RU2386819C2 - Method of energy conversion with regeneration of energy sources in barchan cyclic process - Google Patents

Abstract

FIELD: power industry.

SUBSTANCE: in energy conversion method with regeneration of energy sources in the cyclic process, non-separated gasification products are supplied to the engine - the first working medium at the expansion of which in the engine the heat and kinetic energy of mixture is converted to mechanical energy, and the first waste working medium cooled in the engine is divided into hydrogen, carbon oxide and by-products if any; at that, separated hydrogen and carbon oxide is supplied to reactor-methanator in which during catalytic reaction there obtained is methane steam mixture - the second working medium which is supplied to the second circuit of the engine or to the other engine where it converts mixture energy during expansion to mechanical energy, and waste methane steam mixture in the engine and by-products are returned to gasification or conversion reactor in which mixture of hydrogen and carbon oxide is obtained again; at that, the cycle is completed.

EFFECT: invention allows reducing fuel consumption for energy generation and increasing efficiency coefficient of the process.

4 cl, 7 dwg

Description

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

Cyclic processes are common in nature and are widely used in industry. These include, for example, the cycle of water and carbon in nature, the restoration of biomass volume [1, v.3, C 280-281], the industrial production of urea, sulfuric acid, absorption and adsorption processes, all kinds of cyclic modes in chemical technology, photochemical processes and many others [1, t.1. C 11-14, C 62, C 785, v. 4, C 647, v. 5, C 715-719]. No less widely used in industry are the processes of regeneration of various substances and materials, for example, recycling of waste paper and worn textiles, redistribution of scrap metal and others.

In the energy sector, the processes of heat recovery and the working fluid of steam turbines are popular. The processes of regeneration of energy carriers (fuels) on an industrial scale are realized only in nuclear energy, however, spent nuclear fuel is partially regenerated at specialized enterprises and then transported to the place of reuse by special vehicles.

At the same time, the energy and substances released in cyclic processes with the regeneration of energy carriers, as follows from the prior art, were not previously used for the operation of heat engines, despite the fact that their use would significantly reduce fuel consumption and increase process efficiency generally.

The most famous and common way to obtain mechanical energy by processing carbon-containing raw materials is to burn it. 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 combustion energy into mechanical energy occurs in a heat engine. The regeneration of energy (fuel) in the engine in the foreseeable future is unpromising.

There is also a method of converting chemical energy obtained in a cyclic thermochemical process into mechanical energy with regeneration of the working fluid of the engine by utilizing the dissipated thermal energy of industrial enterprises (gas hydrates of hydrocarbon gases, hydrides of metals and alloys, hydrogen peroxide) or a source of ionizing radiation (water) or a high-temperature heat source (a mixture of hydrogen and carbon monoxide), according to which a mixture of hydrogen and carbon monoxide in a molar ratio of 3: 1 is supplied from the container in the methanator reactor, wherein a mixture of methane and steam (working fluid) during the catalytic reaction and supplied to the engine, resulting in expansion of the mixture produced mechanical energy. 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, compared with the known ones, to reduce fuel consumption for energy production and increase the efficiency of the energy conversion process, in the case when the engine is an integral part of a nuclear power plant or a technological plant producing a given product, however, it also has the following disadvantages:

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

- to ensure the cyclicity of the process, an independent, high-temperature source of thermal energy is required, which ensures the flow of the endothermic process of steam methane conversion;

- the method can be implemented only in stationary conditions and in the immediate vicinity of 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.

Closest to the claimed method of energy conversion according to the technical essence and the technical result achieved during its implementation is a method of converting the energy released in the exothermic process into mechanical work, including the supply of raw materials to the first reactor, the interaction of the components of the raw materials in the exothermic process, as a result of which hydrogen and carbon monoxide are formed, which are fed to a methanator reactor, in which they form a working medium through a catalytic reaction - meta vapor-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 supply to the first reactor, while 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 K to 1400 K and a pressure of 0.6-20.0 MPa, while the engine is used or a rotary engine, or a piston engine, or a rotary piston engine, or a turbine, and the operation of the aforementioned reactors and the engine is carried out without the release of gaseous products into the environment, and with a small amount of consumed feedstock, they provide any given engine power due to the accumulation of hydrogen and carbon monoxide, and the engine operation process on the carbon-containing feedstock is carried out without burning this feedstock, while at a certain temperature determined by the properties of the catalyst, The spent methane is converted directly without oxygen consumption, and a plasma torch in the form of a plasma torch is used for gasification of aqueous mixtures of carbon-containing raw materials; moreover, when utilizing the raw materials, the desired chemical products are produced along with energy (application for invention of the Russian Federation No. 2005140383/06, IPC F01K 23 / 04, 2005).

