EP4345191A1 - Procédé et installation de production d'un produit contenant de l'hydrogène par électrolyse - Google Patents

Procédé et installation de production d'un produit contenant de l'hydrogène par électrolyse Download PDF

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Publication number
EP4345191A1
EP4345191A1 EP22020474.7A EP22020474A EP4345191A1 EP 4345191 A1 EP4345191 A1 EP 4345191A1 EP 22020474 A EP22020474 A EP 22020474A EP 4345191 A1 EP4345191 A1 EP 4345191A1
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EP
European Patent Office
Prior art keywords
electrolysis
cells
during
period
operating
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
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EP22020474.7A
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German (de)
English (en)
Inventor
Andreas Peschel
Harald Klein
Johanna HEMAUER
Steffen Fahr
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Linde GmbH
Technische Universitaet Muenchen
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Linde GmbH
Technische Universitaet Muenchen
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Application filed by Linde GmbH, Technische Universitaet Muenchen filed Critical Linde GmbH
Priority to EP22020474.7A priority Critical patent/EP4345191A1/fr
Priority to PCT/EP2023/025411 priority patent/WO2024068048A2/fr
Publication of EP4345191A1 publication Critical patent/EP4345191A1/fr
Pending 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
    • C25B1/02—Hydrogen or oxygen
    • 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
    • C25B15/02—Process control or regulation
    • C25B15/021—Process control or regulation of heating or cooling
    • 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
    • C25B9/70—Assemblies comprising two or more cells
    • C25B9/73—Assemblies comprising two or more cells of the filter-press type

Definitions

  • the invention relates to a process and a plant for producing a hydrogen-containing product using electrolysis.
  • Hydrogen can be produced by converting gaseous, solid or liquid carbon sources such as natural gas, naphtha or coal.
  • Another way to produce hydrogen from corresponding carbon sources involves catalytic partial oxidation (POX) and catalytic reforming in different configurations such as steam reforming or autothermal reforming. Combined processes can also be used here.
  • hydrogen can also be produced electrolytically from water, as explained in the article mentioned in Ullmann's Encyclopedia of Industrial Chemistry, especially in Section 4.2, "Electrolysis".
  • AEL alkaline electrolysis
  • AEM anion exchange membrane
  • PEM proton exchange membrane
  • the present invention relates in particular to water electrolysis and generally to low-temperature electrolysis, whereby any separators (such as diaphragms in alkaline electrolysis and membranes in electrolysis with proton or anion exchange membranes) are used. More specific embodiments of the invention take place either in the form of alkaline electrolysis or using anion- or proton-conducting ion exchange membranes.
  • high-temperature electrolysis can also be carried out, which can also be carried out with alkaline electrolytes (i.e. as AEL) with adapted membranes, for example polysulfone membranes, as well as using solid oxide electrolysis cells (SOEC) and high-temperature materials that conduct oxygen ions.
  • AEL alkaline electrolytes
  • SOEC solid oxide electrolysis cells
  • high-temperature materials that conduct oxygen ions.
  • the latter materials include in particular doped zirconium dioxide or doped oxides of other rare earths, which become technically significantly conductive at more than 600°C.
  • specialist literature such as Hauch et al., "Recent advances in solid oxide cell technology for electrolysis", Science 2020, Vol. 370, No. 6513 , and Ebbesen et al. al., "Poisoning of Solid Oxide Electrolysis Cells by Impurities", J. Electrochem. Soc. 2010, Vol. 157, No. 10 , referred to.
  • High-temperature electrolysis which is carried out using one or more solid oxide electrolysis cells, can also be used for the electrochemical production of carbon monoxide from carbon dioxide.
  • oxygen is formed on the anode side and carbon monoxide on the cathode side.
  • the WO 2014/154253 A1 , the WO 2013/131778 A2 , the WO 2015/014527 A1 and the EP 2 940 773 A1 referred to.
  • the present invention has the object of facilitating the production of hydrogen or hydrogen-containing products (a hydrogen-containing product can be a mixture of hydrogen and other components or pure hydrogen) using electrolysis.
