EP4337601A1 - Procédé de conversion de co2 - Google Patents

Procédé de conversion de co2

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Publication number
EP4337601A1
EP4337601A1 EP22728965.9A EP22728965A EP4337601A1 EP 4337601 A1 EP4337601 A1 EP 4337601A1 EP 22728965 A EP22728965 A EP 22728965A EP 4337601 A1 EP4337601 A1 EP 4337601A1
Authority
EP
European Patent Office
Prior art keywords
production
rwgs
reactor
electrified
process according
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP22728965.9A
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German (de)
English (en)
Inventor
Luca Basini
Nicola MONDELLI
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Rosetti Marino SpA
Original Assignee
Rosetti Marino SpA
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Filing date
Publication date
Application filed by Rosetti Marino SpA filed Critical Rosetti Marino SpA
Publication of EP4337601A1 publication Critical patent/EP4337601A1/fr
Pending legal-status Critical Current

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Classifications

    • 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
    • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
    • C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide 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
    • C01B3/02—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
    • C01B3/386—Catalytic partial combustion
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/12—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon dioxide with hydrogen
    • 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
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/026—Increasing the carbon monoxide content, e.g. reverse water-gas shift [RWGS]
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/02—Hydrogen or oxygen
    • C25B1/04—Hydrogen or oxygen by electrolysis of water
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C25B15/081—Supplying products to non-electrochemical reactors that are combined with the electrochemical cell, e.g. Sabatier reactor
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/133—Renewable energy sources, e.g. sunlight

