at elevated temperatures, as well as under the influence of a vacuum, where the reducing agents for metal oxides are solid, liquid and gaseous hydrocarbons mixed into the ore in a stoichiometric composition, which, under the influence of plasma, dissociate into reagents forming synthesis gas, from which methanol is synthesized in the apparatus, where the substance of minerals is separated in the crucible due to reduction, and then in the crucible turbine due to the gravitational field of high gravity, forming metals and non-metals including compounds consisting of oxides, carbides, fluorides or nitrides, where the process is arranged in such a way that from the melt in one direction there is crystallization of pure metal, and in the other direction there is displacement of non-metallic impurities, including gaseous ones, thereby preventing the reverse reaction of their interaction, and during the reduction and dissociation of metals and non-metals from a mixture of ore and hydrocarbons, The reducing agents for metals are hydrogen, carbon and carbon monoxide formed as a result of the dissociation of hydrocarbons, where ores serve as catalysts for the conversion of hydrocarbons, accelerating reactions and reducing energy costs, while reverse reactions of oxidation of metals are prevented by the release of reducing agents hydrogen, carbon and carbon monoxide.

The plasma-arc electrolytic centrifugal conversion (PAECC) method for the production of metals, non-metals and energy resources consists of reagents heated in a crucible, consisting of chemical compounds of metals, ores, hydrocarbons and water, representing the charge, forming a falling stream and moving along the shaft, which is then melted by an electric arc burning on electrodes forming plasma fed from a power plant, electromagnetic fields, irradiation with flows of elementary particles, electrolysis, dissociation and centrifugal forces of rotation under the action of a crucible turbine, a rectification column, condensation rods, sluice gates, as well as electromagnetic fields of a solenoid, are reduced in a certain volume to metals and slags, forming a board-shaped ingot, with the formation of chemical compounds in the form of gases, which are synthesized in the apparatus into hydrocarbon products, including use in the production process of thermal power plants generating electricity and heat, as well as energy consumption facilities where the substance is supplied through pipelines and the reaction products are returned, characterized in that the process of generating electricity and heat is combined with the process of processing the substance, supplying the substance to the energy consumer in the form of a liquid energy carrier through a pipeline with the reverse return of part of the substance from the consumer in the form of a refrigerant through a pipeline, forming a closed system for processing the substance and energy, where the restoration and dissociation of metals and non-metals, including methanol synthesis, is accelerated and requires significantly less energy due to the simultaneous reaction, separation, synthesis and energy generation, where a combined power plant is used to produce electrical and thermal energy, including the main units of power plants based on nuclear power plants, VTES and TE assembled into a single complex, where the released hydrogen and oxygen from the chemical-metallurgical process of processing the substance enter, where it is sent for combustion to generate heat and electricity, in turn, the released heat, electricity and water from the power plant enter the plasma-chemical process site and the methanol synthesis site. The process of energy production and consumption, reduction of metals, non-metals, dissociation of complex compounds into simpler compounds is combined with the process of synthesis of chemical products and preparation of the batch into a single process of energy and substance processing, where the intersection of the process chains of all production sections enclosed in the production circuit and all sections enclosed in the consumption circuit occurs, which include all the necessary initial components at ambient temperature and from which reagents and reaction products go beyond the circuit boundary, at ambient temperature, where the heat released from any type of production inside the circuit goes to heating the incoming reagents, and the cold taken in goes to cooling the steam of power plants and production equipment, while from the production circuit to the consumption circuit, the energy carrier in the form of methanol enters through a pipeline, going beyond boundary of the circuit at ambient temperature, and from the consumption circuit the refrigerant returns in the form of gaseous carbon dioxide, moving outside the consumption circuit, at ambient temperature, the refrigerant, entering the production circuit, is used to cool the steam of power plants and methanol leaving the production circuit and then, being heated, the carbon dioxide goes to the formation of plasma, the synthesis of methanol or dissociation to obtain carbon and oxygen, while at the same time, metal is reduced from the incoming reagents, chemical compounds are synthesized, hydrogen is burned on power equipment, that is, the system operates as a single whole, where the processes are controlled by a computer program with the participation of an automated control system. All the released thermal energy due to exothermic reactions, hydrogen combustion and thermonuclear reactions is redistributed within the production circuit for heating the substance, due to heat pipes and heat pumps, where excess heat is converted into mechanical and electrical energy due to Stirling engines, directed to maintaining the arc combustion and the operation of equipment mechanisms, forming a closed production cycle, where as a result, a ring ingot and new chemical compounds are formed at the output in the form of a product, including methanol, sent to the consumption circuit, for energy production, as a result of the conversion of which the coolant is returned back in the form of carbon dioxide, cooling the power equipment and then entering the recycling process, for the synthesis of methanol and the production of carbon and oxygen, allowing to bring the energy costs for the output products close to the theoretical energy costs, the chemical elements included in the energy carrier are included in the circuit with recycling, allowing to more fully process the reagents and separate them into elementary molecules, where carbon is the main reducing agent for metals, and hydrogen and oxygen are the main reagents for combustion in power plants, thus, these chemical elements enter any devices inside the production circuit and the consumption circuit in a circular closed cycle, due to this, the system, using a computer program and an automated control system, can regulate any specified amount of reagents necessary for the course of various reactions that allow the production of an optimal amount of metals, non-metals and energy carriers, simultaneously with the processes of production of metals, non-metals and energy carriers, processes of additional production of carbon and hydrogen associated with iron-steam conversion, dissociation of carbon dioxide in plasma, dissociation of methane inside the ore and in the melt of metals due to liquid metal pyrolysis, which occur during the movement of the ore, from the moment it enters the furnace body until the moment of melting, which allows for the complete decomposition of methane into hydrogen and carbon, where the dissociation reaction is completed by the passage of methane through the plasma, which allows the process to be used for the primary production of hydrogen and carbon in large quantities, the plasma acts as a heater, forms melts from the incoming ore reagents, which serve as effective catalysts for the dissociation of the incoming hydrocarbon reagents, allowing them to be divided into simpler compounds with the lowest energy costs, where hydrogen and carbon are produced at a high rate at the same time, which in turn are reducing agents for metals from the ore, and the plasma also acts as a source of a flow of elementary particles that, by acting on the interatomic molecular bonds of the substance, destroy them with the lowest energy costs. During the reaction, gas flows containing different amounts of CH4; O2; H2O; CO and CO2, which continue to react with each other as they move, where all the zones for carrying out the said reactions are separated, allowing for an autothermal reaction of synthesis gas to be carried out, which is used to synthesize methanol and produce energy, where the batch consisting of ore serves as a catalyst for the division of hydrocarbons for the synthesis of methanol, and the batch containing hydrocarbons, after division into components, serves as reducing agents for the production of metals from ore, where autothermal reactions are carried out during the process, where there is no need to carry out the operation of restoring the catalyst, since the ore is automatically renewed, which significantly simplifies the process, where maintaining an autothermal reaction during the process is carried out due to the possibility of regulating the temperature, pressure and volume of reagents, under the influence of a computer program and an automated control system, redirecting the substance to various production areas inside the circuit, accordingly selecting the melting time of a given volume of the batch, humidity, the degree of dissociation of the substance, the amount of reagents and other parameters, it is possible to achieve a mode in which the maximum amount of metal can be restored with the least energy consumption, non-metal and synthesize the maximum amount of energy carrier, during melting from the charge through the gas phase, all toxic chemical elements are eliminated, captured on cooled filters and separated from the melt of the reduced metal with non-metals, which is then merged and divided into components in the turbine, forming a disk, where all heavy metals, including rare earths and platinum group metals, accumulate in the outer part, and the volatile part of the substance, passing into the gaseous phase, is divided into fractions during condensation, due to different boiling point, including magnesium, zinc, arsenic, which together with the synthesis gas form a flow passing through a filter of falling ore particles on which solid particles settle, including soot carbon, then the purified flow enters the rectification columns, where condensation rods are installed in each column, on which the substance with a higher boiling point condenses, condensation rods, of which two or more, are alternately heated, allowing the substance to be drained into separate crucibles, from which the condensate, consisting of various substances, is removed through separators, entering the Market, and the slags are again returned to the repeated melting process, while the purified flow of synthesis gas and low-boiling impurities enters the separator through a pipeline, is separated into the main gases, from where the synthesis gas goes to the production of energy, the separated impurities enter the Market. As a result of the work, a ring ingot is produced containing pure metals, without impurities including carbon, and after the ingot crystallizes and the turbine stops rotating, the ingot is extracted through sluice gates, then the separation of pure metal from heavy and light impurities frozen into its circuit is carried out by electrolysis, mechanical cutting, crushing or chemical etching, where an additional reduction in energy costs in the production of metals and non-metals, including energy carriers, is achieved through the use of hydrogen and oxygen extracted during the separation of matter, burned in power plants, producing additional electricity and heat sent back in the process, while a significant reduction in energy costs is achieved by using all the heat released in power plants to heat the reagents supplied to metallurgical and chemical production, and an additional reduction in energy costs is achieved by transferring the energy carrier to the place of consumption at ambient temperature, from where carbon dioxide is returned, also at ambient temperature, which at the entrance to the production circuit acts as a coolant, cooling the power plants and then, in a heated state, it is fed to the synthesis of the energy carrier or passes through the plasma, forming reagents, which are also fed to the synthesis of the energy carrier or the production of carbon and oxygen, while power plants do not use the combustion of organic matter in the form of complex compounds, which has a low yield of thermal energy and a high yield of toxic compounds, where the most common power plant is a combined complex consisting of equipment from a classic nuclear power plant, a high-temperature thermal power plant and a fuel cell, where only hydrogen is used as fuel for combustion, while the nuclear thermonuclear reactor operates at a constant power during the process, which is in range from 1 to 50% of the total capacity of the power plant, and additional energy capacity, smoothing out pulsations in energy consumption, inevitable in the results of the process, is produced by burning hydrogen fuel at VTES and TE, obtained from processed raw materials, thus, a scheme for processing heat and electricity generated by the power plant into metals, non-metals and energy carriers is formed, where all the generated energy is converted into a substance representing metals, non-metals and energy carriers that can be stored indefinitely, allowing all types of ore and hydrocarbon raw materials to be processed into finished, high-quality products, where the energy carrier in the form of methanol or synthetic oil accumulates at the production facility and, if necessary, is transported to the consumer through pipelines, where hydrogen is extracted from it, with the help of which the necessary energy is produced and carbon dioxide is transported back, that is, when using this scheme, almost the entire volume of ore and hydrocarbon raw materials is converted into metals, non-metals and an energy carrier, which are sent to the consumer and to the Market, with higher profits. Hydrocarbons are processed into hydrogen, where when it is burned, the greatest amount of energy is produced, as well as carbon, which enters the market as a useful material, while from the reagents of the batch, consisting of ore, water and hydrocarbons, an energy carrier is synthesized in the form of liquid fuel, which has a three times higher cost on the Market than gaseous fuel, which requires significantly lower costs for storage and transportation to the consumer, and the supply of thermal energy and its conversion is carried out inside the production circuit, where reagents are fed to the input at ambient temperature, and products are supplied to the output, also having a temperature equal to the ambient temperature, increasing the orderliness of the system with a decrease in entropy, making the PDECC process energy-efficient, where only hydrogen is burned at power plants producing electricity inside the production circuit, due to its highest energy efficiency, and as a result of combustion, water is formed, which as a valuable raw material enters the Market, and part of the formed water is used as a coolant and raw material for the production of energy carriers, while the carbon that is currently burned in classical power plants is used as a reducing agent for reagents, a finished product entering the Market and as a raw material for the production of plasmatron electrodes, which are automatically changed during the melting process, for this purpose a carbon processor is used, where the Boudoir reaction 2CO CO2 + C takes place, from where carbon, in the form of scaly, threadlike or lamellar graphite enters the accumulator, and due to the plasma, a given volume of oxygen and carbon monoxide is extracted from carbon dioxide, where it dissociates according to the reaction CO2 -> CO + 0.5O2, then the resulting oxygen is used for the autothermal reaction of synthesis gas formation, combustion or other necessary reactions.

The plasma-arc electrolytic centrifugal converting device (PAECC) contains a consumable plasma torch consisting of a graphite cathode and an anode, a power source, a rectifier, batch reagents including compounds of ore, hydrocarbons and water, reducing agents in the form of solid particles, liquids or gases, a crucible, a crucible turbine, movement lines, an electrode holder, a vacuum pump, a batch crusher, a vacuum chamber, horizontal and vertical shafts, a screw, a piston, a branch pipe, a needle, a filter, an accumulator, a rod, a drive, turbine blades, an electrode, a solenoid, an inductor, an electromagnetic field, plasma, a production circuit, a consumption circuit, a condenser, pipelines, contacts, a nozzle, a crucible turbine, a melt bath, compressors, pipelines, power plants including nuclear power plants (NPP), hydrogen thermal power plants (HTPP) and fuel cells (TE), heat pumps (TH), heat pipes (HT) and Stirling engines (SE), compressor, support plate, valve, synthesis apparatus producing chemical products including methanol, characterized in that for melting the reagents a mixture of ore particles and hydrocarbons is created in the form of a charge, which is fed under the torch of the plasma torch through a horizontal shaft, under the end of the central cathode and tubular anode, which are the electrodes of the plasma torch, where an arc is ignited, burning on the inner surface of the electrodes with its rotation, inside which plasma is formed, creating a molten bath to which the anode is closed when immersed, and the melt acts as a cathode, producing electrolysis of the melt, where the negative pole from the rectifier and the power source is connected to the molten bath, and the molten bath after the reduction of metals due to the opening of the valve merges in the form of a jet into a rotating crucible turbine, which is spun by a stream of methane gas, where the falling the melt stream is irradiated by a stream of elementary plasma particles, transferring the melt to a supercritical high-temperature state due to the compression of the stream by the electromagnetic field of the solenoid, then the superheated melt expands and is separated due to the rotation of the crucible turbine, where heavy chemical elements move to the periphery, and light chemical elements to the center of rotation, forming a ring-shaped disc ingot, after melting the consumable electrode, the ingot and slag are removed from the disassemblable crucible turbine and the ingot is fed to electrolysis. Bottom the support plate, where the melt bath is formed, is made with a bottom opening in the form of a tapering cone and is closed by a valve for releasing the melt and re-accumulating the freed space with the batch, for re-collecting the melt bath, in which an additional increase in the plasma temperature is produced due to the electromagnetic field of the solenoids, which covers the internal space of the melt bath, allowing for more intensive reduction of metals and dissociation of compounds, affecting the course of chemical reactions and the amount of the reduced, dissociated and synthesized substance, which participates in the production of energy and, in the form of the energy carrier methanol, is sent through a pipeline for processing into the consumption circuit for the production of energy away from the production circuit, from where it is returned from the consumption circuit through a pipeline in the form of a coolant - carbon dioxide, for cooling the production products and re-involving them in processing, and around the released stream of melt, located between the support plate and the crucible turbine, a separate solenoid is placed, creating a more powerful electromagnetic field of influence on the plasma and the substance, and lasers, electron beam guns or magnetrons are placed, additionally irradiating the substance of the melt stream, the crucible turbine is driven by a methane gas stream entering the turbine blades fixed on the crucible turbine, allowing to abandon the use of a drive and to provide cooling of the crucible turbine and the melt and allowing to simultaneously dissociate methane into carbon and hydrogen captured by a vacuum pump, where carbon settles on the falling particles in the vertical shaft and is directed as a reducing agent for the reduction of metals in the melt of the charge, and hydrogen is directed to the synthesis of methanol, forming with carbon monoxide, which in turn is formed by the fusion of carbon and oxygen due to the reduction of metal oxides, forming synthesis gas, while the melting process is carried out in a vacuum chamber, which is pumped out through a branch pipe by a vacuum pump, accelerating the process of metal reduction and the dissociation of substances, where volatile particles of metal and gaseous reaction products at the exit from pipe are captured by a filter from the falling particles of the charge and then enter the rectification columns, settling on the heated rods and settling in separate crucibles that act as a trap-refrigerator for the condensation and crystallization of metal vapors, including magnesium, zinc, manganese, sulfur, carbon, phosphorus and other, more volatile compounds, enter the separator, which separates the substances into various chemical elements. A gaseous hydrocarbon reducing agent is fed into the arc combustion zone to form plasma, including methane, ethane, propane or pyrolysis gas, which, when dissociated in the electric arc into soot carbon and hydrogen reduce metal oxides, and carbon dioxide is supplied as a plasma-forming gas, which dissociates into carbon monoxide and oxygen, while carbon monoxide reduces metals, and oxygen ensures the flow of automatic reactions during interaction with methane, steam and carbon dioxide to form synthesis gas, which is sent to a specialized device where methanol is synthesized, where the heat generated by the synthesis of the exothermic reaction, plasma and combustion of hydrogen is directed to heating the reagents and producing steam, to generate electricity, the operation of compressors and mechanisms, including the rotation of the charge crusher, while the process ends with the formation of a disk ingot. The PDECC scheme is combined into a single system of energy production, smelting, reduction of metals and non-metals sections, limited within the boundaries of the production circuit, which in turn, through pipelines with an energy carrier and a coolant, is connected to the consumption circuit, where the energy carrier - methanol is converted into hydrogen from which energy is produced and carbon dioxide, which is returned to the production circuit for cooling the reaction products and steam, then heated, goes for reprocessing, including the formation of methanol, carbon and oxygen, forming a single structure and allowing for the simultaneous production from the initial ore and hydrocarbon reagents, gaseous reaction products synthesized into methanol and a solid residue in the form of a disk ingot with the simultaneous production of superheated steam used to rotate a steam turbine, a generator producing electricity to maintain the combustion of an electric arc of plasma, heating reagents, driving mechanisms and compressors, in order to reduce the cost of production of metals and non-metals, including energy carriers and coolants, due to creation in this scheme of a closed-loop energy cycle in the production circuit combined with the consumption circuit, while using nuclear power plants or renewable energy power plants as a starting source of electricity, where the process of producing chemicals becomes the most environmentally friendly and less energy-consuming. The device is used as a waste processing plant, where waste crosses the line of the production circuit, at ambient temperature, and inside the circuit, water is cooled, which goes to cool the steam in the condenser, while industrial waste, which has a similar composition to industrial ore, is supplied to the tank with water along one line, being minerals that mainly contain oxygen in their composition and which, when processed, will further serve as a constituent element in the synthesized methanol and water, and along the other line into the tank with water household waste is received, which mainly contain hydrocarbons, carbon and metals, where carbon is mainly contained in paper, wood, cardboard, etc., and hydrocarbons are contained in plastic, which, when processed, will also serve as constituent elements in the synthesized methanol and water, where further the working scheme with the processing of industrial and household waste works similarly to the scheme, processing of ordinary ore and hydrocarbons, where the waste also represents a charge and, mixing in a crusher, enters a vertical and horizontal shaft, and to move the waste along the horizontal shaft, a screw mechanism or a mechanism such as a piston pushing the substance is used, when mixing the waste, fossil hydrocarbons are added to the resulting charge, entering the horizontal shaft through a pipeline and mixed into the charge with a screw, liquid hydrocarbons include oil, fuel oil or heavy waste from oil refining, and solid hydrocarbons are fed into the charge in the form of coal, combustible, shale, peat, oil sands, along the line into a bath of water, where industrial waste is loaded and then fed to the melting zone at once through several shafts, of which there may be two or more, where when feeding waste through several shafts, a more uniform alignment of the chemical composition of the charge occurs, where it is produced in the melting zone due to the receipt of waste with different chemical composition in each shaft, and the diameter of the crusher and shaft is selected to be larger in area, relative to the storage of the vehicle that delivers household waste for processing, after melting and draining a portion of the melt into the turbine, an ingot is formed, which contains reduced metals and remelted metals found in household waste, for example, copper, iron, aluminum, tin, etc., while copper will be concentrated on the outer contour of the ingot, as the densest metal, which contains all the accompanying precious metals, and then with a decrease in density all other metals and non-metals and then the lightest solids impurities such as silicon oxide, silicon and carbon, which is cooled by steam through a nozzle, which produces water gas, which is a raw material for the production of methanol, and after the ingot is extracted, further separation of the resulting substances is carried out by known industrial methods, which include electrolysis, crushing, separation, melting and other methods, while the processing of household and industrial waste is no different from the processing of ordinary ore with the addition of coal, peat, shale, oil sands, etc. By analogy with conventional batch, it can process floating garbage in the oceans, which is household waste and which will be collected without its separation, sent to the crusher for mixing with any soil containing metal oxides, while to create a working batch, fossil ore located next to the garbage will be added to the household waste as a source of oxygen, as this ore, sand, clay, pebbles and similar compounds are mined from the seabed, which are mixed into household waste, then fed into the mine under the action of pressing mechanisms for processing in the melting chamber, where as a result of processing metals, non-metals, methanol and water will be obtained, and during the operation of the floating factory, floating garbage islands will be considered as floating mines for the extraction of minerals. The block diagram of the device operation combines the industrial circuit with the consumption circuit into a single system connected to each other by pipelines transmitting energy carriers and refrigerants, where thermal energy is consumed outside the industrial circuit and the consumption circuit depending on its thermal conductivity, and inside the industrial circuit, at the closest possible distance from each other, sections of various industries are located, the boundaries of which intersect, since they use common nodes and are combined for the reuse of each other's substance and energy, where primary and secondary heat and electricity are produced, energy carrier, methanol is synthesized, the batch is prepared, reduced and smelted, while the input of the original substance into the circuit is carried out at ambient temperature, while water flows, third-party power lines and air do not enter the circuit, since for the production of water, energy and air, all components are contained in the original substance, which allows the system to operate under water or in outer space, from where the substance is released at ambient temperature in the form of finished products for the Market, namely metals, non-metals, including energy carriers and water, wherein the energy carrier is transferred through a pipeline, and the coolant is returned through another pipeline at ambient temperature, where all processes carried out within the boundaries of the circuit do not incur heat losses due to the transfer of energy to the environment, except for heat losses lost through the boundary of the circuit, and when maintaining the temperature inside the circuit equal to the ambient temperature, these losses are eliminated, in addition, heat pumps and heat pipes are used to eliminate heat losses, collecting energy from the outer surface of the circuits and directing the resulting heat to heat the reagents or to the Stirling engine, which allows for the additional generation of mechanical energy, which will be used to move the substance inside the circuits, generate electricity or increase or decrease the temperature at a given point in space inside the system, allowing for the additional reduce energy losses and manufacture products with energy consumption close to the theoretical energy consumption. Around or inside the production circuit and the consumption circuit, it is possible to place sections of various production, including mechanical engineering, metallurgy, chemistry, etc. production, where the necessary energy in the form of heat or electricity, as well as water and carbon dioxide are generated in the circuits and can be used for the needs of this production, for example, carbon dioxide can be consumed in a certain volume by the food industry, and the use of the consumption circuit is possible, by analogy with a classic thermal power plant, where the generated electric energy is supplied to the outside through terminals, and heat is transferred outside the circuit through a heat pipeline for heating the premises, where the production circuit can be used for these purposes, while the contact outputs and heat pipelines are located within a certain radius to which it is possible to transfer electric energy and heat without significant losses. The device is used near cities as thermal power plants, power plants and waste processing plants that do not produce emissions, therefore, their placement can be in the center, around which a city or industrial zone can be built, which will place metallurgical, chemical and machine-building plants around the circumference, using the substance and energy produced inside the production circuit, which solves the problem of reducing energy costs in the production of metals, non-metals and energy carriers, due to the placement of power plants generating electricity inside the production circuit, together with metallurgical, chemical and other installations, due to the fact that power plants spend all the generated electricity and heat on the production of the product, allowing it to be produced an order of magnitude more than according to the classical production scheme, this allows, approximately, ten times more raw materials to be processed than conventional power plants located at a considerable distance from a particular production, and also allows reducing energy costs when separating interatomic and intermolecular bonds, due to the irradiation of the substance by the flow elementary particles of plasma, with the simultaneous impact on the separated substance of a gravitational field of high gravity, allowing an additional reduction in energy costs during irradiation of the substance, which can also be reduced by an order of magnitude, allowing, with the same power of the power plant, to process ten times more substance, while spending ten times less energy on the division of intermolecular bonds, therefore, the total energy costs, in terms of a unit of production, can be reduced by a hundred times. The proposed method of plasma-arc electrolytic centrifugal conversion (PAECC) is implemented by the device of plasma-arc electrolytic centrifugal conversion (PAECC), shown in Fig. 1. The device includes a plasma torch consisting of two electrodes, a graphite tubular anode 1, inside which there is a graphite rod cathode 2, an electric arc 3 burns inside the electrodes, blown out by a plasma-forming gas supplied from a cylinder 4 through a reducer 5 and a pipeline 6. The plasma torch is installed in a melting chamber 7, in which horizontal shafts 8 are installed along a plane, through which a charge 9 is fed by means of a reverse reciprocating movement of a piston 10. The charge is fed into the shaft 8 through a vertical shaft 11, which moves under the action of gravity or under the action of mechanisms such as a screw. The charge under the effect of heating in the melting chamber forms a melt bath 12, around which a heating zone 13 of the charge coming from horizontal shafts is located. Volatile impurities evaporate above the mirror of the melt bath, which are removed through a branch pipe 14 and a pipeline 15, where the main filter 16 is installed, catching the bulk of the volatile impurities. Pumping out volatile impurities is performed by a vacuum pump 17, at the outlet of which there is a finishing filter 18, catching the remaining impurities. The melting chamber is placed on a support plate 19, where a support ring 20 is installed in the lower part, inside which a copper cooled tray 21 is installed with a central opening 22 blocked by a copper cooled valve 23, upon opening of which the melt 12 is drained into a turbine 24 rotating on an axis 25 mounted on a rotary disk 26 around an axis 27. The turbine and the movement mechanisms are protected from the atmosphere by a lower chamber 28. An electromagnetic field created by a lower solenoid 29 mounted in the support ring and an upper solenoid 30 mounted around the melting chamber is used to control the electric arc 3 and to mix the melt. The power source of the plasma torch 31 is connected to the anode and cathode of the plasma torch. The power source 32 of the main arc is connected by a negative terminal to the pallet through the support plate, and the positive terminal during heating and melting of the charge at a certain time is connected to the anode 1 of the plasma torch by means of the switch 33. Under the action of the arc and gas combustion, a plasma torch is formed between the end of the plasma torch and the surface of the charge, which turns into a melt. The melt reaches the bottom of the pallet made with a recess in the form of a cone, which allows for electrical conductivity and switching on the power source 32 by means of the switch 33, establishing the combustion of the main electric arc 3.

