US20140014527A1 - Method for mounting oxygen-consuming electrodes in electrochemical cells and electrochemical cells - Google Patents

Method for mounting oxygen-consuming electrodes in electrochemical cells and electrochemical cells Download PDF

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Publication number
US20140014527A1
US20140014527A1 US13/992,456 US201113992456A US2014014527A1 US 20140014527 A1 US20140014527 A1 US 20140014527A1 US 201113992456 A US201113992456 A US 201113992456A US 2014014527 A1 US2014014527 A1 US 2014014527A1
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Prior art keywords
oxygen
film
consuming electrodes
consuming
silver
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Andreas Bulan
Michael Grossholz
Randolf Kiefer
Peter Woltering
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Covestro Deutschland AG
Thyssenkrupp Nucera Italy SRL
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Bayer Intellectual Property GmbH
Uhdenora SpA
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Assigned to UHDENORA S.P.A., BAYER INTELLECTUAL PROPERTY GMBH reassignment UHDENORA S.P.A. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: WOLTERING, PETER, KIEFER, RANDOLF, DR., BULAN, ANDREAS, GROSSHOLZ, MICHAEL
Publication of US20140014527A1 publication Critical patent/US20140014527A1/en
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    • C25B11/035—
    • 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
    • C25B11/04—Electrodes; Manufacture thereof not otherwise provided for characterised by the material
    • C25B11/051—Electrodes formed of electrocatalysts on a substrate or carrier
    • C25B11/052—Electrodes comprising one or more electrocatalytic coatings on a substrate
    • 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
    • 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
    • C25B11/02—Electrodes; Manufacture thereof not otherwise provided for characterised by shape or form
    • C25B11/03—Electrodes; Manufacture thereof not otherwise provided for characterised by shape or form perforated or foraminous
    • C25B11/031—Porous electrodes
    • 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
    • C25B11/04—Electrodes; Manufacture thereof not otherwise provided for characterised by the material
    • C25B11/051—Electrodes formed of electrocatalysts on a substrate or carrier
    • 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
    • C25B11/04—Electrodes; Manufacture thereof not otherwise provided for characterised by the material
    • C25B11/051—Electrodes formed of electrocatalysts on a substrate or carrier
    • C25B11/073—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the electrocatalyst material
    • C25B11/091—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the electrocatalyst material consisting of at least one catalytic element and at least one catalytic compound; consisting of two or more catalytic elements or catalytic compounds
    • C25B11/095—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the electrocatalyst material consisting of at least one catalytic element and at least one catalytic compound; consisting of two or more catalytic elements or catalytic compounds at least one of the compounds being organic
    • 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
    • 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
    • H01M4/88—Processes of manufacture
    • 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
    • H01M8/02—Details
    • 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
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T29/00—Metal working
    • Y10T29/49—Method of mechanical manufacture
    • Y10T29/49002—Electrical device making
    • Y10T29/49108—Electric battery cell making

Definitions

  • the invention relates to a method of installing an oxygen-consuming electrode in an electrolysis apparatus and an electrolysis apparatus, in particular for use in chloralkali electrolysis, in which regions which are critical in terms of being gastight are covered in a particular way.
  • the invention starts out from oxygen-consuming electrodes known per se, which are configured as gas diffusion electrodes and usually comprise an electrically conductive support and a gas diffusion layer having a catalytically active component.
  • the oxygen-consuming electrode hereinafter also referred to as OCE for short, has to meet a number of requirements in order to be able to be used in industrial electrolysers.
  • the catalyst and all other materials used have to be chemically stable to sodium hydroxide solution having a concentration of about 32% by weight and to pure oxygen at a temperature of typically 80-90° C.
  • a high degree of mechanical stability is required for the electrodes to be installed and operated in electrolysers having a size of usually greater than 2 m 2 in area (industrial size). Further properties are: a high electrical conductivity, a low layer thickness, a high internal surface area and a high electrochemical activity of the electrocatalyst.
  • Suitable hydrophobic and hydrophilic pores and an appropriate pore structure for the conduction of gas and electrolyte are likewise necessary, as are freedom from leaks so that gas space and liquid space remain separated from one another.
  • the long-term stability and low production costs are further particular requirements which an industrially usable oxygen-consuming electrode has to meet.
  • the OCE should be able to be installed in the electrolysis apparatus and replaced in a simple manner. Various methods have been described for installation.
  • DE 4444114 A1 describes the installation of an OCE by contacting with the base structure of an electrochemical reaction apparatus by formation of a clamp contact.
