WO2021234426A1 - 燃料電池システム及び燃料電池システムの制御方法 - Google Patents

燃料電池システム及び燃料電池システムの制御方法 Download PDF

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Publication number
WO2021234426A1
WO2021234426A1 PCT/IB2020/000505 IB2020000505W WO2021234426A1 WO 2021234426 A1 WO2021234426 A1 WO 2021234426A1 IB 2020000505 W IB2020000505 W IB 2020000505W WO 2021234426 A1 WO2021234426 A1 WO 2021234426A1
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WO
WIPO (PCT)
Prior art keywords
fuel cell
temperature
fuel
oxidant gas
cell system
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Legal status (The legal status 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 status listed.)
Ceased
Application number
PCT/IB2020/000505
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English (en)
French (fr)
Japanese (ja)
Inventor
小幡武昭
筑後隼人
島田一秀
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Renault SAS
Nissan Motor Co Ltd
Original Assignee
Renault SAS
Nissan Motor Co Ltd
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Filing date
Publication date
Application filed by Renault SAS, Nissan Motor Co Ltd filed Critical Renault SAS
Priority to JP2022523735A priority Critical patent/JP7323065B2/ja
Priority to PCT/IB2020/000505 priority patent/WO2021234426A1/ja
Priority to EP20936088.2A priority patent/EP4156350B1/en
Priority to US17/925,422 priority patent/US12388096B2/en
Priority to CN202080101228.3A priority patent/CN115702516B/zh
Publication of WO2021234426A1 publication Critical patent/WO2021234426A1/ja
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
    • H01M8/04014—Heat exchange using gaseous fluids; Heat exchange by combustion of reactants
    • 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
    • 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
    • H01M8/0432—Temperature; Ambient temperature
    • H01M8/0435—Temperature; Ambient temperature of cathode exhausts
    • 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
    • H01M8/04694—Processes for controlling fuel cells or fuel cell systems characterised by variables to be controlled
    • H01M8/04746—Pressure; Flow
    • H01M8/04753—Pressure; Flow of fuel cell reactants
    • 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
    • H01M8/0618—Reforming processes, e.g. autothermal, partial oxidation or steam reforming
    • 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 having a fuel cell and a control method for the fuel cell system.
  • JP2017-117550A discloses a method of detecting the temperature of the central portion of the cell stack, which has the highest temperature, and controlling the temperature distribution of the entire fuel cell to be uniform.
  • This fuel cell system aims to make the temperature distribution of the entire fuel cell uniform by supplying an inert gas to the central portion of the cell stack, which has the highest temperature, and lowering the temperature of the central portion of the cell stack. ..
  • JP2017-117550A assumes that the central part of the cell stack has the highest temperature, but depending on the fuel cell configuration and / or the driving scene, the central part of the cell stack is compared with other parts. Is not always the highest temperature.
  • a reforming catalyst configured to reform fuel
  • the anode when performing partial oxidation reforming, the anode is more than the central portion of the cell stack.
  • the end on the inlet side is relatively hottest. Therefore, in this internally modified fuel cell, if the temperature is controlled based on the temperature of the central portion of the cell stack, the heat resistance upper limit temperature may be exceeded in a part of the cell stack.
  • An object of the present invention is to provide a fuel cell system capable of controlling the temperature within a range not exceeding the heat resistance upper limit temperature of the fuel cell and a control method thereof when the cell stack having a reforming catalyst is provided.
  • the control method of the fuel cell system is a cell stack having a reforming catalyst that produces hydrogen from hydrocarbons, a first flow path for supplying fuel containing hydrocarbons to the cell stack, and facing the fuel.
  • it is a control method of a fuel cell system including a fuel cell having a second flow path for supplying an oxidant gas to the cell stack so as to flow orthogonally, and is an oxidant gas discharged from the second flow path. The temperature of a certain exhaust oxidant gas is detected, and the temperature of the fuel cell is controlled based on the temperature of the exhaust oxidant gas.
  • FIG. 1 is a block diagram showing a configuration of the fuel cell system of the first embodiment.
  • FIG. 2 is an explanatory diagram showing a fuel flow path and an oxidant gas flow path in the cell stack.
  • FIG. 3 is a schematic graph showing the temperature distribution in the fuel cell in the case of performing partial oxidation reforming.
  • FIG. 4 is a flowchart relating to temperature control of the fuel cell.
  • FIG. 5 is a graph schematically showing temperature control in warm-up operation.
  • FIG. 6 is a graph schematically showing temperature control in steady operation.
  • FIG. 7 is a block diagram showing the configuration of the fuel cell system of the second embodiment.
  • FIG. 8 is an explanatory diagram of a modified example in which the mounting position of the temperature sensor is changed.
  • FIG. 9 is an explanatory diagram of a modified example in which the configurations of the flow paths of the fuel and the oxidant gas are changed.
  • FIG. 10 is an explanatory diagram of a modified example in which the configuration of the flow path of the fuel and the oxidant gas and the mounting position of the temperature sensor are changed.
  • FIG. 1 is a block diagram showing a configuration of the fuel cell system 10 of the first embodiment.
  • the fuel cell system 10 includes a power generation device 11 and a controller 12.
  • the power generation device 11 is a device that generates electricity using the fuel cell 20, and in addition to the fuel cell 20, the fuel flow rate adjusting device 31, the air flow rate adjusting device 33, the oxidant gas supply device 41, the heat exchanger 43, and the combustor 51. , And a temperature sensor 60 and the like.
  • the controller 12 is a control device that comprehensively controls the power generation device 11 and each unit constituting the power generation device 11.
  • the fuel cell 20 includes a fuel cell (hereinafter, simply referred to as a cell) configured to generate electricity by an electrochemical reaction using fuel and an oxidant gas.
  • the fuel cell 20 includes a cell stack 21 composed of a single cell or a stack of a plurality of cells so as to generate the required electric power as a whole.
  • the cell stack 21 has a reforming catalyst (hereinafter referred to as an internal reforming catalyst) inside.
  • the internal reforming catalyst 22 reforms the fuel supplied to the fuel cell 20 (hereinafter referred to as raw fuel) by generating or promoting a specific chemical reaction, and the raw fuel directly to the power generation. Produces usable fuel (hereinafter referred to as reformed fuel (anodic gas)).
  • the raw material fuel is, for example, a fuel containing a raw material containing a hydrocarbon group such as an alkyl group as a main component, and specifically, a hydrocarbon such as methane or an alcohol such as methanol.
  • the internal reforming catalyst 22 produces a reforming fuel containing hydrogen used for power generation from a raw fuel containing hydrocarbons. Therefore, the fuel cell 20 is a so-called direct internal reforming type, and in principle, a separate reformer is not required, and the fuel cell 20 itself supplies unreformed raw fuel or incompletely reformed raw fuel. It can receive and generate electricity.
