WO2012128369A1 - Système de pile à combustible - Google Patents

Système de pile à combustible Download PDF

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Publication number
WO2012128369A1
WO2012128369A1 PCT/JP2012/057628 JP2012057628W WO2012128369A1 WO 2012128369 A1 WO2012128369 A1 WO 2012128369A1 JP 2012057628 W JP2012057628 W JP 2012057628W WO 2012128369 A1 WO2012128369 A1 WO 2012128369A1
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WO
WIPO (PCT)
Prior art keywords
pressure
hydrogen
reformed gas
feed pump
reformer
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PCT/JP2012/057628
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English (en)
Japanese (ja)
Inventor
修平 咲間
俊幸 海野
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Ｊｘ日鉱日石エネルギー株式会社
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Priority to JP2013506045A priority Critical patent/JPWO2012128369A1/ja
Publication of WO2012128369A1 publication Critical patent/WO2012128369A1/fr

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    • 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
    • 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
    • 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 fuel cell system.
  • a reformer that generates reformed gas using a hydrogen-containing fuel, a cell stack that generates power using the reformed gas, and desulfurization of hydrogen-containing fuel supplied to the reformer
  • the thing which comprises the desulfurizer which performs this is known.
  • Such a fuel cell system includes, for example, a supply flow path for supplying a hydrogen-containing fuel to a desulfurizer, and a feed pump (raw fuel compressor) provided in the supply flow path, as described in Patent Document 1.
  • a circulation channel (recycling line) that circulates part of the reformed gas supplied from the reformer to the cell stack to the supply channel.
  • an object of the present invention is to provide a fuel cell system that can reliably circulate the reformed gas at a low cost.
  • a fuel cell system includes a reformer that generates a reformed gas using a hydrogen-containing fuel, a cell stack that generates power using the reformed gas, A desulfurizer that performs desulfurization of the hydrogen-containing fuel supplied to the catalyst, a hydrogen-containing fuel supply passage for supplying the hydrogen-containing fuel to the desulfurizer, and a hydrogen-containing fuel that is provided upstream or downstream of the desulfurizer.
  • the hydrogen-containing fuel supply flow path is provided upstream of the junction with the circulation flow path so that the suction pressure of the feed pump is lower than the pressure of the reformed gas supplied from the reformer to the cell stack. Supplied to the feed pump A first pressure drop section to reduce the pressure of that the hydrogen-containing fuel, and a.
  • the pressure of the hydrogen-containing fuel is reduced at the upstream side of the junction with the circulation passage in the supply passage by the first pressure reduction portion, and the suction pressure of the feed pump is changed from the reformer to the cell stack.
  • the pressure is lower than the pressure of the reformed gas supplied. Therefore, a pressure difference is generated between the pressure on the inlet side and the pressure on the outlet side in the circulation channel so that the reformed gas circulates, and the reformed gas is supplied to the supply channel without providing a feed pump or the like in the circulation channel.
  • it is reliably circulated to the upstream side of the feed pump by self-pressure. Therefore, the reformed gas can be reliably circulated at a low cost.
  • FIG. 1 is a schematic block diagram showing a fuel cell system according to a first embodiment. It is a schematic block diagram which shows the fuel cell system which concerns on 2nd Embodiment. It is a schematic block diagram which shows the fuel cell system which concerns on 3rd Embodiment. It is a schematic block diagram which shows the fuel cell system which concerns on 4th Embodiment.
  • FIG. 1 is a schematic block diagram showing a fuel cell system according to the first embodiment.
  • the fuel cell system 1 includes a desulfurizer 2, a reformer 3, and a cell stack 4.
  • the fuel cell system 1 generates power in the cell stack 4 using a hydrogen-containing fuel and an oxidant.
  • the type of the cell stack 4 in the fuel cell system 1 is not particularly limited, and examples thereof include a polymer electrolyte fuel cell (PEFC), a solid oxide fuel cell (SOFC), and phosphoric acid.
