RU2323351C2 - Method of conversing energy emanating during exothermic process, into mechanical work - Google Patents

Abstract

FIELD: power engineering.

SUBSTANCE: according to method of conversing energy, emanating during process of thermo-chemical reaction, into mechanical work, initial raw material is supplied into first reactor. Components of raw materials interact during exothermic process which results to formation of hydrogen and carbon oxide. Both compositions are supplied into reactor-methanator where working body, namely methane-vapor mixture, is formed due to catalyst reaction. When mixture expands in engine, mechanical work is done. Worked-out working body is sent to re-generation and subsequent supply to first reactor. Initial raw material in first reactor is subject to auto-thermal or thermal gasification to separate hydrogen and carbon oxide, supplied to reactor-methanator from accompanying products. Catalyst reaction between hydrogen and carbon oxide is carried out at temperature of 600K-1400K and pressure of 0,6-20,0 MPa.

EFFECT: improved efficiency of energy conversion process.

8 cl, 7 dwg, 3 ex

Description

The invention relates to energy, and specifically to the conversion of energy released in an exothermic process during the processing of carbon-containing raw materials, including gases, industrial and household waste, with the aim of obtaining commercial energy and / or commercial chemical products on an industrial scale using exothermic cyclic processes by gasification solid or liquid feedstocks, or conversion (reforming) of gaseous hydrocarbon feedstocks, followed by re-gasification or conversion of non-target products and regeneration of the obtained compounds, for their reuse in a cyclic process.

Cyclic processes are well known in nature. These include, for example, the water cycle, the ornithine cycle of vertebrate and invertebrate animals [1, t.3, P.280-281], the industrial production of urea, the nitrous method for the production of sulfuric acid, for domestic and industrial heat supply [1, t. 1, C 785, v. 4, C 647]. At the same time, the energy obtained in cyclic processes, as follows from the prior art, was not previously used to carry out the operation of heat engines, despite the fact that its use would significantly increase the efficiency of the processes as a whole.

The most famous and most common way of obtaining mechanical energy by processing carbon-containing raw materials is to burn them. Combustion is a non-cyclic chemical process in which the transformation of a substance is accompanied by intense energy and heat and mass transfer with the environment. In this case, the conversion of chemical energy into mechanical energy occurs in a heat engine.

Existing heat engines are divided into three main types:

- steam (M.I.Polzunov, 1763, J. Watt, 1774-84) - combustion occurs outside the engine. The chemical energy of combustion is transferred to the water in the boiler unit, the water turns into water vapor (working fluid), which enters the engine, expands and performs mechanical work;

- Stirling engines (R. Stirling, 1816-40) - or external combustion engines. The working fluid (hydrogen or helium) is constantly in a confined space and changes its volume when one of the walls is heated. Heating is due to external combustion of the fuel, and cooling is due to the expansion of the working fluid;

- internal combustion engines (E. Lenoir, 1860) - fuel burns inside the engine. The working fluid is a mixture of combustion products (carbon dioxide, water vapor, nitrogen, etc.) having a high temperature and pressure. The working fluid expands and produces mechanical work.

In all three cases, combustion products are released into the environment, causing serious damage to its ecology.

Known modern methods for producing thermal energy are based either on the direct combustion of solid, liquid or gaseous carbon substances, or on the combustion of gases resulting from the gasification of solid and liquid hydrocarbon fuels, including waste [2-4], or on the combustion of hydrogen.

The disadvantages of these methods, for all their diversity, are of a general nature and are as follows:

- the impossibility of processing waste with a water content of more than 70%;

- theoretical efficiency of the processes of the best heat power plants does not exceed 75%, and effective - 55%;

- combustion products emitted into the atmosphere exacerbate the tense ecological situation in the environment and create problems for the existence of life itself on Earth;

- natural, non-renewable fuel and energy resources are used inefficiently;

- biomass of plants and waste products of humans and animals are used to generate energy occasionally and ineffectively.