In the known technical solution, it was possible to significantly increase a number of technical characteristics, to eliminate the inherent disadvantages of the method, revealed in the process of practical implementation of the invention. However, in the process of converting energy into mechanical work are not used:

- energy and gases released during the conversion or gasification of the feedstock;

- no more than 20% of the energy released in the reactors is used to convert energy into mechanical work;

- to convert energy into mechanical work, the energy and gases released in the synthesis reactors of the target chemical compounds are not used;

- plasmochemical conversion or gasification of raw materials is provided only for the processing of water mixtures and is not intended for the processing of other types of raw materials, although in some cases it eliminates the use of oxygen, additional water, reduces the range and amount of spent catalysts;

- hardware implementation of the method does not provide for the conversion of methane to hydrogen and carbon monoxide in the engine, and the gasification reactor is constantly connected to the engine, which increases the productivity and size of the gas purification and separation unit.

The task underlying the claimed invention is to create a method of converting energy with the regeneration of energy in a cyclic process in 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 above-mentioned technical solutions representing prior art.

The technical result achieved by the implementation of the proposed method is to significantly increase the efficiency of converting the energy of a chemical process into mechanical energy, to reduce the consumption of water, oxygen and catalysts for gasification and gas conversion in the engine circuits.

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 energy with the regeneration of energy in a cyclic process, comprising supplying the prepared raw materials to a gasification or conversion reactor, in which it is gasified or converted into an autothermal or thermal regime with the formation of hydrogen, carbon monoxide and possibly related products, separation of related products when they are formed, feeding the mixture into of hydrogen and carbon monoxide into a methanator reactor, in which a mixture of methane and water vapor is formed - the working fluid, feeding this mixture into the engine with its subsequent expansion and conversion into mechanical energy, in accordance with the invention, the formed inseparable gasification products are fed into the engine - the first the working fluid, during the expansion of which the thermal and kinetic energy of the mixture is converted into mechanical energy in the engine, and the spent and cooled in the engine, the first working fluid is separated into hydrogen, carbon oxide kind and related products, if the latter are formed, while the separated hydrogen and carbon monoxide are fed into the reactor methanator of the engine, where in the catalytic process a methane-vapor mixture is formed - the second working fluid, which is also fed to the second circuit of the said engine or to another engine, where it during the expansion process, it also converts the energy of the mixture into mechanical energy, and the spent methane-vapor mixture and associated products are returned to the gasification or conversion reactor, in which the water-water mixture is again formed kind and carbon monoxide, while the cycle closes;

- and also the fact that the gasification or conversion of the feedstock is carried out in a plasma-chemical or plasma-catalytic mode, while the plasma-forming substance in the plasma-chemical or plasma-catalytic reactor is water or carbon dioxide or a mixture of water with carbon dioxide;

- and also by the fact that in the mixture of hydrogen and carbon monoxide, as well as methane and water vapor, a noble gas or a mixture of noble gases are added to utilize the excess thermal energy.

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 (with efficiency up to 95%) production of chemical products and energy, in the case of the creation of energy-chemical enterprises, without emissions of gaseous polluting products 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, and then is regenerated by the formation of methane or other compounds in a catalytic exothermic mode.

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.

Any organic or inorganic carbon-containing raw materials or raw materials with the addition of carbon or hydrocarbon, the processing of which is economically feasible, for example, salt water, or is necessary for environmental reasons (hospital waste, corpses of sick animals, impregnated with oil products or toxic soil, dumps of coal processing plants, a mixture of water and oil products or other hydrocarbons, oil sludge, gases and gas mixtures containing coal odorody and oxide or carbon dioxide, peat, shale, peat and coals, bitumen, natural and industrial gases, carbonates, petroleum, crude oil, etc.

