US20140291162A1 - METHOD AND SYSTEM FOR TREATING CARBON GASES BY ELECTROCHEMICAL HYDROGENATION IN ORDER TO OBTAIN A CxHyOz COMPOUND - Google Patents

METHOD AND SYSTEM FOR TREATING CARBON GASES BY ELECTROCHEMICAL HYDROGENATION IN ORDER TO OBTAIN A CxHyOz COMPOUND Download PDF

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Publication number
US20140291162A1
US20140291162A1 US14/350,837 US201214350837A US2014291162A1 US 20140291162 A1 US20140291162 A1 US 20140291162A1 US 201214350837 A US201214350837 A US 201214350837A US 2014291162 A1 US2014291162 A1 US 2014291162A1
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Prior art keywords
electrolyser
heating means
treating
cathode
proton
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US14/350,837
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English (en)
Inventor
Béatrice Sala
Frédéric Grasset
Olivier Lacroix
Abdelkader Sirat
Elodie Tetard
Kamal Rahmouni
Joel Mazoyer
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Areva SA
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Areva SA
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    • C25B3/04—
    • 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
    • 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
    • C25B3/00—Electrolytic production of organic compounds
    • C25B3/20—Processes
    • C25B3/25—Reduction
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/202—Hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/502—Carbon monoxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • 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
    • B01D53/32—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 electrical effects other than those provided for in group B01D61/00
    • B01D53/326—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 electrical effects other than those provided for in group B01D61/00 in electrochemical cells
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
    • 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
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • the present invention relates to a method and a system for treating carbon gases—carbon dioxide (CO 2 ) and/or carbon monoxide (CO)—from very reactive hydrogen generated by electrolysis of water in order to obtain a CxH y O z type compound, particularly where x ⁇ 1; 0 ⁇ y ⁇ (2x+2) and 0 ⁇ z ⁇ 2x.
  • CO 2 carbon dioxide
  • CO carbon monoxide
  • Conductive ceramic membranes are today the subject of wide-spread research to enhance their performances; notably, said membranes find particularly interesting applications in the fields:
  • the production method illustrated in FIG. 1 , uses an electrolyte capable of conducting protons and operating at temperatures generally comprised between 200° C. and 800° C.
  • FIG. 1 schematically represents an electrolyser 10 comprising a proton-conducting ceramic membrane 11 assuring the function of electrolyte separating an anode 12 and a cathode 13 .
  • H + ions or OH o . in the Kröger-Vink notation migrate through the electrolyte 11 , to form hydrogen H 2 on the surface of the cathode 13 according to the equation:
  • this method provides at the outlet of the electrolyser 10 pure hydrogen ⁇ cathodic compartment—and oxygen mixed with steam ⁇ anodic compartment.
  • H 2 goes through the formation of intermediate compounds which are hydrogen atoms adsorbed on the surface of the cathode with variable energies and degrees of interaction and/or radical hydrogen atoms H. (or H Electrode X in the Kröger-Vink notation). These species being highly reactive, they normally recombine to form hydrogen H 2 according to the equation:
  • the aim of the invention is to reclaim the carbon gases resulting for example from the production of heating from carbon products (coal, wood, oil), or the incineration of waste, and to reduce in an optimal manner the production of greenhouse gases for carrying out the treatment by hydrogenation.
  • the invention proposes a method for treating CO 2 and/or CO by electrochemical hydrogenation in order to obtain a C x H y O z type compound, where x ⁇ 1; 0 ⁇ y ⁇ (2x+2) and z is comprised between 0 and 2x, said CO 2 and/or CO being obtained by the combustion of carbon products via heating means ( 160 ), said method comprising:
  • Reactive hydrogen atoms are taken to mean atoms absorbed on the surface of the cathode and/or radical hydrogen atoms H (or H Electrode X in the Kröger-Vink notation).
  • the method according to the invention makes it possible to recycle the carbon gases produced by heating means resulting from the combustion of carbon products by using jointly the electrolysis of steam, which generates highly reactive hydrogen at the cathode of the electrolyser, with an electrocatalysed hydrogenation of the carbon products injected at the cathode of the electrolyser by reaction with highly reactive hydrogen.
  • said CxH y Oz type compounds are paraffins C n H 2n+2 , olefins C 2n H 2n , alcohols C n H 2n+2 OH or C n H 2n ⁇ 1 OH, aldehydes and ketones C n H 2n O.
  • the CxH y Oz compounds produced are compounds making it possible to supply the combustion of heating means so as to reduce the external input of carbon products.