The closest to the claimed invention in technical essence and the achieved result when used, is a method of converting chemical energy obtained in a cyclic thermochemical process into mechanical energy, according to which a mixture of hydrogen and carbon monoxide in a molar ratio of 3: 1 is supplied from the tank to the methanator reactor in which during the catalytic reaction a mixture of methane and water vapor (working fluid) is formed and fed to the engine, as a result of expansion of the mixture, mechanical energy is generated and I. The spent methane-vapor mixture is sent to the cooling system of a gas-cooled high-temperature nuclear reactor, where it is converted to the original hydrogen and carbon monoxide, the cycle closes (PCT / NO 2003/000133).

This method allows significantly, in comparison with the known, to increase the efficiency of the energy conversion process, however, it also has the following disadvantages:

- gas-cooled high-temperature nuclear reactor has not yet been created;

To ensure the cyclical nature of the process, an independent, high-temperature source of thermal energy is required, which ensures the occurrence of the endothermic process of steam methane conversion;

- the method can be implemented only in stationary conditions, and in close proximity to a high-temperature energy source;

- the method does not allow the use of other types of carbon-containing raw materials;

- the method does not allow you to create autonomous and transport engines.

The task underlying the claimed invention is to create a method for converting the energy released in the exothermic process during the processing of carbon-containing raw materials, including gases, industrial and household waste, into mechanical work, free from the above-mentioned disadvantages inherent in the aforementioned technical solutions representing a known level technicians.

The technical result achieved during the implementation of the proposed method is to significantly increase the efficiency of the conversion process, while any raw material containing carbon, or raw materials with the addition of carbon or hydrocarbon, the processing of which is economically feasible, and the entire conversion process can be used for processing without emissions of pollutants into the environment.

The task underlying the claimed invention, with the achievement of the above technical result, is solved by the fact that in the known method of converting the energy released in the exothermic process into mechanical work, including supplying raw materials to the first reactor, the interaction of the components of the raw materials in the exothermic process, The result of which is a mixture of gases - a working fluid, during the expansion of which mechanical work is performed in the engine, while part of the spent working fluid directs For regeneration and subsequent supply to the first reactor, in accordance with the invention, any natural or synthetic carbon-containing raw material that is subjected to autothermal or thermal gasification in the first reactor or the conversion of gaseous feedstock to produce hydrogen is used as the feedstock fed to the first reactor and carbon monoxide, which are separated from the by-products and fed into a methanator reactor, in which a methane-vapor mixture is formed during the catalytic reaction - whose body is fed into the engine, which converts the energy of the chemical process into mechanical energy, and the methane-vapor mixture spent in the engine is returned to the first reactor if gas is used as a raw material, or to an additional reactor if solid or liquid raw materials are used, in which the methane-vapor mixture is again converted to hydrogen and carbon monoxide and fed to a methanation reactor;

- and also the fact that as natural or synthetic, carbon-containing raw materials, either carbon dioxide, or carbides and carbonates, or waste, or wastewater is used;

- as well as the fact that the catalytic reaction between hydrogen and carbon monoxide is carried out at a temperature of from 600 K to 1400 K and a pressure of 0.6-20.0 MPa;

- as well as the fact that hydrogen and carbon monoxide released during autothermal or thermal gasification or the conversion of gaseous feeds are separated from related products;

- and also the fact that either a rotary engine, or a piston engine, or a rotary piston engine, or a turbine can be used as an engine;

- as well as the fact that the operation of the said reactors and engine is carried out without the release of gaseous products into the environment;

- as well as the fact that with a small amount of consumed feedstock any given engine power is provided due to the accumulation of hydrogen and carbon monoxide;

- as well as the fact that the engine operation process on the carbon-containing feedstock is carried out without burning this feedstock;

- and also the fact that at a certain temperature determined by the properties of the catalysts, the thermal conversion of spent methane is carried out without oxygen consumption;

- as well as the fact that a plasma torch in the form of a plasma torch is used to gasify aqueous mixtures of carbon-containing raw materials;

- as well as the fact that during utilization of the feedstock, in addition to energy, a given chemical product is produced in an amount corresponding to the content of elements in the processed feedstock.

