WO2015014415A1 - Procédé et système de régénération d'empilements de pile à combustible empoisonnée au souffre - Google Patents

Procédé et système de régénération d'empilements de pile à combustible empoisonnée au souffre Download PDF

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Publication number
WO2015014415A1
WO2015014415A1 PCT/EP2013/069497 EP2013069497W WO2015014415A1 WO 2015014415 A1 WO2015014415 A1 WO 2015014415A1 EP 2013069497 W EP2013069497 W EP 2013069497W WO 2015014415 A1 WO2015014415 A1 WO 2015014415A1
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WO
WIPO (PCT)
Prior art keywords
gas
fuel cell
regeneration
anode
sulfur
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PCT/EP2013/069497
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English (en)
Inventor
Thomas Rostrup-Nielsen
Rahul Singh
Original Assignee
Topsøe Fuel Cell A/S
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Publication of WO2015014415A1 publication Critical patent/WO2015014415A1/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
    • H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
    • H01M8/0675—Removal of sulfur
    • 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
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/043—Processes for controlling fuel cells or fuel cell systems applied during specific periods
    • H01M8/04302—Processes for controlling fuel cells or fuel cell systems applied during specific periods applied during start-up
    • 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
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/043—Processes for controlling fuel cells or fuel cell systems applied during specific periods
    • H01M8/04303—Processes for controlling fuel cells or fuel cell systems applied during specific periods applied during shut-down
    • 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
    • H01M8/24—Grouping of fuel cells, e.g. stacking of fuel cells
    • H01M8/241—Grouping of fuel cells, e.g. stacking of fuel cells with solid or matrix-supported electrolytes
    • H01M8/2425—High-temperature cells with solid electrolytes
    • 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
    • H01M8/24—Grouping of fuel cells, e.g. stacking of fuel cells
    • H01M8/241—Grouping of fuel cells, e.g. stacking of fuel cells with solid or matrix-supported electrolytes
    • H01M8/2425—High-temperature cells with solid electrolytes
    • H01M8/243—Grouping of unit cells of tubular or cylindrical configuration
    • 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
    • H01M8/12—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte
    • H01M2008/1293—Fuel cells with solid oxide electrolytes
    • 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
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
    • H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
    • H01M8/04119—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying
    • H01M8/04126—Humidifying
    • 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
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/04313—Processes for controlling fuel cells or fuel cell systems characterised by the detection or assessment of variables; characterised by the detection or assessment of failure or abnormal function
    • H01M8/04664—Failure or abnormal function
    • H01M8/04679—Failure or abnormal function of fuel cell stacks
    • 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
    • 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 a novel method for regen- eration of a sulfur-poisoned fuel cell, fuel cell part, fuel cell stack or fuel cell stack system, especially a solid oxide fuel cell (SOFC) stack. More specifically, the invention concerns a method for regeneration of sulfur- poisoned solid oxide fuel cell stacks by feeding a suitable gas to the anode in the presence of water for a period of time defined as the time needed to regenerate the cell po ⁇ tential partially or completely. The invention further re ⁇ lates to a system for carrying out the method. The method can be used for regeneration of single cells, one or more stacks, an assembly of stacks, systems of stacks, several systems of stacks etc.
  • SOFC solid oxide fuel cell
  • H 2 0 + * 0* + H 2 does not influence the chemisorption of sulfur, and thus water chemisorption cannot displace sulfur.
  • the present invention concerns a method for regenera- tion of a sulfur-poisoned fuel cell, fuel cell part, fuel cell stack or fuel cell stack system, especially a solid oxide fuel cell (SOFC) stack, where said method comprises feeding a suitable gas to the anode in the presence of wa- ter for a period of time defined as the time needed to re ⁇ generate the cell potential partially or completely.
  • SOFC solid oxide fuel cell
  • the anode is preferably a nickel anode, a modified nickel anode with infiltrates, a metal-supported anode or a perov- skite anode.