Definitions

  • the present invention concerns a process for the conversion of pure CO 2 or various gaseous streams containing CO 2 by using an Electrified Reverse Water Gas Shift (E-RWGS) reactor.
  • E-RWGS Electrified Reverse Water Gas Shift
  • the electrified reactors that can be expediently used in the process include, for example, resistance-heated reactors (Science 364, (2019), 756-759) and induction-heated reactors (Ind. Eng. Chem. Res., 56 (2017) 14006-14013).
  • the innovative process subject of the present invention refers to a solution for the transformation of gases containing CO 2 into gases containing carbon monoxide (CO) and hydrogen (H 2 ), molecules that provide the building blocks for important activities in the production of chemicals, fertilizers and fuels.
  • This solution therefore aims to help reduce the concentration of GHG (Greenhouse Gases) by removing and transforming their main component, CO 2 , and re- introducing it into the production cycle.
  • GHG Greenhouse Gases
  • thermodynamic as CO 2 is the end product of most human activities: i) those necessary for life (breathing emits one kilogram of CO 2 every day, equivalent to 2.5 billion tons emitted by the entire human race every year), ii) those dedicated to industrial processes for the production and use of energy, iii) those relating to chemical industry production. Overall these last two types of activity produce approximately 40.5 billion tons of CO 2 per year (see, for example https://www,ispionline.it/it//pubblica condominium/co2--da ⁇ --- spa-risorsa-29423) . However, this situation can be changed by defining specific solutions for the use of CO 2 emissions .
  • European Union (EU Green Deal https://ec .europa.eu/commission/presscorner/detail/it/IP_ 19_6691) targets the use of electrical energy produced from renewable sources via the electrolysis of water and therefore for the production and use of H 2 .
  • the reduction of GHG will have to take into consideration both the reduction of CO 2 emissions and separation and re-use of CO 2 .
  • CCS is therefore a transitional solution, suitable for specific contexts in which storage solutions are available and also the possibility of recovering the CO 2 from industrial emissions, which is not always feasible.
  • the Applicant believes that the CCU solutions in which the CO 2 is re-used in the production cycle are much more effective and widely applicable and, among other things, can be more effectively integrated with activities for the production and use of H 2 , in particular activities that produce it via water electrolysis processes.
  • the present invention therefore concerns a process for the conversion of pure CO 2 or various gaseous streams containing CO 2 by using chemical processes that include the use of an Electrified Reverse Water Gas Shift (E- RWGS) reactor.
  • E- RWGS Electrified Reverse Water Gas Shift
  • the innovative process subject of the present invention refers to a solution for converting gases containing CO 2 into gases containing carbon monoxide (CO) and hydrogen (H 2 ), molecules that provide the building blocks for important activities in the production of chemicals, fertilizers and fuels.
  • CO carbon monoxide
  • H 2 hydrogen
  • the present invention provides a process, as defined previously, in which transformation of the CO 2 that takes place in the E-RWGS reactor uses, as a reactant, H 2 produced by electrolysis processes or made available as a by-product from various industrial processes.
  • the present invention provides a process, as previously defined, in which the electricity necessary for the E-RWGS and/or electrolysis processes is produced from renewable sources.
  • the present invention provides a process, as defined previously, in which the E-RWGS reactor is integrated into process schemes: for the production of MeOH and its derivatives usable in the chemical and energy sectors;
  • SR Steam Reforming
  • ATR AutoThermal Reforming
  • CR Combined Reforming
  • CPO Catalytic Partial Oxidation
  • the E-RWGS reactor is operated at pressures between 10 and 100 atm (1.10 MPa and 10.13 MPa) and preferably at pressures between 30 and 80 atm (3.04 MPa and 8.11 MPa) and temperatures between 500 and 1000°C and preferably at temperatures between 650 and 950°C.
  • figure 1 illustrates a simplified block diagram that integrates the unitary operations of E-RWGS, production of H 2 via water electrolysis processes (Solid Oxide Electrolysis Cell - SOEC, Alkaline Electrolyzer - AE, Polymer Electrolyte Membrane Electrolyzer - PEME) and synthesis of MeOH according to the present invention
  • figure 2 illustrates a simplified block diagram that integrates the unitary operations of E-RWGS, production of H 2 via water electrolysis processes (Solid Oxide Electrolysis Cell - SOEC, Alkaline Electrolyzer - AE, Polymer Electrolyte Membrane Electrolyzer - PEME) and synthesis of liquid hydrocarbons via the Fischer-Tropsch process
  • figure 3 illustrates a simplified block diagram of the CAMERE process described in Ind.
  • figure 4 illustrates a simplified block diagram of a process that allows the production, from biogas, of Bio- CH 4 and MeOH obtained from renewable sources and which, except for the CO 2 produced to obtain electrical energy, is configured as a CO 2 negative emission process
  • figure 5 illustrates a simplified block diagram of a process that allows hydrogen to be obtained via the CPO (Catalytic Partial Oxidation) process and a stream of CO 2 which by means of the E-RWGS unit is converted into synthesis gas that is used in the production of MeOH; this process, except for the CO 2 produced to obtain electrical energy, is configured as a CO 2 negative emission process
  • figure 6 illustrates a simplified block diagram of a process that allows hydrogen to be obtained via the CPO process and a stream of CO 2 which by means of the E-RWGS unit is converted into a synthesis gas with the appropriate composition to obtain the production of liquid hydrocarbons via the Fischer-Tropsch synthesis and which, except for the CO 2 produced to obtain electrical energy
  • R-01 is the RWGS electrified reactor