  • the compounds formed are carbon product fuels, such as for example aliphatics or aromatics belonging to the family of alkanes, alkenes or alkynes, substituted or not, being able to include one or more alcohol, aldehyde, ketone, acetal, ether, peroxide, ester, anhydride functions.
  • the invention also makes it possible to use advantageously the heat produced by the heating means (resulting from the combustion of carbon products) to heat the proton-conducting electrolyser, the heating of the electrolyser being required to carry out the electrolysis reaction and the electrocatalysed hydrogenation reaction.
  • the electrolyser does not require the use of specific costly heating means, generating greenhouse gases.
  • the method according to the invention may also have one or more of the characteristics below, considered individually or according to any technically possible combinations thereof:
  • the subject matter of the invention is also a system for treating carbon gases by electrochemical hydrogenation for the implementation of the method according to the invention, said system comprising:
  • the heating means are formed of a boiler.
  • FIG. 1 is a simplified schematic representation of a proton-conducting steam electrolyser
  • FIG. 2 is a schematic representation of a system for treating carbon gases produced by a boiler during the combustion of carbon products
  • FIG. 3 is a general simplified schematic representation of an electrolysis cell for the implementation of the method according to the invention.
  • FIG. 2 schematically represents a system for treating carbon gases 100 enabling the implementation of the method according to the invention.
  • the treatment system 100 comprises:
  • the means 34 for inducing a current circulating between the anode 32 and the cathode 34 may be a voltage, current generator or a potentiostat (in this case, the cell will also comprise at least one reference cathodic or anodic electrode).
  • FIG. 3 illustrated in a more detailed manner an embodiment example of an electrolysis cell 30 of the electrolyser 110 used to form CxH y Oz type compounds (where x ⁇ 1, 0 ⁇ y ⁇ (2x+2) and 0 ⁇ z ⁇ 2x) after the reduction of the CO 2 and/or the CO.
  • the water is oxidised while releasing electrons while H + ions (in OH o . form) are generated.
  • H + ions migrate through the electrolyte 31 and are thus capable of reacting with different compounds that could be injected at the cathode 33 , carbon compounds of CO 2 and/or CO type reacting at the cathode 33 with said H + ions to form C x H y O z type compounds (where x ⁇ 1, 0 ⁇ y ⁇ (2x+2) and 0 ⁇ z ⁇ 2x) and water at the cathode 33 .
  • the nature of the CxH y O z compounds synthesized at the cathode 33 depends on numerous operating parameters such as, for example, the pressure of the cathodic compartment, the partial pressure of the gases, the operating temperature T1, the couple potential/current/voltage applied at the cathode 33 or at the terminals of the electrolyser, the dwell time of the gas and the nature of the electrodes.
  • the operating temperature T1 of the electrolyser is comprised in the range between 200 and 800° C., advantageously between 350° C. and 650° C.
  • the operating temperature T1 in this range of temperature is also going to depend on the nature of the CxH y Oz carbon compounds that it is wished to generate.
  • the hydrogen/CxH y Oz compound mixture has the advantage of aiding the combustion of the CxH y O z compound in the heating means.
  • the operating parameters are defined so as to obtain a mixture formed of 90% CxH y Oz compound and 10% hydrogen.
  • the anode 32 and the cathode 33 are preferentially formed of a cermet constituted of the mixture of a proton-conducting ceramic and an electron-conducting passivable alloy that is able to form a protective oxide layer so as to protect it in an oxidising environment (i.e. at the anode of an electrolyser).
  • Said passivable alloy is preferentially a metal alloy.
  • the passivable alloy comprises for example chromium (and preferentially at least 40% of chromium) so as to have a cermet having the particularly of not oxidising at temperature.
  • the chromium content of the alloy is determined such that the melting point of the alloy is above the sintering temperature of the ceramic.
  • Sintering temperature is taken to mean the sintering temperature required to sinter the electrolyte membrane so as to make it leak tight to gas.
  • the chromium alloy may also comprise a transition metal so as to retain an electron-conducting character of the passive layer.
  • the chromium alloy is an alloy of chromium and one of the following transition metals: cobalt, nickel, iron, titanium, niobium, molybdenum, tantalum, tungsten, etc.
  • the ceramic of the anodic and cathodic 32 and 33 electrodes is advantageously the same ceramic as that used by the formation of the electrolytic membrane of the electrolyte 31 .
  • the proton-conducting ceramic used by the formation of the cermet of the electrodes 32 and 33 and the electrolyte 31 is a perovskite of zirconate type of generic formula AZrO 3 being able to be doped advantageously by an element A selected from lanthanides.