  • PEFC polymer electrolyte fuel cell
  • SOFC solid oxide fuel cell
  • phosphoric acid phosphoric acid
  • MCFC Molten Carbonate Fuel Cell
  • hydrocarbon fuel a compound containing carbon and hydrogen in the molecule (may contain other elements such as oxygen) or a mixture thereof is used.
  • hydrocarbon fuels include hydrocarbons, alcohols, ethers, and biofuels. These hydrocarbon fuels are derived from conventional fossil fuels such as petroleum and coal, and synthetic systems such as synthesis gas. Those derived from fuel and those derived from biomass can be used as appropriate. Specific examples of hydrocarbons include methane, ethane, propane, butane, natural gas, LPG (liquefied petroleum gas), city gas, town gas, gasoline, naphtha, kerosene, and light oil.
  • methanol and ethanol are mentioned as alcohols.
  • ethers include dimethyl ether.
  • biofuels include biogas, bioethanol, biodiesel, and biojet.
  • oxygen-enriched air is used as the oxidizing agent.
  • the desulfurizer 2 desulfurizes the hydrogen-containing fuel supplied to the reformer 3.
  • the desulfurizer 2 has a desulfurization catalyst for removing sulfur compounds contained in the hydrogen-containing fuel.
  • the desulfurizer 2 employs a hydrodesulfurization method in which a sulfur compound is removed by reacting with hydrogen.
  • an adsorptive desulfurization system that adsorbs and removes sulfur compounds may be used in combination.
  • the desulfurizer 2 supplies the desulfurized hydrogen-containing fuel to the reformer 3.
  • the reformer 3 generates a reformed gas as a hydrogen-rich gas (hydrogen-containing gas) from the supplied hydrogen-containing fuel.
  • the reformer 3 reforms the hydrogen-containing fuel and generates a reformed gas by a reforming reaction using a reforming catalyst.
  • the reforming method in the reformer 3 is not particularly limited, and for example, steam reforming, partial oxidation reforming, autothermal reforming, and other reforming methods can be employed.
  • the reformer 3 may have a configuration for adjusting the properties in addition to the reformer reformed by the reforming catalyst depending on the properties of the hydrogen-rich gas required for the cell stack 4.
  • the reformer 3 is configured to remove carbon monoxide in the hydrogen-rich gas. (For example, a shift reaction part and a selective oxidation reaction part). The reformer 3 supplies the reformed gas to the cell stack 4.
  • PEFC polymer electrolyte fuel cell
  • PAFC phosphoric acid fuel cell
  • the cell stack 4 generates power using the reformed gas and oxidant from the reformer 3.
  • the cell stack 4 supplies a reformed gas and an oxidant that have not been used for power generation as off-gas to a subsequent combustion section (not shown).
  • the fuel cell system 1 includes a hydrogen-containing fuel supply channel R1, a reformed gas supply channel R2, a reformed water supply channel R3, and a circulation channel R4.
  • the hydrogen-containing fuel supply flow path R ⁇ b> 1 is a hydrogen-containing fuel supply line for supplying at least a hydrogen-containing fuel to the desulfurizer 2, and is connected to the desulfurizer 2.
  • the hydrogen-containing fuel supply flow path R1 is provided with a feed pump P as pressure feeding means.
  • the feed pump P is provided upstream of a later-described branch portion G1, and adjusts the flow rate of fuel supplied to the cell stack 4.
  • the reformed gas supply flow path R2 is a reformed gas supply line for supplying reformed gas from the reformer 3 to the cell stack 4, and is connected to the reformer 3 and the cell stack 4.
  • the reforming water supply flow path R ⁇ b> 3 is a reforming water line for supplying the reforming water as steam to the reformer 3, and is connected to the reformer 3.
  • the circulation flow path R4 is a recycle line for circulating a part of the reformed gas supplied from the reformer 3 to the cell stack 4 to the upstream side of the feed pump P of the hydrogen-containing fuel supply flow path R1.
  • the circulation channel R4 is connected to the reformed gas supply channel R2 and the hydrogen-containing fuel supply channel R1 upstream of the feed pump P.
