WO2016157320A1 - 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 PDFInfo
- Publication number
- WO2016157320A1 WO2016157320A1 PCT/JP2015/059712 JP2015059712W WO2016157320A1 WO 2016157320 A1 WO2016157320 A1 WO 2016157320A1 JP 2015059712 W JP2015059712 W JP 2015059712W WO 2016157320 A1 WO2016157320 A1 WO 2016157320A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- fuel cell
- flow rate
- temperature
- fuel
- stack
- Prior art date
Links
- 239000000446 fuel Substances 0.000 title claims abstract description 430
- 238000000034 method Methods 0.000 title claims description 15
- 239000012528 membrane Substances 0.000 claims abstract description 180
- 239000003792 electrolyte Substances 0.000 claims abstract description 161
- 238000010248 power generation Methods 0.000 claims abstract description 81
- 230000007423 decrease Effects 0.000 claims abstract description 78
- 239000007800 oxidant agent Substances 0.000 claims abstract description 49
- 230000004044 response Effects 0.000 claims abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 217
- 238000004364 calculation method Methods 0.000 claims description 177
- 230000001590 oxidative effect Effects 0.000 claims description 44
- 238000001514 detection method Methods 0.000 claims description 41
- 238000001816 cooling Methods 0.000 claims description 27
- 230000003247 decreasing effect Effects 0.000 claims description 13
- 239000003507 refrigerant Substances 0.000 claims description 9
- 239000007789 gas Substances 0.000 description 581
- 239000000498 cooling water Substances 0.000 description 110
- 238000009736 wetting Methods 0.000 description 60
- 230000001105 regulatory effect Effects 0.000 description 25
- 238000010586 diagram Methods 0.000 description 22
- 230000001276 controlling effect Effects 0.000 description 16
- 230000009467 reduction Effects 0.000 description 12
- 230000008859 change Effects 0.000 description 11
- 239000002826 coolant Substances 0.000 description 10
- 238000005259 measurement Methods 0.000 description 9
- 238000009792 diffusion process Methods 0.000 description 8
- 238000011144 upstream manufacturing Methods 0.000 description 8
- 239000003054 catalyst Substances 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 6
- 230000002596 correlated effect Effects 0.000 description 6
- 238000002847 impedance measurement Methods 0.000 description 6
- 230000007704 transition Effects 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- 238000010926 purge Methods 0.000 description 5
- 229920006395 saturated elastomer Polymers 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 239000002737 fuel gas Substances 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 230000007812 deficiency Effects 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- 239000013585 weight reducing agent Substances 0.000 description 3
- 238000013459 approach Methods 0.000 description 2
- 230000000875 corresponding effect Effects 0.000 description 2
- 238000003411 electrode reaction Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000007562 laser obscuration time method Methods 0.000 description 2
- 239000012466 permeate Substances 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 230000001052 transient effect Effects 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 238000012935 Averaging Methods 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 1
- 230000002159 abnormal effect Effects 0.000 description 1
- 230000005856 abnormality Effects 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000006229 carbon black Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 230000006870 function Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000003014 ion exchange membrane Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 230000004580 weight loss Effects 0.000 description 1
Images
Classifications
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
- H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
- H01M8/04119—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
- H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
- H01M8/04119—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying
- H01M8/04156—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying with product water removal
- H01M8/04179—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying with product water removal by purging or increasing flow or pressure 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
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
-
- 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
- H01M8/04067—Heat exchange or temperature measuring elements, thermal insulation, e.g. heat pipes, heat pumps, fins
-
- 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
- H01M8/04492—Humidity; Ambient humidity; Water content
- H01M8/04529—Humidity; Ambient humidity; Water content of the electrolyte
-
- 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
- H01M8/04537—Electric variables
- H01M8/04604—Power, energy, capacity or load
-
- 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
- H01M8/04701—Temperature
- H01M8/04708—Temperature 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
- H01M8/04—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
- H01M8/04—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
- H01M8/04828—Humidity; Water content
- H01M8/0485—Humidity; Water content of the electrolyte
-
- 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
- H01M8/04858—Electric variables
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/10—Fuel cells with solid electrolytes
- H01M2008/1095—Fuel cells with polymeric electrolytes
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M2220/00—Batteries for particular applications
- H01M2220/20—Batteries in motive systems, e.g. vehicle, ship, plane
-
- 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
- Y02E60/10—Energy storage using batteries
-
- 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 for adjusting a flow rate of fuel supplied to a fuel cell and a temperature of the fuel cell, and a control method for the fuel cell system.
- Japanese Patent No. 5104950 discloses a fuel cell that maintains the wet state of the electrolyte membrane by increasing or decreasing the flow rate of the fuel supplied to the electrolyte membrane when the dry operation for reducing the wetness (water content) of the electrolyte membrane is completed. A system is disclosed.
- the oxidant gas supplied to the fuel cell is humidified by water vapor accompanying power generation, the water vapor is discharged from the fuel cell together with the unused oxidant gas. For this reason, when the dry operation is performed, the temperature of the fuel cell is raised in order to increase the amount of water vapor that can be held in the oxidant gas.
- the present invention has been made paying attention to such problems, and an object of the present invention is to provide a fuel cell system and a fuel cell system control method for efficiently controlling the wet state of the fuel cell.
- a fuel cell system includes a fuel supply unit that supplies fuel to an electrolyte membrane of a fuel cell, an oxidant supply unit that supplies an oxidant to the electrolyte membrane, and the oxidant supply unit.
- Power generation control means for controlling power generation of the fuel cell by controlling supply of an oxidant and fuel supply by the fuel supply means.
- the fuel cell system includes: a wet state detection unit that detects a wet state of the electrolyte membrane; a flow rate adjustment unit that adjusts a flow rate of fuel supplied to the fuel cell by the fuel supply unit; and the oxidant supply unit.
- Temperature adjusting means for adjusting the temperature of the oxidant supplied to the fuel cell.
- the power generation control means reduces the flow rate of the fuel when the moisture content of the electrolyte membrane is reduced by a signal output from the wetness state detection means, compared to when the moisture content of the electrolyte membrane is increased, and the wet status.
- the temperature of the oxidizing agent is raised in accordance with a signal from the detecting means.
- FIG. 1 is a perspective view showing a configuration of a fuel cell in an embodiment of the present invention.
- 2 is a cross-sectional view of the fuel cell shown in FIG. 1 taken along the line II-II.
- FIG. 3 is a diagram showing the configuration of the fuel cell system in the present embodiment.
- FIG. 4 is a block diagram illustrating an example of a functional configuration of a controller that controls the fuel cell system.
- FIG. 5 is a diagram showing an example of a functional configuration for detecting the wet state of the electrolyte membrane in the fuel cell.
- FIG. 6 is a diagram showing an example of the relationship between the magnitude of the load connected to the fuel cell and the minimum temperature of the fuel cell.
- FIG. 7 is a diagram showing the relationship between the magnitude of the load connected to the fuel cell and the target wet state of the electrolyte membrane.
- FIG. 8 is a diagram illustrating an example of a functional configuration for calculating the target flow rate of the anode gas supplied to the fuel cell.
- FIG. 9 is a diagram showing the relationship between the flow rate ratio of the anode gas and the cathode gas supplied to the fuel cell and the relative humidity of the cathode gas.
- FIG. 10 is a diagram illustrating an example of a functional configuration for calculating the target temperature of the cooling water supplied to the fuel cell stack.
- FIG. 11 is a flowchart illustrating an example of a control method for controlling the fuel cell system according to the first embodiment.
- FIG. 12 is a time chart showing changes in the state of the fuel cell system when a dry operation for reducing the water content of the electrolyte membrane is executed.
- FIG. 13 is a time chart showing changes in the state of the fuel cell system when the temperature of the fuel cell is used instead of the minimum temperature of the fuel cell in the dry operation.
- FIG. 14 is a diagram illustrating an example of a functional configuration for controlling power generation of the fuel cell according to the second embodiment of the present invention.
- FIG. 15 is a diagram showing the relationship between the operation of the anode circulation pump and the anode gas flow rate.
- FIG. 16 is a flowchart showing an example of a control method of the fuel cell system in the second embodiment.
- FIG. 17 is a time chart showing changes in the state of the fuel cell system when the dry operation is executed.
- FIG. 18 is a time chart showing an example of a state change of the fuel cell system in a dry operation in which the wetness is lowered during a transition.
- FIG. 19 is a time chart showing an example of a change in the state of the fuel cell system when the amount of decrease during transition is increased.
- FIG. 20 is a diagram illustrating an example of the configuration of the impedance measuring apparatus.
- the fuel cell includes an anode electrode as a fuel electrode, a cathode electrode as an oxidant electrode, and an electrolyte membrane disposed so as to be sandwiched between these electrodes.
- An anode gas containing hydrogen is supplied as fuel to the anode electrode of the fuel cell.
- a cathode gas containing oxygen as an oxidant is supplied to the cathode electrode of the fuel cell.
- the fuel cell generates power using an anode gas containing hydrogen and a cathode gas containing oxygen.
- the electrode reaction that proceeds in both the anode electrode and the cathode electrode is as follows.
- Anode electrode 2H 2 ⁇ 4H + + 4e ⁇ (1)
- Cathode electrode 4H + + 4e ⁇ + O 2 ⁇ 2H 2 O (2) Due to the electrode reactions (1) and (2), the fuel cell generates an electromotive force of about 1 V (volt).
- FIG. 1 and 2 are views for explaining the configuration of a fuel cell 10 according to an embodiment of the present invention.
- FIG. 1 is a perspective view of the fuel cell 10
- FIG. 2 is a cross-sectional view of the fuel cell 10 shown in FIG.
- the fuel cell 10 includes a membrane electrode assembly (MEA) 11, and an anode separator 12 and a cathode separator 13 disposed so as to sandwich the MEA 11.
- MEA membrane electrode assembly
- the MEA 11 includes an electrolyte membrane 111, an anode electrode 112, and a cathode electrode 113.
- the MEA 11 has an anode electrode 112 on one surface side of the electrolyte membrane 111 and a cathode electrode 113 on the other surface side.
- the electrolyte membrane 111 is a proton conductive ion exchange membrane formed of a fluorine-based resin.
- the electrolyte membrane 111 exhibits good electrical conductivity with an appropriate degree of wetness.
- the wetness of the electrolyte membrane 111 corresponds to the amount of water (water content) contained in the electrolyte membrane 111. It means that the moisture content of the electrolyte membrane 111 increases as the wetness level increases, and the moisture content of the electrolyte membrane 111 decreases as the wetness level decreases.
- the anode electrode 112 includes a catalyst layer 112A and a gas diffusion layer 112B.
- the catalyst layer 112 ⁇ / b> A is a member formed of platinum or carbon black particles carrying platinum or the like, and is provided in contact with the electrolyte membrane 111.
- the gas diffusion layer 112B is disposed outside the catalyst layer 112A.
- the gas diffusion layer 112B is a member formed of carbon cloth having gas diffusibility and conductivity, and is provided in contact with the catalyst layer 112A and the anode separator 12.
- the cathode electrode 113 includes a catalyst layer 113A and a gas diffusion layer 113B.
- the catalyst layer 113A is disposed between the electrolyte membrane 111 and the gas diffusion layer 113B, and the gas diffusion layer 113B is disposed between the catalyst layer 113A and the cathode separator 13.
- the anode separator 12 is disposed outside the gas diffusion layer 112B.
- the anode separator 12 includes a plurality of anode gas passages 121 for supplying anode gas to the anode electrode 112.
- the anode gas flow path 121 is formed as a groove-shaped passage. That is, the anode gas channel 121 constitutes a fuel channel through which fuel passes through the other surface of the electrolyte membrane 111.
- the cathode separator 13 is disposed outside the gas diffusion layer 113B.
- the cathode separator 13 includes a plurality of cathode gas passages 131 for supplying cathode gas to the cathode electrode 113.
