RU2791358C1 - Hydrogen production method - Google Patents

Abstract

FIELD: hydrogen production.

SUBSTANCE: hydrogen production method can be used in the petrochemical and gas chemical industries for large-scale production of hydrogen. The hydrogen production method includes increasing the pressure of the feedstock in the form of natural gas using compressor equipment, and/or liquefied hydrocarbon gases (LHG), and/or light gasoline, and/or hydrocarbon mixtures using pumping equipment. The feedstock and the first hydrogen stream are mixed to obtain a feed stream, the feed stream is heated and purified from impurities of sulphur compounds and unsaturated hydrocarbons in a series-connected catalytic hydrogenation reactor and a system of desulfurization reactors. Next, the purified feed stream is mixed with steam, the resulting mixture is heated and fed to the adiabatic preliminary reforming reactor, the resulting reaction mixture is mixed with steam and heated, followed by supply to the steam reforming furnace to produce synthesis gas. The synthesis gas is cooled and fed into the carbon monoxide shift reactor. The converted synthesis gas is cooled and separated with separation of process condensate, the cooled separated synthesis gas is supplied for two-stage purification. At the same time, carbon dioxide is removed using an aqueous solution of potash in an absorber at the first purification stage, followed by absorbent regeneration and drying. At the second stage of purification, carbon monoxide and other impurities are removed in the absorber system. The resulting hydrogen is divided into two streams: the first is sent for mixing with the feedstock before the catalytic hydrogenation reactor, and the second is sent to consumers.

EFFECT: invention makes it possible to increase the yield of hydrogen, reduce the energy and material intensity of production, increase its environmental friendliness, and expand the raw material base.

21 cl, 1 dwg

Description

The invention relates to a method for the production of hydrogen and can be used in the oil refining, petrochemical and gas chemical industries for large-scale production of hydrogen.

A variety of raw materials are used to produce hydrogen, most often natural gas, while the following reactions occur during its catalytic steam reforming:

CH ₄ + H ₂ O \u003d CO + 3H ₂ ;

CH ₄ + 2H ₂ O \u003d CO ₂ + 4H ₂ ;

CO + H ₂ \u003d CO ₂ + H ₂ ;

allowing to obtain four hydrogen molecules by the interaction of one methane molecule with two water molecules. Similarly, hydrogen can be obtained from heavier paraffinic hydrocarbons contained in natural gas (ethane, propane, butane, etc.) and in light straight-run oil fractions.

A known method for producing a hydrogen-containing gas, which includes two successive stages: at the first stage at a temperature of T=1000-1100°C, a non-catalytic matrix conversion of methane into synthesis gas is carried out in the presence of steam, and at the second stage in a flow reactor, a catalytic conversion of the methane obtained at the first stage is carried out. synthesis gas stage at a temperature of T=500-900°C (patent for invention RU 2769311, IPC S01V 3/26, S01V 3/24, applied on 10/05/2020, published on 03/30/2022). The disadvantages of the invention are:

lack of justification for the installation of equipment in the combustion chamber;

lack of evidence of the possibility of a large-scale transition from a laboratory matrix reactor for the oxidation of 20 l/h of methane to an industrial apparatus of a similar design, but thousands of times greater productivity and tens of times larger.

A known method for producing hydrogen and carbon monoxide, which includes the steps: (a) obtaining a hot gas mixture, consisting mainly of carbon dioxide and steam and containing from 0 to about 2% by volume of carbon monoxide, while the specified hot gas mixture has a temperature of at least measure 1000°C, by burning hydrocarbon fuel with oxygen-enriched gas in a high temperature furnace, while oxygen is present in an amount in the range from a stoichiometric amount to about 110% by volume of the stoichiometric amount; and (b) producing a gaseous product enriched in hydrogen and carbon monoxide by contacting at least a portion of said hot gas mixture with a hydrocarbon material in a reactor at a temperature and pressure high enough to cause the hydrocarbon material to react with carbon dioxide and steam. invention US 5714132, IPC C01B 31/20, C01B 3/18, C01B 3/00, C01B 3/24, C01B 3/26, C01B 3/34, application 26.09.1995, published 03.02.1998 ). The disadvantages of the invention are:

the absence of preliminary purification of hydrocarbon feedstock from organosulfur impurities, which, when they enter the reforming catalyst, reduce its activity and indirectly - the productivity of the installation;

lack of substantiation for the choice of a hydrogen concentration system, since The recommended adsorption purification of hydrogen-containing gas by the “temperature swing” method is energy-intensive and requires large expenditures on the adsorbent, adsorption purification by the “pressure swing” method leads to a large loss of hydrogen during pressure relief during adsorbent regeneration, and the proposed combination of adsorption purification of the first or second type and cryogenic rectification dramatically increases the energy costs for obtaining concentrated hydrogen.

A known method for producing hydrogen from gaseous hydrocarbon feedstock - natural gas, associated petroleum gas, and hydrocarbon gas obtained by evaporation of liquid fuel, including purification of the supplied gas from sulfur compounds, mixing of the purified gas with steam, catalytic steam reforming of hydrocarbons with the supply of high-temperature heat and obtaining converted gas, catalytic steam reforming of carbon monoxide with removal of low-temperature heat by evaporative cooling and release of commercial hydrogen from hydrogen-containing gas, while gaseous hydrocarbon feedstock is supplied to the desulfurization unit with a pressure of at least 0.5 MPa and, after purification from sulfur compounds, is divided into two streams , one of the streams is supplied for mixing with steam, which is then subjected to steam catalytic conversion at a temperature of 800-1050 ° C in a radial-spiral type reactor, the resulting converted gas is fed as a heating medium to a waste heat boiler a generator for partial cooling, catalytic steam reforming of carbon monoxide is carried out in a radial-helical reactor at a temperature of 190-230°C, then the resulting hydrogen-containing gas is additionally cooled to a temperature of 20-40°C by an external coolant and separated from moisture in a gas cooler-dryer, after which it is fed to the hydrogen-containing gas separation unit, in which the final product - commercial hydrogen is separated, and the purge gas is removed from the hydrogen-containing gas separation unit and mixed with the second stream of hydrocarbon gas purified from sulfur, the resulting mixture is fed as fuel gas to the burner of the catalytic conversion reactor hydrocarbons, and before being fed to the burner, this mixture and the air necessary for combustion are heated in the heat recovery unit due to the partial cooling of the flue gases leaving the catalytic hydrocarbon conversion reactor, after which the flue gases are additionally cooled to separate moisture by an external coolant in the cooler. flue gas tele-dryer and removed from the plant, and the condensate released in the coolers-driers of hydrogen-containing gas and flue gases is subjected to purification in the water treatment unit and sent to produce steam, necessary for steam reforming of hydrocarbons, in a hydrogen waste heat boiler (patent for the invention RU 2394754, IPC S01V 3/34, S01V 3/12, Appl. March 6, 2009, publ. July 20, 2010). The disadvantages of the invention are:

technological irrationality of the proposed hydrotreatment of liquid feedstock after its evaporation, since during the processing of diesel fuel, naphtha and other high-molecular hydrocarbon feedstock in the hydrotreatment reactor, 2.5-5.0 MPa and 350-380°C are maintained, at which the feedstock in the hydrotreatment reactor is in liquid phase state;

excessively costly separation of hydrogen-containing gas into sales hydrogen and purge gas in the pressure swing adsorption unit, since the content of impurities in hydrogen-containing gas after the carbon monoxide steam reforming reactor and water condenser is very high (unreacted hydrocarbons and carbon monoxide, carbon dioxide, residual moisture), which will require the use of adsorbers with a large load of the adsorbent, which leads to significant losses of hydrogen with the stripping gas at the desorption stage;

inexpedient use of part of the hydrotreated feedstock as fuel in the presence of cheaper and less valuable fuels.

