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WO2001078173A1 - Procede de fabrication d'une pile a combustible du type polymere solide et procede de fabrication d'une electrode a diffusion de gaz pour cette pile - Google Patents

Procede de fabrication d'une pile a combustible du type polymere solide et procede de fabrication d'une electrode a diffusion de gaz pour cette pile Download PDF

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Publication number
WO2001078173A1
WO2001078173A1 PCT/JP2001/002780 JP0102780W WO0178173A1 WO 2001078173 A1 WO2001078173 A1 WO 2001078173A1 JP 0102780 W JP0102780 W JP 0102780W WO 0178173 A1 WO0178173 A1 WO 0178173A1
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WO
WIPO (PCT)
Prior art keywords
gas diffusion
diffusion electrode
catalyst
exchange resin
fuel cell
Prior art date
Application number
PCT/JP2001/002780
Other languages
English (en)
Japanese (ja)
Inventor
Toshihiro Tanuma
Original Assignee
Asahi Glass Company, Limited
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 Asahi Glass Company, Limited filed Critical Asahi Glass Company, Limited
Publication of WO2001078173A1 publication Critical patent/WO2001078173A1/fr

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Classifications

    • 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
    • H01M8/10—Fuel cells with solid electrolytes
    • H01M8/1004—Fuel cells with solid electrolytes characterised by membrane-electrode assemblies [MEA]
    • 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
    • H01M4/8663—Selection of inactive substances as ingredients for catalytic active masses, e.g. binders, fillers
    • H01M4/8668—Binders
    • 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
    • H01M4/8803—Supports for the deposition of the catalytic active composition
    • H01M4/881—Electrolytic membranes
    • 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
    • H01M4/8875—Methods for shaping the electrode into free-standing bodies, like sheets, films or grids, e.g. moulding, hot-pressing, casting without support, extrusion without support
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M2300/00—Electrolytes
    • H01M2300/0017—Non-aqueous electrolytes
    • H01M2300/0065—Solid electrolytes
    • H01M2300/0082—Organic polymers
    • 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
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/50—Manufacturing or production processes characterised by the final manufactured product