- the cathode gas channel 131 is formed as a groove-shaped passage. That is, the cathode gas channel 131 constitutes an oxidant channel through which the oxidant passes with respect to one surface of the electrolyte membrane 111.
- the cathode separator 13 includes a plurality of cooling water passages 141 for supplying cooling water for cooling the fuel cell 10.
- the cooling water channel 141 is formed as a groove-shaped passage. That is, the cooling water channel 141 constitutes a refrigerant channel through which a refrigerant for cooling the fuel cell 10 passes.
- the cathode separator 13 is configured such that the flow direction of the cooling water flowing through the cooling water flow channel 141 and the flow direction of the cathode gas flowing through the cathode gas flow channel 131 are the same. Note that these flow directions may be opposite to each other. Moreover, you may comprise so that these flow directions may have a predetermined angle.
- the anode separator 12 and the cathode separator 13 are configured such that the flow direction of the anode gas flowing through the anode gas flow path 121 and the flow direction of the cathode gas flowing through the cathode gas flow path 131 are opposite to each other. Moreover, you may comprise so that these flow directions may have a predetermined angle.
- FIG. 3 is a configuration diagram showing an example of the fuel cell system 100 according to the first embodiment of the present invention.
- the fuel cell system 100 constitutes a power supply system that supplies an anode gas and a cathode gas necessary for power generation from the outside to the fuel cell, and generates the fuel cell according to an electric load.
- the fuel cell system 100 includes a fuel cell stack 1, a cathode gas supply / discharge device 2, an anode gas supply / discharge device 3, a stack cooling device 4, a load device 5, an impedance measurement device 6, and a controller 200. .
- the fuel cell stack 1 is a stacked battery in which a plurality of fuel cells 10 are stacked as described above.
- the fuel cell stack 1 is connected to the load device 5 and supplies power to the load device 5.
- the fuel cell stack 1 generates a DC voltage of, for example, several hundred V (volts).
- the cathode gas supply / discharge device 2 is a device that supplies cathode gas to the fuel cell stack 1 and discharges cathode off-gas discharged from the fuel cell stack 1 to the atmosphere. That is, the cathode gas supply / discharge device 2 constitutes an oxidant supply means for supplying an oxidant to the electrolyte membrane 111 of the fuel cell 10.
- the cathode gas supply / discharge device 2 includes a cathode gas supply passage 21, a compressor 22, a flow rate sensor 23, a pressure sensor 24, a cathode gas discharge passage 25, and a cathode pressure regulating valve 26.
- the cathode gas supply passage 21 is a passage for supplying cathode gas to the fuel cell stack 1. One end of the cathode gas supply passage 21 is open, and the other end is connected to the cathode gas inlet hole of the fuel cell stack 1.
- the compressor 22 is provided in the cathode gas supply passage 21.
- the compressor 22 takes in oxygen-containing air from the open end of the cathode gas supply passage 21 and supplies the air to the fuel cell stack 1 as cathode gas.
- the rotation speed of the compressor 22 is controlled by the controller 200.
- the flow sensor 23 is provided in the cathode gas supply passage 21 between the compressor 22 and the fuel cell stack 1.
- the flow sensor 23 detects the flow rate of the cathode gas supplied to the fuel cell stack 1.
- the flow rate of the cathode gas supplied to the fuel cell stack 1 is simply referred to as “cathode gas flow rate”.
- the flow sensor 23 outputs a signal that detects the cathode gas flow rate to the controller 200.
- the pressure sensor 24 is provided in the cathode gas supply passage 21 between the compressor 22 and the fuel cell stack 1.
- the pressure sensor 24 detects the pressure of the cathode gas supplied to the fuel cell stack 1.
- the pressure of the cathode gas supplied to the fuel cell stack 1 is simply referred to as “cathode gas pressure”.
- the pressure sensor 24 outputs a signal that detects the cathode gas pressure to the controller 200.
- the cathode gas discharge passage 25 is a passage for discharging the cathode off gas from the fuel cell stack 1.
- One end of the cathode gas discharge passage 25 is connected to the cathode gas outlet hole of the fuel cell stack 1, and the other end is opened.
- the cathode pressure regulating valve 26 is provided in the cathode gas discharge passage 25.
- the cathode pressure regulating valve 26 is controlled to open and close by the controller 200.
- the cathode gas pressure is adjusted to a desired pressure by this open / close control.
- the cathode pressure regulating valve 26 opens as the opening degree of the cathode pressure regulating valve 26 increases, and the cathode pressure regulating valve 26 closes as the opening degree of the cathode pressure regulating valve 26 increases.
- the anode gas supply / discharge device 3 is a device for supplying anode gas to the fuel cell stack 1 and circulating the anode off-gas discharged from the fuel cell stack 1 to the fuel cell stack 1. That is, the anode gas supply / discharge device 3 constitutes a fuel supply means for supplying fuel to the electrolyte membrane 111 of the fuel cell 10.
- the anode gas supply / discharge device 3 includes a high-pressure tank 31, an anode gas supply passage 32, an anode pressure regulating valve 33, an ejector 34, an anode gas circulation passage 35, an anode circulation pump 36, a pressure sensor 37, and a purge valve. 38.
- the high pressure tank 31 stores the anode gas supplied to the fuel cell stack 1 in a high pressure state.
- the anode gas supply passage 32 is a passage for supplying the anode gas stored in the high-pressure tank 31 to the fuel cell stack 1.
- One end of the anode gas supply passage 32 is connected to the high-pressure tank 31, and the other end is connected to the anode gas inlet hole of the fuel cell stack 1.
- the anode pressure regulating valve 33 is provided in the anode gas supply passage 32 between the high pressure tank 31 and the ejector 34.
- As the anode pressure regulating valve 33 for example, an electromagnetic valve capable of changing the opening degree of the valve in stages is used.
- the anode pressure regulating valve 33 is controlled to open and close by the controller 200. By this opening / closing control, the pressure of the anode gas supplied to the fuel cell stack 1 is adjusted.
- the ejector 34 is provided in the anode gas supply passage 32 between the anode pressure regulating valve 33 and the fuel cell stack 1.
- the ejector 34 is a mechanical pump provided at a portion where the anode gas circulation passage 35 joins the anode gas supply passage 32.
- the ejector 34 sucks the anode off gas from the fuel cell stack 1 by accelerating the flow rate of the anode gas supplied from the anode pressure regulating valve 33 to generate a negative pressure.
- the ejector 34 discharges the anode off gas together with the anode gas supplied from the anode pressure regulating valve 33 to the fuel cell stack 1.
- the ejector 34 includes, for example, a conical nozzle whose opening is narrowed from the anode pressure regulating valve 33 toward the fuel cell stack 1 and a diffuser having a suction port for sucking the anode off gas from the fuel cell stack 1.
- the anode gas circulation passage 35 may be simply joined to the anode gas supply passage 32.
- the anode gas circulation passage 35 is a passage through which the anode off gas from the fuel cell stack 1 is circulated to the anode gas supply passage 32.
- One end of the anode gas circulation passage 35 is connected to the anode gas outlet hole of the fuel cell stack 1, and the other end is connected to the suction port of the ejector 34.
- the anode circulation pump 36 is provided in the anode gas circulation passage 35.
- the anode circulation pump 36 circulates the anode off gas through the fuel cell stack 1 via the ejector 34.
- the rotation speed of the anode circulation pump 36 is controlled by the controller 200. Thereby, the flow rate of the anode gas circulating through the fuel cell stack 1 is adjusted.
- the flow rate of the anode gas circulating through the fuel cell stack 1 is simply referred to as “anode gas circulation flow rate”.
- the purge valve 38 is provided in the anode gas discharge passage branched from the anode gas circulation passage 35.
- the purge valve 38 discharges impurities contained in the anode off gas to the outside. Impurities are nitrogen gas in the air that has permeated the electrolyte membrane 111 from the cathode gas flow path 131, generated water accompanying power generation, and the like.
- the opening degree of the purge valve 38 is controlled by the controller 200.
- the anode gas discharge passage joins the cathode gas discharge passage 25 on the downstream side of the cathode pressure regulating valve 26.
- the anode off-gas discharged from the purge valve 38 is mixed with the cathode off-gas in the cathode gas discharge passage 25, so that the hydrogen concentration in the mixed gas is set to a value equal to or lower than the discharge allowable concentration.
- the stack cooling device 4 is a device that supplies a coolant for cooling the fuel cell 10 to the fuel cell stack 1 and adjusts the fuel cell stack 1 to a temperature suitable for power generation.
- cooling water is used as the refrigerant.
- the stack cooling device 4 functions as a gas temperature adjusting device for increasing the temperature of the cathode gas passing through the cathode gas flow path 131 in order to increase the amount of water vapor in the cathode gas discharged from the fuel cell stack 1. That is, the stack cooling device 4 constitutes temperature adjusting means for adjusting the temperature of the oxidant supplied to the fuel cell 10.
- the stack cooling device 4 includes a cooling water circulation passage 41, a cooling water pump 42, a radiator 43, a bypass passage 44, a three-way valve 45, an inlet water temperature sensor 46, and an outlet water temperature sensor 47.
- the cooling water circulation passage 41 is a passage for circulating cooling water through the fuel cell stack 1. One end of the cooling water circulation passage 41 is connected to the cooling water inlet hole of the fuel cell stack 1, and the other end is connected to the cooling water outlet hole of the fuel cell stack 1.
- the cooling water pump 42 is provided in the cooling water circulation passage 41.
- the cooling water pump 42 supplies cooling water to the fuel cell stack 1 via the radiator 43.
- the rotation speed of the cooling water pump 42 is controlled by the controller 200.
- the amount of heat dissipated from the fuel cell 10 to the coolant increases as the rotational speed of the coolant pump 42 increases.
- the temperature of the battery stack 1 decreases.
- the lower the rotational speed of the cooling water pump 42 the lower the heat exchange rate, and thus the temperature of the fuel cell stack 1 increases.
- the radiator 43 is provided in the cooling water circulation passage 41 downstream of the cooling water pump 42.
- the radiator 43 cools the cooling water warmed in the fuel cell stack 1 with a fan.
- the bypass passage 44 is a passage that bypasses the radiator 43 and that directly circulates the cooling water discharged from the fuel cell stack 1 to the fuel cell stack 1.
- One end of the bypass passage 44 is connected to the coolant circulation passage 41 between the coolant pump 42 and the radiator 43, and the other end is connected to one end of the three-way valve 45.
- the bypass passage 44 may be provided with a heater for warming up the fuel cell stack 1 when the fuel cell system 100 is started below zero.
- the three-way valve 45 adjusts the temperature of the cooling water supplied to the fuel cell stack 1.
- the three-way valve 45 is realized by a thermostat.
- the three-way valve 45 is provided at a portion where the bypass passage 44 in the coolant circulation passage 41 joins between the radiator 43 and the coolant inlet hole of the fuel cell stack 1.
- the cooling water passage from the radiator 43 to the fuel cell stack 1 is blocked, and only the cooling water that has passed through the bypass passage 44 is used as fuel. Supply to the battery stack 1. As a result, cooling water having a higher temperature than the cooling water passing through the radiator 43 flows through the fuel cell stack 1.
- the opening of the cooling water passage from the radiator 43 to the fuel cell stack 1 starts to gradually increase.
- the three-way valve 45 mixes the cooling water that has passed through the bypass passage 44 and the cooling water that has passed through the radiator 43, and supplies the cooling water to the fuel cell stack 1. As a result, cooling water having a temperature lower than that of the cooling water passing through the bypass passage 44 flows through the fuel cell stack 1.
- the inlet water temperature sensor 46 and the outlet water temperature sensor 47 detect the temperature of the cooling water.
- the temperature of the cooling water is used as the temperature of the fuel cell stack 1 or the temperature of the cathode gas.
- the temperature of the fuel cell stack 1 is also referred to as “stack temperature”.
- the inlet water temperature sensor 46 is provided in the cooling water circulation passage 41 located in the vicinity of the cooling water inlet hole formed in the fuel cell stack 1.
