EP4269658A1 - Procédé permettant de faire fonctionner une installation d'électrolyse en ce qui concerne la gestion de l'eau et installation d'électrolyse - Google Patents

Procédé permettant de faire fonctionner une installation d'électrolyse en ce qui concerne la gestion de l'eau et installation d'électrolyse Download PDF

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Publication number
EP4269658A1
EP4269658A1 EP22020192.5A EP22020192A EP4269658A1 EP 4269658 A1 EP4269658 A1 EP 4269658A1 EP 22020192 A EP22020192 A EP 22020192A EP 4269658 A1 EP4269658 A1 EP 4269658A1
Authority
EP
European Patent Office
Prior art keywords
feed medium
water
unit
electrolysis
reduction unit
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
Application number
EP22020192.5A
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German (de)
English (en)
Inventor
Carsten Taube
Volker Göke
Andreas Peschel
David Miklos
Katrin Eitzenberger
Jörg Hieckmann
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.)
Linde GmbH
Original Assignee
Linde 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 Linde GmbH filed Critical Linde GmbH
Priority to EP22020192.5A priority Critical patent/EP4269658A1/fr
Priority to PCT/EP2023/025125 priority patent/WO2023208408A1/fr
Publication of EP4269658A1 publication Critical patent/EP4269658A1/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
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C25B15/083—Separating products
    • 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
    • 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
    • C25B15/033—Conductivity
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C25B15/085—Removing impurities
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C25B15/087—Recycling of electrolyte to electrochemical cell
    • 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