  • the gas is preferably hydrogen, and hydrogen and water are both supplied externally. Another possibility is that the water is supplied externally, while the hydrogen is gener- ated internally by electrolysis, or that the feed comprises both hydrogen and water, but more hydrogen is generated internally by electrolysis.
  • feed gases such as AdBlue (which is a 32.5 wt% solution of urea in demineral- ized water normally used to reduce emission of nitrogen ox- ides in exhaust gases from heavy diesel vehicles) , will al ⁇ so work.
  • AdBlue which is a 32.5 wt% solution of urea in demineral- ized water normally used to reduce emission of nitrogen ox- ides in exhaust gases from heavy diesel vehicles
  • Anode exhaust from one or more other SOFC stacks can also be used as a regeneration gas, especially if a possible sulfur content is reduced or virtually eliminated, e.g. by a sulfur removal device such as a ZnO material or a Ni material.
  • the regeneration gas has a residence time of be ⁇ tween 1 ms and 10 s.
  • the feed gas comprises 2-80 %, prefer ⁇ ably 10-60 % water, and 40-100 % hydrogen.
  • the feed gas comprises CO (0-100 %) , C0 2 (0-100 %) , H 2 0 (0-100 %), N 2 (0-100 %), CH 4 (0-100 %) and H 2 (0-100 %) .
  • the gas may contain a portion of anode exhaust from another stack system and additional 3 ⁇ 4 is generated internally via elec ⁇ trolysis .
  • the regeneration gas may contain a portion of the outlet of a secondary steam reformer for methane, pro ⁇ pane or LPG (liquefied petroleum gas) , a liquid fuel re ⁇ former, a clean coal pyrolyzer, a syngas generator or a truck exhaust with a cleaning section.
  • a secondary steam reformer for methane, pro ⁇ pane or LPG liquefied petroleum gas
  • a liquid fuel re ⁇ former e.g., a liquid fuel re ⁇ former
  • a clean coal pyrolyzer e.g.
  • a syngas generator e.g., a truck exhaust with a cleaning section.
  • other species may also be removed from the sulfur-poisoned fuel cell, fuel cell part, fuel cell stack or fuel cell stack system, said species being one or more elements selected from C, Si, CI, F, Br, P, Cr, Na, K, Al, Sr, Se, As, Sb, Pb, Hg and Cd.
  • the method according to the invention can be carried out in a once-through system as shown in Fig. 1.
  • the system comprises an optional power supply. If the power supply is not used, the feed stream and the product gas stream will have approximately the same gas composition.
  • the product gas will contain sulfur species, and thus sulfur will be removed from the stack as long as the feed gas has a lower sulfur content.
  • the feed gas contains no sulfur or at least only a negligible amount of sulfur.
  • AdBlue AdBlue
  • feeds can be used as well.
  • a feed it is advantageous to have a relatively high hydrogen content and a suitable water concentration as discussed for preferred compositions, because then a good regeneration throughout the stack is provided. If water is supplied externally, while the hydrogen is generated internally by electrolysis, the hydrogen concentration will be very low at the inlet and the regeneration will be slower than if the feed had some hydrogen. But as the gas passes through the stack, the concentration of hydrogen will increase, making the regen- eration faster.
  • Fig. 4 shows an example of a recycle based system.
  • the gas leaving the SOFC stack exit will contain sulfur and possibly be in equilibrium with the adsorbed sulfur in the stack.
  • a direct recycling of the gas will therefore not re ⁇ sult in any further sulfur removal. It is thus necessary to remove all the sulfur or a part thereof from the recycle gas.
  • This can be done by passing the recycle gas through a sulfur removal device such as an adsorption bed capable of adsorbing sulfur.
  • Said adsorption bed must contain a suitable adsorption material, such as a Ni based reforming cata ⁇ lyst, a ZnO based material or the like.
  • This adsorption bed can be placed in the system in many ways: (a) As shown in Fig. 4 as part of a dedicated route used during regeneration, while under normal SOFC operation the bed is bypassed by the anode recycle typically used. (b) In the anode recycle loop, thus always exposed to gas flow, both in regeneration mode and in typical SOFC operation mode with anode recycle.
  • a recycle flow typically operates at a low ⁇ er temperature than the SOFC exit stream, and thus a cool ⁇ ing heat exchanger is applied.
  • the adsorption bed can be placed either before or after said heat exchanger, but preferably in a position where the temperature is optimal for adsorption, in which case several heat exchangers may be used. Furthermore, by using heat exchangers it is possi ⁇ ble to place valves controlling the recycle flow paths in a cold position, thereby eliminating the need for hot valves.
  • the method for regeneration of a sulfur- poisoned fuel cell stack results in the regeneration of the anode of the fuel cell stack.
