WO2021023435A1 - Procédé de conversion électrochimique d'un gaz de départ au niveau d'une électrode de diffusion de gaz avec détermination de la pression différentielle - Google Patents

Procédé de conversion électrochimique d'un gaz de départ au niveau d'une électrode de diffusion de gaz avec détermination de la pression différentielle Download PDF

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Publication number
WO2021023435A1
WO2021023435A1 PCT/EP2020/067907 EP2020067907W WO2021023435A1 WO 2021023435 A1 WO2021023435 A1 WO 2021023435A1 EP 2020067907 W EP2020067907 W EP 2020067907W WO 2021023435 A1 WO2021023435 A1 WO 2021023435A1
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Prior art keywords
differential pressure
gas
cathode
regeneration
control unit
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PCT/EP2020/067907
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German (de)
English (en)
Inventor
Marc Hanebuth
David Hartmann
Ralf Krause
Erhard Magori
Remigiusz Pastusiak
Kerstin Wiesner-Fleischer
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Siemens Aktiengesellschaft
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Publication of WO2021023435A1 publication Critical patent/WO2021023435A1/fr

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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
    • 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
    • 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
    • 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
    • Y02P20/141—Feedstock

Definitions

  • the present invention relates to a method for the electrochemical conversion of an educt gas on a gas diffusion electrode, comprising measuring the pressure on the gas side of the gas diffusion electrode and the pressure on the electrolyte side of the gas diffusion electrode.
  • Gas diffusion electrodes are currently used as cathodes in carbon dioxide electrolysis. Similar to the oxygen-consuming cathode in chlor-alkali electrolysis, the largest possible three-phase boundary between the liquid electrolyte, the gaseous carbon dioxide and the solid particles of an electrode catalyst is used here.
  • an electrolysis cell with two electrolyte compartments, separated by an ion exchange membrane, is used.
  • the anode is for example a platinum electrode or consists of an iridium mixed oxide.
  • the cathode is designed as a gas diffusion electrode, that is to say it is in contact with an electrolyte on the one hand, and is supplied with carbon dioxide or a carbon dioxide-containing feed gas flow on the other.
  • the gas diffusion electrode can contain various metals and metal compounds that have a catalytic effect on the carbon dioxide reduction reaction.
  • the electrochemical conversion of carbon dioxide can take place, for example, on silver electrodes according to the following reaction equation:
  • Gas diffusion electrodes used to date consist of a carrier matrix, materials for mechanical stabilization, such as carrier grids, and a catalyst material.
  • auxiliaries for adjusting the porosity or hydrophobicity can be included.
  • a gas flow flows behind the porous electrode on the gas side, in particular with the feed gas, and the product gas either leaves the electrolysis cell on the gas side, which is referred to as flow-by mode, or the product gas leaves the electrolyte cell on the electrolyte side, what is referred to as flow-through operation, wherein the educt gas diffuses through the pores of the gas diffusion electrode, is converted, and the product gas, e.g.
  • the differential pressure i.e. the gas pressure
  • an increase in the performance of the electrolyte cell is achieved with a higher pressure on the gas side, since the surface on the gas side is then not occupied by electrolyte that has penetrated by capillary action.
  • a higher pressure on the gas side has the effect that the electrolyte paths are shortened to the detriment of the gas phase diffusion paths, which are usually less resistant. It has now been shown that during operation in both operating method variants, the pores of the gas diffusion electrode as material transport paths are closed by deposited salts and poorly soluble electrolyte components.
  • the reactant gas to be converted no longer reaches all the catalytic centers in sufficient quantities, since these are either covered by the electrolyte or by deposited solid substances.
  • the gas diffusion electrode continuously loses its conversion rate up to the point at which, in the absence of catalytic centers, hydrogen electrolysis begins. In flow-through operation, this can also lead to an increase in differential pressure above the mechanically tolerable limit.
  • DE 102016 211 819 A1 discloses an arrangement for carbon dioxide electrolysis and a method for its operation, an electrolyte outlet being provided in a gas space on the cathode side, which is provided with a shut-off device that opens after a threshold value of a differential pressure has been overwritten becomes. In this case, however, there is no regulation and / or control in such a way that a regeneration differential pressure is set, but the pressure difference changes due to the electrolyte running off on the gas side.
  • EP 3375 907 A1 a device for a carbon dioxide electrolysis is specified in which a differential pressure is changed from depending on a desired product.
  • a regeneration of a gas diffusion electrode due to salification is not mentioned and also not recognized as a problem.
  • DE 102013 226 357 A1 describes a pulsating operation of an electrolytic cell. A specific setting of a differential pressure is not disclosed there.
  • the proposed solution should enable a reduction in carbon dioxide by means of an electrolysis cell with gas diffusion electrode, which has a good conversion rate in operation, and minimizes the salinity of the material transport routes.