Definitions

  • the present invention relates to a method for manufacturing a polymer electrolyte fuel cell and a method for manufacturing a gas diffusion electrode therefor.
  • the present invention relates to a polymer electrolyte fuel cell, particularly to a polymer electrolyte fuel cell having excellent initial activity and capable of obtaining a stable output for a long period of time, and a method for producing a gas diffusion electrode therefor.
  • a fuel cell is a battery that directly converts the reaction energy of a gas serving as fuel into electric energy.
  • a hydrogen-oxygen fuel cell has the characteristic that its reaction product is in principle only water.
  • polymer electrolyte fuel cells that use ion exchange membranes as electrolyte membranes can operate at room temperature and provide high power density.
  • polymer electrolyte fuel cells which are expected to be used as power sources for electric vehicles and stationary power sources, usually use proton-conducting ion exchange membranes as electrolyte membranes.
  • An ion exchange membrane made of a perfluorocarbon polymer having a sulfonic acid group (hereinafter referred to as a sulfonic acid type perfluorocarbon polymer) has excellent basic characteristics.
  • gas diffusion electrodes are formed on both sides of this ion exchange membrane, and power is generated by supplying a gas containing hydrogen, which is the fuel, to the anode, and oxygen and air, which are the oxidizing agents, to the power source.
  • the catalyst contained in the catalyst layer of the gas diffusion electrode usually has a high loading ratio of a platinum-based noble metal catalyst or platinum alloy catalyst on a conductive carbon black carrier with a large specific surface area. And used with good dispersibility.
  • the electrolyte, the catalyst, and the fuel gas are simultaneously present.
  • the electrolyte, the catalyst, and the fuel gas hydrogen or oxygen
  • ion exchange resin is contained in the electrode layer, and the catalyst is coated with ion exchange resin to expand the three-phase interface. Let me.
  • a platinum-supported carbon catalyst powder and a solution of an ion-exchange resin composed of a sulfonic acid-type perfluorocarbon polymer are mixed, and the catalyst is coated with the resin.
  • the state of the coating of the catalyst powder with the resin differs depending on the pore structure, the aggregation state, and the like of the catalyst powder.
  • a method to increase the three-phase interface by increasing the resin coverage of platinum is being studied.
  • the coverage cannot be increased due to the influence of the pore structure and the aggregation state of the carbon carrier used for the platinum-supported carbon catalyst, and the output characteristics are not sufficient. Disclosure of the invention
  • the present invention provides a method for producing a gas diffusion electrode for a polymer electrolyte fuel cell, in which the three-phase interface is enlarged, the resin coverage of the catalyst is high, and the pore volume of the power catalyst is large as compared with the conventional art.
  • the purpose is to do.
  • Still another object of the present invention is to provide a method for producing a polymer electrolyte fuel cell having excellent initial output characteristics and a stable output over a long period of time by having the gas diffusion electrode.
  • the present invention relates to a method for producing a gas diffusion electrode for a polymer electrolyte fuel cell having a catalyst layer disposed adjacent to an electrolyte membrane comprising an ion exchange membrane and comprising a catalyst and a fluorine-containing exchange resin.
  • a solvent capable of dissolving the fluorinated ion exchange resin After bringing the catalyst and the fluorinated ion exchange resin into contact with each other in a solvent capable of dissolving the fluorinated ion exchange resin, the solid obtained by removing the solvent is converted into a saturated hydrocarbon or an aromatic hydrocarbon.
  • a fluorinated alcohol, a fluorinated ether and a fluorinated alkane are dispersed in at least one dispersion medium selected from the group consisting of the above, and the catalyst layer is formed using the obtained dispersion.
  • the present invention provides a method for producing a gas diffusion electrode for a polymer electrolyte fuel cell.
  • the present invention is a method for producing a polymer electrolyte fuel cell comprising a membrane-electrode assembly in which gas diffusion electrodes are arranged and bonded on both sides of an electrolyte membrane composed of an ion exchange membrane, A method for manufacturing a polymer electrolyte fuel cell, wherein a gas diffusion electrode arranged on at least one side of the above is manufactured by the method for manufacturing a gas diffusion electrode.