A method for producing hydrogen from a hydrocarbon feedstock, including mixing the feedstock with an oxidant, mainly oxygen, and partial oxidation of the feedstock in a combustion chamber of a cooled flow reactor to obtain a gas-vapor mixture containing hydrogen, carbon mono- and carbon dioxide, water vapor and by-products of the combustion reaction, which is moistened and cooled to a predetermined temperature by injecting water into the gas stream and a two-stage catalytic steam conversion of carbon monoxide is carried out, followed by hydrogen evolution, while the hydrocarbon feedstock previously purified from sulfur impurities is heated, moistened with water vapor and mixed with an oxidizer, partial oxidation of the feedstock is carried out at a pressure of combustion chamber 6.0-7.0 µPa, the heat of the gas-vapor mixture is used to heat the raw material and produce steam, the steam catalytic conversion of carbon monoxide is carried out on a single catalytic composition using the same type of Cu-Zn-cement-containing catalyst in three stages, the first conversion stage being carried out at a temperature of 350-550°C using a catalyst with a mass content of zinc oxide of 40.0 ± 4.0% and copper oxide of 27.0 ± 4.0%, the second and third conversion stages are carried out at temperature of 300-450°C using a catalyst with a mass content of zinc oxide of 22.5±2.5% and copper oxide of 48.0±3.0%, and hydrogen evolution is carried out by sequentially cooling the gas mixture to a temperature of 50-60°C with separation of water condensate, and then further cooling of the gas mixture to a temperature of 15-18 ° C with separation of carbon dioxide condensate (patent for invention 2643542, IPC C01B 3/02, C01B 3/26, C01B 3/36, dec. November 11, 2016, publ. February 2, 2018). The disadvantages of the invention are:

lack of detailing the method of purification of hydrocarbon raw materials from organosulfur impurities, which significantly affects the efficiency of the process as a whole;

the use of pure oxygen or air enriched with oxygen as an oxidizing agent, which requires the construction of an additional plant for the production of oxygen;

concentration of hydrogen in the hydrogen-containing gas by condensation of carbon dioxide while cooling the hydrogen-containing gas from 50-60 to 10-15°C at a pressure of at least 5.5 MPa, ensuring the condensation of only pure carbon dioxide.

Also known closest to the claimed invention is a method for producing hydrogen at an absolute pressure of at least about 400 kPa, including supplying a steam reforming zone with partial oxidation of a hydrocarbon-containing feedstock, air and steam, characterized by the presence of free oxygen in a molar ratio to carbon in the feedstock in a ratio of approximately from 0.4:1 to 0.6:1 and the presence of steam in a molar ratio to carbon in the feed in an amount of at least about 4:1; maintaining in this zone the conditions for reforming with partial oxidation, including the specified pressure, providing partial oxidation of a part of the feedstock with heat generation, as well as reforming of a part of the feedstock with hydrogen generation, as a result of which the output reformate stream contains hydrogen, carbon monoxide and carbon dioxide; cooling the reformate effluent stream by indirect heat exchange with a stream containing liquid water to form a steam-containing stream at a temperature of at least about 300° C., which is recycled to the reformer with partial oxidation, with at least about 40% of the steam in the feed mixture being formed due to the specified indirect heat transfer (patent for invention 2378188, IPC S01B 3/38, declared 05/05/2005, publ. 01/10/2010). The disadvantages of the invention are:

excessively costly separation of hydrogen-containing gas into sales hydrogen and purge gas in the pressure swing adsorption unit, since the content of impurities in hydrogen-containing gas after the carbon monoxide steam reforming reactor and water condenser is very high (unreacted hydrocarbons and carbon monoxide, carbon dioxide, residual moisture), which will require the use of adsorbers with a large load of the adsorbent, which leads to significant losses of hydrogen with the stripping gas at the desorption stage.