  • the circulation flow path R4 is branched from the middle of the reformed gas supply flow path R2 (hereinafter, the branched portion is referred to as a branch portion G1), and upstream of the feed pump P of the hydrogen-containing fuel supply flow path R1.
  • the joined part is referred to as a joining part G2).
  • the reformed gas circulated in the circulation flow path R4 is used, for example, for hydrodesulfurization or for catalyst regeneration of the desulfurizer 2.
  • the heat exchanger 6 for transferring heat from the reformed gas to the reformed water is provided in the reformed water supply channel R3 and the circulation channel R4. Thereby, the retained water of the reformed gas is utilized to heat the reformed water. Further, a drainage drain 7 for collecting and draining water (condensed water) generated from the reformed gas flowing through the circulation channel R4 is provided downstream of the heat exchanger 6 in the circulation channel R4. Thereby, it is possible to prevent the condensed water from flowing into the feed pump P together with the reformed gas flowing through the circulation flow path R4.
  • a first pressure reduction unit 8 such as a capillary that is a capillary for generating a differential pressure is provided on the upstream side of the merging portion G (merging portion G2) with the circulation channel R4 in the hydrogen-containing fuel supply channel R1. It has been.
  • the first pressure reduction unit 8 reduces the pressure of the hydrogen-containing fuel so that the suction pressure of the feed pump P is lower than the pressure of the reformed gas supplied from the reformer 3 to the cell stack 4.
  • the first pressure reduction unit 8 is not limited.
  • a first pressure reduction unit that reduces a predetermined amount of pressure from the inlet pressure of the first pressure reduction unit 8 itself.
  • the amount of pressure that can be reduced from the inlet pressure of the lowering portion 8 itself can be adjusted in multiple stages, and the outlet pressure of the lowering portion 8 can be adjusted in advance regardless of the inlet pressure of the first pressure lowering portion 8 itself.
  • What reduces to a certain fixed pressure value etc. can be selected suitably.
  • an orifice, a check valve, a proportional valve, a pressure reducing valve, a zero governor, or the like can be used.
  • a second pressure reduction unit 9 such as a capillary that is a capillary for generating a differential pressure is provided between the drainage recovery drain 7 and the junction G (junction G2).
  • the second pressure reduction unit 9 reduces the pressure of the reformed gas circulating to the hydrogen-containing fuel supply channel R1 so that the flow rate of the reformed gas becomes a predetermined flow rate. If the pressure drop amount in the circulation flow path R4 is sufficient, the second pressure drop unit 9 can be omitted. However, by providing the second pressure drop unit 9, for example, fluctuations in the power generation amount of the fuel cell system 1 can be achieved. Based on this, even if the discharge pressure of the feed pump P fluctuates, the reformed gas can be circulated more stably.
  • an orifice, a check valve, a proportional valve, a pressure reducing valve, a zero governor, and the like can be used in addition to the capillary.
  • the pressure of the hydrogen-containing fuel flowing at a pressure of 2.5 kPa is reduced by the first pressure reducing unit 8, 1
  • the outlet pressure of the pressure drop unit 8 is a negative pressure (for example, ⁇ 5 kPa).
  • the hydrogen-containing fuel is merged with the reformed gas from the circulation flow path R4 via the merging portion G (merging portion G2), and the hydrogen-containing fuel and the reformed gas are downstream at a discharge pressure of, for example, 5 kPa by the feed pump P. Pumped to the side. Thereafter, these hydrogen-containing fuel and reformed gas are supplied to the desulfurizer 2.
  • the numerical value of the pressure illustrated in the above is a gauge pressure (hereinafter the same).
  • the hydrogen-containing fuel is desulfurized by the desulfurizer 2
  • the hydrogen-containing fuel is reformed by the reformer 3 to generate a reformed gas.
  • the pressure of the reformed gas decreases (for example, 0.4 kPa) due to pressure loss in the desulfurizer 2 and the reformer 3.