  • the voltage potential applied to the sulfur-poisoned fuel cell stack ranges from 0.1 to 5 V per cell, preferably from 0.7 to 1.5 V per cell.
  • the period of regeneration time sufficient to increase the cell potential after regenera ⁇ tion in SOFC mode of the sulfur-poisoned fuel cell stack is from about 0 to about 20 hours, preferably from about 0 to about 3 hours, more preferably from about 0 to about 1 hour .
  • the regeneration is initiated after a detected performance loss or before the cell stack is subjected to an electrical load.
  • de ⁇ tected performance loss could mean any decrease in average cell potential after the cell stack has been subjected to an electrical load for any period of time.
  • the regeneration can be initiated after any percentage de ⁇ crease in average cell potential of the fuel cell stack.
  • the regeneration can be a full regeneration, a partial regeneration or a full regeneration and an improvement.
  • Full regeneration means that the performance is recovered to a value corresponding to the performance of the fuel cell before the previous drop in performance associated with the fuel cell being subjected to an electrical load and a sulfur-containing fuel or an anode feed gas compris ⁇ ing sulfur (e.g. sulfur containing species such as 3 ⁇ 4S, SO 2 , COS, and organic sulfur containing components) .
  • Fig.5 illustrates a full recovery.
  • the initial performance here shown as voltage e.g. average cell voltage, is the voltage obtained after the previous regeneration or the original performance.
  • voltage e.g. average cell voltage
  • the recovery can be un ⁇ derstood as having removed enough sulfur from the anode to restore the performance to the level obtained initially or just after the last regeneration.
  • Fig. 6 illustrates a full recovery with improvement.
  • the initial performance here shown as voltage, e.g. average cell voltage, is the voltage obtained after the previous regeneration or the original performance.
  • voltage e.g. average cell voltage
  • the performance degrades as il ⁇ lustrated by a drop in the voltage.
  • the voltage loss levels off to a relatively stable level.
  • the Fig. illustrates the application of the regeneration, and the performance obtained afterwards is initially at a level which is higher that the initial performance. This series of events can be repeated any number of times.
  • the recovery can be understood as having removed enough sulfur from the anode to restore the performance and to improve it to the level which is higher than obtained initially or just after the last regeneration.
  • Partial regeneration means that the performance of a fuel cell stack is increased by less than 100% of the loss in performance observed after the fuel cell stack is first used or less than 100% of the performance obtained after the previous regeneration.
  • Fig. 7 illustrates a partial re ⁇ covery.
  • the initial performance here shown as voltage, e.g. average cell voltage, is the voltage obtained after the previous regeneration or the original performance.
  • voltage e.g. average cell voltage
  • Fig. 8 illustrates a series of partial regenerations vs. initial performance.
  • a further embodiment of the invention is subjecting the fuel cell stack to a flow of gases during regeneration. Flowing a gas through the anode side will facilitate a purge of liberated sulfur species from the anode.
  • a suita ⁇ ble gas used as anode feed gas comprises one or more of the following gaseous components: Hydrogen, nitrogen, water (steam), oxygen, carbon monoxide and carbon dioxide.
  • the anode feed gas during regeneration may be: an inert gas, preferably nitrogen
  • the anode gas may also contain oxygen, either continuously or in pulses .
  • a further embodiment of the invention is that the anode feed gas flow is about 30 Nl/min/ (100 cm 2 anode area) or less.
  • Anode area means the geometric area of the anode, e.g. a 10 cm x 10 cm anode will have an anode area of 100 cm 2 .
  • the anode feed gas of N 2 is between about 0 and about 10 Nl/min/ (100 cm 2 anode area) . More preferably the anode feed gas of N 2 is about 5 Nl/min/ (100 cm 2 anode area) .
  • the an ⁇ ode feed gas of H 2 is between about 0 and about 2
  • the anode feed gas of H 2 is about 0.21 Nl/min/ (100 cm 2 anode area) .
  • the anode feed gas of H 2 0 is between about 0 and about 5 Nl/min/ (100 cm 2 anode area), even more prefera ⁇ bly the anode feed gas of H 2 is about 2 Nl/min/ (100 cm 2 an ⁇ ode area) .
  • the cathode may either have no flow during regeneration or have a flow of e.g. air.
  • the flow rate of air may be reduced as compared to what is used in normal SOFC oper ⁇ ation, e.g. in order to control the stack temperature.
  • the following parameters may be monitored during the use of the fuel cell stack, e.g. power generating mode of the fuel cell stack (s), or during stand-by mode:
  • Voltage loss Once a certain performance loss (depending on operating conditions such as cur- rent density, sulfur concentration, fuel utilizat ⁇ tion etc.) since the last regeneration (or initial operation) has been realized, then a new regeneration cycle is initiated.
  • the voltage loss can be defined as a fraction of the full loss po- tential or the full potential at which point a steady state is reached.
  • Fig. 5 illustrates re ⁇ generation after reaching close to steady state
  • Fig. 9 illustrates regeneration after reaching some performance loss, which is less than the expected steady state performance loss.
  • Rate of voltage change Once the rate of change in voltage has dropped below a certain lower limit, then a new regeneration cycle is initiated. The rate of change is measured over a period of time long enough to establish a stable value, the trend of which can be monitored.
  • - Regeneration is initiated after a certain amount of time has passed since the last regeneration.
  • This can be absolute time, time at a certain tern- perature, time operating in fuel cell mode, time weighted by the amount of fuel flow passing the anode (a representation of the amount of sulfur entering the anode) or a suitable combination of these methods.
  • the above parameters may be used individually or together to indicate a suitable period for regeneration of the fuel cell and a suitable duration and suitable conditions for the regeneration or regeneration sequence.
  • the regeneration of the fuel cell may occur at any point in time. If the fuel cell stack system is used intermittently (e.g. a truck APU system), then the regeneration could con- veniently take place: during start-up of the fuel cell stack system, during stand-by of the fuel cell stack system, where the system is kept warm,
  • the stack when operating load can be supplied by another source, e.g. a battery, and the stack can be re- generated.
  • another source e.g. a battery
  • the anode regeneration gas can be supplied to the anode and a suitable gas (e.g. air) can be supplied to the cathode, and the regeneration can be initiated.
  • a suitable gas e.g. air
  • Figs. 10 and 11 show data obtained with a Ni/YSZ anode.
  • concentration of 3 ⁇ 4S in the gas phase increases as the water content increases.
  • 3 ⁇ 4S concentration declines again at higher water concentrations.
  • Fig. 12 shows results obtained with a modified Ni/YSZ an ⁇ ode.
  • concentration of 3 ⁇ 4S in the gas phase increases as the water content increases. It declines again at higher water concentrations with 20 % water, but then it increases sharply at higher water concentrations, i.e. 40 and 60 %. This suggests an optimal water content in the range of about 5-80 %, especially 10-60 %. With a preferred high hy ⁇ drogen concentration of 40-100 %, the optimum water content is about 30-60 %.
  • the optimum gas composition is one wherein the hydrogen concentration is above 20 %, preferably above 40 % and most preferred above 60 %, and wherein the water content is more than 1 % of the total gas composition and preferably more than 10 % of the total gas composition.
  • the water content should constitute more than 50 % of the non-hydrogen gas content, preferably more than 80 % of the non-hydrogen gas content.
  • This example is based on keeping a fixed flow rate to the stack and aiming at obtaining a fixed conversion of 85 % of the steam entering the stack.
  • the example clearly shows the advantage of increasing the recycle.
  • the feed material con ⁇ sumption and the power consumption for electrolysis both drop essentially linearly towards zero as the recycle split increases towards 100 %.
  • SR is the split to recycle (%)
  • Rff is the relative feed flow (%)
  • RP is the relative power (%) .
  • Example 2 is shown graphically in Fig. 13.
  • Example 3 is shown graphically in Fig. 13.
  • This example shows the effect of increasing the conversion of the feed stream at a constant recycle split of 95 % us ⁇ ing AdBlue as the feed material.
  • the conversion is shown as two values :
  • Example 3 is illustrated graphically in Fig. 14, which shows the mole fraction in the exit gas (in percent) as a function of the 3 ⁇ 40 conversion by electrolysis vs feed.
  • a similar relationship can be determined for any given feed (AdBlue, water, mixtures etc.) to determine which operating condition will minimize the power consumption while obtain- ing gas compositions which will facilitate regeneration.
  • Fig. 15 shows results obtained by operating a stack on a simulated feed resembling a diesel CPO (catalytical partial oxidation) based system with anode recycle.
  • the stack was operated on the simulated feed gas including 0.7 ppm (vol) of 3 ⁇ 4S, and at different intervals a regeneration cycle was simulated by passing (once through) a gas comprising 80 % 3 ⁇ 4 and 20 % 3 ⁇ 40 over the stack for about 3-4 hours.
  • Fig. 15 indicates, the successive regenerations result in an improved performance.

