WO2018103769A1 - Cellule d'électrolyse et procédé pour faire fonctionner ladite cellule - Google Patents

Cellule d'électrolyse et procédé pour faire fonctionner ladite cellule Download PDF

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Publication number
WO2018103769A1
WO2018103769A1 PCT/DE2017/000373 DE2017000373W WO2018103769A1 WO 2018103769 A1 WO2018103769 A1 WO 2018103769A1 DE 2017000373 W DE2017000373 W DE 2017000373W WO 2018103769 A1 WO2018103769 A1 WO 2018103769A1
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WO
WIPO (PCT)
Prior art keywords
water
anode
electrolysis
cathode
oxygen
Prior art date
Application number
PCT/DE2017/000373
Other languages
German (de)
English (en)
Inventor
Martin Müller
Geert Tjarks
Denise Günther
Wiebke Lüke
Original Assignee
Forschungszentrum Jülich GmbH
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 Forschungszentrum Jülich GmbH filed Critical Forschungszentrum Jülich GmbH
Publication of WO2018103769A1 publication Critical patent/WO2018103769A1/fr

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Classifications

    • 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
    • C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
    • 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
    • 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
    • C25B9/60—Constructional parts of cells
    • C25B9/65—Means for supplying current; Electrode connections; Electric inter-cell connections
    • 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
    • C25B9/70—Assemblies comprising two or more cells
    • C25B9/73—Assemblies comprising two or more cells of the filter-press type
    • 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