  • the present invention proposes a method and a plant for obtaining a hydrogen-containing product using electrolysis with the features of the independent patent claims.
  • Embodiments are the subject of the dependent claims and the following description.
  • electrolysis or electrolysis cell is referred to below in the singular, it is understood that embodiments of the present invention are implemented with several electrolysis cells, whereby corresponding electrolysis cells can in particular be part of an electrolysis stack (cell stack, etc., English stack) of a known type, in which such electrolysis cells are present in large numbers.
  • an electrolysis stack a plurality of arrangements consisting of anode, electrolyte and cathode can be provided, with means for feeding in or removing the respective fluids to be processed or processed being provided on the anode and cathode sides. These are connected to feed or collecting lines that supply the entire electrolysis stack.
  • an electrolysis stack is referred to below in the singular, it is also understood that embodiments with one or more electrolysis stacks can be meant.
  • the temperature of the electrolytic cells can be controlled, for example, by the current or the inlet temperature of a cooling medium, e.g. water, which is supplied to the electrolytic cells.
  • a cooling medium e.g. water
  • the present invention now proposes, in a departure from the known, an operation of an electrolysis, which comprises increasing the operating temperature of an electrolysis stack at a certain point during its life in order to compensate for its performance degradation.
  • the electrolysis is carried out using an electrolysis stack having a plurality of electrolysis cells, the electrolysis cells being produced during a continuous or a discontinuous production period between a first point in time and a second time with an electrolysis voltage applied to the electrolysis stack, and that the electrolysis cells are operated during the production period with an operating temperature set to a default value.
  • the default value for the operating temperature is increased during a continuous or discontinuous partial period that occurs after a predetermined point in time during the operating period.
  • a “discontinuous” period is understood to mean, in particular, an overall period that is made up of sub-periods.
  • an operating period in which electrolysis is carried out and therefore the electrolysis cells are supplied with electricity and corresponding media can be interrupted by various other periods, for example maintenance or repair periods, and still form an overall period, which is particularly between a lifetime - or the beginning of the operating period (Begin of Life, BoL) and the end of the service life or the end of the operating period (EoL).
  • An "increase" of a value can, within the scope of the present invention, be in particular a gradual, step-by-step increase or an increase corresponding to a specific mathematical function. Since this occurs in a discontinuous period, it may also be interrupted by periods of no increase or decrease.
  • the service life of the electrolysis stack can be extended and at the same time the maximum voltage and/or power consumption of the electrolysis stack can be limited.
  • Electrolysis stacks can be used over a longer period of time without exceeding a certain threshold voltage, whereby the nominal production rate and/or current density of the electrolysis plant can be achieved. Overengineering of power supply units can be reduced, as also explained further below with reference to embodiments of the invention, without thereby shortening the service life of the electrolysis stack.
  • the point in time from which the default value for the operating temperature is increased i.e. a corresponding continuous or discontinuous period of time begins, is specified on the basis of at least one parameter that correlates with a degree of degradation of the electrolysis cells of the electrolysis stack. Further details are also explained below. In particular, this makes it possible to precisely select a corresponding point in time and adapt it to real operation.
  • an operating voltage with which the electrolysis cells are operated is increased, the parameter that correlates with a degree of degradation of the electrolysis cells of the electrolysis stack being reached or a threshold value is exceeded by the operating voltage.
  • Such an increase can advantageously be provided to compensate for degradation of the electrolytic cells. It can take place depending, for example, on a production rate of the electrolysis product, in particular in order to keep this constant.
  • a maximum achievable current intensity at which the electrolytic cells are operated can be reduced during a continuous or discontinuous partial period that lies before the specified time, the parameter being associated with a degree of degradation Electrolysis cells of the electrolysis stack correlate, reaching or falling below a threshold value through the maximum achievable current intensity.
  • the maximum achievable operating voltage with which the electrolytic cells are operated is no longer increased during the partial period that lies after the predetermined point in time.
  • the same can also be provided for the maximum achievable current strength.