  • the method according to the invention for the electrochemical implementation of a feed gas comprising carbon dioxide on a gas diffusion electrode comprises the measurement of the pressure difference between the gas side of the gas diffusion electrode and the electrolyte side of the gas diffusion electrode, which is a cathode, arranged in a cathode compartment which passes through the cathode into a cathode gas compartment (I) and a catholyte dream (II) is divided further comprises the modulation of the differential pressure, a distinction being made at least between an operating differential pressure Dr B and a regeneration differential pressure Dr k .
  • the regeneration differential pressure is lower than the operating differential pressure.
  • the modulation includes differential pressure control and / or differential pressure regulation.
  • the differential pressure can, as described below, be regulated, but can also be set in a targeted manner, for example by means of a defined gas flow that is dammed up at a throttle point.
  • the differential pressure is more useful- set or regulate wisely with sufficiently precise strength.
  • the pressure measurements take place e.g. at the electrolysis cell outlet, i.e. H.
  • the electrolysis cell outlet i.e. H.
  • the distinction between the operating pressure and the differential pressure has the advantage that a differential pressure based on optimized cell performance can very well be set, but the salinisation of the gas diffusion electrode pores can be effectively counteracted when the regeneration differential pressure is set.
  • the regulation of the differential pressure also has the advantage that no continuously decreasing conversion rate has to be accepted during the operating period and the operating point of the gas diffusion electrode remains stable.
  • the differential pressure By lowering the differential pressure, an overpressure is created on the electrolyte side, as a result of which electrolyte penetrates further into the pores and dissolves the salt deposited there again until it reaches the gas-side surface and exits the pores there.
  • the gas-side surface of the gas diffusion electrode can be flushed in the regeneration step in order to detach the salt on the surface.
  • an additional cleaning step can be dispensed with and the differential pressure reduction for regeneration of the electrolytic cell lasts so long that the gas-side surface is purged solely by the escaping electrolyte and is cleaned.
  • the continuous flow of educt gas can also be used to detach the salt from the surface. After sufficient cleaning, the differential pressure can then be set back to the operating differential pressure.
  • the regeneration differential pressure is set as a function of time after a predefinable operating time.
  • timing can be based on experience. For example, a regeneration cycle can be used after one day of operation.
  • the determination of the Faraday efficiency is included by measuring the electrolysis yield and the regeneration differential pressure is set after the electrolysis yield falls below a limit value.
  • the Faraday efficiency FEi is the ratio of the electrons involved in the conversion of CO2 to CO to the electrons used (cell current). It is based on measured variables (gas flow V co , current density j, cell area A and other measured variables and constants).
  • the Faraday efficiency of the electrolysis cell should not drop below 80%.
  • This efficiency-dependent Re regulation between operating and regeneration differential pressure has the advantage that, for. B. a varying product composition due to a decreasing product rate is avoided by the salinization of the catalytic centers.
  • gas diffusion electrodes from different manufacturing processes can also be subject to fluctuations in quality, which lead to different operating times. Accordingly, individual reactions to the system can be made by measuring the product composition. The problem of aging of the gas diffusion electrode is also avoided through efficiency-dependent regeneration phases.
  • the differential pressure can then be raised again to the operating differential pressure value.
  • the cell can be operated regularly until the measurement of the Faraday efficiency falls below the specified limit again.
  • the limit value is selected so high that the salinity cannot have caused any irreparable damage to the gas diffusion electrode.
  • the limit value is particularly preferably selected such that a constant product gas composition is guaranteed in the operating mode.
  • the cell can continue to be operated with electricity, for example. Then a changed product gas composition is either consciously accepted or the product gas arising during the regeneration step is diverted from the electrolysis cell separately from the desired product gas through a shuttle valve. Alternatively, the cell can be de-energized during the regeneration step and the corresponding voltage for the electrolysis operation is only applied again after the differential pressure has been raised to the operating differential pressure.
  • the method described has the advantage that the useful life of the electrochemical process is no longer limited in time by the salinization.
  • the regeneration differential pressure is set after a presettable pressure value has been exceeded on the gas side of the cathode.
  • the regeneration of the gas diffusion electrode takes place in situ and accordingly simply and efficiently. There are no additional costs for the regeneration operation described. Also, no additional components are required as built-in components in the electrolysis cell.
  • the described regulation between the operating differential pressure and the regeneration differential pressure extends the life of the electrolysis system, since, for example, high mechanical loads caused by an increasing differential pressure, in particular special in flow-through operation, are avoided.
  • Another advantage of the method described is a significantly reduced maintenance effort.