Definitions

  • the invention relates to an electrolysis cell, in particular an electrolysis cell for generating hydrogen and oxygen from water, and preferably an electrolysis cell with a proton-conducting membrane (PEM).
  • an electrolysis cell in particular an electrolysis cell for generating hydrogen and oxygen from water, and preferably an electrolysis cell with a proton-conducting membrane (PEM).
  • PEM proton-conducting membrane
  • An electrolytic cell is basically always the same.
  • the electrolysis cell comprises two electrodes, between which an electrolyte is arranged.
  • the electrolyte consists of a proton-conducting membrane.
  • the unit of the two electrodes and the electrolyte is also referred to as MEA (Membrane Electrode Assembly).
  • MEA Membrane Electrode Assembly
  • media supplies in the form of flow distributor structures and corresponding manifolds are generally integrated into cells and stacks both on the anode side and on the cathode side. This regularly increases manufacturing costs and increases the cost of stacks.
  • bipolar plates The power is conducted to the individual electrolysis cells via the bipolar plates.
  • suitably structured bipolar plates simultaneously take over the functions of the electrical contacting and the media supply to the electrodes.
  • the tasks of the system components of the anodic region of an electrolytic cell consist in the supply of the electrolyzer with water and in the removal of the oxygen produced, as well as the phase separation of oxygen and entrained liquid.
  • the structure looks similar. On a water supply can be omitted.
  • the removal of the hydrogen produced also takes place via flow distributor structures. Since, during operation, water is normally drawn from the anode side through the membrane to the cathode side, a hydrogen / water mixture always forms on the cathode side, which is removed as a mixture. In a downstream separation this water is then usually separated from the hydrogen produced and optionally forwarded again for disassembly to the anode.
  • the hydrogen is generated on the anode side (negative pole) and the oxygen on the cathode side (positive pole).
  • electrolysis stack is usually arranged between two end plates, which on the one hand ensure the supply of the electrical current to the individual cells and on the other hand ensure the necessary contact pressure for sealing the individual cells.
  • the end plates are usually braced against each other.
  • gas diffusion layers are arranged on both sides of the MEAs, which are each separated by bipolar plates, which can be configured structured, for the separation of the individual electrolysis cells.
  • a gas diffusion layer is porous and serves as a distributor structure of the supply and discharge of the operating materials, or the product gases generated, hydrogen and oxygen, to or from an electrode. Normally, the mass transport in the gas diffusion layers diffusely takes place perpendicular to the membrane plane while in the medium supply it takes place as a flow parallel to the membrane plane.
  • the gas diffusion layer can simultaneously assume the function of an electrode in the areas close to the membrane and is then called a gas diffusion electrode.
  • EP 2957659 A1 discloses a PEM electrolysis cell in which the positive pole (the cathode) is fed with demineralized water, which is decomposed at the negative pole (anode) into oxygen gas and protons (H + ). The protons migrate through the proton-conducting membrane (electrolyte) to the cathode, where they recombine to form hydrogen gas.
  • the gas diffusion layers arranged adjacent to the electrodes ensure, in addition to contacting the electrodes, the optimum distribution of water and thus the wetting of the proton-conducting membrane as well as the removal of the gases produced.
  • the gas diffusion layers comprise an electrically conductive material and are made porous.
  • various variants of the operation management are conceivable. There are the classic concepts with a liquid water supply at the anode or the anode and cathode. In addition, variants with a vaporous supply of the anode are possible, and depending on the pressure level on the cathode side results there liquid or gaseous water. In the case of a cathodic overpressure, the liquid water can also be used to cool the system.
  • the object of the invention is to provide an alternative electrolysis system which, compared to the prior art, on the one hand requires less production effort and at the same time saves installation space, so that the system as a whole is more cost-effective than hitherto.
  • Another object of the invention is to provide a method of operating such an alternative electrolysis system.
  • the objects of the invention are achieved by a method for operating a PEM electrolysis cell with the features of the skin claim, by a PEM electrolysis cell according to the first additional claim and by a PEM electrolysis stack according to further independent claim.
  • the operation of an electrolytic cell for the production of hydrogen usually the anode side water is supplied, which then reacts electrochemically to hydrogen with elimination of protons.
  • the oxygen formed at the anode during the electrolysis is removed together with excess water from the anode space and fed to a gas / liquid separation. There, the oxygen is separated and the excess water usually fed back to the anode or the anode compartment.
  • electrolysis systems therefore have a separate media supply both on the anode and the cathode side and are very complex, which nachteii- lig increases the manufacturing cost in the production of electrolysis cells.
  • electrolysis systems generally also have corresponding separating devices for the generated product gases on the anode or cathode side, in order to free them from excess water.
  • the transport path of the water through the proton-conducting membrane to the anode is a kind of transport limitation in comparison with the direct supply to the anode according to the prior art and preferably results in sufficient water reaching the anode, where it is split up into oxygen and protoners but on the other hand there remains only so little excess and unreacted water that the oxygen generated and derived at the anode has significantly less water than has hitherto been customary.