  • clamp or press contacts it has been found that the electrical contact resistance thereof frequently deteriorates during the course of operation of the arrangement, which results in an undesirable increase in the consumption of electric energy.
  • a further disadvantage is that the regions of the clamping bars are electrochemically inactive and the OCE area is thus reduced.
  • a more electrically durable connection between electrodes and electrochemical reaction apparatus can be achieved by means of welding processes, as described in EP 1041176 A1.
  • a gas diffusion electrode having an unperforated, circumferential, metal margin is used, direct welding to the base structure of the electrode can be carried out.
  • the continuous edge mentioned in EP 1041176 A1 of the electrode base structure requires a perforated or slotted metal sheet as support structure.
  • the electrodes to be integrated therefore often consist of a metallically conductive base structure which is open-pored over the entire region and in the voids of which the electrochemically active composition, hereinafter referred to as coating, is embedded. Attempts to weld the coated electrode directly founder on the decomposition of the coating composition which usually takes place at high joining temperatures.
  • coating composition has to be absent in the welding zone: the open-pored base structure of the electrode is therefore free of coating composition in this region and would allow mixing of the media present on the two sides of the electrode, viz. electrolyte and gas, in the electrochemical reaction apparatus during operation without measures for achieving a sealing action.
  • the uncoated welding zone is provided with liquid or paste-like materials which solidify after some time and seal the open-pored structure at this place at the time of application.
  • Solidification of the sealing materials can, for example, be effected by chemical curing of a liquid or paste-like applied substance. Owing to the usually very chemically aggressive conditions prevailing in the electrochemical reaction apparatus, the operating life of the seals produced in this way has been found to be very short; it varies in the range from weeks to a few months and therefore stands in the way of efficient long-term use of the electrochemical reaction apparatus.
  • DE 10152792 A1 describes a method of producing a connection between a gas diffusion electrode and the base structure of an electrochemical reaction apparatus, in which separation of the media which are present on the front and rear side of the electrode can be ensured by producing an electrically low-ohm join between the margin of the electrode and a metallic fold-like configuration of a circumferential frame which accommodates the margin and the electrically low-ohm connection of the circumferential frame to the base structure of the electrochemical reaction apparatus.
  • the method according to DE 10152792 A1 is characterized in that the folded part of the frame is made of profiles which are cut in the edge regions for a diagonal joint and are joined to one another by means of laser welding or other welding or soldering processes.
  • An overall disadvantage of the method is that the installation measure is very complicated and costly. Replacement of the OCEs is likewise very complicated and cannot be carried out without an appropriate workshop and tools. A further disadvantage affecting the performance is that the folded regions/profiles are electrochemically inactive and active OCE area is thus lost. The consequence is that the OCE is operated at a higher current density than the counterelectrode (anode), which leads to an increase in the electrolysis voltage and to a deterioration in the economics.
  • EP 1029946 A2 describes a gas diffusion electrode consisting of a reactive layer and a gas diffusion layer and a collector plate, e.g. a silver mesh.
  • the coating does not completely cover the collector plate but leaves a margin which is free of coating.
  • a thin, frame-like metal plate, preferably of silver, is applied to the gas diffusion electrode in such a way that the metallic frame covers a very small area of the electrochemically active coating and a sealing action is also achieved.
  • the frame projecting beyond the OCE serves to join the OCE to the electrolysis apparatus, for example by means of welding.
  • This contacting is complicated and covers part of the area of the OCE, as a result of which the local current density of the free OCE area increases and the performance of the electrolyser drops because of a higher electrolysis voltage.
  • the complicated installation results in high manufacturing costs for the electrolyser or high costs for replacing the OCE.
  • DE 10330232 A1 describes the installation of an OCE, in which the production of an electrical contact between OCE and electrolysis apparatus and establishment of a seal between gas space and electrolyte space are carried out in one operation.
  • a metallic strip is placed both on the coating-free margin of the OCE and on the catalyst-coated region of the OCE and joined to the support structure of the electrolysis apparatus by means of laser welding.
  • This process has the disadvantage that the regions of the metallic strip and also of the weld are electrochemically inactive and that the process selected is very complicated.
  • OCEs are not available in dimensions such that only one OCE has to be installed in each electrolyser apparatus, a plurality of OCEs have to be installed in each electrolysis apparatus.
  • the installation can be effected by slight overlapping of the OCEs or by abutting installation. Even if one OCE per electrolysis apparatus were to be available, regions at which the OCE is creased as a result of installation could be present.