Fig. 1 shows how, when the melt reaches the bottom of the pallet, the main arc is switched on, passing through the space of the charge along the vertical axis, to ensure flow of electrolysis, which allows for more intensive recovery of metals from ore. When the melt reaches valve 23, immediately after that, without turning off the arc, the melt is drained into the turbine, where it is separated by density under the action of centrifugal forces.

Fig. 1 shows that the magnetic field of the solenoids is used to change the temperature gradient inside the charge. The upper solenoid 30 and the lower solenoid 29, covering the internal space of the melt with an electromagnetic field, increasing the intensity in one direction, compress the arc along the vertical axis, thereby increasing its combustion temperature. The arc, compressing to a high density at its center, can reach 50,000 K. [28] When the solenoids are turned on in countercurrent to the current in the coils, that is, in the opposite direction, the arc will expand, reducing the temperature.

The moment the melt reaches the set temperature is recorded by sensors located on the surface of the tray and the valve. The turbine rotation is ensured by a gas stream coming from the gas nozzle. The turbine is supplied with turbine blades 34 on the outside, to which the gas stream is supplied. Compressed gas (air, steam, nitrogen, hydrogen, methane, argon, helium, carbon monoxide and carbon dioxide, etc.) can be used as a medium creating rotation and cooling. This design allows, without unnecessary mechanisms, due to the gas flow, to simultaneously create rotation and cooling of the turbine, as well as a certain environment (reducing, oxidizing or neutral) affecting the process of reduction, refining and synthesis of substances. The proposed design combines several functions, i.e. it enhances the division of the substance, cooling of the substance, increases the reliability of the structure and creates a given environment. Gas simultaneously performs the functions of an energy carrier, a medium and a coolant. Reducing the weight of the turbine structure results in lower energy consumption and allows very high rotation speeds to be achieved. To reduce friction on the axis 25, an aerodynamic bearing is used by feeding gas through the pipeline 35, which passes through the cavity of the axis 36, ensuring a reduction in friction between the surface of the axis and the seat of the turbine 37.

This design allows for quick replacement of turbines with new ones by removing one turbine from the axis and installing a new one not filled with melt. Two or more turbines are placed simultaneously on the rotary disk 26, which change their location under the valve due to the rotary axis 27. After the melt is drained into the turbine and the valve is closed, the disk rotates, which allows for a new turbine to be installed along the axis. To carry out the melting process in a long-term mode, according to the continuous steel casting scheme or the blast furnace operation scheme, a plasmatron replacement device is provided, namely its electrodes with new ones, which is not shown in Fig. 1. Replacing the plasmatron electrodes allows them to be changed during melting, at the moment of pouring the melt into the turbine, for example, by turning the plasmatron and replacing it with a backup one. By turning on the continuous steel casting diagram, the pouring ladles are changed. The substance of the plasmatron electrodes, consisting of graphite, takes part in the process of melting and reducing the metal.

Fig. 1 shows a diagram of the installation with a vacuum melting chamber, which is pumped out through the branch pipe 14 by a vacuum pump 17. The vacuum allows accelerating the metal recovery process. Solid volatile impurities, metal particles and compounds are captured by a filter 16 when exiting the branch pipe 14, which can act as a trap-refrigerator for condensation and crystallization of metal and non-metal vapors. To reveal the technological capabilities of the method, we will give an example of copper recovery from sulfide ore. The greatest effect of using this method can be achieved when processing copper ore with simultaneous smelting into matte and obtaining an anode ingot. At the present stage, ore is processed to an ingot using a multi-pass scheme.

Fig. 2 shows the stages of melting the charge and reducing copper from the ore. According to the new scheme, the melt will be obtained in a neutral environment without oxidation of sulfur, which, evaporating, will be captured by filters. At the first stage, copper sulfide dissociates under the influence of temperature in the melt blown with natural gas (methane), and then iron sulfide. The separation of sulfur from copper and iron is enhanced by electrolysis. Copper collects at the bottom of the bath, iron forms a bath above the copper, and the remaining slag collects above the iron in the upper part of the bath. Then, the melt will be poured into a turbine, where it will be possible to obtain a ring-shaped ingot of copper and iron.

[29] Sulfide ores such as chalcopyrite CuFeS2 account for about 80% of world copper production, with the remaining ores containing _Cu2O oxides. The modern copper production process includes operations such as heating the charge, reducing iron and copper oxides, oxidizing sulfur, and forming slags.

FeS + 3Fe ₃ O ₄ + 5SiO ₂ = 5 (2FeO SiO ₂ ) + SO ₂ ;

2CU ₂ S + 3O ₂ = 2CU ₂ O + 2SO ₂ .

During the melting process, copper and iron sulfides fuse to form a matte, which is enriched with copper:

_{SiO22CU2S ​}

2FeS + 2CU ₂ O -I- SiO ₂ = 2FeO - I, -I- 4 into slag into matte The matte, where the density is ~5 g/ ^cm3 , collects at the bottom of the furnace, and the slag with a density of ~3.5 g/ ^cm3 forms the top layer.

Today, as a rule, copper concentrates are smelted in reverberatory furnaces. Electric furnaces have not yet found wide application, and shaft water jacket furnaces are used to smelt lump copper ore. When the shaft furnace is sealed and a reducing atmosphere is created, sulfur vapors are formed, condensing inside the filters.

The proposed method of PDECC is expedient to use for the production of anode copper directly from ore. Fig. 2a shows the moment of melting of chalcopyrite in a neutral environment, where methane is used as a plasma-forming gas. After filling the melting chamber 7 with the charge 9, which enters through the shafts under the action of pistons, the plasma torch 38 is ignited, which melts the charge from above. As a result of heating, a melt bath 12, a heating zone 13 are formed and gaseous sulfur is released, removed by a vacuum pump and captured by a filter. Hydrogen sulfide is formed in the plasma environment, which, upon further heating, decomposes into hydrogen and sulfur.

[30] Sulfur nitride N4S4 is obtained by the interaction of sulfur with liquid ammonia, its decomposition temperature is 300 °C. [31] Copper sulfide at atmospheric pressure decomposes at a temperature of 1065 °C: CLHS —> Cu2- _x S + xCu. In a vacuum, the decomposition of the molecule occurs at a temperature of 700 °C: CuiS —> 2Cu + S. [32] The onset temperature of pyrite dissociation is 500 °C, on the basis of which the decomposition of chalcopyrite can be taken to be within 1000 °C.

Fig. 26 shows the moment of formation of a melt bath, into which a plasma torch is immersed, from the anode of which the main arc burns, closed on the melt and the tray, which acts as a cathode and performs the operation of carrying out electrolysis. When sulfur evaporates from the melt, reduced copper 39 accumulates at the bottom of the bath, iron 40 accumulates above, which practically does not fuse with copper, and the mirror of the melt bath is covered with slag 41. [33] An alloy of iron and copper does not exist due to different melting temperatures and solubility properties. When copper and iron are melted, two melt baths are obtained, one above the other. Electrolysis enhances the temperature dissociation of copper and iron from sulfur.

[24] Copper electrolysis is usually carried out in baths filled with a solution of copper sulfate, acidified with sulfuric acid according to the reaction Cu - Cu ²⁺

— 2e. Copper ions from the solution are reduced and precipitate in the form of crystals on the cathode according to the reaction Cu ²⁺ + 2e — Cu. Impurities with a more negative potential (Zn, Fe, Ni, Bi, Sb, As, etc.) pass into solution but are not released at the cathode. Gold, silver, sulfur, selenium and tellurium compounds form a sludge and settle to the bottom of the bath.

When implementing the PDECR method, the electrolyte is a melt of metal sulfides (matte). The new method can be considered high-temperature electrolysis, and the PDECR device can be considered a high-temperature electrolyzer.

Fig. 26 shows the moment of release of the stream of melt 42 by opening the valve 23 into the rotating turbine 24, where first the melt of copper 39 is discharged, and then the iron 40 and metal compounds in the form of slag 41. The discharged melt is constantly irradiated with elementary particles of plasma, allowing with the least energy expenditure to destroy the interatomic-molecular bonds of the substance, the rupture of which is enhanced by the rotation and the effect of the substance of the high-gravity field.

The effect of breaking interatomic-molecular bonds is enhanced by compression of the melt stream by the compressed plasma flow 43, magnetic field 44 created by solenoids. Increasing the magnetic field intensity leads to compression of the compressed plasma flow and an increase in temperature, which increases the speed of movement of atoms and molecules inside the melt, and contributes to a more intense rupture of bonds. The temperature in the melt due to the compression of the plasma flow can increase to 10,000 K or more, which transfers the substance to a supercritical high-temperature state. When exposed to such high temperatures, any substance begins to evaporate intensively, but due to the short time of exposure of the substance to temperature, the short-range order between atoms and molecules is preserved, preventing them from going into the gas phase and evaporating. A substance in a supercritical high-temperature state, under the action of rotation, begins to expand and quickly loses the obtained temperature due to expansion. At the same time, chemical elements and stronger mechanical compounds, under the action of the kinetic energy of rotation, due to different densities, begin to separate from each other, which creates the effect of high-speed separation. At this stage, the technology includes a period of transferring the substance to a supercritical high-temperature state, in which the melt enters a high gravitational field, due to the rotation of the turbine and losing the obtained heating temperature, it begins to intensively separate by density. The presence of this moment in the technological chain of the PDECC, where the melt during movement acquires rotation and is intensively irradiated by a plasma flow compressed by the electromagnetic field of the solenoid, fundamentally distinguishes the proposed method from existing methods of metal recovery and methods of their separation. Transferring the melt to a supercritical high-temperature state for a short period of time, in within 0.1 0.001 sec, it is possible to divide these bonds with the least energy expenditure. At the same time, by regulating the temperature range inside the substance, it is possible to destroy the bonds of individual substances, producing a given separation of the substance with the release of the necessary chemical elements and their compounds.

The transfer of a substance to a high-temperature state for the longest period of time with the breaking of bonds in a high-gravity field is similar to the Ranque effect, which allows to obtain simpler substances from complex substances, with significantly lower energy costs. It should be noted that the compression of the plasma around the melt, which is also compressed under the action of the electromagnetic field of the solenoid, allows, at some separation from the graphite anode 1 and cathode 2 of the plasma torch, to act on the substance of the melt, subjecting it to high-temperature heating, while not destroying the material of the anode and cathode under the action of ultra-high temperatures. To obtain ultra-high temperatures, it is possible to place a separate solenoid around the falling stream of melt 42, creating a more powerful electromagnetic field of action on the plasma and the substance, and it is also possible to place lasers, electron beam guns or magnetrons, additionally irradiating the substance of the melt stream.

Fig. 2c shows the moment when after draining the melt bath, the valve returns back, blocking the tray 21, the plasma torch is moved upward to its original position. The internal volume of the turbine cavity exceeds the volume of the melt being drained, which, under the action of centrifugal forces of rotation, is separated by density, solidifying in the form of an annular ingot (disk). Anode copper 39 accumulates on the outer diameter of the disk, followed by iron 40, and then closer to the center, the compounds of metals with sulfur, oxygen and nitrogen, i.e. slag 41. Immediately after draining and closing the valve, the charge enters the melting chamber, including the heated charge 45, which moves to the center under the action of the pistons and cold charge 9, until the internal space of the melting chamber is filled.

Fig. 2g shows the moment when immediately after this the plasma torch 38, which was not switched off, begins to melt the heated charge 45 mixed with the cold charge 9, forming a bath 12 and a heating zone 13. The plasma torch is gradually immersed in the melt and after reaching a certain electrical conductivity of the melt, the main arc is switched on, providing additional heating of the melt bath, up to the pallet and the valve. During the switching on of the main arc, electrolysis is ensured in the entire volume of the melt bath, accelerating the reduction and separation of the chalcopyrite molecule into metals. and sulfur. After separation of chemical elements by electrolysis, the melt is drained into a rotating turbine while simultaneously irradiating the melt flow with plasma particles, i.e. photons, ions, protons, electrons, etc. particles. The process of irradiating the melt in a high-gravity gravitational field, as described earlier, accelerates the process of dividing interatomic and intermolecular bonds at lower energy costs. The division of the substance into constituent chemical compounds is enhanced by its rotation in the turbine with the formation of a new ingot, and then the process is repeated. Today, radioactive and radiation emissions are used to reduce energy costs in hydrocarbon processing, where the ionization of the substance leads to a change in its structure and properties. For example, this method includes Upgrading, which uses an electron flow with a power of up to 800 kW, 5 MeV, with low metal consumption and without the use of expensive catalysts. Another method called "Radiation Wave Cracking" (RWC) uses the Ranque effect by irradiating (microwave) hydrocarbons with ultra-high-frequency waves and ions, where energy costs can be reduced by 10 times compared to conventional technologies. The ingot is then sent to electrolysis as anode copper or to melting for smelting copper anodes for standard electrolysis. The produced ingots after electrolysis are cleaned of slag by mechanical cutting, crushing or electrohydropulse crushing. Slag with more stable oxides is sent for reprocessing by the PDECK method.

[34] For comparison with the analogues of the new method of PDECC, it is necessary to take into account that the process of ore reduction takes place in the melt at high heating with the flow of electrolysis. Then the separation of the melt into chemical elements with different density is carried out in a field of high gravity. The separation process is combined with the process of directional crystallization of the ingot. The reduction and separation of metal in the electric arc centrifugal reactor will differ from conventional metallurgical processes in the following:

1. At the boundary of two media (liquid metal - growing crystal), where the interphase energy is significantly less than the interphase energy at the boundary of two media (gas - liquid metal) in the surface layer of the solid there are significantly fewer free bonds than at the boundary with the gas phase. In this regard, all impurities during the crystallization of the metal into an ingot pass into the liquid phase. In this case, favorable conditions are created for the formation of pure metals in the solid phase;

2. The effect and speed of metal refining can be enhanced by increasing the rotation speed. The existence of a gas bubble in a metal melt is determined by the pressure in it: p _n = p _v n + pgh +2?/g, where p v n is the external pressure above the melt, pgh is the metallostatic pressure, where p is the density of the melt, g is the acceleration of gravity, h is the depth, 2?/g is the capillary pressure, depending on the interphase energy at the melt-gas boundary and the bubble radius r.

[34] From a technical point of view, the meaning of this formula can be divided into three parts:

1. When changing p _in n - the external pressure above the melt, melt degassing can either decrease or increase. For example, by using vacuum above the melt, a low gas content is achieved. In the case of centrifugal pressure acting on the melt, gases are distilled from the melt according to the same scheme as in the case of vacuum, since the pressure in the melt increases significantly, and one atmosphere continues to act on it from the side of the bath mirror.

2. Metallostatic pressure pgh, in the case of using conventional metallurgical furnaces, changes only due to the depth of the gas from the surface of the melt. With increasing depth, the buoyancy force on the gas bubble increases, but in order to leave the melt, the gas bubble has to travel a large distance. In the case of centrifugal action on a gas bubble located at a small depth, the metallostatic pressure is very high due to a significant increase in gravity. Therefore, the gas quickly leaves the thin layer of molten metal.

3. Capillary pressure 2o/g depends very much on the viscosity of the melt. Thus, when the temperature above the melt bath mirror decreases, incomplete removal of gas from the melt is observed, in other words, quenching of the gas solution occurs first in the liquid metal, and then in the solid. When using centrifugal converting, heating of the melt bath mirror is used, therefore, quenching of gas in the melt does not occur.

Additionally, it is necessary to take into account that when implementing the PDECC method, the process of electrolysis occurs simultaneously with the chemical reactions, i.e. less time is required to carry out the reactions, and at the final stage before the formation of the ingot, the process of separation of the reaction products occurs due to irradiation and rotation in a high-gravity field. The process is designed in such a way that crystallization of pure metal occurs from the melt in one direction, and displacement occurs in the other direction. impurities, including gases, thereby preventing the reverse reaction of their interaction.

[34] For the recovery and separation of metals by density, increased gravity will play a positive role, accelerating the process of separating pure metal from impurities. The centrifugal force acting on a metal particle, at a turbine rotation frequency n, is equal to:

P = m*r* ^co2 where m is the mass of the particle, kg; r is the radius of rotation, m; co = ts*u30 is the rotation frequency of the mold, min ¹ .

When calculating the turbine rotation speed based on the gravity coefficient, it is taken into account that the melt particles are subject to centrifugal force:

Fif = m* V ² /R, where m is the mass of the particle, kg; V is the linear velocity, m/s; R is the radius of rotation of the particle, m.

If the centrifugal force is greater than the force of gravity Fg = m*g by more than an order of magnitude, then the melt will occupy the entire lateral area of the rotating container.

The gravity coefficient k is calculated based on the formula: k = F ₄ /F _g = V ² /R*g.

For example, if the internal diameter of the turbine at a rotation speed of u = 240 rpm is 2 m, the rotation radius will be R = 1 m, the peripheral speed V = 6.28 m/sec, therefore, the gravity coefficient will be k ~ 64. This is a significant gravity coefficient, ensuring rapid separation of the final reduction products, where a ring-shaped metal ingot without impurities is produced at the outlet.

According to the presented scheme, it is possible to produce nickel, cobalt, iron and other metals from sulfur and oxide ore compounds. For industry, the proposed method may be of particular interest for processing pyrite and arsenopyrite containing precious metals. As a result of production, precious metals get into the outer part of the disk ingot, as they have the highest density. Precious metals are not alloyed with iron, and electrolysis is used to extract them from the outer surface of the ingot. As a result of melting pyrite and arsenopyrite in a neutral environment, harmful impurities in the form of sulfur and arsenic, evaporating, are captured by the filter, without forming toxic volatile compounds.

The proposed method of PDECC can be further expanded for the production of magnesium.

[35] The most well-known method in industry is the Pidgeon method, which recovers magnesium from dolomite under vacuum using ferrosilicon: 2MgO( _T ) + 2CaO( _T ) + (Si-Fe)(T) - 2Mgr + 2CaO SiO ₂ (T) + Fe.

Magnesium oxide is reduced to gaseous magnesium, and calcium oxide binds the resulting silica into refractory dicalcium silicate. Iron does not participate in the reduction process. At the operating temperature of the process of 1150 °C, interaction of CaO and Si is possible with the appearance of liquid Ca - Si alloys and dicalcium silicate:

2CaO SiO ₂ : 4CaO _(t) + 2Si _(T >= Ca ₂ Si _(3K) + 2CaO SiO _{2 (l)} ,

4CaO( _T ) + 3Si( _T ) ⁼ 2CaSi(at) + 2CaO SiO ₂ ( )

Further interaction of the Ca ₂ Si melt with magnesium oxide leads to the formation of gaseous magnesium:

4MgO( _T ) + Ca ₂ Si(>K) = 4Mg(r)+ 2CaO SiO ₂ ( _T )

The thermal energy released during the formation of dicalcium silicate facilitates the reduction of magnesium oxide by lowering the reaction start temperature. The retort contains calcined dolomite and ferrosilicon. The reduction cycle is approximately 13 hours, the residual pressure is 10 kPa, and the process temperature is 1150 °C.

The Pidgeon method was developed in China, where a number of improvements were introduced. These include replacing the generator gas with coal powder, installing vacuum pumps equipped with a steam ejector instead of mechanical ones, where the steam supplied to the pumps is generated by the heat of the exhaust gases of the retort furnace. The first installations used horizontal retorts, while in China, vertical retorts of large diameter were used. These measures reduced energy consumption, increased productivity, and improved the magnesium recovery process, which allowed China to take first place in the world in magnesium production.

Magnetherm technology has improved the silicothermic reduction of magnesium by reducing magnesium oxide in a slag melt, where an electric resistance furnace is used to melt the charge. The slag is removed from the furnace without breaking the vacuum at 35 kPa, at a temperature of 1600 °C. With a capacity of 4.4 MW, 7.5 t of magnesium are produced daily. The charge is loaded from sealed bins for 8.5 hours, and magnesium vapor enters the condenser at 650 °C, flowing into a water-cooled steel crucible, which, after filling with molten magnesium, is separated from the condenser and transported to the ingot casting. The energy consumption for melting in the furnace is 11 MWh/t with an 85% magnesium recovery.

Fig. 3 shows a modification of the PDETSK plant for the production of magnesium. The plant is equipped with sealed bunkers 44 for loading the charge, which enters through the sealing valve 45. The charge exits at a given speed and volume through the regulating valve 46, into the vertical shaft 47. The charge 48 falls in the form of raindrops through the upper partition 49 and the lower partition 50, creating a sand filter for magnesium vapors 51, along with which other chemical substances evaporate, settling on the falling charge 48. Due to this operation, the charge is heated and captures particles of soot carbon evaporating with magnesium vapor, which makes it possible to reduce the consumption of metal reducing agent during smelting. Purified magnesium vapors 52 condense on pipes 53, through which vacuum is pumped out, of which there are two or more, serving for alternate heating and draining of magnesium from their surface. The pipes are fixed on a flange 54, closed by a chamber 55, from which vacuum is also pumped out through a pipeline 56, passing through the main filter 57, where volatile impurities are captured. Vacuum is pumped out by a vacuum pump 58, equipped with a steam ejector, where a finishing filter 59 is installed at the outlet, capturing the remaining impurities from the pumped-out flow of substances.