  • the reformed gas having a pressure of 0.4 kPa for example, is supplied to the cell stack 4 in the reformed gas supply channel R2.
  • an off gas having a pressure of, for example, 0.1 kPa is generated from the cell stack 4.
  • the reformed gas supply flow path R2 a part of the reformed gas supplied from the reformer 3 to the cell stack 4 (here, the reformed gas supplied from the reformer 3 to the cell stack 4). About 5%) flows from the branch part G1 into the circulation channel R4.
  • the reformed gas heats the reformed water in the reformed water supply channel R3 via the heat exchanger 6, and then the water in the reformed gas is recovered by the drainage recovery drain 7.
  • the reformed gas is reduced in pressure by the second pressure reduction unit 9 so that the flow rate becomes a predetermined flow rate, and then, as described above, the hydrogen-containing fuel supply flow path R1 contains hydrogen through the junction G. Joined with fuel.
  • the pressure of the hydrogen-containing fuel supplied to the feed pump P in the hydrogen-containing fuel supply flow path R1 is reduced by the first pressure reduction unit 8, and the feed pump P
  • the suction pressure is set to a negative pressure ( ⁇ 5 kPa) lower than the pressure (0.4 kPa) of the reformed gas supplied from the reformer 3.
  • the suction pressure of the feed pump P is set to a value smaller than a value obtained by subtracting the pressure drop amount in the entire circulation flow path R4 from the pressure of the reformed gas supplied from the reformer 3 to the cell stack 4. .
  • the circulation flow path R4 a pressure difference is generated between the pressure on the inlet side and the pressure on the outlet side, and the reformed gas can be circulated at its own pressure so as to be sucked from the inlet side to the outlet side.
  • the reformed gas is reliably and stably circulated to the hydrogen-containing fuel supply flow path R1 without separately providing a pressure feeding means such as a feed pump in the circulation flow path R4.
  • the first pressure drop unit 8 is arranged in the suction line (upstream) of the feed pump P, and the reformed gas can be supplied to the cell stack 4 after the suction pressure of the feed pump P is set to a negative pressure.
  • the pressure difference between the pressure of the reformed gas from the reformer 3 and the suction pressure of the hydrogen-containing fuel and the reformed gas by the feed pump P is artificially generated by pumping the hydrogen-containing fuel at a feed pump discharge pressure. To produce.
  • the reformed gas can be circulated through the circulation flow path R4 at its own pressure. Therefore, according to the present embodiment, it is possible to reliably circulate the reformed gas at a low cost.
  • a control mode in which the amount of power generation is changed in accordance with a change in power demand.
  • the required hydrogen-containing fuel increases and decreases according to the increase and decrease of the power generation amount. That is, the fuel discharge amount per unit time of the feed pump P increases and decreases, and the reformed gas pressure supplied to the cell stack 4 also varies. In such a case, there may be a delay in response to control of the feed pump P or pressure change.
  • the second pressure drop unit in the circulation flow path R4 it is possible to reduce the transient pressure fluctuation and stably circulate the reformed gas flowing in the circulation flow path R4.
  • the pressure difference between the suction pressure of the feed pump P and the pressure of the reformed gas from the reformer 3 is smaller in the case of the SOFC cell stack 4 than in the case of the PEFC because the pressure loss of the cell stack 4 is small.
  • This embodiment is particularly effective in the case of the SOFC cell stack 4 because the reformed gas is not easily circulated by the self-pressure.
  • the heat exchanger 6 is provided in the reforming water supply channel R3 and the circulation channel R4, and heat is transferred from the reformed gas to the reforming water. This makes it possible to recover the retained heat of the reformed gas circulated in the circulation channel R4 with the reformed water.
  • FIG. 2 is a schematic block diagram showing a fuel cell system according to the second embodiment.
  • the fuel cell system 200 of the second embodiment is mainly different from the first embodiment (see FIG. 1) in that the feed pump P is provided on the downstream side of the desulfurizer 2.
  • the heat exchange unit 6 cools the reformed gas with a heat medium.
