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EP0157777A1 - Element chimio-electrique possedant au moins une electrode gazeuse - Google Patents

Element chimio-electrique possedant au moins une electrode gazeuse

Info

Publication number
EP0157777A1
EP0157777A1 EP84900135A EP84900135A EP0157777A1 EP 0157777 A1 EP0157777 A1 EP 0157777A1 EP 84900135 A EP84900135 A EP 84900135A EP 84900135 A EP84900135 A EP 84900135A EP 0157777 A1 EP0157777 A1 EP 0157777A1
Authority
EP
European Patent Office
Prior art keywords
gas
electrode
air
chemo
electrolyte
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP84900135A
Other languages
German (de)
English (en)
Inventor
Olle LINDSTRÖM
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.)
Olle Lindstrom AB
Original Assignee
Olle Lindstrom AB
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 Olle Lindstrom AB filed Critical Olle Lindstrom AB
Publication of EP0157777A1 publication Critical patent/EP0157777A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M4/00—Electrodes
    • H01M4/86—Inert electrodes with catalytic activity, e.g. for fuel cells
    • H01M4/8605—Porous electrodes
    • H01M4/8626—Porous electrodes characterised by the form
    • 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
    • C25B1/34—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis
    • C25B1/46—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis in diaphragm cells
    • 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
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M10/00—Secondary cells; Manufacture thereof
    • H01M10/42—Methods or arrangements for servicing or maintenance of secondary cells or secondary half-cells
    • H01M10/4214—Arrangements for moving electrodes or electrolyte
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • 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
    • Y02E60/10—Energy storage using batteries
    • 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
    • Y02E60/50—Fuel cells