Vacuum pump 58 is fed through pipeline 60 to supply steam generated during cooling of the melting chamber, tray, valve and other units of the installation. Condensate goes back through pipeline 61 to cool the units of the PDECR installation. It is advisable to use olivine mineral as a charge 62, where carbon gets for magnesium production, which contains MgO - 48%; SiCh - 40%; FC2O3 - 8%; CaO - 0.5%. Methane is used as a charge reducing agent, which is fed from cylinder 63 through pipeline 64 into plasma torch 65. In the combustion zone of the main arc 66, methane is separated into hydrogen and carbon. At an arc temperature above 2000 °C, hydrogen does not participate in the reduction reaction and works as a protective environment. Carbon first reduces iron and then silicon, creating ferrosilicon in the melt bath 67, which begins to reduce magnesium 51, evaporating above the bath. The magnesium reduction reaction is accelerated by free carbon, forming carbon monoxide due to the capture of oxygen from metal oxides. As a result of melting, at the outlet of the vacuum pump and filter, synthesis gas consisting of hydrogen and CO enters the accumulator 69 through pipeline 68, which can then be used to synthesize chemical hydrocarbons or for combustion at thermal power plants to generate electricity, which can be used by the plasma torch of the PDECR installation.

In the melt bath 67, the reduction of magnesium is accelerated by electrolysis occurring under the action of the main arc 66, since the melt is the cathode where the reduction reactions occur. As is known, ferrosilicon is a material with low thermal conductivity, which prevents the reduction of magnesium. To eliminate this drawback, the melt bath is set in motion, mixing the substance under the action of the electromagnetic fields of the main arc, due to the upper 70 and lower 71 solenoids. After magnesium has evaporated from the charge, the melt is drained into a rotating turbine 72, where an annular ingot is formed under the action of plasma irradiation and centrifugal forces. A ring 73 of iron is formed on the outer diameter of the ingot, then a ring 74 of calcium oxide with a density of 3.3 g / cm ³ , and inside a ring 75 of silicon oxide with a density of 2.3 g / cm ³ . To unload liquid magnesium 76 from crucible 77, without stopping the process, a vacuum chamber 78 is installed, in which one crucible is replaced by another. As a result of the operation of the PDECR plant, production significantly reduces time, costs and energy consumption, obtaining at the output several products with high market value - magnesium, iron, synthesis gas, calcium oxide and silicon.

In order to reduce energy costs and increase the production speed, the proposed invention may be used to reduce aluminum. Using the proposed method of PDECC, it is possible to produce aluminum from bauxites by reducing it with carbon in the presence of hydrogen. For this purpose, natural gas or methane is supplied through a plasma torch into the arc combustion zone, which, when decomposed in the arc combustion zone into C and H, will reduce aluminum with carbon. As a result, the resulting synthesis gas is then sent to the production of chemical products or combustion for the production of heat and electricity.

Fig. 4 shows the scheme of the PDECC plant for the production of aluminum. Natural gas (methane) is used as an aluminum reducing agent, which enters through a pipeline 79, through a reducer 80 to a nozzle 81, from which a gas stream 82 breaks out, spinning and cooling a turbine 83, where the reduced aluminum, the remaining aluminum oxide and carbon are discharged. When forming a ring ingot, a ring 84 of aluminum oxide with a density of 3.9 g/cm ³ is formed on the outer part, then a ring of aluminum 85 with a density of 2.7 g/cm ³ and in the center a ring 86 of carbon with a density of 1.8 g/cm ³ . The heated gas obtained after the rotation and cooling of the turbine is pumped out of the sealed chamber 87 by means of the compressor 88 and accumulates in the receiver 89. Then, when the valve 90 is opened, it passes through the pipeline 91 through the housing of the installation, additionally heating up to a certain temperature, entering through the reducer 92 into the internal cavity of the plasma torch. Preliminary heating of the methane allows to reduce energy consumption during its dissociation in the plasma. Due to the combustion of the plasma and the main arc 93, a melt bath 94 is formed from aluminum oxide, which melts at a temperature about 2050°C. Due to the reduction of aluminum by carbon in the hydrogen atmosphere above the melt bath, synthesis gas and soot carbon evaporate, which pass through a sand filter 97 created by particles of falling aluminum oxide powder via pipeline 96. The synthesis gas is freed from soot carbon particles due to their deposition on the aluminum oxide particles. Therefore, the carbon returns again together with the heated charge 98 to the melting process, reducing the costs of carbon consumption from methane and overall heating. The purified synthesis gas contains a portion of methane undissociated in the plasma, which enters the gas separator 99, where it is separated from the synthesis gas. The methane captured in the separator is directed via pipeline 100 to continue the process in the plasmatron. Through pipeline 101, synthesis gas enters main filter 102, passes through vacuum pump 103 with steam ejector, passes finishing filter 104 and enters storage tank 105.

By using the proposed invention for the production of aluminum, it is possible not only to reduce energy costs by two and a half times, but also to produce synthesis gas for use in chemical production.

[5] The use of a new invention in a similar scheme for the production of titanium is promising. Reduced titanium due to carbon, like aluminum, will form a molten bath containing slags consisting of carbides and oxides. In the melt, the density of titanium is 4.1 g / cm ³ , which is less than that of oxides and titanium carbide TiO2 - 4.23 g / cm ³ , Ti2O3 - 4.49 g / cm ³ , TiO - 4.95 g / cm ³ , PS - 4.93 g / cm ³ , but greater than the density of carbon - 2.26 g / cm ³ . When draining the molten bath into a rotating turbine, all titanium compounds, as heavier ones, will be displaced to the outer contour of the ingot, and carbon will be displaced from the titanium melt to the center of rotation. Subsequently, after the ingot is extracted, pure titanium will be separated from ceramic impurities by mechanical crushing.

[36] As is known, titanium oxide and carbon, when heated, enter into a chemical reaction according to the scheme:

2TiO ₂ + C <-» Ti ₂ O ₃ 4” CO', Ti ₂ O ₃ + C 2ТЮ + CO', TiO + 2С ТЮ + CO;

TU + C T1 + CO;

Ti + C TYu;

Tiu ₂ + ZS «-> TiC + 2СО.

Thermodynamic calculations show that carbide formation reactions will occur first. The process of carbide formation by the overall reaction T Ю ₂ + 3C <-> TiC + 2CO proceeds through the formation of a series of intermediate oxides, which form a continuous series of solid solutions with titanium carbide. An increase in temperature or a decrease in pressure shifts the equilibrium of the Ti — TiCxOy — C — CO system towards the replacement of oxygen by carbon. Practically pure titanium carbide can be obtained at atmospheric pressure and a temperature of about 2430 °C. At a pressure below 1000 Pa and a temperature above 1300 °C, complete deoxygenation of the solid solution is achieved and metallic titanium is released due to the reaction:

TiC + CO2 Ti + 2CO, as well as the related reaction Ti + C <-> TiC, which proceeds under these conditions to the left.

Titanium metal can be obtained by reducing its dioxide with carbon at a temperature of about 3000 °C in a vacuum according to the overall reaction:

Т1О2 З - 2TiC -» 3Ti + 2СО.

Previously, under laboratory conditions, titanium recovery was carried out in retorts, where after extraction the metal was always contaminated with carbon, oxygen, and nitrogen.

Today, when using the PDECC installation, it is possible to restore titanium, which in liquid form, under the action of centrifugal forces, will crystallize into a skull, forming a ring ingot, while displacing light impurities of oxygen, carbon and hydrogen to the center of rotation, and heavy titanium compounds to the periphery. At the anode, which is a plasma torch, oxygen anions will be oxidized with the release of CO. In the well-known "Cambridge" process, only CO2 is released at the anode, since the reaction temperature is very low and the surface layer of the anode is saturated with anions, which are bombarded by a flow of electrons. In the proposed PDECC method, the reduction of titanium will be accelerated due to the increased temperature of the melt bath (more than 2000 ° C), at which carbon becomes the most active reducing agent, compared to any other reducing agents, which shifts the chemical reaction towards the reduction of the metal, simultaneously with the chemical process, the electrolysis process occurs. When titanium is reduced in a melt bath, which is a cathode, the reduction of the metal is enhanced by “hot” electrolysis. The produced titanium from chemical and electrolytic reduction, when entering a rotating turbine, is removed from the reverse reaction of interaction with carbon and oxygen, due to plasma irradiation and centrifugal forces of rotation in the presence of hydrogen, which prevents the interaction of titanium with carbon and oxygen. Titanium, having the highest density in the melt, compared to hydrogen, oxygen and carbon, will shift to the periphery of the ingot, where it will freeze in the annular ingot, without the presence of these chemical elements. Additional purification from impurities is carried out due to zone purification, during the crystallization of titanium layer by layer into an ingot. Titanium, when solidifying, increases its density, which increases the displacement of lower-density impurities of hydrogen, carbon and oxygen into the melt. As the temperature decreases, hydrogen will react with oxygen, forming water, which will be removed in the form of vapors through a vacuum system. Hydrogen also reacts with carbon, forming hydrocarbons, which are pumped out by a vacuum pump. Hydrogen, which most actively gets into the titanium melt, prevents oxygen and carbon from getting into the melt and is later removed from the titanium by vacuum annealing.

The PDECC method, the scheme of which is shown in Fig. 5, can be most effectively used for energy production together with the production of metals and non-metals, the production of energy carriers in the form of methanol, its storage and transportation to the energy consumer, with the return of carbon dioxide used at the first stage as a coolant, and at the second stage as a raw material for the production of the energy carrier. In this scheme, at the PDECC installation, the production of metals and non-metals is combined with the process of energy and energy carrier production, closed to the energy consumer.

To produce an energy carrier, which is methanol, it is necessary to maintain a certain ratio of the amount of reagents for its effective synthesis. Therefore, the process of methanol synthesis is carried out by accumulating reagents and burning part of them during the production of electricity, which is spent on plasma combustion. Two or more power plants ensure the maintenance of a given ratio of the amount of generated electricity in relation to thermal energy, since generation is carried out with power plants that have different efficiencies. Power plants that are connected into a single system allow you to stably maintain a given ratio, regardless of the change in the ratio of the amount of hydrogen and oxygen produced in the process of fission of the substance. Therefore, in the energy generation section, the ratio of the share of generated electricity in relation to the share of thermal energy is automatically adjusted. An increase in the share of electricity generation in relation to the generation of thermal energy leads to an increase in the power of the plasma torch and, accordingly, to an increase in the volumes of batch processing, methanol synthesis and the number of volumes of refrigerant cooling the equipment of the metallurgical and chemical section, while the consumption of refrigerant for cooling the turbine condenser is reduced, which leads to an increase in the efficiency of the process production of energy carriers, metals and non-metals. An increase in the share of thermal energy production in relation to the generation of electricity leads to a decrease in the plasmatron power, a decrease in the volumes of batch processing, methanol synthesis and the amount of coolant volumes, while the volume of coolant for cooling the metallurgical and chemical section decreases and at the same time the volume of coolant for cooling the turbine condenser increases, which leads to a decrease in the efficiency of the process of producing energy carriers, metals and non-metals.

In connection with the above, a scheme is built in the area of electric power production, which includes a condenser-type power plant that generates a given capacity, but which does not operate due to the combustion of multi-component organic fuel, which includes hydrocarbon fossil fuel. A nuclear power plant operating at a constant capacity is most suitable for this. Nuclear power plants are most effectively used together with power plants on renewable energy sources, which allows the generated energy to be converted into metals, non-metals and an energy carrier. When thermal power plants operate on organic fuel, such as methane, oil, fuel oil, coal, peat or shale, a separate combustion furnace is required, in which there are inevitable losses of energy and matter, but the main losses occur as a result of inefficient combustion of combustible chemical elements such as carbon and hydrogen found in compounds. As a result of combustion, organic fuel does not release the maximum possible amount of heat, which is released when hydrogen and carbon, which are part of various fuels, are burned separately. Therefore, the system of several types of power plants will include nuclear power plants and power plants operating on the combustion of hydrogen, which is not an organic fuel. To start the process and produce the required volume of hydrogen fuel, as well as for the stable operation of the entire scheme, of the various types of power plants available today, the nuclear power plant is the most suitable. Electricity generation at nuclear power plants is related to thermal energy as 30-70%. This ratio in terms of the share of electricity is not very effective, while nuclear power plants do not require the combustion of organic fuel and do not produce harmful emissions. [14] To increase the efficiency of electricity generation, nuclear power plant turbines are combined with hydrogen combustion chambers. [14] Another type of condenser power plants that are most suitable for the implementation of the process are hydrogen thermal power plants (HTPP). These power plants, like nuclear power plants, contain steam turbines, but at HTPP the turbines are equipped with combustion chambers. Therefore, to implement the PDECK process, the nuclear power plant and HTPP schemes are combined into a common scheme, where There is a common turbo plant on which superheaters are located, and high and medium pressure cylinders are equipped with combustion chambers (CC) operating on regular steam and steam obtained by burning oxygen and hydrogen in the CC. Specialized NPPs, where steam turbines are supplemented with combustion chambers for burning hydrogen, increase the efficiency of electricity generation to 37%. The efficiency of HTPPs reaches 69%, therefore, when combining NPPs and HTPPs, the average efficiency will be approximately 53%. The system generating electricity, created on the basis of NPPs and HTPPs, to increase the efficiency, is supplemented with high-temperature fuel cells (HTC), having an efficiency of electricity generation reaching 85%. HTCs require heating in the range of 650-950 ° for their operation, therefore the necessary heat is used from NPPs and HTPPs. As a result of the combination, a combined power plant is created with an efficiency of electricity generation reaching an average of 69%. All units of the power plant created on the basis of the NPP-VTES-VTE are combined and operate according to an interconnected scheme. The practical advantage of the power plant created on this basis from three different systems is the flexible adjustment for the generation of electricity and heat at any time, which is necessary for the operation of the entire PDETSK process. As a result of the process, different amounts of electricity are absorbed in relation to heat at different times, since different amounts of oxidizers and combustible substances are released over time. The nuclear reactor operates most efficiently and safely with a constant load and is not used in the case of its constant change. Consequently, the reactor capacity in relation to the capacity of other types of power plants can be in the range from 1 to 50%, and load fluctuations are damped or replenished by the VTES and VTE.

The process of redistribution of energy and substance is arranged in such a way that at any time, the necessary chemical reagents, such as hydrogen, CO, CO2, H2O and energy, are directed to one or another section of production where they are needed. For example, storing hydrogen is a fairly expensive process, so its main volume, immediately after the release of hydrogen during the plasma-chemical reaction, is directed to the synthesis of methanol for its long-term and unlimited storage. Excess hydrogen is sent for combustion in the combustion chambers of turbines of power plants or in fuel cells, and a small part of the hydrogen volume is stored in a storage tank to smooth out pulsations during the generation of the required energy capacity or to replenish the volume during the synthesis of methanol. To generate more energy, hydrogen is extracted from methanol using a methanol processor, which receives water and methanol. When heated, a catalytic reaction of methanol with water occurs, forming hydrogen and carbon dioxide. Hydrogen is sent for combustion in the combustion chambers of the power plant. Carbon dioxide is used in the energy production section as a steam heater, in the melting section as a plasma-forming gas and in the methanol synthesis section as a reagent. As a result of a deeper conversion of carbon dioxide under the influence of plasma, a reaction of its dissociation into oxygen and carbon monoxide occurs. Oxygen ensures the autothermal reaction of the formation of synthesis gas for the synthesis of methanol, together with methane and steam, and oxygen is also used to burn hydrogen in turbines and fuel cells. Carbon monoxide works as a reducing agent for metals from ore and is a reagent for the synthesis of methanol.

To completely eliminate thermal emissions into the environment, a scheme is used to use ore, hydrocarbons and final products of production as coolants, i.e. the process of generating electricity and heat is combined with the process of processing the substance, supplying the substance to the energy consumer and returning part of the substance from the consumer. Today, iron accounts for the largest amount of all metals produced by industry in the world. Consequently, iron production consumes the largest amount of energy and associated reagents, compared to other metals. The PDECC method is aimed at reducing energy costs in the production of iron and associated metals and non-metals, which include hydrocarbons.

As an example of the implementation of the method of the PDCK for the production of metals, non-metals and energy carriers, including iron, the PDCK device shown in Fig. 5 is proposed. For the primary generation of electric power, a nuclear reactor 1 is used, but if necessary, any type of power plant operating on renewable energy or fuel combustion can be used. Water circulating along circuit 2 passes through reactor 1 and is heated, under the action of pump 3 heating the water in heat exchanger 4, through which a steam line 5 passes, feeding water from below, which exits in the form of steam, entering the combustion chamber 6 of the high-pressure turbine 7. An oxygen pipeline 8 and a hydrogen pipeline 9 are fed into the combustion chamber 6, and steam is fed through pipeline 10, where the gas volume is adjusted by valves 11, 12, 13. To start the turbine, a bypass 14 with valve 15 is used, allowing energy to be generated without a combustion chamber. At the turbine outlet, a pipe 16 is installed, through which steam passes directly through valve 17. enters the medium pressure turbine 18, and through pipeline 19 through valve 20 and pipeline 21, the steam enters the combustion chamber 22, where hydrogen is supplied through pipeline 23 and valve 24, and oxygen through pipeline 25 and valve 26. From the medium pressure turbine the steam exits through the pipeline 27, gets into the heat exchanger 28 and through the pipeline 29 goes to the low pressure turbine 30, from where through the pipeline 31 the steam enters the condenser 32, from where through the pipeline 33 part of the condensate under the action of the pump 34 through the heat exchanger 28 and the heat exchanger 35 installed on the medium pressure turbine and the valve 36 returns to the pipeline 21. The other part of the condensate by the pump 37 through the pipeline 38 through the heat exchanger 39 goes to the heat exchanger 28 valve 40, and the steam comes to the combustion chamber 6. Through the heat exchanger 28 passes the pipeline 41, where the oxygen is heated, and gets to the distribution valve 42, from where through the pipeline 43 it can enter the combustion chambers, and through the pipeline 44 to the fuel element 45.

[14] The hydrogen turbine uses the latest development, which allows achieving an efficiency of 69% in the generation of electric power, due to the generator 46, which transmits the energy carrier to the external network through contacts 47. The generated power is transmitted for internal consumption through a transformer 48, which supplies two rectifiers 49 and 50, from where electric power is supplied to the contacts of the plasma torch 51; 52; 53. Electric power can be supplied to the transformer 48 through the inverter 54 and contacts 55 from the fuel cell 45.

The fuel cell (FC) can generate power comparable to a hydrogen turbine, for which a high-temperature fuel cell is most suitable, which additionally heats the oxygen in the pipeline 44 with its heat through the heat exchanger 56, which is supplied to the cathode of the FC.

[15] High-temperature fuel cells are adopted as an analogue of the fuel cell, allowing the generation of up to 20 MW or more. Hydrogen is supplied to the anode of the fuel cell via pipeline 57 through distribution valve 58, where hydrogen can be supplied via pipeline 59, heated in heat exchanger 60 from storage tank 61 or via pipeline 62 from methanol processor 63. Methanol is supplied to the processor via pipeline 64, heated in heat exchanger 65, where it is supplied via distribution valve 66 via pipeline 67 from storage tank 68, into which it is supplied by pump 69 from discharge tank 70. Water is also supplied to processor 63 via pipeline 71 through distribution valve 72, coming from fuel cell 45 by pump 73. As a result of the interaction of methanol and water, in addition to hydrogen, carbon dioxide, which from the processor through the storage tank 74 via the pipeline 75 is directed to the distribution valve 76, from where the gas is supplied in two directions. Through the pipeline 77 into the distribution valve 78 and the reducer 79, the gas enters the plasma torch 80 through the opening 81, passing around the central electrode 82 and inside the tubular electrode 83 ensuring the combustion of the arc 84, which forms the plasma 85. The electrodes in the plasma torch are separated by an insulator 86 fixed in the cooled bushing 87 installed in the body of the furnace 88. Natural gas (methane) enters the plasma torch in a controlled volume through the valve 89, pipeline 90 and the distribution valve 91. Methane enters through pipeline 92, pre-compressed by compressor 93, passing through distribution valve 94, entering via pipeline 95 and passing for the purpose of purification through separator 96, from which impurities, including sulfur, enter storage tank 97. Gas enters separator 96 through pipeline 98, pre-heated in heat exchanger 99 and 100. An additional volume of methane enters the production chain through distribution valve 94 via pipeline 101 from storage tank 102. In addition to feeding a certain volume of methane into the plasma torch, where it enters through pipeline 90, through valve 89 and reducer 79 to maintain plasma combustion, another portion of methane is supplied via pipeline 103, through distribution valve 104, via pipeline 105, which is fed to cool the chamber body 88. Methane, cooling the chamber body, passing through the internal coils, is heated and exits through pipeline 106, entering filter 107, dumping impurities into tank 108 and then entering mixer (pre-reforming) 109. From distribution valve 104 through pipeline 110, another portion of methane is fed at a certain point in time through nozzle 111, creating a jet 112 that spins crucible turbine 113 and simultaneously cools it from the outside through the planes of blades 114. With valve 115 closed, methane enters lower chamber 116, from where it is fed through pipeline 117 by pump 118 into pipeline 119, and then through opening 120, methane enters inside batch 121, where reactions begin to occur with the release of carbon and hydrogen. The batch is pushed and mixed by the screw 122. At the same time, oil enters the internal volume of the batch together with methane through the opening 120, which is supplied in a certain volume through the distribution valve 123, where the oil enters through the pipeline 124, having been preheated in the heat exchangers 125 and 126. Fuel oil or other liquid mixtures of hydrocarbons can be used as oil, after the refinery. After opening the valve 115 and draining a certain volume of melt 127, which is in the plasma 85 during melting, skull 128 into the crucible turbine 113, an ingot (disk) 129 is formed, consisting of a substance of varying density. During the opening of the valve, methane, entering through the nozzle 111, passes through the plasma 85 and the heated skull 128, partially dissociating into carbon and hydrogen and then, entering the pipes 130, passing through the flow of ore particles 131 and passing through the rectification columns 132, 133, 134, pumped out through the pipeline 135 by the pump 136, enters the separator 137. Together with methane, gases consisting of carbon monoxide and carbon dioxide, hydrogen and oxygen, water and carbon vapors, as well as vapors of metals and non-metals contained in the reagents being remelted enter the gas flow 138 during the operation of the plasma. The gas flow 138, passing through the mesh catalyst 139, forms a certain volume of synthesis gas in the flow, and then passing through the flow of ore particles, heats it and is freed from some of the impurities, such as carbon, which is deposited on the ore particles. Then the gas flow, passing through the rectification columns, is freed in the first column from the most refractory metals and non-metals, which accumulate in the form of a melt in the tank 140. In the next tank 141, substances with an average melting point accumulate, and in the tank 142, more easily melting substances. Tanks 140, 141 and 142 are located in chamber 143, where the melts are heated and then drained into separators 144, 145 and 146. From these separators, the reduced metals and non-metals are pumped to the storage location by pumps 147, 148 and 149, and the slags are fed by pumps 150, 151 and 152 for reprocessing through pipeline 153 and opening 154, and enter the remelted batch.

121. Crucible turbine 113 with solid disk 129 through sluice gate 156 enters chamber 157, where outer and inner plane of turbine are processed by steam jet 158 rotating and cooling it. Steam enters through nozzle 159 and 160, and before that enters through distribution valve 161 and wire 162, leaving support plate 163, where water enters through pipeline 164.