The proposed method, in its most general form, is implemented as follows. Pre-prepared solid or liquid raw materials containing carbon or hydrocarbons are 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;

- formed undivided gasification products - the first working fluid, is fed into the engine, where they expand, converts the thermal and kinetic energy of the mixture into mechanical energy;

- spent and cooled in the engine, the first working fluid is divided into hydrogen, carbon monoxide and related products, if they are formed;

- hydrogen and carbon monoxide are fed to a methanator reactor, where they 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 methane-vapor mixture;

- the resulting methane-vapor mixture — the second working fluid — is fed into the second circuit of the aforementioned engine or into another engine, where it expands and converts the thermal and kinetic energy of the incoming mixture into mechanical energy;

- the spent methane-vapor mixture and associated products - gases (except nitrogen), liquids, dust, and possibly soot - are returned to the gasification or conversion reactor, in which the gas mixture again consists of hydrogen and carbon monoxide, that is, the cycle closes;

- excess heat energy released in the reactors and supplied to the gas purification and separation unit is utilized in waste heat boilers, steam enters the turbines, and hot water enters the heating system (in some cases it is advisable to add noble gases or mixtures of noble gases to the working fluid, heating which reduces the temperature of the working fluid at the engine inlet);

- 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);

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

- the separated nitrogen is packed up or, if it is emitted in a small amount, is returned to the environment;

- solid vitrified slags are used in construction or must be disposed of in the prescribed manner.

- in large-capacity plants, for a more complete conversion of the energy released in reactors into mechanical energy, steam of low-boiling liquids obtained in steam boilers or heat exchangers built into reactors and gas separation units can be used as working fluids in engines.

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 of the many possible practical implementations of the claimed method.

Example 1

Processed raw materials - purified natural gas or bottled gas (propane or a mixture of propane with butane or a mixture of other gases). It should be noted that this is one of the simplest and cheapest options for implementing the proposed method. Such low power installations can be used on vehicles. The process diagram is presented in figure 1. The method is implemented as follows.

Gas from the storage or cylinder is fed to conversion unit 1, in which the catalytic exothermic conversion of gas takes place at a temperature of 783-2473 K with the formation of hydrogen, carbon monoxide and minor amounts of other gases. The gases formed - the first working fluid, enter the first circuit of engine 2 (Fig. 1) or a separate engine 2 (Fig. 1a), where they expand, convert the thermal and kinetic energy of gases into mechanical energy, and are supplied without separation from engine 2 into the reactor, a methanator 3, in which a catalytic exothermic reaction between hydrogen and carbon monoxide takes place to form a methane-vapor mixture. The process is carried out according to one of the known technologies at a pressure of from 0.5 to 20 MPa, while the temperature develops up to 1400 K. The methanopar mixture - the second working fluid, enters the second circuit of engine 2a (Fig. 1) or a separate engine 4 (Fig. 1a), expands and converts the thermal and kinetic energy of the mixture into mechanical energy. The spent mixture is again fed into the block of conversion reactors 1 for re-conversion. The cycle closes.

With a large amount of processed raw materials, for example, crude petroleum associated gases, the process flow diagram (Fig. 1b) is supplemented by a synthesis reactor unit for a given chemical product 5, a gas purification and separation unit 8, and it is advisable to equip all the reactors with waste heat boilers 6 and additional steam turbines 7 (figb) or add noble gases or noble gas mixtures to the mixture of conversion products.

Theoretically, this process consumes oxygen and a small amount of water to start the installation, as well as catalysts that are deactivated during operation and are subject to periodic replacement or regeneration. The oxygen consumption for starting the process is up to 0.5-0.6 m ³ per 1 m ^{3 of} gas (depending on the composition of the gas), the flow rate of water vapor is up to 0.8 kg per 1 kg of gas.

Since the methane conversion process is reversible, a mixture of hydrogen and carbon monoxide obtained under stationary conditions (at metallurgical, oil refining, or chemical enterprises) can be used as a processed gas. A diagram of one of the possible embodiments of such a process is depicted in FIG.

A mixture of gases from cylinders or storage is fed to the reactor methanator 3, in which a mixture of methane and water vapor is formed. From the reactor, the mixture is transferred to engine 4, where it expands and converts the thermal and kinetic energy of the mixture into mechanical energy, and from engine 4 to the block of conversion reactors 1, in which the methane-vapor mixture is again converted into a mixture of hydrogen and carbon monoxide, which are fed into engine 2, where it expands and converts the thermal and kinetic energy of the mixture into mechanical energy, and from engine 2 the spent mixture is returned to the methanator reactor 3. The cycle closes.