  • the entrained water discharged with the oxygen does not exceed the saturation point, so that as a further advantage of the method according to the invention a subsequent gas / liquid separation unit can be dispensed with.
  • gas transport in the plane of the porous structure can now be sufficient for removing the generated oxygen.
  • the process according to the invention can be carried out under atmospheric conditions at temperatures between 10 ° C. and not more than 95 ° C. Operating temperatures between 60 ° C and 90 ° C and in particular operating temperatures around 80 ° C have proven to be advantageous. Above 95 ° C, an increased degradation of the polymers used is to be expected, so that this temperature range is permanently not meaningful. In addition, in unpressurized operation and at such high temperatures, a high heat output due to the evaporation of water is to be expected, which requires an additional heating, which reduces the efficiency.
  • the inventive method is also suitable to be carried out under pressure.
  • the water intended for decomposition can be fed to the cathode side of the electrolysis cell at pressures of from 1,000 hPa to 50,000 hPa, preferably between 2,000 hPa and 20,000 hPa bar. It can be distinguished between a constant pressure method and a differential pressure method. In Gleichschul compassion anode and cathode are kept at the same pressure level, whereas in the differential pressure operation, only the cathode side is operated under pressure. In the case of pressure-charged operation, the liquid water is brought to the cathode side by means of a pump to the desired pressure. This is advantageous under energetic considerations, since water is an incompressible medium and no volume change work is required. In the case of constant pressure operation, the generated oxygen is the anode side via a pressure control valve.
  • the method according to the invention can be operated in both modes.
  • a suitable for implementing the method according to the invention electrolytic cell differs from the prior art in that is dispensed with a separate media supply on the anode side.
  • the PEM electrolysis cell according to the invention has no supply line for water to the anode side.
  • the electrolysis cell in its interior next to a porous anode and no further separate distribution structure as a media supply.
  • the media supply thus takes place exclusively via the cathode side.
  • the diffusive water transport in the membrane is used to supply the catalyst layer lying on the anode with water.
  • a separate media supply of the anode with water is no longer necessary.
  • Separate distributor structures and manifolds for supplying and distributing the supplied water to the anode can therefore advantageously be dispensed with.
  • simple thin unstructured bipolar plates can now be used advantageously.
  • all hitherto customary polymer membranes can be used as PEM membrane.
  • NAFION ® membranes have proven to be very suitable for electrolysis cells and also for the novel process.
  • NAFION ® membranes are already ⁇ with different layer thicknesses in the range of, for example, 22 to 183 offered ⁇ .
  • the required suitable layer thickness of the PEM membrane can easily be determined by a person skilled in the art and the electrolysis cell designed accordingly.
  • the PEM membrane used, the more limiting the diffusive transport of water through the membrane.
  • the PEM membrane should not be designed as thin as desired. This is to be considered in particular in the case of the differential pressure operation, since the Membrane must withstand the mechanical stresses resulting from the differential pressure permanently.
  • anode of the PEM electrolysis cell As material for the anode of the PEM electrolysis cell according to the invention, all conventional anode materials can be used. For example, a porous titanium sintered ceramic is particularly suitable for this purpose. Conventional anodes of an electrolytic cell have layer thicknesses between 1 mm and 1.5 mm. Conceivable and suitable would be thinner anodes with thicknesses in the range of 0.2 to 1 mm.
  • the porous anode of the PEM electrolysis cell according to the invention is suitable according to the invention to dissipate the generated there during operation oxygen flow directly in the layer plane to the outside. The required sufficient porosity and layer thickness of the anode can easily be determined by a person skilled in the art and the electrolysis cell can be designed accordingly.
  • cathode for the PEM electrolysis cell also all conventional cathode materials can be used.
  • the thickness of the cathodes is in the range of 0.1 to 0.5 mm, typically 0.2 mm.
  • the catalysts used for the electrolysis according to the invention at the anode and the cathode also correspond to the hitherto conventional catalysts.
  • platinum is particularly suitable as a catalyst for the cathode and iridium as a catalyst for the anode. This results in a significant simplification for the inventive PEM electrolysis cell, which advantageously reduces the investment costs.
  • Another advantage of the PEM electrolysis cell according to the invention is that can be significantly reduced by the invention, the space required for an electrolysis cell or an electrolysis stack.
  • an unstructured thinner bipolar plate of preferably less than 1 mm used which is only responsible for the electrical contact instead of a structured, 1 to 2 mm thick bipolar plate with distribution structures, which also takes over the contact simultaneously also the function of a media supply and as it is known from the prior art, now an unstructured thinner bipolar plate of preferably less than 1 mm used which is only responsible for the electrical contact.
  • This can be According to the invention have a thickness of even less than 0.8 mm and advantageously even be configured only between 0.3 to 0.6 mm thick.
  • an electrolysis system comprising one or more electrolysis cells according to the invention also advantageously be dispensed with a hitherto conventional gas / liquid separator for the discharged oxygen, since this usually has only up to its saturation limit water.