On the inner surface of disk 129 carbon accumulates, which has the lowest density among the components of the charge. When interacting with steam, heated carbon forms water gas, which from chamber 157 together with steam, through pipeline 165, under the action of pump 166, enters pipeline 153, mixing with slags and then through opening 154, mixes with charge 121, under the action of auger

122, enters under the plasma. A certain volume of steam through the distribution valve 161 enters through the pipeline 167 to the compressor 168 and then under pressure into the pipeline 169, through which methane moves, forming a mixture in the mixer 109. Due to the formation of the mixture, the pre-reforming process takes place, from where the gas mixture exits through the pipeline 170, mixing with carbon dioxide in the pipeline 171, where it enters, compressed by compressor 172, moving along pipeline 173 from distribution valve 174. Carbon dioxide enters this valve via pipelines 175 and 176. In pipeline 177, formed by the merger of pipelines 170 and 171, synthesis gas is formed, which is directed to heating and passed through the internal cavity of the cooled sleeve 87 of the plasma torch, exiting through pipeline 178, entering compressor 179. From this compressor, through pipeline 180, the synthesis gas enters under pressure into heat exchanger 181 and then into methanol reactor 182, where, passing along the outer perimeter of its body downwards, the synthesis gas is heated due to the temperature of the reagents and then passes upwards, getting onto catalyst 183 and then the formed mixture of methanol and synthesis gas moves downwards through pipes 184, through filter 185, exiting through pipeline 186, passing through heat exchanger 181, where it is cooled and exits through pipeline 187, further cooling, passing through heat exchanger 188. From this heat exchanger, the mixture enters separator 189, where a methanol bath 190 is formed in the lower part, drained through pipeline 191 into collecting tank 70. Synthesis gas not converted into methanol through pipeline 192 leaves separator 189, and, compressed by compressor 193, through circulation pipelines 194 and 195 again enters heat exchanger 181. An additional volume of synthesis gas is fed into pipeline 195 due to its supply through pipeline 196, which is formed inside the body of plasma furnace 88. Synthesis gas is formed from hydrogen entering through pipeline 197, pre-compressed by compressor 198, through distribution valve 199, where hydrogen comes through pipeline 200 from separator 137. From the same separator, through pipeline 201, through distribution valve 202, carbon monoxide comes, being compressed by compressor 203 and through pipeline 204, connecting with pipeline 197, where it forms synthesis gas, which, moving through pipeline 196, then goes to pipeline 195 for methanol synthesis. Through distribution valve 199 and pipeline 205, storage tank 61 is filled with hydrogen from separator 137. Through pipeline 206, from separator 137, storage tank 207 is filled with oxygen, from where it enters heat exchanger 210 through pipeline 208 under the action of pump 209, where it exits through pipeline 41, being heated. Water exits separator 137 through pipeline 211, accumulating in storage tank 212, from where it enters distribution valve 215 through pipeline 213 under the action of pump 214, and through pipeline 216, through opening 217, in a certain volume it enters inside the body of furnace chamber 88, affecting the concentration of gas reagents of flow 138. The water flow, being heated inside the furnace, gets onto catalyst 139, cleans its surface from surface deposits and restores its operability. By adjusting the volume of water supplied to the chamber the furnace body regulates the formation of the maximum volume of synthesis gas. Another part of the water volume from the distribution valve 215 is directed through the pipeline 218 and 219 into the bath 220, where coal 222 enters from above through the line 221. Any carbon-containing substances can be used as coal, including peat, sawdust, wood, cardboard and others. The water in the bath is cooled and passing along the entire length from below is taken through the pipeline 223, under the action of the pump 224, entering the bath 225, where ore 227 enters from above through the line 226, also cooling the water. Any ore enrichment waste, river sand, pebbles, clay and other similar substances can be used as ore, since for the PDECC process they are industrial ores. Water is taken from the bottom of the bath by pipeline 228 under the action of pump 229, passing through filter 230, from where it goes to cool condenser 32 by pipeline 231, returning in heated form by pipeline 232, connecting with pipeline 218, entering a repeated cooling cycle in the baths, due to coal and ore. Small impurities captured from water by filter 230 by line 233 enter outlet tray 234 of crusher 235, where ore and coal heated in the baths enter tray 236 by line 237 and line 238. From the outlet chute 234, a mixture of crushed ore and coal with the addition of particles from the filter, goes through line 239 to the pressing press 240, which removes excess water, which returns through pipeline 241 to the bath 220, and the finished mixture enters through pipeline 242 into the vertical shaft 243 of the furnace body.

Part of the water volume, after the condenser 32, is fed into the pipeline 33 and 38, for the operation of the turbines, and the water that was formed as a result of the combustion of hydrogen is collected by the pump 244 and combined with a part of the water flow obtained at the fuel cell moving along the pipeline 245 and having given off part of the heat to the heat exchanger 39, leaving the distribution valve 72. This part of the water in the volume of two thirds is also formed by the combustion of hydrogen at the fuel cell and is not used in the methanol processor for the extraction of hydrogen and carbon dioxide from methanol. Excess water formed during combustion of hydrogen in turbines and in the fuel cell is directed through pipeline 246 through heat exchanger 100 for preheating methane and then into heat exchanger 126 for preheating oil, entering distribution valve 247. From this valve, excess water is directed outside through pipeline 248 at ambient temperature in order to eliminate energy losses from the system located inside the production circuit. Another portion of the water from distribution valve 247 goes through pipeline 249 to distribution valve 250, from where one portion of it goes through pipeline 251 to cool valve 115, from where heated water goes through line 252 to cool support plate 163, from where through Water is sent to pipeline 253 to heat heat exchanger 125, through which oil and heat exchanger 99 are heated, heating the methane flow. Cooling, water enters pipeline 260 to the junction with pipeline 219, through which the water movement cycle was described earlier. Another portion of water from distribution valve 250 moves along pipeline 261, entering distribution valve 262, from where part of the water enters pipeline 164, through which water movement was described earlier. Another portion of water from valve 262 is sent through pipeline 263 to cool heat exchanger 188, where the methane and synthesis gas mixture is cooled, and the heated water returns through pipeline 264 to the junction with pipeline 259, then the water movement cycle is repeated according to the previously presented description.

From separator 137, volatile impurities captured from the gas phase and which are not reused enter separator 266 via pipeline 265 to form plasma and represent a finished product consisting of various gases and non-volatile impurities, entering the Market. From separator 266, each gas or impurity, separately, enters storage tanks 267 via pipelines and is removed from the system, crossing the boundary of the production circuit, at ambient temperature. From separator 137, carbon dioxide leaves via pipeline 268 and accumulates in tank 269, from where it is directed via distribution valve 270 via pipeline 271 to distribution valve 78. Methanol, which is produced inside the system, from storage tank 68 via pipeline 67, via distribution valve 66 is directed outside via pipeline 272 for cooling in heat exchanger 273, leaving the system at ambient temperature via pipeline 274, beyond production circuit 275. Pipeline 274 leaves production circuit 275 of the system, where the energy carrier and separation of the substance are produced. Then pipeline 274 crosses the boundary of consumption circuit 276, where the energy carrier is consumed for energy generation. Immediately upon crossing the boundary of the consumption circuit 276, methanol in pipeline 274 begins to heat up in heat exchangers 277, 278, 279 and enters methanol processor 280.

[37] Hydrogen is produced from methanol together with water in the presence of a catalyst according to the general reaction CH3OH + H2O = CO2 + 3H2 - 49.5 kJ/mol, which is endothermic. Conversion per cycle is 95%, and unreacted feedstock is recycled, according to a scheme similar to that used in the synthesis of methanol from synthesis gas. [38] Fuel cells have 20 times more energy density than lithium-ion batteries, where the efficiency of electricity generation exceeds 80%. For comparison, when burning organic fuel, the average efficiency is only 33.5%. When operating a fuel cell, it is most efficient to use methanol as an energy carrier, as well as to store hydrogen in a liquid compound for an unlimited time, which, if necessary, is converted at any time to extract hydrogen. Extracting hydrogen from other energy sources, such as gasoline, diesel fuel, natural gas requires significantly more energy. For methanol, the conversion of hydrogen requires heating to 275 ° C, and for example, for methane or gasoline, heating above 850 ° C is required. This is due to the fact that methane and gasoline consist of only two chemical elements, carbon and hydrogen, and methanol of three - carbon, hydrogen and oxygen. Therefore, the chemical bonds of methanol are destroyed at a lower energy cost. As shown earlier, chemical compounds and mixtures of chemical compounds, including the largest number of different chemical elements, are divided into simpler chemical compounds with lower energy costs. On the contrary, the combustion of these multicomponent mixtures leads to the smallest release of thermal energy. As an example, the simplest compound methane, which includes two main combustible chemical elements, hydrogen and carbon, releases the largest amount of energy, compared to more complex hydrocarbon compounds. At the same time, methane is inferior in its energy efficiency to hydrogen, since combustion is carried out in a compound of two chemical elements; if the carbon and hydrogen in methane are burned separately, then 20% more thermal energy will be obtained.

[39] Today, methanol and ammonia are increasingly used in the world to store hydrogen in liquid phase compounds, but the latter requires greater energy consumption to extract hydrogen. The greater energy consumption to extract hydrogen from ammonia, as shown above, is due to the fact that ammonia consists of only two chemical elements, nitrogen and hydrogen, in contrast to methanol, which contains three chemical elements: hydrogen, carbon and oxygen.

Water from fuel cell 284 enters the processor via pipeline 281 through distribution valve 282 by means of pump 283. Hydrogen enters the anode of fuel cell 284 via pipeline 285 from the processor, and oxygen enters the cathode via pipeline 286, preheated in heat exchanger 287 from storage tank 288, where air 289 enters from the processor. Air is pumped into the processor from the outside by pump 290, being heated in heat exchanger 291, where air enters via pipeline 292. From the air processor, nitrogen leaves for the market through heat exchanger 277 via pipeline 293, crossing consumption circuit 276 at ambient temperature. From distribution valve 282, a portion of water in the amount of two thirds, not consumed in the methanol processor, is directed to heat exchanger 294 through which passes water heating circuit 295, used for space heating. The water in the circuit moves under the action of the circulation pump 296, passing through the accumulator 297, which is replenished with water through the pipeline 298 and the distribution valve 299, where the water enters through the pipeline 300. From the distribution valve 299, the main part of the water through the pipeline 301 enters the consumption system 302, from which it is pumped out by the pump 303, through the heat exchanger 279, crossing the boundary of the consumption circuit 276 at the ambient temperature, through the pipeline 304. The current generated on the TE 284 enters the inverter 305 and then through the contacts 306 for external consumption, and through the contacts 307, for internal consumption. Methanol processor 280 produces carbon dioxide, which accumulates in tank 308 and then, under the action of pump 309, through heat exchanger 278 and 291 along pipeline 310, sends it for processing. Carbon dioxide crosses the boundary of consumption circuit 276 and enters the production circuit, crossing boundary 275 at ambient temperature.

Carbon dioxide enters the distribution valve 311 via pipeline 310 and then goes to the condenser 32 via pipeline 312 to cool the low-pressure turbine steam. After the condenser, carbon dioxide passes through the heat exchanger 210, 60, 65 via pipeline 175, giving off heat, and enters the distribution valve 174 and then moves according to the previously presented description. Part of the carbon dioxide from the distribution valve 311, depending on the ambient temperature, the steam in the condenser and methanol, in a given volume via pipeline 313, passes through the heat exchanger 273, cooling the methanol to the ambient temperature. Then the carbon dioxide, entering pipeline 175, follows the previously presented description.

The crucible turbine IZ after cooling in chamber 157 opens to extract disk 129, which through the lower lock 314, along line 315 enters into the electrolysis bath 316. The bath is filled with electrolyte and contact 317 is connected to disk 129, which serves as the anode, and contact 318 is fixed on the electrolysis bath and serves as the cathode. After electrolysis, a sediment 319 is formed on the inner surface of the bath, consisting of a mixture of pure metals and sludges containing mainly precious metals, platinum group metals and rare earth metals, which, according to electronegativity is primarily released at the cathode, that is, on the inner surface of the bath.

After electrolysis, sediment 319 is separated from the bath (mechanically, by acid-base method, by melting, etc.) and is sent to the refining limit via line 320, crossing production circuit 275, at ambient temperature. Disk 129 after electrolysis via line 321 is removed from the bath and goes to electrohydropulse crushing, which allows separating the reduced metals from ceramics. For example, from iron compounds including aluminum oxide, magnesium, calcium and carbon. The substance, divided into particles, goes to separation, where it is further separated due to density, magnetic or other properties, entering the Market, crossing production circuit 275, at ambient temperature.

The PDECC method shown in Fig. 5, simultaneously with the reduction of metals and non-metals, allows for the production of large quantities of hydrogen using known methods. For example, in the classic iron-steam method, steam is fed into the device to produce hydrogen, and water vapor is fed into the device to reduce iron from oxides. The disadvantage of the classic iron-steam method is its periodicity, which requires the reduction of iron, which complicates the operation and design of the device, making the method unprofitable.

In case of implementation of the PDECC method, the disadvantages of the classic iron-steam method are eliminated by eliminating its periodicity. When implementing the new method, iron ore, having participated in the implementation of hydrogen production, goes to recovery and melting. To generate a new volume of steam and hydrogen, a new portion of wet ore is constantly supplied to the furnace body. In the classic iron-steam method, hydrogen is contaminated with impurities entering it from water gas, and in the case of using PDECC, the purest hydrogen is produced, since the stage of repeated ore reduction is not used. To determine the possible amount of hydrogen produced from wet iron ore, when implementing the PDECC method, it is necessary to use the statistics of studies on the content of various iron oxides in the ore.

When producing methanol using the PDECC method, which uses ore containing iron oxides, it becomes possible to produce an additional volume of hydrogen using the iron-steam method, and therefore an additional volume of methanol.

[40] According to the “General Chemistry Course,” the iron-steam process occurs at a temperature of 650-700 °C. In this case, iron forms several products that correspond to various degrees of its oxidation, and water vapor, being reduced, decomposes with the release of hydrogen.

[41] According to Doctor of Chemical Sciences I.B. Rapoport, the iron-steam process is carried out within the range of 700 - 800 °C, taking into account that water gas is more expensive than steam, the reduction process is carried out to ferrous oxide, and not to metallic iron, where the steam consumption is 1.75 kg per 1 m3 ^of hydrogen.

[42] The ratio of divalent and trivalent iron in ores is determined by their mineral composition. Determining the ratio between Beg ⁺ and Res ⁺ in ores is of great importance for assessing their quality.

When determining the FeO content in iron ores, a range of 3 to 25% was established, i.e. the average content is 14%. Therefore, in a ton of ore, on average 140 kg of FeO will be oxidized, where the reaction will require 11.7 kg of water. In practice, as shown above, 41% of hydrogen is formed, i.e. 0.54 kg, therefore, the amount of remaining steam 59% will be 6.9 kg.

[43] The oxidation reaction of iron oxide proceeds according to two schemes, at temperatures below 570 °C:

FeO + H ₂ O = Fe ₃ O ₄ + H ₂ + 372 kJ/kg Re and at temperatures above 570 °C:

_FeO + _H2O = _Fe3O4 + _H2 + 497 kJ/kg Fe.

To implement the PDECC process, the hydrogen recovery temperature is taken to be 700 °C, where it is necessary to determine the consumption of thermal energy spent on heating one kg of ore and one kg of water.

[44] The ore contains two oxides, Fe2O3 and FeO, which have different heat capacities, which also increase with increasing temperature. The heat consumed by one kg of Fe2O3 in the range from 0 °C to 700 °C is 533.4 kJ, 418.6 kJ will be spent on heating water from 0 to 100 °C, 2260 kJ will be spent on the phase transition, 1206 kJ will be spent on heating steam from 100 to 700, which in total is 3885 kJ.

For one ton of ore consists of 140 kg FeO and 860 kg Fe2O3, to which 11.7 kg of water are added. Consequently, one kilogram of reagents contains 138.4 g FeO, 850.1 g Fe2O3 and 11.5 g H2O. The required amount of heat required to heat one kg of reagents is FeO - 72.15 kJ, Fe2O3 - 453.44 kJ and, accordingly, for heating water and forming steam 44.68 kJ, which, when heated to 700 °C, will require thermal energy equal to 570.27 kJ.

Taking into account the exothermic reaction, where up to 570 °C 372 kJ is released per kg of iron, and above 570 °C 497 kJ, respectively, an average of 400 kJ is released. Therefore, approximately 170 kJ will be required to heat a kilogram of reagents. When oxidizing FeO with a mass of 138.4 g, theoretically 148.67 grams of FeO4 should be formed, where the mass increase is 10.27 g. In practice, the increase will be only 41%, which is equal to 4.21 g, that is, a mixture of FC3O4 + FeO with a mass of 142.61 g is formed. The solid phase in a kilogram of reagents will be 992.71 g (FeO3 - 850.1 g; FeO4 + FeO - 142.61 g). Considering that 59% of water from 11.5 g will pass into steam, and hydrogen is formed from 41% of water, as a result of the reaction of one kg of reagents, hydrogen weighing 0.505 g and steam of 6.785 g will be obtained. When burning the produced hydrogen, approximately 70 kJ will be obtained, as a result, energy costs within 100 kJ are required to carry out the reaction, at which iron oxides are heated to 700 °C with the formation of steam. Heated substances in the metallurgy section transfer thermal energy to other production sections in the pdeck device.

The production of additional hydrogen obtained by drying the ore during its transportation to the smelting zone, through the reaction of water vapor with the ore, is the most energy efficient and allows for the production of the product in large volumes and at high speed.

It is most expedient to feed wet powder charge into the plasma combustion zone, since the ore drying process typical for agglomeration is eliminated, and when steam is formed during heating, ore oxidation with hydrogen release will occur. In this regard, without drying the ore, hydrogen is produced before the reagents enter the melting zone, forming an additional volume of synthesis gas. The final volume of synthesis gas in the melting process will be produced due to multi-stage reactions involving carbon, methane, oxygen, hydrogen, water vapor and other chemical compounds.

[45] The produced hydrogen is in a mixture of reagents that are moved to melting by plasma, where they are reduced to metals by heating, interacting with oxides. As is known, hydrogen can completely reduce iron in 35 minutes at a temperature of 900 °C. Using this reaction in the PDECC device, it is advisable to reduce iron at the stage of its movement to the melting zone, simultaneously producing an additional volume of hydrogen due to the passage of natural gas through the ore.

The reduced iron particles can serve as centers for catalytic reactions, so it is also advisable to feed natural gas into this zone for its decomposition (dissociation) into hydrogen and carbon. For this purpose, methane (Fig. 5), supplied through pipeline 124, is fed through distribution valve 123 into pipeline 119 and opening 120 for interaction with the ore, which is heated to 900 °C or more, before melting allows methane to dissociate into hydrogen and carbon. The resulting carbon, interacting with the oxygen of the ore, reduces it to iron, forming CO and CO2, and hydrogen, reducing iron, forms water vapor. Water vapor, interacting again with the ore, forms hydrogen, and with methane, with the participation of a catalyst, which is the ore, forms synthesis gas, which is used to produce methanol. The duration of the ore heating and melting process at the PDETSK plant can reach an average of two to twenty hours, therefore, during this time, natural gas completely dissociates into carbon and hydrogen.

Heating one kg of methane requires thermal energy approximately equal to 2415 kJ. The calculation is made for heating the gas, where the temperature of 700 °C is maintained in the charge. The calculation is made taking into account the specific heat capacity of methane, which in the range from 0 to 700 °C, on average equals 3450 J / kg- ° C. The produced hydrogen, due to the dissociation of methane, enters the separator 137 and then into the accumulator 212, from where it can be pressed for the restoration of the charge or for the generation of electricity. The ore, which has undergone preliminary reduction, due to hydrogen and having captured carbon, begins to enter the melting zone, where it is intensively reduced by carbon at a temperature above 1500 °C. It is possible to regulate the feed rate of the charge 121 by changing the rotation speed of the screw mechanism 122, located inside the horizontal shaft. The auger may be used to mix the reagents, accelerating reactions during iron-steam conversion and methane dissociation. During the separation of gas mixtures in separator 137, gas impurities such as sulfur compounds, chlorine, fluorine, phosphorus, etc. are separated, which are captured and collected in separate storage tanks 267 for further use outside, i.e., supplied to the Market, crossing the boundary of production circuit 275 at ambient temperature.

Another part of the synthesis gas is formed due to water vapor separated in separator 137 entering via pipeline 213, under the action of pump 214 through valve 215, via pipeline 216, from where the steam enters through pipe 117 onto mesh catalyst 139, where a mixture of gases and sooty volatile carbon also enters from the furnace. [12] During the endothermic reaction, 74.8 kJ will be absorbed per mole of carbon. A nickel catalyst placed on the surface of magnesium and aluminum oxides is most suitable for carrying out steam conversion of carbon. At the same time, carbon monoxide enters catalyst 139, which also reacts with water vapor. Steam conversion of CO is exothermic, therefore it occurs with the release of heat - 41 kJ / mol, compensating for the loss of heat during steam conversion of carbon. By adjusting in the chamber melting the amount of formed soot carbon, hydrogen, water vapor, carbon monoxide and carbon dioxide, it is possible to carry out autothermal conversion of synthesis gas.

In order to reduce energy consumption in the PDECC unit, during autothermal conversion, it is possible to produce various reaction combinations. [46] For example, for this purpose, it is possible to use mixed conversion of CH4 + H2O + O2, with a combination of two catalysts, as well as conversion of mixtures of CH4 + CO2 + O2 and CH4 + H2O + O2 according to the works. The thermal effect of the process at 800 °C in a mixture of SECSCOg g = 60:16:24 is close to zero, where synthesis gas of the composition 2H2:1CO is produced. As is known, the main difficulty in creating autothermal reactors is associated with the occurrence of reactions at different temperatures, for this it is necessary to separate the space of the reaction zone, but for the PDECC device these difficulties are eliminated in view of the already existing separated space at different temperatures.

The adjustment is carried out by changing the volume of reagents supplied, according to a given program, using an automated control system (ACS). The ACS controls the mechanisms, valve opening, speed and temperature of reagent supply, due to the feedback received when the substance leaves the melting zone, where the quantitative composition of chemical elements, pressure and temperature are determined. All communications in the diagram of the PDETSK device form a closed production circuit, inside which the amount of reagents, temperature and pressure, as well as the amount of energy generated are adjusted, which allows obtaining reduced metal, methanol, electricity, hydrogen and related substances in a solid residue at the output, completely eliminating any harmful emissions. For example, to redistribute steam, if it is necessary to reduce its volume supplied to the furnace, steam from separator 137 is sent through pipeline 218 to heat the ore and coal. The electric power generated by the generator 46 can be directed in three directions, for example, to the inverter 54 through the transformer 48, to start the high-temperature fuel element 45, to the plasma torch 80 or to the terminals 47 in the external network.

Thus, the PDECC process uses reagents with repeating cycles of their processing, controlling their volume according to a given program using an automated control system. Chemical elements that form energy carriers are all processed without exception in a repeating closed cycle.

When implementing the PDECC method, hydrogen is produced not only by iron-steam conversion and by dissociation of methane in solid ore particles, but also by liquid-crystalline pyrolysis of methane. In Fig. 5, the liquid-metal pyrolysis process pyrolysis of methane occurs in two directions. In the first case, when methane is fed into the plasmatron cavity, passing through plasma 85, entering the melt bath 121 from above, and in the second case, when methane is fed through openings 120 and 154, entering the melt bath 121 from below, where liquid metal pyrolysis occurs.

In the melt zone at high temperatures above 2000 °C, dissociation and reduction reactions occur simultaneously, where carbon becomes the main reducing agent for iron, forming CO in the form of a gas flow above the melt bath, triggering the reaction of carbon dioxide conversion of methane, which occurs in the presence of catalysts. Nickel catalysts exhibit the greatest activity in the carbon dioxide conversion of methane, but lose activity during coking. Catalysts where nickel is applied to metal oxides are the least susceptible to the influence of coke. For example, the N1/AI2O3 catalyst has the greatest activity without coking, and the Ni/MgO, Ni/CaO, Ni/MnO, Ni/ZrOi catalysts surpass it in performance, demonstrating resistance to coke formation.

The series of catalytic activity increases from copper to iron, according to experimental data: Fe > Ni > Rh > Ru > Ir > Pd > Pt > Cu. However, in practice, Ni is preferable to Fe, because nickel is less susceptible to coke deposition, and Ru is better than Rh, because ruthenium is cheaper. Industrial use of carbon dioxide conversion of methane is hampered by the low stability of catalysts with respect to coking. In the context of the problem of combating coking, the PDCK method is used, where the ore, being a catalyst, is constantly renewed. During the PDCK process in a wide range, it is possible to regulate the transfer of part of the substance, electricity and heat to various production areas. This allows, depending on the task, at any given time, to produce energy, substance or energy carrier in the required volume.

