WO2023229491A2 - Method for producing hydrogen - Google Patents

Abstract

A method for producing hydrogen can be used in the petroleum refining and petrochemical industry for large-scale hydrogen production. The present method for producing hydrogen includes increasing the pressure of an initial feedstock in the form of natural gas, using compressor equipment, and/or liquefied petroleum gas (LPG) and/or light gasoline and/or hydrocarbon mixtures, using pumping equipment. The initial feedstock is mixed with a first stream of hydrogen to produce a feed stream which is then heated and purified of sulphur compound and unsaturated hydrocarbon impurities in a catalytic hydrogenation reactor and a system of desulphurization reactors, which are connected in series. Next, the purified feed stream is mixed with water vapour, the resulting mixture is heated and fed into an adiabatic pre-reforming reactor, and the resulting reaction mixture is mixed with water vapour and heated before being fed into a steam reformer furnace to produce synthesis gas. The synthesis gas is cooled and fed into a carbon monoxide conversion reactor. The converted synthesis gas is cooled and subjected to separation to remove process condensate, and the cooled separated synthesis gas is fed to two-stage purification. In the first purification stage, carbon dioxide is extracted using an aqueous potash solution in an absorber, followed by recovery of the absorbent and drying. In the second purification stage, carbon monoxide and other impurities are extracted in a system of absorbers. The hydrogen obtained is divided into two streams: the first stream is sent for mixing with the initial feedstock upstream of the catalytic hydrogenation reactor, and the second stream is sent to consumers via a tank farm. The invention makes it possible to increase the yield of hydrogen, reduce the energy and material costs of production, improve the environmental friendliness thereof, and expand the range of potential feedstock.

Description

HYDROGEN PRODUCTION METHOD FIELD OF TECHNOLOGY

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

To produce hydrogen, a variety of raw materials are used, most often natural gas, and during its catalytic steam reforming the following reactions occur:

CH4 + H2OCG+3H2;

CH4 + 2H20C02+4H2;

CO+H2O=CO2+H2; allowing to obtain four molecules of hydrogen by reacting one molecule of methane with two molecules of water. Similarly, hydrogen can be obtained from heavier paraffinic hydrocarbons contained in natural gas (ethane, propane, butane, etc.) and in light straight-run oil fractions.

BACKGROUND ART

There is a known method for producing hydrogen-containing gas, which includes two successive stages: in the first stage, at a temperature T = 1000-1100 °C, non-catalytic matrix conversion of methane into synthesis gas is carried out in the presence of water steam, and in the second stage, catalytic conversion of what is obtained in the first stage is carried out in a flow reactor. synthesis gas stage at temperature T=500-900 °C (invention patent RU 2769311, IPC COIB 3/26, COIB 3/24, declared 10/15/2020, published 03/30/2022). The disadvantages of the invention are:

• lack of justification for installing 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 higher productivity and tens of times larger in size. There is a known method for producing hydrogen and carbon monoxide, which includes the steps of: (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, wherein said hot gas mixture has a temperature of less than at least 1000 °C, by burning a hydrocarbon fuel with oxygen-enriched gas in a high-temperature furnace, with oxygen present in an amount ranging from the 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 hydrocarbon material in a reactor at a temperature and pressure sufficiently high to cause the hydrocarbon material to react with carbon dioxide and steam (patent invention US 5714132, IPC S01B 31/20, SOSH 3/18, S01B 3/00, S01B 3/24, S01B 3/26, S01B 3/34, declared 09/26/1995, published 02/03/1998). The disadvantages of the invention are:

• lack of preliminary purification of hydrocarbon raw materials from organosulfur impurities, which, when contacted with the reforming catalyst, reduce its activity and indirectly reduce the productivity of the installation;

• lack of justification for choosing a hydrogen concentration system, because the recommended adsorption purification of hydrogen-containing gas using the “temperature swing” method is energy-intensive and requires high costs for the adsorbent, adsorption purification using the “pressure swing” method leads to a large loss of hydrogen when the pressure is released during regeneration of the adsorbent, and the proposed combination of adsorption purification of the first or second type and cryogenic rectification sharply increases the energy costs for producing concentrated hydrogen.