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

Abstract

La présente invention concerne un procédé de régénération d'un empilement de pile à combustible empoisonnée au souffre, particulièrement un empilement de pile à combustible à oxyde solide (SOFC), consistant à amener un gaz approprié vers l'anode en la présence d'eau dans une atmosphère de réduction. Le gaz amené peut, par exemple, être de l'hydrogène ou un gaz contenant de l'AdBlue, et le procédé peut être conduit dans un système à une seule traversée ou un système basé sur un recyclage pour maintenir une vitesse de régénération élevée, comprenant éventuellement un ou plusieurs lits d'adsorption servant à éliminer le sulfure du gaz recyclé.
PCT/EP2013/069497 2013-08-01 2013-09-19 Procédé et système de régénération d'empilements de pile à combustible empoisonnée au souffre WO2015014415A1 (fr)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016087131A1 (fr) * 2014-12-02 2016-06-09 Thyssenkrupp Ag Régénération de cellules électrochimiques à oxyde solide
WO2022123015A1 (fr) * 2020-12-11 2022-06-16 Commissariat A L'energie Atomique Et Aux Energies Alternatives Procede de fonctionnement en mode stand-by chaud d'une pile a combustible sofc ou d'un reacteur soec

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EP1236495A1 (fr) * 2001-03-02 2002-09-04 Engelhard Corporation Procédé et dispositif pour pour éliminer des composés sulfurés d'un courant d'hydrocarbures
US20020192136A1 (en) * 2001-06-15 2002-12-19 Omg Ag & Co. Kg Process for preparing a low-sulfur reformate gas for use in a fuel cell system
JP2005353348A (ja) * 2004-06-09 2005-12-22 Aisin Seiki Co Ltd 燃料電池システム
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EP1977823A1 (fr) * 2007-03-30 2008-10-08 Kabushiki Kaisha Toyota Chuo Kenkyusho Support de catalyseur de reformage et son procédé de fabrication
DE102010034271A1 (de) * 2010-08-13 2012-02-16 Forschungszentrum Jülich GmbH Festoxid-Brennstoffzelle (Solid Oxide Fuel Cell, SOFC) sowie Verfahren zum Betreiben derselben

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EP1236495A1 (fr) * 2001-03-02 2002-09-04 Engelhard Corporation Procédé et dispositif pour pour éliminer des composés sulfurés d'un courant d'hydrocarbures
US20020192136A1 (en) * 2001-06-15 2002-12-19 Omg Ag & Co. Kg Process for preparing a low-sulfur reformate gas for use in a fuel cell system
JP2005353348A (ja) * 2004-06-09 2005-12-22 Aisin Seiki Co Ltd 燃料電池システム
JP2007220553A (ja) * 2006-02-17 2007-08-30 Toyota Central Res & Dev Lab Inc 燃料電池システム
EP1977823A1 (fr) * 2007-03-30 2008-10-08 Kabushiki Kaisha Toyota Chuo Kenkyusho Support de catalyseur de reformage et son procédé de fabrication
DE102010034271A1 (de) * 2010-08-13 2012-02-16 Forschungszentrum Jülich GmbH Festoxid-Brennstoffzelle (Solid Oxide Fuel Cell, SOFC) sowie Verfahren zum Betreiben derselben

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Title
JENS R. ROSTRUP-NIELSEN: "Catalytic Steam Reforming", 1984, SPRING- ER-VERLAG, pages: 96 - 97
SETHURAMAN V A ET AL: "Analysis of sulfur poisoning on a PEM fuel cell electrode", ELECTROCHIMICA ACTA, ELSEVIER SCIENCE PUBLISHERS, BARKING, GB, vol. 55, no. 20, 12 May 2010 (2010-05-12), pages 5683 - 5694, XP027114543, ISSN: 0013-4686, [retrieved on 20100512] *
WANG; LIU, JOURNAL OF POWER SOURCES, vol. 176, 2008, pages 23 - 30

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016087131A1 (fr) * 2014-12-02 2016-06-09 Thyssenkrupp Ag Régénération de cellules électrochimiques à oxyde solide
KR101808997B1 (ko) 2014-12-02 2017-12-13 티센크룹 악티엔게젤샤프트 고체 산화물 연료 전지들의 재생
WO2022123015A1 (fr) * 2020-12-11 2022-06-16 Commissariat A L'energie Atomique Et Aux Energies Alternatives Procede de fonctionnement en mode stand-by chaud d'une pile a combustible sofc ou d'un reacteur soec
FR3117684A1 (fr) * 2020-12-11 2022-06-17 Commissariat A L'energie Atomique Et Aux Energies Alternatives Procédé de fonctionnement en mode stand-by chaud d’une pile à combustible SOFC ou d’un réacteur SOEC.

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