  • Fuel reforming that can be performed by the cell stack 21 includes, for example, partial oxidation reforming (POX), steam reforming (SR), carbon dioxide reforming, and the like.
  • POX partial oxidation reforming
  • SR steam reforming
  • carbon dioxide reforming and the like.
  • the internal reforming catalyst 22 contributes to some or all of these reforming reactions.
  • Partial oxidation reforming is a reforming reaction in which oxygen (O 2 ) is mixed with a raw material to partially oxidize the raw material to obtain a reformed fuel.
  • oxygen O 2
  • the partial oxidation reforming proceeds mainly by the partial oxidation reaction shown in (1) below.
  • complete combustion (complete oxidation) shown in the following (2) is generated and progresses. Therefore, in the partial oxidation reforming, not only hydrogen (H 2 ) but also water (H 2 O) is generated. Both the partial oxidation reaction of (1) and the complete combustion of (2) are exothermic reactions.
  • partial oxidation modification is an exothermic reaction.
  • the partial oxidation modification is a reaction that consumes oxygen. Therefore, the partial oxidation reforming does not occur uniformly in the entire cell stack 21, but the amount of oxygen generated is relatively large in the upstream portion of the fuel flow path (first flow path 23 described later), and oxygen is generated. The amount generated is relatively small in the downstream part of the flow path of the consumed fuel. This is because oxygen is abundant in the upstream portion, but in the downstream portion, oxygen is sequentially consumed as the partial oxidation reform progresses, and the amount of oxygen contained is relatively small.
  • Steam reforming is a reforming reaction in which a raw fuel or a reformed fuel is partially oxidized to obtain a reformed fuel by the reaction between the raw fuel and water (steam).
  • steam reforming proceeds mainly by the oxidation reaction shown in (3) or (4) below.
  • Steam reforming can be carried out using newly supplied water or water generated by partial oxidation reforming (particularly complete combustion).
  • the cell stack 21 performs steam reforming using water generated by partial oxidation reforming.
  • Steam reforming is an endothermic reaction.
  • Carbon dioxide reforming is a partial reaction of raw fuel or reformed fuel reformed by partial oxidation reforming or steam reforming with carbon dioxide (CO 2). It is a reforming reaction that oxidizes to obtain reformed fuel.
  • carbon dioxide reforming proceeds mainly by the partial oxidation reaction shown in (5) below.
  • Carbon dioxide reforming can proceed by utilizing newly supplied carbon dioxide or carbon dioxide generated by partial oxidation reforming (particularly complete combustion) or steam reforming.
  • the cell stack 21 performs carbon dioxide reforming by utilizing carbon dioxide generated by partial oxidation reforming and / or steam reforming.
  • Carbon dioxide modification is an endothermic reaction. CH 4 + CO 2 ⁇ 2CO + 2H 2 ... (5)
  • the fuel cell 20 is, for example, a solid oxide fuel cell (SOFC).
  • SOFC solid oxide fuel cell
  • the cell stack 21 is oxidized with the first flow path 23, which is a flow path of the raw fuel and / or the reformed fuel (hereinafter, simply referred to as fuel unless a distinction is necessary). It has a second flow path 24, which is a flow path for the agent gas, and an electrolyte (not shown) made of a solid oxide.
  • the cell stack 21 has a structure in which the first flow path 23 and the second flow path 24 are adjacent to each other via an electrolyte. Therefore, the internal reforming catalyst 22 is provided in the first flow path 23, which is the flow path of the fuel.
  • an electrode (hereinafter referred to as an anode) configured to function as a negative electrode is provided on the surface of the electrolyte in the first flow path 23, and the surface of the electrolyte in the second flow path 24 functions as a positive electrode.
  • a configured electrode (hereinafter referred to as a cathode) is provided.
  • the internal reforming catalyst 22 is separate from the anode, but a part or all of the anode may function as the internal reforming catalyst 22. Further, the internal reforming catalyst 22 is provided substantially uniformly throughout the cell stack 21. That is, the internal reforming catalyst 22 is not provided only in a specific part of the first flow path 23, and the raw material fuel is substantially any part of the first flow path 23 in the cell stack 21. Can be reformed.
  • the fuel cell 20 has an anode inlet A1, an anode outlet A2, a cathode inlet C3, and a cathode outlet C4.
  • the anode inlet A1 is an upstream end of the first flow path 23, and is an inlet for raw fuel to the fuel cell 20. Therefore, the anode inlet A1 is connected to the fuel flow rate adjusting device 31 via the fuel supply path 32.
  • the anode outlet A2 is an end portion on the downstream side of the first flow path 23, and used fuel and gas generated by power generation (hereinafter referred to as exhaust fuel (anode off gas)) are sent to the outside of the fuel cell 20. Discharge.
  • the anode outlet A2 is connected to the combustor 51 via the fuel discharge path 34.
  • the cathode inlet C3 is the upstream end of the second flow path 24, and is the inlet of the oxidant gas to the fuel cell 20.
  • the cathode inlet C3 is connected to the oxidant gas supply device 41 via the oxidant gas supply path 42.
  • the cathode outlet C4 is an end portion on the downstream side of the second flow path 24, and oxidant gas used for power generation, gas generated by power generation, and the like (hereinafter referred to as exhaust oxidant gas (cathode off gas)). It is discharged to the outside of the fuel cell 20.
  • the cathode outlet C4 is connected to the combustor 51 via the oxidant gas discharge path 44.
  • the fuel cell 20 supplies electric power to a device or device connected to the fuel cell 20.
  • the device or device connected to the fuel cell 20 is, for example, a storage battery, a motor used as a drive source for an electric vehicle, or the like.
  • the fuel cell 20 is connected to a storage battery connected to a motor for driving an electric vehicle. Therefore, the fuel cell 20 indirectly functions as an energy source for driving the electric vehicle.
  • the fuel flow rate adjusting device 31 is a device (fuel supply device) that supplies raw fuel to the fuel cell 20, and is a device that adjusts the flow rate of the raw material and fuel supplied to the fuel cell 20.
  • the fuel flow rate adjusting device 31 is connected to the anode inlet A1 via the fuel supply path 32.
  • the fuel flow rate adjusting device 31 includes a fuel tank and an injector.
  • the fuel tank stores raw fuel, for example, in a liquid state.
  • the injector ejects raw fuel from the fuel tank to the fuel supply path 32.
  • the fuel flow rate adjusting device 31 supplies the raw fuel to the fuel cell 20.