Hydrocarbon processing, like metallurgy, also requires high energy consumption. Chemical and oil refineries (OR) mainly operate by burning organic fuel. The proposed method of PDECC allows to reduce energy costs by combining metallurgical and chemical processes, where, for example, the processing of hydrocarbons requires the use of catalysts, which are ores from which metals are simultaneously reduced. A certain part of the ore or part of the reduced ore to metals such as iron, aluminum, magnesium, copper and other metals serves as catalysts. In turn, for the reduction of metals in the PDECC installation, reducing agents such as hydrogen and carbon or their compounds are required, therefore, together with ore to carry out reactions, hydrocarbons are supplied. Reducing agents are fed into the melting zone in the form of oil, fuel oil, paraffin, natural gas, coal, shale, peat and other hydrocarbon-containing natural substances.

[16] For example, when processing heavy oil at refineries, it is usually possible to extract no more than 30% of fuel fractions. This is due to the low distillation temperature, which does not exceed 580 °C, as well as the presence of chlorine, sulfur and other substances that reduce the efficiency of the catalysts. When using the PDECC method, where hydrocarbons and water vapor are present in the batch along with metal oxides, there are no restrictions on heating to high temperatures, and there is no possibility of catalyst failure, since their role is played by ores that are constantly renewed. In addition to heavy oil, it is more difficult to process oil residues from refineries using conventional methods, but when using the PDECC device, these residues are used as ordinary ore mixed with hydrocarbons.

The process of processing ore and hydrocarbon raw materials at the PDETSK plant is accompanied by the extraction of metals and non-metals from the reaction products, including the extraction of hydrogen and oxygen, which in this process serve simultaneously as products for the synthesis of energy carriers and as fuel for combustion in the production of energy that supports the melting process and the synthesis of energy carriers.

To improve energy efficiency, the process of processing and synthesizing a new substance is combined with power plants that contain condenser turbo plants and fuel cells. To further improve energy efficiency, losses of substance and energy into the environment are eliminated. The PDECC process of processing a substance is carried out in a closed circuit and combined with the process of consuming an energy carrier in another closed circuit. After processing the energy carrier in the consumption circuit, the carbon dioxide formed during the reaction returns to the production circuit, where at the first stage it serves as a coolant for the power plant condenser, and at the second stage it is processed into an energy carrier. The PDECC method is similar to the process occurring in known shaft furnaces, which include a blast furnace or a Midrex furnace, where metal reduction occurs through carbidization from higher oxides to lower ones. The difference between the PDECC method and known methods of iron reduction is the absence of the agglomeration process, since the charge is ore iron powder mixed with hydrocarbon raw materials. As hydrocarbon raw materials for iron reduction, mountain shale, oil sand, peat, paraffin, heavy oil, bitumen and other similar hydrocarbon substances can be used. The PDECC method does not require fillers in the form of bentonite gluing the particles of the agglomerate, as well as flux reducing the melting temperature. [47] As is known, in ferrous metallurgy, the greatest environmental damage is caused by agglomeration production, where the volume of emissions reaches 52%, and coke production with an emission volume of up to 9%, therefore, the use of a new method will make the process environmentally friendly. For example, the modern blast furnace process produces a significant amount of carbon dioxide emissions and is the most material- and energy-intensive. Therefore, the world is actively searching for new methods that require less energy consumption for blast furnace-free, coke-free and agglomeration-free metallurgy.

[48] To solve this problem, plasma-based methods are increasingly being used. In Russia, the first developments of plasma furnaces were implemented at the Chelyabinsk Metallurgical Plant and the Yuzhuralnickel plant.

In the implementation of the PDECC method for steel production, as in the production of magnesium, aluminum or titanium, plasma is used to reduce iron from ore. During the melting and reduction of the charge consisting of metal oxides and hydrocarbons in the plasma combustion zone, synthesis gas, oxygen, sulfur, water vapor and other chemicals are formed. Synthesis gas must contain two hydrogen molecules per one CO molecule in order to subsequently produce methanol from this composition. Therefore, the PDECC process is designed to maintain a given ratio of molecules for methanol synthesis, extract excess water, oxygen, hydrogen or carbon monoxide from the mixture. Excess hydrogen and oxygen go to the combustion chamber of turbo plants combined with nuclear power plants or to fuel cells to generate heat and electricity.

In the production of methanol, Fig. 5 shows that part of the synthesis gas is extracted from separator 137, carbon monoxide enters the accumulator, distribution valve 202 and is compressed by compressor 203, and hydrogen through distribution valve 199 goes to compression by compressor 198. The resulting mixture of hydrogen and carbon monoxide is combined in the required volume due to pipelines 197 and 204 and then through pipeline 196 enters circulation pipeline 194. The compressor stages are driven by steam turbines, where the steam reaches a pressure of 12 MPa and a temperature of 600°C. Steam for the compressors is supplied through pipelines that are not shown in Fig. 5, due to the heating of water, which cools the equipment located in the sections of metallurgical production, methanol synthesis or energy production. Crusher 235 is also driven by this steam. The other part of the synthesis gas is formed by feeding methane, which cools the furnace body, through pipeline 105, where the heated gas exits through pipeline 106 and is cleaned in filter 107, exits through pipeline 169, combining with the steam flow. Steam is formed due to the flow of water cooling the furnace support plate, where it enters through pipeline 164. The heated steam exits through pipeline 162 and through distribution valve 161 through pipeline 167, enters compressor 168. The mixture of methane and steam enters pre-reformer 109 and, exiting it through pipeline 170, merges with carbon dioxide moving through pipeline 171. The resulting mixture is directed through pipeline 177 to heat the plasma torch and returns through pipeline 178 for compression by compressor 179 and then goes to methanol synthesis. Thus, a scheme for the synthesis of methanol from two streams is created: an external one, where the heating of the reagents occurs due to the cooling of the metallurgical equipment, and an internal one, where the synthesis gas is formed during the autothermal reaction. The volume of methanol produced can be regulated due to two streams, for example, by reducing the volume of the internal stream, increasing the volume of the external stream. Consequently, the specified volume of methanol synthesis will be maintained, regardless of the production of synthesis gas due to the autothermal reaction. For the synthesis of methanol, the circulating gas is heated to 205 - 225 ° C and sent to the synthesis reactor 182, in which the process of methanol formation occurs on the catalyst 183. The temperature of the catalyst layers in the reactor is maintained by introducing colder gas through pipelines 184. The synthesized methanol leaves the reactor through pipeline 186, passing through recuperative heat exchanger 181, and then, cooling in refrigerator-condenser 188, passes into separator 189, collector 70 and methanol storage 68.

In the closed circuit of the PDETSK device, cooled steam or water is returned to closed pipeline lines to produce more heated steam or water, which drive turbines, compressors and mechanisms. The circuit allows heating steam or water to a given temperature by passing it through various pipelines and steam heaters, separating and mixing the steam in the necessary proportions to obtain a given temperature. Excess water produced by burning hydrogen in power plants through pipeline 248 is discharged outside, at ambient temperature.

[49] In Fig. 5, for the implementation of the PDCK process, in the methanol synthesis section, the working scheme of the analog [13] is used, where the unit has a capacity of up to 400 thousand tons per year, and the device uses a pressure of up to 9 MPa. In the general design shown in Fig. 5 of the PDCK device, the device of the apparatus for methanol synthesis is combined with devices for metal melting, energy production and energy consumption. As a result of energy production, division of matter and production of energy carrier with its consumption at the PDETSK plant, energy costs for the implementation of these processes are significantly reduced and become minimal. Energy is not lost to the environment and the total energy costs are divided between all products entering the Market, which include various metals, non-metals, synthesized methanol and energy. As a result, when calculating for a separate product, energy costs are significantly reduced.

The PDETSK method can be used not only for ore recovery and separation, but can be effective in processing any waste. Today, one of the main methods of waste processing is incineration, which significantly reduces the involvement of raw materials in waste in industry. During incineration, up to 90% of the substance is lost, which is released into the atmosphere as gas. The amount of harmful emissions from waste incineration is only half as much as from coal combustion, and toxic soot carbon and nitrogen compounds must be disposed of in solid residues.

When using the PDECC technology, household and industrial waste must be considered as ore mixed with hydrocarbons, which does not need to be separated into components and can be processed according to the above scheme. In order to preserve and reuse all chemical elements contained in the waste, it is necessary to replace the combustion process with a reduction process, i.e., hydrocarbons must be used as a melting medium, where carbon and hydrogen are formed, which are the strongest reducing agents. When heating and melting waste containing hydrocarbons, hydrogen and carbon are formed, as in the reduction of ore raw materials shown in Fig. 5. The proposed PDECC scheme eliminates the process of separating household and industrial waste, which is currently used to isolate a portion of the useful raw materials, which significantly reduces the time and costs of waste processing.

The modern strategy of waste separation into components not only increases the amount of waste due to the use of separate containers, but also requires specialized equipment for each type of waste, which makes all modern recycling methods ineffective. Separation of waste requires additional labor costs, containers, space, transport and equipment for different types of raw materials. Today, all of humanity produces more than 2 billion tons of waste annually, of which only a small part is burned. Consequently, waste disposal requires space, which many countries do not have enough of. At the same time chemical elements that go to waste must be extracted from the earth's interior again for production. Accordingly, humanity is reducing the space of the habitat by developing mines and creating landfills. Therefore, the waste recycling strategy should be revised in favor of a scheme where all waste generated in a certain area is immediately sent for recycling in order to obtain industrial raw materials and produce energy resources. This scheme does not include landfills, incineration plants, or waste separation before recycling them into components.

In connection with the above, it is proposed to use a new technology for waste processing, CCECK, where waste must be presented as ore raw material, which is processed without separation. Waste at the PDECR plant, in the process of heating, melting and evaporation, will be simultaneously separated into different groups by density and properties. As a result of this processing, various petrochemical compounds will be obtained at the output, including methanol, metals, non-metals, gas and other compounds, which will again be sent to industry.

The basic operation diagram of the waste processing plant using the new PDETSK technology is shown in Fig. 6. The waste crosses the production circuit line 275 at ambient temperature, and inside the circuit, water is cooled, which is used to cool the steam in the condenser 32. Industrial waste, which has a similar composition to industrial ore, enters the tank 225 via line 226. Industrial waste is minerals that mainly contain oxygen, which, when processed using the PDETSK method, will serve as a constituent element in methanol and water. Household waste, which contains hydrocarbons, carbon and metals, enters the tank 220 via line 221. Carbon is contained in paper, wood, cardboard, etc., and hydrocarbons contained in plastic serve as a source of hydrogen and carbon, which, when processed using the PDETSK method, will serve as constituent elements in methanol and water. The entire operating diagram is in Fig. 6 with industrial and household waste works similarly to the scheme shown in Fig. 5. Waste consisting of a mixture of household and industrial waste enters a vertical and horizontal shaft, and to move the waste along the horizontal shaft, it is possible to use a screw mechanism or a mechanism such as a piston pushing the substance.

When using the PDETC technology, there is an operation of mixing waste with hydrocarbons supplied through pipeline 124, where oil is located, fuel oil or heavy waste of oil refining with liquid flowability. The addition of hydrocarbons is necessary to maintain the process of PDETSK, if the household waste does not contain enough hydrocarbons in the form of plastic or other products. Waste is fed to the melting zone at once through several shafts, of which there can be two, five, twelve or more. When feeding waste through several shafts, a more uniform alignment of the chemical composition of the charge occurs, where the mixing of the compositions is carried out in the melting zone due to the receipt of waste with different chemical composition in each shaft. The diameter of the crusher and shaft is selected to be larger in area, relative to the storage of the vehicle that delivers household waste for processing. For waste, the diameter of the crusher and shaft will be more than two meters, where any waste can be fed without resistance. In turbine 113, after the melt portion is drained, an ingot is formed, which contains recovered metals and remelted metals found in household waste, such as copper, iron, aluminum, tin, etc. Copper will be concentrated on the outer contour of the ingot, as the densest metal, which contains all the accompanying precious metals. Closer to the center, the ingot contains iron and accompanying metals such as nickel, chromium, cobalt, and then even closer to the center, aluminum and accompanying metals.

The next substances, close to the center of the ring, contain more stable oxides, such as aluminum oxide, magnesium, calcium, and then the lightest solid impurities, such as silicon oxide, silicon and carbon. After the ingot is extracted, further separation of the obtained substances is carried out by known industrial methods, which include electrolysis, crushing, separation, melting and other methods. Otherwise, the processing of household and industrial waste at the PDETSK plant is no different from the processing of ordinary ore with the addition of coal, peat, shale, oil sands, etc.

The technology may be of particular interest for recycling ocean waste, where the contaminated area will soon be comparable to the area of the continent of Australia. For this purpose, the PDETSK unit can be placed on a ship equipped with a nuclear reactor to provide electricity for the PDETSK process. Floating waste containing hydrocarbons will be used as a reducing agent. Floating waste will be collected without separation and sent to a mine under the action of pressing mechanisms for processing in a melting chamber. To create a working charge, fossil ore located near the waste will be added to household waste as a source of oxygen. Sand, clay, pebbles and similar compounds from the seabed are used as this ore. As a result of processing, the following will be obtained: metals, non-metals, methanol and water. When the floating factory operates, the floating garbage islands will be considered as floating mines for mineral extraction.

The block diagram of the operation of the PDETSK device is shown in Fig. 7, including the industrial circuit in a single system with the consumption circuit. The circuits are interconnected by pipelines with an energy carrier and a coolant. Industrial circuit 1 is shown as a large circle, beyond the boundary of which thermal energy is consumed depending on its thermal conductivity. Inside the industrial circuit, at the closest possible distance from each other, there are ring sections of various industries, the boundaries of which intersect, since they use common nodes and are combined for the reuse of each other's substance and energy. Circle 2 denotes the boundary of the energy production section, where primary heat and electric power are produced. The second circle 3 denotes the boundaries of the energy carrier production section, where methanol is synthesized. The third circle 4 denotes the boundaries of the mining and metallurgical production section, where the preparation of the charge, reduction and smelting are carried out. Shaft 5 denotes the input of the substance at ambient temperature for its processing, including the input of ore and hydrocarbons. Water flows, external power lines do not enter the circuit 1 and, if necessary, it is not required to supply air to the circuit, since all components for air production are contained in the processed substance. Thus, the new system can operate underwater or in outer space. The second shaft 6 means the output of the substance at the ambient temperature in the form of finished products for the Market, namely metals and non-metals, including energy carriers and water. Pipeline 7 means the transfer of the energy carrier, and the second pipeline 8 - the return of the coolant at the ambient temperature from the consumption circuit 9. Methanol moves in pipeline 7, and carbon dioxide moves in the second pipeline 8. The block diagram shows that all processes performed within the boundaries of circuit 1 do not bear heat losses due to the transfer of energy to the environment, except for heat losses lost through the circuit boundary. When maintaining the temperature inside the circuit equal to the ambient temperature, these losses are eliminated. Elimination of losses is achieved through the use of heat pumps and heat pipes that collect energy from the outer surface of the circuits, directing the resulting heat to the Stirling engine, which allows for additional generation of mechanical energy that will be used to move matter within the circuits, generate electricity, or increase or decrease the temperature at a given point in space, within the system. The use of heat pumps, heat pipes and Stirling engines inside the production circuit and the consumption circuit to remove low-potential heat from equipment and circuits for its use in internal processes allows for an additional reduction in energy losses and the manufacture of products with energy consumption close to the theoretical energy consumption. The consumption circuit 9, shown as a circle, also loses thermal energy due to the thermal conductivity of the construction material, and when the temperatures inside and outside the circuit are equal, these losses are eliminated. The fourth circle 10 denotes the boundary of the oxygen production section from the air. The fifth circle 11, the boundary of the energy production section, which is advisable to generate using heat energy, to generate the maximum amount of electrical energy, and a turbohydrogen unit is most suitable for generating the bulk of the thermal energy. The sixth circle 12, in Fig. 7, denotes the boundary of the production section of other necessary consumption processes, which include ventilation, cooling, movement of matter, etc. The boundaries of circles 10, 11, 12 also intersect, depicting the use of partially common equipment and the sequential processing of matter and energy, by analogy with the production circuit. Inside the consumption circuit 9, it is advisable to locate not only circles 10, 11, 12, but also sections for deep processing of raw materials. Around or inside the consumption circuit, it is possible to locate sections of various production, including mechanical engineering, metallurgy, chemistry, etc., where energy in the form of heat or electricity is needed, as well as water and carbon dioxide, which are produced in the circuits. For example, carbon dioxide can be consumed in a certain volume by the food industry. Depending on the purpose of the consumption circuit, the necessary substances enter through the third shaft 13, and the reaction products exit through the fourth shaft 14 at ambient temperature. When using the consumption circuit 9, by analogy with a classic thermal power plant, the generated electric power is supplied to the outside via terminals 15, and heat for heating the premises outside the circuit is supplied via the heat pipeline 16. The production circuit can also be used for these purposes, where the outputs of contact 17 and the second heat pipeline 18 are located. The radii Ri, R2, 3, Ш in Fig. 7 show the optimal distance to which it is possible to transmit electric power and heat without significant losses. For a more detailed disclosure of the operation of the block diagram, the mechanism for processing matter and energy is presented below.

The scheme with reprocessing of chemical elements of energy carriers allows more complete processing of reagents in the process of PDECC and their separation into elementary molecules. In particular, carbon is a valuable product for metal recovery, and hydrogen as a valuable reagent for combustion in power plants. Thus, the substance can be fed in a closed-loop cycle to any devices of production areas located inside the production circuit, which includes the area of reagent preparation, metallurgy, methanol synthesis and energy production. Due to this, the system can regulate any specified amount of reagents, including hydrogen, carbon, water, methane, etc., necessary for the reactions that allow producing the optimal amount of reduced metals, non-metals, methanol and electricity. As discussed earlier, for example, methane that has not had time to separate into hydrogen and carbon is captured in separator 137 (Fig. 5), separated from the remaining gases and sent for reprocessing. Due to this, methane is fully utilized in the PDECC process. In the PDECC device, simultaneously with the processes of methane dissociation, processes related to iron-steam conversion, dissociation of carbon dioxide in plasma, dissociation of methane inside the ore, as well as with the participation of the melt, i.e. liquid metallurgical pyrolysis of methane, occur. Simultaneously, processes of iron reduction occur in the sections of ore movement from the moment of getting inside the furnace body to the moment of melting, where the metal is reduced by chemical reactions and with the participation of electrolysis.

The implementation of the PDECC method allows for the complete decomposition of methane into hydrogen and carbon passing through the plasma and melt of the charge according to the liquid metal pyrolysis scheme, which in turn allows the proposed invention to be directed to the production of hydrogen in large quantities. The plasmatron in the PDECC device plays the role of a heater that forms metal melts from the ore, which serve as an effective catalyst for the dissociation of methane passing through the plasma and melt. High plasma temperatures and an effective catalyst allow for the production of hydrogen and carbon in large quantities with the lowest energy costs and at a high speed. In connection with this PDECC method, it is possible to use the PDECC method for the production of hydrogen from methane as the main product, and the production of methanol, metals and non-metals as auxiliary products.

During the reaction, flows containing different amounts of CH2; H2; H2O; CO and CO2 will go to the exit of the furnace, which will continue to react with each other as they move. In this regard, for production, it is necessary to obtain synthesis gas and hydrogen at the exit in the maximum amount with the least cost, which will go to the synthesis of methanol and energy production. With regard to the implementation of the PDECC method, this problem is solved by the proposed PDECC device, where All zones of the above reactions are separated, allowing autothermal conversion of methane into synthesis gas. During the autothermal reaction, metals and non-metals are simultaneously reduced and separated, hydrogen is obtained for the generation of heat and electricity.

Today, when extracting metals from ore, the ore is crushed to a size of approximately 70 microns with subsequent flotation, which allows extracting only part of the useful products. In this case, products containing precious metals and rare earths are removed to waste, which have to be removed to dumps due to the concentration of toxic substances in them, such as arsenic, sulfur, phosphorus, thallium, etc. Using the PDECC method, during melting from the ore through the gas phase, all toxic substances are removed, captured on cooled filters. The melt of reduced metals and oxides is drained and divided into components in a turbine, forming a disk, where all heavy metals, including platinum group metals and all rare earths, accumulate in the outer part. The volatile part of the substance, passing into the gaseous phase, is divided into fractions during condensation due to different boiling points. Volatile substances, which include magnesium, zinc, arsenic, together with synthesis gas form a flow that passes through a filter of falling ore particles on which solid particles, including soot carbon, settle. Then the purified flow enters the rectification columns, where condensation rods are installed in each column, on which the substance with a higher boiling point condenses. Condensation rods, of which there are two or more, are alternately heated, allowing the substance to be drained into crucibles. Condensate from various substances is removed from the crucibles through separators, without stopping the entire process at the PDECC plant. The purified gas flow, which mainly contains synthesis gas and low-boiling impurities, enters the separator through a pipeline.

The gas mixture in the separator is divided into the main gases that participate in the PDECC process and that enter the Market. The proposed method differs from its analogues in that the charge, consisting of ore and hydrocarbons, serves as a catalyst for the synthesis of methanol, and the hydrocarbon products serve as reducing agents for the production of metals. During the autothermal reaction process, there is no need to perform a catalyst recovery operation, since the ore is automatically renewed, which significantly simplifies the process. Maintaining the autothermal reaction during the process is carried out due to the ability to regulate the temperature, pressure and volume of reagents, redirecting them to various production areas of the PDECC device. By selecting the melting time of a given batch volume, batch humidity, methane dissociation degree, reagent quantity and other parameters, it is possible to achieve a mode in which the maximum amount of metal can be restored and the maximum amount of methanol can be synthesized with the least energy consumption. Using the PDECC process, the metals that are restored, which have a higher density during centrifugal separation, will go to the periphery of the ingot, lighter metal oxides will shift closer to the center of rotation, and carbon will be displaced to the inner surface of the ring ingot. In this case, precious metals and heavy metals will concentrate on the outer diameter of the ingot. This reduction scheme allows freezing into the skull, for example, iron without impurities, which are displaced into the melt and then crystallized are separated by density.

The result of the operation of the PDECC device will be the production of a ring ingot containing pure iron, which does not contain carbon, turning it into cast iron. Therefore, the new method does not require additional processing of cast iron into steel. After the crystallization of the ingot, the rotation of the turbine stops and the ingot is removed. Separation of pure metal from heavy and light impurities frozen into its contour is performed by electrolysis, mechanical cutting, crushing or chemical etching. The PDECC method is of particular interest for iron production, since compared to other metals, iron is produced in the world in the largest amount. The annual mass of iron produced reaches two billion tons. At the same time, approximately ten billion tons of auxiliary substances are additionally involved in the iron production process, which must be mined, heated and utilized. In this regard, it is strategically important to reduce energy costs, material intensity and harmful emissions in iron production. For this purpose, it is proposed to reduce iron using hydrocarbon raw materials, which act as a reducing agent and after the reaction is converted into finished chemical products, including methanol. Additional reduction in energy consumption in the production of metals and non-metals, including iron and methanol, is achieved by using hydrogen and oxygen extracted during the separation of the substance as energy carriers producing additional electricity. A significant reduction in energy costs when organizing the process scheme is achieved by using all the heat released at the power plants involved in the separation of the substance, which is spent on heating the reagents supplied to the metallurgical and chemical production. Additional reduction in energy costs is achieved by transferring the energy carrier to the place of consumption at ambient temperature, from where carbon dioxide is returned gas, also at ambient temperature, which at the input to the production circuit functions as a coolant, cooling power plants and then in a heated state entering the synthesis of the energy carrier. At the same time, oxidized and reduced iron, including associated metals, act as a catalyst for the dissociation of hydrocarbons, reducing energy costs during the synthesis of methanol. Therefore, the new steel production process allows for a significant reduction in time and energy costs due to its combination with the process of hydrocarbon dissociation, where methanol and associated substances are formed at the output, and with energy production processes.