Definitions

  • Chemo-electric cell with at least one gas electrode Chemo-electric cell with at least one gas electrode.
  • Gas diffusion electrodes are used in fuel cells, metal/ air batteries, chloral ali cells with air electrodes, etc.
  • one side of the gas diffusion electrodes is in contact with electrolyte while the other side is in contact with the reaction gas, e.g. air.
  • the gas diffu ⁇ sion electrode is thus facing a gas chamber, e.g. an air chamber, on one side and an electrolyte chamber on its other side.
  • the Swedish patent 407721 describes, however, a chemo-electric cell where the gas- and electrolyte cham ⁇ bers have been integrated so that one or both sides of the gas diffusion electrode at the same time is in contact with the electrolyte and the reaction gas.
  • the present invention is related to chemo-electric cells with electrodes of this kind where at least one side is in simultaneous contact with the reaction gas and the electrolyte.
  • Chemo-electric cells with gas diffusion electrodes accord ⁇ ing to the Swedish patent 407721 show great constructive simplicity. Weight and volume are reduced considerably by the integration of the gas- and electrolyte chambers. This reduction causes a somewhat higher resistance which, however, is compensated for by the reduction in weight and volume in relation to the area of the current flow.
  • the present invention is a surprising further development of the arrangement reported in the Swedish patent which in the first hand allows a considerably higher power density counted on the electrode area.
  • the invention also improve the qualities of these electrodes in other respects.
  • gas diffusion electrode shows that the mass transfer by gas diffusion is an important phenomenon in these electrodes.
  • Optimized gas diffusion electrodes e.g. according to the Swedish patents 407721 or 360951 are so designed that the transport of the reactant to the reaction sitesin the inner parts of the gas electrode is rate-determining.
  • the characteristic feature for the invention is that it comprises a chemo-electric cell with at least one gas electrode for electrochemical conversion of a gaseous reactant in primary and secondary iron/air and zink/air batteries, fuel cells for hydrogen/air and ethanol/air, electrochemical oxygen generators, cells for electrolysis of solutions of alkali metal halogenides etc. characterized in that gas spaces (11, 12) are disposed on each side of the gas electrode (6) whereby one gas space, the upstream space (T1) , is connected to means (13, 14) for supply of the reaction gas whereas the other gas space, the downstream space (12) is connected to means (15, 16) for discharge of the spent reaction gas which has been transported through the gas electrode.
  • Figure 1 shows completely schematically the principle, exemplified by an iron/air battery with a gas convection electrode for air in the monopolar embodiment.
  • Figure 2 explains the design of the air electrode in Figure 1.
  • Figure 3 shows a bipolar electrode embodiment.
  • Figure 4 shows a bipolar electrode with a corrugated shape.
  • Fi ⁇ gure 5 shows a gas convection electrode covered with a selective gas permeable coating.
  • Figures 6-10 show in the same principal way as Figure 2 how the invention can be used with different known chemoelectric cells with gas electrodes.
  • Figure 11 shows voltage current curves.
  • the purpose with Figure 1 is only to demonstrate the prin ⁇ ciple.
  • the measures in the figure as well as in the other figures are not correct.
  • the figures show only the most important components.
  • the porous iron electrodes (1) which could be manufactured according to the Swedish patent 360952, are mounted in plastic frames (2) , so as to provide intermediate electrolyte chambers (3) which contain a so-called third electrode (4) supported by a plastic grid (5) .
  • the new gas con ⁇ vection electrode (6) has several things in common with prior art gas diffusion electrodes according to the Swedish patent 407721 with integrated air and electrolyte chambers.
  • the parts which carry electrolyte comprise ribs (7) of a porous material which has been sintered onto the air electrode (6) .
  • FIG. 2 shows a part of the air electrode seen from above.
  • Figure 2 demonstrates the design of the air electrode (6) in more detail.
  • a nickel wire mesh (8) serving as a support and electrical conductor, carries a layer (9) of electrocatalytically active material, e.g. Raney silver bonded with polytetrafluorethylene.
  • the wire mesh is not coated in the area of contact (10) between the sepa ⁇ rator rib (7) and the wire mesh (8) so as to provide a good bond between the separator rib and.the electrode and a good electrolyte contact.
  • Figure 1 and Figure 2 show two gas chambers on each side of the electrode, i.e. the gas chambers (11) and (12) respectively.
  • a continuous electrolyte contact is deve ⁇ loped between the electrolyte chamber (3),. the porous iron electrode (1), the separator rib (7) and the naked part of the air electrode (10) and the active part (9) of the air electrode L which contains a thin electrolyte film whereas it is at the same time permeable for gas.
  • the characteristic feature of the invention is that gas is brought to flow from the gas chamber (11) through the exposed part of the electrode (9) to the gas chamber (12)
  • Gas in this case air, is fed by means of channel system, which is only indicated in the figure by means of the bi-channel (13), to the gas chamber (11).
  • This chamber is in the following called the upstream chamber, since it is located upstream in the gas flow.
  • connection (13) is connected to an outer connection (14) by means of a main channel, which is not shown.
  • the gas is leaving the second gas chamber (12) , which in the following is called the down-stream chamber by means of the bi-channel (15), which is in connection with an
  • Gas is thus delivered to the system by means of the connection (14) and is then distributed to the upstream chambers (11) by means of the bi-channels (13). The gas is then flowing through the electrode to the downstream chambers (12) and leaves by the bi-channel(15) and the connection (16).
