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WO2025068673A1 - Procédé de synthèse de méthanol avec préparation et traitement de gaz de synthèse optimisés - Google Patents

Procédé de synthèse de méthanol avec préparation et traitement de gaz de synthèse optimisés Download PDF

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Publication number
WO2025068673A1
WO2025068673A1 PCT/GB2024/052276 GB2024052276W WO2025068673A1 WO 2025068673 A1 WO2025068673 A1 WO 2025068673A1 GB 2024052276 W GB2024052276 W GB 2024052276W WO 2025068673 A1 WO2025068673 A1 WO 2025068673A1
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gas
unit
methanol
hydrogen
synthesis
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Kar Chi YIU
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Johnson Matthey Davy Technologies Ltd
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Johnson Matthey Davy Technologies Ltd
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Priority claimed from GBGB2314964.4A external-priority patent/GB202314964D0/en
Priority claimed from GBGB2316095.5A external-priority patent/GB202316095D0/en
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Publication of WO2025068673A1 publication Critical patent/WO2025068673A1/fr
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/1516—Multisteps
    • C07C29/1518—Multisteps one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis
    • 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
    • C01B3/382—Multi-step processes
    • 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
    • C01B3/48—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 followed by reaction of water vapour with carbon monoxide
    • 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
    • C01B3/501—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by diffusion
    • 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
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
    • C07C29/78—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by condensation or crystallisation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
    • C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
    • C07C31/02—Monohydroxylic acyclic alcohols
    • C07C31/04—Methanol
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0244—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being an autothermal reforming step, e.g. secondary reforming processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/061—Methanol production
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0822—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel the fuel containing hydrogen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas

Definitions

  • This invention relates to a process for synthesising methanol, in particular a process for synthesising methanol with low emissions of carbon dioxide from the process.
  • Methanol synthesis is generally performed by passing a synthesis gas comprising hydrogen and carbon monoxide and/or carbon dioxide at an elevated temperature and pressure through one or more beds of a methanol synthesis catalyst, which is often a copper-containing composition, in a synthesis reactor.
  • a crude methanol is generally recovered by cooling the product gas stream to below the dew point and separating off the product as a liquid.
  • the crude methanol is typically purified by distillation.
  • the process is often operated in a loop: thus unreacted gas may be recycled to the synthesis reactor as part of the feed gas via a circulator.
  • Fresh synthesis gas termed makeup gas, is added to the recycled unreacted gas to form the feed gas stream.
  • a purge stream is taken from the circulating gas stream to avoid the build-up of inert gasses in the loop.
  • W02023/180114 discloses a process for the co-production of ammonia and methanol with reduced carbon dioxide emission comprising the steps of (a) providing a hydrocarbon feed stock; (b) preheating the hydrocarbon feed stock in a fired heater and/or a reformer waste heat section; (c) steam reforming the preheated hydrocarbon feed stock in at least one steam re- former to a raw synthesis gas comprising hydrogen and carbon oxides where the module M is ⁇ 2.05; (d) splitting the raw synthesis gas into a first and second stream; (e) passing the first stream of the raw synthesis gas to water gas shift section comprising one or more shift reactors for generating a shifted synthesis gas; (f) passing the shifted synthesis gas to a carbon dioxide removal section for generating a carbon dioxide depleted synthesis gas; (g) cleaning the carbon depleted synthesis gas in a cleaning unit to a cleaned synthesis gas comprising hydrogen or hydrogen and nitrogen, optionally adding nitrogen to the cleaned synthesis gas to generate an ammonia
  • WO2012/069821 (A1) describes removing a purge stream from a methanol synthesis loop, separating hydrogen from the purge stream, passing the purge stream to a reformer, carrying out shift, separating out the hydrogen from carbon dioxide and supplying the separated hydrogen to the synthesis loop.
  • the carbon-rich stream or tail gas
  • the carbon-rich stream is used as a fuel and combusted to heat feeds for the process, or in the generation of steam.
  • the tail gas contains carbon-containing compounds, such as methane, the combustion of the purge gas leads to CO2 emissions from the process.
  • a portion of the syngas may be advantageously used as a source of hydrogen to fire the heaters with tail gas recycled to the process. This avoids the need for additional reforming equipment in producing hydrogen for use as fuel and provides a simpler means to manage the purge gas duty.
  • the invention provides a process for synthesising methanol comprising the steps of (i) reforming a feed gas comprising a hydrocarbon in a hydrocarbon reforming unit comprising a fired heater and an autothermal reformer in series to form a synthesis gas containing hydrogen, carbon monoxide and carbon dioxide; (ii) dividing the synthesis gas into a first portion and a second portion, (iii) converting the first portion of synthesis gas into a methanol product in a methanol synthesis unit comprising one or more methanol synthesis reactors; and (iv) recovering a purge gas stream from the methanol synthesis unit, wherein the second portion of synthesis gas is passed to a hydrogen production unit where it is subjected to one or more stages of water gas shift in a water-gas shift unit to form a hydrogen-enriched gas, the a hydrogen-enriched gas is subjected to a step of carbon dioxide removal in a carbon dioxide removal unit to form a hydrogen product stream and a carbon dioxide stream, the carbon dioxide stream
  • This process may be established in a new methanol synthesis unit, or an existing methanol synthesis unit may be retrofitted with a hydrogen production unit comprising a water-gas shift unit and a carbon dioxide removal unit and means to recover carbon dioxide and feed a hydrogen stream recovered from the carbon dioxide removal unit to the fired heater as a fuel.
  • the second portion of synthesis gas is fed through a carbon dioxide unit that separates CO2 and other gases from the hydrogen product, it is possible to pass a portion of the purge gas stream and/or a portion of the off gas from the hydrogen recovery unit to the feed gas for processing without building up unwanted inerts in the synthesis loop in the methanol synthesis unit.
  • a portion of the off gas stream is combined with the feed gas and in some arrangements a portion of the purge gas stream is combined with the feed gas.
  • Methanol is recovered from one or more of the product gas mixtures. This may be achieved by cooling one or more of the methanol product gas streams to below the dew point, condensing methanol, and separating a crude liquid methanol product from the unreacted gases.
  • the second methanol synthesis reactor may be a cooled reactor selected from a tube cooled converter (TCC) and a gas-cooled converter (GCC).
  • TCC tube cooled converter
  • GCC gas-cooled converter
  • the first and second methanol synthesis reactors may be connected in series in which case the synthesis gas fed to the second methanol synthesis reactor comprises at least a portion of a methanol product gas stream recovered from the first methanol synthesis reactor.
  • the synthesis gas fed to the second methanol synthesis reactor comprises all of the methanol product gas stream recovered from the first methanol synthesis reactor.
  • Particularly preferred methanol synthesis units are described in US7790775, W02017/121980 A1 and WO2017/121981 A1.
  • the methanol synthesis catalysts in each of the methanol synthesis reactors may be the same or different.
  • the methanol synthesis catalysts are preferably copper-containing methanol synthesis catalysts, which are commercially available.
  • the methanol synthesis catalysts are one or more particulate copper/zinc oxide/alumina catalysts, which may comprise one or more promoters.
  • Particularly suitable catalysts are Mg-promoted copper/zinc oxide/alumina catalysts as described in US4788175 and SiC>2-doped copper/zinc oxide/alumina catalysts as described in WO2020/212681 A1.
  • Methanol synthesis may be effected in the one or more methanol synthesis reactors at pressures in the range 10 to 120 bar abs, and temperatures in the range 130°C to 350°C.
  • the pressures at the one or more reactor inlets is preferably 50-100 bar abs, more preferably 70-90 bar abs.
  • the temperature of the synthesis gas at the one or more reactor inlets is preferably in the range 200- 250°C and at the one or more reactor outlets preferably in the range 230-280°C.
  • the portion of the unreacted gas mixture making up the recycle gas stream will typically be at a lower pressure than the make-up gas and so preferably the recycle gas stream is compressed by one or more compressors or circulators. At least one compressor is used to circulate the unreacted gas stream.
  • the resulting compressed recycle gas stream may be mixed with make-up gas to form the feed to the one or more methanol synthesis reactors.
  • the crude liquid methanol recovered from the methanol synthesis unit contains water, along with small amounts of higher alcohols and other impurities.
  • the crude methanol may first be fed to a flash column or let-down vessel, where dissolved gases are released and separated from the crude liquid methanol stream.
  • the crude liquid methanol may also be subjected to one or more purification stages including one or more, preferably two or three, stages of distillation in a methanol purification unit comprising one, two or more distillation columns.
  • the de-gassing stage and distillation stages may be heated using heat recovered from the process, for example in the cooling of a product gas stream, or by other sources.
  • Preferably at least a portion of the crude methanol is purified by distillation to produce a purified methanol product.
  • Dissolved gases released from the flash column or let-down vessel and one or more purification stages may be recycled back to the hydrocarbon reforming unit, methanol synthesis unit or directly to the hydrogen production unit.
  • the purified methanol product may be subjected to further processing, for example to produce derivatives such as dimethyl ether or formaldehyde.
  • the methanol may be used as a fuel.
  • a portion of the unreacted gas mixture separated from the crude liquid methanol is removed from the loop as the purge gas stream.
  • the purge gas stream is preferably removed continuously to prevent the unwanted build-up of inert gases, such as nitrogen, argon and methane in the synthesis loop.
  • the purge gas stream may be recovered from the separated unreacted gases before or after compression in the circulator.
  • the purge gas stream may comprise 50-90% by volume of hydrogen and one or more of carbon monoxide, carbon dioxide, nitrogen, argon and methane.
  • the purge gas is supplied to a hydrogen recovery unit that separates a hydrogen stream.
  • the separated hydrogen stream may contain at least 80% by volume, preferably at least 90% by volume of H2.
  • the hydrogen recovery units are known and may be selected from a membrane separation unit, a pressure-swing absorption unit or a cryogenic separation unit.
  • the separated hydrogen may be added to the first portion of synthesis gas fed to the methanol synthesis unit to improve the stoichiometry of the synthesis gas.
  • the hydrogen recovery unit also produces an off-gas or carbon-rich tail gas.
  • the off-gas or carbon-rich tail gas may be recycled to the feed gas comprising hydrocarbon that is subjected to autothermal reforming.
  • the purge gas stream may contain methanol and so, if desired, upstream of the hydrogen recovery unit, methanol may optionally be recovered from the purge gas stream using a water wash, and the recovered methanol and water sent for purification with the crude methanol.
  • a portion of the purge gas, orwashed purge gas, and/or a portion of the hydrogen product stream recovered from the hydrogen production unit may be used to strip dissolved gases from the crude methanol and the resulting enriched hydrogen fed to the inlet of the compressor feeding the first portion of synthesis gas to the methanol synthesis unit.
  • the second portion of synthesis gas is passed to a hydrogen production unit where it is subjected to one or more stages of water gas shift in a water-gas shift unit to form a hydrogen-enriched gas, and a step of carbon dioxide removal from the hydrogen-enriched gas in a carbon dioxide removal unit to form a hydrogen product stream and a carbon dioxide stream.
  • the carbon dioxide stream is recovered and may be stored or used to synthesis additional methanol or other chemical products. At least a portion of the hydrogen product stream is fed to the fired heater as a fuel.
  • a portion of the hydrogen product stream may be combined with the first portion of synthesis gas fed to the methanol synthesis unit.
  • the invention may therefore include installation into an existing methanol synthesis unit a hydrogen production unit comprising one or more water-gas shift reaction vessels configured to provide a hydrogen-enriched gas, a carbon dioxide removal unit configured to provide a hydrogen stream and a carbon dioxide stream, and means to convey at least a portion of the hydrogen stream to the fired heater as a fuel.
  • the second portion of synthesis gas is subjected to one or more stages of water-gas shift in a water- gas shift unit.
  • Steam is necessary for the water-gas shift reaction. If insufficient steam is present in the synthesis gas, steam may be added upstream of the water gas shift unit, e.g. by direct addition.
  • the second portion of the synthesis gas may be passed through one or more beds of water-gas shift catalyst in one or more shift vessels to generate hydrogen and thus produce a hydrogen- enriched, or “shifted”, synthesis gas.
  • the water gas shift unit converts carbon monoxide in the second portion of the synthesis gas to carbon dioxide.
  • the reaction may be depicted as follows;
  • the one or more water-gas shift stages may include stages of high-temperature shift, mediumtemperature shift, isothermal shift and low-temperature shift.
  • High-temperature shift may be operated adiabatically in a shift vessel at inlet temperatures in the range 300-400°C, preferably 320-360°C, over a bed of a reduced iron catalyst, such as chromia- promoted magnetite.
  • a potassium promoted zinc-aluminate catalyst may be used.
  • a single stage of high-temperature shift may be used in the present invention.
  • a combination of high-temperature and medium- temperature or low-temperature shift may be used.
  • Medium-temperature shift and low-temperature shift stages may be performed using shift vessels containing supported copper-catalysts, particularly copper/zinc oxide/alumina compositions.
  • a gas containing carbon monoxide (preferably ⁇ 6% vol CO on a dry basis) and steam (at a steam to total dry gas molar ratio in range 0.3 to 1 .5) may be passed over the catalyst in an adiabatic fixed bed with an outlet temperature in the range 200 to 300°C.
  • the outlet carbon monoxide content may be in the range 0.1 to 1.5%, especially under 0.5% vol on a dry basis if additional steam is added.
  • the gas containing carbon monoxide and steam may be fed to the catalyst at an inlet temperature in the range 200 to 240°C although the inlet temperature may be as high as 280°C.
  • the outlet temperature may be up to 300°C but may be as high as 360°C.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