The proposed method of energy conversion, including cyclic technologies for the processing of hydrocarbon raw materials, is intended for highly efficient production of electric and thermal energy, as well as for highly efficient (from efficiency up to 95%) production of chemical products and energy, in the case of the creation of energy chemical enterprises, without emissions of gaseous products of combustion polluting the atmosphere.

After thermal or autothermal gasification or conversion of the feedstock, the resulting mixture of hydrogen and carbon monoxide, which is the main reagent and energy carrier, is used without burning to produce energy or energy and chemicals due to the catalytic exothermic process of the formation of methane or other compounds.

The resulting methane-vapor mixture or a mixture of other organic compounds, cooled, for example, in an expansion turbine, is again subjected to conversion with the formation of hydrogen and carbon monoxide, thus ensuring the circulation of the energy carrier in the system.

All products resulting from side reactions, products resulting from incomplete gasification, and non-target products obtained in organic synthesis are also re-converted or gasified.

For processing, any, without exception, carbon-containing raw materials or raw materials with the addition of carbon or hydrocarbon can be used, the processing of which is economically feasible (for example, salt water) or necessary for environmental reasons, for example, hospital waste, dead animals, soaked in petroleum products or toxic substances include soil, dumps of coal processing plants, a mixture of water and oil products or other hydrocarbons (with a water content of up to 99.9%), oil sludge, gases and gas mixtures containing coal hydrocarbons and carbon monoxide or dioxide, peat, shale, lignite and coal, asphalt, natural and process gases, petroleum products and crude oil, etc.

The proposed method, in its most general form, is implemented as follows. Solid or liquid raw materials containing carbon or hydrocarbons, is gasified in thermal or autothermal mode by any known method suitable for this type of raw material, and gaseous raw materials are converted (reformed) in order to obtain the maximum amount of hydrogen and carbon monoxide;

- hydrogen and carbon monoxide are separated, if necessary, from related products and undergo (in whole or in part) catalytic conversion (reforming) at a temperature of 600 K to 1400 K and a pressure of 0.6-10 MPa (depending on the type of engine used) with the formation of a methane-vapor mixture;

- related products - gases (except nitrogen), liquids, dust and possibly soot - are sent for re-gasification;

- methane-vapor mixture — the working fluid in the engine — enters the expansion (expander) turbine or other engine and does the work;

- the mixture emerging from the turbine or engine is subjected to steam-oxygen or steam-oxygen-carbon dioxide conversion in an autothermal mode, as a result of which a gas mixture consisting of hydrogen and carbon monoxide is formed again, that is, the cycle closes;

- excess heat energy released in the reactors and supplied to the gas purification and separation unit is utilized in recovery boilers, steam enters the turbines, and hot water enters the heating system;

- in the case of the conversion of some part of hydrogen and carbon monoxide, the non-converted part is sent for the synthesis of the given chemical compounds (methyl and ethyl alcohols, dimethyl ether, alkanes, paraffins, artificial fuel, oils, aldehydes, ethylene, propylene and many others);

- part of the hydrogen and carbon monoxide that did not react during the synthesis and associated non-target products are sent to the reactor for conversion, that is, the cycle closes;

- the separated nitrogen and, possibly, argon, is packed up or, if they are emitted in a small amount, is returned to the environment;

- solid slag is used in the construction of roads or must be disposed of in the prescribed manner.

The proposed method allows you to process any amount of raw materials (from several grams to several hundred thousand tons per day) and can be used to carry out the work of any heat engine of known design (turbines, rotor, piston, rotary piston, etc.), as well as provide work engines on virtually any type of fuel (solid, liquid, gaseous) and / or simultaneously produce chemical products, including clean water, providing consumers with the necessary amount of energy.