  • the heat exchanging unit 6 is provided in the circulation flow path R4, and water, air, oil, and the like are circulated as a heat medium.
  • the heat recovered by the heat medium is stored in, for example, a hot water tank and can be used as hot water.
  • the feed pump P is provided between the desulfurizer 2 and the reformer 3. However, if the feed pump P is provided downstream of the merging portion G2 and between the branch portions G1, the feed pump P is used to circulate the reformed gas. This is because a necessary pressure difference can be generated.
  • this embodiment can be suitably implemented in a fuel cell system in which the supply pressure to the cell stack 4 is relatively high. If the pressure of the branch part G1 is high, the reformed gas can be circulated without excessively reducing the pressure of the merge part G2, so that even if the feed pump P is provided downstream of the desulfurizer 2, good desulfurization conditions are maintained. Because it can.
  • FIG. 3 is a schematic block diagram showing a fuel cell system according to the third embodiment.
  • the fuel cell system 300 according to the third embodiment is provided between the second pressure drop portion 9 and the merging portion G2 of the circulation flow path R4 in addition to the first embodiment (see FIG. 1).
  • the condensate water removed by the drainage drain 7 is reused as reforming water.
  • the pressure of the hydrogen-containing fuel supplied to the feed pump P by the first pressure reduction unit 8 is set so that the pressure of the reformed gas supplied to the cell stack 4 becomes larger than the suction pressure of the feed pump P.
  • the pressure at the junction G2 changes to the pressure at the branch G1. May be more transiently high.
  • hydrogen-containing fuel that has not been subjected to fuel treatment such as desulfurization or reforming is supplied to the cell stack 4.
  • the circulation flow path R ⁇ b> 4 includes the backflow prevention unit 11, whereby supply of untreated hydrogen-containing fuel to the cell stack 4 can be suppressed.
  • the backflow prevention part 11 was arrange
  • the backflow prevention unit 11 is provided downstream of the drainage recovery drain 7. It is preferable. Thereby, it can suppress that the condensed water containing a sulfur compound touches an untreated hydrogen-containing fuel and mixes in reformed water, and that sulfur compound is supplied to the cell stack 4 via the reformer 3 by extension. It is possible to suppress a decrease in the life of the cell stack 4 due to the above.
  • the second pressure drop unit 9 can be omitted.
  • any pressure difference can be generated by adjusting the cracking pressure.
  • FIG. 4 is a schematic block diagram showing a fuel cell system according to the fourth embodiment.
  • the fuel cell system 400 of the fourth embodiment includes a pressure measurement unit 12 that measures the feed pump suction pressure, and a control unit 13 that operates the first pressure reduction unit. And a reforming water tank 14 for storing the reforming water.
  • a proportional valve 8a is used as the first pressure drop unit 8.
  • the control unit 13 measures the suction pressure of the feed pump P by the pressure measurement unit 12. The control unit 13 compares whether or not the measured suction pressure of the feed pump P is within a predetermined reference suction pressure range of the feed pump P. When the suction pressure is smaller than the suction reference pressure range, the control unit 13 controls the proportional valve 8a so as to increase the opening degree of the proportional valve 8a to reduce the pressure drop amount. On the other hand, when the suction pressure is larger than the suction reference pressure range, the control unit 13 controls the proportional valve 8a so as to increase the pressure drop amount by decreasing the opening degree of the proportional valve 8a.
  • the reforming tank 14 stores the introduced reforming water and the reforming water recovered by the drainage recovery drain 7 and supplies the reforming water to the heat exchanger 6.
  • the pressure decrease amount of the first pressure decrease unit 8 is increased or decreased according to the suction pressure of the feed pump P is shown, but the pressure decrease amount of the second pressure decrease unit 9 is changed. It may be increased or decreased.
  • the reformed gas can be circulated with a circulation amount suitable for regeneration.
  • the pressure of the hydrogen-containing fuel supplied to the feed pump P is reduced to the negative pressure by the first pressure reduction unit 8, but the reformer 3 does not have to be reduced to the negative pressure.