There is a known method for producing hydrogen from gaseous hydrocarbon raw materials - natural gas, associated petroleum gas, as well as hydrocarbon gas obtained by evaporation of liquid fuel, including purification of the supplied gas from sulfur compounds, mixing of purified gas with water steam, catalytic steam conversion of hydrocarbons with the supply of high-temperature heat and production of converted gas, catalytic steam conversion of carbon monoxide with removal of low-temperature heat by evaporative cooling and the release of commercial hydrogen from hydrogen-containing gas, while the 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 mixed with water steam, which is then subjected to steam catalytic conversion at a temperature 800-1050 °C in a radial-spiral reactor, the resulting converted gas is supplied as a heating medium to a steam recovery boiler for partial cooling, catalytic steam conversion of carbon monoxide is carried out in a radial-spiral 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 supplied to a hydrogen-containing gas separation unit, in which the final product - commercial hydrogen - is isolated, and the purge gas is removed from the hydrogen-containing gas separation unit gas and mixed with a second stream of hydrocarbon gas purified from sulfur, the resulting mixture is supplied as fuel gas to the burner of the catalytic reactor for hydrocarbon conversion, and before supplying the burner, this mixture and the air necessary for combustion are heated in a heat recovery unit due to partial cooling of the flue gases, coming out of the catalytic hydrocarbon conversion reactor, after which the flue gases, to separate moisture, are additionally cooled with an external coolant in the flue gas cooler-dryer and removed from the installation, and the condensate released in the cooler-driers of hydrogen-containing gas and flue gases is subjected to purification in the unit water treatment and sent to produce steam necessary for steam conversion of hydrocarbons to a hydrogen recovery steam boiler (invention patent RU 2394754, IPC COIB 3/34, С01В 3/12, declared 03/26/2009, published 07/20/2010 .). The disadvantages of the invention are:

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

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

• inappropriate use of part of the hydrotreated raw material as fuel when cheaper and less valuable types of fuel are available.

A method for producing hydrogen from hydrocarbon raw materials, including mixing the raw materials with an oxidizing agent, predominantly oxygen, and partial oxidation of the raw materials in the combustion chamber of a flow-through cooled reactor to produce a vapor-gas mixture containing hydrogen, carbon monoxide and 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 carrying out two-stage steam catalytic conversion of carbon monoxide followed by the release of hydrogen, while previously purified from sulfur impurities hydrocarbon raw materials are heated, moistened with water vapor and mixed with an oxidizer, partial oxidation of the raw materials is carried out at a pressure in the combustion chamber of 6.0-7.0 MPa, the heat of the steam-gas mixture is used to heat the raw materials and produce water steam, steam catalytic conversion of carbon monoxide is carried out on a single catalytic composition using the same Cu-Zn-cement-containing catalyst in three stages, with the first stage of conversion 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 stages of conversion are carried out at a 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 sequentially cooling the gas mixture to a temperature of 50-60 °C with separation of water condensate, and then further cooling the gas mixture to a temperature of 15-18 °C with separation of carbon dioxide condensate (invention patent 2643542, IPC COIB 3/02, С01В 3/26 , С01В 3/36, declared 11/11/2016, published 02/02/2018). The disadvantages of the invention are:

• lack of detail on the method for purifying hydrocarbon raw materials from organosulfur impurities, which significantly affects the efficiency of the process as a whole;

• use of pure oxygen or air enriched with oxygen as an oxidizer, which requires the construction of an additional installation for the production of oxygen;