L'invention concerne un procédé de synthèse de méthanol comprenant les étapes consistant à (i) reformer une charge d'alimentation hydrocarbonée dans une unité de reformage d'hydrocarbures comprenant un dispositif de chauffage à combustion et un reformeur autothermique en série pour former un gaz de synthèse contenant de l'hydrogène, du monoxyde de carbone et du dioxyde de carbone ; (ii) diviser le gaz de synthèse en une première partie et une seconde partie, (iii) convertir la première partie de gaz de synthèse en un produit de méthanol dans une unité de synthèse de méthanol comprenant un ou plusieurs réacteurs de synthèse de méthanol ; et (iv) récupérer un flux de gaz de purge provenant de l'unité de synthèse de méthanol, la seconde partie de gaz de synthèse étant transmise à une unité de production d'hydrogène où elle est soumise à une ou plusieurs étapes de conversion eau-gaz dans une unité de conversion eau-gaz pour former un gaz enrichi en hydrogène, le gaz enrichi en hydrogène est soumis à une étape d'élimination de dioxyde de carbone dans une unité d'élimination de dioxyde de carbone pour former un flux de produit d'hydrogène et un flux de dioxyde de carbone, le flux de dioxyde de carbone est récupéré et au moins une partie du flux de produit d'hydrogène est introduite dans le dispositif de chauffage à combustion en tant que carburant.
PCT/GB2024/052276 2023-09-29 2024-09-02 Procédé de synthèse de méthanol avec préparation et traitement de gaz de synthèse optimisés Pending WO2025068673A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
GB2314964.4 2023-09-29
GBGB2314964.4A GB202314964D0 (en) 2023-09-29 2023-09-29 Process for synthesising methanol
GB2316095.5 2023-10-20
GBGB2316095.5A GB202316095D0 (en) 2023-10-20 2023-10-20 Process for synthesising methanol