When creating the invention, the task was to develop a highly efficient method for the production of hydrogen, which simultaneously provides an increase in the yield of commercial hydrogen, a decrease in the energy and material consumption of production, as well as an increase in its environmental friendliness.

The problem is solved due to the fact that the hydrogen production method includes increasing the pressure of the feedstock in the form of natural gas using compressor equipment and/or liquefied hydrocarbon gases (hereinafter referred to as LPG) and/or light gasoline and/or hydrocarbon mixtures using pumping equipment, mixing feedstock and the first hydrogen stream to obtain a feed stream, heating and cleaning the feed stream from impurities of sulfur compounds and unsaturated hydrocarbons in a series-connected catalytic hydrogenation reactor and a system of desulfurization reactors, mixing the purified feed stream with steam, heating the resulting mixture and feeding it to the reactor adiabatic pre-reforming, mixing the resulting reaction mixture with steam and heating it, followed by feeding it to a steam reforming furnace to produce synthesis gas, cooling and supplying the resulting synthesis gas to the carbon monoxide shift reactor, cooling and separating conversion of converted synthesis gas with separation of process condensate, supply of cooled separated synthesis gas for two-stage purification with removal of carbon dioxide using an aqueous solution of potash in the absorber at the first stage of purification, followed by regeneration of the absorbent and with drying and extraction of carbon monoxide and other impurities in the system adsorbers at the second stage of purification, separation of the resulting hydrogen into two streams: the first is sent for mixing with the feedstock before the catalytic hydrogenation reactor, and the second - through the product fleet to consumers. The proposed solution allows:

expand the resource base and, when implementing the method within the petrochemical cluster, involve the least valuable low-margin hydrocarbons in processing;

to prevent coking of the catalyst due to the removal of impurities of unsaturated hydrocarbons, while the conversion of organosulfur impurities into hydrocarbons increases the amount of converted feedstock and indirectly - the yield of hydrogen, and the removal of sulfur in the form of hydrogen sulfide prevents poisoning of the catalyst and its deactivation;

to increase the feedstock conversion in the adiabatic pre-reformer by increasing the residence time of the reaction mixture in this reactor due to the fractional supply of steam to the adiabatic pre-reformer and to the steam reformer;

significantly reduce the amount of expensive adsorbent in the adsorber system due to two-stage purification of synthesis gas.

It is advisable, if possible, to pre-collect and compound the liquid feedstock.

Additionally, physical and/or chemical absorbent absorption techniques can be used to remove sulfur compound impurities from the feed stream. It is also possible to additionally remove undesirable impurities of chlorine compounds and/or heavy metals from the feed stream by adsorption on a solid absorber.

It is advisable to cool the purified feed stream and separate it from the hydrogen-containing gas, which is then sent to the first stage of synthesis gas purification, since a hydrogen-containing gas circulation loop appears, excluding the passage of this hydrogen through the adiabatic pre-reforming reactor and the steam reforming furnace to produce synthesis gas, which indirectly reduces the cost of the catalyst and the dimensions of the apparatus.

In the adiabatic pre-reformer, it is recommended to load a nickel-molybdenum or cobalt-molybdenum catalyst or a catalyst based on noble metals or metals of the νΐίΐ group or oxides of these metals.

It is expedient to load the reaction tubes of the steam reforming furnace with a nickel catalyst or a catalyst based on noble metals or Group VIII metals or oxides of these metals or cobalt molybdate or nickel-thorium-magnesium or nickel-aluminum-magnesium or nickel-magnesium on a support of aluminum oxide or carbon. or magnesium oxide or alumina-magnesia or thorium-magnesium to increase the conversion of hydrocarbons up to 99%.

In order to reduce energy costs, it is advisable to use the heat of the flue gases of the steam reformer to heat the feedstock and/or the purified feed stream and/or process streams before entering the adiabatic pre-reformer reactor and/or the reaction tubes of the steam reformer and/or to generate steam and/or for heating the boiler feed water and/or for heating the air supplied as an oxidant to the steam reformer. For this purpose, when the synthesis gas is cooled downstream of the steam reformer, steam is generated and/or boiler feed water is heated and/or the feedstock is heated.

