WO2023229491A2 - Procédé de production d'hydrogène - Google Patents
Procédé de production d'hydrogène Download PDFInfo
- Publication number
- WO2023229491A2 WO2023229491A2 PCT/RU2023/000130 RU2023000130W WO2023229491A2 WO 2023229491 A2 WO2023229491 A2 WO 2023229491A2 RU 2023000130 W RU2023000130 W RU 2023000130W WO 2023229491 A2 WO2023229491 A2 WO 2023229491A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- gas
- hydrogen
- synthesis gas
- purification
- stage
- Prior art date
Links
- 239000001257 hydrogen Substances 0.000 title claims abstract description 70
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 70
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 56
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 24
- 239000007789 gas Substances 0.000 claims abstract description 91
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 43
- 238000000034 method Methods 0.000 claims abstract description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 40
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 39
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 39
- 238000000746 purification Methods 0.000 claims abstract description 38
- 238000006243 chemical reaction Methods 0.000 claims abstract description 34
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 29
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 29
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 29
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 27
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 26
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 22
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 21
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 20
- 239000000203 mixture Substances 0.000 claims abstract description 19
- 239000012535 impurity Substances 0.000 claims abstract description 18
- 238000002407 reforming Methods 0.000 claims abstract description 18
- 239000002250 absorbent Substances 0.000 claims abstract description 14
- 230000002745 absorbent Effects 0.000 claims abstract description 14
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 14
- 238000002156 mixing Methods 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims abstract description 13
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims abstract description 11
- 239000006096 absorbing agent Substances 0.000 claims abstract description 11
- 229940072033 potash Drugs 0.000 claims abstract description 11
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 claims abstract description 11
- 235000015320 potassium carbonate Nutrition 0.000 claims abstract description 11
- 239000003345 natural gas Substances 0.000 claims abstract description 9
- 238000009903 catalytic hydrogenation reaction Methods 0.000 claims abstract description 8
- 238000001035 drying Methods 0.000 claims abstract description 5
- 238000005086 pumping Methods 0.000 claims abstract description 5
- 229930195735 unsaturated hydrocarbon Natural products 0.000 claims abstract description 5
- 239000003915 liquefied petroleum gas Substances 0.000 claims abstract description 4
- 239000011541 reaction mixture Substances 0.000 claims abstract description 4
- 239000003502 gasoline Substances 0.000 claims abstract description 3
- 238000000629 steam reforming Methods 0.000 claims description 31
- 239000002994 raw material Substances 0.000 claims description 24
- 238000001816 cooling Methods 0.000 claims description 16
- 239000003054 catalyst Substances 0.000 claims description 15
- 238000010438 heat treatment Methods 0.000 claims description 15
- 239000003546 flue gas Substances 0.000 claims description 14
- 239000000395 magnesium oxide Substances 0.000 claims description 12
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 12
- 239000003463 adsorbent Substances 0.000 claims description 11
- 230000008929 regeneration Effects 0.000 claims description 10
- 238000011069 regeneration method Methods 0.000 claims description 10
- 239000000446 fuel Substances 0.000 claims description 9
- 238000001179 sorption measurement Methods 0.000 claims description 9
- 239000007864 aqueous solution Substances 0.000 claims description 8
- 229910052751 metal Inorganic materials 0.000 claims description 8
- 239000002184 metal Substances 0.000 claims description 8
- 150000002739 metals Chemical class 0.000 claims description 8
- 150000003464 sulfur compounds Chemical class 0.000 claims description 7
- 239000002826 coolant Substances 0.000 claims description 5
- 238000006477 desulfuration reaction Methods 0.000 claims description 5
- 230000023556 desulfurization Effects 0.000 claims description 5
- 239000002737 fuel gas Substances 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 5
- 239000007800 oxidant agent Substances 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 4
- 238000010521 absorption reaction Methods 0.000 claims description 4
- 238000000605 extraction Methods 0.000 claims description 4
- 229910000510 noble metal Inorganic materials 0.000 claims description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 2
