WO2006046033A1 - Pile a combustible - Google Patents

Pile a combustible Download PDF

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Publication number
WO2006046033A1
WO2006046033A1 PCT/GB2005/004133 GB2005004133W WO2006046033A1 WO 2006046033 A1 WO2006046033 A1 WO 2006046033A1 GB 2005004133 W GB2005004133 W GB 2005004133W WO 2006046033 A1 WO2006046033 A1 WO 2006046033A1
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WO
WIPO (PCT)
Prior art keywords
catalyst
fuel cell
cell stack
anode
fuel
Prior art date
Application number
PCT/GB2005/004133
Other languages
English (en)
Inventor
Alvaro Amieiro-Fonseca
Janet Mary Fisher
David Thompsett
Original Assignee
Johnson Matthey Public Limited Company
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 Johnson Matthey Public Limited Company filed Critical Johnson Matthey Public Limited Company
Publication of WO2006046033A1 publication Critical patent/WO2006046033A1/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
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
    • H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
    • H01M8/0637—Direct internal reforming at the anode of the fuel cell
    • 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
    • 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
    • H01M4/90—Selection of catalytic material
    • H01M4/92—Metals of platinum group
    • 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
    • H01M4/90—Selection of catalytic material
    • H01M4/92—Metals of platinum group
    • H01M4/925—Metals of platinum group supported on carriers, e.g. powder carriers
    • 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
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
    • H01M8/0668—Removal of carbon monoxide or carbon dioxide
    • 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