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

Also known is the method closest to the claimed invention for producing hydrogen at an absolute pressure of at least about 400 kPa, including supply to the steam reforming zone with partial oxidation of 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 0.4: 1 to 0.6:1 and the presence of steam in a molar ratio to carbon in the feedstock in an amount of at least approximately 4 :1; maintaining in this zone conditions for reforming with partial oxidation, including the specified pressure, providing partial oxidation of a portion of the feedstock with the generation of heat, as well as reforming a portion of the feedstock with the generation of hydrogen, resulting in the output stream of the reformate product containing hydrogen, carbon monoxide and carbon dioxide; cooling the reformate effluent stream by indirect heat exchange with a stream containing liquid water to produce a steam containing stream at a temperature of at least about 300 °C, which is recycled to the reforming zone with partial oxidation, at least about 40% of the steam in the feed mixture being generated due to the specified indirect heat exchange (patent for invention 2378188, IPC S01B 3/38, declared 05/25/2005, published 01/10/2010). The disadvantages of the invention are:

• excessively costly separation of hydrogen-containing gas into commercial hydrogen and purge gas in the pressure-cycle adsorption unit, since the content of impurities in the hydrogen-containing gas after the carbon monoxide steam reforming reactor and the 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 adsorbent, leading to significant losses of hydrogen with the stripping gas at the desorption stage.

DISCLOSURE OF INVENTION

When creating the invention, the task was to develop a highly efficient method for producing hydrogen, providing at the same time an increase in the yield of commercial hydrogen, a decrease energy and material intensity of production, as well as increasing its environmental friendliness.

The problem is solved due to the fact that the method of hydrogen production 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 initial raw material and the first hydrogen stream to produce a raw material stream, heating and purification of the raw material 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 raw material stream with water steam, heating the resulting mixture and feeding it into the reactor adiabatic preliminary reforming, mixing the resulting reaction mixture with water steam and heating it, followed by feeding it into a steam reforming furnace to produce synthesis gas, cooling and supplying the resulting synthesis gas to the carbon monoxide conversion reactor, cooling and separation of the converted synthesis gas with separation of process condensate, supply of cooled separated synthesis gas for two-stage purification with extraction of carbon dioxide using an aqueous solution of potash in an 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 is sent through the commercial park to consumers.

The proposed solution allows:

• expand the raw material base and, when implementing the method within the boundaries of the petrochemical cluster, involve the least valuable low-margin hydrocarbons in processing; • prevent coking of the catalyst by removing impurities of unsaturated hydrocarbons, while the conversion of organosulfur impurities into hydrocarbons increases the amount of converted raw materials 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;

• increase the conversion of feedstock in the adiabatic preliminary reforming reactor by increasing the residence time of the reaction mixture in this reactor due to the fractional supply of water steam to the adiabatic preliminary reforming reactor and to the steam reforming furnace;

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

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

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

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 circulation circuit of the hydrogen-containing gas appears, eliminating the passage of this hydrogen through the adiabatic preliminary 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.

It is recommended to load nickel-molybdenum or cobalt-molybdenum into the adiabatic pre-reforming reactor catalyst or catalyst based on noble metals or Group VIII metals or oxides of these metals.

It is advisable to load 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-magnesia or nickel-aluminum-magnesia or nickel-magnesia on a carrier of aluminum oxide or carbon into the reaction tubes of the steam reforming furnace or magnesium oxide or aluminum oxide-magnesia or thorium-magnesia to increase hydrocarbon conversion to 99%.

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

The generated water vapor is mixed with 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 coolant 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 as both a reagent and a coolant of the required parameters. It is advisable to load an iron-chromium oxide catalyst into the carbon monoxide conversion reactor, and to maintain the temperature in the reaction zone, cool it 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 completely purifying the 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 parallel with the potash purification absorber, followed by regeneration of the absorbent.

It is advisable to use the method of short-cycle adsorption (hereinafter referred to as PSA) at the second stage of synthesis gas purification, since it deeply purifies contaminated hydrogen obtained at high pressure and a temperature of 30-40 °C in the first stage of synthesis gas purification, and the regeneration of the adsorbent is ensured by the desorption of previously sorbed impurities when releasing pressure in the adsorber system, which significantly reduces the energy intensity of the process compared to adsorbent regeneration by increasing the temperature to 300-350 °C. Energy costs are also reduced due to the fact that the PSA strip gas is supplied to the steam reforming furnace as a fuel gas and/or to the fuel network, since the strip gas generated during adsorbent regeneration is a high-calorie fuel; in addition, there is no direct discharge of strip gas into the atmosphere improves the environmental performance of production. The environmental performance of production is also improved by extracting carbon dioxide from the flue gases of a steam reforming furnace using an aqueous solution of potash.