  • the corresponding voltage or current can be limited and further degradation can be compensated for by the increase in the operating temperature provided in embodiments of the invention.
  • a corresponding threshold value for an operating voltage can be 101 to 150% or 104 to 120% of an initial value of the operating voltage. This makes it possible to provide corresponding power supply units that are only powerful enough to allow this voltage increase. Overdesign can be avoided. Accordingly, a corresponding threshold value for a current can be 50 to 99% or 80 to 96% of the initial value of the current.
  • the electrolysis can be carried out using electrolysis membranes, wherein the electrolysis membranes and/or one or more further components of the electrolysis cells are designed to convert hydrogen permeating through the electrolysis membranes with oxygen to form water.
  • an appropriate material can be introduced into the arrangement of membrane and electrodes. This is designed to recombine the hydrogen that penetrates into the membrane on the anode side of the electrolytic cell with oxygen to form water. Degradation can lead to a thinning of the membrane and thus increase the passage of gas through the membrane. In addition, the permeation of hydrogen and oxygen through typical membrane material may be increased at higher temperatures. Accordingly, when operating a membrane-based electrolysis system at elevated temperatures during a In a state of high degradation, it may be advantageous to incorporate an appropriate means for recombining permeated oxygen and hydrogen in order to meet safety requirements, such as the maximum limit of hydrogen in oxygen.
  • the agent for recombining oxygen and hydrogen can be a catalyst, for example based on platinum, which can be embedded in the membrane, mixed with the anode-side catalyst, or applied as a thin layer between the anode catalyst and the membrane.
  • the electrolysis membranes and/or one or more further components of the electrolysis cells which are designed to convert the hydrogen permeating through the electrolysis membranes with oxygen to form water, can have a platinum-based catalyst.
  • Alternative embodiments of the present invention can also be set up to use alkaline electrolysis, i.e. the electrolysis can be carried out using electrolysis cells that are set up for alkaline water electrolysis, as are basically known from the prior art.
  • embodiments of the present invention can in particular provide for an anode-side hydrogen concentration to be monitored and the operation of the electrolysis to be adjusted depending on this.
  • the operation can be adapted in particular by changing the operating conditions, e.g. the cell voltage and the cell temperature, so that a threshold value of the hydrogen concentration at the anode is not exceeded.
  • the threshold value can in particular be below the lower explosion limit of 4%.
  • threshold values can also be 2% or lower in order to provide an appropriate safety buffer.
  • the hydrogen concentration on the anode side is particularly high at high temperatures and low current densities. Therefore, the measured concentration can be used to set an upper limit on temperature or a lower limit on cell voltage and/or current density. Especially when operating at low load, ie at low Voltage and current density is desired, lowering the temperature to limit the hydrogen concentration at the anode can be advantageous.
  • the operation of the electrolysis can be adjusted or further adjusted according to embodiments of the invention if the anode-side hydrogen concentration exceeds a value of 2% or 4%.
  • the electrolysis can be operated at least temporarily during the operating period with subnominal current densities, with the operating temperature being set depending on the current densities.
  • the temperature can be varied depending on the temporarily applied voltage.
  • the electrolysis stack can be operated at a lower temperature than the operating temperature used at the same degradation or level of degradation and at the rated current density. Operation at this lower current density may be possible despite the given degradation level without increasing the temperature or exceeding the predetermined threshold voltage. Operating at a lower temperature can reduce gas transfer, which can be critical at low current densities, and can reduce degradation.
  • the operating temperature can be increased by reducing a coolant flow through and/or increasing a coolant inlet temperature into the electrolysis cells.
  • the higher operating temperature can be achieved by reducing the coolant flow and/or increasing the temperature of the coolant entering the electrolysis stack.
  • this water can be purified, for example by using an ion exchange resin.
  • the The temperature of the water entering the cleaning unit does not exceed a threshold temperature, for example 60°C.