  • HX-03 is the low temperature heat recovery exchanger
  • HX-01 is the RWGS reactor feed/product recuperator
  • V-01 is the first H 2 O separator
  • V-02 is the second H 2 O separator
  • HX-02 is the high pressure steam generator
  • HW High Pressure Boiler Feed Water
  • figure 8 shows a process flow diagram of the production process of Example 1, sheet 2, in which:
  • HX-05 is the MeOH product feed recuperator
  • R-02 is the MeOH synthesis reactor
  • HX-06 is the MeOH condenser
  • V-03 is the MeOH high pressure separator
  • V-04 is the MeOH low pressure separator
  • HW High Pressure Boiler Feed Water
  • the block diagram describes for example one of the innovative conceptual solutions subject of the present invention.
  • a gaseous stream containing CO 2 is mixed with hydrogen produced by an electrolyzer and is sent to an electrified reactor in which the E-RWGS reaction takes place so as to produce a mixture of syngas suitable for synthesis of the methanol .
  • Analogously figure 2 describes a process solution in which the E-RWGS reactor is integrated in a scheme in which liquid hydrocarbons are produced by means of Fischer-Tropsch (FT) synthesis. Also in this case, a gaseous stream containing the CO 2 is mixed with hydrogen produced electrolytically and sent to the E-RWGS reactor so as to obtain a syngas with a composition suited to the Fisher-Tropsch synthesis and therefore to the production of liquid hydrocarbons.
  • FT Fischer-Tropsch
  • the electrified reactors that can be expediently used in the process include the resistance-heated reactors in which the catalyst is heated by Joule effect as described, for example, in the article published in Science 364, (2019), 756-759.
  • This solution allows the radial temperature gradients through the catalyst layer to be significantly reduced, with much more effective transfer than in the SR thermal reactors - which use furnaces that are strong emitters of CO 2 - of the heat from the area where the strongly endothermic reactions occur, as in [6] below.
  • the electrified reactors that can be expediently used in the process of the present invention include induction- heated reactors which exploit the electromagnetic induction heating of an electrically conductive object through the heat generated inside the object itself by eddy currents.
  • This type of reactor is described for example in the publication Ind. Eng. Chem. Res., 56 (2017) 14006-14013, which experimentally demonstrates the possibility of carrying out the SR reactions in a reactor containing nickel-cobalt nanoparticle-based catalysts.
  • the co-component of the catalyst with a high Curie temperature is in this case able to transfer the necessary heat to the reaction environment.
  • Table 1 reports, in short, the comparison values between consumption and emissions per ton of methanol produced using: i) the Best Available Technologies (BAT) that use natural gas; ii) the CO 2 direct hydrogenation processes that use H 2 produced by electrolysis of H 2 O; iii) the methanol production processes with the process of the present invention in which an E- RWGS intermediate step is included (see Example 1) and H 2 produced by the electrolysis of H 2 O is used .
  • BAT Best Available Technologies
  • the process of the present invention offers a considerable advantage in terms of carbon efficiency values (moles of carbon introduced into the process/moles of carbon converted into MeOH) with respect to the production of MeOH obtained by direct hydrogenation of CO 2 using electrolytically produced hydrogen (also called E-MeOH processes) and also with respect to the production processes of MeOH from natural gas.
  • the process of the present invention also allows CO 2 emissions to be reduced by more than one order of magnitude compared to those of the other technological reference solutions.
  • the Energy Efficiency and Carbon Efficiency values are influenced mainly by the quantity and quality of electrical energy consumed in the electrolysis processes (see Example 1) and obviously make the technological solution more advantageous in contexts in which a surplus of electrical energy is used that would be otherwise difficult to use and/or in contexts in which renewable electrical energy is available.
  • the process of the present invention is compared with a known solution, developed from the end of the 1990s and called CAMERE (CO 2 Hydrogenation to form Methanol via a Reverse-Water-Gas-Shift Reaction; published in Ind. Eng. Chem. Res. 38 (1999) 1808-1812).
  • CAMERE CO 2 Hydrogenation to form Methanol via a Reverse-Water-Gas-Shift Reaction; published in Ind. Eng. Chem. Res. 38 (1999) 1808-1812.
  • the process, illustrated in Figure 3 is composed of two sections; in the first, a mixture containing CO 2 and H 2 enters a RWGS thermal reactor at approximately 500°C and 10 atm (1.01 MPa) producing CO and H 2 O according to the equation previously described [1].
  • the water is subsequently separated and 40% of the gaseous mixture is recycled, while the remaining 60% v/v, which must have a composition in which the ratio (H 2 -CO 2 )/(CO+CO 2 ) is approximately equal to 2 v/v, is sent to the following section for compression and then synthesis of the MeOH which in the CAMERE process is carried out at a temperature of 250°C and pressure of 30 atm (3.04 MPa).
  • the CAMERE process only reached the pilot plant stage and has never been developed on an industrial scale.
  • the RWGS thermal reactor should operate preferably at high temperature (above 700°C) and low pressure (below 15 atm) to discourage the methanation parasite reactions previously described in equations [4- 5].
  • the industrial thermal reactor would therefore require the use of a furnace that would use the combustion of hydrocarbons and which would therefore emit the very CO 2 that is intended to be converted.
  • the synthesis of MeOH is favoured by high pressures (P > 50 atm) and by relatively low reaction temperatures (approximately 250°C).
  • the syngas produced at low pressure in the RWGS would then have to be cooled and compressed, entailing a high energy expenditure.