Below are examples that are not limitations of the claimed method, but only show a few possible practical implementations of the claimed method.

Example 1

The processed raw materials are natural gas. This is one of the simplest options for implementing the proposed method. Low power plants can be used on vehicles. The process diagram is presented in figure 1. The method is implemented as follows.

Natural gas from the storage or cylinder enters the conversion (reforming) reactor 1, in which the catalytic autothermal vapor-oxygen conversion of natural gas occurs at a temperature of 1100-1372 K with the formation of mainly hydrogen, carbon monoxide and a small amount of carbon dioxide (less than 5 %). The gases formed after purification and separation, or directly from a conversion (reforming) reactor 1, enter a methanator reactor 2, in which a catalytic exothermic reaction between gases takes place to form a methane-vapor mixture. The process is carried out in a known manner at a pressure of from 6 to 10 MPa, while a temperature of about 1400 K develops. For a turbine, the pressure is chosen to be about 10 MPa, for a rotary engine - 6-8 MPa, for a piston engine - 1-5 MPa. The methane vapor mixture (working fluid) enters the engine 3, expands and does the work. The spent mixture again enters the reactor 1 for re-conversion. The cycle closes. With a large amount of processed raw materials, all reactors are equipped with waste heat boilers and additional steam turbines.

Theoretically, this process consumes oxygen, a small amount of water to start the installation, and catalysts that are poisoned during operation and are subject to periodic replacement or regeneration. However, practical operation indicates that there are unintended leaks of up to 0.15% per day. The oxygen consumption for starting the process is 0.5-0.6 m ³ per 1 m ^{3 of} gas (depending on the gas composition), the steam consumption is 0.8 kg per 1 kg of gas. The yield of a mixture of hydrogen and carbon monoxide is 2.84-2.86 kg per 1 kg of methane or about 2.1 m ³ per 1 m ^{3 of} methane in the conversion of CO ₂ that is formed in the system.

Since the methane conversion process is reversible, a mixture of hydrogen and carbon monoxide obtained under stationary conditions (at metallurgical, oil refining, and chemical enterprises) can be used as raw material. A diagram of such a process is presented in figa.

The mixture of gases from the cylinders or storage enters the methanator reactor 2, in which methane is formed, from the reactor 2 the mixture enters the engine 3, and from the engine into the conversion (reforming) reactor 1, in which the methane-vapor mixture (working medium) is again converted into a mixture of hydrogen and carbon monoxide, which are returned to the reactor-methanator 2. The cycle closes.

Calculation of the power of an engine operating according to the method for generating energy shown in the diagrams is performed according to the formula

where N is power, W;

k is the adiabatic exponent;

R is the specific gas constant, J / (kg · K);

T is the absolute temperature of the methane-vapor mixture at the inlet to the engine (turbine), K;

p _I - pressure of the gas mixture at the inlet of the turbine, Pa;

p _o - pressure of the gas mixture at the outlet of the turbine, Pa;

n is the flow rate of the working fluid, kg / s.

The initial data accepted for calculation:

- engine type - turbine;

- p _I = 10 MPa — pressure of the gas-vapor mixture at the turbine inlet;

- p _o = 0.11 MPa is the pressure of the gas mixture at the outlet of the turbine;

- T = 1400 K — temperature of the gas-vapor mixture at the turbine inlet;

- μ _M = 16.04 - molecular weight of methane;

- μ _n = 18.016 — molecular weight of water vapor at T = 1400 K and p = 10 MPa;

- μ _Mn = 17,028 is the molecular weight of the methane-vapor mixture;

- With _{p, n} = 2,620 kJ / (kg · K) - heat capacity at constant pressure of water vapor at T = 1400 K and p = 10 MPa;