  • the invention is based on the idea, when operating a PEM electrolysis cell or a PEM electrolysis stack completely on the anodic media supply, i. to dispense with the supply of water to the anode, and to use only the cathodic supply.
  • the water intended for decomposition is fed exclusively to the cathode.
  • a supply of water is provided exclusively to the cathode side of the electrolysis cell.
  • the hitherto customary separate anodic media distribution (distributor structure) is eliminated, which significantly reduces the installation space of a single electrolysis cell and in particular of an electrolysis stack.
  • the oxygen generated at the anode can be directly discharged to the outside via a sufficiently porous anode.
  • the cell has a PEM membrane which is arranged in a U-shape, wherein the porous cathode and the associated media supply are arranged on one side of the membrane between the arms of the membrane and the porous anode is arranged on the other side of the membrane , The contacting of the anode via at least one bipolar plate, which now extends from the anode to the cathode side and is arranged outside the arms of the PEM membrane.
  • Such a special embodiment of the invention is very advantageous, for example, for use in combination with photovoltaic cells.
  • the electrolysis cell or cells could on the back of a photovoltaic cell are arranged in such a way that the cathode side is arranged with the two contacts directed against this.
  • a contacting of both electrodes on one side of the cell is advantageous because then the current generated in the solar cell can be passed directly into the electrolysis cell without detours.
  • the opposite side (anode side) of the electrolysis cell would be free, for example, to be able to dissipate the oxygen generated there directly into the ambient air.
  • Figure 1 Schematic representation of an electrolytic cell according to the prior art.
  • FIG. 1 Schematic representation of the operation of an electrolytic cell according to
  • FIG. 3 Schematic representations of the operation of the invention
  • Figure 5 Schematic representation of an overall system with an electrolytic cell according to the prior art.
  • Figure 6 Schematic representation of an overall system with an embodiment of the
  • FIG. 7 Graphical representation of the current / voltage curve of a device according to the invention
  • FIG. 8 Special embodiment of the electrolytic cell according to the invention with contacting on the cathode side.
  • Figure 9 Schematic representation of classical modes of operation for an electrolysis (a) and a chloralkali electrolysis (b).
  • 1 bipolar plate
  • 2 anode
  • 3 membrane
  • 4 cathode
  • 6 flow distributor structure.
  • 1 shows a schematic representation of an electrolytic cell according to the prior art.
  • the center forms the PEM membrane 3 with the electrodes adjoining on both sides (anode 2 and cathode 4).
  • On both sides of the membrane-electrode assembly (2 + 3 + 4) are devices for supplying media with flow distributor structures 6 and thus formed separate media channels 5 for anodic and cathodic supply of water, as well as for the discharge of an oxygen / water mixture on the anode side and a hydrogen / water mixture on the cathode side.
  • the flow distributor structures 6 are formed here simultaneously by the bipolar plates 1, which ensure the electrical contacting of the electrolysis cell.
  • FIG. 1 The operation of an electrolytic cell according to the prior art is shown in FIG.
  • the intended for decomposition water is fed mainly to the anode.
  • some of the water is also supplied to the cathode, wherein the water supplied to the cathode is usually that separated from the discharged hydrogen / water mixture water.
  • Excess water from the anode side to the cathode side is transported through the membrane in addition to the protons.
  • the discharge of the generated product gases hydrogen and oxygen takes place.
  • the electrolysis cell shown in FIG. 2 the electrolysis cell shown in FIG.
  • FIG. 3 a) shows an electrolysis cell optimized for the operation according to the invention, in which separate media channels are dispensed with on the anode side and a simple, unstructured thin bipolar plate is now provided instead of a correspondingly structured bipolar plate (prior art).
  • FIG. 4 illustrates the difference in installation space between a conventional electrolysis stack and an embodiment of the invention.
  • electrolysis cells according to the invention were constructed and current-voltage investigations were carried out.
  • electrolytic cells of different PEM membranes were thick comprising Nafion ® used with an area of 17.84 cm, respectively.
  • the different materials and layer thicknesses of the membranes used can be taken from the table below.
  • the anode used was a catalyst layer based on an iridium catalyst in combination with a 0.2 mm thick diffusion structure. Alternatively, the use of titanium sintered metals with a porosity of about 20 vol .-% is possible.
  • the cathode used was a catalyst layer based on a platinum catalyst.
  • As a diffusion substrate a carbon fiber fleece with a layer thickness of 0.2 mm was also used here. The results of the investigations are shown in FIG.
  • the electrolyte is arranged in a U-shape with the cathode having the cathode supply between the arms of the U-shaped electrolyte and the anode on the opposite side of the PEM membrane.
  • the contacting can advantageously take place for both electrodes, while on the other side of the cell, the oxygen can be transported away directly via the porous anode.
  • such an arrangement can be ideally coupled to a photovoltaic cell in which the generated electricity can be used directly for the electrolysis and there especially for the production of hydrogen.
  • the aforementioned embodiment of the cell with the possibility of contacting on only one side of the electrolysis cell would be particularly advantageous.
  • the oxygen produced can be removed separately (not shown in FIG. 8) or else released directly to the environment via the porous anode.