  • the electrolysis stack temperature can be controlled by a bypass via the heat exchanger that cools the water. More generally, water supplied to the electrolysis cells can be supplied to a temperature control and a cleaning device in an adjustable first portion, and a remaining portion can be guided around the temperature control and cleaning device (or only the temperature control or the cleaning device) and recombined with the first portion downstream of this. Thus, at least part of the water that is guided around the temperature control unit can also be guided around the cleaning unit, so that the water at the inlet of the electrolysis stack can have a higher temperature than the water at the inlet of the cleaning unit. Any bypasses of a corresponding type are possible and can be provided in embodiments of the present invention.
  • At least some of the water may be directed to the heat exchanger and the resin at an initial time, while at least another portion of the water bypasses the heat exchanger and the resin.
  • a portion of the anode and/or cathode current may be diverted from the system or bypass the heat exchanger and water purification unit.
  • the system proposed according to the invention for producing a hydrogen-containing product is set up to carry out electrolysis and has an electrolysis stack having a large number of electrolysis cells for carrying out the electrolysis. It is designed to apply an electrolysis voltage applied to the electrolysis stack to the electrolysis cells during a continuous or discontinuous production period between a first point in time and a second point in time and to operate the electrolysis cells during the production period with an operating temperature set to a default value.
  • means are provided which are designed to increase the default value for the operating temperature during a continuous or discontinuous sub-period that occurs after a predetermined point in time during the operating period.
  • FIGS. 1 to 5 are diagrams illustrating the background and features of embodiments of the present invention.
  • Figure 6 illustrates a system according to an embodiment of the invention.
  • Different embodiments of the invention may include, have, consist of, or consist essentially of other useful combinations of the described elements, components, features, parts, steps, means, etc., even if such combinations are not specifically described herein.
  • the disclosure may include other inventions that are not currently claimed but that may be claimed in the future, particularly if included within the scope of the independent claims.
  • the splitting of water into oxygen and hydrogen in electrolysis is an energy-intensive process.
  • the energy required for the water splitting reaction is provided by applying an electrical current to an arrangement of electrolysis cells, the electrolysis stack just explained.
  • the electrical energy consumed by the electrolysis stack can be calculated as the product of the current flowing through each electrolysis cell, the voltage across each electrolysis cell, and the number of electrolysis cells in the electrolysis stack.
  • the voltage across each electrolysis cell is also referred to as cell voltage U cell and can be assumed to be approximately the same for each electrolysis cell in an electrolysis stack.
  • the cell voltage can be divided into the reversible voltage U rev , i.e. the thermodynamic minimum voltage at which a reaction can take place, and an overvoltage.
  • the overvoltage includes the activation overvoltage at the catalyst surface and the voltages required to conduct the cell current across the ohmic resistances of the various components of the electrolysis cell, as well as other overvoltages due to Mass transport limitations. In contrast to the reversible voltage, the overvoltage increases with the current density.
  • the cell voltage of an electrolytic cell is greater than its thermoneutral voltage U tn , i.e. the voltage at which the energy transferred into the electrolytic cell (i.e. the transferred charge multiplied by the applied voltage) is greater than the reaction enthalpy. Accordingly, heat is generated in the electrolysis stack and dissipated via a cooling medium, usually unconverted water.
  • Typical curves for the reversible voltage, the thermoneutral voltage and the cell voltage versus current density are shown in Figure 1
  • the relationship between cell voltage and current density is often referred to as the Ui curve.
  • Figure 2 which represents a current density in A/cm 2 on the horizontal axis against the cell voltage in V on the vertical axis, and in which corresponding curves for temperatures of 30, 40, 55, 60, 70, 80 and 90°C are shown from top to bottom, there is a temperature dependence of the Ui curve.
  • the cell voltage is not only a function of the current density but also of the operating temperature. This relationship is particularly relevant in the context of the present invention. As the operating temperature increases, the reversible voltage decreases due to the underlying thermodynamics of the water splitting reaction. In addition, the various resistances within the electrolysis cell decrease with increasing temperature, which also leads to a decrease in the overvoltage. As a result, the cell voltage and thus the specific energy consumption of the cell decreases with increasing operating temperature. However, it has been shown that increasing the temperature accelerates the degradation of the electrolysis cell, so that a compromise must typically be made between cell efficiency and lifetime.