- the inlet water temperature sensor 46 detects the temperature of the cooling water flowing into the cooling water inlet hole of the fuel cell stack 1.
- the temperature of the cooling water flowing into the cooling water inlet hole of the fuel cell stack 1 is referred to as “stack inlet water temperature”.
- the inlet water temperature sensor 46 outputs a signal that detects the stack inlet water temperature to the controller 200.
- the outlet water temperature sensor 47 is provided in the cooling water circulation passage 41 located in the vicinity of the cooling water outlet hole formed in the fuel cell stack 1.
- the outlet water temperature sensor 47 detects the temperature of the cooling water discharged from the fuel cell stack 1.
- the temperature of the cooling water discharged from the fuel cell stack 1 is referred to as “stack outlet water temperature”.
- the outlet water temperature sensor 47 outputs a signal that detects the stack outlet water temperature to the controller 200.
- the load device 5 is driven by receiving the generated power supplied from the fuel cell stack 1.
- the load device 5 includes, for example, an electric motor that drives the vehicle, a part of an auxiliary device that assists the power generation of the fuel cell stack 1, a control unit that controls the electric motor, and the like.
- Examples of the auxiliary equipment of the fuel cell stack 1 include the compressor 22, the anode circulation pump 36, the cooling water pump 42, and the like.
- the load device 5 includes a DC / DC converter, an electric motor inverter is connected to one of the DC / DC converters, a battery is connected to the other, and a power supply line between the DC / DC converter and the battery is supplemented.
- the structure which connects a part of machine may be sufficient.
- the control unit that controls the load device 5 outputs the required power required for the fuel cell stack 1 to the controller 200. For example, the required power of the load device 5 increases as the amount of depression of an accelerator pedal provided in the vehicle increases.
- a current sensor 51 and a voltage sensor 52 are disposed between the load device 5 and the fuel cell stack 1.
- the current sensor 51 is connected to a power supply line between the positive terminal 1p of the fuel cell stack 1 and the load device 5.
- the current sensor 51 detects the current output from the fuel cell stack 1 to the load device 5 as the output power of the fuel cell stack 1.
- the current output from the fuel cell stack 1 to the load device 5 is referred to as “stack output current”.
- the current sensor 51 outputs a signal that detects the stack output current to the controller 200.
- the voltage sensor 52 is connected between the positive terminal 1p and the positive terminal 1n in the fuel cell stack 1.
- the voltage sensor 52 detects an inter-terminal voltage that is a voltage between the positive terminal 1p and the positive terminal 1n in the fuel cell stack 1.
- the terminal voltage of the fuel cell stack 1 is referred to as “stack output voltage”.
- the voltage sensor 52 outputs a signal that detects the stack output voltage to the controller 200.
- the impedance measuring device 6 is a device that detects the wet state of the electrolyte membrane 111.
- the impedance measuring device 6 measures the internal impedance of the fuel cell stack 1 correlated with the wet state of the electrolyte membrane 111.
- the internal impedance of the fuel cell stack 1 is used as a parameter indicating the wet state of the electrolyte membrane 111.
- the fuel cell stack 1 is provided with a positive electrode tab connected in series with the positive electrode terminal 1p and a negative electrode tab connected in series with the positive electrode terminal 1n.
- the impedance measuring device 6 is provided on each of the positive electrode tab and the negative electrode tab. Is connected.
- the impedance measuring device 6 supplies an alternating current having a frequency suitable for detecting the electric resistance of the electrolyte membrane 111 to the positive electrode terminal 1p.
- the frequency suitable for detecting the electric resistance of the electrolyte membrane is hereinafter referred to as “electrolyte membrane response frequency”.
- the impedance measuring device 6 detects an AC voltage generated between the positive electrode terminal 1p and the positive electrode terminal 1n by an AC current having an electrolyte membrane response frequency, and the amplitude of the detected AC voltage is supplied to the positive electrode terminal 1p.
- the internal impedance is calculated by dividing by.
- the fuel cell 10 located in the middle is provided with a halfway tab, and the impedance measuring device 6 is also connected to the middle tab.
- the halfway tab is grounded in the impedance measuring device 6.
- the impedance measuring device 6 supplies an alternating current having an electrolyte membrane response frequency to both the positive terminal 1p and the positive terminal 1n.
- the impedance measuring device 6 calculates the internal impedance on the positive electrode side by dividing the amplitude of the alternating voltage between the positive electrode terminal 1p and the halfway tab by the amplitude of the alternating current supplied to the positive electrode terminal 1p. Furthermore, the impedance measuring device 6 calculates the internal impedance on the negative electrode side by dividing the amplitude of the alternating voltage between the positive electrode terminal 1n and the halfway tab by the amplitude of the alternating current supplied to the positive electrode terminal 1n.
- HFR High Frequency Resistance
- the controller 200 includes a microcomputer that includes a central processing unit (CPU), a read-only memory (ROM), a random access memory (RAM), and an input / output interface (I / O interface).
- CPU central processing unit
- ROM read-only memory
- RAM random access memory
- I / O interface input / output interface
- the controller 200 includes output signals from the flow sensor 23, the pressure sensor 24, the pressure sensor 37, the inlet water temperature sensor 46, the outlet water temperature sensor 47, the current sensor 51, the voltage sensor 52, and the impedance measuring device 6 and the requirements of the load device 5. Power is input. These signals are used as parameters relating to the operating state of the fuel cell system 100.
- the controller 200 controls the flow rate and pressure of the cathode gas by controlling the compressor 22 and the cathode pressure regulating valve 26 according to the operating state of the fuel cell system 100, and also controls the anode pressure regulating valve 33 and the anode circulation pump 36. Thus, the flow rate and pressure of the anode gas are controlled. Furthermore, the controller 200 controls the temperature of the fuel cell 10 and the cathode gas in the fuel cell stack 1 by controlling the cooling water pump 42 and the three-way valve 45 in accordance with the operating state of the fuel cell system 100.
- the controller 200 calculates the target flow rate and target pressure of the cathode gas and the target flow rate and target pressure of the anode gas based on the required power of the load device 5.
- the controller 200 controls the rotational speed of the compressor 22 and the opening degree of the cathode pressure regulating valve 26 based on the target flow rate and target pressure of the cathode gas, and the anode circulation pump based on the target flow rate and target pressure of the anode gas.
- the rotational speed of 36 and the opening degree of the anode pressure regulating valve 33 are controlled.
- the controller 200 calculates a stack target temperature for maintaining the power generation performance of the fuel cell stack 1, and controls the rotation speed of the cooling water pump 42 based on the stack target temperature. For example, when the stack temperature is higher than the stack target temperature, the controller 200 increases the rotation speed of the cooling water pump 42 as compared with the case where the stack temperature is lower than the stack target temperature.
- the controller 200 operates the wet state of the fuel cell stack 1 so that the wet state of the fuel cell stack 1 is suitable for power generation within a range where the required power of the load device 5 can be secured.
- the transition of the wet state of the fuel cell stack 1 to the dry (dry) side that is, the reduction of excess moisture in the electrolyte membrane 111 is referred to as “dry operation”.
- the transition of the wet state of the fuel cell stack 1 to the wet (wet) side that is, the increase of moisture in the electrolyte membrane 111 is referred to as “wet operation”.
- the controller 200 controls the cathode gas flow rate, the cathode gas pressure, the anode gas flow rate, and the stack temperature.
- the cathode gas flow rate control by the controller 200 is mainly executed by the compressor 22, and the cathode gas pressure control is mainly executed by the cathode pressure regulating valve 26.
- the controller 200 increases the cathode gas flow rate or decreases the cathode gas pressure in order to increase the amount of water discharged from the fuel cell stack 1.
- the controller 200 decreases the cathode gas flow rate or increases the cathode gas pressure.
- the anode gas flow rate control by the controller 200 is mainly executed by the anode circulation pump 36.
- the anode gas flowing through the anode gas passage 121 shown in FIG. 2 is humidified by water vapor leaking (permeating) from the downstream side of the cathode gas passage 131 through the electrolyte membrane 111.
- the flow rate of the humidified anode gas is increased, the moisture contained in the anode gas tends to spread from the upstream to the downstream of the anode gas flow path 121, and the wetness of the fuel cell stack 1 is likely to increase.
- the controller 200 increases the flow rate of the anode gas circulating through the fuel cell stack 1 in order to increase the flow rate of the anode gas humidified in the fuel cell stack 1.
- the controller 200 decreases the flow rate of the anode gas circulating through the fuel cell stack 1.
- the stack temperature control by the controller 200 is mainly executed by the cooling water pump 42.
- the temperature of the fuel cell 10 is higher than the stack inlet water temperature. Therefore, if the flow rate of the cooling water flowing through the cooling water channel 141 shown in FIG. 2 is reduced, the temperature of the cathode gas flowing through the cathode gas channel 131 increases. The temperature of the fuel cell 10 itself rises. When the cathode gas temperature in the cathode gas channel 131 rises, the amount of water vapor that can be held by the cathode gas increases, so that the water discharged from the fuel cell stack 1 increases. As described above, when the stack temperature is raised, the moisture discharged from the fuel cell stack 1 increases, so that the wetness of the fuel cell stack 1 decreases.
- the controller 200 increases the stack temperature so that the temperature of the cathode gas in the fuel cell stack 1 increases.
- the controller 200 decreases the stack temperature.
- the controller 200 executes the weight reduction control for reducing the flow rate of the anode gas circulating through the fuel cell stack 1 in preference to the temperature increase control for increasing the stack temperature in the dry operation.
- FIG. 4 is a block diagram illustrating an example of a functional configuration of the controller 200 according to the present embodiment. Here, control parameters when performing the dry operation are shown.
- the controller 200 includes a film wet state detection unit 201, a power generation control unit 202, an anode gas supply / discharge device command unit 203, and a stack cooling device command unit 204.
- the power generation control unit 202 includes an anode gas target flow rate calculation unit 220 and a stack target temperature calculation unit 230.
- the membrane wet state detection unit 201 constitutes a wet state detection unit that detects the wet state of the electrolyte membrane 111 in the fuel cell stack 1.
- the membrane wet state detection unit 201 acquires the HFR of the fuel cell stack 1 measured by the impedance measuring device 6 as wet state information indicating the wetness of the electrolyte membrane 111.
- the HFR output from the impedance measurement device 6 is referred to as “measurement HFR”.
- the membrane wet state detection unit 201 calculates a target water balance for maintaining the wet state of the electrolyte membrane 111 in a state suitable for power generation based on the measured HFR from the impedance measuring device 6.
- the target water balance is a parameter indicating the excess or deficiency of moisture with respect to the target wet state of the electrolyte membrane 111. That is, the target water balance is a parameter that correlates with the wetness of the electrolyte membrane 111.
- the membrane wet state detection unit 201 determines that the moisture of the electrolyte membrane 111 is large, and the target water balance is minus (negative) smaller than zero (0). Set the value of.
- the power generation control unit 202 executes a wet operation for increasing the moisture in the electrolyte membrane 111.
- the membrane wet state detection unit 201 determines that the moisture of the electrolyte membrane 111 is low, and sets the target water balance to a positive (positive) value greater than zero. Set.
- the power generation control unit 202 performs a dry operation for reducing excess moisture in the electrolyte membrane 111.
- the film wet state detection unit 201 outputs the calculated target water balance to the anode gas target flow rate calculation unit 220 and the stack target temperature calculation unit 230.
- the membrane wet state detection unit 201 outputs, for example, the stack temperature to the anode gas target flow rate calculation unit 220 as the temperature of the cathode gas flowing in the fuel cell stack 1.
- the membrane wet state detection unit 201 calculates the lowest stack temperature, which is the operation temperature for making the electrolyte membrane 111 wet most by the wet operation.
- the minimum stack temperature is set to the lower limit of the range in which the stack cooling device 4 can adjust the temperature of the fuel cell stack 1 in the wet operation. That is, the minimum stack temperature is an operation temperature at the time of wet operation used for maximizing the water content of the electrolyte membrane 111 within a range in which the power generation of the fuel cell stack 1 can be stably controlled.