  • the present invention relates to fuel cell stacks and components that may be incorporated into fuel cell stacks.
  • a fuel cell is an electrochemical cell comprising two electrodes separated by an electrolyte.
  • a fuel e.g. hydrogen or methanol
  • an oxidant e.g. oxygen or air
  • Electrochemical reactions occur at the electrodes, and the chemical energy of the fuel and the oxidant is converted to electrical energy and heat.
  • Fuel cells are a clean and efficient power source, and may replace traditional power sources such as the internal combustion engine in both stationary and automotive power applications.
  • the electrolyte is a solid polymer membrane which is electronically insulating but ionically-conducting.
  • Proton- conducting membranes such as those based on perfluorosulphonic acid materials are typically used, and protons, produced at the anode, are transported across the membrane to the cathode, where they combine with oxygen to create water.
  • the principle component of a polymer electrolyte fuel cell is known as a membrane electrode assembly (MEA) and is essentially composed of five layers.
  • the central layer is the polymer membrane.
  • an electrocatalyst layer typically comprising a platinum-based electrocatalyst.
  • An electrocatalyst is a catalyst that promotes the rate of an electrochemical reaction.
  • a gas diffusion substrate adjacent to each electrocatalyst layer there is a gas diffusion substrate.
  • the gas diffusion substrate must allow the reactants to reach the electrocatalyst layer and must conduct the electric current that is generated by the electrochemical reactions. Therefore the substrate must be porous and electrically conducting.
  • MEAs typically tens or hundreds of MEAs are required to provide enough power for most applications, so multiple MEAs are assembled to make up a fuel cell stack.
  • Field flow plates are used to separate the MEAs. The plates perform several functions: supplying the reactants to the MEAs, removing products, providing electrical connections and providing physical support.
  • Conventional PEMFC membrane materials such as perfluorosulphonic acid materials require the presence of water to facilitate proton conduction. Water is produced by the fuel cell reactions but additional humidification of incoming gases is often necessary, particularly at low current densities. Humidification can be achieved by a number of processes: (i) steam injection, (ii) passing gas through sparger bottles filled with hot water or (iii) use of a Membrane Substrate Assembly (MSA) within the stack
  • Relative humidity reaching the MEA is determined by water temperature in the sparger bottle or at the MSA, or by the amount of steam injected.
  • hydrogen fuel is produced by converting a hydrocarbon fuel (such as methane or gasoline) or an oxygenated hydrocarbon fuel (such as methanol) to a gas stream known as reformate in a process known as reforming.
  • the reforming process typically includes a stage of steam reforming, partial oxidation or autothermal reforming, followed by high temperature and low temperature water gas shift stages.
  • the reformate gas contains hydrogen, about 25% carbon dioxide, small amounts of carbon monoxide (typically at levels of around 1%) and may contain other contaminants.
  • reformer systems include an additional catalytic reactor known as a preferential or selective oxidation reactor. Air or oxygen is injected into the reformate gas stream, which is then passed over a selective oxidation catalyst which oxidises the carbon monoxide to carbon dioxide. This can reduce the levels of CO from about 1% down to below lOOppm, but even at these levels the anode electrocatalyst is poisoned.
  • Electrocatalysts that have increased tolerance to CO such as PtRu alloy catalysts, have been developed.
  • An oxygen or air bleed is typically supplied to fuel cells to oxidise any CO in the fuel to CO 2 .
  • US 5,482,680 describes how a catalyst for the selective oxidation of CO to CO 2 is positioned within the fuel cell stack in a portion of the fuel stream passageway, and oxygen/air is supplied with the fuel.
  • EP 736 921 and WO 00/79628 disclose that catalysts for the selective oxidation of CO to CO 2 can be incorporated into anodes, and WO 00/79628 discloses that the catalysts are preferably supported catalysts with electrically non ⁇ conducting supports. An air bleed is required for these anodes to function effectively.
  • WGS catalysts catalyse the WGS reaction at temperatures of 200-400 0 C.
  • WGS catalysts are commonly used in reformer systems to reduce CO concentration, and the WGS reactors are typically operated at temperatures of between 200-450 0 C.
  • PEM fuel cells typically operate at temperatures of around 100 0 C and, because known WGS catalysts are not active at this temperature, it has not previously been proposed to incorporate WGS catalysts into fuel cells. The present inventors have realised that it would be advantageous to remove CO within the fuel cell by the WGS reaction instead of the selective oxidation reaction.
  • the water gas shift (WGS) reaction has the advantages that it does not require oxygen, so no air bleed is necessary; it produces hydrogen, which can be used in the fuel cell electrocatalytic reactions; and it is less exothermic than the selective oxidation reaction so will not release significant amounts of heat into the cell.
  • selective oxidation catalysts are typically not entirely selective and may consume hydrogen, and their activity may be inhibited at higher concentrations of carbon monoxide (e.g. greater than lOOOppm).
  • the present inventors have recently developed WGS catalysts that are active at temperatures typically found in fuel cells and can therefore be used to reduce CO concentration when incorporated in a fuel cell.
  • the present invention provides a fuel cell stack comprising at least one membrane electrode assembly, comprising a polymer electrolyte membrane interposed between an anode and a cathode, wherein the anode comprises an anode gas diffusion substrate and an anode electrocatalyst layer; and a fuel inlet through which fuel is supplied to the fuel cell stack; characterised in that the fuel cell stack further comprises a catalyst that can promote the water gas shift reaction at a temperature in the range from ambient to 15O 0 C, and the catalyst is located such that fuel supplied at the fuel inlet will contact the catalyst before reaching the anode electrocatalyst layer.