  • the controller 12 controls the timing at which the fuel flow rate adjusting device 31 supplies the raw fuel to the fuel cell 20, the amount of the raw fuel supplied, and the like.
  • the fuel flow rate adjusting device 31 may include a heat exchanger or the like, if necessary. In this case, the fuel flow rate adjusting device 31 can adjust the temperature, phase, pressure, etc. of the raw material and fuel by heating, heat exchange, or the like. In the present embodiment, the fuel flow rate adjusting device 31 vaporizes the raw fuel and supplies it to the fuel cell 20.
  • the air flow rate adjusting device 33 is connected to the fuel supply path 32, and is a device (air supply device) that mixes air with the raw fuel supplied to the fuel cell 20 by the fuel flow rate adjusting device 31 as needed. Moreover, it is a device that adjusts the flow rate of air mixed with raw materials and fuel.
  • the air flow rate adjusting device 33 is, for example, an air blower.
  • the purpose of mixing air with the raw material by the air flow rate adjusting device 33 is to generate partial oxidation reforming in the cell stack 21 by adding oxygen to the raw material, or it is generated in the cell stack 21. It is to promote partial oxidative reforming. Therefore, the air flow rate adjusting device 33 only needs to be able to mix oxygen with the raw material and fuel as needed.
  • the air flow rate adjusting device 33 may be configured to mix oxygen only, a gas other than oxygen-containing air, air whose constituent components, temperature, etc. are adjusted, and the like, instead of natural air, with the raw material and fuel.
  • the controller 12 controls the timing at which the air flow rate adjusting device 33 mixes air with the raw material, the amount of air mixed with the raw material, and the like.
  • the oxidant gas supply device 41 is a device that supplies the oxidant gas to the fuel cell 20, and is connected to the cathode inlet C3 via the oxidant gas supply path 42.
  • the oxidant gas is air containing oxygen used by the fuel cell 20 for power generation. That is, in the present embodiment, the oxidant gas supply device 41 is an air blower.
  • the heat exchanger 43 is provided in the oxidant gas supply path 42, and heats the oxidant gas by heat exchange. Therefore, the heat exchanger 43 supplies the heated oxidant gas to the fuel cell 20.
  • the heat exchange for heating the oxidant gas is performed with the gas discharged by the combustor 51 (hereinafter referred to as exhaust gas).
  • the combustor 51 is supplied with the discharged fuel from the fuel cell 20 via the fuel discharge path 34. Further, the exhaust oxidant gas is supplied from the fuel cell 20 to the combustor 51 via the oxidant gas discharge passage 44. Then, the combustor 51 burns the discharged fuel and the discharged oxidant gas by, for example, catalytic combustion. The exhaust gas generated as a result of this combustion is discharged from the exhaust passage 52 to the outside of the fuel cell system 10 via the heat exchanger 43. Therefore, the heat generated by the electrochemical reaction in the fuel cell 20 and the generation of exhaust gas is used for heating the oxidant gas in the oxidant gas supply path 42 by heat exchange in the heat exchanger 43.
  • the temperature sensor 60 is provided in the oxidant gas discharge path 44.
  • the temperature sensor 60 detects the temperature of the oxidant gas discharged from the fuel cell 20, more specifically, the oxidant gas discharged from the second flow path 24.
  • the temperature sensor 60 inputs the detected temperature of the discharged oxidant gas to the controller 12.
  • the controller 12 controls the temperature of the fuel cell 20 based on the temperature of the exhaust oxidant gas detected by the temperature sensor 60.
  • the controller 12 controls the temperature of the fuel cell 20 by the heat generated by the partial oxidation reforming in the cell stack 21.
  • the specific method in which the controller 12 controls the temperature of the fuel cell 20 will be described in detail later.
  • the controller 12 is a computer or a microcomputer configured by using a processor such as a CPU or a GPU, a memory, or the like.
  • the controller 12 can be configured as a dedicated computer for controlling the fuel cell system 10, or can be configured as a part of a computer for controlling other devices or systems.
  • the vehicle controller that controls the driving of the electric vehicle can be made to function as the controller 12 of the fuel cell system 10.
  • the controller 12 can be configured as a server-type computer that controls the controller 12 by communicating with the power generation device 11.
  • FIG. 2 is an explanatory diagram showing a fuel flow path and an oxidant gas flow path in the cell stack 21 of the present embodiment.
  • the first flow path 23 is a flow path for supplying fuel to the cell stack 21.
  • the second flow path 24 is a flow path for supplying the oxidant gas to the cell stack 21 so that the oxidant gas flows toward the fuel.
  • the first flow path 23 and the second flow path 24 are parallel in shape as a flow path, but the direction in which fuel flows through the first flow path 23 and the direction in which the oxidant gas flows through the second flow path 24 are opposite. be.
  • the first flow path 23 and the second flow path 24 are antiparallel or antiparallel, and the fuel and the oxidant gas have a so-called counterflow.
  • the second flow path 24 can be a flow path for supplying the oxidant gas to the cell stack 21 so that the oxidant gas flows orthogonally to the fuel.
  • FIG. 3 is a schematic graph showing the temperature distribution in the fuel cell 20 in the case of performing partial oxidation reforming.
  • the fuel cell 20 is formed when the cell stack 21 has reached a temperature above a level at which partial oxidative reforming can occur as a whole, and the cell stack 21 is subjected to partial oxidative reforming.
  • the temperature at which partial oxidative modification can occur is, for example, about 300 degrees or higher.
  • the horizontal axis represents the position along the first flow path 23 and the second flow path 24. Each cell constituting the cell stack 21 is stacked in the direction of the vertical axis.
  • the graph 101 shown by the solid line represents the temperature of the fuel in the fuel cell 20
  • the graph 102 shown by the broken line represents the temperature of the oxidant gas.
  • the temperatures of the fuel and the oxidant gas in the cell stack 21 can be regarded as substantially the same as the temperature of the fuel cell 20.
  • the fuel cell 20 has the highest temperature Tp at a predetermined position (a position near the anode inlet A1 or the anode inlet A1) biased toward the anode inlet A1 rather than the position of the central portion of the fuel cell 20. Become.
  • the temperature distribution of the oxidant gas follows the temperature distribution formed by the partial oxidative reforming as described above, and has almost the same temperature distribution at least in the cell stack 21. This is because the fuel and the oxidant gas flow in the cell stack 21 integrally on the front and back via the electrolyte, which is a thin film, and thus reach substantially the same temperature due to mutual heat exchange. Therefore, the exhaust oxidant gas discharged from the cathode outlet C4 correlates with a temperature substantially equal to the maximum temperature of the temperature distribution formed by the partial oxidative reforming or the maximum temperature in the temperature distribution formed by the partial oxidative reforming. It is discharged at a certain temperature.