- the film wet state detection unit 201 increases the minimum stack temperature because the amount of heat radiated from the fuel cell 10 increases as the required power of the load device 5 increases.
- the film wet state detection unit 201 outputs the calculated minimum stack temperature to the anode gas target flow rate calculation unit 220.
- the film wet state detection unit 201 may generate wet state information using the temperature of the fuel cell stack 1 instead of the measurement HFR.
- the membrane wet state detection unit 201 calculates the average value of the stack inlet water temperature and the stack outlet water temperature as the temperature of the fuel cell stack 1.
- membrane wet state detection part 201 produces
- the film wet state detection unit 201 may generate wet state information using the required power of the load device 5 instead of the measurement HFR.
- the film wet state detection unit 201 acquires the required power from the control unit of the load device 5, refers to a predetermined wet estimation map, and wet state information associated with the acquired required power Is generated.
- the membrane wet state detection unit 201 increases the degree of wetness of the electrolyte membrane 111 indicated in the wet state information because the amount of generated water generated with power generation increases as the required power of the load device 5 increases.
- the power generation control unit 202 controls power generation of the fuel cell 10 by controlling supply of anode gas by the anode pressure regulating valve 33 and anode circulation pump 36 and supply of cathode gas by the compressor 22 and cathode pressure regulating valve 26. Configure.
- the power generation control unit 202 increases the stack temperature according to the size of the target water balance while reducing the anode gas flow rate as compared with the case of performing the wet operation. That is, the power generation control unit 202 reduces the anode gas circulation flow rate and reduces the membrane wetness when reducing the water content of the electrolyte membrane 111 based on the signal from the membrane wet state detection unit 201 as compared with increasing the water content of the electrolyte membrane 111. In response to a signal from the state detection unit 201, the temperature of the cathode gas flowing in the fuel cell stack 1 is increased.
- the power generation control unit 202 when the dry operation is executed, performs control to reduce the anode gas flow rate by the anode circulation pump 36 in preference to the control to increase the stack temperature by the cooling water pump 42. Execute.
- the anode gas target flow rate calculation unit 220 calculates an anode gas target flow rate for controlling the anode gas flow rate supplied to the fuel cell stack 1.
- the anode gas target flow rate calculation unit 220 calculates the required load flow rate of the anode gas necessary for power generation of the fuel cell stack 1 based on the required power of the load device 5 and maintains the wet state of the fuel cell stack 1. The required anode gas wetting flow rate is calculated. The anode gas target flow rate calculation unit 220 outputs the larger one of the load request flow rate and the wet request flow rate of the anode gas to the anode gas supply / discharge device command unit 203 as the anode gas target flow rate.
- the anode gas target flow rate calculation unit 220 acquires the target water balance and the minimum stack temperature from the membrane wet state detection unit 201, acquires the measured value of the cathode gas flow rate from the flow rate sensor 23, and the pressure sensor 24. Get the measured value of cathode gas pressure.
- the anode gas target flow rate calculation unit 220 calculates an anode gas wetting request flow rate used for wet control based on the target water balance, the minimum stack temperature, the measured value of the cathode gas flow rate, and the measured value of the cathode gas pressure. To do.
- the anode gas target flow rate calculation unit 220 increases the anode gas wetting request flow rate in order to increase the water content of the electrolyte membrane 111 as the target water balance increases.
- the anode gas target flow rate calculation unit 220 decreases the anode gas wetting request flow rate in order to reduce the water content of the electrolyte membrane 111 as the target water balance decreases.
- the anode gas target flow rate calculation unit 220 decreases the anode gas wetting request flow rate in order to reduce the moisture in the anode gas circulating through the fuel cell stack 1 as the minimum stack temperature decreases. On the other hand, the anode gas target flow rate calculation unit 220 increases the required anode gas wetting flow rate as the minimum stack temperature increases.
- the minimum stack temperature set by the film wet state detection unit 201 is usually lower than the measured value of the stack temperature.
- the anode gas target flow rate calculation unit 220 can reduce the required anode gas wetting flow rate in the dry operation as compared with the case where the measured value of the stack temperature is used. Furthermore, by using the minimum stack temperature, the required anode gas wetting flow rate can be reduced even faster within a range where the fuel cell system 100 can be operated safely.
- the anode gas target flow rate calculation unit 220 outputs the calculated anode gas wetting request flow rate to the stack target temperature calculation unit 230.
- the stack target temperature calculation unit 230 calculates a stack target temperature for adjusting the temperature of the fuel cell stack 1.
- the stack target temperature calculation unit 230 outputs the stack target temperature to the stack cooling device command unit 204.
- the stack target temperature calculation unit 230 acquires the required anode gas wetting flow rate from the anode gas target flow rate calculation unit 220 and acquires the target water balance from the membrane wet state detection unit 201. Further, the stack target temperature calculation unit 230 acquires a measured value of the cathode gas flow rate from the flow sensor 23 and acquires a measured value of the cathode gas pressure from the pressure sensor 24.
- the stack target temperature calculation unit 230 calculates the stack target temperature used for the wet control based on the required anode gas wetting flow rate, the target water balance, the measured value of the cathode gas flow rate, and the measured value of the cathode gas pressure. .
- the stack target temperature calculation unit 230 lowers the stack target temperature in order to reduce the moisture in the cathode gas discharged from the fuel cell stack 1 as the target water balance increases. On the other hand, the stack target temperature calculation unit 230 increases the stack target temperature in order to increase the water discharged from the fuel cell stack 1 as the target water balance decreases.
- the anode gas supply / discharge device command unit 203 controls the rotation speed of the anode circulation pump 36 and the opening of the anode pressure regulating valve 33 so that the circulation flow rate of the anode gas circulating through the fuel cell stack 1 becomes the anode gas target flow rate. To do.
- the stack cooling device command unit 204 controls the rotation speed of the cooling water pump 42 so that the temperature of the fuel cell stack 1 becomes the stack target temperature.
- the stack cooling device command unit 204 sets the rotational speed of the coolant pump 42 so that the temperature of the fuel cell stack 1 becomes the stack target temperature. The opening degree of the three-way valve 45 is controlled.
- FIG. 5 is a block diagram illustrating an example of a functional configuration of the film wet state detection unit 201.
- the film wet state detection unit 201 includes a priority control unit 201A and a target water balance calculation unit 201B.
- the priority control unit 201A sets the order of controlling the operation of the anode gas supply / discharge device 3 and the operation of the stack cooling device 4.
- the priority control unit 201 ⁇ / b> A controls the operation of the anode gas supply / exhaust device 3 with priority over the operation of the stack cooling device 4 when performing a dry operation for reducing the moisture of the electrolyte membrane 111.
- the priority control unit 201A when the dry operation is executed by the power generation control unit 202, the priority control unit 201A sets the minimum stack temperature during the wet operation in the anode gas target flow rate calculation unit 220.
- the priority control unit 201A includes a stack target current calculation unit 211 and a minimum stack temperature calculation unit 212.
- the stack target current calculation unit 211 calculates a stack target current based on the load connected to the fuel cell stack 1. For example, in the stack target current calculation unit 211, the IV (current voltage) characteristics of the fuel cell stack 1 are recorded in advance. When the stack target current calculation unit 211 acquires the required power from the load device 5, the stack target current calculation unit 211 refers to the IV characteristics of the fuel cell stack 1 and calculates the current as the acquired generated power as the stack target current.
- the IV characteristic of the fuel cell stack 1 may be estimated based on the stack output current and the stack output voltage when the output current of the fuel cell stack 1 is changed.
- the stack target current calculation unit 211 outputs the stack target current to the anode gas target flow rate calculation unit 220 and the minimum stack temperature calculation unit 212.
- the minimum stack temperature calculation unit 212 calculates the minimum stack temperature Tmin when the fuel cell stack 1 is most cooled within the operation range of the stack cooling device 4 based on the stack target current.
- a minimum stack temperature map indicating the relationship between the stack target current and the minimum stack temperature is recorded in the minimum stack temperature calculation unit 212 in advance. Details of the minimum stack temperature map will be described later with reference to FIG.
- the minimum stack temperature calculation unit 212 When acquiring the stack target current, the minimum stack temperature calculation unit 212 refers to the minimum stack temperature map and calculates the minimum stack temperature T min related to the acquired stack target current. The minimum stack temperature calculation unit 212 may calculate the minimum stack temperature T min based on the rotational speed of the cooling water pump 42, the opening degree of the three-way valve 45, or the like.
- the minimum stack temperature calculation unit 212 executes a dry operation for reducing the water content of the electrolyte membrane 111 or a wet operation for increasing the water content of the electrolyte membrane 111 based on the target water balance from the feedback control unit 214. Judge whether or not.
- the minimum stack temperature calculation unit 212 determines that the dry operation is started when the target water balance is larger than a predetermined upper limit threshold.
- the minimum stack temperature calculation unit 212 acquires the target water balance at a predetermined sampling cycle, and determines that the dry operation is started when the current value of the target water balance is smaller than the previous value. Also good.
- the minimum stack temperature calculation unit 212 When it is determined that the dry operation is started, the minimum stack temperature calculation unit 212 outputs the minimum stack temperature T min to the anode gas target flow rate calculation unit 220.
- the temperature raising control for increasing the stack temperature may be disabled.
- the lowest stack temperature calculation unit 212 outputs a measured value of the stack temperature instead of the lowest stack temperature Tmin .
- the minimum stack temperature calculation unit 212 calculates a value obtained by averaging the detected value from the inlet water temperature sensor 46 and the detected value from the outlet water temperature sensor 47 as a measured value of the stack temperature.
- the calculation in the minimum stack temperature calculation unit 212 may be stopped.
- the required flow rate of the anode gas wetting is calculated using the actual cooling water temperature (stack temperature) supplied to the fuel cell stack 1, so that the stack temperature control system The dry operation suitable for the abnormal state can be executed.
- the lowest stack temperature calculation unit 212 outputs an average value of the stack inlet water temperature and the stack outlet water temperature as a measured value of the stack temperature. Even when it is determined that the wet operation is started, the minimum stack temperature calculation unit 212 outputs the minimum stack temperature T min in the same manner as when it is determined that the dry operation is started. You may do it.
- the target water balance calculation unit 201B includes a target HFR calculation unit 213 and a feedback control unit 214.
- the target HFR calculator 213 calculates a target HFR for controlling the wet state of the electrolyte membrane 111 to a target state according to the operating state of the fuel cell stack 1.
- a film wetting control map showing the relationship between the stack output current and the target HFR is recorded in advance in the target HFR calculating unit 213.
- the film wetting control map will be described in detail with reference to FIG.
- the target HFR calculation unit 213 calculates a target HFR related to the acquired stack output current Is with reference to the film wetting control map.
- the target HFR calculating unit 213 may calculate the target HFR based on the stack output current Is using a predetermined calculation formula. Further, the target HFR calculation unit 213 may calculate the target HFR using the required power of the load device 5 instead of the stack output current Is.
- the target HFR calculating unit 213 outputs the calculated target HFR to the feedback control unit 214.
- the feedback control unit 214 calculates a target water balance Q w_t for increasing or decreasing the water content of the electrolyte membrane 111 so that the wet state of the electrolyte membrane 111 becomes a target state.
- the feedback control unit 214 acquires the target HFR from the target HFR calculation unit 213 and acquires the measurement HFR from the impedance measurement device 6. Then, the feedback control unit 214 calculates the target water balance Q w_t so that the deviation between the measured HFR and the target HFR converges to zero.
- the feedback control unit 214 calculates the target water balance by subtracting the target HFR from the measured HFR to obtain a deviation between the measured HFR and the target HFR, and executing PI control based on the deviation.
- the feedback control unit 214 outputs the calculated target water balance to the minimum stack temperature calculation unit 212 and the anode gas target flow rate calculation unit 220.