  • the CAMERE process was tested, operating the RWGS thermal reactor at approximately 500°C and 10 atm and then compressing the synthesis gas obtained to 30 atm and carrying out synthesis of the MeOH at 250°C.
  • the hydrogen was produced from non-renewable sources.
  • the process, subject of the present invention clearly exceeds the limits of the known CAMERE process, using an E-RWGS reactor that can operate at high temperature, ranging from 650°C to 1000°C (in conditions that inhibit the methanation reaction [4-5]) and preferably between 700°C and 950°C and at high pressure ranging from 25 to 100 atm (2.53 MPa and 10.13 MPa) and preferably between 30 and 80 atm (3.04 MPa and 8.11 MPa).
  • the process subject of the present invention entails the use of sources of hydrogen (AE, SOEC, PEME) produced via hydrolysis processes that preferably use renewable energy or surplus of electrical energy or energy coming from other industrial processes that do not use hydrogen directly.
  • sources of hydrogen AE, SOEC, PEME
  • the process of the present invention also entails the possibility of using CO 2 separated from various hydrocarbon sources (for example biogas and acid gases) or obtained as a by-product of different industrial processes (for example those from which blue-hydrogen can be obtained).
  • hydrocarbon sources for example biogas and acid gases
  • obtained as a by-product of different industrial processes for example those from which blue-hydrogen can be obtained.
  • Figure 4 shows a diagram in which the stream of treated CO 2 comes from the biogas which in this way allows a stream of biomethane (Bio-CH 4 ) and Bio-MeOH to be obtained from renewable sources.
  • FIG. 4 allows a production of Bio-CH 4 and Bio-MeOH to be obtained with negative emissions of CO 2 except for that emitted in the production of electrical energy. If the latter is obtained completely or at least partly from renewable sources or if it is taken from a situation that produces it in excess, the scheme configures a process with negative emissions of CO 2 .
  • Figure 5 shows a simplified block diagram in which a production process of Blue-Hydrogen (like the one described in US2012/031391 A1 in which a stream of hydrogen and a high concentration stream of CO 2 is obtained) is integrated with a step of E-RWGS and synthesis of the MeOH.
  • Blue-Hydrogen like the one described in US2012/031391 A1 in which a stream of hydrogen and a high concentration stream of CO 2 is obtained
  • Figure 6 shows a simplified block diagram in which a production process of Blue-Hydrogen (like the one described in US2012/031391 A1), in which a current of hydrogen and a high concentration current of CO 2 is obtained, is integrated with a step of E-RWGS and Fischer Tropsch (F-T) synthesis of the liquid hydrocarbons.
  • Blue-Hydrogen like the one described in US2012/031391 A1
  • F-T Fischer Tropsch
  • the schemes of Figures 5 and 6 include, in particular, a technology of Catalytic Partial Oxidation (CPO)(the following pages include the references of 16 patents and 5 publications that describe the technology) with low contact time which allows the production of syngas without using pre-heating furnaces, therefore making the technology particularly suitable for confining all the CO 2 emissions within the process gas from which it can be entirely recovered.
  • CPO Catalytic Partial Oxidation
  • W02020058859 (Al), WO2016016257 (Al), WO2016016256 (Al), W02 016016253 (Al), W02016016251 (Al), WO 2011151082, WO 2009065559, WO 2011072877, US 2009127512, WO 2007045457, WO 2006034868, US 2005211604, WO 2005023710, WO 9737929, EP 0725038, EP 0640559;
  • SCT-CPO Short Contact Time Catalytic Partial Oxidation
  • the process exemplified combines flows of CO 2 coming from the biogas and green H 2 obtained via electrolysis, for the production of MeOH.
  • the syngas thus obtained is mixed with the recycle stream of the MeOH synthesis section and heated to 250°C before entering the MeOH synthesis reactor which operates at approximately 50 bar.
  • the reaction product is cooled to 25°C to separate the mixture of water and MeOH from the species that remain gaseous. 10% v/v of the gaseous stream is purged to avoid the accumulation of by-products (e.g. CH 4 ) while the remainder is recycled to the MeOH synthesis reactor.
  • the reactor operates at equilibrium at 950°C and 50 atm using a Ni/Al2C>3 catalyst and a gas hour space velocity (GHSV) equal to 5000 NL/(kg x hour).
  • the electrification of the reactor is designed with a 90% transfer efficiency of heat generated by Joule effect.
  • the generation of heat in situ in the reaction environment minimizes heat transfer limitations. This situation is obtained by using, for example, as a support in the catalytic bed, a FeCrAl monolith in the form of high resistivity knitted gauze on the surface of which the active phase is deposited.
  • the resistivity within the catalytic bed is maximized by dispersing the networks among ceramic materials that avoid electric short circuits and at the same time allow the reaction mixture to cross the catalytic bed.
  • the power load is obtained by minimizing the current flow using a low voltage and a high amperage.
  • the reactor operates at 50 bar and at an isothermal temperature of 250°C and was simulated as an equilibrium reactor with approach temperatures of 10°C.
  • the results of the simulation were compared with those of an industrial reactor that uses a commercial catalyst based on Cu/Zn0/Al 2 O 3 and that operates with a GHSV of 8,000 NL/ (kg x hour).
  • the purge on the recycle gas was obtained by inserting a Pressure Swing Adsorption (PSA) unit that allows 90% of the hydrogen to be recovered and re introduced into the synthesis loop.
  • PSA Pressure Swing Adsorption
  • Tables 2-9 include indications on the material and energy balances and on the main process conditions.
  • Table 10 includes the overall consumption of material and energy for two cases:
  • Case B 10% v/v of the recycle gas of the methanol synthesis loop is purged, 5.6% v/v of methane at the inlet, 7.1% v/v of methane at the outlet. The purge is burnt to produce thermal energy which is used by an Organic Rankine Cycle.