  • the catalyst promotes the WGS reaction at the operating temperature of the fuel cell, so that the CO concentration of the fuel is reduced before it reaches the anode electrocatalyst layer and CO poisoning of the anode electrocatalyst layer is alleviated.
  • the catalyst developed by the inventors comprises gold dispersed on a ceria- zirconia support material. This catalyst is active for the WGS reaction at HO 0 C.
  • Suitable catalysts are likely to comprise gold and/or copper dispersed on a non-conductive support material comprising one or more of ceria, zirconia, iron oxide, zinc oxide and titania. Suitable catalysts can be identified by testing their WGS activity at temperatures from ambient to 15O 0 C.
  • Suitable catalysts will preferably convert at least 70% of CO to CO 2 via the WGS reaction at a temperature in the range from ambient to 15O 0 C, and will most preferably convert at least 80% of CO to CO 2 .
  • the WGS catalyst is located such that fuel supplied at the fuel inlet will contact the catalyst before reaching the anode electrocatalyst layer.
  • the WGS catalyst is associated with the anode gas diffusion substrate.
  • the WGS catalyst may be embedded within the anode gas diffusion substrate, and/or the WGS catalyst may be present on one or both surfaces of the anode gas diffusion substrate, provided that the fuel will contact the WGS catalyst before it reaches the anode electrocatalyst layer.
  • the WGS catalyst may be present as a layer on the majority of a surface of the anode gas diffusion substrate, or may be present as a patch on a small portion of a surface of the anode gas diffusion substrate, e.g. a patch adjacent to the point where fuel enters the anode gas diffusion substrate.
  • the WGS catalyst may be associated with the anode gas diffusion substrate by methods that are within the competence of the person skilled in the art.
  • the WGS catalyst can be incorporated into an ink and sprayed, printed or coated onto the substrate, either across the entire surface of the substrate or just onto a small portion of the surface.
  • the ink suitably comprises the WGS catalyst, a solvent such as water and optionally a binder such as PTFE.
  • the ink further comprises carbon black to increase the conductivity of the WGS catalyst region.
  • the WGS catalyst may be embedded into the substrate by mixing the catalyst with a material such as carbon black that is then embedded into the substrate, e.g. by the methods disclosed in EP 791 974.
  • the present invention provides components that can be used to form a fuel cell stack according to the first embodiment of the invention.
  • the present invention therefore provides a gas diffusion substrate comprising a catalyst that can promote the water gas shift reaction at a temperature in the range from ambient to 150 0 C.
  • the substrate can be incorporated into a membrane electrode assembly, which can be incorporated into a fuel cell stack according to the first embodiment of the invention.
  • An electrocatalyst layer may be present on one surface of the substrate.
  • the present invention also provides a membrane electrode assembly comprising a polymer electrolyte membrane interposed between an anode and a cathode, wherein the anode comprises an anode gas diffusion substrate and an anode electrocatalyst layer, characterised in that the anode gas diffusion substrate comprises a catalyst that can promote the water gas shift reaction at a temperature in the range from ambient to 15O 0 C.
  • the membrane electrode assembly can be incorporated into a fuel cell stack according to the first embodiment of the invention.
  • the fuel cell stack comprises an anode field flow plate adjacent to the anode of the membrane electrode assembly and the WGS catalyst is incorporated into the anode field flow plate.
  • Anode field flow plates typically have channels for the supply of fuel and the WGS catalyst may be incorporated into the channels.
  • the WGS catalyst may be incorporated into the anode field flow plate by methods that are within the competence of the person skilled in the art.
  • the WGS catalyst can be incorporated into an ink and sprayed or printed onto the plate, either across the entire surface of the plate or just into the channels.
  • the present invention provides field flow plates that can be used to form a fuel cell stack according to the second embodiment of the invention.
  • the present invention therefore provides a field flow plate comprising a catalyst that can promote the water gas shift reaction at a temperature in the range from ambient to 15O 0 C.
  • the field flow plate can be positioned adjacent to the anode of a membrane electrode assembly and incorporated into a fuel cell stack according to the second embodiment of the invention.
  • the fuel cell stack comprises at least one humidifier assembly and the WGS catalyst is incorporated into the humidifier assembly.
  • the humidifier assembly suitably comprises a membrane interposed between two gas diffusion substrates. Humidification plates are adjacent to the gas diffusion substrates. Fuel is supplied via a humidification plate to one substrate, and water is supplied via a second humidification plate to the second substrate. Water is transported across the membrane and the fuel is humidified. The fuel may contact the WGS catalyst either in a humidification plate or a gas diffusion substrate of the humidifier assembly.
  • the WGS catalyst may be incorporated in a humidification plate or a gas diffusion substrate of the humidifier assembly by the same methods used to incorporate the catalyst into anode field flow plates and anode gas diffusion substrates.
  • the present invention provides humidifier assemblies than can be used to form a fuel cell stack according to a third embodiment of the invention.
  • the present invention therefore provides a humidifier assembly comprising a catalyst that can promote the water gas shift reaction at a temperature in the range from ambient to 15O 0 C.