- C _{p, M} = 5.251 kJ / (kg · K) - heat capacity at constant methane pressure at T = 1400 K and p = 10 MPa;

- R _Mn = 488.3 J / (kg · K) - specific gas constant of the methane-vapor mixture;

- With _{p, Mn} = 3.857 kJ / (kg · K) is the specific heat at constant pressure of the methane-vapor mixture;

- C _{V, Mn} = C _{p, Mn} -R _Mn = 3.369 kJ / (kg · K) - heat capacity at a constant volume of methane-vapor mixture;

- показатель адиабаты для метанопаровой смеси.-

- adiabatic exponent for methane-vapor mixture.

равна 791 К.Taking a flow rate of n = 1 kg / s, we obtain a power of N = 2.35 MW. For comparison: a turbine running on superheated steam, with the same parameters, has a capacity of 1.95 MW. The exhaust temperature according to the formula:

equal to 791 K.

If the process of catalytic reforming of methane is carried out at temperatures of 1023-1143 K, then at an exhaust pressure of 0.51 to 1.24 MPa, the exhaust gases will have the indicated temperature. In this case, it will not be necessary to consume oxygen and it will be sufficient to limit ourselves to steam catalytic reforming (conversion), because The temperature in the reactor will be provided by the exhaust gases.

After starting the process, only the catalyst that is poisoned during operation will be the consumable. Water vapor and gas will be consumed only to compensate for possible leaks and replenish the system by separating gases not participating in the reaction (nitrogen, argon, etc.).

With the above process parameters and a gas pressure after the turbine of 0.84 MPa, the engine power will be 1.46 MW. The amount of energy released in the process is determined from the reactions:

СО + 3Н ₂ → СН ₄ + Н ₂ О + 206.2 kJ / mol and

CH ₄ + 0.5O ₂ → CO + 2H ₂ +34 kJ / mol.

The total heat input of the process is 12.12 + 2.512 = 14.242 MW. The internal thermal efficiency of the cyclic process in the first case is 0.165.

In the second case (at a power of 1.46 MW), the supplied thermal power is 12.12 MW, and the internal efficiency is 0.12.

. В первом случае он составляет 0,44, во втором - 0,27.The internal efficiency of the Carnot cycle is calculated by the formula:

. In the first case, it is 0.44, in the second - 0.27.

When using a hot water boiler, the capacity will increase by 1,055 MW and the efficiency will be 0.24, and the efficiency of the Carnot cycle - 0.687.

With a large volume of processed gas, the method is implemented according to the scheme shown in Fig. 1b, which is supplemented by a block of synthesis reactors 4 of a given product, waste heat boilers 5-8 with turbogenerators, and conversion reactor 1 and reactor-methanator 2 can have superheaters. Unreacted gases and non-target products are returned for reforming to the reactor 1, possibly through an expansion turbine (not shown in Fig. 1b). At the same time, along with electricity (2.7 kW · h per 1 normal. M ³ gas), at the same time will be produced a given chemical product, for example methyl alcohol, in the amount of 1.015 kg per 1 norm. m ³ gas. The efficiency of the process, determined by the amount of energy contained in the resulting product, is 0.914.

Example 2

Processed raw materials - solid or liquid hydrocarbons or waste containing carbon, hydrocarbons or carbohydrates. The diagram is presented in figure 2, 2A, 2B. The method is implemented as follows.