  • the acquisition of the time intervals between the triggered regeneration processes is also included, as well as the determination of an ideal time interval for setting the regeneration differential pressure.
  • the cell operation is adjusted in such a way that salinisation occurs less frequently or no longer at all. This ensures operation with optimal product yield near the limit of salinization.
  • pressure and efficiency threshold values are still used for process monitoring and process assurance.
  • exceeding pressure or efficiency limit values are coupled to the triggering of an acoustic warning signal. This process has the advantage of consistently high product yield.
  • the efficiency of the electrolysis system for the electrochemical conversion of carbon dioxide can be optimally used, as the operating differential pressure is optimally set for the product yield without any compromise to avoid salinization, and the salinization problem is overcome by the in situ regeneration steps. Accordingly, by means of the method described, continuous operation is possible without the running time limit of the gas diffusion electrode due to salinization.
  • the inventive device for the electrochemical conversion of an educt gas, comprising carbon dioxide, on a gas diffusion electrode has at least one electrolysis cell, an electrolyte line, at least one pump, an anode and a cathode, the cathode being designed as a gas diffusion electrode and being arranged in a cathode compartment which is divided by the cathode into a cathode gas space and a catholyte space.
  • the device also has a first gas inlet into the cathode gas space for a carbon dioxide-containing feed gas and a differential pressure sensor to determine the pressure difference between the cathode gas space and catholyte space, and a differential pressure control unit and / or control unit for modulating the differential pressure, the differential pressure control unit and / or control unit is designed to set at least one operating differential pressure and a regeneration differential pressure, wherein the regeneration differential pressure is lower than the operating differential pressure.
  • the device has the advantage of ensuring an independent, reliable electrolysis operation even with quality or process parameter control. This is particularly useful when several cells are connected, e.g. B. in a cell stack advantageous.
  • the electrolysis system does not require any additional system components in the electrolysis cell, such as nozzles for humidifying the feed gas or cleaning agents. supply nozzles in the gas space.
  • the method according to the invention can be carried out, so that statements on the method can also be applied to the device and vice versa.
  • the device according to the invention furthermore preferably comprises an outlet from the cathode gas space, more preferably a gas outlet, and an outlet from the catholyte space, in particular a catholyte outlet.
  • the differential pressure control unit and / or control unit is designed as a differential pressure control unit.
  • the differential pressure control unit and / or control unit, in particular the differential pressure control unit, of the device according to the invention is connected to at least one data line via which signals can be sent to a pump.
  • the device further comprises at least one actuator, e.g. B. an actuator which has a water column container with a connecting line between the water column container and the gas outlet of the cathode compartment.
  • the operating differential pressure in particular is continuously regulated so that the continuous salinization and consequent shifting of the active zone within the pores of the gas diffusion electrodes is continuously counteracted until the pressure limit value or the efficiency limit value or the corresponding point in time for switching to the regeneration differential pressure is reached .
  • the regeneration differential pressure is usually 0.
  • it comprises a catholyte feed line and an anolyte feed line.
  • an electrolyte line splits into a catholyte feed line and an anolyte feed line.
  • a single pump can be provided in the electrolyte line or one pump each in the catholyte feed line and anolyte feed line.
  • the device advantageously comprises a separator which separates the cathode compartment and the anode compartment from one another.
  • the cathode gas chamber can be designed as a pressure chamber, for example.
  • the cathode gas space is designed as a gas gap.
  • the device comprises an electrolyte reservoir, in which catholyte line and anolyte line are brought together and to which the electrolyte line is connected.
  • an electrolyte reservoir serves to balance ions and pH values in the electrolyte circuit.
  • the device comprises a controllable valve for adjusting the flow rate of the educt gas, which is connected to the differential pressure control unit and / or control unit via at least one data line.
  • the feed gas flow can be influenced via the controllable valve.
  • the flow rate of the educt gas can be increased in the regeneration step for the purpose of rinsing the electrode surface.
  • the device according to the invention comprises a device for determining the Faraday efficiency of the electrolysis, in particular for products on the cathode side, which is designed to measure the Faraday efficiency of the electrolysis, in particular for products on the cathode method page, to specific.
  • a device for determining the Faraday efficiency of the electrolysis is not particularly restricted and can, for example, be a gas chromatograph, etc., and / or also continuously detecting sensors for products of electrolysis, for example the main products of CCh electrolysis, eg CO and H2.
  • the device for determining the Faraday efficiency of the electrolysis is preferably connected to the differential pressure control unit and / or control unit.