Calculation of the thermal power of an engine operating according to the method of energy conversion shown in schemes 1, 1a, 1b, 1c can be performed by the formula

where N is the engine power, W;

k is the adiabatic exponent;

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

T is the temperature of the working fluid at the engine inlet, K;

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

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

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

The initial data accepted for calculation:

- engine type - a turbine is used as an engine;

- p _I = 10 MPa - pressure of gas-vapor and gas mixtures at the inlet of the turbine;

- p _o = 0.1 MPa - pressure of gas-vapor and gas mixtures at the outlet of the turbines;

- T = 1400 K — temperature of the methane-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;

- С _{v, Mn} = С _{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;

- K = 340 - adiabatic index for a mixture of hydrogen and carbon monoxide;

- R = 976.5 J / (kg.K) - specific gas constant of a mixture of hydrogen and carbon monoxide.

Taking the flow rate of the working fluid n = 1 kg / s, we obtain the thermal power of the engine (s) N = 6.10 MW, and in the prototype 2.35 MW.

The temperature of the exhaust gas is determined by the formula:

For a mixture of hydrogen and carbon monoxide, it is 445 K, for a methane-vapor mixture it is 780 K. If the catalytic conversion of methane is carried out at a temperature of more than 783 K, then at a pressure of more than 0.12 MPa, the exhaust gas mixture will have the indicated temperature. In this case, it is not necessary to consume oxygen and it will be sufficient to limit ourselves to steam catalytic conversion, since the necessary temperature in the reactor will provide the exhaust gases.

After starting this process, only the catalyst that is deactivated during operation will be the consumable. Water vapor and natural gas will be consumed only to compensate for possible leaks.

With the above process parameters and the gas pressure after the 0.12 MPa turbine, the engine power will be 5.74 MW, and in the prototype 1.46 MW.

The amount of energy released in a chemical process in reactors can be determined from the reactions:

CO + 3H ₂ → CH ₄ + H ₂ O + 206.2 kJ / mol;

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

CH ₄ + 2O ₂ = CO ₂ + 2H ₂ O + 882 kJ / mol.

Considering that in the last reaction no more than 4% of the reagents are consumed, the total heat output in the reactors is 12.12 + 2.512 + 2.2 = 16.442 MW. The internal thermal efficiency of the cyclic process is 0.790, and in the prototype - 0.165.

When using a hot water boiler, the capacity will increase by 1,055 MW and then the efficiency for the capacity of 6.1 MW will be 0.853.

With a large volume of processed gas, the method is implemented according to the scheme shown in Fig. 1b, the basis for which is the scheme shown in Fig. 1a, which in this case is supplemented by a synthesis unit for a given product 5, steam boilers 6 with superheaters and a turbogenerator 7, Unreacted gases and non-target products are returned from the synthesis unit of the desired product 5 for conversion to the conversion reactor unit 1, for example, through an expansion turbine (not shown), which ultimately provides additional energy. With this scheme of implementation of the invention, along with electricity, a given chemical product will be produced, for example, methyl alcohol in an amount of 1.015 kg per 1 norm. m ³ gas or ethyl alcohol, or diesel fuel, or other products. The efficiency of the production process of methyl alcohol, determined by the amount of energy contained in the resulting product, taking into account the costs of the energy generated to drive the auxiliary mechanisms of the synthesis reactor unit 5, is 0.960. Processed raw materials are not consumed for energy production.

Example 2

Processed raw materials - solid or liquid hydrocarbons or waste containing carbon. The scheme is presented in figa, 2b. The method is implemented as follows.

The raw material, after appropriate preparation according to one of the known technologies, is loaded into the gasification reactor block 1 (Fig. 2), intended for processing solid or liquid raw materials, in which it is gasified by oxygen, or steam and oxygen, or plasma. The gas obtained in the process of gasification, consisting mainly of hydrogen and carbon monoxide, is supplied to the engine 2, where it expands and converts the thermal and kinetic energy of the mixture into mechanical energy. The mixture of gases worked out in the engine is separated in the separation unit 8, hydrogen and carbon monoxide are fed to the methanator reactor 3, in which a catalytic exothermic reaction between hydrogen and carbon monoxide takes place to form a mixture of methane and water vapor. The separated products are returned to the gasification reactor block 1, and the methane-vapor mixture is fed to the second engine 4, where it expands and converts the thermal and kinetic energy of the mixture into mechanical energy. From engine 4, the spent mixture enters the gasification reactor block 1, in which it again turns into hydrogen and carbon monoxide. The cycle closes.