  • the WGS catalyst is incorporated adjacent to the fuel inlet, so that the fuel passes over the WGS catalyst immediately after entering the fuel cell stacks
  • the WGS catalyst may be coated on the inside of a fuel supply line or a bed of catalyst may be incorporated into a fuel supply line. Methods of coating catalysts onto the inside of metal tubes are within the competence of the skilled person, e.g dip coating may be used.
  • the WGS catalyst may be coated onto a flow-through catalyst substrate such as a monolith, foam or static mixer, and the flow-through catalyst substrate may be incorporated into the fuel supply line.
  • the present invention further provides a method of operating a fuel cell stack according to the invention, comprising steps of: a) supplying a fuel comprising hydrogen and carbon monoxide at the fuel inlet; b) passing the fuel and water over the WGS catalyst, thereby providing a fuel with a reduced concentration of carbon monoxide; and c) providing the fuel with a reduced concentration of carbon monoxide to the anode electrocatalyst layer.
  • the method further comprises a step of humidifying the fuel, either within the fuel cell stack or before it is supplied to the fuel cell stack. It is possible that sufficient water is present in the stack because the cell reactions produce water, but it is likely that additional humidification will be required. In the fourth embodiment of the invention, wherein the WGS catalyst is incorporated adjacent to the fuel inlet, it will be necessary for the fuel to be humidified before it reaches the fuel inlet.
  • no air bleed is used, i.e. no air is supplied at the fuel inlet.
  • Known fuel cell systems typically employ air bleeds to reduce CO concentration by selective oxidation, but an air bleed is not required when CO concentration is reduced by the WGS reaction.
  • the use of an air bleed reduces fuel cell performance and increases the complexity of the fuel cell stack, so it is an advantage of the present invention that an air bleed is not required.
  • the fuel supplied to the stack suitably comprises up to 20,000p ⁇ m carbon monoxide.
  • the fuel cell stack is preferably operated at a temperature between 9O 0 C and 15O 9 C.
  • Figure 1 shows a portion of a fuel cell stack according to an embodiment of the invention.
  • Figure 2 shows a fuel cell stack according to an alternative embodiment of the invention.
  • Figure 3 shows the amounts of carbon monoxide and carbon dioxide measured at the outlet of a microreactor containing a WGS catalyst.
  • Figure 4 shows the carbon monoxide conversion of a WGS catalyst in a microreactor.
  • FIG. 1 shows a portion of a fuel cell stack comprising two membrane electrode assemblies (1) and a humidification assembly (2).
  • Each membrane electrode assembly comprises a membrane (3), electrocatalyst layers (4), gas diffusion substrates (5) and field flow plates (6).
  • the field flow plates comprise channels (7).
  • the humidification assembly comprises a membrane (3), gas diffusion substrates (5) and humidification plates (8).
  • the humidification plates comprise channels (9).
  • the WGS catalyst can be present in any portion of the fuel cell stack provided that the fuel will contact the catalyst before reaching the anode electrocatalyst layer.
  • the WGS catalyst is incorporated into the gas diffusion substrate (5) of the membrane electrode assembly (1).
  • the WGS catalyst is incorporated into the field flow plate (6).
  • the WGS catalyst is incorporated into the humidification plate (8) or the gas diffusion substrate (5) of the humidification assembly (2).
  • FIG 2 shows a fuel cell stack (10) comprising membrane electrode assemblies (11).
  • the stack (10) has a fuel inlet (12) and a bed of WGS catalyst (13) is adjacent to the fuel inlet. The fuel will contact the WGS catalyst (13) before reaching the MEAs (11).
  • Ceria-zirconia (50:50 mol ratio Ce:Zr, purchased from Rhodia) was calcined at 500 0 C for 2 hours. 19.6g of the ceria-zirconia was slurried in water (1.61) with overhead stirring and warmed to 6O 0 C. Na 2 CO 3 (0.05M) was pumped into the slurry until the pH was 8.0. HAuCl 4 (1.62g, 49.24%Au) was dissolved in water and pumped into the oxide slurry at about lOml/miri. The pH was maintained at 8.0 by addition OfNa 2 CO 3 (0.05M). When the gold addition was complete the reaction slurry was stirred at 6O 0 C for a further 30 minutes. The catalyst was recovered by filtration, washed free of chloride ions and dried overnight at 105 0 C.
  • the WGS activity of the catalyst was tested in a micro-reactor at HO 0 C. Carbon monoxide was passed over the catalyst, initially in the absence of steam. The levels of carbon monoxide and carbon dioxide at the outlet were measured. Figure 3 shows that in the absence of steam some of the carbon monoxide is oxidised to carbon dioxide. This is due to reduction of the ceria surface by the carbon monoxide (this will occur at HO 0 C only in the presence of highly dispersed gold, otherwise temperatures around 400 0 C are needed to reduce surface ceria with carbon monoxide). At 3000s, no carbon dioxide is measured at the outlet, suggesting that the reduction of the ceria surface is complete.
  • Figure 3 shows most of the carbon monoxide is converted to carbon dioxide via the WGS reaction.
  • Figure 4 shows that the percentage carbon monoxide conversion was above 80%.
  • the catalyst is active for the WGS reaction at HO 0 C, so is active at the operating temperature of a PEM fuel cell.
  • the WGS catalyst was incorporated into a catalyst ink comprising carbon black, water and fluorinated organic binder.
  • the ink was coated onto a Toray® carbon paper gas diffusion substrate.
  • An MEA was prepared by combining the WGS catalyst coated carbon paper with an anode, a perfluorosulphonic acid polymer membrane and a cathode.
  • the WGS catalyst coated carbon paper was positioned adjacent to the anode such that the fuel passed through the WGS catalyst region before reaching the anode electrocatalyst. Ex-situ testing of the WGS catalyst confirmed that catalyst activity was retained when the catalyst was formulated for use within the MEA.