  • the differential pressure control unit and / or regulating unit is designed in particular to detect the Faraday efficiency, and more preferably designed to set the regeneration differential pressure after the electrolysis yield falls below a limit value.
  • the differential pressure control unit and / or regulation unit is designed according to certain embodiments to set the regeneration differential pressure on the gas side of the cathode after a predefinable pressure value has been exceeded.
  • the differential pressure control unit and / or regulation unit is designed to raise the differential pressure again to the operating differential pressure value after sufficient regeneration and cleaning of the gas diffusion electrode surface.
  • the cell was operated with differential pressure Dr, e.g. in flow-through operation, salt forms on the gas side.
  • differential pressure Dr is reduced to 0, the salt dissolves again and can be washed off.
  • an electrolysis test stand for setting the differential pressure Dr is shown as an example.
  • Two separate electrolyte circuits 13, 15 are implemented via a cathode or anode-side pump 4, which convey electrolyte from a reservoir 3 into the cathode II or anode space III of the electrolytic cell 20 and back into the reservoir 3. Both compartments II, III are separated by a membrane SEP separated from each other.
  • Educt gas flows through a gas supply line 11 into the cell 20 and is converted to carbon monoxide CO according to the above equations 1 and 2 at the gas diffusion electrode, for example containing silver particles.
  • Hydrogen gas H2 is produced as a by-product. The gases finally leave the gas space I of the cell 20 via the gas outlet 12.
  • the differential pressure sensor 1 which is connected between the gas outlet 12 and the catholyte outlet 14, measures the pressure ratios on both sides of the gas diffusion electrode GDK as a differential value Dr.
  • the hydrostatic pressure increases with the immersion depth of the gas-out tube in the water column. The higher the hydrostatic pressure, the higher the differential pressure Dr between the gas and catholyte sides of the gas diffusion cathode GDK, and vice versa.
  • This example shows the setting of the differential pressure Dr via the hydrostatic pressure of a water column between the gas and electrolyte side of a gas diffusion electrode GDK.
  • the displacement of the active zone 10 with the differential pressure Dr is sketched schematically in FIG.
  • FIG. 3 shows a diagram in which the Faraday efficiency FE is plotted in% over the operating time t in h.
  • Phases i, operating differential pressure Dr B of, for example, 30 mbar, ii, regeneration differential pressure Dr k of, for example, 13 mbar and iii, operating differential pressure Dr B of, for example, 30 mbar are run through.
  • the cell is operated at, for example, a current density of 200 mA / cm 2 .
  • the differential pressure Dr is reduced from the operating differential pressure Dr B of, for example, 30 mbar to the regeneration differential pressure Dr k of, for example, 13 mbar.
  • the Faraday efficiency for the carbon monoxide formation FE-CO decreases from 91% to 85% and for the hydrogen formation FE-H2 it increases from 9% to 15%.
  • the active zone 10 is thus shifted in the direction of the gas side g.
  • the model shift is supported by the observation that a permeate flow from the cathode II into the gas space I of the cell 20 begins instantaneously with the decrease in the differential pressure from the operating differential pressure Dr B to the regeneration differential pressure Dr k .
  • a drop formation on the gas-side GDK surface can be observed. If the differential pressure Dr is then increased again to the operating differential pressure Dr B , the Faraday efficiencies FE-CO and FE-H2 are regenerated and the permeate flow disappears after a few seconds.
  • FIG. 4 shows a further diagram in which the Faraday efficiency FE is plotted in% over the operating time t in h, for a further exemplary embodiment which advantageously uses the differential pressure variation described above to carry out electrode washing during the test.
  • the differential pressure control unit 5 can be implemented in the form of a computer. This is connected to an actuator 6, which comprises, for example, a water column container 2, a valve for the gas inlet and / or a pump 4 for the electrolyte flow rate.
  • the controlled system 7 comprises a multi-variable system and is limited by the pressures p gas and p ei ⁇
  • an input and operating interface 8 is preferably provided.
  • a computer program is used to keep a log, output error messages and / or acoustic signals and to carry out an emergency shutdown.
  • a controllable valve for setting the flow rate of the educt gas is connected as an actuator 6 via at least one data line 41 to the differential pressure control unit 5.
  • Process parameters for example, combinatorial, analog or sequential, such as flow rate, composition, pressure, pH value, can be passed on via data line 41.
  • Another data line 42 is provided, for example, for feedback such as signals (in particular binary signals), measured values (in particular analog signals), see Figure 6.
  • Another data line 43 is preferably provided for, for example, feedback to process monitoring 9.
  • the feed gas flow can be influenced via the controllable valve 6.
  • the flow rate of the educt gas can be increased for the purpose of flushing the electrode surface.
  • Differential pressure control unit e.g. computer
  • actuator (includes e.g. water column container 2, valve for gas inlet, pump 4 for electrolyte flow rate)
  • Dr B operating differential pressure d (t) disturbance variable, e.g. due to electrolyte composition, gas bubble formation in the electrolyte or salinisation of the gas diffusion cathode GDK GDE gas diffusion electrode (general)
  • Material input includes e.g. reactant gas, electrolyte
  • Product output includes e.g. electrolysis products, by-products, circulating material, redeemed educt gas