  • the temperature having a correlation with the maximum temperature means a temperature at which the maximum temperature in the fuel cell 20 can be calculated or estimated based on the temperature having a certain relationship with the maximum temperature in the fuel cell 20.
  • the temperature sensor 60 detects the temperature of the discharged oxidant gas. As a result, the temperature sensor 60 detects the maximum temperature in the fuel cell 20 or the temperature that correlates with the maximum temperature in the fuel cell 20.
  • the controller 12 controls the temperature of the fuel cell 20 based on the temperature of the exhaust oxidant gas detected by the temperature sensor 60, thereby controlling the temperature of the fuel cell 20 based on the maximum temperature in the fuel cell 20.
  • the temperature of the discharged oxidant gas is almost equal to the maximum temperature of the temperature distribution formed by the partial oxidative reforming. Therefore, the temperature sensor 60 substantially detects the maximum temperature in the fuel cell 20 by detecting the temperature of the discharged oxidant gas. Then, the controller 12 directly controls the temperature of the fuel cell 20 based on the maximum temperature in the fuel cell 20 by using the temperature of the exhaust oxidant gas detected by the temperature sensor 60.
  • the temperature of the fuel cell 20 drops in the central portion of the cell stack 21 because steam reforming and / or carbon dioxide reforming, which are endothermic reactions, proceed. Further, the temperature of the fuel cell 20 rises from the central portion of the cell stack 21 to the anode outlet A2 and the cathode inlet C3 because the heated oxidant gas is supplied from the cathode inlet C3.
  • FIG. 4 is a flowchart relating to temperature control of the fuel cell 20. That is, when the temperature of the fuel cell 20 is controlled by the heat generated by the partial oxidation reforming in the cell stack 21, the controller 12 has the exhaust oxidant gas temperature acquisition step S101, the determination step S102, the temperature rise limit calculation step S103, and the target calorific value.
  • the temperature of the fuel cell 20 is controlled by repeatedly executing the calculation step S104, the fuel flow rate calculation step S105, the mixed air flow rate calculation step S106, and the control execution step S107 at predetermined time intervals in this order.
  • the "temperature control of the fuel cell 20" is particularly performed in the temperature rise limit calculation step S103, the target calorific value calculation step S104, the fuel flow rate calculation step S105, the mixed air flow rate calculation step S106, and the control execution step S107. Refers to control.
  • the controller 12 acquires the temperature of the exhaust oxidant gas detected by the temperature sensor 60. That is, the controller 12 is configured to function as an exhaust oxidant gas temperature acquisition unit.
  • the controller 12 changes the temperature inside the fuel cell 20 to a temperature at which partial oxidation reform is possible, depending on the temperature of the exhaust oxidant gas detected by the temperature sensor 60 reflecting this temperature. It can be determined whether or not the temperature has been reached.
  • the controller 12 regards the temperature of the exhaust oxidant gas acquired from the temperature sensor 60 as the maximum temperature in the fuel cell 20 and controls the temperature of the fuel cell 20. Perform the steps that follow. If there is a possibility that the temperature of the exhausted oxidizer gas deviates from the maximum temperature in the fuel cell 20 to the extent that a control error is caused due to the operating state of the fuel cell 20, it is detected as necessary. The temperature of the exhaust oxidant gas may be corrected.
  • the controller 12 performs the following steps in consideration of the correlation between the temperature of the discharged oxidant gas and the maximum temperature in the fuel cell 20. Further, when estimating the maximum temperature in the fuel cell 20 using the temperature of the exhaust oxidant gas, for example, it is possible to use a map in which the temperature of the exhaust oxidant gas and the maximum temperature in the fuel cell 20 are associated with each other. can.
  • the controller 12 determines whether or not the temperature of the discharged oxidant gas is equal to or higher than the temperature at which partial oxidation reform is possible. That is, the controller 12 is configured to function as a determination unit. When the temperature of the discharged oxidant gas is lower than the temperature at which partial oxidative reforming is possible, the controller 12 does not execute the step following the determination step S102 and continues to acquire the temperature of the discharged oxidant gas at a predetermined cycle. .. If the temperature of the exhaust oxidant gas, that is, even the maximum temperature of the fuel cell 20 has not reached a temperature at which partial oxidative reforming can be performed, partial oxidative reforming does not occur, and the heat is used for temperature control of the fuel cell 20. Because it cannot be done. When the temperature of the discharged oxidant gas is equal to or higher than the temperature at which partial oxidation reform is possible, the controller 12 executes the temperature rise limit calculation step S103.
  • the controller 12 calculates the temperature rise limit ⁇ Tm using the detected temperature Tq of the discharged oxidant gas. That is, the controller 12 is configured to function as a temperature rise limit calculation unit.
  • the temperature rise limit ⁇ Tm is the exhaust oxidant gas detected from the heat resistance upper limit temperature (hereinafter, simply referred to as the heat resistance upper limit temperature) of the part having the lowest heat resistance temperature among the parts constituting the cell stack 21 and other fuel cells 20. It is a temperature obtained by subtracting the temperature Tq of.
  • the controller 12 calculates a predetermined target calorific value Qt based on the temperature Tq of the discharged oxidant gas. As a result, the controller 12 sets the target calorific value Qt so that the temperature Tq of the discharged oxidant gas does not exceed the heat resistance upper limit temperature Tk of the internal reforming catalyst 22 in the temperature control of the fuel cell 20. That is, the controller 12 is configured to function as a target calorific value calculation unit and / or a target calorific value setting unit.
  • the target calorific value Qt is a target value of the calorific value due to partial oxidation reforming.
  • the target calorific value Qt is a target value of the calorific value per predetermined time (for example, the detection cycle of the temperature Tq of the discharged oxidant gas).
  • the target calorific value Qt can be obtained.
  • the controller 12 calculates the flow rate of the fuel (oxygen) for achieving the target calorific value Qt based on the calorific value obtained from the reaction formula of the partial oxidation reforming.
  • the controller 12 calculates the fuel flow rate Ff, which is the flow rate of the raw fuel, based on the target calorific value Qt. That is, the controller 12 is configured to function as a fuel flow rate calculation unit.
  • the fuel flow rate Ff is the flow rate of the raw fuel required to reach the target calorific value Qt by partial oxidation reforming.
  • the fuel flow rate Ff calculated in the fuel flow rate calculation step S105 is the flow rate of raw fuel for maintaining power generation while achieving the target calorific value Qt.
  • the controller 12 calculates the mixed air flow rate Fa, which is the amount of air to be mixed with the raw fuel, based on the target calorific value Qt. That is, the controller 12 is configured to function as a mixed air flow rate calculation unit.