  • the suction pressure of the feed pump P may be lowered to be lower than the pressure of the reformed gas supplied to the cell stack 4.
  • the outlet pressure of the first pressure drop unit 8, the pressure of the junction G2 of the circulation flow path R4, and the suction pressure of the feed pump P are regarded as the same pressure for the sake of convenience.
  • the outlet pressure of the reformer 3, the supply pressure of the reformed gas supplied to the cell stack 4, and the pressure of the branching portion of the circulation flow path R4 are assumed to be pressures in another region. However, there may be a pressure gradient that can be implemented between them.
  • the value of the suction pressure of the feed pump P is the value of the outlet pressure of the first pressure drop unit 8 or the junction of the circulation flow path R4 from the viewpoint of convenience or practical (handling).
  • the pressure value of G2 can also be used.
  • the reformed gas can be reliably circulated at a low cost.

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Abstract

L'invention porte sur un module de pile à combustible, qui comporte : un reformeur, qui utilise un combustible contenant de l'hydrogène pour générer un gaz reformé ; un empilement de cellules qui utilise ledit gaz reformé pour générer de l'électricité ; un désulfurant qui désulfurise le combustible contenant de l'hydrogène fourni au reformeur ; un canal d'alimentation en combustible contenant de l'hydrogène pour fournir le combustible contenant de l'hydrogène au désulfurant ; une pompe d'alimentation, pour fournir le combustible contenant de l'hydrogène au désulfurant, laquelle est disposée en amont du désulfurant dans le canal d'alimentation en combustible contenant de l'hydrogène ; un canal de circulation pour renvoyer une partie du gaz reformé qui est fourni à l'empilement de cellules par le reformeur, vers l'amont de la pompe d'alimentation dans le canal d'alimentation en combustible contenant de l'hydrogène ; et une première partie de réduction de pression qui est disposée dans le canal d'alimentation en combustible contenant de l'hydrogène, en amont de la jonction entre ledit canal et le canal de circulation, et qui réduit la pression du gaz contenant de l'hydrogène fourni à la pompe d'alimentation, de telle sorte que la pression d'aspiration de la pompe d'alimentation est inférieure à la pression du gaz reformé fourni à l'empilement de cellules par le reformeur.
PCT/JP2012/057628 2011-03-24 2012-03-23 Système de pile à combustible WO2012128369A1 (fr)

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Cited By (6)

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JP2013225411A (ja) * 2012-04-20 2013-10-31 Toshiba Fuel Cell Power Systems Corp 燃料電池発電システム
WO2014083794A1 (fr) * 2012-11-29 2014-06-05 パナソニック株式会社 Système de pile à combustible
JP2016012487A (ja) * 2014-06-30 2016-01-21 アイシン精機株式会社 燃料電池システム
JP2016012486A (ja) * 2014-06-30 2016-01-21 アイシン精機株式会社 燃料電池システム
JP2016012485A (ja) * 2014-06-30 2016-01-21 アイシン精機株式会社 燃料電池システム
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JP2013225411A (ja) * 2012-04-20 2013-10-31 Toshiba Fuel Cell Power Systems Corp 燃料電池発電システム
WO2014083794A1 (fr) * 2012-11-29 2014-06-05 パナソニック株式会社 Système de pile à combustible
US9478817B2 (en) 2012-11-29 2016-10-25 Panasonic Intellectual Property Management Co., Ltd. Fuel cell system
JP2016012487A (ja) * 2014-06-30 2016-01-21 アイシン精機株式会社 燃料電池システム
JP2016012486A (ja) * 2014-06-30 2016-01-21 アイシン精機株式会社 燃料電池システム
JP2016012485A (ja) * 2014-06-30 2016-01-21 アイシン精機株式会社 燃料電池システム
JP2016207378A (ja) * 2015-04-20 2016-12-08 パナソニックＩｐマネジメント株式会社 固体酸化物形燃料電池システムの運転方法

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