- FIG. 6 is a conceptual diagram illustrating an example of a minimum stack temperature map set in the minimum stack temperature calculation unit 212.
- the horizontal axis is the stack target current, and the output power of the fuel cell stack 1 increases as the stack target current increases.
- the vertical axis is the minimum stack temperature.
- the minimum stack temperature is set for each stack target current.
- the minimum stack temperature is a value measured in advance or a value calculated in advance when the rotation speed of the fan provided in the cooling water pump 42 or the radiator 43 is set to a predetermined upper limit value.
- the stack target current is within a large current range that is larger than the predetermined current value I 1 , the amount of heat generated by the fuel cell stack 1 increases, so that the minimum stack temperature increases as the stack target current increases.
- FIG. 7 is a conceptual diagram illustrating an example of a film wetting control map set in the target HFR calculating unit 213.
- the horizontal axis represents the stack output current, and the output power of the fuel cell stack 1 increases as the stack output current increases.
- the vertical axis is the target HFR. The larger the target HFR, the easier the electrolyte membrane 111 dries, and the smaller the target HFR, the easier the electrolyte membrane 111 gets wet.
- the target HFR is set so that the flow of the cathode gas is not hindered due to the liquid water staying in the cathode gas flow path 131.
- the target HFR decreases as the stack output current increases.
- the reason for setting in this way is that the smaller the cathode gas flow rate supplied to the fuel cell stack 1, the more easily the cathode gas flow is hindered by the liquid water staying in the cathode gas channel 131. Therefore, the target HFR at the time of low load operation where the required power of the load device 5 is low is set higher than that at the time of normal operation.
- the target HFR within the large current range is set to a constant value that is smaller than the target HFR within the small current range.
- FIG. 8 is a block diagram illustrating an example of a functional configuration of the anode gas target flow rate calculation unit 220.
- the anode gas target flow rate calculation unit 220 includes an anode gas load required flow rate calculation unit 221, a power generation generated water amount calculation unit 222, a target drainage amount calculation unit 223, a minimum temperature saturated water vapor pressure calculation unit 224, and a cathode relative humidity calculation unit 225. Including.
- the anode gas target flow rate calculation unit 220 further includes an anode / cathode flow rate ratio calculation unit 226, an anode gas wetting request flow rate calculation unit 227, and an anode gas target flow rate setting unit 228.
- the anode gas load required flow rate calculation unit 221 calculates a load required flow rate that is the minimum anode gas flow rate required for power generation of the fuel cell stack 1 based on the required power of the load device 5.
- a load required flow rate map indicating the relationship between the stack target current and the anode gas flow rate is recorded in advance.
- the anode gas load request flow rate calculation unit 221 acquires the stack target current from the stack target current calculation unit 211, the anode gas load request flow rate calculation unit 221 refers to the load request flow rate map and determines the anode gas flow rate associated with the acquired stack target current as the load request flow rate. Calculate as
- the anode gas load request flow rate calculation unit 221 outputs the calculated load request flow rate to the anode gas target flow rate setting unit 228.
- the power generation generated water amount calculation unit 222 calculates a power generation generated water amount that is the total amount of water generated by the power generation of each fuel cell 10 in the fuel cell stack 1 based on the output current of the fuel cell stack 1.
- the power generation generated water amount calculation unit 222 acquires the stack output current Is from the current sensor 51, and calculates the power generation generated water amount Qw_in based on the stack output current Is as shown in the following equation (3).
- N is the number of fuel cells 10 and F [C / mol] is the Faraday constant (96485.39). Further, “60” is a converted value from a second unit (sec) to a minute unit (min), and “22.4” is a volume of 1 mol (mol) of an ideal gas in a standard state.
- the generated power generation water amount calculation unit 222 outputs the calculated generated power generation water amount Q w_in to the target drainage amount calculation unit 223.
- the target drainage amount calculation unit 223 calculates a target drainage amount Qw_out that is moisture to be discharged from the fuel cell stack 1 by calculating a difference between the power generation generated water amount Qw_in and the target water balance Qw_t .
- the target water discharge amount calculation unit 223, as the following formula (4) by subtracting the target water balance Q W_t from the generator water quantity Q W_in, calculates a target amount of waste water Q w_out.
- Minimum temperature saturated steam pressure calculating unit 224 based on the minimum stack temperature T min is set by the priority control unit 201A, and calculates the saturated vapor pressure P Sat_min at a minimum stack temperature T min.
- the minimum temperature saturated water vapor pressure calculation unit 224 obtains the minimum stack temperature T min from the minimum stack temperature calculation unit 212 and, based on the minimum stack temperature T min , the minimum temperature as shown in the following equation (4).
- the saturated water vapor pressure P sat — min is calculated.
- the cathode relative humidity calculation unit 225 calculates a cathode outlet relative humidity RH c_out that indicates a ratio of the humidity of the cathode gas to the humidity of the anode gas in the fuel cell stack 1 based on the minimum temperature saturated water vapor pressure P sat — min .
- the cathode outlet relative humidity RH c_out is the cathode gas humidity at the outlet (downstream) side of the cathode gas channel 131 shown in FIG. 2 and the anode gas at the inlet (upstream) side of the anode gas channel 121. It is the value divided by the humidity.
- the cathode relative humidity calculation unit 225 acquires the measured value Q c_sens of the cathode gas flow rate from the flow sensor 23 and acquires the measured value P c_sens of the cathode gas pressure from the pressure sensor 24.
- the cathode relative humidity calculation unit 225 calculates the cathode outlet relative humidity RH based on the minimum temperature saturated water vapor pressure P sat_min , the cathode gas pressure P c_sens , the cathode gas flow rate Q c_sens, and the target drainage amount Q w_out as shown in the following equation (6). c_out is calculated.
- the cathode relative humidity calculation unit 225 outputs the calculated cathode outlet relative humidity RH c_out_min to the anode / cathode flow ratio calculation unit 226.
- the anode / cathode flow ratio calculation unit 226 calculates an anode / cathode flow ratio K ac_min indicating a ratio of the anode gas flow rate to the cathode gas flow rate based on the cathode outlet relative humidity RH c_out_min .
- a flow rate map showing the relationship between the cathode outlet relative humidity and the anode / cathode flow rate ratio is recorded in advance in the anode / cathode flow rate calculation unit 226. Details of the flow rate ratio map will be described later with reference to FIG.
- the anode / cathode flow ratio calculation unit 226 obtains the cathode outlet relative humidity RH c_out_min from the cathode relative humidity calculation unit 225
- the anode / cathode flow rate related to the cathode outlet relative humidity RH c_out_min is referred to by referring to the flow rate ratio map.
- the ratio K ac_min is calculated.
- the anode / cathode flow rate calculation unit 226 outputs the calculated anode / cathode flow rate ratio K ac_min to the anode gas wetting request flow rate calculation unit 227.
- the anode gas wetting request flow rate calculation unit 227 calculates an anode gas wetting request flow rate Q a_rw for setting the wet state of the fuel cell stack 1 to a target state.
- Anode gas wet required flow rate calculation unit 227 as follows (7), by multiplying the anode / cathode flow ratio K Ac_min the cathode gas flow rate measurement value Q C_sense, calculates the anode gas wetting required flow rate Q A_rw .
- the anode gas wetting request flow rate calculation unit 227 outputs the calculated anode gas wetting request flow rate Q a_rw to the stack target temperature calculation unit 230 and the anode gas target flow rate setting unit 228.
- the anode gas target flow rate setting unit 228 uses the larger one of the anode gas wetting request flow rate Q a_rw and the load request flow rate from the anode gas load request flow rate calculation unit 221 as the anode gas target flow rate, and the anode gas supply / discharge device command unit It outputs to 203.
- FIG. 9 is a conceptual diagram showing an example of a flow rate map set in the anode / cathode flow rate calculation unit 226.
- the vertical axis represents the cathode outlet relative humidity indicating the relative humidity of the cathode gas discharged from the fuel cell stack 1
- the horizontal axis represents the anode / cathode flow rate ratio indicating the ratio of the anode gas flow rate to the cathode gas flow rate.
- the flow rate ratio map showing the relationship between the cathode outlet relative humidity and the anode / cathode flow rate ratio is set in advance by experimental data or the like when the cathode gas flow rate and the anode gas flow rate are mutually changed in this embodiment.
- the characteristics of the flow rate ratio map are set using, for example, an average value when the cathode gas pressure, stack temperature, hydrogen concentration, or the like is changed, or a value with small variations in characteristics.
- the anode / cathode flow ratio K ac_min based on the lowest stack temperature T min increases as the cathode outlet relative humidity RH c_out decreases. For this reason, when the cathode gas flow rate is constant, the anode gas flow rate increases as the cathode outlet relative humidity RH c_out decreases.
- the cathode outlet relative humidity RH c_out in order to reduce the anode gas wetting required flow rate Q a_rw as much as possible during the dry operation.
- the saturated water vapor pressure P sat_min in order to increase the cathode outlet relative humidity RH c_out , the saturated water vapor pressure P sat_min must be reduced from the relationship of the equation (6), and in order to reduce the saturated water vapor pressure P sat_min , the equation From the relationship (5), it is necessary to reduce the set value of the stack temperature.
- the priority control unit 201A illustrated in FIG. 5 determines that the dry operation is performed, the minimum stack temperature T min is set to the anode gas target instead of the measured value of the stack temperature.
- the flow rate calculation unit 220 is set.
- the saturated water vapor pressure P sat — min is reduced compared to the case where the measured value of the stack temperature is simply used, so that the cathode outlet relative humidity RH c — out can be increased.
- the anode / cathode flow rate ratio K pc_sens becomes small, so that the anode gas wetting required flow rate Q a_rw can be lowered early.
- FIG. 10 is a block diagram illustrating an example of a functional configuration of the stack target temperature calculation unit 230.
- the stack target temperature calculation unit 230 includes a target saturated water vapor pressure calculation unit 231 and a target cooling water temperature conversion unit 232.
- the target saturated water vapor pressure calculation unit 231 calculates a target saturated water vapor pressure P sat_t for maintaining the wetness of the electrolyte membrane 111 at a target value based on the anode gas wetting required flow rate Q a_rw .
- the target saturated water vapor pressure calculation unit 231 acquires the anode gas wetting request flow rate Q a_rw and acquires the measured value Q c_sens of the cathode gas flow rate from the flow rate sensor 23. Then, the target saturated water vapor pressure calculator 231 calculates the anode / cathode flow rate ratio K ac based on the anode gas wetting request flow rate Q a_rw and the cathode gas flow rate Q c_sens as shown in the following equation (8).
- the humidity RH c_out is calculated.
- the target saturated water vapor pressure calculation unit 231 acquires the measured value P c_sens of the cathode gas pressure from the pressure sensor 24, and acquires the target drainage amount Q w_out from the target drainage amount calculation unit 223. As shown in FIG. 4, the target saturated water vapor pressure calculation unit 231 obtains the target water balance Q w_t from the membrane wet state detection unit 201 and calculates the target drainage amount Q w_out based on the equation (4). It may be.
- the target saturated water vapor pressure calculation unit 231 performs the target saturated water vapor based on the target drainage amount Qw_out , the cathode gas pressure P c_sens , the cathode outlet relative humidity RH c_out, and the cathode gas flow rate Q c_sens as shown in the following equation (9).
- the pressure P sat — t is calculated.
- the target saturated water vapor pressure calculation unit 231 outputs the calculated target saturated water vapor pressure P sat — t to the target cooling water temperature conversion unit 232.
- the target cooling water temperature conversion unit 232 converts the target saturated water vapor pressure P sat — t into a target cooling water temperature T t that is a target value of the cooling water temperature in the fuel cell stack 1.
- the target cooling water temperature conversion unit 232 calculates the target cooling water temperature T t based on the target saturated water vapor pressure P sat — t as shown in the following equation (10).
- the target cooling water temperature conversion unit 232 outputs the target cooling water temperature T t to the stack cooling device command unit 204 as the stack target temperature.