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
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  • Automation & Control Theory (AREA)
  • Inorganic Chemistry (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)

Abstract

L'invention concerne un procédé de conversion électrochimique d'un gaz de départ au niveau d'une électrode de diffusion de gaz, selon lequel la pression différentielle (Δp) est mesurée et modulée, une distinction étant effectuée au moins entre une pression différentielle de fonctionnement (ΔpΒ) et une pression différentielle de régénération (ΔpR), la pression différentielle de régénération (ΔpR) étant inférieure à la pression différentielle de fonctionnement (ΔpΒ).
PCT/EP2020/067907 2019-08-08 2020-06-25 Procédé de conversion électrochimique d'un gaz de départ au niveau d'une électrode de diffusion de gaz avec détermination de la pression différentielle WO2021023435A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102019211942.5A DE102019211942A1 (de) 2019-08-08 2019-08-08 Verfahren zur elektrochemischen Umsetzung eines Eduktgases an einer Gasdiffusionselektrode mit Differenzdruckermittlung
DE102019211942.5 2019-08-08

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP4276223A1 (fr) * 2022-05-09 2023-11-15 Siemens Energy Global GmbH & Co. KG Mode de fonctionnement d'électrolyse de dioxyde de carbone

Citations (5)

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Publication number Priority date Publication date Assignee Title
DE102013226357A1 (de) 2013-12-18 2015-06-18 Siemens Aktiengesellschaft Pulsierende Elektrolytzufuhr in den Reaktionsraum einer Elektrolysezelle mit gasentwickelnden Elektroden
WO2018001637A1 (fr) * 2016-06-30 2018-01-04 Siemens Aktiengesellschaft Agencement et procédé pour l'électrolyse du dioxyde de carbone
DE102016211151A1 (de) * 2016-06-22 2018-01-11 Siemens Aktiengesellschaft Anordnung und Verfahren für die Kohlendioxid-Elektrolyse
EP3375907A1 (fr) 2017-03-14 2018-09-19 Kabushiki Kaisha Toshiba Dispositif électrolytique de dioxyde de carbone
WO2020143970A1 (fr) * 2019-01-10 2020-07-16 Siemens Aktiengesellschaft Procédé d'électrolyse pour la réduction du dioxyde de carbone

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102013226357A1 (de) 2013-12-18 2015-06-18 Siemens Aktiengesellschaft Pulsierende Elektrolytzufuhr in den Reaktionsraum einer Elektrolysezelle mit gasentwickelnden Elektroden
DE102016211151A1 (de) * 2016-06-22 2018-01-11 Siemens Aktiengesellschaft Anordnung und Verfahren für die Kohlendioxid-Elektrolyse
WO2018001637A1 (fr) * 2016-06-30 2018-01-04 Siemens Aktiengesellschaft Agencement et procédé pour l'électrolyse du dioxyde de carbone
DE102016211819A1 (de) 2016-06-30 2018-01-18 Siemens Aktiengesellschaft Anordnung und Verfahren für die Kohlendioxid-Elektrolyse
EP3375907A1 (fr) 2017-03-14 2018-09-19 Kabushiki Kaisha Toshiba Dispositif électrolytique de dioxyde de carbone
WO2020143970A1 (fr) * 2019-01-10 2020-07-16 Siemens Aktiengesellschaft Procédé d'électrolyse pour la réduction du dioxyde de carbone

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP4276223A1 (fr) * 2022-05-09 2023-11-15 Siemens Energy Global GmbH & Co. KG Mode de fonctionnement d'électrolyse de dioxyde de carbone
WO2023220520A1 (fr) * 2022-05-09 2023-11-16 Siemens Energy Global GmbH & Co. KG Mode de fonctionnement d'électrolyse du dioxyde de carbone

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