  • the mixed air flow rate Fa is the flow rate of air that needs to be mixed with the raw fuel in order to reach the target calorific value Qt by partial oxidation reforming.
  • the mixed air flow rate Fa is the flow rate of oxygen-containing air corresponding to the amount of partial oxidation reform to be generated.
  • the controller 12 controls the fuel flow rate adjusting device 31 and the air flow rate adjusting device 33, respectively, so as to realize the calculated fuel flow rate Ff and the mixed air flow rate Fa. That is, the controller 12 operates the fuel flow rate Ff and the mixed air flow rate Fa so that the calorific value of the partial oxidation reforming in the cell stack 21 becomes the target calorific value Qt. Therefore, the controller 12 is configured to function as a fuel flow rate control unit that controls the flow rate of the raw fuel supplied to the fuel cell 20 by the fuel flow rate adjusting device 31. Further, the controller 12 is configured to function as a mixed air flow rate control unit that controls the flow rate of the air mixed with the raw material and fuel by the air flow rate adjusting device 33.
  • the fuel cell 20 By controlling the fuel flow rate Ff and the mixed air flow rate Fa in this way, even when a temperature distribution that decreases from the anode inlet A1 to the anode outlet A2 is generated inside the fuel cell 20 due to partial oxidation reforming, the fuel cell 20
  • the temperature of the internal reforming catalyst 22 is controlled within a range not exceeding the heat resistance upper limit temperature Tk. Therefore, the fuel cell system 10 operates continuously and efficiently without damaging the internal reforming catalyst 22 even if the fuel is reformed by partial oxidative reforming inside the cell stack 21. be able to.
  • the temperature control of the fuel cell 20 performed by the heat generation of the partial oxidation reforming in the cell stack 21 is performed by the operation scene in which the fuel cell system 10 is warmed up at the start of the fuel cell system 10 and the cell stack 21 by steam reforming or the like. It is particularly useful in an operation scene in which the temperature of the cell stack 21 is restored when the temperature drops.
  • these driving scenes will be described in detail.
  • FIG. 5 is a graph schematically showing temperature control in warm-up operation.
  • the temperature Ta is a temperature at which partial oxidation reform is possible, and is, for example, about 300 degrees.
  • the temperature Tb is a temperature at which power generation is possible when the fuel cell 20 is a solid oxide fuel cell, and is, for example, about 500 degrees.
  • the temperature Tc is a temperature maintained during steady operation in consideration of power generation efficiency when the fuel cell 20 is a solid oxide fuel cell, and is, for example, about 800 degrees to about 1000 degrees.
  • each graph G1 to G6 in FIG. 5 shows the temperature of the oxidant gas when measured at predetermined time intervals and the like.
  • the controller 12 warms up the fuel cell 20 by flowing the oxidant gas obtained by heating the oxidant gas to the fuel cell 20 while supplying the oxidant gas and the raw fuel to the combustor 51.
  • the fuel cell 20 gradually warms up and approaches a temperature at which power can be generated.
  • the temperature Td1 is the temperature Tq of the discharged oxidant gas at the time point of the graph G1.
  • the temperature Td2 is the temperature Tq of the discharged oxidant gas at the time point of the graph G2.
  • the fuel cell 20 warms up slowly and reaches a temperature at which the fuel cell 20 can generate electricity, as shown by the intervals between the graphs G1 and G3. It takes a long time to reach it. Therefore, as shown in the graph G3, when the temperature Tq of the discharged oxidant gas reaches the temperature Td3 and becomes a temperature equal to or higher than the temperature Ta at which partial oxidation reform is possible, the controller 12 starts from the heat resistance upper limit temperature Tk. By subtracting the detected temperature Td3 of the discharged oxidizer, the temperature rise limit ⁇ 3, which is the temperature rise limit ⁇ Tm at the time of the graph G3, is calculated.
  • the controller 12 calculates the target calorific value Qt based on the temperature rise limit ⁇ 3, and further calculates the fuel flow rate Ff and the mixed air flow rate Fa based on the calculated target calorific value Qt. After that, when the controller 12 controls the fuel flow rate adjusting device 31 and the air flow rate adjusting device 33 according to the calculated fuel flow rate Ff and the mixed air flow rate Fa, respectively, as shown in the graph G3 *, in the predetermined range Rpox of the cell stack 21. Partial oxidation reform progresses. As a result, the temperature of this predetermined range Rpox rises due to the heat generation of the partial oxidation reforming. However, even in the predetermined range Rpox, the maximum temperature of the fuel cell 20 is equal to or less than the heat resistant upper limit temperature Tk.
  • the heat generated by the partial oxidation modification of the graph G3 * propagates through the cell stack 21. Therefore, as shown in the graph G4, at the timing of detecting the temperature Tq of the discharged oxidant gas next, the interval between the graphs G3 and the graph G4 is larger than the interval between the graphs G1 and the graph G3. Become. That is, in the operation scene of warm-up operation, the warm-up of the fuel cell 20 is promoted by generating the partial oxidation reforming.
  • the temperature Tq of the discharged oxidant gas is the temperature Td4, which is lower than the temperature Tb at which power generation is possible, but higher than the temperature Ta at which partial oxidation reform is possible. Therefore, the controller 12 performs partial oxidation reforming again in the cell stack 21 in the same manner as described above, and promotes warming up of the fuel cell 20 by the heat thereof. That is, the controller 12 calculates the temperature rise limit ⁇ 4 at the time of the graph G4. Then, the controller 12 calculates the target calorific value Qt based on the temperature rise limit ⁇ 4, and further calculates and controls the fuel flow rate Ff and the mixed air flow rate Fa based on the calculated target calorific value Qt. As a result, as shown in the graph G4 *, partial oxidative reforming occurs in the predetermined range Rpox of the cell stack 21, and the heat propagates to accelerate the warm-up of the fuel cell 20 again.
  • the target calorific value Qt at the time of graph G4 is smaller than the target calorific value Qt at the time of graph G3.
  • the fuel flow rate Ff and the mixed air flow rate Fa at the time of the graph G4 are also smaller than the fuel flow rate Ff and the mixed air flow rate Fa at the time of the graph G3.
  • the calorific value of the partial oxidation modification generated in the predetermined range Rpox of the cell stack 21 is suppressed at the time point of graph G4 than at the time point of graph G3.
  • the maximum temperature of the fuel cell 20 is maintained at the heat resistance upper limit temperature Tk or less even if the partial oxidation reform is additionally performed at the time of graph G4.
