EP4276223A1 - Betriebsart für kohlendioxyd-elektrolyse - Google Patents

Betriebsart für kohlendioxyd-elektrolyse Download PDF

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Publication number
EP4276223A1
EP4276223A1 EP22172254.9A EP22172254A EP4276223A1 EP 4276223 A1 EP4276223 A1 EP 4276223A1 EP 22172254 A EP22172254 A EP 22172254A EP 4276223 A1 EP4276223 A1 EP 4276223A1
Authority
EP
European Patent Office
Prior art keywords
pressure
electrochemical cell
phase boundary
cathode
mbar
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.)
Withdrawn
Application number
EP22172254.9A
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English (en)
French (fr)
Inventor
Maximilian Fleischer
Erhard Magori
Baran Sahin
Elfriede Simon
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Siemens Energy Global GmbH and Co KG
Original Assignee
Siemens Energy Global GmbH and Co KG
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Siemens Energy Global GmbH and Co KG filed Critical Siemens Energy Global GmbH and Co KG
Priority to EP22172254.9A priority Critical patent/EP4276223A1/de
Priority to PCT/US2023/066147 priority patent/WO2023220520A1/en
Publication of EP4276223A1 publication Critical patent/EP4276223A1/de
Withdrawn legal-status Critical Current

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    • 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
    • C25B1/23—Carbon monoxide or syngas
    • 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
    • C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
    • C25B11/02—Electrodes; Manufacture thereof not otherwise provided for characterised by shape or form
    • C25B11/03—Electrodes; Manufacture thereof not otherwise provided for characterised by shape or form perforated or foraminous
    • C25B11/031—Porous electrodes
    • C25B11/032—Gas diffusion electrodes
    • 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
    • C25B15/02—Process control or regulation
    • C25B15/023—Measuring, analysing or testing during electrolytic production
    • 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
    • C25B15/02—Process control or regulation
    • C25B15/023—Measuring, analysing or testing during electrolytic production
    • C25B15/025—Measuring, analysing or testing during electrolytic production of electrolyte parameters
    • 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
    • C25B3/01—Products
    • C25B3/03—Acyclic or carbocyclic hydrocarbons
    • 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
    • C25B3/01—Products
    • C25B3/07—Oxygen containing compounds
    • 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
    • C25B3/26—Reduction of carbon dioxide
    • 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
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
    • C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
    • C25B9/23—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms comprising ion-exchange membranes in or on which electrode material is embedded