  • electrolysis plants are operated at constant pressure and constant temperature throughout their entire service life, whereby the temperature of the electrolysis cells can be controlled, for example, by the current or the inlet temperature of a cooling medium, e.g. water, which is supplied to the electrolysis cells.
  • a cooling medium e.g. water
  • the voltage required to maintain the system's nominal hydrogen production is often cited as a criterion for replacing the electrolysis stack.
  • An exchange occurs when a certain threshold is reached. This threshold can be a fixed voltage, for example 2.2 V, or a percentage degradation, for example 10%.
  • a power supply unit must be able to deliver more power at a higher voltage as cells age, which requires at least some degree of overdesign of the power supply unit compared to the requirements at the beginning of the equipment's life.
  • the criterion for replacing the electrolysis stack can therefore also be that the power requirement of the electrolysis stack becomes greater than the maximum output power of the power supply unit at a certain current, or becomes too large for economical operation. More generally, any criterion may be taken into account that is related to the voltage across the electrolysis stack and/or a part of the electrolysis stack reaching a certain upper threshold or the maximum achievable current reaching a certain lower threshold.
  • the present invention proposes an operation of an electrolysis which comprises increasing the operating temperature of an electrolysis stack at a certain point during its service life in order to compensate for its performance deterioration. This can extend the service life of the electrolysis stack and at the same time limit the maximum voltage and/or power consumption of the electrolysis stack. As mentioned, this can comprise increasing the temperature from a certain point up to which degradation is compensated by means of an increase in voltage or a reduction in the maximum achievable current.
  • the drop in performance can preferably initially be compensated by increasing the electrolysis stack voltage until a threshold voltage is reached.
  • an operating voltage of the electrolysis cells of the electrolysis stack is increased from the beginning of the operating period until a threshold voltage is reached, which is selected depending on a nominal voltage of the electrolysis cells of the electrolysis stack.
  • a threshold voltage is reached, which is selected depending on a nominal voltage of the electrolysis cells of the electrolysis stack.
  • This increase can in turn take place during a continuous or discontinuous period, ie the voltage can also be increased in the meantime reduced again, for example to reduce a production rate or because the reduction of reversible degradation effects enables a corresponding reduction.
  • an increase is made, ie in particular the voltage maxima increase before the start of the operating period until they reach a threshold value. This can take place over a period of years.
  • an operating current density of the electrolysis cells of the electrolysis stack can be reduced until a lower threshold current density is reached.
  • a maximum achievable current strength at which the electrolysis cells are operated can be reduced, the parameter that correlates with a degree of degradation of the electrolysis cells of the electrolysis stack being whether the maximum achievable current strength reaches or falls below a threshold value.
  • an interim increase in the current strength can take place as long as the current strength maxima decrease until the threshold value is reached.
  • the threshold voltage in embodiments of the invention, as mentioned, may be expressed in the form of a percentage of the nominal voltage at the beginning of the operating period, and the criterion may be applied to one or more voltages, each measured across one or more cells. Accordingly, a current intensity threshold can be expressed as a percentage of an initial value.
  • the electrolysis stack temperature can be increased from a corresponding period of time in order to achieve the production target without violating the voltage criterion.
  • the proposed strategy allows an electrolysis stack that has experienced a certain degree of degradation to achieve production rates that can no longer be achieved within the nominal temperature and voltage range. Therefore, the proposed strategy allows an extension of the operational lifetime of the electrolysis stack while maintaining the operating conditions, such as the achievable production rate.
  • the resulting temperature and voltage profile over time is shown as an example for stationary operation in Figure 4 , in which an operating period in years is shown on the horizontal axis, a temperature difference between the current operating temperature and the operating temperature at the beginning of the service life or the operating period shown in K on the left vertical axis, and a ratio of the used to the nominal operating voltage in percent on the right vertical axis.
  • the upper curve refers to the voltage ratio, the lower to the temperature difference.