Definitions

  • the invention relates to a method for operating an electrolysis system, in particular water management with regard to the ion concentration, as well as such an electrolysis system, which is used, for example, to obtain hydrogen from water.
  • electrolysis in which, for example, water is split into oxygen and hydrogen using electrical energy.
  • water electrolysis which is known, for example, as so-called proton exchange membrane electrolysis (PEM electrolysis, " Proton Exchange Membrane” electrolysis) can be carried out, the basics of which can be found, for example, in “Bessarabov et al: PEM electrolysis for hydrogen production. CRC Press " are known.
  • the electrolysis of water can produce ions that increase the electrical conductivity of the water and thus the risk of short circuits and reduce the lifespan of the electrolysis cells.
  • the present invention therefore has the task of providing improved options for operating an electrolysis system, particularly with regard to water management.
  • Electrolysis systems are typically used to produce or obtain hydrogen using electrolysis.
  • water in particular demineralized water
  • PEM electrolysis a proton exchange membrane
  • HO - radicals increase the decomposition reactions on the fluoridated perfluorosulfonic acid membranes, which are preferably used as cation-conducting solid electrolytes, which leads to the release of fluoride into the water used in the electrolysis unit, which is usually circulated in a circuit on the anode side, but also via the membrane reaches the cathode side.
  • the release of cations and anions into the demineralized water increases the electrical conductivity of the water and thus the risk of a short circuit in the electrolysis unit or the actual electrolysis cell.
  • organic carbon molecules from polymeric materials e.g. water pipes
  • additives e.g. plasticizers, dyes, stabilizers
  • Oxidation reactions with hydrogen peroxide or OH - radicals can break down large molecules into smaller, ionic molecules, which also increase the electrical conductivity of the water.
  • the electrical conductivity of the water should be limited, for example to values below 10 ⁇ S/cm, preferably below 3 ⁇ S/cm, more preferably below 1.5 ⁇ S/cm.
  • a continuous concentration of ions can be counteracted, for example, by using a so-called mixed-bed polisher ion exchange unit (MBP).
  • MBP mixed-bed polisher ion exchange unit
  • ion components in the water supplied to the electrolysis unit as a feed medium and in the water circulated in the circuit are reduced by means of such an ion reduction unit.
  • the release rate of ions such as fluoride is typically relatively high in the first hundred or several hundred hours after starting up a PEM electrolysis, then decreases and ultimately remains at a low level.
  • the maximum fluoride concentration in the circulated water or the feed medium must be a maximum of 50 or if necessary 100, possibly even up to 250 ppb in order to achieve an electrical conductivity of less than 1.5 ⁇ S/cm.
  • the concentration of ions such as fluoride and thus the electrical conductivity can be controlled, i.e. limited to the values mentioned, by using a certain proportion, for example up to 6%, of the circulating medium or water is branched off and cleaned using an ion reduction unit such as an MBP.
  • the ion reduction unit must therefore be designed to clean of ions not only the feed medium supplied from outside (water), which is converted into hydrogen and oxygen during electrolysis, but also the portion diverted from the circulated feed medium and, if necessary, that through the membrane Water that reached the cathode side of the electrolysis unit was collected there and returned to the circuit. Since the amount of water circulated in the circuit per unit of time is usually very high, the ion reduction unit must also be very large. The proportion of up to 6% of the circulating feed medium is usually many times higher than the amount of water supplied as feed medium. In particular, the water occurring on the cathode side of the electrolysis unit has been shown to contribute particularly strongly to increasing the concentration of ions. This ultimately means that the ion reduction unit (e.g. an MBP) has to be very large or very powerful, which is associated with high costs.
  • the ion reduction unit e.g. an MBP
  • part of the feed medium is removed from the circuit, in particular a so-called blown-down is carried out, ie this part of the feed medium is removed for desalination or for the purpose of desalination.
  • This part of the feed medium is in particular removed from the water circuit of the electrolysis unit.
  • the discharged water can be used in various ways and/or ion contents can be reduced in other ways so that the water can be returned to the circuit. If the water that is removed is not returned, more fresh feed medium can be added.
  • At least part of the discharged feed medium is removed from the circulated feed medium.
  • the amount of circulating feed medium is thereby reduced, so that less feed medium has to be fed into the ion reduction unit, which can therefore be made smaller.
  • the amount of feed medium to be freshly supplied per unit of time is greater than the amount of feed medium converted into hydrogen and oxygen per unit of time (possibly plus other losses that otherwise have to be compensated for).
  • Excess, i.e. supplied but not converted feed medium, in particular as part of the circulated feed medium, can then be removed; This part then no longer has to be returned.
  • the excess feed medium can, for example, be at least partially discharged as wastewater.
  • the excess feed medium can at least partially be used (or reused) externally, for example as cooling water. Due to its quality, the discharged feed medium can easily be used elsewhere as process water.
  • the ion concentration can be determined at a suitable location in the electrolysis unit (e.g. together or separately for several types of ions) and/or the conductivity can be measured directly. Depending on the level of the current conductivity, more or less (or even no) water can be removed. Accordingly, more or less feed medium is then supplied fresh.
  • ion components of the removed part of the circulated feed medium are at least partially reduced by means of a second ion reduction unit, in particular selectively (i.e. only certain types of ions such as fluoride).
  • the part of the discharged feed medium treated in this way is then at least partially fed to the first ion reduction unit.
  • the first ion reduction unit itself can therefore be smaller in size since there is a second, possibly different, ion reduction unit.