Definitions

  • the present invention relates in general to a carbon dioxide (CO 2 ) electrolysis operation mode, and more specifically to an improved CO 2 reduction reaction (CO 2 RR) utilizing back pressure, and most specifically to a CO 2 RR electrochemical cell operation mode utilizing back pressure.
  • CO 2 carbon dioxide
  • CO 2 RR improved CO 2 reduction reaction
  • CO 2 RR has many beneficial aspects.
  • One aspect involves the clean generation of reaction products, such as hydrocarbons, alcohols, H 2 and/or CO, that then can be used to feed any of a variety of industrial, commercial, individual or common inputs such as factories, gas turbines, equipment, vehicles, etc., as well as repositories and other storage mediums, as well as ambient or polluted air.
  • Another aspect involves the consumption or destruction of greenhouse gas CO 2 , such as from CO 2 emitting industrial, commercial, individual or common sources such as factories, gas turbines, equipment, vehicles, etc., as well as repositories and other storage mediums, as well as ambient or polluted air.
  • Yet another aspect involves integration of CO 2 RR with renewable energy sources such as solar, wind, geothermal, etc., whereby the renewable energy sources provide the requisite electricity or E o to initiate or sustain the CO 2 RR.
  • Still another aspect involves combinations of two or more the above aspects, such as consuming CO 2 flue gas from a factory source while sustaining the CO 2 RR from electricity generated from solar panels on the factory roof and then storing or feeding the produced value-added reaction product, such as ethene or higher order hydrocarbons, for a desired use.
  • CO 2 RR, electrochemical cell and operation mode problems may include CO 2 reaction inefficiency and instability over time.
  • Some efforts to overcome these problems involve modifying the catalyst surface such that the CO 2 and its intermediary reactants are more strongly bounded on the catalyst.
  • Other efforts to overcome these problems involve modifying the cathode to optimize gas diffusivity, porosity, thickness, hydrophilicity, electrical conductivity, ionic conductivity, wettability, etc.
  • a CO 2 RR 2 comprising a three-phase boundary 14 having: a gaseous CO 2 diffused at least partially through a porous cathode 8, a solid catalyst 10 operatively associated with the cathode 8, and a catholyte 12 or membrane 16 in communication with the catalyst 10; a pressure controller 30 adapted to control the pressure in gas chamber 6 and consequently the back pressure (pressure difference between the gas feed chamber 6 and the catholyte chamber 12) within, at or near the three-phase boundary 14; and a reaction product of the CO 2 RR such as but not limited to hydrocarbons, alcohols, H 2 and/or CO.
  • an electrochemical cell 2 comprising: an inlet 4 through which gaseous CO 2 enters the electrochemical cell 2 and advances into a chamber 6; a porous cathode 8 through which the gaseous CO 2 in the chamber 6 can at least partially diffuse through; a solid catalyst 10 adhered to the cathode 8; a liquid catholyte 12 in fluid communication with the solid catalyst 10, wherein the gaseous CO 2 contained in the porous cathode 8 and the solid catalyst 10 and the liquid catholyte 12 collectively form a three-phase boundary 14; a membrane 16 that separates the cathode 8 from an anode 20 to prevent short circuiting of the electrochemical cell 2 while allowing cations to circulate between the liquid catholyte 12 and a liquid anolyte 18; an outlet 22 through which reaction product(s) of the CO 2 RR exits the electrochemical cell 2; a pressure sensor 24 arranged within, at or near the three-phase boundary 14 to detect the pressure in cathol
  • a CO 2 RR utilizing back pressure to control CO 2 dwell or occupation within, at or near a three-phase boundary and thereby control the CO 2 RR and desired reaction product(s) is provided.
  • the illustrated three-phase boundary comprises a gaseous CO 2 diffused at least partially through a porous cathode 8, a solid catalyst 10 operatively associated with the porous cathode 8, and a liquid (or solid polymer) catholyte 12 or membrane 16 in communication with the catalyst 10.
  • Establishing a back pressure, at or near the three-phase boundary 14 to 0 - 400 mbar and preferably to 30- 130 mbar is particularly suited for the efficient generation of hydrocarbon product(s).
  • Reaction products may include hydrocarbons (of either or both higher and lower order), alcohols, H 2 and/or CO. If no catholyte 12 is used, the catholyte 12 alkaline environment functionality may be achieved by membrane 16. Also in this catholyte-less configuration, the three-phase boundary 14 becomes the cathode 8, catalyst 10 and membrane 16, with membrane 16 liquidity source-able from the liquid anolyte 18 or other suitable liquid source associated with the cell 2.
  • an operation mode utilizing back pressure on a CO 2 RR electrochemical cell 2 is also provided.
  • the illustrated electrochemical cell 2 comprises a CO 2 inlet 4, a three-phase boundary 14 comprising a porous cathode 8 through which gaseous CO 2 is diffused, a solid catalyst 10 adhered to the cathode 8, a liquid catholyte 12 in fluid communication with the catalyst 10, as well as a membrane 16 that separates the cathode 8 from an anode 20 2 while allowing cations to circulate between the liquid catholyte 12 and a liquid analyte 18, along with a reaction product outlet 22.
  • a pressure sensor 24 is arranged within, at or near the three-phase boundary 14 to detect the pressure in catholyte chamber 12 within, at or near the three-phase boundary 14.
  • a pressure controller 30 is adapted to control the pressure in gas chamber 6 and consequently the pressure difference (back pressure) between gas chamber 6 and catholyte chamber 12. The pressure controller 30 maintains a pressure difference of 0 - 400 mbar and preferably 30 - 130 mbar between gas chamber 6 and catholyte chamber 12.
  • the electrochemical cell 2 has a CO 2 inlet 4 configured to receive CO 2 gas from any one or more of a variety of CO 2 sources, including without limitation, industrial, commercial, individual or common sources such as factories, gas turbines, equipment, vehicles, etc., as well as repositories and other storage mediums, as well as ambient or polluted air.