  • Figure 1 shows also a bi-channel (17), which is disposed in the lower part of the downstream chamber.
  • This bi- channel is connected to the outer connection (18) with a valve (19).
  • This conduit can be used among other things for draining of the downstream chamber.
  • the upstream- chamber (11) is also furnished with an upper bi-channel (20) which is connected to an outer conduit (21) con- taining the valve (22).
  • This conduit can be used for venting the upstream chamber, e.g. in ,a special embodi ⁇ ment where a gas selective coating is disposed on the surface of the electrode facing the upstream chamber.
  • Electrolyte is carried to the electrolyte chamber (3) by the bi-channel (23) , which is connected to an outer connection (24) ; part of the not shown external electrolyte system.
  • This external electrolyte system contains a surge tank, heat exchangers, pumps, concentration indicators etc.
  • This system is using circulating electrolyte as described in the U.S. patent 3,801,376 where the electro ⁇ lyte is leaving the upper part of the electrolyte chamber by means of an overflow to a surrounding container.
  • the current collectors (25) to the iron anodes are connec ⁇ ted to a main collector (26) .
  • the air cathodes are in the same way furnished with current collectors (27) connected to a main collector (28) .
  • the third electrodes are also connected with the current collectors (29) joined to the main collector (30) . It is evident from this description that it should be no difficulty for the artisan using the spirit of this invention to convert an iron/air battery according to the earlier status of this technology, e.g. represented by the Swedish patent 407721, from the mode of gas diffusion operation to the mode of gas convection opera ⁇ tion. This could be done by means of channels and gas separators to form an upstream side and a downstream side of the gas electrode for convective transport of gas through the electrode.
  • FIG. 3 shows the separating wall or collector (31) of the bipolar electrode, which sepa ⁇ rating wall is electrically conducting but impermeable for electrolyte.
  • One side of this separating wall is in contact with in this case the iron electrode (1) , whereas the other side is in contact with the active layer (5) of the gas electrode by means of contact ele ⁇ ments (32) which connect electrically the air electrode with the separating wall. Gas is flowing from the upstream chambers (11) to the downstream chambers (12).
  • Figure 4 shows an embodiment, where the air electrode has an undulated shape.
  • the nodes on one side are in contact with the separating wall in the points (33) whereas the nodes on the other side are in contact with the separator (34) in the points (35) .
  • the gas is flowing from the upstream chambers (11) to the downstream chambers (12) .
  • the new gas convection electrode lends itself also to an unexpected process improvement which has a great im ⁇ portance.
  • O alkaline electrolyte is that the electrolyte is picking up carbon dioxide from the air.
  • the electrolyte has to be exchanged after about fifty cycles or so in case the system is not equipped with a special scrubber.
  • Figure 5 shows how this problem can be eliminated or at least reduced considerably in importance.
  • the surface of the electrode which is facing the upstream chamber is here coated with a thin film of a selectively permeable po ⁇ lymer (36) .
  • the other surfaces in the upstream chamber are sealed with a tight polymer film (37) .
  • the selec ⁇ tively permeable film or coating permits transport of oxygen molecules to the active part of the air electrode and from there to the downstream chamber (12) .
  • the gas permeable film could be made of silicone rubber. It could also consist of poly-carbonate, poly-urethane, poly-acetate, various vinyl polymers, cellulose-acetate, crosslinked poly-glutamine etc.
  • the thickness of the film is frequently below 1 ⁇ m. It is advisable . to use a backing of e.g. porous polytetrafluorethylene or poly-sulphon (38) so as to support the film and prevent formation of small holes in the film.
  • This technique can also be used with the same advantages with hydrogen containing non-desirable components like nitrogen, smaller quantities of oxygen, carbon dioxide, by means of suitable polymers.
  • a suitable polymer has to be chosen from case to case by means of laboratory tests.
  • Figures 6-12 show in the same principal way as Figure 2 how the invention can be used with different chemo- electric cells with gas electrodes.
  • Figure 6 thus shows the principal design of a bipolar electrode for a cell with phosphoric acid as electrolyte. This design con ⁇ stitutes an application of the invention on. the so- called ABA electrode developed by Engelhard Industries.
  • Figure 6 shows only the hydrogen side of the bipolar electrode. The air side is designed in the same way but the air flow is carried transversely to the flow on the hydrogen side.
  • the impermeable separator wall of the bipolar electrode (31) is here a densified graphite paper.
  • the separating wall is disposed in contact with an element of a carbonized felt structure (39) which is furnished with fine channels (40) so as to facilitate the in-transport of gas (40) .
  • This element (39) corre- sponds to the so-called A-element of the ABA electrode whereas the separating wall (31) corresponds to the B element.
  • the element (39) is serving as an upstream chamber (11).
  • the felt structure (39) is nermeable for gas and contains at the same time a reserve of electrolyte.
  • the gas convection electrode (6) comprises in this case a porous carbon paper, which is catalyzed by means of a noble metal electro-catalyst.
  • the downstream chamber (12) contains a felt structure (40) furnished with chan- nels (41).
  • the felt structure (40) is a non-conductor and is made of e.g. fibres of PTFE which can withstand the chemical environment in question.
  • the other side of the element (40) is in direct contact with the electrolyte element (41), which comprises a porous layer of silicon carbide bonded by PTFE which is completely filled up with phosphoric acid.