  • This water (collected water) is collected and preferably supplied as a feed medium at least partially directly, ie without treatment in an ion reduction unit, to the oxygen or anode side of the electrolysis unit.
  • the collection water is expediently freed of hydrogen before it is at least partially fed to the oxygen side of the electrolysis unit. This can be done, for example, by stripping with nitrogen. This not only reduces the proportion of hydrogen in the water, but also improves explosion protection.
  • the collection water is comprised of the part of the circulated feed medium that is discharged.
  • ion components can be reduced therein by means of a third ion reduction unit, in particular selectively (i.e. only certain types of ions such as fluoride).
  • a third ion reduction unit in particular selectively (i.e. only certain types of ions such as fluoride).
  • an anion exchanger can be used;
  • selective fluoride removal is possible (this can be done both regeneratively and non-regeneratively).
  • the part of the circulated feed medium that is removed is fed to the third ion reduction unit, for example as so-called backwash water.
  • the third ion reduction unit is only used in at least one predetermined phase of the electrolysis, in particular the start-up or commissioning (of the system). This makes it possible to take into account the effect that the ion concentration when the system is started up is typically higher than in normal operation, during which the third ion reduction unit is no longer required. Likewise, the third ion reduction unit can also be switched on or off in other operating phases (correspondingly, the water flows may not have to be routed over it). If the third ion reduction unit is not used, the feed medium taken as collection water, in particular after it has been freed of hydrogen, can be fed directly, at least in part, to the oxygen side of the electrolysis unit.
  • the invention also relates to an electrolysis system for producing hydrogen from water, which is set up to carry out a method described above.
  • FIG. 1 A system or electrolysis system 100 is shown schematically, as is known from the prior art, on which the background of the invention will be explained in more detail.
  • the system 100 has a tank or storage tank 110 for water to be supplied as an insertion medium. New water (so-called make-up water) can be supplied externally. From the tank 110, the water can then be fed as stream b to an ion reduction unit 120, in which the ion content of the water is reduced.
  • the ion reduction unit can in particular be a so-called mixed bed polisher ion exchange unit (MBP).
  • MBP mixed bed polisher ion exchange unit
  • an adsorber or a so-called RO-CDI unit RO stands for "Reverse Osmosis", CDI stands for "Capacitive Deionization" also comes into consideration.
  • the system 100 has an electrolysis unit 130, which in turn has an oxygen-water separator 131 (on the oxygen side), an actual electrolysis cell 133 with a proton exchange membrane 134, and a hydrogen-water separator 132 (on the hydrogen side).
  • Water or feed medium, see stream c is removed from the ion reduction unit 120 and fed to the electrolysis unit 130 via the oxygen-water separator 131. From there, the water, cf. stream d, is supplied to the oxygen side of the electrolysis cell 133 by means of a pump 135.
  • the water is split into oxygen and hydrogen. Together with water, oxygen e collects in the oxygen-water separator 131, where oxygen g is separated and removed.
  • the hydrogen f also collects together with water in the hydrogen-water separator 132, where hydrogen h is separated and discharged.
  • both the hydrogen h and the oxygen g can be stored or used directly.
  • the water (collective water) in the hydrogen-water separator 132 is returned via line k to the tank 110, from where it is fed to the ion reduction unit 120 to reduce its ion content.
  • the amount of water per unit of time (volume flow) is therefore greater for stream b than for stream a.
  • the amount per time or the volume flow of water that the ion reduction unit 120 has to cope with is therefore the sum of the amounts per time or the volume flows of the streams a, k and i, which together correspond to the current c.
  • An exemplary volume flow for stream a (make-up water) is 4.2 m 3 /h, that for stream d (and thus the circulated water) is 1590 m 3 /h, and that for stream k is 23, 2 m3 /h.
  • stream i which corresponds to a volume flow of 94.4 m 3 /h.
  • the ion reduction unit 120 must therefore handle a volume flow of 122.8 m 3 /h.
  • FIG 2 a system 200 for carrying out a method according to the invention is shown schematically in a preferred embodiment.
  • Annex 200 largely corresponds to Annex 100 Figure 1 , so that only other or additional components as well as other or additional streams of water or feed medium or anything else should be explicitly explained. By the way, be aware of the Figure 1 and the associated description.
  • no part of the circulated feed medium d is diverted and fed to the ion reduction unit 120.
  • the collection water k from the hydrogen-water separator 132 is not fed to the tank 110, but is first treated in a stripper unit or a stripper 140 with a stripping gas I - such as nitrogen - in order to remove any hydrogen contained.
  • the feed medium or water purified in this way is then fed to the oxygen-water separator 131 without further treatment.
  • part of the circulated feed medium d is branched off via lines n and o as a so-called blow-down (for desalination).
  • the stream n can be wastewater
  • the stream o can be water that is used for other purposes, for example for cooling purposes, in particular outside the system 200.
  • only the current n or only the current o or both can be used in appropriate proportions.
  • the amount per unit of time (or volume flow) that is discharged from the circulated feed medium d as streams n and/or o depends on the electrical conductivity of the circulated feed medium d.
  • a measuring and control device 142 is provided, by means of which, for example, the electrical conductivity in the stream d is measured and a valve 144 is controlled in order to regulate the volume flow of water discharged depending on the electrical conductivity.
  • FIG 3 a system 300 for carrying out a method according to the invention is shown schematically in a further preferred embodiment.
  • Appendix 300 largely corresponds to Appendix 100 Figure 1 , so that only other or additional components as well as other or additional streams of water or feed medium or anything else should be explicitly explained. By the way, be aware of the Figure 1 and the associated description.