  • the OCE sometimes has to be conducted around corners, as a result of which severe mechanical stress acts on the OCE and leaks can occur. As described above, leaks lead to electrolyte being able to get from the electrolyte space into the gas space or gas to get from the gas space into the electrolyte space.
  • the installation of the OCEs in electrolysis apparatuses in which a gas space is separated from an electrolyte space should be such that gas cannot get from the gas space into the electrolyte space and electrolyte cannot get from the electrolyte space into the gas space.
  • the OCE should be leak-free at a pressure difference between the gas space and the liquid space of 1-170 mbar.
  • leak-free means that no visible exit of gas bubbles into the electrolyte space can be observed.
  • liquid-tight means that an amount of liquid of not more than 10 g/(h*cm 2 ) passes through the OCE (where g is the mass of liquid, h is an hour and cm 2 is the geometric electrode surface area).
  • the object has been able, for example, to be achieved by the overlap regions/creased or abutting edges of an OCE being covered during installation with a film comprising a polymeric component and silver oxide.
  • the invention provides a method for the gastight installation of one or more joining oxygen-consuming electrodes in an electrochemical half cell, characterized in that creased regions and/or cracked regions of the oxygen-consuming electrodes and/or abutting edge regions and/or overlap regions of adjacent oxygen-consuming electrodes occurring when the oxygen-consuming electrodes are brought into juxtaposition with the frame of the gas compartment of the half cell are covered with an additional film, hereinafter also referred to as sealing film, which has a composition comparable to the oxygen-consuming electrodes and is thinner than the layer thickness of the oxygen-consuming electrode.
  • the novel method can, in particular, be applied to gas diffusion electrodes which contain silver and/or silver oxide as catalytically active component.
  • the invention preferably relates to the installation of gas diffusion electrodes in an electrolysis apparatus in which a gas space is separated from an electrolyte space.
  • OCEs which are based on silver and whose production is described by way of example in DE 3710168 A1 or EP 115 845 A1 are used. It is likewise possible to use OCEs based on catalysts in which silver is supported on carbon.
  • the sealing film has the same catalytically active material as the oxygen-consuming electrode.
  • the sealing film and/or the oxygen-consuming electrodes are preferably based, independently of one another, on a fluorinated or partially fluorinated polymer, in particular polytetrafluoroethylene (PTFE), and a silver-containing catalytically active material.
  • a fluorinated or partially fluorinated polymer in particular polytetrafluoroethylene (PTFE), and a silver-containing catalytically active material.
  • the catalytically active component in the sealing film and/or in the oxygen-consuming electrodes comprises, independently, silver, silver(I) oxide or silver(II) oxide or mixtures of silver and silver oxide.
  • the content of the catalytically active components in the sealing film particularly preferably comprises at least 50% by weight of silver oxide, particularly preferably at least 80% by weight of silver oxide.
  • a further particularly preferred method according to the invention is characterized in that the sealing film and/or the oxygen-consuming electrodes comprises mixtures which, independently of one another, contain, as catalytically active component, from 70 to 95% by weight of silver oxide, 0-15% by weight of silver metal powder and 3-15% by weight of a fluorinated polymer, in particular PTFE.
  • the sealing film and the oxygen-consuming electrodes are preferably pressed together after application of the sealing film.
  • the sealing film and the oxygen-consuming electrodes join together at their contact points after application of the sealing film when the cell is started up.
  • the overlap or/and abutting regions and/or creased regions are particularly preferably located at places in the electrolysis apparatus in which the electrolysis apparatus exerts mechanical force on the sealing film described after assembly.
  • silver oxide having a particle size distribution having a D50 of 1-30 ⁇ m is used, but coarser or finer powders can also be used.
  • the polymer used should be chemically stable under the conditions under which the OCE is used. For example, in chloralkali electrolysis, the polymer should be stable to 32% strength by weight NaOH at 90° C. in the presence of pure oxygen. It is possible to use, for example, fluorinated or partially fluorinated polymers such as polytetrafluoroethlyene (PTFE). Furthermore, the polymer should likewise be largely stable to the oxidizing action of silver oxide, in particular under manufacturing conditions.
  • PTFE polytetrafluoroethlyene
  • the polymer component is used in such an amount that a handleable film which can withstand mechanical loads is produced.
  • able to withstand mechanical loads means that the sealing film can be installed in an industrial electrolysis apparatus without being destroyed, i.e. no creases or ruptures in which the sealing film forms relatively large holes or wide cracks.
  • a woven reinforcing fabric can be incorporated into the sealing film.