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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)
  • General Chemical & Material Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Mram Or Spin Memory Techniques (AREA)
  • Gasification And Melting Of Waste (AREA)

Abstract

La présente invention concerne un procédé de conversion de CO2, pur ou contenu dans des courants gazeux de divers types par l'intermédiaire de l'utilisation d'un réacteur E-RWGS (conversion eau-gaz inverse chauffée électriquement). Plus spécifiquement, le procédé innovant objet selon la présente invention porte sur une solution pour la conversion de gaz contenant du CO2 en gaz contenant du monoxyde de carbone (CO) et de l'hydrogène (H2), des molécules qui fournissent les blocs de construction pour des activités importantes dans la production de produits chimiques, d'engrais et de carburants.
EP22728965.9A 2021-05-14 2022-05-10 Procédé de conversion de co2 Pending EP4337601A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IT102021000012551A IT202100012551A1 (it) 2021-05-14 2021-05-14 Processo per la conversione della co2
PCT/IB2022/054338 WO2022238899A1 (fr) 2021-05-14 2022-05-10 Procédé de conversion de co2

Publications (1)

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EP4337601A1 true EP4337601A1 (fr) 2024-03-20

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IT (1) IT202100012551A1 (fr)
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WO2023194286A1 (fr) * 2022-04-08 2023-10-12 Topsoe A/S Rénovation de boucle de production méthanol par co-intensification

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WO2016016256A1 (fr) 2014-07-29 2016-02-04 Eni S.P.A. Procédé intégré d'oxydation catalytique partielle à temps de contact court/reformage autotherme (sct-cpo/atr) pour la production de gaz de synthèse
WO2016016257A1 (fr) 2014-07-29 2016-02-04 Eni S.P.A. Procédé intégré d'oxydation catalytique partielle à temps de contact court pour la production de gaz de synthèse
WO2016161998A1 (fr) * 2015-04-08 2016-10-13 Sunfire Gmbh Procédé et installation de production de méthane/d'hydrocarbures gazeux et/ou liquides
DE102018210303A1 (de) * 2018-06-25 2020-01-02 Siemens Aktiengesellschaft Elektrochemische Niedertemperatur Reverse-Watergas-Shift Reaktion
US11492315B2 (en) 2018-09-19 2022-11-08 Eni S.P.A. Process for the production of methanol from gaseous hydrocarbons
WO2021063796A1 (fr) * 2019-10-01 2021-04-08 Haldor Topsøe A/S Gaz de synthèse à la demande à partir de méthanol

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