  • the downstream chamber (12) is thus situated between the gas convection electrode (6) and the electrolyte element (41).
  • the fuel cell is of course furnished with bi-channels which are disposed so that hydrogen will flow from the upstream chamber ( ' 11) through the gas convection electrode (6) to the downstream cham ⁇ ber (12) .
  • a similar arrangement is disposed on the air- side of the bipolar electrode.
  • FIG. 7 shows one side of a bipolar electrode for a fuel Cell with molten carbonate electrolyte according to the invention.
  • the so-called electrolyte tile (42) is furnished with ribs (43) , which are in contact with the gas convection electrode (6) , which in this case is a cathode of porous nickel oxide.
  • the separating wall (31) is in this case an undulated stainless steelplate which is furnished with ribs (44) which are disposed in electronic contact with the gas convection electrode.
  • An upstream chamber (11) is formed between one- side of the gas convection electrode (6) and a downstream cham- ber (12) on the other side.
  • Other bipolar fuel cells with solid electrolyte e.g.
  • FIG. 8 shows a so-called oxygen generator for electro ⁇ chemical concentration of the oxygen of the air to pure oxygen.
  • the oxygen generator contains an air cathode and an oxygen anode.
  • the oxygen is developed anodic- ally on one side of the separator wall (31) , which is in contact with the ribbed separator (46) .
  • the oxygen gas is leaving through the electrolyte filled channels (47) .
  • the ribbed separator (46) is in its turn in con ⁇ tact with another ribbed separator (48) , the ribs of which (49) are located in corresponding pockets in the undulated gas convection electrode (6) , which are point welded at the separator wall.
  • the upstream chamber (11) and the downstream chamber (12) are formed on each side of the gas convection electrode (6) .
  • the separator ele- ment (46) and (48) have a micro-porous structure so as to prevent leakage of air in the upstream chambers and in the downstream chambers through the separator into the anolyte spaces (47) .
  • FIG 9 shows a detail of a chlor alkali cell with air cathodes, which are designed as gas convection electrodes.
  • the chlorine gas is developed at the dimensionally stable anode (50).
  • the anolyte space (51) is separated from the catholyte space (52) by the membrane (53) which could - be e.g. Nafion ,
  • the catholyte space (52) contains the upstream chamber (11) and the downstream chamber (12) separated by the air electrode (6) .
  • the upstream cham ⁇ ber (11) contains elements (49) of the same kind as shown in Figure 6.
  • the air electrode (6) is in electronic con ⁇ tact with the separator wall (31) by means of contact elements (32) .
  • the gas convection electrode can be coated with a material with a low oxygen over-voltage, e.g. nickel, on the upstream side for oxygen development during charge.
  • the gas convection electrode can also be designed as a two layer electrode (compare Swedish patent 360952) , whereby the layer for oxygen develop ⁇ ment is facing the upstream side. It may also be possible to furnish the downstream side with a similar layer (three layer electrode) .
  • the layers for oxygen de ⁇ velopment have to be porous so that gas can penetrate from the upstream side to the downstream side. We are thus in this case not concerned with barrier layers of the type used in conventional two-layer gas diffusion electrodes.
  • the outer layer for oxygen development should have larger pores than the layer for oxygen re- duction.
  • the gas convection electrode according to the invention could also be used with other rechargeable metal/air batteries than iron/air, e.g. zinc/air batteries.
  • the absence of free electrolyte in the space between the electrodes reduces the tendency to dendrite formation to ⁇ wards the air electrode during charge.
  • Zinc electrodes stabilized with different polymers therefore show a con ⁇ siderable increase of cycle life, when they are used together with gas convection electrodes according to the invention.
  • a third electrode is used in a zinc/air battery den ⁇ drite formation against the third electrode could be reduced considerably, if the third electrode is by mechanical means brought to move up and down slowly duri charge, Figure 10. It may also in this case be possible to use a zinc electrode of the solution type which during charge is precipitated on a perforated thin iron plate (55) the backside of which is in contact with the separa ⁇ tor ribs of. the gas convection electrode.
  • OM? ⁇ elements in the electrolyte space could in this case consist of plates of highly porous sintered polymer
  • upstream chambers have for the sake of simplicity been disposed on one side of the electrode in its entirety and the downstream chambers on the other side of the electrode in its entirety. It is, however, also possible to dispose a sequence of downstream and upstream chambers on each side of the electrode which will produce a gas movement through the electrode back and forth several times ⁇ from the inlet to the outlet.
  • FIG. 13 shows a voltage current curve for such a battery operating in the mode of gas diffusion.
  • the air electrodes were designed according to Figure 2. The air flows were adjusted so that about 50% of the available oxygen was reacting at the electrode. In a comparative experiment the valve (22) was closed almost completely so that about 95% of the incoming air had to pass through the air electrode whereas only 5% was vented through the channel (20) and •its connection (21). This change im ⁇ proved cell performance considerably as is evident from Figure 11.
  • the convection electrode will in general be somewhat thicker with coarser pores and a smaller speci ⁇ fic surface compared to the diffusion electrode whereas the total surface, however, will be somewhat larger.
  • the electrolyte content of the electrode is also somewhat higher.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Metallurgy (AREA)
  • Manufacturing & Machinery (AREA)
  • Inorganic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Sustainable Energy (AREA)
  • Hybrid Cells (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
  • Inert Electrodes (AREA)