  • the woven reinforcing fabric should have some stability to the oxidizing action of silver oxide, i.e. it should survive the manufacturing process through to the finished sealing film without appreciable corrosion or deterioration in the mechanical properties. Chemical resistance of the woven reinforcing fabric under use conditions is not absolutely necessary. It is therefore also possible to use materials which, for example, are not stable to sodium hydroxide, e.g. polyesters. It is possible to use, for example, electrically conductive supports such as mesh, woven fabric, braid, knitteds, nonwoven or foam composed of metal, in particular nickel, silver or mixtures of nickel and silver or else nickel-copper alloys. It is likewise possible to use nonmetallic resistant materials, e.g. materials based on polypropylene, for the woven reinforcing fabric.
  • the proportion of the polymeric component in the mixture with silver oxide for the sealing film is preferably selected so that electrochemical reduction of the silver oxide in the sealing film can still occur under the conditions of operation of the OCE in the electrolysis apparatus.
  • the proportion of silver oxide is therefore greater than 50% by weight, particularly preferably greater than 80% by weight.
  • polymer for the sealing film particular preference is given to using polytetrafluoroethylene (PTFE).
  • a sealing film can be produced from the polymeric component and the silver oxide in a manner similar to the methods known in principle from the prior art for producing OCEs. This can, for example, be carried out by means of the following different methods:
  • One possibility is to extrude the silver oxide and the polymeric component in powder form to produce a film.
  • the silver oxide is incorporated like a filler into the polymeric component, in the case of PTFE in a manner similar to production of OCEs as described in EP 951500 A1, by paste extrusion to produce a porous sealing film.
  • the silver oxide prefferably be, for example, scattered on a porous PTFE film and subsequently pressed in.
  • the polymer can be processed in a manner analogous to the mixing process described in DE 2941774 and subsequently calendered or pressed with or without a woven reinforcing fabric to give a film.
  • a silver catalyst can preferably be precipitated onto PTFE.
  • a reducing agent is added in the precipitation of silver nitrate with sodium hydroxide in order to reduce the resulting silver oxide directly to silver. If the reducing agent is omitted, silver oxide can be precipitated on PTFE.
  • This material can be filtered off, dried and processed by means of a mixing process according to DE 2941774 A1 to give a powder which can then be pressed as described in DE 3710168 A1 or EP 115 845 A2 to give a film.
  • the sealing film particularly preferably comprises from 60 to 99% by weight of silver oxide and from 1 to 40% by weight of PTFE.
  • a silver powder can optionally be added in addition. This should, in particular, have an average particle diameter of less than 50 ⁇ m.
  • the amount of additional silver powder is particularly preferably from 0 to 15% by weight.
  • the thickness of the sealing film which is preferably used in the novel method is from 10 ⁇ m to 800 ⁇ m, preferably from 50 ⁇ m to 600 ⁇ m.
  • the sealing film is particularly preferably made thin, i.e. with a thickness of less than 500 ⁇ m.
  • the layer thickness of the oxygen-consuming electrode without sealing film is typically from 0.1 to 0.9 mm, preferably from 0.2 to 0.7 mm.
  • the invention further provides an electrochemical half cell having one or more adjoining oxygen-consuming electrodes ( 1 , 1 a ), characterized in that the oxygen-consuming electrodes have creased regions, and/or cracked regions of the oxygen-consuming electrodes and/or abutting edge regions and/or overlap regions of adjacent oxygen-consuming electrodes occurring on installation on the frame of the gas compartment of the cell and these regions are covered with an additional film which has a composition comparable to the oxygen-consuming electrodes and is thinner than the layer thickness of the oxygen-consuming electrode.
  • a preferred electrochemical cell is characterized in that it contains fluorinated polymers, in particular polytetrafluoroethylene (PTFE), in the gas diffusion layer of the oxygen-consuming electrodes.
  • fluorinated polymers in particular polytetrafluoroethylene (PTFE)
  • a further preferred embodiment of the electrochemical cell has an electrically conductive flexible textile structure, in particular composed of metal threads, preferably composed of nickel and/or silver-coated nickel, as additional support element in the oxygen-consuming electrodes and/or in the film.
  • a woven reinforcing fabric preferably comprises a woven metal fabric, e.g. a nickel mesh, silver mesh or silver-plated nickel mesh, in which the mesh opening is greater than 0.1 mm and the wire thickness is greater than 60 ⁇ m. It is likewise possible to use other materials.
  • the sealing film should have a calculated porosity of 20-70%.
  • the calculated porosity is derived from the ratio of the density of the materials used and the amount present in the finished sealing film and also the density of the sealing film produced (without the woven reinforcing fabric).