  • the cell stack 21 After that, as shown in the graph G5, when the temperature Tq of the discharged oxidant gas becomes the temperature Td5 and exceeds the temperature Tb that can generate power, the cell stack 21 generates power by supplying the fuel and the oxidant gas. Begins. Generally, the higher the temperature of the fuel cell 20, the higher the power generation efficiency. Therefore, the fuel cell 20 is operated at a high temperature as much as possible within the range of the heat resistance upper limit temperature Tk or less. Therefore, even after the start of power generation, as shown in the graph G5, when the temperature Tc, which is the target of steady operation, is not reached, the controller 12 warms the fuel cell 20 in the same manner as described above. Continue the opportunity. That is, the controller 12 calculates the temperature rise limit ⁇ 5 at the time of graph G5.
  • the controller 12 calculates the target calorific value Qt based on the temperature rise limit ⁇ 5, and further calculates and controls the fuel flow rate Ff and the mixed air flow rate Fa based on the calculated target calorific value Qt.
  • the controller 12 calculates the target calorific value Qt based on the temperature rise limit ⁇ 5, and further calculates and controls the fuel flow rate Ff and the mixed air flow rate Fa based on the calculated target calorific value Qt.
  • the warm-up operation is completed in a short time as compared with the case where the warm-up operation is performed by flowing the oxidant gas heated only by the heater or the combustor 51 as in the conventional case, and the fuel cell system 10 is equipped with the fuel cell system 10. It is possible to shift to a steady operation in which power is generated in the cell stack 21.
  • FIG. 6 is a graph schematically showing temperature control in steady operation. Even if the temperature of the fuel cell 20 exceeds the temperature Tc maintained during steady operation and the steady operation is continued, the fuel cell may be affected by the amount of heat absorbed by steam reforming or the load on the fuel cell 20. The temperature of 20 may drop. For example, when the output power required for the fuel cell 20 is medium or low and the load on the fuel cell 20 is low or medium for steady operation, the temperature distribution in the fuel cell 20 is generally cathode. The temperature distribution is such that the temperature rises from the inlet C3 to the cathode outlet C4.
  • the temperature distribution in the fuel cell 20 is the temperature distribution in the fuel cell 20 from the cathode inlet C3 to the cathode outlet C4. May be a temperature distribution that decreases.
  • the amount of heat generated by power generation is large, but the amount of heat absorbed by steam reforming or the like is even larger, so that the amount of heat generated by power generation is lower than the amount of heat absorbed by steam reforming or the like.
  • the temperature of the fuel cell 20 changes during the steady operation even after the start of the steady operation. It may be below the temperature Tc to be maintained. If the steady operation is simply continued in such a state, the temperature may fall below the temperature Tb at which power generation is possible, and power generation may not be continued.
  • the controller 12 continues to detect the temperature Tq of the discharged oxidant gas even after shifting to the steady operation. Then, when the temperature of the discharged oxidant gas becomes Tq or less, which should be maintained during steady operation, the controller 12 heats the fuel cell 20 by the heat generated by the partial oxidation reforming. For example, as shown in the graph G7, when the temperature Tq of the discharged oxidant gas becomes the temperature Td7 and falls below the temperature Tc to be maintained during steady operation, the controller 12 calculates the temperature rise limit ⁇ 7.
  • the controller 12 calculates the target calorific value Qt based on the temperature rise limit ⁇ 7, and further calculates and controls the fuel flow rate Ff and the mixed air flow rate Fa based on the calculated target calorific value Qt.
  • the controller 12 calculates the target calorific value Qt based on the temperature rise limit ⁇ 7, and further calculates and controls the fuel flow rate Ff and the mixed air flow rate Fa based on the calculated target calorific value Qt.
  • partial oxidation modification occurs in the predetermined range Rpox of the cell stack 21.
  • the temperature of the fuel cell 20 becomes a temperature equal to or higher than the temperature Tc that should be maintained during steady operation, as shown in Graph G8.
  • the fuel cell 20 can continue power generation while satisfying the required output power even if the high load state continues.
  • the controller 12 controls the temperature based on the temperature Tq of the exhaust oxidant gas. Therefore, the temperature of the fuel cell 20 does not exceed the heat resistance upper limit temperature Tk even when viewed locally. Therefore, the fuel cell system 10 can stably continue steady operation without damaging the fuel cell 20.
  • the control method of the fuel cell system 10 of one embodiment includes a cell stack 21 having an internal reforming catalyst 22 which is a reforming catalyst for generating hydrogen from hydrocarbons, and the cell stack 21 containing hydrocarbons.
  • a fuel cell system 10 comprising a fuel cell 20 comprising a first flow path 23 for supplying fuel and a second flow path 24 for supplying an oxidant gas to the cell stack 21 so as to flow opposite or orthogonal to the fuel.
  • the temperature Tq of the exhausted oxidant gas which is the oxidant gas discharged from the second flow path 24, is detected, and the temperature of the fuel cell 20 is controlled based on the temperature Tq of the discharged oxidant gas.
  • the temperature may be relatively high near the anode inlet A1 rather than the central portion of the cell stack 21.
  • the fuel cell 20 is a so-called counter flow or cross flow, and the temperature of the cathode outlet C4 can be regarded as the temperature of the anode inlet A1 which is a relatively high temperature portion.
  • the controller 12 of the fuel cell system 10 controls the temperature of the fuel cell 20 based on the temperature Tq of the exhaust oxidant gas detected at the cathode outlet C4 near the anode inlet A1.
  • the temperature is controlled based on the temperature of the relative high temperature portion in the fuel cell 20, so that the heat resistance upper limit temperature Tk, which is the heat resistance standard, can be more reliably determined. Stable control that complies with can be realized.
  • the control method of the fuel cell system 10 can operate the fuel cell 20 more reliably and stably without damaging the fuel cell 20 as compared with the control method of the conventional fuel cell system.
  • the above control method of the fuel cell system 10 is particularly suitable when partial oxidation reform occurs in the cell stack 21.
  • the anode inlet A1 side is the fuel cell 20 due to the heat generated by the partial oxidation reforming. It becomes the highest temperature in the temperature distribution inside. Therefore, even when partial oxidative reforming is performed to warm up the fuel cell 20, the temperature Tq of the exhaust oxidant gas is detected by the temperature sensor 60 provided at the cathode outlet C4 as described above, and the detected emission is performed.
  • the temperature of the fuel cell 20 By controlling the temperature of the fuel cell 20 based on the temperature Tq of the oxidant gas, it is possible to promote warming up of the fuel cell 20 within a range that does not exceed the heat resistance upper limit temperature Tk even when viewed locally.
  • the temperature Tq of the exhaust oxidant gas detected by the temperature sensor 60 is substantially equal to the maximum temperature of the fuel cell 20. Therefore, the above temperature control can be performed particularly accurately.
  • the temperature control of the fuel cell 20 is controlled so that the temperature of the fuel cell 20 is equal to or less than the heat resistant upper limit temperature Tk, which is a predetermined temperature.