  • the catalyst layer of the gas diffusion electrode obtained by the present invention contains a catalyst and a fluorinated ion exchange resin.
  • a catalyst a substance which promotes an electrode reaction with an anode and a power source is used, and a platinum group metal such as platinum or an alloy thereof is preferable.
  • the catalyst may be used as fine particles as they are, but it is preferable to use a supported catalyst, and as the carrier, it is preferable to use activated carbon having a specific surface area of 20 Om 2 Zg or more, a power pump rack or the like.
  • the amount of supported metal is preferably 10 to 70% of the total mass of the catalyst.
  • the amount of supported metal is preferably 10% or more.
  • the fluorinated ion exchange resin contained in the catalyst layer has an ion exchange capacity of 0.5 to 2.0 milliequivalent Z gram dry resin, particularly 0.8 to 1.5 in terms of conductivity and gas permeability. Preferably, it is a milliequivalent / gram dry resin.
  • the fluorine-containing ion exchange resin is preferably made of a copolymer containing a polymerization unit based on tetrafluoroethylene and a polymerization unit based on a perfluorovinyl compound having a sulfonic acid group.
  • One O p - is preferably one represented by S_ ⁇ 3 H - (CF 2) n .
  • X is a fluorine atom or a trifluoromethyl group
  • m is an integer of 0 to 3
  • n is an integer of 1 to 12
  • p is 0 or 1.
  • preferred specific examples include compounds represented by any one of formulas 1 to 3 below. However, in the following formula, q and r are integers of 1 to 8, and t is an integer of 1 to 3.
  • CF 2 CFOCF 2 CF (CF 3 ) O (CF 2 ), .S 0 3 H Equation 2
  • the catalyst and the fluorinated ion exchange resin contained in the catalyst layer of the gas diffusion electrode are such that the mass ratio of the catalyst to the fluorinated ion exchange resin is 40:60 to 95: 5 in terms of electrode conductivity and water repellency. Is preferred. Particularly, 60:40 to 80:20 is preferable.
  • the mass of the catalyst in the case of a supported catalyst includes the mass of the carrier.
  • the solvent dissolving the fluorinated ion exchange resin is at least one selected from the group consisting of alcohols having 1 to 6 carbon atoms, ethers having 2 to 6 carbon atoms, and dialkyl sulfoxide having 2 to 6 carbon atoms. Is preferred.
  • Water and the like may be mixed with these solvents and used.
  • Specific examples of the solvent include methanol, ethanol, 1-propanol, 2-propanol, 1-butanol, 2-butanol, 1,4-dioxane, n-propyl ether, and dimethyl sulfo. Oxide and the like.
  • the catalyst is dispersed in the solution and the fluorinated ion exchange resin is brought into contact with the catalyst. At this time, it is considered that the fluorinated ion exchange resin is adsorbed on the catalyst.
  • the solid content concentration (the total amount of the fluorinated ion exchange resin and the catalyst) in the dispersion obtained by the above operation is 0.1 to 20%, particularly 1 to 15% of the total mass of the dispersion. Power is preferred. If the solid content concentration is too low, the efficiency of the solvent removal operation in the next step is poor.
  • the solvent is removed from the above-mentioned dispersion liquid, and it is preferably dried. This operation is important for firmly coating the catalyst with the fluorinated ion exchange resin. It is preferable to completely remove the solvent, but if it is removed at least until the content of the solid matter becomes 5% or less, the fluorine-containing ion exchange will be performed when the above catalyst is dispersed in the solvent in the next step. This is preferable because the resin does not elute into the liquid phase. +
  • the removal of the solvent is preferably performed by heating at a temperature at which the fluorinated ion exchange resin does not deteriorate, and preferably at 180 ° C. or lower. It is also preferable to heat under reduced pressure using an evaporator. When using an evaporator, it is preferable to heat at a temperature of about 40 to 70 ° C.
  • the solvent removal operation is preferably performed in an atmosphere containing no oxygen, such as a nitrogen atmosphere.
  • the solid obtained by removing the solvent is dispersed in a dispersion medium, and the dispersion medium includes a saturated hydrocarbon, an aromatic hydrocarbon, a fluorinated alcohol, a fluorinated ether, and a fluorinated alkane.
  • the dispersion medium used here is preferably difficult to dissolve the fluorinated ion-exchange resin.
  • the pore volume of the catalyst When dispersed in the dispersion medium, the pore volume of the catalyst can be increased, and the number of reaction fields can be increased, so that the performance as a polymer electrolyte fuel cell is improved.