- the target saturated water vapor pressure P is reduced as the anode gas wetting required flow rate Q a — rw decreases in consideration of the characteristics of the cathode outlet relative humidity in the fuel cell 10.
- sat_t is low.
- the lower the target saturated water vapor pressure P sat — t the lower the stack target temperature Tt.
- the stack target temperature T t decreases as the anode gas wetting request flow rate Q a — rw decreases. Therefore, the power generation control unit 202 decreases the stack temperature as the anode gas flow rate decreases.
- the power generation control unit 202 increases the stack temperature as the wetness of the electrolyte membrane 111 increases.
- the power generation control unit 202 can quickly increase the stack target temperature if the target discharge amount Q w_out does not decrease even when the anode gas wetting request flow rate Q a_rw is being decreased. That is, the power generation control unit 202 can increase the stack temperature increase amount if the wetness of the fuel cell stack 1 does not decrease when the anode gas flow rate is decreased in the dry operation.
- FIG. 11 is a flowchart showing an example of a control method for controlling the fuel cell system 100 in the present embodiment. This control method is repeatedly executed at a predetermined cycle.
- step S1 the controller 200 detects the operating state of the fuel cell stack 1.
- the controller 200 detects the HFR of the fuel cell stack 1 using the impedance measuring device 6 shown in FIG. 3, detects the cathode gas flow rate using the flow rate sensor 23, and uses the pressure sensor 24. Detect the cathode gas pressure.
- Step S1 constitutes a wet state detection step of detecting the wet state of the electrolyte membrane 111.
- step S2 the controller 200 acquires the measured value of the cathode gas flow rate from the flow sensor 23 and acquires the measured value of the cathode gas pressure from the pressure sensor 24.
- step S3 the controller 200 acquires a measurement HFR correlated with the electrolyte membrane 111 from the impedance measurement device 6 as a parameter indicating the wet state of the fuel cell stack 1.
- step S4 the controller 200 calculates a target HFR for maintaining the power generation performance of the fuel cell stack 1.
- the target HFR calculating unit 213 illustrated in FIG. 5 acquires the stack output current from the current sensor 51, and is related to the acquired stack output current using the target HFR map illustrated in FIG. A target HFR is calculated.
- step S5 the membrane wet state detection unit 201 of the controller 200 calculates a target water balance for compensating for the excess or deficiency of moisture with respect to the wet state of the electrolyte membrane 111 so that the measured HFR converges to the target HFR.
- the feedback control unit 214 shown in FIG. 5 calculates the target water balance based on the target HFR and the measured HFR.
- step S6 the controller 200 determines whether or not a dry operation is performed based on the wet state of the electrolyte membrane 111. For example, the controller 200 determines that the dry operation is performed when the measured HFR is smaller than the target HFR.
- the minimum stack temperature calculation unit 212 shown in FIG. 5 determines whether or not the target water balance exceeds a predetermined upper limit value, and when the target water balance exceeds a predetermined upper limit value, the dry operation is performed. Is determined to be executed.
- step S7 the controller 200 calculates the minimum stack temperature of the fuel cell stack 1 by the stack cooling device 4 when the dry operation is executed.
- the minimum stack temperature calculation unit 212 acquires the stack target current, and calculates the minimum stack temperature associated with the acquired stack target current using the minimum stack temperature map shown in FIG.
- step S8 when the dry operation is executed, the controller 200 calculates the anode gas target flow rate based on the minimum stack temperature, the target water balance, the cathode gas flow rate, and the cathode gas pressure.
- the electrical generation product water amount calculating unit 222 calculates a power generation amount of produced water Q W_in based on stack output current I s from a current sensor 51. Then the target wastewater calculating unit 223, as illustrated in formula (4), from the generator water quantity Q W_in by subtracting the target water balance Q W_t calculates a target amount of waste water Q w_out.
- the minimum temperature saturated steam pressure calculating unit 224 as illustrated in formula (5), based on the minimum stack temperature T min, to calculate the minimum temperature saturated vapor pressure P sat_min.
- the cathode relative humidity calculation unit 225 calculates the cathode outlet relative humidity based on the minimum temperature saturated water vapor pressure P sat_min , the cathode gas pressure P c_sens , the target drainage amount Q w_out, and the cathode gas flow rate Q c_sens as shown in Equation (6).
- RH c_out_min is calculated.
- the anode / cathode flow ratio calculation unit 226 calculates an anode / cathode flow ratio K ac_min related to the cathode outlet relative humidity RH c_out_min using the flow ratio map shown in FIG.
- the anode gas wetting request flow rate calculation unit 227 calculates the anode gas wetting request flow rate Q a_rw based on the anode / cathode flow rate ratio K ac_min as shown in Expression (7).
- the anode gas load required flow rate calculation unit 221 calculates the anode gas load required flow rate based on the stack target current, and the anode gas target flow rate setting unit 228 calculates the larger one of the anode gas load required flow rate and the wet required flow rate. Is set as the anode gas target flow rate.
- step S9 the power generation control unit 202 calculates the stack target temperature based on the anode gas wetting request flow rate, the target water balance, the cathode gas pressure, and the cathode gas flow rate.
- the target saturated water vapor pressure calculation unit 231 calculates the anode / cathode flow ratio K ac based on the anode gas wetting request flow rate Q r_w and the cathode gas flow rate Q c_sens as shown in Expression (8). Then, the target saturated water vapor pressure calculator 231 calculates the cathode outlet relative humidity RH c_out associated with the anode / cathode flow ratio K ac using the flow ratio map shown in FIG.
- the target saturated water vapor pressure calculation unit 231 performs the target saturated water vapor pressure based on the cathode outlet relative humidity RH c_out , the target drainage amount Q w_out , the cathode gas pressure P c_sens, and the cathode gas flow rate Q c_sens as shown in Expression (9).
- P sat — t is calculated.
- the target cooling water temperature conversion unit 232 calculates the target cooling water temperature T t based on the target saturated water vapor pressure P sat — t as shown in Expression (10), and sets the target cooling water temperature T t as the stack target temperature. Output.
- step S9 when the moisture of the electrolyte membrane 111 is reduced by a signal related to the wet state of the electrolyte membrane 111, the flow rate of the fuel is decreased and the electrolyte membrane 111 is reduced as compared with the case of increasing the moisture of the electrolyte membrane 111.
- a power generation control step for increasing the temperature of the oxidant in accordance with a signal indicating the wet state of the battery is configured.
- step S10 the controller 200 controls the rotation speed of the anode circulation pump 36 based on the anode gas target flow rate, and controls the rotation speed of the cooling water pump 42 based on the stack target temperature. That is, step S10 constitutes a flow rate adjusting step for adjusting the flow rate of the fuel supplied to the fuel cell 10 and a temperature adjusting step for adjusting the temperature of the oxidant supplied to the fuel cell 10.
- step S6 If the wet operation is performed in step S6, the controller 200 proceeds to the process of step S11.
- step S11 when it is determined that the wet operation is performed, the controller 200 calculates the temperature of the fuel cell stack 1.
- the controller 200 acquires the stack inlet water temperature from the inlet water temperature sensor 46, acquires the stack outlet temperature from the outlet water temperature sensor 47, and calculates the average value of the stack inlet water temperature and the stack outlet water temperature as the stack temperature. .
- step S12 when it is determined that the dry operation is performed, the controller 200 determines the anode gas target flow rate based on the stack temperature, the target water balance, the cathode gas flow rate, and the cathode gas pressure calculated in step S11. Calculate. Then, each process of step S9 and step S10 is performed sequentially, and the control method of the fuel cell system 100 is complete
- FIG. 12 is a time chart showing changes in the operating state of the fuel cell system 100 during the dry operation in the present embodiment.
- FIG. 12 (A) is a flowchart showing a change in the target water balance to compensate for excess or deficiency of moisture in the fuel cell stack 1.
- the target water balance increases or decreases within a predetermined range so that the wetness of the electrolyte membrane 111 is maintained at the target value.
- FIG. 12B is a flowchart showing changes in the flow rate of the anode gas supplied to the fuel cell stack 1.
- FIG. 12C is a flowchart showing a change in the temperature of the cooling water circulating through the fuel cell stack 1. When the temperature of the cooling water rises, the temperature of the cathode gas passing through the fuel cell stack 1 rises and the stack temperature rises.
- FIG. 12 (D) is a flowchart showing a change in circulating storage water in the anode gas circulating through the fuel cell stack 1.
- the circulating storage water is the amount of water vapor stored in the anode gas circulation path from the ejector 34 through the fuel cell stack 1 to the suction port of the ejector 34.
- the horizontal axis of each figure from FIG. 12 (A) to FIG. 12 (D) is a common time axis.
- the priority control unit 201A determines that the dry operation is executed by the power generation control unit 202, and the priority control unit 201A sets the minimum stack temperature as the cathode gas temperature in the anode gas target flow rate calculation unit 220.
- the anode gas target flow rate calculation unit 220 calculates the anode gas wetting request flow rate based on the target water balance and the minimum stack temperature. Here, since the anode gas wetting request flow rate is larger than the load request flow rate, the anode gas target flow rate calculation unit 220 outputs the anode gas wetting request flow rate as the anode gas target flow rate.
- the decrease amount per unit time of the anode gas target flow rate that is, the decrease rate is compared with the decrease rate of the anode gas target flow rate when the actual stack temperature is used. growing. Thereby, the rotational speed of the anode circulation pump 36 is lowered, and the flow rate of the anode gas passing through the fuel cell stack 1 is lowered. Along with this, the amount of water vapor mixed in the anode gas decreases, so that the circulating storage water decreases as shown in FIG.
- the stack target temperature calculation unit 230 calculates the stack target temperature based on the anode gas wetting request flow rate and the target water balance. As described above, the anode gas wetting request flow rate is set to a small value as the target water balance decreases, so that the stack target temperature is kept constant without increasing.
- the anode gas flow rate is decreased so as to follow the decrease in the target water balance, so that an increase in stack temperature can be suppressed.
- the stack target temperature calculation unit 230 increases the stack target temperature in accordance with the decrease in the target water balance.
- the dry operation for reducing the anode gas flow rate by the anode circulation pump 36 is limited
- the dry operation for increasing the cathode gas temperature by the cooling water pump 42 is executed. That is, in the dry operation, the controller 200 executes the reduction control for reducing the anode gas flow rate by the anode circulation pump 36 in preference to the temperature increase control for increasing the cathode gas temperature by the cooling water pump 42.
- FIG. 13 is a time chart showing a change in the operating state of the fuel cell system when the temperature increase control of the cathode gas temperature is executed prior to the decrease control of the anode gas flow rate as a comparative example.
- the fuel cell system 100 includes an anode gas supply / discharge device 3 as fuel supply means for supplying fuel (anode gas) to the electrolyte membrane 111 of the fuel cell 10, and the electrolyte membrane 111. And a cathode gas supply / discharge device 2 as an oxidant supply means for supplying an oxidant (cathode gas).
- the fuel cell system 100 includes a controller 200 as power generation control means for controlling power generation of the fuel cell 10 by controlling supply of an oxidant by the cathode gas supply / discharge device 2 and fuel supply by the anode gas supply / discharge device 3. .
- the fuel cell system 100 includes an impedance measuring device 6 as a wet state detecting unit that detects a wet state of the electrolyte membrane 111 and an anode circulation pump as a flow rate adjusting unit that adjusts the flow rate of the fuel supplied to the fuel cell 10. 36 and a stack cooling device 4 as temperature adjusting means for adjusting the temperature of the oxidant supplied to the fuel cell 10.
- an impedance measuring device 6 as a wet state detecting unit that detects a wet state of the electrolyte membrane 111 and an anode circulation pump as a flow rate adjusting unit that adjusts the flow rate of the fuel supplied to the fuel cell 10.
- 36 and a stack cooling device 4 as temperature adjusting means for adjusting the temperature of the oxidant supplied to the fuel cell 10.