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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)
  • Inorganic Chemistry (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)

Abstract

L'objet de l'invention est, pour l'électrolyse de l'eau de manière à obtenir de l'oxygène et de l'hydrogène, de se passer totalement de l'alimentation en milieu sur le côté anode. Etant donné que la membrane conductrice de protons transporte de l'eau par diffusion, il s'avère suffisant que l'eau servant à la décomposition soit amenée exclusivement au côté cathode ou à la chambre cathodique de la cellule d'électrolyse. L'eau nécessaire à la décomposition est alors dirigée vers l'anode, simplement par diffusion, au moyen de la membrane électrolytique échangeuse de protons, afin d'y réagir sous l'effet de l'émission de protons et d'obtenir de l'oxygène. Les protons formés à cet endroit se diffusent à nouveau vers le côté cathode, où ils se recombinent en hydrogène. L'invention se base sur l'idée de se passer totalement de l'alimentation anodique en milieu, c'est à-dire de l'amenée d'eau, et d'utiliser simplement l'alimentation cathodique, lors du fonctionnement d'une cellule d'électrolyse à membrane échangeuse de protons ou d'un empilement électrolytique à membrane échangeuse de protons. L'eau servant à la décomposition est amenée exclusivement à la cathode.
PCT/DE2017/000373 2016-12-05 2017-11-07 Cellule d'électrolyse et procédé pour faire fonctionner ladite cellule WO2018103769A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102016014396.7A DE102016014396A1 (de) 2016-12-05 2016-12-05 Elektrolysezelle sowie Verfahren zum Betreiben einer solchen
DE102016014396.7 2016-12-05

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2020525653A (ja) * 2017-07-03 2020-08-27 シンテフ・テーテーオー・アクシェセルスカプＳｉｎｔｅｆ Ｔｔｏ Ａｓ ＰＥＭ水電解槽システム、ＰＥＭ水電解槽セル（又は電池；ｃｅｌｌ）、スタック及びシステムにて水素を生成するための方法
WO2023138807A1 (fr) * 2022-01-21 2023-07-27 Siemens Energy Global GmbH & Co. KG Systèmes à tampon pour éviter la dégradation due à la corrosion dans l'électrolyse de l'eau à membrane échangeuse de protons

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110483822B (zh) * 2019-08-16 2022-02-11 上海博暄能源科技有限公司 一种提高质子交换膜抗氧化化学稳定性的方法

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US5350496A (en) * 1992-08-13 1994-09-27 United Technologies Corporation Solid state high pressure oxygen generator and method of generating oxygen
JP3366549B2 (ja) * 1997-03-18 2003-01-14 神鋼パンテツク株式会社 水素・酸素発生装置及びこれに用いる電解セル
US20110198232A1 (en) * 2010-02-15 2011-08-18 Hamilton Sundstrand Corporation High-differential-pressure water electrolysis cell and method of operation
WO2015147142A1 (fr) * 2014-03-26 2015-10-01 独立行政法人宇宙航空研究開発機構 Procédé d'électrolyse de l'eau et dispositif d'électrolyse de l'eau
EP2957659A1 (fr) 2014-06-16 2015-12-23 Siemens Aktiengesellschaft Couche de diffusion de gaz, cellule électrolytique PEM équipée d'une telle couche de diffusion de gaz, ainsi qu'électrolyseur

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Publication number Priority date Publication date Assignee Title
US5350496A (en) * 1992-08-13 1994-09-27 United Technologies Corporation Solid state high pressure oxygen generator and method of generating oxygen
JP3366549B2 (ja) * 1997-03-18 2003-01-14 神鋼パンテツク株式会社 水素・酸素発生装置及びこれに用いる電解セル
US20110198232A1 (en) * 2010-02-15 2011-08-18 Hamilton Sundstrand Corporation High-differential-pressure water electrolysis cell and method of operation
WO2015147142A1 (fr) * 2014-03-26 2015-10-01 独立行政法人宇宙航空研究開発機構 Procédé d'électrolyse de l'eau et dispositif d'électrolyse de l'eau
EP2957659A1 (fr) 2014-06-16 2015-12-23 Siemens Aktiengesellschaft Couche de diffusion de gaz, cellule électrolytique PEM équipée d'une telle couche de diffusion de gaz, ainsi qu'électrolyseur

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2020525653A (ja) * 2017-07-03 2020-08-27 シンテフ・テーテーオー・アクシェセルスカプＳｉｎｔｅｆ Ｔｔｏ Ａｓ ＰＥＭ水電解槽システム、ＰＥＭ水電解槽セル（又は電池；ｃｅｌｌ）、スタック及びシステムにて水素を生成するための方法
JP7219973B2 (ja) 2017-07-03 2023-02-09 ハイスター・アクシェセルスカプ ＰＥＭ水電解槽システム、ＰＥＭ水電解槽セル（又は電池；ｃｅｌｌ）、スタック及びシステムにて水素を生成するための方法
WO2023138807A1 (fr) * 2022-01-21 2023-07-27 Siemens Energy Global GmbH & Co. KG Systèmes à tampon pour éviter la dégradation due à la corrosion dans l'électrolyse de l'eau à membrane échangeuse de protons

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