As an alternative, compression of the strip gas by PSA is provided, followed by purification from carbon dioxide using an aqueous solution of potash and/or other chemical and/or physical absorbents and supply to the steam reforming furnace as fuel gas and/or to the fuel network.

It is useful for carbon dioxide recovered from synthesis gas and/or flue gases and/or PSA strip gas to be used as a marketable product and/or disposed of, for example, by injection into waste oil fields to reduce greenhouse gas emissions into the atmosphere.

It is advisable at the second stage of synthesis gas purification to reduce the load on the PSA to use an additional refrigeration unit, 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 the synthesis gas, which will reduce the loading of 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, you can additionally use the glycol drying method.

LIST OF DRAWINGS

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

1-30 - pipelines;

101 - feedstock compressor;

102 - heating block;

103 - catalytic hydrogenation reactor;

104 - desulfurization reactor system;

105 - adiabatic preliminary reforming reactor;

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

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

107, 109 - cooling unit;

108 - carbon monoxide conversion reactor;

110 - separator;

AND 111 - absorber;

112 - regenerator;

113 - adsorber system;

114 - pump;

115 - water vapor generation system;

116 - hydrogen recirculation compressor.

BRIEF DESCRIPTION OF THE DRAWINGS

The main natural gas is supplied through pipeline 1 to the feedstock compressor 101 to increase the pressure, after which it is sent through pipeline 2 to be mixed with a small amount of product hydrogen supplied through pipeline 27 from the hydrogen recirculation compressor 116. The mixture of compressed natural gas and hydrogen is first through pipeline 3 is supplied to the heating unit 102 and then sequentially passes through pipeline 4 and pipeline 5 through the catalytic hydrogenation reactor 103 and the desulfurization reactor system 104, where the conversion of sulfur compounds of the feed stream into hydrogen sulfide with its subsequent removal and hydrogenation of unsaturated hydrocarbons occurs. Through pipeline 6, the purified raw material stream is sent for mixing with water vapor supplied through pipeline 12 from the steam generation system 115, and subsequent supply through pipeline 7 to the flue gas heat recovery unit of the steam reforming furnace 106/1. The superheated mixture through pipeline 8 enters the adiabatic preliminary reforming reactor 105 to convert hydrocarbons C2 and higher into methane, after which it passes sequentially through pipeline 11 into the flue gas heat recovery unit of the steam reforming furnace 106/1 and through pipeline 13 into the reactor block of the steam reforming furnace reforming 106/2. The resulting synthesis gas is supplied 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 supplied through pipeline 17 for separation condensed water vapor into the PO separator. The separated process condensate follows pipeline 19 to pump 114, which is pumped through pipeline 28 into the water vapor generation system 115. The cooled separated synthesis gas is supplied through pipeline 18 for potash purification from carbon dioxide into absorber 111, where regenerated absorbent is supplied via pipeline 22. The purified stream through pipeline 20 is supplied to the adsorber system 113 to release hydrogen. The saturated absorbent is supplied through pipeline 21 to the regenerator 112, from where the captured carbon dioxide is removed through pipeline 23. The product hydrogen removed through pipeline 24 from the adsorber system 113 is divided: the first part through pipeline 25 is removed for further use, and the second part through pipeline 26 is supplied to the hydrogen recirculation compressor 116 for mixing with compressed natural gas. To obtain steam, demineralized water is supplied through pipeline 29 to the steam generation system 115, 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 water steam, part of which is removed through pipeline 10 is involved in the steam reforming process through pipeline 12, while excess water vapor is exported through pipeline 30.