Abstract

Dans les électrodes gazeuses connues pour des piles à combustible, des éléments métal/air etc., le réactif gazeux est transporté jusqu'au site de réaction dans l'électrode par diffusion. On appelle ces électrodes des électrodes à diffusion gazeuse. L'invention constitue un développement des électrodes gazeuses avec des chambres de gaz et d'électrolytes intégrées, où le processus de diffusion est remplacé par un processus de convexion. La nouvelle électrode de convexion gazeuse est pourvue d'organes permettant le transport forcé de gaz depuis une chambre en amont (11) au travers d'une partie active de l'électrode (9) jusqu'à une chambre en aval (12). Un côté (ou les deux) de l'électrode est/sont simultanément en contact avec l'électrolyte dans des modes de réalisation bipolaires ou monopolaires. Une membrane sélective perméable au gaz (36) du côté en amont de l'électrode est utilisée dans un mode de réalisation pour séparer les composants indésirables présents dans le gaz de réaction.
EP84900135A 1982-12-08 1983-12-07 Element chimio-electrique possedant au moins une electrode gazeuse Withdrawn EP0157777A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE8206994A SE8206994L (sv) 1982-12-08 1982-12-08 Kemoelektrisk cell med atminstone en gaselektrod
SE8206994 1982-12-08

Publications (1)

Publication Number Publication Date
EP0157777A1 true EP0157777A1 (fr) 1985-10-16

Family

ID=20348909

Family Applications (1)

Application Number Title Priority Date Filing Date
EP84900135A Withdrawn EP0157777A1 (fr) 1982-12-08 1983-12-07 Element chimio-electrique possedant au moins une electrode gazeuse

Country Status (4)

Country Link
EP (1) EP0157777A1 (fr)
JP (1) JPS60500190A (fr)
SE (1) SE8206994L (fr)
WO (1) WO1984002429A1 (fr)

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US4702973A (en) * 1986-08-25 1987-10-27 Institute Of Gas Technology Dual compartment anode structure
US4810485A (en) * 1986-08-25 1989-03-07 Institute Of Gas Technology Hydrogen forming reaction process
US4911993A (en) * 1988-02-01 1990-03-27 Eltech Systems Corporation Bipolar, filter-press, consumable metal anode battery
US5300370A (en) * 1992-11-13 1994-04-05 Ballard Power Systems Inc. Laminated fluid flow field assembly for electrochemical fuel cells
CA3019358A1 (fr) 2016-07-22 2018-01-25 Nantenergy, Inc. Systeme d'elimination de brume pour cellules electrochimiques
JP2019521497A (ja) 2016-07-22 2019-07-25 ナントエナジー，インク． 電気化学セル内の水分及び二酸化炭素管理システム
BR112019004880A2 (pt) 2016-09-15 2019-06-11 Nantenergy, Inc. sistema de bateria híbrida
WO2018075870A1 (fr) 2016-10-21 2018-04-26 Fluidic Inc. Électrode à combustible ondulée
WO2018187561A1 (fr) 2017-04-06 2018-10-11 Jaramillo Mateo Cristian Batterie rechargeable pour réseau électrique et son procédé d'utilisation
US11611115B2 (en) 2017-12-29 2023-03-21 Form Energy, Inc. Long life sealed alkaline secondary batteries
US12237548B2 (en) 2018-06-29 2025-02-25 Form Energy, Inc. Stack of electric batteries including series of fluidly connected unit cells
US11973254B2 (en) 2018-06-29 2024-04-30 Form Energy, Inc. Aqueous polysulfide-based electrochemical cell
CN112805868A (zh) 2018-06-29 2021-05-14 福恩能源公司 金属空气电化学电池构架
CN120049075A (zh) 2018-07-27 2025-05-27 福恩能源公司 用于电化学电池的负电极
US12308414B2 (en) 2019-06-28 2025-05-20 Form Energy, Inc. Device architectures for metal-air batteries
US12294086B2 (en) 2019-07-26 2025-05-06 Form Energy, Inc. Low cost metal electrodes
US11949129B2 (en) 2019-10-04 2024-04-02 Form Energy, Inc. Refuelable battery for the electric grid and method of using thereof
US12381244B2 (en) 2020-05-06 2025-08-05 Form Energy, Inc. Decoupled electrode electrochemical energy storage system

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SE407721B (sv) * 1975-06-18 1979-04-09 Lindstroem Ab Olle Cell for stromalstring eller elektrolys, serskilt metalluftcell, brenslecell eller kloralkalicell

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Title
See references of WO8402429A1 *

Also Published As

Publication number Publication date
JPS60500190A (ja) 1985-02-07
SE8206994D0 (sv) 1982-12-08
SE8206994L (sv) 1984-06-09
WO1984002429A1 (fr) 1984-06-21

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