- QEFDIAQGSDRHQW-UHFFFAOYSA-N [O-2].[Cr+3].[Fe+2] Chemical compound [O-2].[Cr+3].[Fe+2] QEFDIAQGSDRHQW-UHFFFAOYSA-N 0.000 claims description 2
- 229910052782 aluminium Inorganic materials 0.000 claims description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 2
- 150000001412 amines Chemical class 0.000 claims description 2
- 150000001805 chlorine compounds Chemical class 0.000 claims description 2
- WHDPTDWLEKQKKX-UHFFFAOYSA-N cobalt molybdenum Chemical compound [Co].[Co].[Mo] WHDPTDWLEKQKKX-UHFFFAOYSA-N 0.000 claims description 2
- KYYSIVCCYWZZLR-UHFFFAOYSA-N cobalt(2+);dioxido(dioxo)molybdenum Chemical compound [Co+2].[O-][Mo]([O-])(=O)=O KYYSIVCCYWZZLR-UHFFFAOYSA-N 0.000 claims description 2
- 229910001385 heavy metal Inorganic materials 0.000 claims description 2
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 2
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 2
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 claims description 2
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 2
- 239000003507 refrigerant Substances 0.000 claims description 2
- 238000005057 refrigeration Methods 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- 229910002090 carbon oxide Inorganic materials 0.000 claims 1
- ZGDWHDKHJKZZIQ-UHFFFAOYSA-N cobalt nickel Chemical compound [Co].[Ni].[Ni].[Ni] ZGDWHDKHJKZZIQ-UHFFFAOYSA-N 0.000 claims 1
- 239000013065 commercial product Substances 0.000 claims 1
- 238000011084 recovery Methods 0.000 abstract description 8
- 230000007613 environmental effect Effects 0.000 abstract description 5
- 239000000463 material Substances 0.000 abstract description 5
- 239000005864 Sulphur Substances 0.000 abstract 1
- 238000005504 petroleum refining Methods 0.000 abstract 1
- -1 sulphur compound Chemical class 0.000 abstract 1
- 238000011144 upstream manufacturing Methods 0.000 abstract 1
- 230000003197 catalytic effect Effects 0.000 description 11
- 230000003647 oxidation Effects 0.000 description 7
- 238000007254 oxidation reaction Methods 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000003795 desorption Methods 0.000 description 3
- 238000009434 installation Methods 0.000 description 3
- 238000010926 purge Methods 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- QPLDLSVMHZLSFG-UHFFFAOYSA-N Copper oxide Chemical compound [Cu]=O QPLDLSVMHZLSFG-UHFFFAOYSA-N 0.000 description 2
- 239000005751 Copper oxide Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 229910000431 copper oxide Inorganic materials 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 239000011159 matrix material Substances 0.000 description 2
- 239000011787 zinc oxide Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000001193 catalytic steam reforming Methods 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- NVIVJPRCKQTWLY-UHFFFAOYSA-N cobalt nickel Chemical compound [Co][Ni][Co] NVIVJPRCKQTWLY-UHFFFAOYSA-N 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
Definitions
- 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.
- CO+H2O CO2+H2; allowing to obtain four molecules of hydrogen by reacting one molecule of methane with two molecules of water.
- hydrogen can be obtained from heavier paraffinic hydrocarbons contained in natural gas (ethane, propane, butane, etc.) and in light straight-run oil fractions.
- 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.
- 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 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
- 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.
- 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.
- 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.
- 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.
- PSA short-cycle adsorption
- 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.
- carbon dioxide recovered from synthesis gas and/or flue gases and/or PSA strip gas 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.
- 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.
- 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.
- 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.
- 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.
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Inorganic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