The generated water vapor is mixed with the process streams and is involved in the process of adiabatic pre-reforming and/or steam reforming and/or carbon monoxide conversion and/or is used to generate electrical energy and/or is used as a heat carrier for heating process streams, including for regeneration absorbent and adsorbent for two-stage purification of synthesis gas, and/or is used as a working gas in an expander unit to drive compressor and pumping equipment, fully ensuring the production of hydrogen both as a reagent and as a coolant of the required parameters.

It is expedient to load an iron-chromium oxide catalyst into the carbon monoxide conversion reactor, and to maintain the temperature in the reaction zone, to carry out cooling using boiler feed water or another refrigerant that compensates for the thermal effect of the reaction.

Since potash purification at the first stage of synthesis gas purification does not allow to completely purify synthesis gas from carbon dioxide, it is advisable to additionally carry out absorption with an aqueous solution of amine in an additional absorber installed in series or in parallel with the potash purification absorber, followed by regeneration of the absorbent.

It is advisable to use the method of pressure swing adsorption (hereinafter referred to as PSA) at the second stage of synthesis gas purification, since it deeply purifies polluted hydrogen obtained at high pressure and at a temperature of 30-40°C of the first stage of synthesis gas purification, and regeneration of the adsorbent is ensured by desorption of previously adsorbed impurities when depressurizing the system of adsorbers, which significantly reduces the energy intensity of the process compared to the regeneration of the adsorbent by increasing the temperature to 300-350°C. Energy costs are also reduced due to the fact that the PSA stripping gas is supplied to the steam reformer as a fuel gas and / or to the fuel network, since the stripping gas arising from the regeneration of the adsorbent is a high-calorie fuel, in addition, the absence of stripping gas discharge directly into the atmosphere improves the environmental performance of production. The extraction of carbon dioxide from the flue gases of the steam reformer with the help of an aqueous solution of potash also serves to improve the environmental performance of the production.

As an alternative, it is envisaged to compress the PSA stripping gas with subsequent purification from carbon dioxide using an aqueous solution of potash and/or other chemical and/or physical absorbents and supply it to the steam reformer as fuel gas and/or to the fuel network.

It is useful to use carbon dioxide recovered from synthesis gas and/or flue gases and/or PSA stripping gas as a commercial product and/or dispose of, for example, by injection into spent oil fields to reduce greenhouse gas emissions to the atmosphere.

It is advisable to use an additional refrigeration unit at the second stage of synthesis gas purification in order to reduce the load on the PSA, which makes it possible to achieve a lower positive temperature value, reducing it from 30–40 to 5–8°C, and to condense a larger amount of water vapor from synthesis gas, which will reduce the loading of an expensive adsorbent and the dimensions of the adsorber system, reducing operating and capital costs for two-stage purification of synthesis gas.

At the second stage of synthesis gas purification, the glycol drying method can be additionally used.

The figure shows an example of the implementation of the claimed invention using the following notation:

1-30 - pipelines;

101 - feedstock compressor;

102 - heating unit;

103 - catalytic hydrogenation reactor;

104 - system of desulfurization reactors;

105 - adiabatic pre-reforming reactor;

106/1 - unit for heat recovery of flue gases of the steam reforming furnace;

106/2 - reactor block of the steam reforming furnace;

107, 109 - cooling unit;

108 - carbon monoxide conversion reactor;

110 - separator;

111 - absorber;

112 - regenerator;

113 - adsorber system;

114 - pump;

115 - steam generation system;

116 - hydrogen recirculation compressor.