- the fuel cell system 100 is controlled by the controller 200. Whether the controller 200 acquires a signal related to the wetness of the electrolyte membrane 111 from the impedance measuring device 6 and executes a dry operation or a wet operation to reduce excess moisture of the electrolyte membrane 111 using the acquired signal. Judging.
- the controller 200 When executing the dry operation, the controller 200 reduces the flow rate of the fuel supplied to the fuel cell 10 as compared with the case where the wet operation is performed, and the fuel according to the signal from the impedance measuring device 6. The temperature of the oxidant flowing through the battery 10 is increased.
- the controller 200 when performing a dry operation for reducing the wetness of the electrolyte membrane 111, the controller 200 reduces the anode gas flow rate while the wetness of the electrolyte membrane 111 does not fall to the target value for maintaining the power generation performance. Then, the temperature of the fuel cell 10 is raised using the stack cooling device 4.
- the controller 200 decreases the anode gas flow rate and increases the temperature of the fuel cell 10. .
- the controller 200 reduces the flow rate of the anode gas supplied to the fuel cell 10 and reduces the flow rate of the electrolyte membrane 111 in accordance with the wetness of the electrolyte membrane 111 when the moisture content of the electrolyte membrane 111 is reduced. Increase the cathode gas temperature.
- the temperature of the fuel cell 10 can be suppressed from increasing and the moisture in the anode gas can be suppressed, so that it is necessary to reduce excess moisture in the electrolyte membrane 111. Time can be shortened. Therefore, the wet state of the fuel cell 10 can be controlled efficiently.
- the controller 200 increases the rotational speed of the compressor 22 in order to increase the cathode gas flow rate compared to the wet operation. For this reason, if dry operation becomes long, the power consumption of the compressor 22 will increase.
- the wasteful operation shown in FIG. 13 can be reduced, and excess water in the electrolyte membrane 111 can be reduced, so that an increase in power consumption of the fuel cell system 100 can be suppressed, The wet state of the fuel cell 10 can be controlled efficiently.
- the controller 200 when the controller 200 executes the dry operation, the controller 200 performs the reduction control for reducing the flow rate of the anode gas by the anode circulation pump 36 than the temperature increase control for increasing the temperature of the cathode gas by the cooling water pump 42. Priority is also given to execution.
- the time required for the dry operation can be shortened as described above. Further, since the rotation speed of the anode circulation pump 36 is lowered first, the power consumption of the anode circulation pump 36 is compared with the case where the rotation speed of the cooling water pump 42 is lowered first as shown in FIG. Can be reduced.
- the controller 200 reduces the target water balance corresponding to the difference between the measured HFR and the target HFR correlated with the wetness of the electrolyte membrane 111 while decreasing the anode gas flow rate. Raise the stack temperature to converge.
- the power generation control unit 202 decreases the anode gas flow rate and raises the temperature of the cathode gas so that the difference between the wetness of the electrolyte membrane 111 and the target value becomes small.
- the controller 200 includes a priority control unit 201A, an anode gas target flow rate calculation unit 220, and a stack target temperature calculation unit 230.
- the priority control unit 201A sets the order of controlling the operation of the cooling water pump 42 and the operation of the anode circulation pump 36. When executing the dry operation, the priority control unit 201A sets the operation order of the anode circulation pump 36 to be higher than the operation order of the cooling water pump 42, and prioritizes the operation of the cooling water pump 42. Make it work.
- the priority control unit 201 ⁇ / b> A sets the minimum stack temperature set when the moisture of the electrolyte membrane 111 is increased to the upper limit by the wet operation as the anode gas target of the fuel cell 10.
- the flow rate calculation unit 220 is set.
- the anode gas target flow rate calculation unit 220 reduces the anode gas flow rate based on the minimum stack temperature and the target water balance based on the measured HFR.
- the stack target temperature calculation unit 230 controls the temperature of the fuel cell stack 1 based on the anode gas target flow rate and the target water balance for wetness control.
- the anode gas target flow rate calculation unit 220 when performing a dry operation, the anode gas supplied to the fuel cell 10 based on the temperature lower than the temperature of the fuel cell 10 and the wetness of the electrolyte membrane 111. Reduce the flow rate.
- the stack target temperature calculation unit 230 controls the temperature of the fuel cell 10 based on the target flow rate of the anode gas and the wetness of the electrolyte membrane 111.
- the anode gas target flow rate calculation unit 220 decreases the anode gas target flow rate for wet control as the stack temperature decreases.
- the stack target temperature calculation unit 230 increases the stack target temperature as the anode gas target flow rate decreases, as described in FIG.
- the stack temperature at the time of the wet operation (low temperature control) is input to the anode gas target flow rate calculation unit 220. Therefore, in the anode gas target flow rate calculation unit 220, the stack target temperature calculation unit 230 It is recognized that a wet operation is being performed instead of a dry operation. For this reason, the anode gas target flow rate calculation unit 220 further increases the amount of decrease in the anode gas flow rate per unit time as compared with the case where the current stack temperature is higher than the stack temperature during the wet operation. On the other hand, since the anode gas target flow rate for wetting control is input to the stack target temperature calculation unit 230, the anode gas target flow rate calculation unit 220 increases the stack temperature as usual.
- the controller 200 can execute the weight reduction control for reducing the anode gas flow rate in preference to the temperature increase control for increasing the stack temperature. For this reason, the time required for the dry operation can be shortened.
- the priority control unit 201A sets the minimum stack temperature to a predetermined lower limit value within a range in which the stack cooling device 4 can adjust the stack temperature.
- the controller 200 can maximize the decrease rate of the flow rate of the anode gas supplied to the fuel cell stack 1 within a range in which the fuel cell stack 1 can be stably controlled. For this reason, the time required for the dry operation can be further shortened.
- the anode gas target flow rate calculation unit 220 measures the rate of decrease of the anode gas flow rate for the temperature of the fuel cell stack 1 instead of the minimum stack temperature when performing a dry operation. Increase compared to the rate of decrease when the value is used. Then, the stack target temperature calculation unit 230 lowers the stack target temperature as the anode gas target flow rate for wet control decreases, and increases the stack target temperature as the wetness of the electrolyte membrane 111 increases.
- the stack target temperature calculation unit 230 can supplement the dry operation by the anode gas target flow rate calculation unit 220 while suppressing unnecessary temperature increase control.
- the anode gas supply / discharge device 3 is provided in the anode gas circulation passage 35 for circulating the anode gas discharged from the fuel cell 10 to the fuel cell 10 and the anode gas circulation passage 35.
- an anode circulation pump 36 that adjusts the circulation flow rate of the anode gas that is circulated to the engine 10.
- the wetness of the electrolyte membrane 111 is likely to be increased by the moisture contained in the anode gas as the circulation flow rate of the anode gas is increased.
- the controller 200 when performing the dry operation, the controller 200 reduces the circulation flow rate of the anode gas, thereby reducing the anode gas in the anode gas that circulates through the fuel cell 10 via the anode gas circulation passage 35. Moisture can be reduced.
- the controller 200 increases the stack temperature after reducing the circulation flow rate of the anode gas. As a result, the moisture in the fuel cell stack 1 is reduced and then the stack temperature is raised, so that the dry operation can be executed efficiently while suppressing the humidification of the electrolyte membrane 111 due to the moisture in the anode gas. .
- the fuel cell 10 includes the cathode gas passage 131 that allows the cathode gas to pass through one surface of the electrolyte membrane 111 and the other surface of the electrolyte membrane 111. And an anode gas passage 121 for passing the anode gas in a direction opposite to the direction of the cathode gas flowing through the cathode gas passage 131. Further, the fuel cell 10 is formed between the upper surface of the cathode gas channel 131, that is, between the anode gas channel 121 and the cathode gas channel 131, and a cooling water flow through which cooling water (refrigerant) for cooling the fuel cell 10 is passed. Path 141 is included.
- the stack cooling device 4 supplies cooling water to the cooling water flow channel 141 in the same direction as the cathode gas flowing through the cathode gas flow channel 131, and the anode gas supply / discharge device 3 is discharged from one end of the anode gas flow channel 121.
- the anode gas is circulated to the other end of the anode gas passage 121.
- the temperature of the cathode gas on the downstream side becomes higher than the temperature of the cathode gas on the upstream side of the cathode gas channel 131 due to the cooling water passing through the cooling water channel 141. Further, as the cathode gas flows from the upstream to the downstream of the cathode gas channel 131, the moisture of the cathode gas increases. For this reason, the cathode gas on the downstream side of the cathode gas flow channel 131 contains a larger amount of water vapor than the cathode gas on the upstream side.
- the water vapor on the downstream side of the cathode gas channel 131 passes through the electrolyte membrane 111 and is mixed into the anode gas on the upstream side of the anode gas channel 121.
- the anode gas upstream of the anode gas flow path 121 contains water vapor.
- the water vapor in the anode gas permeates the electrolyte membrane 111 and returns to the anode gas upstream of the cathode gas passage 131.
- the water vapor accompanying power generation circulates in the fuel cell 10.
- the impedance measuring device 6 detects the impedance of the fuel cell 10 and outputs the detected signal to the controller 200 as a parameter correlated with the wetness of the electrolyte membrane 111.
- the membrane wet state detection unit 201 calculates a target water balance correlated with the wetness of the electrolyte membrane 111 based on the impedance. Thereby, the power generation control unit 202 can accurately execute a dry operation for reducing the wetness of the electrolyte membrane 111.
- the stack target temperature is calculated using the required anode gas wetting flow rate.
- the load request flow rate is selected as the anode gas target flow rate
- the anode gas wetting request flow rate and the actual anode gas flow rate may greatly deviate, and extra time may be required for the dry operation. .
- the second embodiment of the present invention an example of a fuel cell system in which the difference between the target value of the anode gas flow rate used for calculating the stack target temperature and the anode gas flow rate supplied to the fuel cell stack 1 is reduced will be described.
- the configuration of the fuel cell system according to the present embodiment is the same as the configuration of the fuel cell system 100 shown in FIG.
- FIG. 14 is a block diagram showing an example of the configuration of the power generation control unit 202A in the second embodiment of the present invention.
- the power generation control unit 202A calculates the stack target temperature using the estimated value of the anode gas flow rate instead of the anode gas wetting request flow rate.
- the power generation control unit 202A includes an anode gas flow rate estimation unit 240. Since other configurations are the same as those in the first embodiment, the same reference numerals are given and description thereof is omitted here.
- the anode gas flow rate estimation unit 240 estimates the anode gas flow rate supplied to the fuel cell stack 1.
- the anode gas flow rate estimation unit 240 estimates the anode gas flow rate based on the operating state of the anode gas supply / discharge device 3.
- a flow rate estimation map showing the relationship between the rotation speed of the anode circulation pump 36 and the anode gas flow rate is recorded in advance in the anode gas flow rate estimation unit 240. Details of the flow rate estimation map will be described later with reference to FIG.
- the anode gas flow rate estimation unit 240 acquires the rotation speed of the anode circulation pump 36 from, for example, a rotation speed sensor provided in the anode circulation pump 36.
- the anode gas flow rate estimation unit 240 calculates the anode gas flow rate related to the acquired rotation speed with reference to the flow rate estimation map.
- the anode gas flow rate estimation unit 240 outputs the calculated anode gas flow rate to the stack target temperature calculation unit 230.
- the anode gas flow rate estimation unit 240 sets the estimated value of the anode gas flow rate in the stack target temperature calculation unit 230 instead of the anode gas wetting request flow rate. As a result, the stack target temperature corresponding to the actual anode gas flow rate is calculated, so that the dry operation based on the anode gas flow rate can be appropriately supplemented by controlling the stack temperature.
- the anode gas flow rate estimation unit 240 may be provided in the priority control unit 201 illustrated in FIG.
- FIG. 15 is a diagram illustrating an example of a flow rate estimation map set in the anode gas flow rate estimation unit 240.
- the horizontal axis represents the rotational speed of the anode circulation pump 36
- the vertical axis represents the anode gas flow rate.