  • the heat resistance upper limit temperature Tk is arbitrary. Therefore, the control method of the fuel cell system 10 according to the above embodiment is particularly suitable when the temperature of the fuel cell 20 is controlled to be equal to or lower than a predetermined temperature, and the fuel cell 20 and the fuel cell system 10 are damaged or the like. It is possible to realize stable control with reduced fear.
  • the fuel flow rate adjusting device 31 for adjusting the flow rate of the fuel supplied to the fuel cell 20 and the air for adjusting the flow rate of the air to be mixed with the fuel are adjusted.
  • a flow rate adjusting device 33 is further provided.
  • the calorific value of the partial oxidation reforming in the cell stack 21 is a predetermined value based on the temperature Tq of the exhaust oxidant gas.
  • the fuel flow rate Ff which is the flow rate of the fuel
  • the mixed air flow rate Fa which is the flow rate of the air to be mixed with the fuel
  • the control method of the fuel cell system 10 of the above embodiment realizes the temperature control of the fuel cell 20 by utilizing the partial oxidation reforming that inevitably occurs due to the nature of the internal reforming catalyst 22. That is, in the control method of the fuel cell system 10 of the above embodiment, the temperature control of the fuel cell 20 without the preparation of a special heat source or cold heat source is realized.
  • partial oxidation reforming is positively generated by mixing air with the fuel by the air flow rate adjusting device 33. Then, in the fuel cell system 10, the target calorific value Qt is determined based on the temperature Tq of the exhausted oxidant gas, and the fuel flow rate Ff and the mixed air flow rate Fa are controlled. As a result, in the fuel cell system 10, the temperature of the fuel cell 20 is controlled by controlling the calorific value of the generated partial oxidation reforming. As described above, if the heat generation of the partial oxidation reforming is controlled based on the temperature Tq of the discharged oxidant gas, the temperature control of the fuel cell 20 can be suitably performed.
  • the fuel cell system 10 when warming up the fuel cell 20 and when trying to maintain the temperature of the fuel cell 20 in order to continue using the fuel cell 20 with a high load, the fuel cell system 10 can be viewed locally.
  • the temperature of the fuel cell 20 can be controlled particularly appropriately within a range not exceeding the heat resistance upper limit temperature Tk.
  • the warm-up can be promoted by the above-mentioned temperature control using the heat generated by the partial oxidation reforming.
  • the temperature Tc that should be maintained for steady operation can be maintained.
  • the target calorific value Qt is set so that the temperature Tq of the discharged oxidant gas does not exceed the heat resistance upper limit temperature Tk of the internal reforming catalyst 22 which is the reforming catalyst.
  • Tk the heat resistance upper limit temperature of the internal reforming catalyst 22 which is the reforming catalyst.
  • the fuel and the fuel are mixed.
  • the temperature of the fuel cell 20 is controlled by supplying air or the like.
  • the temperature of the fuel cell 20 can be controlled by appropriately supplying the fuel and air mixture only when the temperature range at which partial oxidation reform is possible is reached, and utilizing the heat generated by the partial oxidation reform. ..
  • waste of fuel can be eliminated and problems such as carbon precipitation can be prevented.
  • the fuel cell system 10 of the above embodiment has a cell stack 21 having an internal reforming catalyst 22 which is a reforming catalyst that generates hydrogen from hydrocarbons, and a first fuel cell system 21 that supplies fuel containing hydrocarbons to the cell stack 21.
  • a fuel cell 20 including a flow path 23 and a second flow path 24 that supplies an oxidant gas to the cell stack 21 so as to flow facing or orthogonal to the fuel, and oxidation discharged from the second flow path 24. It includes a temperature sensor 60 that detects the temperature Tq of the exhausted oxidant gas, which is an agent gas, and a controller 12 that controls the temperature of the fuel cell 20 based on the temperature Tq of the exhausted oxidant gas.
  • the configuration of the fuel cell system 10 can be changed within a range that does not deviate from the purpose of temperature control of the fuel cell 20 according to the above embodiment.
  • the temperature of the fuel cell 20 is controlled by utilizing the heat generated by the partial oxidation reforming has been described, but the temperature of the fuel cell 20 is controlled based on the temperature Tq of the exhaust oxidant gas. If this can be done, the temperature of the fuel cell 20 can be controlled by a method other than utilizing the heat generated by the partial oxidation reforming, such as heating with a heater.
  • the controller 12 uses an oxidant gas supply device so that the temperature Tq of the exhaust oxidant gas reaches a desired temperature (for example, to keep a predetermined upper limit temperature).
  • a desired temperature for example, to keep a predetermined upper limit temperature.
  • the amount of air supplied by 41 or the amount of fuel, exhaust gas, and / or new air supplied to the combustor 51 may be controlled.
  • the temperature control of the fuel cell 20 using the partial oxidation reforming is particularly preferable because a special configuration for controlling the temperature of the fuel cell 20 is not required.
  • the fuel cell system 10 of the first embodiment includes one internally reformed fuel cell 20 having a cell stack 21 having an internal reformed catalyst 22.
  • Such an internally modified fuel cell 20 is used by supplying raw fuel in an excessive amount in order to prevent carbon precipitation and the like. Therefore, the fuel utilization rate is low. Therefore, in the fuel cell system 10 of the first embodiment, the fuel utilization rate can be improved by using another fuel cell in combination as described below.
  • FIG. 7 is a block diagram showing the configuration of the fuel cell system 210 of the second embodiment.
  • the fuel cell 20 of the fuel cell system 10 of the first embodiment is used as the first fuel cell, and the second fuel cell 220 is added. Therefore, the configuration common to the fuel cell system 10 of the first embodiment is designated by the same reference numerals as those of the first embodiment, and the description thereof will be omitted.
  • the second fuel cell 220 is a fuel cell having a cell stack 221 having a smaller number of internal reforming catalysts 22 as compared with the fuel cell 20 which is the first fuel cell.
  • the cell stack 221 of the second fuel cell 220 is a solid oxide fuel cell having no internal reforming catalyst 22. That is, the second fuel cell 220 generates electricity by supplying the reformed fuel.
  • the anode inlet A3 of the second fuel cell 220 is connected to the anode outlet A2 of the fuel cell 20. Further, the anode outlet A4 of the second fuel cell 220 is connected to the combustor 51 via the fuel discharge path 34. That is, in the second fuel cell 220, the fuel discharged from the fuel cell 20 is supplied as fuel. Since the raw fuel is supplied in excess, the discharged fuel of the fuel cell 20 is not completely used as fuel, hydrogen remains, and it can still be used as fuel. On the other hand, almost all of the raw fuel of the exhaust fuel of the fuel cell 20 is reformed to hydrogen by the internal reforming of the fuel cell 20. Therefore, the discharged fuel of the fuel cell 20 is used as the reforming fuel in the second fuel cell 220.