  • the use of this type of ceramic for the formation of the membrane thus requires the use of a high sintering temperature in order to obtain a sufficient densification to be leak tight to gas.
  • the sintering temperature of the electrolyte 31 is more particularly defined as a function of the nature of the ceramic but also as a function of the desired porosity level. Conventionally, it is estimated that to be leak tight to gas, the electrolyte 31 has to have a porosity level below 6% (or a density above 94%).
  • the sintering of the ceramic is carried out under a reducing atmosphere so as to avoid the oxidation of the metal at high temperature, i.e. under an atmosphere of hydrogen (H 2 ) and argon (Ar), or even carbon monoxide (CO) if there is no risk of carburation.
  • a reducing atmosphere so as to avoid the oxidation of the metal at high temperature, i.e. under an atmosphere of hydrogen (H 2 ) and argon (Ar), or even carbon monoxide (CO) if there is no risk of carburation.
  • the electrodes 32 and 33 of the cell 30 are also sintered at a temperature above 1500° C. (according to the example of sintering of a ceramic of zirconate type).
  • the anode 32 and the cathode 33 may also be formed of a ceramic material which is a perovskite doped with a lanthanide.
  • the perovskite may be a zirconate of formula AZrO 3 .
  • the zirconate is doped with a lanthanide, which is for example erbium.
  • the perovskite doped with lanthanide is doped with a doping element taken from the following group: niobium, tantalum, vanadium, phosphorous, arsenic, antimony, bismuth.
  • doping elements are chosen to dope the ceramic because they can go from a degree of oxidation equal to 5 to a degree of oxidation of 3, which makes it possible to release oxygen during sintering. More specifically, the doping element is preferably niobium or tantalum. Each electrode may also comprise a metal mixed with the ceramic so as to form a cermet. The ceramic comprises for example between 0.1% and 0.5% by weight of niobium, between 4 and 4.5% by weight of erbium and the remainder zirconate. The fact of doping the ceramic with niobium, tantalum, vanadium, phosphorous, arsenic, antimony or bismuth makes it possible to render the ceramic conductive to electrons.
  • the ceramic is then a ceramic with mixed conduction; in other words, it is conducting both to electrons and protons whereas in the absence of said doping elements, perovskite doped with a lanthanide with a single degree of oxidation is not conducting to electrons.
  • perovskite doped with a lanthanide with a single degree of oxidation is not conducting to electrons.
  • the system 100 further comprises a condenser 130 receiving at the inlet the CxH y O z compound synthesized at the cathode 33 of the electrolyser 110 .
  • the condenser 130 makes it possible to separate the CxH y O z compound in the gaseous state and the water that are produced by the hydrogenation reaction.
  • the condenser 130 traps the water in liquid form making it possible to obtain at the outlet of the condenser 130 uniquely the synthesized CxH y O z compound in the gaseous state (carbon compound fuel in the embodiment example illustrated in FIG. 2 ).
  • the CxH y O z compound is then injected into the carbon product supply circuit of the boiler 160 after dehydration in a desiccant cartridge 170 .
  • the input of the synthesized CxH y O z compound makes it possible to reduce the specific input of carbon products.
  • the system according to the invention thus makes it possible to operate in semi-closed circuit, the external input of fuel being reduced by the supply of the boiler with synthesized CxH y O z compound.
  • the water recovered in the condenser 130 is then re-injected into the water supply circuit so as to limit external inputs of water.
  • the system 100 also comprises a condenser 140 receiving at the inlet the oxygen produced by electrolysis of steam at the anode 31 .
  • the oxygen being mixed with water at the outlet of the electrolyser 110 , the condenser 140 makes it possible to separate oxygen from water.
  • the oxygen is then re-injected into the boiler 160 to supply the combustion of the carbon products, and the water is re-injected into the water supply circuit.
  • the oxygen thereby injected makes it possible to carry out an oxycombustion using directly the oxygen coming out of the electrolyser as oxidant instead of air.
  • the condensers 130 and 140 also have the function of cooling the compounds entering into the condensers so as to re-inject into the different circuits of the system 100 compounds cooled to a temperature comprised between 80 and 85° C.
  • the heating of the electrolyser 110 is carried out by heat transfer from the boiler 160 to the electrolyser 110 such that the electrolyser reaches the temperature T1 not less than 200° C. and not more than 800° C., advantageously comprised between 350° C. and 650° C.
  • the temperature T1 of the electrolyser must be advantageously comprised between 500° C. and 600° C.
  • the heat transfer is achieved by positioning the electrolyser 110 in a heat area 150 around the boiler 160 .