With constant processing of raw materials, if the generated energy is consumed in limited quantities, hydrogen and carbon monoxide can be fed into the synthesis reactor block 5 (Fig. 2a), bypassing the methanator reactor 3 and engine 4. In the synthesis reactor block 5, the synthesis of the specified chemical compounds takes place, which are stored, and non-target products and purge gases through the engine 9 are returned to the gasification reactor 1.

To make full use of the energy released in this cycle, all reactors and the gas purification and separation unit 8 can be equipped with steam boilers 6 with superheaters (Fig. 2a). The steam obtained in steam boilers is supplied to a steam turbine 7, providing the generation of additional energy.

In the transport embodiment of the power plant implementation (for example, diesel or ship) from the process diagram shown in Fig. 2a, the synthesis reactor block 5, steam boilers 6 and engine 7 are excluded, and the methane-steam mixture spent in engine 4 is fed directly to the gasification reactor block 1. To completely convert the thermal energy released in the reactors into mechanical energy and to reduce the temperature of the working fluid at the inlet of the engines, instead of steam boilers, noble gases can be added to the gasification products or impurity noble gases such as argon and helium mixture or other mixture.

Given in this example, one of the possible implementations of the claimed method allows you to process from several kilograms to several tens of thousands of tons of raw materials per day. Depending on the type of processed raw materials, the amount of gas produced (hydrogen and carbon monoxide) ranges from 1-1.5 m ³ / kg for low-grade brown coal and household waste, up to 3-3.5 m ³ / kg for fuel oil, oil residues and crude oil.

If the method described in this example is used for processing constantly incoming waste or other raw materials, it is necessary to produce chemical products, since in another way it is impossible to prevent the release of gaseous products into the atmosphere.

The calculation of engine power can be carried out according to the formula given in example 1. The processed raw materials are pressed sawdust. Steam consumption for gasification is 0.4 kg per 1 kg of sawdust, oxygen consumption is 0.3 kg per 1 kg of sawdust.

We accept the following initial data for the calculation:

- the yield of methyl alcohol (methanol) is 0.492 kg per 1 kg of sawdust;

- enthalpy of combustion of methyl alcohol - 22.3 MJ / kg;

- enthalpy of combustion of pressed sawdust - 19.4 MJ / kg

- gasification process temperature - 2073 - 2173 K;

- pressure at the outlet of the gasification reactor block - 8 MPa;

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

- pressure at the outlet of the methanator reactor-10 MPa;

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

- the temperature at the outlet of the methanol synthesis reactor 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;

- vapor pressure in the low pressure system - 1.2 MPa;

- the amount of gas generated during gasification is 1.95 kg per 1 kg of sawdust;

- the amount of unreacted purge gases in the methanol synthesis reactor is 0.54 kg per 1 kg of sawdust;

- the amount of sharp steam to a steam turbine during coal gasification - 0.94 kg per 1 kg of sawdust;

- the amount of intermediate overheating steam to a steam turbine during gasification of sawdust - 0.84 kg per 1 kg of sawdust;

- the amount of low pressure steam to a steam turbine during gasification of sawdust - 1.28 kg per 1 kg of sawdust.

The following calculation results were obtained:

- the amount of electricity generated by a steam turbine during gasification of 1 kg of sawdust - 0.70 kW · h;

- the amount of electricity generated by the main engines during gasification of 1 kg of sawdust - 1.23 kWh;

- the total amount of energy generated by all turbines, as a result of gasification of 1 kg of sawdust - 1.93 kWh;

- the amount of energy contained in the methanol produced is -3.07 kWh;

- thermal efficiency of the methanol production process - 0.928.

Example 3

Processed raw materials - water not suitable for drinking, or a mixture of water with any carbon-containing organic or inorganic compounds, including waste and gases. One possible implementation of such a process is presented in figure 3. The method is implemented as follows.