The raw material after appropriate preparation according to the accepted (known) technology is loaded into a gasifier reactor 9, intended for processing solid or liquid raw materials, in which gasification occurs under the action of steam and oxygen. Slag is unloaded. The resulting gas, which consists mainly of hydrogen and carbon monoxide, as well as hydrocarbons (gases - up to 6-8%, liquids - less than 1%), enters the purification and separation unit 10. The hydrocarbons, dust, and possibly , carbon black, are returned to the gasification reactor 9, and the mixture of hydrogen and carbon monoxide is returned to the methanation reactor 2, in which a catalytic exothermic reaction occurs between the components of the mixture with the formation of a methane-vapor mixture. The methane-vapor mixture is fed into the engine 3, expands and does the job. From engine 3, the spent mixture enters the conversion reactor 1, in which it again turns into hydrogen and carbon monoxide, and then either completely returns to the methanation reactor 2 and the cycle closes, or completely or partially enters block 4, and partially returns to the reactor methanator 2. The presence of a separate conversion reactor 1 allows you to accumulate the reaction mixture and increase the power of power plants with a small amount of processed raw materials. In block 4, the synthesis of the specified organic compounds takes place, which are then shipped to the consumer, and non-target products and purge gases through engine 11 (expansion turbine) go directly to conversion reactor 1. Hydrogen and carbon monoxide obtained in conversion reactor 1 are fed back to the methanation reactor 2 to form a methanopar mixture. The cycle closes.

To make full use of the energy released in this cycle (Fig. 2a), all reactors 1, 2, 9 and the purification and separation unit 10 have recovery boilers 6, and reactor 9 and possibly 2 have superheaters 9 (in Fig. 2a) not shown). Received in waste heat boilers 6 steam is fed into the turbine 12.

In the transport version of the power plant, the process diagrams shown in Fig. 2 are excluded: unit 4, in which the synthesis of organic compounds is carried out, as well as conversion reactor 1, and the methane-vapor mixture from engine 3 goes directly to the gasification reactor 9.

With a large amount of recyclable waste (from several hundred to several thousand tons per day) in the circuit shown in Fig. 2a, it is advisable to install an additional expansion turbine 11, conversion reactor 1 and reactor in order to use the energy of purge gases coming from the unit of synthesis reactor 4 the conversion of gaseous and liquid hydrocarbons 13. In its entirety, a diagram of the implementation of the method in this embodiment is shown in Fig.2b.

Given in this example, one of the possible options for implementing the inventive method allows you to process from several kilograms to several hundred thousand tons of raw materials per day. Depending on the type of processed raw materials, the amount of gas produced varies from 1-1.5 m ³ / kg for low-grade brown coal and household waste, to 3-3.5 m ³ / kg for fuel oil, oil residues and crude oil.

If the method described in the example is used for processing constantly incoming waste, it is necessary either to release chemical products or increase the capacity of the power plant until the amount of processed waste fully compensates for possible losses in the cycle, since otherwise it is impossible to prevent the release of gaseous products into the atmosphere .

The consumption of processed raw materials will be determined by the purity of the circulating reagents and the amount of inert, non-gasifiable components (nitrogen, argon). The power calculation is carried out according to the formula given in example 1. The processed raw material is brown coal. Steam consumption for gasification is 0.5 kg per 1 kg of coal, oxygen consumption is 0.395 kg per 1 kg of coal. The initial data for the calculation:

- the yield of methyl alcohol (methanol) - 0.41 kg per 1 kg of coal;

- enthalpy of coal combustion - 15.85 MJ / kg;

- temperature of the gasification process - 1173 K;

- gasification pressure - 2 MPa;

- the temperature of the methane formation process is 1400 K;

- pressure of the process of methane formation - 10 MPa;

- the pressure of the methanol synthesis process is 8 MPa;

- the temperature at the outlet of the methanol synthesis reactor block is 543 K;

- direct steam pressure - 3 MPa;

- enthalpy of hot steam - 3390 kJ / kg;

- vapor pressure of the intermediate overheating - 2.1 MPa;

- vapor enthalpy of intermediate overheating - 3450 kJ / kg;

- low pressure steam pressure - 1.2 MPa;

- the amount of gas generated during gasification is 1,624 kg per 1 kg of coal;

- the amount of purge gases in the methanol synthesis reactor block is 0.451 kg per 1 kg of coal;

- percentage of gases in gasification products:

hydrogen - 33%, carbon monoxide - 27.9%, carbon dioxide - 14.9%, water vapor - 2.6%, methane - 1.32%, sulfur oxide - 0.1%, nitric oxide - 0.18 %;

- the amount of hot steam to a steam turbine during coal gasification - 0.78 kg per 1 kg of coal;

- the amount of steam intermediate overheating on a steam turbine during coal gasification - 0.70 kg per 1 kg of coal;

- the amount of low pressure steam to a steam turbine during coal gasification - 1.07 kg per 1 kg of coal.