L'invention concerne un procédé de production d'hydrogène qui peut être utilisé dans les branches de l'industrie de transformation du pétrole et de l'industrie chimique du pétrole et du gaz pour la production d'hydrogène à tonnage élevé. Ce procédé de production d'hydrogène consiste à augmenter la pression de la matière première de départ consistant en du gaz naturel en utilisant un équipement de compression et/ou des gaz hydrocarbures liquéfiés (GHL) et/ou de l'essence légère et/ou des mélanges hydrocarbures en utilisant un équipement de pompage. On effectue un mélange de la matière première de départ et d'un premier flux d'hydrogène afin de produire un flux de matière première, on chauffe et on purifie le flux de matière première pour éliminer les impuretés de composés de soufre et d'hydrocarbures insaturés dans un réacteur catalytique d'hydrogénation et un système de réacteurs de désulfuration connectés en série. On effectue ensuite un mélange du flux de matière première purifié avec de la vapeur d'eau, on chauffe le mélange obtenu et on l'envoie dans un réacteur de reformage préliminaire adiabatique, on mélange le mélange de réaction obtenu avec de la vapeur d'eau et on le chauffe avant de l'envoyer dans un four de reformage de vapeur afin d'obtenir un gaz de synthèse. Le gaz de synthèse est refroidi puis envoyé dans un réacteur de conversion de monoxyde de carbone. On effectue un refroidissement et une séparation du gaz de synthèse converti afin de séparer le condensé industriel, et on envoie le gaz de synthèse séparé refroidi vers une purification en deux étapes. On extrait le dioxyde de carbone à l'aide d'une solution aqueuse de potasse dans un absorbeur lors de la première étape de purification, après quoi on régénère d'absorbeur et on le sèche. Lors de la seconde étape de purification, on extrait le monoxyde de carbone et autres impuretés dans un système d'adsorbeurs. L'hydrogène obtenu est divisé en deux flux: un premier envoyé en vue du mélange avec la matière première de départ en amont du réacteur d'hydrogénation catalytique, et le second vers les consommateurs via un parc de stockage. L'invention permet d'augmenter la production d'hydrogène, de réduire les coûts énergétique et en matériaux, d'améliorer le caractère écologique, et d'élargir la gamme des matières premières.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| RU2022111779 | 2022-04-29 | ||
| RU2022111779A RU2791358C1 (ru) | 2022-04-29 | Способ производства водорода |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| WO2023229491A2 true WO2023229491A2 (fr) | 2023-11-30 |
| WO2023229491A3 WO2023229491A3 (fr) | 2024-02-01 |
Family
ID=88919647
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PCT/RU2023/000130 WO2023229491A2 (fr) | 2022-04-29 | 2023-04-27 | Procédé de production d'hydrogène |
Country Status (1)
| Country | Link |
|---|---|
| WO (1) | WO2023229491A2 (fr) |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2088518C1 (ru) * | 1994-08-03 | 1997-08-27 | Акционерное общество Первоуральский новотрубный завод "Уралтрубсталь" | Способ получения водорода из углеводородного газа |
| RU2378188C2 (ru) * | 2004-05-28 | 2010-01-10 | Хайрадикс, Инк. | Способ получения водорода с использованием парового риформинга с частичным окислением |
| RU2379230C2 (ru) * | 2008-04-08 | 2010-01-20 | Борис Тихонович Плаченов | Способ получения водорода паро-углекислотной конверсией природного газа |
| RU2394754C1 (ru) * | 2009-03-26 | 2010-07-20 | Дмитрий Львович Астановский | Способ получения водорода из углеводородного сырья |
| CN103958398B (zh) * | 2011-09-27 | 2016-01-06 | 国际热化学恢复股份有限公司 | 合成气净化系统和方法 |
| US20210269307A1 (en) * | 2018-10-15 | 2021-09-02 | Haldor Topsøe A/S | Carbon recycling in steam reforming process |
-
2023
- 2023-04-27 WO PCT/RU2023/000130 patent/WO2023229491A2/fr unknown
Also Published As
| Publication number | Publication date |
|---|---|
| WO2023229491A3 (fr) | 2024-02-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| AU2018364702B2 (en) | Systems and methods for production and separation of hydrogen and carbon dioxide | |
| RU2394754C1 (ru) | Способ получения водорода из углеводородного сырья | |
| CN115943119A (zh) | 绿色氢气的氨裂解 | |
| US20080272340A1 (en) | Method for Producing Syngas with Low Carbon Dioxide Emission | |
| CN115667132A (zh) | 用于生产氢气的方法 | |
| CN115667131A (zh) | 用于制备氢气的方法 | |
| KR20240017359A (ko) | 이산화탄소 배출량을 낮추면서 증기 개질에 의해 순수 수소를 생산하기 위한 방법 및 플랜트 | |
| JP2008290927A (ja) | 有機ハイドライドを用いる水素精製法およびその装置 | |
| RU2791358C1 (ru) | Способ производства водорода | |
| AU2021286875B2 (en) | Method for the production of hydrogen | |
| RU2203214C1 (ru) | Способ получения метанола | |
| WO2023229491A2 (fr) | Procédé de production d'hydrogène | |
| RU2643542C1 (ru) | Способ получения водорода из углеводородного сырья | |
| JPH03242302A (ja) | 水素及び一酸化炭素の製造方法 | |
| KR20240021941A (ko) | NOx 제거를 이용한 그린 수소를 위한 암모니아 분해 | |
| KR20240021944A (ko) | 그린 수소를 위한 암모니아 분해 | |
| RU2729790C1 (ru) | Газохимическое производство водорода | |
| JP7122042B1 (ja) | パージ方法およびシステム | |
| CN211233617U (zh) | 一种用于处理气体混合物的装置 | |
| RU2786069C1 (ru) | Способ получения водорода из природного газа | |
| CN109609221B (zh) | 一种兰炭炉尾气精脱硫及等温甲烷化工艺 | |
| RU132442U1 (ru) | Установка для получения этилена | |
| WO2022253459A1 (fr) | Procédé et installation de production d'hydrogène pur par reformage à la vapeur avec réduction des émissions de dioxyde de carbone | |
| JP2024524089A (ja) | Ｎｏｘ除去を有するグリーン水素のためのアンモニア分解 | |
| WO2024134157A1 (fr) | Processus de production d'hydrogène |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| 121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 23812233 Country of ref document: EP Kind code of ref document: A2 |