To organize the processing of matter by the PDECC method, a source of electricity is needed that does not use the combustion of organic matter in the form of complex compounds, which has a low yield of thermal energy and a high yield of toxic compounds. The most effective sources are nuclear power plants, hydrogen turbine plants and fuel cells, where all the generated electricity and heat are directed to heating, separation and synthesis of matter.

[50] Currently, industrial consumers receive electricity from thermal power plants burning organic fuel via power lines, where its losses range from 15 to 36%. The average efficiency of electricity generation for thermal power plants is 37%, therefore, 63% is lost in the initial stage as heat, which can be used to heat reagents when implementing the PDECC method. When burning organic fuel, an average of 25% of the theoretically possible energy that can be obtained by burning hydrogen and carbon separately is lost. As a result, no more than ten percent of the energy that the fuel is capable of generating reaches the industrial consumer. According to data [6, 7, 40, 41, 42, 43], at power plants, the resistance of cables increases with distance, where losses reach 20%, and the efficiency of energy use, for example, for lighting with an incandescent lamp, at the consumer is only 0.7% of the energy of the primary sources. Therefore, to power a 60 W incandescent lamp, an average of 250 kg of high-quality coal is needed every year. At the same time, to build power lines, it is necessary to destroy forests that utilize carbon dioxide. As a result, the generated electricity is significantly lost, the amount of harmful emissions increases due to the inefficient operation of thermal power plants, and damage is caused to forests. To eliminate these shortcomings, a new scheme for separating matter and synthesizing methanol converts all the electricity and heat generated by power plants into a finished product, some of which is energy carrier and is sent to the consumer via pipelines. Pipelines do not require the cutting of forests and operate more efficiently, allowing any amount of stored energy to be stored. [51] For example, transporting hydrogen via pipelines is four times more profitable than transmitting electricity via power lines. Accordingly, transmitting methanol via pipeline for transporting energy will be at least an order of magnitude more profitable. For more efficient operation of power plants using power lines, when the consumption load changes, costs are required to transmit power over long distances. For this, power lines from one region of the country are looped with another region, which leads to economic costs and losses of electricity. Nuclear power plants, which are designed to operate at a constant load, are especially sensitive to changes in electricity consumption. In this regard, their development in Russia is constrained by a shortage of sources of constant consumption. Today, in the Russian Federation, nuclear power plants generate only 20% of all electricity produced, yielding approximately five times to the number of power plants operating in the United States. When using the proposed invention, where nuclear power plants are used, the situation in the country may change, since these stations may be built in places where hydrocarbons and ore deposits are concentrated, where it is not possible to build hydroelectric power plants and other power plants.

When constructing NPPs in areas where raw materials are concentrated, it becomes possible to ensure their operation at a constant capacity, where additional energy capacity, if necessary, will be produced by using hydrogen fuel obtained from processed raw materials. Thus, a scheme for processing heat and electricity generated by NPPs into metals, non-metals and energy carriers is built. Thus, NPPs convert all generated capacity into a substance, that is, metals, non-metals and energy carriers, which can be stored indefinitely. Today, to produce energy carriers at refineries, such as gasoline, kerosene, diesel fuel, it is necessary to burn up to a third of the extracted hydrocarbon fuel. At the same time, a third of the hydrocarbons, for technical reasons, is not distilled and is lost in the form of heavy fractions, entering the Market at low prices. In the case of using PDECC, all types of hydrocarbon raw materials are processed into finished, high-quality products. The energy carrier in the form of methanol or synthetic oil is accumulated at the production facility and, if necessary, transported to the consumer via pipelines, where hydrogen is extracted from it, with the help of which the necessary energy is produced and carbon dioxide is transported back. When using this scheme, Almost the entire volume of ore and hydrocarbon raw materials will be converted into metals, non-metals and energy carriers, thereby sent to the consumer with a higher profit. Today, oil and gas are sent to the consumer through pipelines, which are used as raw materials in the chemical industry and as an energy carrier. This does not allow the sending state to receive maximum profit. For example, oil is a colloidal solution containing minerals in addition to hydrocarbons. Oil, processed according to the PDECC scheme, is converted into a significantly larger number of products, including metals obtained from it, non-metals, energy carriers, as well as water, which in certain countries can be the most valuable product. Oil products will be produced in a purer form and will have a higher cost. Natural gas processed according to the PDECC scheme will be processed into hydrogen, which, when burned, can produce more energy, and carbon will enter the market as a useful material. An energy carrier in the form of liquid fuel is synthesized from ore and hydrocarbons, which has a market value three times higher than gaseous fuel, since liquid fuel requires significantly less costs for storage and transportation to the consumer.

To determine the advantages of the PDECC process in relation to analogues, a comparison of energy consumption is necessary.

[50] According to the first law of thermodynamics, energy does not disappear and does not reappear, passing from one form to another, where the heat consumption Q is associated with a change in the internal energy AU and the performance of external work L, that is, Q = AU + L. In thermodynamics, the entropy parameter S is used, establishing the relationship between the amount of heat and temperature, which is expressed in J / K, and the energy related to one kg of substance is called specific entropy J / kg-K. The physical meaning of entropy is expressed in the measure of the value of heat, performance and technological efficiency. With an equal amount of heat Q, if the temperature of the coolant is higher than the ambient temperature, the entropy is correspondingly less, therefore the heat can be used more effectively, both for performing work and for other applications, for example, heating and smelting metals, heating, ore preparation, etc. In an isolated system, entropy measures the loss of work, the more the entropy increases, the more energy is dissipated into the environment and is not converted into work. Entropy, as a measure of disorder, the increase of which is associated with an increase in entropy. When heat is supplied, entropy increases, and when the system is cooled and heat is extracted from it, the order of the system increases, and entropy decreases. According to the third law of thermodynamics, disorder and entropy are equal to zero at absolute zero temperature, which is practically unattainable.

In relation to the implementation of the PDECC method, the supply of thermal energy and its conversion is carried out inside the PDECC device, where reagents are supplied to the input at ambient temperature, and products are supplied to the output, also having a temperature equal to the ambient temperature. Consequently, the orderliness of the system increases, and the entropy decreases, making the PDECC process energy-efficient.

[52] During the production of reagents for methanol at the PDECR plant, the amount of synthesis gas changes depending on the thermodynamic parameters of their production. The ratio of CO:H2 in synthesis gas varies from 1:1 to 1:3. By increasing the temperature during the synthesis, it is possible to increase the amount of CO, and by increasing the pressure it is possible to increase the content of H2 and CH4. As is known, synthesis gas is a feedstock for the production of many petrochemical products (methanol, ammonia, oxo synthesis products, Fischer-Tropsch synthesis products). For the production of synthesis gas, they mainly use the interaction of water vapor and methane, which is carried out at elevated temperature (800-900 degrees Celsius) and pressure in the presence of nickel catalysts. The formula for this process is: СШч + Н2О -> СО + ЗН2. To carry out this process using classical methods, a large amount of heat is required, which is obtained by burning a large amount of natural gas with large emissions of carbon dioxide into the atmosphere. This is expensive, leads to the loss of useful substances and has a negative impact on the environment.

When using the proposed technology, PDECC synthesis gas is produced as a by-product of metallurgical and energy production. For this purpose, hydrogen is burned in the energy production section and hydrocarbons are dissociated and metals are reduced in the metallurgical section.

[53] When the plasma torch is operating, the thermal energy generated is several times greater than the energy required to melt the charge. Therefore, it is most efficient to use the released thermal energy simultaneously for the reduction of metals, the production of non-metals and the production of synthesis gas. The heat generated during the generation of electricity must be used to heat the reagents of the charge, reducing energy costs during the reduction of metals. As a result of the operation of the PDETSK unit, a minimum amount of energy will be used in the production of metals, non-metals and the synthesis of methanol. When implementing the proposed method, excess synthesis gas that is not used as an energy source as methanol can be used to synthesize other useful products, which must be carried out within the production circuit. The resulting synthesis gas using PDECR can be sent to the Fischer-Tropsch synthesis, which can be considered as a reaction of reductive oligomerization of carbon monoxide. In general, it is a series of heterogeneous reactions: nCO + 2PN ₂ = (CH ₂ )n + nH ₂ O,

2nCO + nH ₂ = (CH ₂ )n + nCO ₂ .

The reaction products are alkanes, alkenes and oxygen-containing compounds; highly dispersed iron catalysts applied to aluminum, silicon and magnesium oxides, as well as bimetallic catalysts are used as catalysts for the Fischer-Tropsch synthesis: iron-manganese, iron-molybdenum, metals of group VIII: Ru is the most active, then Co, Fe, Ni. When carrying out the PDECC process, ore containing these chemical elements serves as catalysts.

Side reactions of hydrocarbon synthesis from CO and _H2 are:

CO + 3H ₂ CH ₄ + H ₂ O

2СО _СО2 + С

CO + H ₂ O «-> CO ₂ + H ₂

[54] From a mixture of CO and _H2 at high pressure (10-15 MPa), a mixture of oxygen-containing compounds is formed, and when the pressure is reduced to 3 MPa, mainly hydrocarbons are obtained, including gasoline, diesel fuel, paraffin and more complex alcohols.

At the PDECC plant, it is possible to create a wide range of pressure and temperature in order to produce a given chemical product from synthesis gas.

[55] Today, the need to significantly reduce greenhouse gas emissions, including _CO2 , requires not only the development of effective methods for reducing emissions, but also the search for fundamentally new ways of utilizing them. The currently existing methods of burying carbon dioxide in geological formations and injecting it into oil reservoirs to increase intra-reservoir pressure are of limited value and do not allow us to solve the problem as a whole. In this regard, the development of methods for the direct decomposition of carbon dioxide in accordance with the equations seems extremely relevant:

_CO2 <=> CO + 1/ _2O2 (1)

CO <=> C + 1/2O ₂ (2) Thermodynamic calculations and modeling of direct decomposition of carbon dioxide show that the conversion begins at temperatures above 1500°C according to equation (1), at temperatures above >6000 °C, the decomposition of CO into elements begins (equation 2). Using the PDECC method, where the heating temperature can reach 50,000 °C due to plasma, it is possible to convert not only carbon dioxide, but also carbon monoxide. In the PDECC installation, the plasmatron serves as a tool for dissociating carbon dioxide into carbon monoxide and oxygen, and the carbon monoxide processor allows, according to the Boudoir reaction, to again form carbon dioxide with the production of carbon. Therefore, passing carbon dioxide through a closed cycle, depending on the number of passes, its amount will decrease to the required volume with the production of carbon and oxygen.

[56] For the production of hydrogen and oxygen, there is an industrial technology for the electrolysis of chemically pure water, without the use of any additives 4e“

2Н ₂ О —> 2Н ₂ Т +О ₂ ?, but its implementation requires large energy costs. During melting of the charge in the PDETSK installation, the plasma torch operates in the electrolysis mode, immersing itself in the melt bath, so the water vapor in the charge will decompose into hydrogen and oxygen. The latest work on high-temperature electrolysis shows its efficiency, since energy costs are reduced. Accordingly, when implementing the PDETSK method, energy costs during the electrolysis of hydrogen and oxygen from the charge melt, due to the immersion of the plasma torch into the melt, will also be reduced.

[49] Methanol producers believe that it is economically feasible to use a combination scheme for the production of synthesis gas, where, for example, iron production is involved with the usual production of methanol synthesis. During production, carbon monoxide and carbon dioxide are released, which can possibly be used as reagents for the synthesis of methanol. Accordingly, the proposed PDECC technology implements a scheme for combining metallurgy and the chemical industry, proposed by specialists in the field of methanol production.

As is known, the cost of chemical products consists of the costs of raw materials, energy, wages, depreciation, as well as shop and general plant expenses. In recent years, there has been a reduction in the cost of production due to the introduction of large, almost completely autonomous energy units. Therefore, by combining the production of chemical products with the production of metal, due to By using the PDETSK technology, it is possible to achieve greater economic effect.

The reduction of specific capital investments when combining the production of metal and chemical products occurs as a result of reducing the consumption of raw materials, thermal energy, electricity, construction costs, maintenance personnel and reducing costs associated with environmental protection. When using the proposed invention, the cost of production of metals, non-metals, energy carriers, is reduced due to the creation of an energy-closed cycle with maximum use of heat, electricity, reduced loss of chemical reagents, operating and depreciation costs, as well as the total time of production of products.

For practical development of the method, we will give an example of calculating the main parameters of the ore iron reduction process, including the overall dimensions of the structure. Let's assume that the initial weight of iron oxide is 5 tons. Iron will be reduced by the stoichiometric reaction with carbon: 2Fe2O3 + 3C —> 4Fe + 3CO2, where 1 kg of ore requires 112.8 g of carbon. Consequently, the mass of reagents will be 5564 kg. With an ore density of 5.24 t/ ^m3 and a carbon density of 1.8 t/ ^m3, the volume of reagents will be 0.95 ^m3 and 0.31 ^m3 , in total, the volume of the batch will be 1.26 ^m3 . With a horizontal shaft diameter of 0.6 m, the cross-sectional area will be 0.28 m ² , therefore the horizontal shaft filled with this volume of charge will be 4.46 m long. The iron content in the ore is approximately 70%, and the oxygen content is 30%, therefore, 3.5 tons of iron will be reduced, with an iron density of 7.8 t / m ³ , its volume will be 0.45 m ³ . Therefore, the volume of the turbine, where the separation of iron from slag occurs, should be approximately 1 m ³ . With an internal turbine diameter of 2 m, its internal average height will be 0.3 m. When the turbine rotates at a speed of 240 rpm, the maximum gravity coefficient acting on the melt will be 64 units. [48] With a power of 1 MW, the iron melting rate is 21.8 kg / min. Consequently, the melting time of the charge will be 2 hours 40 minutes. To reduce the melting time, it is possible to use a source with a power of 10 MW, therefore, 2018 kg will be melted per minute and the melting time will be 16 minutes. The energy consumption for melting iron, when using electric arc equipment, is 765 Wh/kg.

[57] Theoretically, heating and melting iron from 20°C to 1657°C requires, in terms of energy consumption, no more than 371 W-h/kg, due to exothermic reactions [58], an additional 14% of heat is released. Therefore, in the combustion zone The arc has additional power that can be directed, for example, to the dissociation of methane or other compounds.

[59] Plasma metallurgy is used for the direct reduction of oxide ores and produces a reducing effect when using methane as the plasma-forming gas. Energy consumption in plasma furnaces decreases with increasing plasma torch power. For example, with a power of 0.1 MW, energy consumption for ore smelting is approximately 5 MWh/t, and with a power of 1 MW it decreases to 2.7 MWh/t. The blast furnace process, for comparison, has an energy consumption of approximately 3.6 MWh/t. With an increase in plasma torch power to 10 MW, energy consumption decreases to 0.55 MWh/t, and at 20 MW, respectively, to 0.5 MWh/t.

During the dissociation of methane in the arc combustion zone, hydrogen and carbon will be formed, which reduces metal oxides. In the arc combustion zone, the temperature develops above 2000°C, which, according to the Ellingham diagram [60], corresponds to the reaction of metal reduction by carbon; hydrogen at this temperature does not reduce the metal from the oxide. From the charge in the volume of 1.26 ^m3, 3.5 tons of iron will be reduced and 1.5 tons of oxygen will be released, which will then be synthesized into methanol CH3OH. In accordance with the atomic mass, oxygen occupies half the mass of the methanol molecule, therefore, as a result of the synthesis, 3 tons of methanol will be obtained.

[61] To calculate the cost of raw materials and profit, we assume that the price per ton of ore on the European market is $53/ton (as of February 2019), and the cost of ore at Novolipetsk Iron and Steel Works is $21/ton, approximately RUB 2,830 thousand/ton. Consequently, the cost of ore weighing 5 tons will be RUB 14,15 thousand. [62] The cost of methane with a mass of 0.67 kg/ ^m3 , per cubic meter at this time, is approximately RUB 15. The cost of methane weighing 1.5 tons is approximately RUB 33,56 thousand. Electricity costs for the production of 3.5 tons of iron will be 2303 kW, which at a cost of RUB 4/kW, reaches RUB 9,24 thousand. The total costs of materials and electricity will be RUB 56,95 thousand. An iron ingot weighing 3.5 tons enters the market at a price of 94.5 thousand rubles, where in 2019, a kg of iron costs 27 rubles / kg. 3 tons of methanol will be produced for the amount of 91.5 thousand rubles ($ 396 / t in February 2019). The total cost of iron and methanol will be 186 thousand rubles.

When organizing production, for example, on the basis of the Novolipetsk Iron and Steel Works, where ore costs $21/t or 1.6 rubles/kg, and methane is supplied at a price of 10 rubles per ^m3 , the cost of materials will decrease by more than one and a half times. When organizing the production process iron and methanol by the PDETSK method, thermal energy will be reused, and electricity costs will not exceed 1 rub. / kW. Consequently, the total costs for 3 tons of produced methanol and 3.5 tons of iron will decrease to 33 thousand rubles. Per year, with the smelting of 300 tons of iron per hour and the synthesis of 257 tons of methanol per hour, it is possible to produce 2.63 million tons of iron and 2.25 million tons of methanol using the new technology. At the same time, the costs of raw materials and electricity will amount to 24.8 billion rubles. To the market at prices

In 2019, it is possible to supply iron worth 70 billion rubles, and methanol worth 65 billion rubles, where the total sales per year will amount to 135 billion rubles.

To reveal the energy efficiency of the PDECC method, due to the use of hydrogen in its power plants, a comparison with power plants operating on hydrocarbon fuel is necessary. When burning hydrocarbon fuel, for objective reasons related to the design of power plants and the combustion scheme, part of the released fuel energy is not spent on heating water and generating electricity. The usefully used heat for heating, evaporation and superheating of steam in the boiler, for different types of organic fuel, is different and depends on the heat loss that goes into the pipe, with external cooling of the structure, incomplete chemical and mechanical heat of combustion and with the physical heat of slags.

[63] According to calculations at the most modern thermal power plants, when burning fuel in steam boilers, losses for natural gas are 9.5%, sulfur fuel oil 10.3%, and coal 14%. In addition to these losses, it is necessary to take into account the energy losses that are not released during the combustion of compounds of chemical elements.

For example, when methane is burned, 50 MJ/kg is released, and when hydrogen and carbon in methane are burned separately, 60.25 MJ is released, that is, the energy released in the compound is 20.5% less. In practice, natural gas containing impurities is burned instead of pure methane to generate electricity. [64] The specific heat of combustion of natural gas is on average 45 MJ/kg, which contains [50] CH4 - 94.9%; CnP - 3.8%; CO2 - 0.4%; N2 - 0.9%, where when hydrogen and carbon are burned separately, 59 MJ/kg is released, which is 26.55% more than when natural gas is burned. At modern thermal power plants, for objective reasons, 9.5% of the thermal energy released during combustion of natural gas is not spent on heating water for the turbine, therefore, taking into account the energy that can be extracted during combustion of carbon and hydrogen separately, the total losses amount to 33.5%.

[65] In the world, 24% of energy is produced in terms of oil equivalent from natural gas, 29% from oil, 27% from coal and 10% from biomass. Accordingly, the maximum amount of oil is used for energy production. For combustion in Sulfur fuel oil is mainly used [50], containing 11.8% hydrogen, 85% carbon and 2.5% sulfur, which releases 40.2 MJ/kg. When hydrogen, carbon and sulfur are burned separately, 45.4 MJ/kg is released, which is 12% more.

At modern thermal power plants, when burning fuel oil, 10.3% of thermal energy is not spent on heating water, and accordingly, total losses amount to 21.1%.

[50] When burning brown coal, which contains an average of 71% carbon, 3.15% sulfur and 5.05% hydrogen, 27 MJ/kg is released. When burning combustible chemical elements contained in coal, 30.8 MJ/kg is released separately, which is 14% more. At modern thermal power plants, when burning coal, 14% is not spent on heating water, accordingly, total energy losses reach 26.04%.

[50] When burning peat, which contains 58% carbon, 6% hydrogen, 0.31 sulfur, 33.6% oxygen, 2.5% N2, 8.12 MJ/kg is released, and when combustible chemical elements are burned separately, 27.7 MJ is released, which is 70.6% more. At thermal power plants with objective heat losses of 14%, total energy losses reach 74.7%.

[66] The peculiarity of the efficiency of peat processing is that it is a renewable energy resource, of which there are more than 600 billion tons in the world. The Russian Federation ranks first in peat reserves, containing 200 billion tons and an additional 1 billion tons being formed annually.

[65] World energy production is measured per million tonnes of oil equivalent (Mtoc). In 2021, the Russian Federation produced 1,516 Mtoc of total energy, meaning that the processing of renewable peat produced annually in the country covers 213 Mtoc of the total energy produced.

[50] At power plants, by analogy with peat, combustible shale is used, containing on average 60.5% carbon, 8.5% sulfur, 8.5 hydrogen, 14.5% oxygen and 0.75 N2, which releases 7.66 MJ/kg when burned. When burning separately, the combustible chemical elements contained in shale release 35.13 MJ/kg, which is 78.2% more. At thermal power plants with overall objective heat losses of 14%, the total losses reach 81.25%. Unlike coal, gas, oil and even peat, shale, in addition to oxygen, also contains minerals in the form of metal oxides. Therefore, burning shale without separating it into its constituent combustible chemical elements is especially ineffective. On the contrary, when isolating hydrogen from shale and synthesizing gasoline from it, only 1.75 kg of shale is required per kilogram. One kilogram of shale costs approximately 0.5 rubles, and a kilogram of gasoline costs 81 rubles, which creates a difference of more than 90 times. All of the above fuels, which produce more than 60% of the world's energy when burned today, do not work to their full potential. Natural gas can produce 33.5% more energy, oil 21.1%, coal 26.04%, peat 74.7%, and shale 81.25%.

[65] In 2020, the total volume of electricity production in the world amounted to 26823 TWh, reaching 14500 million tons, in oil equivalent, where the breakdown by energy type is oil - 29%, coal - 27% and gas - 24%. In the world's electricity production through combustion, this is 80%. As is known, coal contains 71% C and 5% H, oil 85% C and 12% Hi, and gas 74% C and 24% Hi. In the total mixture: oil 36.25%, coal 33.75% and gas 30%, therefore, on average, carbon is 77% and hydrogen 13.24%. One kg of average fuel contains 0.77 kg of carbon, which, when burned, will release 25.41 MJ, and hydrogen 0.1324 kg will release 18.8 MJ. Therefore, by burning carbon and hydrogen separately from kg, it is possible to obtain 44.21 MJ, where carbon accounts for 58% of the energy, and hydrogen for 42% of the energy.

Using the new PDECC scheme, approximately ten times less energy will be required to process the same amount of charge. To produce energy, instead of the usual combustion of coal, gas and oil, hydrogen extracted from a mixture of hydrocarbons will be burned, which will change the amount of fuel burned. For example, if today 14,500 million tons of oil equivalent are burned in the world, then due to the use of the new PDECC scheme, only 3,452 million tons will need to be burned, which is four times less, where hydrocarbons will be processed into hydrogen for combustion, and the resulting carbon will go to construction or other industries.

In the generation of electricity, the production of metals and non-metals, as well as energy sources, the scheme completely eliminates carbon emissions

In connection with the above, all types of organic fuel should be processed into more efficient combustible fuel. As is known, for energy generation by combustion, the most efficient use of hydrogen, which can be burned directly before the turbine in the combustion chamber, which eliminates objective heat losses associated with fuel combustion in boilers. Hydrogen turbines are advisable to use for generating large amounts of electricity, which exceeds 5 MW. Hydrogen combustion in fuel cells is especially effective in generating electricity, where the efficiency reaches 85%. It is advisable to use TE to generate electricity up to 5 MW, for example, at local power plants located in various areas of the city. Considering that when hydrogen is burned, water is formed, which today in the world reaches a cost of 50 rub./kg, when used for consumption and household use, the effect of hydrogen combustion increases many times. Thus, it is necessary to create a new fuel combustion scheme, which serves as hydrogen, while simultaneously creating a scheme for the most efficient production of hydrogen with its storage and transportation to the consumer. To produce hydrogen from various compounds, it is necessary to take into account the energy costs for production and the features of this production, which is shown below in the description.