  • no part of the circulated feed medium d is diverted and fed to the ion reduction unit 120.
  • the collection water k from the hydrogen-water separator 132 is also not supplied to the tank 110, but is first treated in a stripper unit or a stripper 140 with a stripping gas I - such as nitrogen - in order to remove any hydrogen contained.
  • the feed medium or water purified in this way is then fed to the oxygen-water separator 131 without further treatment.
  • part of the circulated feed medium d is fed via lines p and q to a second ion reduction unit 150 in order to remove ions, i.e. to reduce ion components; This can be done particularly selectively, for example for the particularly relevant fluoride.
  • NaOH r can be supplied from a storage unit 152, which serves to regenerate the anion exchange material. If an MBP is also used here (anion and cation exchange), HCl can also be used as a regeneration chemical. Any waste water s can be discharged from the second ion reduction unit 150 and used for other purposes, for example, while the water t with a reduced ion content is fed to the ion reduction unit 120.
  • the amount per unit of time (volume flow) that is discharged from the circulated feed medium d as current p depends on the electrical conductivity of the circulated feed medium d.
  • a measuring and control device 142 is provided, by means of which, for example, the electrical conductivity and/or the (degassed) cation conductivity in the stream d is measured and a valve 144 is controlled in order to regulate the volume flow of water discharged depending on the electrical conductivity.
  • only the current p, only the current q or both can be dissipated.
  • the ion reduction unit 120 must handle a correspondingly larger volume flow. For example, if 3.64 m 3 /h of water is removed, 7.84 m 3 /h must be handled in the ion reduction unit 120. This value is significantly lower than in the example Figure 1 or system 100. This achieves, for example, a fluoride concentration in the system of ⁇ 100 ppb.
  • FIG 4 A system 400 for carrying out a method according to the invention is shown schematically in a further preferred embodiment.
  • Annex 400 largely corresponds to Annex 100 Figure 1 , so that only other or additional components as well as other or additional streams of water or feed medium or anything else should be explicitly explained. By the way, be aware of the Figure 1 and the associated description.
  • part of the circulated feed medium d is branched off and fed to the ion reduction unit 120 via line i, but this part (in the sense of a volume flow) can be lower than in the system 100 according to Figure 1 .
  • the collected water k from the hydrogen-water separator 132 is not fed to the tank 110, but is first treated in a stripper unit or a stripper 140 with a stripping gas I - such as nitrogen - in order to remove any hydrogen contained.
  • the feed medium or water purified in this way is then fed to a third ion reduction unit 160.
  • part q of the circulated feed medium d is also passed into the third ion reduction unit 160 for treatment.
  • ions are removed from the water streams m and q, i.e. ion components are reduced; This can be done particularly selectively, for example for the particularly relevant fluoride.
  • NaOH r can be supplied from a storage 162, and possibly also HCl as described for the system 300. Any wastewater s can be discharged from the ion reduction unit 160 and used for other purposes, for example, while the water v is fed directly to the oxygen-water separator 131.
  • the second ion reduction unit 150 of the system 300 and the third ion reduction unit 160 of the system 400 can be functionally identical.
  • FIG 5 A system 500 for carrying out a method according to the invention is shown schematically in a further preferred embodiment.
  • Annex 500 largely corresponds to Annex 100 Figure 1 , so that only other or additional components as well as other or additional streams of water or feed medium or anything else should be explicitly explained. By the way, be aware of the Figure 1 and the associated description.
  • part of the circulated feed medium d is branched off and fed to the ion reduction unit 120 via line i, but this part (in the sense of a volume flow) can be lower than in the system 100 according to Figure 1 .
  • the collected water, see stream k, from the hydrogen-water separator 132 is not fed to the tank 110, but is first treated in a stripper unit or a stripper 140 with a stripping gas I - such as nitrogen - in order to contain to remove hydrogen.
  • the feed medium or water purified in this way is then fed to a fourth ion reduction unit 170.
  • ion reduction unit 170 In the fourth ion reduction unit 170 m ions are removed from the water from the stream, i.e. ion components are reduced; This can be done particularly selectively, for example for the particularly relevant fluoride.
  • the water v with reduced ion content is then fed directly to the oxygen-water separator 131.
  • the functional principle of the system 500 basically corresponds to that of the system 400, at least with regard to the water k or m collected on the cathode side.
  • a special feature of the system 500 is that the fourth ion reduction unit 170 is mobile and, for example, only for Commissioning of the system 500 is used. After a hundred or a few hundred hours of operation, it is no longer needed. As mentioned, the ion content in the water is no longer that high anyway.
  • This principle of only temporarily using a further ion reduction unit 170 for the primary ion reduction unit 120 can also be transferred to the other systems 300 and 400, where it concerns the ion reduction units 150 and 160.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Automation & Control Theory (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
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  • Inorganic Chemistry (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)
EP22020192.5A 2022-04-28 2022-04-28 Procédé permettant de faire fonctionner une installation d'électrolyse en ce qui concerne la gestion de l'eau et installation d'électrolyse Pending EP4269658A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP22020192.5A EP4269658A1 (fr) 2022-04-28 2022-04-28 Procédé permettant de faire fonctionner une installation d'électrolyse en ce qui concerne la gestion de l'eau et installation d'électrolyse
PCT/EP2023/025125 WO2023208408A1 (fr) 2022-04-28 2023-03-21 Procédé de fonctionnement d'une installation d'électrolyse en ce qui concerne la gestion de l'eau et installation d'électrolyse