  • the heat transfer is achieved by means of a heat exchanger (not represented) making it possible to transfer the thermal energy produced by the boiler to the electrolyser.
  • the system further comprises a turbine positioned at the outlet of the electrolyser, and more specifically at the anodic (steam) and/or cathodic outlet of the electrolyser.
  • a turbine is illustrated as an example in dotted line by the reference 50 .
  • the turbine is positioned in the path of the gaseous flux coming out at the anode of the electrolyser.
  • Such a turbine is adapted to generate electricity by the passage of the gaseous flux.
  • the electricity produced then makes it possible to electrically supply the electrolyser.
  • this particular embodiment makes it possible to reduce the electrical consumption of a specific generator to generate a potential difference at the terminals of the electrolyser.
  • the system according to the invention comprises thermo-electrical devices advantageously placed so as to recover the heat from the products formed by the water electrolysis reaction.
  • the system comprises a heat exchanger adapted to cool the oxygen/water mixture generated at the anode by the electrolysis reaction and to heat the water at the inlet of the electrolyser so as to form steam able to be inserted into the electrolyte via the anode.
  • the invention finds a particularly interesting application for reclaiming carbon gases resulting for example from the production of heating from carbon products (coal, wood, oil), or the incineration of wastes.

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  • Chemical & Material Sciences (AREA)
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  • Materials Engineering (AREA)
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US14/350,837 2011-10-12 2012-10-11 METHOD AND SYSTEM FOR TREATING CARBON GASES BY ELECTROCHEMICAL HYDROGENATION IN ORDER TO OBTAIN A CxHyOz COMPOUND Abandoned US20140291162A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR1159223A FR2981369B1 (fr) 2011-10-12 2011-10-12 Procede et systeme de traitement de gaz carbones par hydrogenation electrochimique pour l'obtention d'un compose de type cxhyoz
FR1159223 2011-10-12
PCT/FR2012/052319 WO2013054053A2 (fr) 2011-10-12 2012-10-11 Procédé et système de traitement de gaz carbonés par hydrogénation électrochimique pour l'obtention d'un composé de type cxhyoz

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US (1) US20140291162A1 (enExample)
EP (1) EP2766514A2 (enExample)
JP (1) JP2014528519A (enExample)
CN (1) CN104024479A (enExample)
BR (1) BR112014008751A2 (enExample)
FR (1) FR2981369B1 (enExample)
IN (1) IN2014DN03032A (enExample)
RU (1) RU2014118837A (enExample)
WO (1) WO2013054053A2 (enExample)

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WO2018170243A1 (en) * 2017-03-16 2018-09-20 Battelle Energy Alliance, Llc Methods and systems for carbon dioxide hydrogenation
US10208665B2 (en) * 2012-02-20 2019-02-19 Thermogas Dynamics Limited Methods and systems for energy conversion and generation
WO2019070526A1 (en) * 2017-10-02 2019-04-11 Battelle Energy Alliance, Llc METHODS AND SYSTEMS FOR ELECTROCHEMICAL REDUCTION OF CARBON DIOXIDE USING SWITCHABLE POLARITY MATERIALS
WO2019197514A1 (en) 2018-04-13 2019-10-17 Haldor Topsøe A/S A method for generating synthesis gas for use in hydroformylation reactions
WO2019197515A1 (en) 2018-04-13 2019-10-17 Haldor Topsøe A/S A method for generating gas mixtures comprising carbon monoxide and carbon dioxide for use in synthesis reactions
EP3670705A1 (en) * 2018-12-21 2020-06-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Carbon dioxide conversion process
US11286573B2 (en) 2018-03-22 2022-03-29 Kabushiki Kaisha Toshiba Carbon dioxide electrolytic device and method of electrolyzing carbon dioxide
US11851774B2 (en) 2021-03-18 2023-12-26 Kabushiki Kaisha Toshiba Carbon dioxide electrolytic device
US11905173B2 (en) 2018-05-31 2024-02-20 Haldor Topsøe A/S Steam reforming heated by resistance heating