[67] When hydrogen is burned, 3.57 kWh/ ^Nm3 is released, therefore, the same energy is theoretically required to produce hydrogen. To obtain 1 m3 ^of hydrogen by decomposing methane, 0.47 kW/ ^Nm3 of energy is theoretically required.

[14] Theoretically, steam reforming of methane requires 0.78 kWh/ ^Nm3 of energy, but in practice, results within 2.25 kWh/ ^Nm3 have been achieved; theoretically, oxidation of heavy oil requires 0.94 kWh/ ^Nm3 , with 4.9 kWh/ ^Nm3 achieved in practice; theoretically, coal gasification requires 1.01 kWh/ ^Nm3 , but in practice 8.6 kWh/ ^Nm3 .

[68] Hydrogen is weakly bound in the hydrogen sulfide molecule, H2S - 4.82 kcal/mol, compared to the bond in the water molecule, H2O - 57.8 kcal/mol. Consequently, the dissociation of the H2S molecule requires 0.25 kW*h/ ^Nm3 , while in practice 0.95 kW*h/ ^Nm3 is spent.

In the presented table 1 (Fig. 8) it is necessary to pay attention to steam conversion of methane (SCM), where practical energy costs are closest to theoretical ones. This is due to the fact that in the world hydrogen production by the SCM method is the most developed. This reaction shows that hydrogen extraction from a mixture of water and hydrocarbons is more effective than hydrogen extraction from water.

As practice shows, when a large number of various complex compounds containing mixtures of various chemical elements participate in a reaction, separation into simpler compounds will be most effective, since during the division of some substances, others act as catalysts. On the contrary, to produce the maximum possible thermal energy by combustion, it is necessary to use pure fuel, which is hydrogen, consisting of one chemical element. When using various chemical mixtures and compounds as fuel, where the molecules in addition to hydrogen contain, for example, carbon, oxygen, sulfur, phosphorus and other chemical elements, a minimum amount of heat will be obtained.

To determine the energy costs for the recovery of metals from ore, it is necessary to take into account not only their strength in oxides, but also the concentration, that is, the percentage content of the metal being recovered in the ore. [69] To recover metals from oxides, it is necessary to evaluate the oxide strength according to the standard change in Gibbs energy.

[70] The Ellingham diagram predicts the conditions for reducing ore to metal.

The reduction processes, according to the diagram, can be slow. The thermodynamic feasibility of the reaction depends on the change in Gibbs free energy associated with the change in enthalpy and entropy by the equation:

The peculiarity of reducing agents such as hydrogen, carbon monoxide and carbon in the reduction of metals from ore is that up to a temperature of 700 °C the reduction occurs due to hydrogen and carbon monoxide, and above a temperature of 700 °C it occurs due to carbon.

[71] The energy saving effect when using the PDETSK method is achieved by eliminating energy losses that are inevitable when operating classic equipment. For example, the level of thermal energy losses at oil refineries reaches 62%, at power plants up to 70%, and at metallurgical plants up to 80%. By redistributing this energy between production areas within the production circuit of the PDETSK device, to obtain a useful product in the form of metals, non-metals and energy carriers, it is possible to approach the theoretical energy costs for obtaining a particular substance. For example, to produce hydrogen by steam conversion of methane, today 2.25 kWh/ ^Nm3 of hydrogen is required, while the theoretical costs are only 0.78 kWh/ ^Nm3 , which is three times less. Therefore, by reducing energy losses during the operation of metallurgical, chemical, power and other equipment through the redistribution of energy and matter within the production circuit, it is possible to achieve energy consumption when obtaining a product close to the theoretical one.

[18] When using the PDETC method, only hydrogen is burned at power plants producing electricity, due to its highest energy efficiency. As a result of combustion, water is formed, which as a valuable raw material enters the Market, part of the formed water is used as a raw material for the production of energy carriers, while water works as a coolant. Carbon, which is currently burned at thermal power plants, at the PDETC installation is used as a reducing agent for reagents or as a finished product entering the Market. For this purpose, in Fig. 5, a carbon processor 323 is used, where the Boudoir reaction 2CO «-> CO2 + C takes place, from where the carbon enters the accumulator 324 and then goes to the Market. Flake, filiform or lamellar graphite is formed in the accumulator, it is sufficient valuable raw material, which today has a cost on the market exceeding 500 rubles per kilogram. From this carbon, graphite electrodes will be manufactured for the plasmatron, closing the carbon cycle in the PDECC process.

[72] The PDECC method, using plasma, allows extracting a given volume of oxygen and carbon monoxide from carbon dioxide, where it is dissociated according to the reaction CO2 -> CO + 0.5O2. The oxygen obtained in the PDECC device is then used for an autothermal reaction during the formation of synthesis gas, hydrogen combustion or other necessary reactions, and the oxygen is also supplied to the Market in its pure form.

[73] As is known, the minimum theoretical energy consumption for the reduction of iron from the oxide He2O3 is 2.06 kW*h/kg (oxide dissociation energy). In the production of cast iron today, energy consumption is approximately three times greater. High energy intensity in steel production is associated with high energy losses in a large chain of equipment located in a large volume of space.

[74] The total cost of ore mining and iron production averages 11.14 kWh/kg, which is more than five times the energy of oxide dissociation. Total energy costs for copper production today are 25.83 kWh/kg, aluminum 45 kWh/kg, nickel 44 kWh/kg, titanium 111 kWh/kg, silver 806 kWh/kg, gold 1472 kWh/kg. Total energy costs for the production of hydrocarbon products, such as methanol, are up to 13 kWh/kg, polyvinyl chloride up to 23 kWh/kg, polypropylene up to 31 kWh/kg, and carbon fiber up to 195 kWh/kg.

[75] The change in the Gibbs free energy AG is equal to AH = TAS, where AH is the change in enthalpy and AS is the change in entropy, together with the Ellingham diagram show the temperature dependence of the stability of compounds. For example, the oxides of Ag, Cu and Hg are reduced first when heated, followed by the reduction of nickel, iron, zinc, chromium, manganese and silicon. The most difficult to reduce are the oxides of titanium, aluminum, magnesium, beryllium and calcium. High temperature stability of compounds requires high energy consumption in the production of a particular metal. Energy consumption in the production of a particular metal by electrolysis varies and depends on the electrochemical series.

[76] According to the electrochemical series of metal voltages, during electrolysis, gold, platinum group metals, silver, mercury, copper, individual rare earth metals, iron, chromium, and then titanium, aluminum, and magnesium will be restored first. Therefore, when temperature affects metal oxides and due to electrolysis, precious metals are restored first, including gold, silver, platinum, and copper, but in practice, in the production of these metals, today very high energy costs. At the same time, the greatest energy costs are spent on the production of nickel, cobalt and rare earth metals, despite their easier recovery at lower temperatures and due to electrolysis. High energy costs, today, in obtaining these metals are primarily associated with their low content in the ore, therefore, their extraction requires a large chain of enrichment and metallurgical equipment, as well as the involvement of a large number of necessary reagents for production.

When using the PDECC method, metals are extracted from compounds in the ore using a scheme different from the classical schemes. Today, the classical method primarily extracts the main metal from the ore by flotation, separation and enrichment, which is then sent for recovery and remelting. According to the PDECC scheme, all metals in the ore are subjected to plasma melting, followed by electrolysis, gravitational separation, and the resulting ingot is freed from precious metals, rare earths and heavy metals due to separate electrolysis. At the same time, during the melting of metal compounds, hydrocarbons are converted to produce energy sources at the output, which allows the initial stage of metal recovery and separation performed on the PDECC device to be recouped. When copper, platinum group metals and precious metals are extracted from the resulting ingot by electrolysis, the PDECC process additionally pays for itself. Next comes the process of processing less valuable metals and non-metals contained in the ingot, which are significantly larger in volume in the original ore.

Therefore, using the PDECC method, energy consumption in the production of products can be reduced to the theoretical level due to the simultaneous reduction of metals, non-metals and methanol synthesis. For example, energy consumption in the production of iron can be reduced by about five times. For copper, the theoretical energy consumption for oxide dissociation, according to the Ellingham diagram, does not exceed 1 kWh/kg, while the actual costs of copper production are 25 kWh/kg. Therefore, energy consumption in the production of copper by the PDECC method can be reduced by twenty-five times. Even greater energy gain will be achieved in the production of nickel, cobalt, titanium, aluminum and similar metals. For the dissociation of silver and gold oxide, energy costs are required not exceeding 0.5 kWh/kg, while in practice, energy costs in the production of silver are 806 kWh/kg, and gold 1472 kWh/kg. Therefore, when using new technology, energy costs for the extraction and restoration of these metals can be reduced by one and a half to three thousand times. The new method will allow for the synthesis of energy carriers and production of hydrogen, as well as reduce energy costs, bringing them closer to theoretically possible. For example, energy costs for the production of hydrogen at the PDECR plant from methane will be reduced three times.

The advantage of the new technology is the exclusion from the iron production chain of the process of agglomeration, iron smelting, converter processing, vacuumization of steel in separate ladles, and from the chain of methanol synthesis, the process of burning hydrocarbons to produce synthesis gas. For modern industry, the PDECC technology can become the most cost-effective and environmentally friendly, where no more than two kW of electricity will be spent on the production of one kg of iron. Today, 10 kWh of electricity is spent to produce 1 kg of iron in the USA, and 15 kWh in the Russian Federation. The difference in energy consumption is due to the use of electrometallurgy in the USA, and blast furnace production in the Russian Federation. Therefore, using the PDECC method in the Russian Federation for metal production, it is possible to reduce energy costs several times, overtaking the USA, while at the same time significantly reducing the burden on the environment.

[77] According to the percentage content of chemical elements in the earth's crust, oxygen is 47%, therefore, to determine, as a first approximation, the energy costs for the amount of substance found in the reagents of the PDECC process, we adopt three main groups of compounds.

The first group contains compounds of metals and oxygen, for simplicity of calculation in the ratio 50% -^ 50% designated MeO, in the second group are hydrocarbon compounds, presented in the form of the simplest compound CH4 and in the third group are compounds of non-metals, including recycled water designated N. The mass fraction of metal oxides is taken as one kg, where oxygen contains 0.5 kg, during the interaction of which with 0.5 kg of methane, one kg of methanol will be formed. The reaction also involves 0.5 kg of chemicals included in the third group of non-metal compounds, therefore the mass of reagents at the input and output is 2 kg. [59] At 20 MW h of plasma torch power, the energy consumption is 0.5 kW h / kg, therefore, 1 kW h is consumed for 2 kg of reagents during plasma heating.

Reagents at the input: 1 k

0,

2 kg costs 0.5

0,

0,5 кг - N" Reagents at the output: 1 kg - CH ₃ OH + 0.5 kg - Me" +

0.5 kg - N"

One kg of produced methanol contains 12.5% hydrogen, i.e. 125 g of which, when burned, releases 4.93 kW h of energy, where approximately one fifth of the hydrogen in the volume of 25 g will be spent on the production of 1 kW h. When this volume is burned, 225 g of water is formed. Consequently, the synthesis of one kg of methanol, with energy costs approaching theoretical ones, will require 0.5 kW h of energy, and the reduction of one kg of metals will require 0.5 kW h and, accordingly, one kg of non-metals 0.5 kW h.

Thus, in the resulting reaction from one ton of metal-containing ore, one ton of methanol, half a ton of reduced metals and half a ton of non-metals are produced, which include water formed during numerous intermediate reactions. At the same time, to maintain the PDECC process, without the participation of nuclear power plants or renewable power plants, which are required to start and maintain the process, a fifth of the synthesized methanol weighing 0.2 tons will be spent, forming at the output water weighing 0.225 tons, which enters the Market. The PDECC method will be of particular interest to Middle Eastern countries, rich in hydrocarbon raw materials, the processing of which will produce metals, non-metals, energy sources and water needed by these regions.

[78] As is known, in 2018, Russia took sixth place in the world in steel production, falling one position, giving way to South Korea. In 2018, the volume of production in Russia amounted to 71.7 million tons. In the same year, all countries produced 1803 million tons of steel, where Russia took a share of 4% of world production, which is very little for our country. At the same time, Russia has more iron and natural gas reserves than any other country.

In connection with the above, it can be confidently stated that the development of steel production in the Russian Federation is held back by the lack of energy-efficient technology. At the moment, steel in the Russian Federation has to be produced using a blast furnace. The more modern Midrex technology belongs to US metallurgical corporations, so its use in the Russian Federation is limited by licenses, but even in the absence of these restrictions, this technology will not allow Russia to make a qualitative leap in steel production. For comparison, Russian steel sales in 2018 amounted to approximately $ 25 billion, and gas sales were approximately $ 45 billion. When using the new technology PDETSK, possibly increasing steel production by at least ten times, while other metals will be produced at the same time, and instead of supplying gas to the external market, methanol produced on the same equipment will be supplied.

Russia, having the largest reserves of iron ore and natural gas, lags behind China in steel production by fifteen times. To return the leading position in our country, it is necessary to increase the volume of steel production by about twenty times. In this case, using the new PDETSK technology, the Russian Federation will be able to receive profit from the sale of steel and methanol, based on 2018, in the amount of at least one trillion dollars. Today, it is quite difficult for China to maintain the achieved level of steel production. In this country, steel production will be restrained due to the lack of hydrocarbons, ore and the use of old technology. Using the new PDETSK technology and the largest natural resources, Russia will be able to take first place not only in steel production, but also in methanol production. At the same time, the problem of carbon-free footprint will be solved, since the new PDETSK technology does not produce emissions, all gases involved in steel production are used to produce methanol. This will fundamentally change the political position of the country in the world, since the cheapest steel will give impetus to the development of mechanical engineering in Russia. Cheap oil products produced using new technology, such as methanol, diesel fuel, gasoline, plastic and other products, will be able to influence the world market no less effectively. Methanol, which has a low cost price, can be supplied to the external market without building new oil pipelines, since those already built will be enough for this. Steel and methanol will allow a more independent foreign policy and load the Northern Sea Route, pushing out competitors in the common Market. It is possible to increase steel production twentyfold by using the ore reserves of the Kursk Magnetic Anomaly and using the electricity of the Kursk NPP. Natural gas will be required for processing the ore, which is now being exempted from deliveries to the West and passes through pipelines through the Kursk region. Upon reaching this production volume, the sales turnover of steel and methanol at 2023 prices may exceed three trillion dollars. Methanol, compared to gas and liquefied gas, is much easier to store and transport.

In conclusion, it should be noted that with the development of a new technology for processing household and industrial waste, there is an opportunity to significantly reduce the burden on the environment and the possibility of extracting minerals concentrated in landfills. The new technology will allow extracting raw materials for industry in more favorable conditions, since waste accumulations are located near cities. Due to the processing of landfills into industrial raw materials, oil and gas reserves will remain untouched, as well as ore in the depths of the north of Russia, where mining conditions are much more difficult.

It is advisable to place waste processing plants created using the PDETSK technology near cities, additionally using them as thermal power plants and power plants. Unlike waste incineration plants, waste processing plants do not produce emissions, therefore, they can be placed in the center, around which a city can be built. Moreover, this facility can be the center of an industrial zone, which will have metallurgical, chemical and machine-building plants around it, which use materials and energy from the waste processing plant.

Russia is the most suitable for mastering the proposed method, where the technology of building nuclear power plants is developed, a large amount of ore and hydrocarbons is concentrated. When adopting this direction, the number of nuclear power plants in Russia can be increased to the number of nuclear power plants used in the USA, which will allow the entire metallurgical and chemical industry to switch to a scheme without carbon emissions. The consumer will use only hydrogen fuel for combustion, since combustion of fuel containing carbon and its compounds is not economically profitable. Hydrogen production by electrolysis from water is not economically profitable due to higher energy costs. When producing hydrogen from a mixture of water and hydrocarbons, energy costs are reduced, and when adding ore minerals to this mixture using plasma-chemical processes, energy costs are significantly reduced, which makes hydrogen production generally available. In this regard, it is advisable to master the PDECC process, which allows for the simultaneous extraction of hydrogen, metals and non-metals from a charge containing ore, water and hydrocarbons. To extract maximum useful substances from the charge, a nuclear power plant is included in the PDETSK process scheme, where all the generated power is spent on processing the charge into useful products. Hydrogen, as the most efficient fuel, will be accumulated in the form of methanol or synthetic oil as an energy carrier. As is known, 70% of the heat generated by nuclear reactors is discharged into the environment. In the PDETSK operation scheme, this heat is completely used to heat the reagents and reaction products, which increases the efficiency of the nuclear power plant to one hundred percent. Thus, a nuclear power plant integrated into the PDETSK scheme allows for ten times more useful product to be produced than a nuclear power plant transmitting energy to an enterprise located at a great distance. Instead of a nuclear power plant or together with a nuclear power plant The most efficient power plants will operate on renewable energy sources. The energy generated by these power plants will be completely spent on the production of metals, non-metals and energy carriers, which are stored for an unlimited amount of time.

It should be noted that the PDECC method solves the problem of reducing energy costs in the production of metals, non-metals and energy carriers by placing power plants that generate electricity inside the production circuit, together with metallurgical, chemical and other plants. Power plants spend all the generated electricity and heat on the production of the product, allowing it to be produced an order of magnitude more than according to the classical production scheme. Power plants used in the PDECC scheme allow, approximately ten times more raw materials to be processed than conventional power plants located at a significant distance from a particular production, due to the use of all the generated heat and electricity in the processes.

The PDECC method, in addition to using all the energy generated by power plants, allows for reducing energy costs during the separation of interatomic and intermolecular bonds by irradiating the substance with a flow of elementary plasma particles with the simultaneous effect of a high-gravity gravitational field on the separated substance. Energy costs during the separation of compounds by irradiating the substance can also be reduced by an order of magnitude, therefore the PDECC method allows for the same power plant capacity to process ten times more substance, while spending ten times less energy on the division of intermolecular bonds, therefore, the total energy costs, in terms of a unit of production, can be reduced by a hundred times.