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

Claims

CLAIM 1 A method for producing hydrogen, including increasing the pressure of the feedstock in the form of natural gas using compressor equipment and/or liquefied hydrocarbon gases (LPG) and/or light gasoline and/or hydrocarbon mixtures using pumping equipment, mixing the feedstock and the first hydrogen stream with the production of a raw material stream, heating and purification of the raw material 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 raw material stream with water steam, heating the resulting mixture and feeding it into the adiabatic preliminary reforming reactor, mixing the resulting reaction mixture with water vapor and its heating with subsequent supply to the steam reforming furnace to produce synthesis gas, cooling and supply of the resulting synthesis gas to the carbon monoxide conversion reactor, cooling and separation of the converted synthesis gas with separation of process condensate, supply of cooled separated synthesis -gas for two-stage purification with the extraction of carbon dioxide using an aqueous solution of potash in an 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, dividing the resulting hydrogen into two streams: the first are sent for mixing with the feedstock before the catalytic hydrogenation reactor, and the second is sent through the commercial park to consumers. 2 Method according to claim 1, characterized in that the liquid feedstock is pre-collected and compounded. 3 The method according to claim 1, characterized in that to remove impurities of sulfur compounds from the raw material 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, unwanted impurities of chlorine compounds and/or heavy metals are removed from the raw material stream by adsorption on a solid absorbent. 5 The method according to claim 1, characterized in that the purified raw material stream is cooled and separated from hydrogen-containing gas, which is then sent to the first stage of synthesis gas purification. 6 The method according to claim 1, characterized in that a nickel-molybdenum or cobalt-molybdenum catalyst or a catalyst based on noble metals or group VIII metals or oxides of these metals is loaded into the adiabatic preliminary reforming reactor. 7 The method according to claim 1, characterized in that 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-magnesia or nickel-aluminum-magnesia or nickel-magnesia on a carrier of aluminum oxide or carbon or magnesium oxide or aluminum oxide-magnesia or thorium-magnesia. 8 The method according to claim 1, characterized in that the heat of the flue gases of the steam reforming furnace is used to heat the feedstock and/or purified feed stream and/or process streams before entering the adiabatic pre-reforming reactor and/or into the reaction tubes of the steam reforming furnace and /or for generating steam and/or for heating boiler feed water and/or for heating air supplied as an oxidizer to the steam reforming furnace. 9 The method according to claim 1, characterized in that when the synthesis gas is cooled after the steam reforming furnace, water vapor is generated and/or the boiler feed water is heated and/or the feedstock is heated. 10 Method according to claim 8 or claim 9, characterized in that the generated water vapor is mixed with process streams and involved in the process adiabatic pre-reforming and/or steam reforming and/or conversion of carbon monoxide and/or used to generate electrical energy and/or used as a coolant for heating process streams, including for the regeneration of 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. And the Method according to claim 1, characterized in that an iron-chromium oxide catalyst is loaded into the carbon monoxide conversion reactor. 12 The method according to claim 1, characterized in that to maintain the temperature in the reaction zone in the carbon monoxide conversion reactor, cooling is used with boiler feed water or another refrigerant. 13 The method according to claim 1, characterized in that at the first stage of synthesis gas purification, absorption is additionally carried out 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. 14 The method according to claim 1, characterized in that at the second stage of synthesis gas purification the method of short-cycle adsorption (hereinafter referred to as PSA) is used. 15 The method according to claim 14, characterized in that the PSA strip gas is supplied to the steam reforming furnace as fuel gas and/or to the fuel network. 16 The method according to claim 15, characterized in that an aqueous solution of potash is used to extract carbon dioxide from the flue gases of a steam reforming furnace. 17 The method according to claim 14, characterized in that the PSA strip gas is first compressed and then purified from carbon dioxide using an aqueous solution of potash and/or other chemical and/or physical absorbents. 16 18 The method according to claim 17, characterized in that the purified compressed PSA strip gas is supplied to the steam reforming furnace as fuel gas and/or to the fuel network. 19 The method according to claim 1 or claim 16 or claim 17, characterized in that carbon dioxide extracted from synthesis gas and/or flue gases and/or PSA strip gas is used as a commercial product and/or utilized. 20 The method according to claim 14, characterized in that at the second stage of synthesis gas purification an additional refrigeration unit is used. 21 The method according to claim 1, characterized in that at the second stage of synthesis gas purification the glycol drying method is additionally used. 17