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

Abstract

L'invention porte sur une pile à combustible comportant au moins un ensemble d'électrodes membranes, une entrée de combustible et un catalyseur assurant la réaction de conversion à la vapeur à une température allant de la température ambiante à 150 °C, ledit catalyseur étant disposé de manière à ce que le combustible arrivant par l'entrée entre en contact avec lui avant d'atteindre la couche (4) anodique d'électrocatalyseur. La quantité de CO produite dans le combustible est réduite du fait de la réaction de conversion à la vapeur d'eau, qui évite l'empoisonnement de la couche anodique d'électrocatalyseur.
PCT/GB2005/004133 2004-10-27 2005-10-26 Pile a combustible WO2006046033A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GBGB0423812.7A GB0423812D0 (en) 2004-10-27 2004-10-27 Fuel cell stack
GB0423812.7 2004-10-27

Publications (1)

Publication Number Publication Date
WO2006046033A1 true WO2006046033A1 (fr) 2006-05-04

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PCT/GB2005/004133 WO2006046033A1 (fr) 2004-10-27 2005-10-26 Pile a combustible

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WO (1) WO2006046033A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008132493A2 (fr) * 2007-05-01 2008-11-06 Ceres Intellectual Property Company Limited Perfectionnements à ou se rapportant aux piles à combustible
DE102012103189A1 (de) * 2012-04-13 2013-10-17 Ceramtec Gmbh Brennstoffzellensystem und dessen Verwendung
WO2022235304A1 (fr) * 2021-05-03 2022-11-10 Utility Global, Inc. Réacteur électrochimique de conversion catalytique et procédé d'utilisation
US11879179B2 (en) 2021-05-03 2024-01-23 Utility Global, Inc. Hydrogen production system and method of use

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5482680A (en) * 1992-10-09 1996-01-09 Ballard Power Systems, Inc. Electrochemical fuel cell assembly with integral selective oxidizer
EP0791974A1 (fr) * 1996-02-28 1997-08-27 Johnson Matthey Public Limited Company Electrode catalytiquement active à diffusion gazeuse comprenant un substrat non-tissé
US6300000B1 (en) * 1999-06-18 2001-10-09 Gore Enterprise Holdings Fuel cell membrane electrode assemblies with improved power outputs and poison resistance
JP2004066003A (ja) * 2002-08-01 2004-03-04 National Institute Of Advanced Industrial & Technology 燃料改質ガスの水性ガスシフト反応用触媒
US20040191594A1 (en) * 2001-07-27 2004-09-30 Kearl Daniel A. Bipolar plates and end plates for fuel cells and methods for making the same

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5482680A (en) * 1992-10-09 1996-01-09 Ballard Power Systems, Inc. Electrochemical fuel cell assembly with integral selective oxidizer
EP0791974A1 (fr) * 1996-02-28 1997-08-27 Johnson Matthey Public Limited Company Electrode catalytiquement active à diffusion gazeuse comprenant un substrat non-tissé
US6300000B1 (en) * 1999-06-18 2001-10-09 Gore Enterprise Holdings Fuel cell membrane electrode assemblies with improved power outputs and poison resistance
US20040191594A1 (en) * 2001-07-27 2004-09-30 Kearl Daniel A. Bipolar plates and end plates for fuel cells and methods for making the same
JP2004066003A (ja) * 2002-08-01 2004-03-04 National Institute Of Advanced Industrial & Technology 燃料改質ガスの水性ガスシフト反応用触媒

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
PATENT ABSTRACTS OF JAPAN vol. 2003, no. 12 5 December 2003 (2003-12-05) *

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2008132493A2 (fr) * 2007-05-01 2008-11-06 Ceres Intellectual Property Company Limited Perfectionnements à ou se rapportant aux piles à combustible
WO2008132493A3 (fr) * 2007-05-01 2009-03-12 Ceres Ip Co Ltd Perfectionnements à ou se rapportant aux piles à combustible
EA016159B1 (ru) * 2007-05-01 2012-02-28 Серес Интеллекчуал Проперти Компани Лимитед Усовершенствования в области топливных элементов
US8778556B2 (en) 2007-05-01 2014-07-15 Ceres Intellectual Property Company Limited Fuel Cells
DE102012103189A1 (de) * 2012-04-13 2013-10-17 Ceramtec Gmbh Brennstoffzellensystem und dessen Verwendung
WO2013153198A1 (fr) * 2012-04-13 2013-10-17 Elringklinger Ag Système de pile à combustible à haute température tolérant au soufre doté d'un catalyseur interne de déplacement de gaz à l'eau
DE102012103189A8 (de) * 2012-04-13 2014-01-16 Ceramtec Gmbh Brennstoffzellensystem und dessen Verwendung
WO2022235304A1 (fr) * 2021-05-03 2022-11-10 Utility Global, Inc. Réacteur électrochimique de conversion catalytique et procédé d'utilisation
US11879179B2 (en) 2021-05-03 2024-01-23 Utility Global, Inc. Hydrogen production system and method of use

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