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WO2025068673A1 true WO2025068673A1 (fr) 2025-04-03

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Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4788175A (en) 1985-08-30 1988-11-29 Imperial Chemical Industries Plc Catalyst
US7790775B2 (en) 2004-08-20 2010-09-07 Davy Process Technology Limited Process for use in gas phase reactions
WO2012069821A1 (fr) 2010-11-24 2012-05-31 Davy Process Technology Limited Procédé d'amélioration de la teneur en hydrogène d'un gaz de synthèse
WO2017121980A1 (fr) 2016-01-15 2017-07-20 Johnson Matthey Davy Technologies Limited Procédé méthanol
WO2017121981A1 (fr) 2016-01-15 2017-07-20 Johnson Matthey Davy Technologies Limited Procédé de synthèse de méthanol
WO2020212681A1 (fr) 2019-04-15 2020-10-22 Johnson Matthey Public Limited Company Catalyseurs contenant du cuivre, de l'oxyde de zinc, de l'alumine et de la silice
WO2020249923A1 (fr) 2019-06-12 2020-12-17 Johnson Matthey Davy Technologies Limited Procédé de synthèse de méthanol
GB2614780A (en) * 2021-11-17 2023-07-19 Johnson Matthey Plc Method for retrofitting a hydrogen production unit
WO2023180114A1 (fr) 2022-03-21 2023-09-28 Topsoe A/S Procédé de co-production d'ammoniac et de méthanol à teneur réduite en carbone

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2619796B (en) * 2022-05-09 2024-06-12 Johnson Matthey Davy Technologies Ltd Process for synthesising methanol

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4788175A (en) 1985-08-30 1988-11-29 Imperial Chemical Industries Plc Catalyst
US7790775B2 (en) 2004-08-20 2010-09-07 Davy Process Technology Limited Process for use in gas phase reactions
WO2012069821A1 (fr) 2010-11-24 2012-05-31 Davy Process Technology Limited Procédé d'amélioration de la teneur en hydrogène d'un gaz de synthèse
WO2017121980A1 (fr) 2016-01-15 2017-07-20 Johnson Matthey Davy Technologies Limited Procédé méthanol
WO2017121981A1 (fr) 2016-01-15 2017-07-20 Johnson Matthey Davy Technologies Limited Procédé de synthèse de méthanol
WO2020212681A1 (fr) 2019-04-15 2020-10-22 Johnson Matthey Public Limited Company Catalyseurs contenant du cuivre, de l'oxyde de zinc, de l'alumine et de la silice
WO2020249923A1 (fr) 2019-06-12 2020-12-17 Johnson Matthey Davy Technologies Limited Procédé de synthèse de méthanol
GB2614780A (en) * 2021-11-17 2023-07-19 Johnson Matthey Plc Method for retrofitting a hydrogen production unit
WO2023180114A1 (fr) 2022-03-21 2023-09-28 Topsoe A/S Procédé de co-production d'ammoniac et de méthanol à teneur réduite en carbone

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