  • the CO 2 optionally may be conditioned before, within or after the inlet 4, such as by humidification via H 2 O or other suitable means.
  • Figure 1 exemplarily illustrates humidified CO 2 passing through the inlet 4 into a chamber 6 that holds and allows dispersion of the CO 2 .
  • no or more than one inlet 4 and no or more than one chamber 12 can be used, and any inlet(s) 4 and chamber(s) 6 used can be arranged at different location(s) on, along, or through the electrochemical cell 2.
  • a porous cathode 8 is arranged to receive the gaseous CO 2 and configured such that the CO 2 can diffuse through at least a portion of the cathode 8.
  • the exemplarily illustrated cathode 8 is a gas diffusion electrode (GDE) that absorbs and converts the CO 2 molecules into the desired CO 2 RR reaction product e.g. hydrocarbons, however other suitable cathodes 8 could be used.
  • GDE gas diffusion electrode
  • a solid catalyst 10 is operatively associated with the cathode 8 by any suitable means, such as drop casting, plating, doping, or spray coating to enhance reaction product selectivity as well as reaction efficiency and stability. Suitable catalysts 10 include but are not limited to Pt, Zn, Cu, Ag, Au, Pd and Sn. Since Cu is the only transition metal catalyst for CO 2 RR to value added C 2 + reaction products e.g. ethene, ethanol, propanol, Cu is therefore preferred but not required when desiring those reaction products.
  • a catholyte 12 is advantageously arranged in communication with the catalyst 10 to provide an alkaline environment close to the three-phase boundary 14 and thereby promoting CO 2 RR thermodynamically and kinetically when hydrocarbon reaction product(s) and/or a CO reaction product is desired.
  • the exemplarily illustrated catholyte 12 is an alkaline buffer liquid solution, such as potassium hydrogen carbonate, cesium hydrogen carbonate, rubidium hydrogen carbonate, lithium bicarbonate or potassium hydroxide, but the catholyte 12 may also be embodied as a solid polymer.
  • a three-phase boundary 14 is thereby formed by: (1) the gaseous CO 2 diffused at least partially through the cathode 8, (2) the solid catalyst 10 operatively associated with the cathode 8, and (3) the liquid (or solid polymer) catholyte 12 in communication with the catalyst 10.
  • Figure 1 provides a detailed illustration of the three-phase boundary, exemplary H+ and CO 2 reaction constituents, as well as exemplary desired and undesired CO 2 RR reaction products.
  • a membrane 16 optionally may be used to separate the cathode 8 from an anode 20 while allowing cations to circulate between the liquid catholyte 12 and a liquid anolyte 18.
  • exemplary suitable membranes 16 include sulfonated tetrafluoroethylene based fluoropolymer-copolymer (Nafion). If used, the anolyte 18 is advantageously an alkaline buffer solution to complete the ion circuitry of the electrochemical cell 2.
  • Exemplary suitable analytes 18 include H 2 O, OH-, H + and electrolyte associated cations and anions (e.g. Cs + and SO 4 -2 ).
  • the anode 60 material can be composed of Ir, Ni and/or Pt, where the anode would be responsible for O 2 evolving reaction and completing the ion circuit in the electrochemical cell by pumping H + to the cathode.
  • the membrane 16 preferably an anion exchange membrane 16 or a bipolar membrane 16 may be used to sustain the alkaline environment rather than or in addition to the catholyte 12.
  • the membrane 16 preferably an anion exchange membrane 16 or a bipolar membrane 16
  • the three-phase boundary 14 becomes the cathode 8, catalyst 10 and membrane 16, with membrane 16 liquidity source-able from the liquid anolyte 18 or other suitable liquid source associated with the cell 2.
  • a reaction product outlet 22 is configured to receive the reaction product, e.g. hydrocarbon gas, from the electrochemical cell 2 and feed the reaction product to any one or more use sources, including without limitation, industrial, commercial, individual or common sources such as factories, gas turbines, equipment, vehicles, etc., as well as repositories and other storage mediums, as well as ambient or polluted air.
  • the CO 2 reaction product optionally may be conditioned before, within or after the outlet 22, such as by liquifying (e.g. to form LNG particularly if methane is a reaction product). Unconditioned reaction products are exemplary shown as passing through the outlet 22.
  • no or more than one outlet 22 can be used, and any outlet(s) 22 used can be arranged at different location(s) on, along, or through the electrochemical cell 2.
  • a pressure sensor 24 is arranged in operative communication with the electrochemical cell 2 in order to detect pressure in catholyte chamber 12 within, at or near the three-phase boundary 14.
  • the exemplary embodiment shows the pressure sensor 24 arranged near the three-phase boundary 14, toward the middle of the catholyte 12 between the cathode 8 and membrane 16, however, depending on the desired reaction product(s), electrochemical cell 2 configuration, three-phase boundary 14 constituents, or a variety of other factors, the pressure sensor 24 may be arranged in any of a variety of locations within, at or near the three-phase boundary 14. Also, if the three-phase boundary 14 is expansive or geometrically complex, then pressure sensors 26, 28 advantageously may be used to better sense the three-phase boundary 14 pressure and control the CO 2 RR
  • An outlet pressure sensor 26 may be advantageously arranged within, at or near the outlet 22 in order to detect pressure within, at or near the outlet 22.
  • the exemplary illustration shows an outlet pressure sensor 26 arranged at the beginning of the outlet 22.
  • one or more optional outlet pressure sensors 26 could be arranged in any of a variety of locations within, at or near the outlet 22 to better sense the outlet pressure and control the CO 2 RR.
  • an inlet pressure sensor 28 may be arranged within, at or near the inlet 4 in order to detect CO 2 pressure within, at or near the inlet 4.
  • the exemplary illustration shows an optional inlet pressure sensor 28 arranged at the end of the inlet 4.