  • the reason why the pore volume of the catalyst becomes large is not always clear, but is considered as follows.
  • the molecular chain of the fluorine-containing ion-exchange resin adsorbed in the pores of the catalyst is entangled.
  • the molecular chain of the fluorinated ion exchange resin is elongated and the pore volume is increased. Due to the large pore volume, the resulting gas diffusion electrode uses a fluorine-containing ion exchange resin. It is thought that the three-phase interface where the catalyst, the resin and the fuel gas (hydrogen or oxygen) are present is enlarged, and the output of the obtained fuel cell is increased.
  • the fluorinated ion exchange resin When a dispersion medium in which the fluorinated ion exchange resin is swollen and mixed by mixing with the fluorinated ion exchange resin is used as the dispersion medium, the fluorinated ion exchange resin is adsorbed by the swelling of the fluorinated ion exchange resin.
  • the dispersibility of the catalyst in the dispersion medium is enhanced, and the catalyst is preferably applied when a gas diffusion electrode is produced using the obtained dispersion.
  • the solid When it is difficult to disperse the solid in the dispersion medium, the solid may be dispersed using a dispersant or the like.
  • a dispersing agent a commonly used dispersing agent can be used.
  • Cationic surfactants such as amine salt, quaternary ammonium salt, pyridinium salt, sulfonium salt, phosphonium salt, polyethylenepolyamine, amino acid, beaine, amino sulfate and the like.
  • amphoteric surfactants such as esters and sulfobetaines
  • nonionic surfactants such as alkyl polyoxyethylene and polyhydric alcohols.
  • dispersion medium for dispersing the above-mentioned solids include, as the saturated hydrocarbon, chain hydrocarbons such as hexane, heptane, nonane, and decane, and the like.
  • chain hydrocarbons such as hexane, heptane, nonane, and decane
  • aromatic hydrocarbon benzene and toluene are used.
  • Xylene and the like are used as the saturated hydrocarbon.
  • fluorinated alcohol examples include 2,2,2-trifluoroethanol, 2,2,3,3,3-pentafluoro-1-propanol, 2,2,3,4,4,4-hexafluoro- Examples include 1-butanol and 1,1,1,3,3,3-hexafluoro-21-propanol.
  • fluorinated alkanes examples include 1,3-dichloro-1,1,2,2,3-fluoropentane, 3,3-dichloro-1,1,1,2,2-pentafluorofluoropropane, 1,1, 1,2,2,3,4,5,5,5-decafluoropentane, 1,1,1,1-trichloro-2,2,3,3,3-pentanofluorop Mouth bread, 1; 1, 2, 2, 3,3,4-heptofluorocyclopentane and the like.
  • fluorinated ethers examples include 2,2,3,3,3-pentylfluoromethyl ether, 2,2,3,3,3-pentafluoropropylfluoromethyl ether, 1,1 1,3,3,3-pentanofluoro-2-trifluoromethylpropyl methyl ether, 1,1,1,2,2,3,3,4,4-nonafluorobutyl methyl ether, 1,1,1,2 , 2, 3, 3, 4, 4-nonafluorobutylethyl ether and the like.
  • the solid content concentration (total amount of the catalyst and the resin) when dispersing the solid in the dispersion medium is preferably 0.01 to 20%, particularly 0.1 to 15% of the total weight of the dispersion. No. If the solid content is too low, a catalyst layer having a predetermined thickness cannot be obtained unless the coating is repeated many times in producing a catalyst layer by coating with a dispersion, resulting in poor production efficiency. If the solid content is too high, the viscosity of the dispersion is too high, and the catalyst layer obtained by coating the dispersion tends to be non-uniform.
  • a catalyst layer of a gas diffusion electrode is prepared using a dispersion in which the solid is dispersed in the dispersion medium.
  • the mass ratio between the catalyst and the fluorinated ion exchange resin in the obtained catalyst layer is 50:50 to 85:15, and particularly preferably 60:40 to 80:20. If this mass ratio is less than 50:50, the pores of the catalyst carrier may be crushed by the resin. In that case, the number of reaction fields decreases, and the performance as a polymer electrolyte fuel cell decreases.
  • the mass ratio is larger than 85:15, the amount of the The catalyst may be insufficiently coated with the exchange resin, and the performance as a polymer electrolyte fuel cell may be reduced.
  • the gas diffusion electrode is disposed adjacent to the ion exchange membrane which is a polymer electrolyte membrane.
  • the gas diffusion electrode may be prepared using the above-mentioned dispersion on both the anode side and the force source side. Only the above-mentioned dispersion liquid may be used.
  • the gas diffusion electrode may be composed of only a catalyst layer prepared using the above-mentioned dispersion liquid.
  • the catalyst layer is disposed adjacent to the electrolyte membrane, and the catalyst layer is formed outside the catalyst layer. It is preferable that a gas diffusion layer is disposed adjacent to the gas diffusion layer, and the gas diffusion electrode is constituted by the catalyst layer and the gas diffusion layer.