The main natural gas is fed through pipeline 1 to the feedstock compressor 101 to increase pressure, after which it is sent through pipeline 2 for mixing with a small amount of product hydrogen supplied via pipeline 27 from the hydrogen recirculation compressor 116. The mixture of compressed natural gas and hydrogen is first via pipeline 3 is supplied to the heating unit 102 and then sequentially passes through pipeline 4 and pipeline 5 the catalytic hydrogenation reactor 103 and the system of desulfurization reactors 104, where the sulfur compounds of the feed stream are converted into hydrogen sulfide, followed by its removal and hydrogenation of unsaturated hydrocarbons. Through pipeline 6, the purified feed stream is sent for mixing with water vapor coming through pipeline 12 from the steam generation system 115, and subsequent supply via pipeline 7 to the flue gas heat recovery unit of the steam reformer 106/1. The superheated mixture enters the adiabatic preliminary reforming reactor 105 through pipeline 8 to convert hydrocarbons C ₂ and higher into methane, after which it passes successively through pipeline 11 to the flue gas heat recovery unit of the steam reforming furnace 106/1 and through pipeline 13 to the reactor block of the furnace steam reformer 106/2. The resulting synthesis gas enters through pipeline 14 to the cooling unit 107 and then through pipeline 15 to the carbon monoxide conversion reactor 108. The converted synthesis gas is sent through pipeline 16 to the cooling unit 109 and cooled is fed through pipeline 17 to separate condensed water vapor into the separator 110 The separated process condensate follows through pipeline 19 to pump 114, which is pumped through pipeline 28 to the steam generation system 115. The cooled separated synthesis gas enters through pipeline 18 for potash purification from carbon dioxide into absorber 111, where regenerated absorbent is supplied through pipeline 22 . The purified stream is fed through pipeline 20 to the system of adsorbers 113 for hydrogen extraction. Saturated absorbent through the pipeline 21 enters the regenerator 112, from where the captured carbon dioxide is discharged through the pipeline 23. The product hydrogen removed via pipeline 24 from the system of adsorbers 113 is separated: the first part is removed via pipeline 25 for further use, and the second part is fed via pipeline 26 to hydrogen recirculation compressor 116 for mixing with compressed natural gas. To obtain steam, demineralized water enters the steam generation system 115 through pipeline 29, and after appropriate preparation, boiler feed water is supplied through pipeline 9 to the flue gas heat recovery unit of the steam reforming furnace 106/1, and steam is removed through pipeline 10, part of which is involved in the steam reforming process through line 12, while the excess steam is exported through line 30.

Thus, the claimed invention solves the problem of developing a highly efficient method for the production of hydrogen, which simultaneously provides an increase in the yield of hydrogen, a decrease in the energy and material consumption of production, and also an increase in its environmental friendliness.

Claims (21)