  • one or more optional outlet pressure sensors 28 could be arranged in any of a variety of locations within, at or near the inlet 4 to better sense the inlet pressure and control the CO 2 RR
  • a pressure controller 30 is arranged in operative communication with the pressure sensor(s) 24, 26 and/or optional pressure sensor 28 and is adapted to adjust pressure detected by the pressure sensor(s) 24, 26 and/or optional pressure sensor 28 in order to adjust the back pressure within, at or near the three phase boundary 14 and/or outlet 22 or inlet 4.
  • the exemplary illustration shows the pressure controller 30 located downstream of the outlet 22 and outlet pressure sensor 26 and embodied as a membrane valve with a flexible diaphragm that allows outlet flow only at, above, below or between a desired pressure.
  • the pressure controller 30 may be embodied through any of a variety of suitable mechanisms and may be arranged in any of a variety of locations. Also, if the electrochemical cell 2, CO 2 feed source, or reaction product feed use is expansive or complex, then additional pressure sensors 30 may be advantageously used to better control and control the CO 2 RR.
  • FIG. 2 an exemplary illustration of CO 2 RR electrochemical cell 2 operation mode utilizing back pressure is provided.
  • the CO 2 RR thereby occurs within, at or near the three-phase boundary 14, with the reaction product then advancing through the outlet 22 for desired collection or use.
  • Reaction product selectivity, as well as efficiency and stability, is improved by controlling the CO 2 pressure within, at or near the three-phase boundary 14.
  • One way to control the CO 2 pressure within, at or near the three-phase boundary 14 is via the pressure controller 30 arranged in operative communication with the pressure sensor(s) 24 and 26, and/or optional pressure sensor 28 to thereby adjust pressures detected by the pressure sensor(s) 24 and 26, and/or optional pressure sensor 28 in order to adjust the back pressure within, at or near the three-phase boundary 14 and/or outlet 22 or inlet 4.
  • CO 2 inlet 4 pressure (P1) is sensed as atmospheric at 1 mbar (within an exemplary preferred range of 0 mbar to 10 mbar), while three-phase boundary 14 pressure (P2) is sensed at 20 mbar (outside an exemplary preferred range of 30 mbar to 130 mbar).
  • the three-phase boundary 14 pressure (P2) is adjusted to a pressure of 85 mbar (or anywhere within the exemplary preferred range of 30 mbar to 130 mbar) in order to better control the CO 2 RR and desired reaction product.
  • CO 2 outlet 22 pressure (P3) is 15 mbar (within an exemplary preferred range of 10 mbar to 30 mbar), while three-phase boundary 14 pressure (P2) varies between 120-150 mbar (partially within and partially outside an exemplary preferred range of 30 mbar to 130 mbar). Based on the P2 and P3 pressure difference and the preferred pressure ranges, the three-phase boundary 14 pressure (P2) is continually adjusted to a desired set pressure of 70 mbar (or anywhere within the exemplary preferred range of 30 mbar and 130 mbar) in order to better control the CO 2 RR and desired reaction products.
  • CO 2 inlet 4 pressure (P1) is 2-4 mbar as continually measured by inlet pressure sensor 28, while three-phase boundary 14 pressure (P2) is 60-75 mbar as continually measures by pressure sensor 24, and outlet 22 pressure (P3) is 5-10 mbar as continually measured by outlet pressure sensor 26.
  • controller 30 Based on the P3, P2 and P1 pressure differences, as well as an exemplarily desired three-phase boundary 14 pressure range of 0 - 400 mbar (P3), an exemplarily desired inlet 4 pressure of 1 mbar (P1) and an exemplarily desired outlet 22 pressure range of 2-5 mbar (P3), controller 30 periodically adjusts the three-phase boundary 14 pressure (P2) to 55 mbar (or anywhere between 0 mbar and 400 mbar), the inlet 4 pressure (P1) to 1 mbar and the outlet 22 pressure (P3) to 4 mbar, in order to better control the CO 2 RR and desired reaction products.
  • CO 2 inlet 4 pressure (P1) is 50-75 mbar as continually measured by inlet pressure sensor 28, while three-phase boundary 14 pressure (P2) is 150-180 mbar as continually measures by pressure sensor 24, and outlet 22 pressure (P3) is 250-270 mbar as continually measured by outlet pressure sensor 26.
  • controller 30 Based on the P3, P2 and PI pressure differences, as well as an exemplarily desired three-phase boundary 14 pressure range of 0-400 mbar (P3), an exemplarily desired inlet 4 pressure of 75-100 mbar (P1) and an exemplarily desired outlet 22 pressure range of 300-320 mbar (P3), controller 30 periodically adjusts the three-phase boundary 14 pressure (P2) to 175 mbar (or anywhere between 80-100), the inlet 4 pressure (P1) to 100 mbar and the outlet 22 pressure (P3) to 250 mbar, in order to better control the CO 2 RR and desired reaction products.
  • a plurality of inlet pressure sensors 28 are employed near inlet 4 from which an average pressure (P1) of 2 mbar is calculated, while a plurality of outlet pressure sensors 26 are employed near outlet 22 from which an average pressure (P3) of 10 mbar is calculated.
  • controller 30 Based on the P3 and PI pressure difference, as well as an exemplarily desired three-phase boundary 14 pressure range of 30 - 130 mbar, an exemplarily desired inlet pressure (P1) of 1 mbar and an exemplarily desired outlet pressure range (P3) of 2-5 mbar, controller 30 adjusts the inlet pressure (P1) to 1 mbar and the outlet pressure (P3) to 3 mbar, in order to better control the CO 2 RR and desired reaction products.
  • pressure sensor 24 is not used while pressure sensors 26 and 28 are used.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Analytical Chemistry (AREA)
  • Automation & Control Theory (AREA)
  • Inorganic Chemistry (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
EP22172254.9A 2022-05-09 2022-05-09 Betriebsart für kohlendioxyd-elektrolyse Withdrawn EP4276223A1 (de)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP22172254.9A EP4276223A1 (de) 2022-05-09 2022-05-09 Betriebsart für kohlendioxyd-elektrolyse
PCT/US2023/066147 WO2023220520A1 (en) 2022-05-09 2023-04-25 Carbon dioxide electrolysis operation mode