  • the following method can be mentioned.
  • a dispersion containing carbon powder and polytetrafluoroethylene (hereinafter referred to as PTFE) is applied to the surface of carbon paper or carbon cloth, and fired in air to form a gas diffusion layer.
  • PTFE polytetrafluoroethylene
  • a dispersion liquid of the above-mentioned catalyst is applied on the gas diffusion layer to form a catalyst layer, and a gas diffusion electrode is formed.
  • a method of forming a catalyst layer on a gas diffusion layer has been described as a method of manufacturing a membrane-electrode assembly.
  • a dispersion of the catalyst is directly applied on an ion exchange membrane.
  • a method of obtaining a membrane-electrode assembly, a method of applying a dispersion of the above-described catalyst on a flat plate to form a catalyst layer, and then transferring the catalyst layer to an ion exchange membrane can also be preferably employed.
  • a separator having a gas flow path for supplying fuel gas is arranged on the outside of the membrane-electrode assembly obtained as described above.
  • a gas containing hydrogen is supplied to the anode, and oxygen is supplied to the power source. Containing gas is supplied.
  • Dispersion liquid 1 was treated with an evaporator at 50 ° C. in a hot water bath to remove the solvent, and 3.7 g of a solid was obtained. This was added to 33.3 g of 2,2,3,3,3-pentanofluoro-11-propanol, mixed well, and dispersed to obtain Dispersion 2.
  • the dispersion 2 was ground in an agate mortar and dried under reduced pressure, and the pore volume was measured using a mercury porosimeter (manufactured by CE Instruments, Inc.). The pore volume was 130 Omm 3 / g.
  • an ion exchange membrane made of sulfonic acid type perfluorocarbon polymer with a ion exchange capacity of 1.0 meq / g dry resin and a thickness of 50 m (trade name: Flemion S membrane, manufactured by Asahi Glass Co., Ltd.) ) It was used.
  • the dispersion 2 was applied once on the above-mentioned ion-exchange membrane so as to have a platinum content of 0.5 mgZcm 2 on both sides of the force source side and the anode side once, and then heated to 120 ° C. After drying for 1 hour, a membrane-electrode assembly (electrode area: 10 cm 2 ) in which a gas diffusion electrode composed of a porous catalyst layer having a thickness of 50 xm was formed on both sides of the membrane was produced.
  • a fuel cell is assembled using the above membrane-electrode assembly, and the fuel cell is supplied with hydrogen to the anode and air to the power source at 0.2 MPa, and 0.60 V at a cell temperature of 70 ° C. was operated continuously with a constant voltage drive. Power density (AZcm 2 ) When the temporal change was measured, the results shown in Table 1 were obtained.
  • Dispersion liquid 3 was prepared in the same manner as in Example 1 except that hexane was used instead of 2, 2, 3, 3, 3-pentafluoro-1-propanol, and a gas diffusion electrode was prepared using this. did. Using this gas diffusion electrode, a membrane-electrode assembly was produced in the same manner as in Example 1, and evaluated in the same manner as in Example 1. Table 1 shows the results. The dispersion 3 was dried in the same manner as the dispersion 2 and the pore volume was measured. The pore volume was 1200 mm 3 g.
  • Dispersion 4 was prepared in the same manner as in Example 1, except that ethanol was used instead of 2,2,3,3,3-pentanofluoro-1-propanol, and a gas diffusion electrode was formed using this. Produced. Using this gas diffusion electrode, a membrane-electrode assembly was produced in the same manner as in Example 1, and evaluated in the same manner as in Example 1. Table 1 shows the results. The dispersion 4 was dried in the same manner as the dispersion 2 and the pore volume was measured to be 75 OmmVg.
  • a membrane-electrode assembly was prepared in the same manner as in Example 1 except that the dispersion 1 in Example 1 was used as it was as a coating liquid for preparing a gas diffusion electrode, and was evaluated in the same manner as in Example 1. Table 1 shows the results.
  • the dispersion 1 was dried in the same manner as the dispersion 2 and the pore volume was measured to be 80 Omm 3 Zg.
  • a gas diffusion electrode is formed simply and satisfactorily on the surface of an ion exchange membrane, and a polymer electrolyte fuel cell using the obtained gas diffusion electrode has a high output and a long continuous operation. Even with this, there is little deterioration over time.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Manufacturing & Machinery (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Sustainable Energy (AREA)
  • Inert Electrodes (AREA)
  • Fuel Cell (AREA)