  • the compaction ratio is in the range from 2 to 5, based on the ratio of film density (without woven reinforcing fabric) to the powder bulk density.
  • FIG. 1 shows a schematic cross section through an electrochemical half cell 2
  • FIG. 2 shows a schematic cross section through a laboratory cell 2 , 10 in the half-opened state—depiction of the abutting region 7
  • FIG. 2 a shows a schematic depiction of the overlap of a sealing film 9 with two oxygen-consuming electrodes 1 and 1 a in the region 7 at which the oxygen-consuming electrodes 1 and 1 a abut one another and also the overlap of a sealing film 9 with a crack 6 in the oxygen-consuming electrode 1 a
  • FIG. 3 shows a schematic cross section through a laboratory cell 2 , 10 —depiction of the overlap region
  • FIG. 3 a shows a schematic depiction of the overlap of a sealing film 9 with two oxygen-consuming electrodes 1 and 1 a in the region 8 in which the oxygen-consuming electrodes 1 and 1 a overlap
  • the thickness of the resulting film 9 was 290 ⁇ m, and the calculated porosity was 44%.
  • the film 9 obtained in this way can be produced as a continuous film. Its width is limited by the width of the rollers of the calender.
  • the film 9 can, when used, be cut to size for the appropriate sealing/crease and/or overlap regions.
  • FIG. 2 a shows, in a schematic side view corresponding to FIG.
  • the anode half cell 10 had an anode 15 made of expanded titanium metal coated with a commercial noble metal oxide-based DSA® coating from Denora. Inflow and discharge of the electrolytes and of the gases are not shown in the figures since they are outside the plane of the section. Since the electrolysis cell was operated as a falling film cell, the cathode inlet is located in the upper part of the half cell and the outlet is located at the lower end of the spacer 12 . The electrolysis cell was subsequently assembled and started up. The alkali pressure at the lower edge of the OCE was 20 mbar.
  • the gas pressure (oxygen) in the gas space 4 was 60 mbar.
  • a sodium chloride solution having a sodium chloride content of 210 g/l served as anolyte and a 30% strength sodium hydroxide solution served as catholyte.
  • the temperature of the electrolytes was about 85° C., and the current density was 4 kA/m 2 . An increase in the cell voltage was not observed.
  • the spacer 12 which keeps the distance between membrane 11 and silver-based OCE 1 ; 1 a constant at 3 mm ran along the abutting edge 7 . After start-up, no gas or liquid breakthrough could be observed.
  • the cell voltage of the laboratory cell was unchanged compared to a cell having a continuous oxygen-consuming cathode without abutting edge 7 .
  • the film 9 also makes it possible to seal, in a manner similar to that described above, creased regions 5 of the oxygen-consuming electrodes 1 , 1 a occurring at the frame 3 of the gas compartment 4 of the half cell 2 (see FIG. 1 ) or overlap regions 8 of adjacent oxygen-consuming electrodes 1 and 1 a (see FIGS. 3 and 3 a ) or else cracks in the oxygen-consuming electrode 1 a in the cracked region 6 (see FIG. 2 a ).

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  • Chemical Kinetics & Catalysis (AREA)
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US13/992,456 2010-12-10 2011-12-05 Method for mounting oxygen-consuming electrodes in electrochemical cells and electrochemical cells Abandoned US20140014527A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102010054159.1 2010-12-10
DE102010054159A DE102010054159A1 (de) 2010-12-10 2010-12-10 Verfahren zum Einbau von Sauerstoffverzehrelektroden in elektrochemischen Zellen und elektrochemische Ze lle
PCT/EP2011/071759 WO2012076472A1 (de) 2010-12-10 2011-12-05 Verfahren zum einbau von sauerstoffverzehrelektroden in elektrochemische zellen und elektrochemische zelle

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US (2) US20140014527A1 (de)
EP (1) EP2649222B1 (de)
JP (1) JP6152054B2 (de)
KR (1) KR101827594B1 (de)
CN (1) CN103562439B (de)
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CA2824795A1 (en) 2012-06-14
EP2649222A1 (de) 2013-10-16
KR101827594B1 (ko) 2018-02-08
JP6152054B2 (ja) 2017-06-21
CA2824795C (en) 2019-03-05
US11136677B2 (en) 2021-10-05
CN103562439A (zh) 2014-02-05
TW201237220A (en) 2012-09-16
DE102010054159A1 (de) 2012-06-14
US20170088961A1 (en) 2017-03-30
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