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP22172254.9A EP4276223A1 (de) 2022-05-09 2022-05-09 Betriebsart für kohlendioxyd-elektrolyse

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EP22172254.9A Withdrawn EP4276223A1 (de) 2022-05-09 2022-05-09 Betriebsart für kohlendioxyd-elektrolyse

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20190233957A1 (en) * 2016-06-30 2019-08-01 Siemens Aktiengesellschaft Arrangement for the Electrolysis of Carbon Dioxide
WO2021023435A1 (de) * 2019-08-08 2021-02-11 Siemens Aktiengesellschaft Verfahren zur elektrochemischen umsetzung eines eduktgases an einer gasdiffusionselektrode mit differenzdruckermittlung
DE102020206447A1 (de) * 2020-05-25 2021-11-25 Siemens Aktiengesellschaft Verfahren zur Steuerung einer Elektrolysevorrichtung
WO2022022849A1 (de) * 2020-07-30 2022-02-03 Linde Gmbh Druckhaltung in einer elektrolyseanlage

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20190233957A1 (en) * 2016-06-30 2019-08-01 Siemens Aktiengesellschaft Arrangement for the Electrolysis of Carbon Dioxide
WO2021023435A1 (de) * 2019-08-08 2021-02-11 Siemens Aktiengesellschaft Verfahren zur elektrochemischen umsetzung eines eduktgases an einer gasdiffusionselektrode mit differenzdruckermittlung
DE102020206447A1 (de) * 2020-05-25 2021-11-25 Siemens Aktiengesellschaft Verfahren zur Steuerung einer Elektrolysevorrichtung
WO2022022849A1 (de) * 2020-07-30 2022-02-03 Linde Gmbh Druckhaltung in einer elektrolyseanlage

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