US11946150B2 (en) 2018-09-19 2024-04-02 Kabushiki Kaisha Toshiba Electrochemical reaction device
US12214327B2 (en) 2018-05-31 2025-02-04 Haldor Topsøe A/S Endothermic reactions heated by resistance heating
US12227414B2 (en) 2019-10-01 2025-02-18 Haldor Topsøe A/S On demand hydrogen from ammonia
US12246964B2 (en) 2019-10-01 2025-03-11 Haldor Topsøe A/S On demand hydrogen from methanol
US12246298B2 (en) 2019-10-01 2025-03-11 Haldor Topsøe A/S Offshore reforming installation or vessel
US12246299B2 (en) 2019-11-12 2025-03-11 Haldor Topsøe A/S Electric steam cracker
US12246970B2 (en) 2019-10-01 2025-03-11 Haldor Topsøe A/S Cyanide on demand
US12246965B2 (en) 2019-10-01 2025-03-11 Haldor Topsøe A/S On demand synthesis gas from methanol
US12410054B2 (en) 2019-10-01 2025-09-09 Haldor Topsøe A/S Synthesis gas on demand

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FR3007425B1 (fr) * 2013-06-20 2016-07-01 Ifp Energies Now Nouveau procede de fabrication d'acide formique
CN111683731B (zh) * 2018-02-12 2022-09-02 朗泽科技有限公司 用于提高碳转化效率的工艺
CN110311161B (zh) * 2019-06-21 2022-04-08 大连理工大学 一种膜法调控电化学氢泵co2加氢反应器中阴极电势的方法

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FR2931168B1 (fr) * 2008-05-15 2010-07-30 Areva Procede de production de composes du type cxhyoz par reduction de dioxyde de carbone (co2) et/ou de monoxyde de carbone (co)
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US10208665B2 (en) * 2012-02-20 2019-02-19 Thermogas Dynamics Limited Methods and systems for energy conversion and generation
WO2018170243A1 (en) * 2017-03-16 2018-09-20 Battelle Energy Alliance, Llc Methods and systems for carbon dioxide hydrogenation
US20220372638A1 (en) * 2017-03-16 2022-11-24 Battelle Energy Alliance, Llc Carbon dioxide hydrogenation systems
US10975477B2 (en) 2017-10-02 2021-04-13 Battelle Energy Alliance, Llc Methods and systems for the electrochemical reduction of carbon dioxide using switchable polarity materials
WO2019070526A1 (en) * 2017-10-02 2019-04-11 Battelle Energy Alliance, Llc METHODS AND SYSTEMS FOR ELECTROCHEMICAL REDUCTION OF CARBON DIOXIDE USING SWITCHABLE POLARITY MATERIALS
US11286573B2 (en) 2018-03-22 2022-03-29 Kabushiki Kaisha Toshiba Carbon dioxide electrolytic device and method of electrolyzing carbon dioxide
WO2019197514A1 (en) 2018-04-13 2019-10-17 Haldor Topsøe A/S A method for generating synthesis gas for use in hydroformylation reactions
CN111971418A (zh) * 2018-04-13 2020-11-20 托普索公司 产生用于合成反应的包含co和co2的气体混合物的方法
WO2019197515A1 (en) 2018-04-13 2019-10-17 Haldor Topsøe A/S A method for generating gas mixtures comprising carbon monoxide and carbon dioxide for use in synthesis reactions
US12215432B2 (en) 2018-04-13 2025-02-04 Haldor Topsøe A/S Method for generating synthesis gas for use in hydroformylation reactions
US11905173B2 (en) 2018-05-31 2024-02-20 Haldor Topsøe A/S Steam reforming heated by resistance heating
US12214327B2 (en) 2018-05-31 2025-02-04 Haldor Topsøe A/S Endothermic reactions heated by resistance heating
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US12227414B2 (en) 2019-10-01 2025-02-18 Haldor Topsøe A/S On demand hydrogen from ammonia
US12246964B2 (en) 2019-10-01 2025-03-11 Haldor Topsøe A/S On demand hydrogen from methanol
US12246298B2 (en) 2019-10-01 2025-03-11 Haldor Topsøe A/S Offshore reforming installation or vessel
US12246970B2 (en) 2019-10-01 2025-03-11 Haldor Topsøe A/S Cyanide on demand
US12246965B2 (en) 2019-10-01 2025-03-11 Haldor Topsøe A/S On demand synthesis gas from methanol
US12410054B2 (en) 2019-10-01 2025-09-09 Haldor Topsøe A/S Synthesis gas on demand
US12246299B2 (en) 2019-11-12 2025-03-11 Haldor Topsøe A/S Electric steam cracker
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CN104024479A (zh) 2014-09-03
JP2014528519A (ja) 2014-10-27
BR112014008751A2 (pt) 2017-04-25
RU2014118837A (ru) 2015-11-20
IN2014DN03032A (enExample) 2015-05-08
FR2981369B1 (fr) 2013-11-15
WO2013054053A2 (fr) 2013-04-18
FR2981369A1 (fr) 2013-04-19
EP2766514A2 (fr) 2014-08-20
WO2013054053A3 (fr) 2013-06-13

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