  • FIG. 5 An example trajectory of hydrogen into oxygen at the anode side for the proposed operating strategy is shown in Figure 5 illustrates where the horizontal axis of the horizontal axis according to Figure 4 corresponds, and the vertical axis shows a percentage content of hydrogen in oxygen.
  • Embodiments of the invention which have already been explained above can be used in particular to compensate for negative effects of this.
  • FIG. 6 a system according to an embodiment of the present invention is illustrated using a highly simplified system diagram.
  • the system is numbered 100 in total.
  • the system 100 can be designed for electrolysis using proton exchange membranes or anion exchange membranes, which can be supplied with water on the cathode and/or anode side.
  • the invention is not limited to this, but can in principle also be used with electrolysis cells that are set up for alkaline electrolysis. Corresponding configurations are not shown separately here solely for reasons of clarity.
  • An electrolysis cell or an electrolysis stack is designated 10 and has an anode side A and a cathode side C.
  • a membrane is illustrated with M.
  • a water stream 101 is supplied to the system 100 and is combined with recycling streams 102 and 103. Portions of these recycle streams 102, 103 shown in dashed lines can be branched off beforehand. Operation without recycling streams 102, 103 is also possible.
  • a return of the recycle streams 102, 103 to a downstream position, as also illustrated by dashed arrows, can also be provided.
  • a variable portion of the correspondingly formed water flow can be branched off as a bypass flow 104.
  • a remainder 105 is cooled by means of a heat exchanger 20 and at least a portion of the exit flow of the heat exchanger 20 is then cleaned in a cleaning device 30.
  • a splitting takes place into two feed streams 106 to the anode side A and 107 to the cathode side C.
  • a material stream 108 containing the gaseous anode products, in particular oxygen, and the unreacted water can be removed and fed to a gas-liquid separator 40.
  • the water used as the recycle stream 102 can be separated and a gaseous anode product 110 can be obtained.
  • the anode product can contain hydrogen which has passed into the anode product due to crossover across the membrane.
  • a material stream 109 containing the gaseous cathode products, in particular hydrogen, and the unreacted water can be removed and fed to a gas-liquid separator 50.
  • the water used as the recycle stream 103 can separated and a gaseous cathode product 111 is obtained.
  • the cathode product analogous to the anode product, if no separation or the like is provided, can contain oxygen which has passed into the cathode product due to crossover across the membrane.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
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EP22020474.7A 2022-09-30 2022-09-30 Procédé et installation de production d'un produit contenant de l'hydrogène par électrolyse Pending EP4345191A1 (fr)

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EP22020474.7A EP4345191A1 (fr) 2022-09-30 2022-09-30 Procédé et installation de production d'un produit contenant de l'hydrogène par électrolyse
PCT/EP2023/025411 WO2024068048A2 (fr) 2022-09-30 2023-09-28 Procédé et installation permettant la préparation d'un produit contenant de l'hydrogène en ayant recours à une électrolyse

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EP22020474.7A EP4345191A1 (fr) 2022-09-30 2022-09-30 Procédé et installation de production d'un produit contenant de l'hydrogène par électrolyse

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US20210071310A1 (en) * 2019-04-09 2021-03-11 Panasonic Intellectual Property Management Co., Ltd. Hydrogen system
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CN114561668A (zh) * 2022-03-01 2022-05-31 国家电投集团氢能科技发展有限公司 具有蓄热装置的制氢***和制氢***的控制方法
JP2022139785A (ja) * 2021-03-12 2022-09-26 株式会社豊田中央研究所 水電解システム、水電解システムの制御方法、および水電解方法

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US20050197743A1 (en) * 2003-09-22 2005-09-08 Ali Rusta-Sallehy Electrolyzer cell stack system
WO2013131778A2 (fr) 2012-03-05 2013-09-12 Haldor Topsøe A/S Appareil de production de monoxyde de carbone de haute pureté
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WO2015014527A1 (fr) 2013-07-30 2015-02-05 Haldor Topsøe A/S Processus de production de co à haute pureté par purification par membrane du co produit par une pile à électrolyse à oxyde solide (soec)
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