  • the cathode inlet C1 of the second fuel cell 220 is connected to the oxidant gas supply device 41 via the oxidant gas discharge path 44. Further, the cathode outlet C2 of the second fuel cell 220 is connected to the cathode inlet C3 of the fuel cell 20. That is, the second fuel cell 220 uses the oxidant gas supplied from the oxidant gas supply device 41 for power generation. After that, the second fuel cell 220 supplies the oxidant gas (exhausted oxidant gas) discharged from the second fuel cell 220 to the fuel cell 20 as the oxidant gas.
  • the exhaust oxidant gas of the second fuel cell 220 contains oxygen, and can sufficiently function as the oxidant gas in the fuel cell 20 as well.
  • the fuel cell system 210 of the second embodiment includes a second fuel cell 220 in addition to the fuel cell 20 which is the first fuel cell. Then, the fuel discharged from the fuel cell 20 is supplied to the second fuel cell 220.
  • the fuel utilization rate is low because the internally reformed fuel cell 20 is used by supplying raw fuel in an excessive manner, but the discharged fuel of the fuel cell 20 is used for power generation in the second fuel cell 220. Will be reused. Therefore, the fuel cell system 210 can be used for power generation with almost no surplus raw fuel, and the fuel utilization rate can be improved as compared with the fuel cell system 10 of the first embodiment.
  • the fuel cell system 210 of the second embodiment supplies the exhausted oxidant gas, which is the oxidant gas discharged from the second fuel cell 220, to the fuel cell 20 as the oxidant gas.
  • the exhausted oxidant gas which is the oxidant gas discharged from the second fuel cell 220
  • the temperature of the fuel cell 20 drops, but as described above, the exhaust oxidant gas heated by the power generation in the second fuel cell 220 is the fuel cell 20.
  • the fuel cell system 210 as a whole can easily maintain the heat balance. Therefore, the controller 12 can easily maintain the internally modified fuel cell 20 in steady operation more stably and with high efficiency.
  • the second fuel cell 220 added by the fuel cell system 210 of the second embodiment adopts one having a smaller number of internal reforming catalysts 22 than the fuel cell 20. Therefore, in the second fuel cell 220, endothermic reactions such as steam reforming are less likely to occur. Therefore, by supplying the exhaust oxidant gas of the second fuel cell 220 to the fuel cell 20, the controller 12 is particularly easy to maintain the heat balance between the heat generated by the power generation in the fuel cell 20 and the heat absorption due to the fuel reforming. Moreover, it is easy to maintain the heat balance as a whole of the fuel cell system 210. When the second fuel cell 220 does not have the internal reforming catalyst 22 as in the second embodiment, it is most likely to maintain these heat balances.
  • the temperature sensor 60 is provided at the cathode outlet C4 in which the second flow paths 24 branching into a plurality of branches in the cell stack 21 are once again integrated into one.
  • the arrangement of the sensor 60 can be arbitrarily changed within a range in which the maximum temperature in the temperature distribution in the fuel cell 20 can be detected or estimated.
  • FIG. 8 is an explanatory diagram of a modified example in which the mounting position of the temperature sensor 60 is changed. As shown in FIG. 8, a part of the second flow path 24 branched in the cell stack 21 is pulled out, a flow path 301 that joins the cathode outlet C4 is provided, and a temperature sensor 60 can be provided in this flow path 301. ..
  • the fuel cell 20 has the first flow path 23 and the first flow path 23 due to the overall structural convenience of the fuel cell 20. Even when the temperature distribution is formed in the Y direction perpendicular to the two flow paths 24, the controller 12 can easily accurately detect or estimate the maximum temperature of the fuel cell 20 regardless of the temperature distribution in the Y direction.
  • the fuel and the oxidant gas of the fuel cell 20 have a counterflow, but the fuel and the oxidant gas of the fuel cell 20 can have a so-called cross flow.
  • FIG. 9 is an explanatory diagram of a modified example in which the configurations of the flow paths of the fuel and the oxidant gas are changed. That is, the fuel cell 20 replaces the counterflow cell stack 21 with a second flow path 24 that supplies the oxidant gas to the cell stack 21 so that the oxidant gas flows orthogonally to the fuel.
  • the cell stack 302 can be adopted.
  • the control methods of the first embodiment and the second embodiment can be executed and the effect can be obtained.
  • the temperature of the exhaust oxidant gas has a certain correlation with the maximum temperature in the temperature distribution in the fuel cell 20, so that the controller 12 can change the temperature of the exhaust oxidant gas into the fuel cell 20 from the temperature of the exhaust oxidant gas. This is because the maximum temperature of can be estimated.
  • a parallel flow cell stack in which the first flow path 23 and the second flow path 24 are parallel to each other and the fuel and the oxidant gas flow in parallel to these flow paths. Also in this case, the control methods of the first embodiment and the second embodiment can be executed and the effects thereof can be obtained.
  • a counterflow cell stack 21 or a crossflow cell stack 302 is adopted in order to make the temperature distribution in the fuel cell 20 evenly close and to improve the power generation efficiency. It is particularly preferable to adopt the counterflow cell stack 21.
  • FIG. 10 is an explanatory diagram of a modified example in which the configuration of the flow path of the fuel and the oxidant gas and the mounting position of the temperature sensor 60 are changed with respect to the first embodiment and the second embodiment.
  • a cross-flow cell stack 302 is adopted, and then a flow path 303 is provided which draws out a part of the second flow path 24 and joins the cathode outlet C4.
  • the temperature sensor 60 is provided in the flow path 303.
  • the cross-flow cell stack 302 is adopted, if the flow path 303 from which a part of the second flow path 24 is drawn out is provided and the temperature sensor 60 is provided here, the temperature distribution in the fuel cell 20 is set.
  • the correlation between the maximum temperature and the temperature Tq of the discharged oxidant gas to be detected becomes high. Therefore, when the controller 12 estimates the maximum temperature in the fuel cell 20, the accuracy is improved, and as a result, the accuracy of the temperature control of the fuel cell 20 is improved.
  • the controller 12 estimates the maximum temperature in the fuel cell 20
  • the accuracy is improved, and as a result, the accuracy of the temperature control of the fuel cell 20 is improved.
  • the heat generated by the partial oxidation reforming causes the maximum on the anode inlet A1 side in the fuel cell 20.
  • the temperature can be detected directly and accurately. Therefore, the temperature control of the fuel cell 20 by the controller 12 can be performed particularly accurately.

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