If water does not contain organic substances, then it is pre-mixed according to one of the known technologies with solid, or liquid, or gaseous, or with all carbon-containing products at the same time, after which it is supplied to the gasification reactor block 1, in which it turns into a mixture of gases during gasification . The amount of the supplied mixture should be such as to ensure a temperature of about 2000-5000 K in the reaction zone of the reactor block, at a plasma temperature of about 8000 K and a pressure of up to 10-15 MPa, depending on the elemental composition of the impurities in the treated water. At this temperature, carbon-free substances are melted, fed to the reactor slag, and then disposed of. Carbon and water are converted into gases consisting of hydrogen, carbon monoxide and partially or fully dissociated water molecules. This mixture is supplied to engine 2, where it expands and converts the thermal and kinetic energy of the mixture into mechanical energy, and the steam from the steam boiler 6 built into the reactor is transferred to the steam turbine 7. After leaving the engine 2, the gases enter block 8, where they are separated and the water condenses. Hydrogen and carbon monoxide are partially sent to the methanator reactor 3, and partially to the unit for the synthesis of organic compounds 5. The mixture of methane and water vapor formed in the methanator reactor is fed to engine 4, where it expands and converts the thermal and kinetic energy of the mixture into mechanical energy, and from the engine - to the gasification reactor block 1. The cycle thus closes.

The treatment of wastewater and water contaminated with organic substances should be accompanied by the release of chemical organic products, since the substances involved in the engine cycle are theoretically not consumed. When using the method for desalination, inorganic products can also be produced.

The initial data used for the calculation:

- the power consumed by plasma torches at a water flow rate of 1 l / s and a plasma temperature of 8000 K is 24.3 MW;

- the amount of heat supplied to the reactor every second is 23.1 MJ;

- water vapor temperature at the turbine inlet - 1400 K;

- steam pressure at the turbine inlet - 10 MPa;

- steam pressure at the outlet of the turbine - 0.05 MPa;

- the amount of heat required to evaporate 1 kg of water and heat 1 kg of water vapor to 1400 K is 5.69 MJ;

- engine power at a flow rate of a mixture of hydrogen and carbon monoxide and a methane-steam mixture of 1 kg / s - 6.1 MW, and in the prototype - 2.35 MW;

- the adiabatic exponent for water vapor is 1.226;

- specific gas constant of water vapor - 461.5 J / kg K.

The following calculation results were obtained:

- the amount of water and steam heated every second by the allocated heat to a temperature of 1400 K - 4.06 kg;

- steam turbine power - 11.59 MW;

- the total power of all engines is 17.69 MW;

- the flow rate of the mixture of hydrogen and carbon monoxide and methane-vapor mixture through the engine to compensate for heat loss - 1.48 kg / s, and in the prototype - 4.6 kg / s

Produced products: distilled water, electricity, thermal energy, inorganic slag, products of organic and inorganic synthesis. The use of energy from third-party sources for the production of these products does not occur.

Information sources

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

Claims (4)

1. A method of converting energy with the regeneration of energy in a cyclic process, comprising supplying the prepared raw materials to a gasification or conversion reactor, in which it is gasified or converted in an autothermal or thermal regime with the formation of hydrogen, carbon monoxide and related products, separation of related products, the supply of a mixture of hydrogen and carbon monoxide in a methanator reactor, in which a mixture of methane and water vapor is formed - the working fluid, feeding this mixture into the engine with its subsequent expansion and conversion into mechanical energy, characterized in that the formed non-separated gasification products are fed into the engine - the first working fluid, when expanded, the thermal and kinetic energy of the mixture is converted into mechanical energy in the engine, and the first working fluid spent and cooled in the engine is separated into hydrogen, oxide carbon and related products, while the separated hydrogen and carbon monoxide are fed to a methanator reactor, where a methane-vapor mixture is formed in the catalytic process - the second working e body, which is also fed into the second circuit of the aforementioned engine, where it also converts the energy of the mixture into mechanical energy during the expansion process, and the spent methane-vapor mixture and associated products are returned to the gasification or conversion reactor, in which the mixture of hydrogen and carbon monoxide is again formed, this closes the cycle. 2. The method according to claim 1, in which the gasification or conversion of raw materials is carried out in a plasma-chemical mode. 3. The method according to claim 2, in which the plasma-forming substance in the plasma-chemical regime is water. 4. The method according to claim 1, wherein a noble gas or a mixture of noble gases is added to a mixture of hydrogen and carbon monoxide, as well as methane and water vapor.

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