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Application Number Priority Date Filing Date Title
EP22020192.5A EP4269658A1 (fr) 2022-04-28 2022-04-28 Procédé permettant de faire fonctionner une installation d'électrolyse en ce qui concerne la gestion de l'eau et installation d'électrolyse

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EP4269658A1 true EP4269658A1 (fr) 2023-11-01

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EP22020192.5A Pending EP4269658A1 (fr) 2022-04-28 2022-04-28 Procédé permettant de faire fonctionner une installation d'électrolyse en ce qui concerne la gestion de l'eau et installation d'électrolyse

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5993618A (en) * 1996-12-19 1999-11-30 Dirk Schulze, Wolfgang Beyer Bonn Device for generating oxygen or a mixture of ozone and oxygen
EP3396024A2 (fr) * 2017-04-20 2018-10-31 H-TEC Systems GmbH Dispositif électrochimique et procédé de fonctionnement d'un dispositif électrochimique
WO2021228412A1 (fr) * 2020-05-15 2021-11-18 Hoeller Electrolyzer Gmbh Procédé de fonctionnement d'un dispositif d'électrolyse de l'eau
DE102020005242A1 (de) * 2020-08-27 2022-03-03 Linde Gmbh Wärmerückgewinnung bei Elektrolyseprozessen

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP4347972B2 (ja) * 1999-11-22 2009-10-21 株式会社神鋼環境ソリューション 水電解装置

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5993618A (en) * 1996-12-19 1999-11-30 Dirk Schulze, Wolfgang Beyer Bonn Device for generating oxygen or a mixture of ozone and oxygen
EP3396024A2 (fr) * 2017-04-20 2018-10-31 H-TEC Systems GmbH Dispositif électrochimique et procédé de fonctionnement d'un dispositif électrochimique
WO2021228412A1 (fr) * 2020-05-15 2021-11-18 Hoeller Electrolyzer Gmbh Procédé de fonctionnement d'un dispositif d'électrolyse de l'eau
DE102020005242A1 (de) * 2020-08-27 2022-03-03 Linde Gmbh Wärmerückgewinnung bei Elektrolyseprozessen

Non-Patent Citations (4)

* Cited by examiner, † Cited by third party
Title
"Impact of iron and hydrogen peroxide on membrane degradation for polymer electrolyte membrane water electrolysis: Computational and experimental investigation on fluoride emission", JOURNAL OF POWER SOURCES, 2019
P. MAROCCO ET AL.: "Online measurements of fluoride ions in proton exchange membrane water electrolysis through ion chromatography", JOURNAL OF POWER SOURCES, 2021, Retrieved from the Internet <URL:https://doi.orq/10.1016/i.ipowsour.2020.229179>
S. SIRACUSANO ET AL.: "Degradation issues of PEM electrolysis MEAs", RENEWABLE ENERGY, 2018, Retrieved from the Internet <URL:https://doi.Org/10.1016/i.renene.2018.02.024>
S.A. GRIGORIEV ET AL.: "Failure of PEM water electrolysis cells: Case study involving anode dissolution and membrane thinning", INT JOURNAL OF HYDROGEN ENERGY, 2014, Retrieved from the Internet <URL:http://dx.doi.Org/10.1016/i.iihvdene.2014.05.043>

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