The obtained calculation results:

- the amount of electricity generated by a steam turbine during gasification of 1 kg of coal - 0.58 kWh;

- the amount of electricity generated by the turbine during gasification of 1 kg of coal is 0.69 kWh;

- the total amount of energy generated from gas obtained as a result of gasification of 1 kg of coal - 13.72 MJ;

- energy efficiency of the process - 0.866.

Example 3

Processed raw materials - a mixture of water unsuitable for drinking (salt water; industrial and domestic wastewater, etc.) and any carbon-containing compounds (hydrocarbons; soot; coal dust; peat; shale, lignin; without exception, industrial and household waste; gases, including CO ₂ , etc.). The process diagram is presented in figure 3. The method is implemented as follows.

If the water does not contain organic substances, then it is pre-mixed with crushed solid, or liquid, or gaseous, or with all carbon-containing products at the same time, after which it is dispersed in block 14 and fed by a spray nozzle 15 into the plasma jet of a plasma torch 16 installed in the boiler -reactor 17 (plasma-forming substance - water vapor, CO ₂ or a mixture of CO ₂ with water vapor). The amount of mixture supplied by the nozzle 15 must be such as to provide a temperature of about 2000-3650 K and a pressure of up to 15 MPa in the reaction zone of the reactor boiler 17, depending on the elemental composition of the impurities in the treated water. At this temperature, inorganic substances are melted, precipitated and disposed of. Organic and organometallic substances undergo steam reforming with the formation of carbon monoxide and hydrogen. The resulting gas mixture enters the engine (turbine) 3, and the steam from the reactor boiler 17 to the steam turbine 12. After exiting the engine (turbine) 3 through the steam boiler 6, the gases are separated in the gas separator 20. Carbon monoxide and hydrogen are sent to drive 22 of a given volume. Water vapor is condensed in the water vapor condenser 19 and the water is sent to the water supply and water treatment system in block 21, after which it is supplied to consumers. Nitrogen and argon are sent to storage 23 for subsequent use by consumers.

The receipt of CO and H ₂ in the accumulator 22 of hydrogen and hydrogen oxide occurs continuously, throughout the entire operation of the installation. From the accumulator 22, CO and H ₂ are supplied in predetermined quantities to the methanation reactor 2 and to the synthesis reactor unit 4. From the methanation reactor 2, the methane-steam mixture enters an additional expansion turbine 11, then to the steam boiler 6 or, bypassing it, returns for autothermal conversion to conversion reactor 1, or through a steam boiler 6, bypassing conversion reactor 1, for dispersion into dispersion unit 14. The hydrogen-carbon-oxide cycle is closed. The amount of circulating carbon monoxide and hydrogen is determined by the set power of the energy block, which is calculated based on the needs of the region and the satisfaction of their own needs. From the synthesis reactor block 4, the products are delivered to a warehouse and then shipped to consumers.

In the processing of wastewater and water contaminated with organic substances, the release of chemical organic products is mandatory, since the substances involved in the cycle are theoretically not consumed. When using the method for desalination, only inorganic products can be produced.

The initial data for the calculation:

- the power of the plasma torch with a water flow of 1 l / s - 24.3 MW;

- the amount of heat supplied to the boiler-reactor 17 every second at a burner efficiency of 0.95-22.91 MJ;

- the temperature of water vapor at the entrance to the steam turbine 12 - 1623.2 K;

- steam pressure at the entrance to the steam turbine 12 - 15 MPa;

- steam pressure at the outlet of the steam turbine 12 - 0.11 MPa;

- the amount of heat required to evaporate 1 kg of water and heat 1 kg of water vapor to 1623.2 K - 6.6 MJ;

- engine (turbine) 3 power at a methane-vapor mixture consumption of 1 kg / s - 2.35 MW.