Abstract

Cette invention se rapporte à un procédé de fabrication d'une électrode à diffusion de gaz, qui consiste à mettre en contact une résine d'échange ionique contenant du fluor avec un catalyseur dans un solvant capable de dissoudre la résine d'échange ionique contenant du fluor, à retirer le solvant pour former un solide, à disperser le solide dans un milieu de dispersion, tel qu'un hydrocarbure saturé, un hydrocarbure aromatique ou un éther contenant du fluor, et à former une couche catalyseur à partir de la dispersion qui en résulte; à un procédé de fabrication d'une pile à combustible de type polymère solide, qui consiste à disposer une électrode à diffusion de gaz fabriqué par le procédé décrit ci-dessus sur au moins un côté d'un film électrolyte polymère, et à joindre cette électrode et ce film électrolyte. Une pile à combustible de type polymère solide fabriquée par ce procédé possède d'excellentes caractéristiques de sortie initiale et peut également conserver une sortie de niveau élevée sur une longue période.
PCT/JP2001/002780 2000-04-05 2001-03-30 Procede de fabrication d'une pile a combustible du type polymere solide et procede de fabrication d'une electrode a diffusion de gaz pour cette pile WO2001078173A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2000103935 2000-04-05
JP2000-103935 2000-04-05

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002151088A (ja) * 2000-11-09 2002-05-24 Asahi Glass Co Ltd 固体高分子型燃料電池の製造方法
WO2003100891A1 (fr) * 2002-05-28 2003-12-04 Nec Corporation Electrode catalysante pour pile a combustible, pile a combustible ainsi equipee, et procedes d'elaboration correspondants
JP2009252560A (ja) * 2008-04-07 2009-10-29 Asahi Glass Co Ltd 固体高分子形燃料電池用ガス拡散層形成用塗工液および固体高分子形燃料電池用ガス拡散層の形成方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH04305249A (ja) * 1991-04-03 1992-10-28 Matsushita Electric Ind Co Ltd 液体燃料電池用触媒の製造方法及びその電極の製造方法
JPH07130376A (ja) * 1993-11-03 1995-05-19 Tokyo Gas Co Ltd 固体高分子型燃料電池用電極の触媒処理法
JPH08148152A (ja) * 1994-11-17 1996-06-07 Tokyo Gas Co Ltd 固体高分子型燃料電池用電極及びその製造方法
JPH08236122A (ja) * 1995-02-27 1996-09-13 Asahi Glass Co Ltd ガス拡散電極及び該電極製造用の触媒分散液
JPH11307108A (ja) * 1998-04-23 1999-11-05 Asahi Glass Co Ltd 固体高分子電解質型の燃料電池用電極−膜接合体の製造方法

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH04305249A (ja) * 1991-04-03 1992-10-28 Matsushita Electric Ind Co Ltd 液体燃料電池用触媒の製造方法及びその電極の製造方法
JPH07130376A (ja) * 1993-11-03 1995-05-19 Tokyo Gas Co Ltd 固体高分子型燃料電池用電極の触媒処理法
JPH08148152A (ja) * 1994-11-17 1996-06-07 Tokyo Gas Co Ltd 固体高分子型燃料電池用電極及びその製造方法
JPH08236122A (ja) * 1995-02-27 1996-09-13 Asahi Glass Co Ltd ガス拡散電極及び該電極製造用の触媒分散液
JPH11307108A (ja) * 1998-04-23 1999-11-05 Asahi Glass Co Ltd 固体高分子電解質型の燃料電池用電極−膜接合体の製造方法

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002151088A (ja) * 2000-11-09 2002-05-24 Asahi Glass Co Ltd 固体高分子型燃料電池の製造方法
JP4529276B2 (ja) * 2000-11-09 2010-08-25 旭硝子株式会社 固体高分子型燃料電池の製造方法
WO2003100891A1 (fr) * 2002-05-28 2003-12-04 Nec Corporation Electrode catalysante pour pile a combustible, pile a combustible ainsi equipee, et procedes d'elaboration correspondants
JP2009252560A (ja) * 2008-04-07 2009-10-29 Asahi Glass Co Ltd 固体高分子形燃料電池用ガス拡散層形成用塗工液および固体高分子形燃料電池用ガス拡散層の形成方法

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