1. A method for the production of hydrogen, including increasing the pressure of the feedstock in the form of natural gas using compressor equipment, and / or liquefied hydrocarbon gases (LHG), and / or light gasoline, and / or hydrocarbon mixtures using pumping equipment, mixing the feedstock and of the first hydrogen stream to obtain a feed stream, heating and cleaning the feed stream from impurities of sulfur compounds and unsaturated hydrocarbons in a series-connected catalytic hydrogenation reactor and a system of desulfurization reactors, mixing the purified feed stream with steam, heating the resulting mixture and feeding it to the adiabatic preliminary reforming reactor , mixing the resulting reaction mixture with water vapor and heating it, followed by feeding it to a steam reforming furnace to produce synthesis gas, cooling and supplying the resulting synthesis gas to the carbon monoxide shift reactor, cooling and separating the converted synthesis gas from the department process condensate supply, supply of cooled separated synthesis gas for two-stage purification with removal of carbon dioxide using an aqueous solution of potash in the absorber at the first stage of purification, followed by regeneration of the absorbent and with drying and extraction of carbon monoxide and other impurities in the adsorber system at the second stage of purification, separation of the resulting hydrogen into two streams: the first is sent for mixing with the feedstock before the catalytic hydrogenation reactor, and the second - through the product fleet to consumers. 2. The method according to p. 1, characterized in that the liquid feedstock is pre-collected and compounded. 3. The method according to p. 1, characterized in that to remove impurities of sulfur compounds from the feed stream, an absorption method with a physical and / or chemical absorber is additionally used. 4. The method according to claim 1, characterized in that, additionally, undesirable impurities of chlorine compounds and/or heavy metals are removed from the feed stream by adsorption on a solid absorber. 5. The method according to claim 1, characterized in that the purified feed stream is cooled and separated from the hydrogen-containing gas, which is then sent to the first stage of synthesis gas purification. 6. Process according to claim 1, characterized in that the adiabatic pre-reformer is loaded with a nickel-molybdenum or cobalt-molybdenum catalyst, or a catalyst based on noble metals, or group VIII metals, or oxides of these metals. 7. The method according to claim 1, characterized in that the reaction tubes of the steam reforming furnace are loaded with a nickel catalyst or a catalyst based on noble metals or Group VIII metals, or oxides of these metals, or cobalt molybdate, or nickel-thorium-magnesium, or nickel aluminium-magnesia or nickel-magnesia on a carrier of alumina, or carbon, or magnesium oxide, or alumina-magnesia, or thorium-magnesia. 8. The method according to claim 1, characterized in that the heat of the flue gases of the steam reformer is used to heat the feedstock and/or the purified feed stream and/or process streams before entering the adiabatic pre-reformer reactor and/or the reaction tubes of the steam reformer reforming, and/or to generate steam, and/or to heat the boiler feed water, and/or to heat the air supplied as an oxidant to the steam reformer. 9. The method according to claim 1, characterized in that when the synthesis gas is cooled after the steam reforming furnace, steam is generated and/or boiler feed water is heated and/or the feedstock is heated. 10. The method according to claim 8 or 9, characterized in that the generated water vapor is mixed with process streams and involved in the process of adiabatic pre-reforming and/or steam reforming and/or carbon monoxide conversion, and/or used to generate electrical energy, and/or used as a heat carrier for heating process streams, including for the regeneration of the absorbent and adsorbent for two-stage purification of synthesis gas, and/or used as a working gas in an expander unit to drive compressor and pumping equipment. 11. The method according to p. 1, characterized in that an iron chromium oxide catalyst is loaded into the carbon monoxide conversion reactor. 12. The method of claim. 1, characterized in that to maintain the temperature in the reaction zone in the carbon monoxide conversion reactor using cooling using boiler feed water or other coolant. 13. The method according to claim 1, characterized in that at the first stage of purification of synthesis gas, absorption is additionally carried out with an aqueous solution of amine in an additional absorber installed in series or in parallel with the absorber of potash purification, followed by regeneration of the absorbent. 14. The method according to p. 1, characterized in that at the second stage of purification of synthesis gas, the method of pressure swing adsorption (hereinafter referred to as PSA) is used. 15. Method according to claim 14, characterized in that the PSA stripping gas is supplied to the steam reformer as fuel gas and/or to the fuel network. 16. The method according to p. 15, characterized in that an aqueous solution of potash is used to extract carbon dioxide from the flue gases of the steam reforming furnace. 17. The method according to claim 14, characterized in that the PSA stripping gas is first compressed and then purified from carbon dioxide using an aqueous solution of potash and/or other chemical and/or physical absorbents. 18. The method according to claim 17, characterized in that the purified compressed PSA stripping gas is supplied to the steam reformer as fuel gas and/or to the fuel network. 19. The method according to p. 1, or 16, or 17, characterized in that the carbon dioxide extracted from the synthesis gas and / or flue gases and / or PSA stripping gas is used as a commercial product and / or disposed of. 20. The method according to claim 14, characterized in that an additional refrigeration unit is used at the second stage of synthesis gas purification. 21. The method according to p. 1, characterized in that at the second stage of synthesis gas purification, the glycol drying method is additionally used.

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