The obtained calculation results;

- the amount of water and steam heated by the allocated heat to a temperature of 1623.2 K - 4.47 kg;

- The total capacity of the turbines is 13.56 MW;

- the amount of heat unused for the production of electricity (enters the heating system) - 10.8 MJ;

- consumption of methane-vapor mixture through the engine (turbine) 3 to compensate for unused heat - 4.6 kg / s

Produced products: distilled water, electricity, thermal energy, inorganic slag, products of organic and inorganic synthesis.

Information sources

1. Chemical encyclopedia. M.: Big Russian Encyclopedia, 1988-1998, t.1-5.

2. Manelis G.B., Polianchik E.V., Fursov V.P. Combustion energy technologies based on the phenomenon of super-adiabatic heating. Chemistry for Sustainable Development, 2000, No. 8, pp. 537-545.

3. Manelis G.B., Fursov V.P., Stesik L.N. and others. The method of processing waste containing hydrocarbons, patent RU No. 2116570 C1, F23G 7/00, 7/05; 1998.

4. Manelis G.B., Fursov V.P., Polianchik E.V. A method of processing combustible solid household waste, patent RU No. 2150045, 1998.

5. Claire A.M., Tyurina E.A. Mathematical modeling and feasibility studies of energy-technological methanol synthesis plants. Novosibirsk: Nauka, 1998 - 127 p.

6. Stepanov B.C. Chemical energy and exergy of substances. Novosibirsk: Nauka, 1990 - 163 p.

7. Gurvich L.V., Karachevtsev G.V. and others. The energy of breaking chemical bonds. Ionization potentials and electron affinity. M .: Nauka, 1974 - 351 p.

8. Vargaftik N.B. Handbook of thermophysical properties of gases and liquids. M .: Nauka, 1972 - 780 p.

Claims (8)

1. A method of converting the energy released in the process of a thermochemical reaction into mechanical work, including supplying the feedstock to the first reactor, the interaction of the components of the feedstock in an exothermic process, resulting in the formation of hydrogen and carbon monoxide, which are fed to a methanator reactor, in which the catalytic reaction is formed by a working fluid - a methane-vapor mixture, during the expansion of which mechanical work is performed in the engine, and the spent working fluid is sent for regeneration and subsequent feeding into the first reactor, characterized in that the feedstock in the first reactor is subjected to autothermal or thermal gasification with the separation of hydrogen and carbon monoxide supplied to the methanator reactor from related products, and the catalytic reaction between hydrogen and carbon monoxide is carried out at a temperature of from 600 to 1400 K and a pressure of 0.6-20.0 MPa. 2. The method according to claim 1, characterized in that either a rotary engine, or a piston engine, or a rotary piston engine, or a turbine is used as the engine. 3. The method according to claim 1, characterized in that the operation of the aforementioned reactors and engine is carried out without the release of gaseous products into the environment. 4. The method according to claim 1, characterized in that with a small amount of consumed feedstock, provide any given engine power due to the accumulation of hydrogen and carbon monoxide. 5. The method according to claim 1, characterized in that the engine operation process on the carbon-based feedstock is carried out without burning this feedstock. 6. The method according to claim 1, characterized in that at a certain temperature determined by the properties of the catalysts, the thermal conversion of spent methane is carried out without oxygen consumption. 7. The method according to claim 1, characterized in that for the gasification of aqueous mixtures of carbon-containing raw materials using a plasma torch in the form of a plasma torch. 8. The method according to claim 1, characterized in that when disposing of the feedstock, along with the energy, a predetermined chemical product is produced.

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