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Claims

CLAUSE OF THE INVENTION 1. A method of plasma-arc electrolytic centrifugal conversion (PAECC) for the production of metals, non-metals and energy carriers, consisting in the fact that reagents heated in a crucible, consisting of chemical compounds of metals, ore, hydrocarbons and water, moving along a shaft representing a charge forming a falling stream and further, which melts due to an electric arc burning on electrodes forming a plasma supplied from a power plant, electromagnetic fields, irradiation with flows of elementary particles, electrolysis, dissociation and centrifugal forces of rotation under the action of a crucible turbine, a distillation column, condensation rods, sluice gates, as well as electromagnetic fields of a solenoid, are reduced in a certain volume to metals and slags, forming a board-shaped ingot, with the formation of chemical compounds in the form of gases, which are synthesized in the apparatus into hydrocarbon products, characterized in that before melting, large pieces ores and solid hydrocarbons are crushed in water to small particles and mixed to form a charge, and liquid and gaseous hydrocarbons in stoichiometric composition are added to it before melting, entering the plasma combustion zone, where a melt bath is formed, in which chemical reactions of reduction occur due to carbon, hydrogen and carbon monoxide, which are enhanced by electrolysis, and the resulting gas compounds form a synthesis gas, from which methanol is synthesized in the apparatus, after the reduction of metals, the melt bath in a plasma flow merges in a continuous stream into a rotating crucible turbine, where the produced reagents, under the action of rotation in a high-gravity field, are separated by density, forming an ingot in the form of a disk, ensuring the separation of chemicals throughout its volume, separating them by density, where the reduced metal is displaced to the peripheral surface of the disk, and the slag is displaced to the center of rotation. 2. The method according to item 1, characterized in that the reagents of the charge are fed through a horizontal shaft into the arc and plasma combustion zone, simultaneously being replenished with the reaction products of the preceding melting, as well as gaseous and liquid hydrocarbons, where during movement they dissociate into soot carbon and hydrogen, which reacts with metal oxides and reduces them with the formation of carbon monoxide, which also produces reduction to carbon dioxide, and when entering the melting zone, at the plasma combustion temperature, where the temperature exceeds two thousand degrees Celsius, the reduction of the metal from the compounds is carried out only due to carbon with the formation of carbon monoxide, where hydrogen creates a protective environment preventing the reverse oxidation reaction of the reduced metal, forming synthesis gas together with carbon monoxide, from which the resulting gas mixture is pumped out of the melting zone and sent to the synthesis production section in the methanol apparatus, where the plasma, forming a melt from the reagents, initially burns above the melt bath mirror, and after the formation of a given volume of melt, the plasma with an electrode acting as an anode is immersed in the melt, allowing the electrolysis process to be carried out with a chemical reducing agent for metals and the dissociation of compounds, and then the drained melt is constantly irradiated with elementary plasma particles, allowing the destruction of interatomic molecular bonds of the substance with the least energy costs, the rupture of which is enhanced by the rotation of the melt in the turbine and the effect of a high-gravity field on its substance, where the effect of rupture of interatomic molecular bonds is enhanced by the compression of the melt stream and the plasma flow, the electromagnetic field of the solenoid, while an increase in the intensity of the electromagnetic field leads to compression of the plasma flow and an increase in temperature, which increases the speed of movement of atoms and molecules inside the melt and promotes a more intense rupture of bonds, which transfers the substance to a supercritical high-temperature state, preventing it from evaporating, due to compression by an electromagnetic field, which is maintained in a supercritical high-temperature state and then, under the action of rotation, begins to expand and lose temperature under the action of the kinetic energy of rotation, and chemical elements, due to different densities, begin to separate from each other, creating the effect of high-speed separation, where a denser substance is squeezed out to the periphery of the ingot, and the least dense substance to the center, while the process of zone purification of the melt occurs, where heavy metals crystallize into a skull on the outer diameter, and light slags are displaced into the melt on the inner diameter of the ingot, into the zone of heating of the melt by plasma. 3. The method according to claim 1, characterized in that the transfer of the melt stream substance to a high-temperature state is carried out for the longest period of time in the range of 0.1-10.01 sec. to break the bonds, under the influence of the photoelectric effect created by the flow of elementary particles in a high-gravity field, which is similar to the Ranque effect, allowing simpler substances to be obtained from complex substances, with significantly lower energy costs, while the bonds are broken at some distance from the plasma torch electrodes, not allowing the substance of the electrodes to be affected by ultra-high temperatures, and to obtain ultra-high temperatures in the falling melt stream, which under normal conditions any substance convert into steam, possibly in the area around the jet, increase the compression of the jet with an additional separate electromagnetic field, and also affect it with laser, electron beam, radioactive and microwave radiation. 4. The method according to claim 1, characterized in that the process of reducing metals in the melt bath and obtaining non-metals is accelerated due to the dissociation of substances at elevated temperatures, as well as under the influence of a vacuum, where the reducing agents for metal oxides are solid, liquid and gaseous hydrocarbons mixed into the ore in a stoichiometric composition, which, under the influence of plasma, dissociate into reagents forming synthesis gas, from which methanol is synthesized in the apparatus, where the mineral substance is separated in the crucible due to reduction, and then in the crucible turbine due to the gravitational field of high gravity, forming metals and non-metals including compounds consisting of oxides, carbides, fluorides or nitrides, where the process is designed in such a way that crystallization of pure metal occurs from the melt in one direction, and non-metallic impurities, including gaseous ones, are displaced in the other direction, thereby preventing the reverse reaction of their interaction, and during the reduction and dissociation of metals and non-metals from a mixture of ore and hydrocarbons, the reducing agents for metals are hydrogen, carbon and carbon monoxide formed as a result of the dissociation of hydrocarbons, where for the conversion of hydrocarbons, ores serve as catalysts accelerating reactions and reducing energy costs, while reverse reactions of oxidation of metals are prevented by the release of reducing agents hydrogen, carbon and carbon monoxide 5. The method of plasma-arc electrolytic centrifugal conversion (PAECC) for the production of metals, non-metals and energy carriers, consisting in the fact that the reagents heated in the crucible, consisting of chemical compounds of metals, ore, hydrocarbons and water, moving along the shaft representing the charge forming a falling stream and further, which melts due to the electric arc burning on the electrodes forming a plasma fed from the power plant, electromagnetic fields, irradiation with flows of elementary particles, electrolysis, dissociation and centrifugal forces of rotation under the action of a crucible turbine, a rectification column, condensation rods, sluice gates, as well as electromagnetic fields of the solenoid, are reduced in a certain volume to metals and slags, forming a board-shaped ingot, with the formation of chemical compounds in the form of gases, which are synthesized in the apparatus into hydrocarbon products, including the use in the production process of thermal power plants generating electricity and heat, as well as energy consumption facilities, where through pipelines a substance is supplied and reaction products are returned, characterized in that the process of generating electricity and heat is combined with the process of processing the substance, supplying the substance to the energy consumer in the form of a liquid energy carrier through a pipeline with the return of part of the substance from the consumer in the form of a coolant through a pipeline, forming a closed system of processing the substance and energy, where the reduction and dissociation of metals and non-metals, including the synthesis of methanol, is accelerated and requires significantly less energy due to the simultaneous reaction, separation, synthesis and generation of energy, where for the production of electrical and thermal energy, a combined power plant is used, including the main units of power plants based on nuclear power plants, VTES and TE assembled into a single complex, where the released hydrogen and oxygen from the chemical metallurgical process of processing the substance enters, where it is sent for combustion to generate heat and electricity, in turn, the released heat, electricity and water from the power plant enter the section where the plasma-chemical process is carried out and the section of methanol synthesis. 6. The method according to claim 5, characterized in that the process of energy production and consumption, reduction of metals, non-metals, dissociation of complex compounds into simpler compounds is combined with the process of synthesis of chemical products and preparation of the batch into a single process of energy and substance processing, where the process chains of all production sections enclosed in the production circuit and all sections enclosed in the consumption circuit intersect, which include all the necessary initial components at ambient temperature and from which reagents and reaction products go beyond the circuit boundary, at ambient temperature, where the heat released from any type of production inside the circuit goes to heating the incoming reagents, and the withdrawn cold goes to cooling the steam of power plants and the manufactured equipment, while from the production circuit to the consumption circuit, the energy carrier in the form of methanol enters through a pipeline, going beyond the circuit boundary at ambient temperature, and from the consumption circuit the refrigerant in the form of gaseous carbon dioxide returns, moving beyond the consumption circuit, at ambient temperature, the refrigerant, entering the circuit production, is used to cool the steam of power plants and methanol leaving the production circuit and then heated carbon dioxide goes to the formation of plasma, the synthesis of methanol or dissociation to obtain carbon and oxygen, while at the same time from the incoming reagents the metal is reduced, chemical compounds are synthesized, hydrogen is burned in power equipment, that is, the system operates as a single unit, where the processes are controlled by a computer program with the participation of an automated control system. 7. The method according to claim 5, characterized in that all the released thermal energy due to exothermic reactions, hydrogen combustion and thermonuclear reactions is redistributed within the production circuit for heating the substance, due to heat pipes and heat pumps, where excess heat is converted into mechanical and electrical energy due to Stirling engines, directed to maintaining the arc combustion and the operation of equipment mechanisms, forming a closed production cycle, where as a result, at the output in the form of a product, an annular ingot and new chemical compounds are formed, including methanol, directed to the consumption circuit, for the production of energy, as a result of the conversion of which the coolant is returned back, in the form of carbon dioxide, cooling the power equipment and then entering into reprocessing, for the synthesis of methanol and the production of carbon and oxygen, allowing to bring the energy costs for the output products close to the theoretical energy costs. 8. The method according to paragraph 5, characterized in that the chemical elements included in the energy carrier are included in a circuit with repeated processing, allowing for more complete processing of the reagents and their separation into elementary molecules, where carbon is the main reducing agent for metals, and hydrogen and oxygen are the main reagents for combustion in power plants, thus, these chemical elements enter any devices within the production circuit and the consumption circuit in a circular closed cycle, due to which the system, using a computer program and an automated control system, can regulate any given amount of reagents necessary for the course of various reactions allowing for the production of an optimal amount of metals, non-metals and energy carriers. 9. The method according to paragraph 5, characterized in that simultaneously with the processes of production of metals, non-metals and energy carriers, processes of additional production of carbon and hydrogen associated with iron-steam conversion, dissociation of carbon dioxide in plasma, dissociation of methane inside the ore and in the metal melt due to liquid metal pyrolysis occur, which occur during the movement of the ore, from the moment it enters the furnace body until the moment of melting, which allows for the complete decomposition of methane into hydrogen and carbon, where the dissociation reaction is completed by the passage of methane through the plasma, which allows the process to be used for the primary production of hydrogen and carbon in large quantities. 10. The method according to item 5, characterized in that the plasma acts as a heater, forms melts from the incoming ore reagents, which serve as effective catalysts for the dissociation of the incoming hydrocarbon reagents, allowing them to be divided into simpler compounds with the least energy expenditure, where hydrogen and carbon are simultaneously produced at a high rate, which in turn are reducing agents for metals from the ore, and the plasma also acts as a source of a flow of elementary particles, which, by acting on the interatomic molecular bonds of the substance, destroy them with the least energy expenditure. 11. The method according to paragraph 5, characterized in that during the reaction, gas flows containing different amounts of C; O2; H2; H2O; CO and CO2, which continue to react with each other as they move, where all the zones for carrying out the said reactions are separated, allowing for an autothermal reaction of synthesis gas to be carried out, which is used to synthesize methanol and produce energy, where the batch consisting of ore serves as a catalyst for the division of hydrocarbons for the synthesis of methanol, and the batch containing hydrocarbons, after division into components, serves as reducing agents for the production of metals from ore, where autothermal reactions are carried out during the process, where there is no need to carry out the operation of restoring the catalyst, since the ore is automatically renewed, which significantly simplifies the process, where maintaining an autothermal reaction during the process is carried out due to the ability to regulate the temperature, pressure and volume of reagents, under the influence of a computer program and an automated control system, redirecting the substance to various production areas inside the circuit, accordingly selecting the melting time of a given volume of the batch, humidity, the degree of dissociation of the substance, the amount of reagents and other parameters, it is possible to achieve a mode in which the maximum amount of metal can be restored with the least energy consumption, non-metal and the maximum amount of energy carrier is synthesized. 12. The method according to paragraph 5, characterized in that during melting from the charge through the gas phase, all toxic chemical elements are removed, being squeezed on cooled filters and separated from the melt of the reduced metal with non-metals, which is then drained and divided into components in the turbine, forming a disk, where all heavy metals, including rare earths and platinum group metals, accumulate in the outer part, and the volatile part of the substance, passing into the gaseous phase, is divided into fractions during condensation, due to different boiling temperatures, including magnesium, zinc, arsenic, which together with the synthesis gas form a flow passing through a filter of falling ore particles on which solid particles settle, including soot carbon, then the purified stream enters the rectification columns, where condensation rods are installed in each column, on which the substance with a higher boiling point condenses, the condensation rods, of which there are two or more, are alternately heated, allowing the substance to be drained into separate crucibles, from which the condensate, consisting of various substances, is removed through separators, entering the Market, and the slags are again returned to the repeated melting process, while the purified stream of synthesis gas and low-boiling impurities enters the separator through a pipeline, is separated into the main gases, from where the synthesis gas goes to the production of energy, the separated impurities enter the Market. 13. The method according to claim 5, characterized in that as a result of the work, a ring-shaped ingot is produced containing pure metals, without impurities including carbon, and after the ingot crystallizes and the turbine stops rotating, the ingot is extracted through sluice gates, then the separation of pure metal from heavy and light impurities frozen into its circuit is carried out by electrolysis, mechanical cutting, crushing or chemical etching, where an additional reduction in energy costs in the production of metals and non-metals, including energy carriers, is achieved through the use of hydrogen and oxygen extracted during the separation of matter, burned in power plants, producing additional electricity and heat sent back in the process, while a significant reduction in energy costs is achieved by using all the heat released in power plants to heat the reagents supplied to metallurgical and chemical production, and an additional reduction in energy costs is achieved by transferring the energy carrier to the place of consumption at ambient temperature, from where carbon dioxide is returned, also at ambient temperature, which at the entrance to the production circuit performs the functions of a coolant, cooling power plants and then in a heated state enters the synthesis of the energy carrier or passes through the plasma forming reagents, which also enter the synthesis of the energy carrier or the production of carbon and oxygen, while power plants do not use the combustion of organic matter in the form of complex compounds, which has a low yield of thermal energy and a high yield of toxic compounds, where the power plant is most often a combined complex consisting of equipment of a classic nuclear power plant, a high-temperature thermal power plant and a fuel cell, where only hydrogen is used for combustion as fuel, while the thermonuclear reactor of the nuclear power plant during the process operates at a constant power, which is in the range from 1 to 50% of the total power of the power plant, and the additional power of energy, smoothing out the pulsations inevitable in the results the implementation of the process is carried out by burning hydrogen fuel at the VTES and TE, obtained from the processed raw materials, thus, a scheme for processing heat and electricity generated by the power plant into metals, non-metals and energy carriers is formed, where all the generated energy is converted into a substance representing metals, non-metals and energy carriers that can be stored indefinitely, allowing the processing of all types of ore and hydrocarbon raw materials into finished, high-quality products, where the energy carrier in the form of methanol or synthetic oil accumulates at the production facility and, if necessary, is transported to the consumer through pipelines, where hydrogen is extracted from it, with the help of which the necessary energy is produced and carbon dioxide is transported back, that is, when using this scheme, almost the entire volume of ore and hydrocarbon raw materials is converted into metals, non-metals and energy carriers, which are sent to the consumer and to the Market, with the receipt of higher profits. 14. The method according to paragraph 5, characterized in that hydrocarbons are processed into hydrogen, where, when burning it, they produce the greatest amount of energy, as well as carbon, which enters the market as a useful material, while from the reagents of the batch, consisting of ore, water and hydrocarbons, an energy carrier is synthesized in the form of liquid fuel, which has a cost on the Market three times higher than gaseous fuel, which requires significantly lower costs for storage and transportation to the consumer, and the supply of thermal energy and its conversion is carried out inside the production circuit, where reagents are fed to the input at ambient temperature, and products are fed to the output, also having a temperature equal to the ambient temperature, increasing the orderliness of the system with a decrease in entropy, making the PDECC process energy-efficient, where only hydrogen is burned at power plants producing electricity inside the production circuit, due to its highest energy efficiency, and as a result of combustion, water is formed, which enters the Market as a valuable raw material, and part of the formed water is used as a coolant and raw material for the production of energy carriers, while carbon, which is now burned in classical power plants, is used as a reducing agent for reagents, a finished product entering the Market and as raw material for the production of plasmatron electrodes, for this purpose a carbon processor is used, where the Boudoir reaction 2CO CO2 + C takes place, from where carbon, in the form of flaky, filamentary or lamellar graphite, enters the accumulator, and due to the plasma, a given volume of oxygen and carbon monoxide is extracted from carbon dioxide, where it is dissociated according to the reaction CO2 -> CO + 0.502, then the resulting oxygen is consumed in the autothermal reaction of synthesis gas formation, combustion or other necessary reactions. 15. A plasma-arc electrolytic centrifugal converting (PAECC) device for the production of metals, comprising a consumable plasma torch consisting of a graphite cathode and an anode, a power source, a rectifier, batch reagents including compounds of ore, hydrocarbons and water, reducing agents in the form of solid particles, liquids or gases, a crucible, a crucible turbine, movement lines, a bearing, an electrode holder, a vacuum pump, a batch crusher, a vacuum chamber, horizontal and vertical shafts, a screw, a piston, a branch pipe, a needle, a filter, an accumulator, a rod, a drive, turbine blades, an electrode, a solenoid, an inductor, an electromagnetic field, plasma, a production circuit, a consumption circuit, a condenser, pipelines, contacts, a nozzle, a crucible turbine, a molten bath, power plants, compressors, pipelines including nuclear power plants (NPP), hydrogen thermal power plants (HTPP) and fuel cells (FC), heat pumps (HP), heat pipes (HP) and Stirling engines (SE), compressor, support plate, valve, synthesis apparatus producing chemical products including methanol, characterized in that for melting the reagents a mixture of ore particles and hydrocarbons is created in the form of a charge, which is fed under the torch of the plasma torch through a horizontal shaft, under the end of the central cathode and tubular anode, which are the electrodes of the plasma torch, where an arc is ignited, burning on the inner surface of the electrodes with its rotation, inside which plasma is formed, creating a molten bath to which the anode is closed when immersed, and the melt acts as a cathode, producing electrolysis of the melt, where the negative pole from the rectifier and the power source is connected to the molten bath, and the molten bath after the reduction of metals due to the opening of the valve merges in the form of a stream into a rotating crucible turbine, which is spun by a stream of methane gas, where the falling stream of melt is irradiated by a stream of elementary plasma particles, transferring the melt to a supercritical high-temperature state due to the compression of the stream by the electromagnetic field of the solenoid, then the superheated melt expands and is separated due to the rotation of the crucible turbine, where heavy chemical elements move to the periphery, and light chemical elements to the center of rotation, forming an annular disk ingot, after melting the consumable electrode, the ingot and slag are removed from the disassemblable crucible turbine and the ingot is sent for electrolysis. 16. The device according to claim 15, characterized in that the bottom of the support plate, where the molten bath is formed, is made with a bottom opening in the form of a tapering cone and is closed by a valve for releasing the melt and re-accumulating the freed space with the batch, for re-collecting the molten bath, in which an additional increase in the plasma temperature is produced due to the electromagnetic field of the solenoids, which covers the internal space of the molten bath, allowing for more intensive reduction of metals and dissociation of compounds, affecting the course of chemical reactions and the amount of the reduced, dissociated and synthesized substance that participates in the production of energy and, in the form of methanol as an energy carrier, is sent through a pipeline for processing into the consumption circuit for the production of energy away from the production circuit, from where it is returned from the consumption circuit through a pipeline in the form of a coolant - carbon dioxide, for cooling the production products and re-involving them in processing, and around the released stream of melt, located between the support plate and the crucible turbine, there is a a separate solenoid that creates a more powerful electromagnetic field of influence on the plasma and matter, and also to place lasers, electron beam guns or magnetrons that additionally irradiate the matter with a molten stream. 17. The device according to claim 15, characterized in that the crucible turbine is driven into rotation by a methane gas stream entering the turbine blades fixed on the crucible turbine, making it possible to dispense with the use of a drive and to provide cooling of the crucible turbine and the melt and allowing the methane to simultaneously dissociate into carbon and hydrogen captured by a vacuum pump, where the carbon settles on the falling particles in the vertical shaft and is directed as a reducing agent for the reduction of metals in the melt of the charge, and the hydrogen is directed to the synthesis of methanol, forming with carbon monoxide, which in turn is formed by the fusion of carbon and oxygen due to the reduction of metal oxides, forming synthesis gas, while the melting process is carried out in a vacuum chamber, which is pumped out through a branch pipe by a vacuum pump, accelerating the process of metal reduction and the dissociation of substances, where volatile particles of metal and gaseous reaction products are captured by a filter from the falling particles of the batch and then enter the rectification columns, settling on heated rods and settling in separate crucibles that act as a trap-refrigerator for the condensation and crystallization of metal vapors, including magnesium, zinc, manganese, sulfur, carbon, phosphorus and others, more volatile compounds enter a separator, which separates the substances into different chemical elements. 18. The device according to claim 15, characterized in that a gaseous hydrocarbon reducing agent is fed into the arc combustion zone to form plasma, including methane, ethane, propane or pyrolysis gas, which, upon dissociation in the electric arc into soot carbon and hydrogen, reduce metal oxides, and carbon dioxide is also fed as a plasma-forming gas, which dissociates into carbon monoxide and oxygen, wherein carbon monoxide reduces metals, and oxygen ensures the occurrence of automatic reactions upon interaction with methane, steam and carbon dioxide to form synthesis gas, which is sent to a specialized apparatus where methanol is synthesized, where the heat generated by the synthesis of the exothermic reaction, plasma and hydrogen combustion is directed to heating the reagents and producing steam, to generate electricity, operating compressors and mechanisms, including rotating the charge crusher, wherein the process is completed by forming a disk ingot. 19. The device according to item 15, characterized in that the PDECC circuit is combined into a single system of energy production, smelting, and reduction sections of metals and non-metals, limited within the boundaries of the production circuit, which in turn is connected to the consumption circuit through pipelines with an energy carrier and a coolant, where the energy carrier - methanol is converted into hydrogen from which energy is produced and carbon dioxide, which is returned to the production circuit to cool the reaction products and steam, then heated, goes for reprocessing, including the formation of methanol, carbon and oxygen, forming a single structure and allowing the simultaneous production from the initial ore and hydrocarbon reagents, gaseous reaction products synthesized into methanol and a solid residue in the form of a disk ingot with the simultaneous production of superheated steam used to rotate a steam turbine, a generator producing electricity to maintain the combustion of a plasma electric arc, heating reagents, driving mechanisms and compressors in order to reduce the cost of metal production and non-metals, including energy carriers and coolants, by creating in this scheme a closed energy cycle in the production circuit combined with the consumption circuit, while using nuclear power plants or power plants from renewable energy sources as a starting source of electricity, where the process of producing chemicals becomes the most environmentally friendly and less energy-intensive. 102 20. The device according to item 15, characterized in that it is used as a waste processing plant, where waste crosses the line of the production circuit, at ambient temperature, and inside the circuit, water is cooled, which is used to cool the steam in the condenser, while industrial waste, which has a similar composition to industrial ore, is supplied to the tank with water along one line, being minerals, which mainly contain oxygen in their composition and which, when processed, will further serve as a constituent element in the synthesized methanol and water, and household waste, which mainly contains hydrocarbons, carbon and metals, where carbon is mainly contained in paper, wood, cardboard, etc., and hydrocarbons are contained in plastic, which, when processed, will also serve as constituent elements in the synthesized methanol and water, is supplied along the other line to the tank with water, where the working scheme with the processing of industrial and household waste operates similarly to the scheme, processing ordinary ore and hydrocarbons, where the waste also represents The batch and mixing in the crusher enter the vertical and horizontal shafts, and a screw mechanism or a piston-type mechanism pushing the substance is used to move the waste along the horizontal shaft. 21. The device according to item 15, characterized in that when mixing waste, fossil hydrocarbons are added to the resulting batch, entering the horizontal shaft via a pipeline and mixed into the batch with a screw, liquid hydrocarbons include oil, fuel oil or heavy waste from oil refining, and solid hydrocarbons are fed into the batch in the form of coal, fuel, shale, peat, oil sands, along a line into a bath with water, where industrial waste is loaded and then fed to the melting zone at once through several shafts, of which there may be two or more, where when feeding waste through several shafts, a more uniform alignment of the chemical composition of the batch occurs, where it is produced in the melting zone due to the receipt of waste with different chemical composition in each shaft, and the diameter of the crusher and the shaft is selected to be larger in area, relative to the storage of the vehicle that delivers household waste for processing, after melting and draining a portion of the melt into the turbine, a an ingot containing recovered metals and remelted metals found in household waste, such as copper, iron, aluminum, tin, etc., with copper concentrated on the outer contour of the ingot as the densest metal, which contains all the accompanying precious metals, and then, with decreasing density, all other metals and non-metals, and then the lightest solid impurities, such as silicon oxide, silicon, etc. 103 carbon, onto which steam is supplied through a nozzle to cool the ingot, due to which water gas is formed, which is a raw material for the production of methanol, and after the ingot is extracted, further separation of the obtained substances is carried out by known industrial methods, which include electrolysis, crushing, separation, melting and other methods, while the processing of household and industrial waste is no different from the processing of ordinary ore with the addition of coal, peat, shale, oil sands, etc. 22. The device according to item 15, characterized in that, by analogy with a conventional batch, it can process floating garbage in the oceans, which is household waste and which will be collected without its separation, sent to a crusher for mixing with any soil containing metal oxides, while to create a working batch, fossil ore located next to the garbage will be added to the household waste as a source of oxygen, as this ore, sand, clay, pebbles and similar compounds are mined from the bottom of the sea, which are mixed into household waste, then fed into a mine under the action of pressing mechanisms for processing in a melting chamber, where as a result of processing metals, non-metals, methanol and water will be obtained, and during the operation of the floating factory, floating garbage islands will be considered as floating mines for the extraction of minerals. 23. The device according to item 15, characterized in that the block diagram of the device operation combines the industrial circuit with the consumption circuit into a single system connected to each other by pipelines transmitting energy carriers and refrigerants, where thermal energy is spent outside the industrial circuit and the consumption circuit depending on its thermal conductivity, and inside the industrial circuit, at the closest possible distance from each other, sections of various industries are located, the boundaries of which intersect, since they use common nodes and are combined for the reuse of each other's substance and energy, where primary and secondary heat and electricity are produced, an energy carrier, methanol is synthesized, the preparation of a batch, reduction and smelting are carried out, while the introduction of the initial substance into the circuit is carried out at ambient temperature, while water flows, third-party power lines and air do not enter the circuit, since for the production of water, energy and air, all components are contained in the initial substance, which allows the system to operate under water or in outer space, from where the substance is released at ambient temperature in the form of finished products for the Market, namely metals, non-metals, including energy carriers and water, while the energy carrier is transferred via a pipeline, and the return of the refrigerant is carried out via 104 another pipeline at ambient temperature, where all processes carried out within the boundaries of the circuit do not incur heat losses due to the transfer of energy to the environment, except for heat losses lost through the boundary of the circuit, and when maintaining the temperature inside the circuit equal to the ambient temperature, these losses are eliminated, in addition, to eliminate heat losses, heat pumps and heat pipes are used, collecting energy from the outer surface of the circuits and directing the obtained heat to heat the reagents or to the Stirling engine, which makes it possible to additionally generate mechanical energy that will be used to move the substance inside the circuits, generate electricity or increase or decrease the temperature at a given point in space inside the system, making it possible to further reduce energy losses and manufacture products with energy consumption close to the theoretical energy consumption. 24. The device according to item 15, characterized in that around or inside the production circuit and the consumption circuit, it is possible to place sections of various production, including mechanical engineering, metallurgy, chemistry, etc. production, where the necessary energy in the form of heat or electricity, as well as water and carbon dioxide are generated in the circuits and can be used for the needs of this production, for example, carbon dioxide can be consumed in a certain volume by the food industry, and the use of the consumption circuit is possible, by analogy with a classic thermal power plant, where the generated electric energy is supplied to the outside through terminals, and heat is transferred outside the circuit through a heating pipeline for heating the premises, where the production circuit can be used for these purposes, while the contact outputs and heating pipelines are placed within a certain radius to which it is possible to transfer electric energy and heat without special losses. 25. The device according to item 15, characterized in that it is used near cities as thermal power plants, power plants and waste processing plants that do not produce emissions, therefore, they can be placed in the center, around which a city or industrial zone can be built, which will place metallurgical, chemical and machine-building plants around the circumference, using the substance and energy produced inside the production circuit, which solves the problem of reducing energy costs in the production of metals, non-metals and energy carriers, due to the placement of power plants generating electricity inside the production circuit, together with metallurgical, chemical and other plants, due to the fact that the power plants spend all the generated electricity and heat on the production of the product, allowing it to be produced by an order of magnitude 105 more than in the classical production scheme, this allows, approximately, ten times more raw materials to be processed than conventional power plants located at a significant distance from a particular production, and also allows to reduce energy costs during the separation of interatomic and intermolecular bonds, due to the irradiation of the substance by a flow of elementary plasma particles, with the simultaneous effect on the separated substance of a gravitational field of high gravity, allowing to further reduce energy costs during the irradiation of the substance, which can also be reduced by an order of magnitude, allowing, with the same power of the power plant, to process ten times more substance, while spending ten times less energy on the division of intermolecular bonds, therefore, the total energy costs, in terms of a unit of production, can be reduced by a hundred times.