- the anode gas flow rate increases as the rotation speed of the anode circulation pump 36 increases.
- the stack target temperature calculation unit 230 the stack target temperature is calculated using the anode gas flow rate [NL / min] in the standard state.
- NL Normal Liter indicates liters in a standard state.
- the anode gas flow rate estimation unit 240 converts the anode gas flow rate Q [L / min] calculated by the flow rate estimation map shown in FIG. 15 into the anode gas flow rate Q 0 [NL / min] in the standard state.
- the anode gas flow rate estimation unit 240 acquires the anode gas pressure P from the pressure sensor 37 and acquires the stack inlet water temperature T from the inlet water temperature sensor 46. Then, the anode gas flow rate estimation unit 240 calculates the anode gas flow rate Q 0 in the standard state based on the anode gas flow rate Q, the anode gas pressure P, and the stack inlet water temperature T as shown in the following equation (11).
- the anode gas flow rate estimation unit 240 outputs the anode gas flow rate Q 0 in the standard state to the stack target temperature calculation unit 230. Then, the stack target temperature calculation unit 230 substitutes the anode gas flow rate Q 0 in the standard state for the anode gas wetting request flow rate Q a_rw in Equation (8).
- FIG. 16 is a flowchart showing an example of a control method of the fuel cell system 100 in the present embodiment.
- step S20 is added after the processes of step S8 and step S12. Therefore, only the process of step S20 will be described below.
- step S20 the anode gas flow rate estimation unit 240 estimates the flow rate of the anode gas circulating through the fuel cell stack 1 based on the rotation speed of the anode circulation pump 36.
- the anode gas flow rate estimation unit 240 when the anode gas flow rate estimation unit 240 acquires the rotation speed of the anode circulation pump 36, the anode gas flow rate estimation unit 240 refers to the flow rate estimation map illustrated in FIG. 15 and calculates the anode gas flow rate related to the acquired rotation speed. calculate.
- the anode gas flow rate estimation unit 240 converts the calculated anode gas flow rate Q into the standard anode gas flow rate Q 0 as shown in equation (11).
- step S9 the stack target temperature calculation unit 230 calculates the anode / cathode flow rate ratio K ac using the anode gas flow rate Q 0 instead of the anode gas wetting request flow rate Q a_rw in the equation (8).
- the stack target temperature calculation unit 230 calculates the stack target temperature Tt based on the calculated anode / cathode flow rate ratio K ac .
- FIG. 17 is a time chart showing changes in the operating state of the fuel cell system 100 in the present embodiment.
- the vertical axis of each figure from FIG. 17 (A) to FIG. 17 (D) is the same as the vertical axis of each figure from FIG. 12 (A) to FIG. 12 (D). It is a common time axis.
- the change in the operation state of the fuel cell system 100 according to the present embodiment is indicated by a solid line
- the change in the operation state of the fuel cell system 100 according to the first embodiment shown in FIG. 12 is indicated by a broken line.
- the target water balance is switched from rising to lowering, and the dry operation is started.
- the output value of the anode gas load request flow rate calculation unit 221 shown in FIG. 8 is larger than a predetermined lower limit value of the anode gas wetting request flow rate.
- the anode gas target flow rate is limited by the load request flow rate.
- the difference between the actual anode gas flow rate and the required anode gas wetting flow rate increases.
- the required anode gas wetting flow rate is input to the stack target temperature calculation unit 230. Therefore, even if the difference between the actual anode gas flow rate and the required anode gas wetting flow rate increases, FIG. As shown by the broken line, the temperature of the cooling water does not rise.
- the anode gas flow rate estimation unit 240 estimates the anode gas flow rate based on the rotation speed of the anode circulation pump 36 and outputs the estimated value to the stack target temperature calculation unit 230.
- the target stack temperature is calculated using the estimated value of the anode gas flow rate, even if the reduction control of the anode gas flow rate is restricted due to some requirement, the stack target temperature is reduced according to the decrease in the target water balance.
- the target temperature can be raised.
- the power generation control unit 202A is configured so that the target water balance is reduced according to the actual anode gas flow rate even in a state where the actual anode gas flow rate and the anode gas wetting request flow rate are different.
- Stack temperature can be increased. That is, even when the wetness of the electrolyte membrane 111 is not fully adjusted by the reduction control for reducing the anode gas flow rate, the temperature increase control for increasing the stack temperature is executed. Can be complemented.
- FIG. 18 is a flowchart showing a change in the operating state of the fuel cell system 100 when the target water balance falls in a pulse shape.
- the vertical axis of each figure from FIG. 18 (A) to FIG. 18 (D) is the same as the vertical axis of each figure from FIG. 17 (A) to FIG. 17 (D). It is a common time axis.
- the anode gas flow rate is indicated by a solid line, and the anode gas target flow rate is indicated by a broken line. Even if the anode gas flow rate changes steeply, the estimated value of the anode gas flow rate output from the anode gas flow rate estimation unit 240 is substantially the same value as the actual anode gas flow rate.
- the target water balance quickly decreases as shown in FIG.
- the anode gas target flow rate calculation unit 220 calculates an anode gas target flow rate that can achieve the target water balance.
- the anode gas flow rate decreases with a delay from the target value due to a response delay of the anode circulation pump 36 and the like.
- the stack target temperature calculation unit 230 increases the stack target temperature by the difference between the estimated value of the anode gas flow rate and the target value, so that the temperature of the cooling water rises transiently as shown in FIG. .
- the circulating storage water increases transiently as shown in FIG.
- the stack target temperature calculation unit 230 lowers the stack target temperature by the amount that has been increased transiently, so that the temperature of the coolant that has risen transiently decreases as shown in FIG. As a result, as shown in FIG. 18D, the circulating storage water is lowered.
- the anode gas flow rate is reduced to the target value as shown in FIG. 18 (B), and accordingly, the temperature of the cooling water is lowered as shown in FIG. 18 (C) to reach a steady state.
- the power generation control unit 202A executes the stack temperature increase control by the delay amount because the amount reduction control by the anode circulation pump 36 is delayed. . That is, when executing the transient dry operation, the power generation control unit 202A reduces the anode gas flow rate and reduces the difference between the wetness of the electrolyte membrane 111 and the target value for maintaining the power generation performance. Increase the temperature of the cathode gas.
- the temperature rise control for increasing the temperature of the cathode gas is executed so as to complement the weight loss control for reducing the anode gas flow rate, so that the efficiency and early can be achieved.
- moisture in the electrolyte membrane 111 can be reduced.
- the power generation control unit 202A decreases the stack temperature as the anode gas flow rate approaches the target value. Thereby, the circulating storage water is reduced, and the wetness of the electrolyte membrane 111 is likely to be lowered, so that the dry operation can be performed efficiently.
- FIG. 19 is a flowchart showing a change in the operating state of the fuel cell system 100 when the target water balance has a large decrease in comparison with FIG.
- the target water balance sharply decreases as in FIG.
- the amount of decrease in the target water balance is larger than that in FIG. 18A, as shown in FIG.
- the reduction range of the target water balance is large, the reduction range of the anode gas target flow rate is also large as shown in FIG. 19 (A). As a result, the amount of circulating storage water decreases.
- the temperature of the cooling water can be increased while reducing the circulating storage water, so that the target water balance can be achieved quickly.
- the power generation control unit 202A reduces the anode gas flow rate.
- stack temperature increase control is started. That is, the power generation control unit 202A raises the stack temperature before the flow rate of the anode gas reaches the lower limit value determined by the wet control.
- the power generation control unit 202A when the degree of decrease in the wetness of the electrolyte membrane 111 exceeds a predetermined value, reduces the anode gas flow rate by the anode circulation pump 36, and raises the temperature of the cathode gas. Are executed in parallel. Thereby, it is possible to efficiently perform the dry operation while shifting the wetness of the electrolyte membrane 111 to a state in which the electrolyte membrane 111 is easily lowered.
- a flow sensor may be provided in the anode gas supply passage 32 downstream of the ejector 34, and a detection signal of the flow sensor may be input to the stack target temperature calculation unit 230. Thereby, a more accurate dry operation can be executed.
- the anode gas target flow rate calculation unit 220 performs a dry operation at a temperature lower than the temperature of the fuel cell 10 and the wetness of the electrolyte membrane 111, as in the first embodiment.
- the anode gas flow rate is reduced based on the measured HFR correlated with the.
- the anode gas flow rate estimation unit 240 is based on the rotational speed of the anode circulation pump 36 and the anode gas pressure detected by the pressure sensor 37, and the fuel cell.
- the anode gas flow rate circulating through the stack 1 is estimated.
- the stack target temperature calculation unit 230 uses the estimated value of the anode gas flow rate instead of the anode gas wetting request flow rate shown in FIG. 4 so that the difference between the measured HFR and the target HFR becomes small. Increase temperature.
- the stack target temperature calculation unit 230 The stack temperature can be controlled based on the equivalent value.
- the stack temperature can be raised according to the difference between the estimated value of the anode gas flow rate and the target value for the wet control (anode gas wetting required flow rate) according to the target water balance. it can.
- the anode gas flow rate estimation unit 240 sets the estimated value of the anode gas flow rate by setting the estimated value of the anode gas flow rate in the stack target temperature calculation unit 230 instead of the required flow rate of the anode gas wetting in the dry operation during the transition.
- the anode circulation pump 36 and the cooling water pump 42 can be operated simultaneously according to the difference between the target value and the target value.
- the anode gas flow rate estimation unit 240 constitutes a priority control unit that sets the operation order of the anode circulation pump 36 and the operation order of the cooling water pump 42 equally in the dry operation during the transition. Thereby, in the dry operation at the time of transition, the operation of the anode circulation pump 36 and the cooling water pump 42 can be performed without waiting for the operation of the anode circulation pump 36 according to the difference between the estimated value of the anode gas flow rate and the target value. Can be operated in parallel.
- the stack target temperature calculation unit 230 can increase the stack temperature in accordance with the actual decrease amount of the anode gas flow rate, so that the dry operation can be executed more efficiently than in the first embodiment.
- the time required for the dry operation can be shortened.
- FIG. 20 is a block diagram showing an example of the configuration of the impedance measuring device 6.
- the impedance measuring device 6 is connected to the intermediate terminal 1C in addition to the positive electrode terminal (cathode electrode side terminal) 1B and the negative electrode terminal (anode electrode side terminal) 1A of the fuel cell stack 1. The portion connected to the midway terminal 1C is grounded.
- the impedance measuring device 6 includes a positive side voltage measurement sensor 61 that measures the positive side AC potential difference V1 of the positive terminal 1B with respect to the midway terminal 1C, and a negative side voltage measurement that measures the negative side AC potential difference V2 of the negative terminal 1A with respect to the midway terminal 1C. Sensor 62.
- the impedance measuring device 6 applies an alternating current I2 to a positive side AC power supply unit 63 that applies an alternating current I1 to a circuit that includes the positive terminal 1B and the intermediate terminal 1C, and a circuit that includes the negative terminal 1A and the intermediate terminal 1C.
- the controller 65 Based on the negative electrode side AC power supply unit 64, the controller 65 that adjusts the amplitude and phase of the AC current I1 and the AC current I2, and the positive side AC potential differences V1 and V2 and the AC currents I1 and I2, the inside of the fuel cell stack 1 And an impedance calculation unit 66 for calculating the impedance Z.
- the controller 65 adjusts the amplitude and phase of the alternating current I1 and the alternating current I2 so that the positive side AC potential difference V1 and the negative side AC potential difference V2 are equal.
- the impedance calculation unit 66 includes hardware such as an AD converter and a microcomputer chip (not shown) and a software configuration such as a program for calculating impedance.
- the impedance calculator 66 calculates the internal impedance Z1 from the halfway terminal 1C to the positive terminal 1B by dividing the positive side AC potential difference V1 by the AC current I1, and divides the negative side AC potential difference V2 by the AC current I2. An internal impedance Z2 from the midway terminal 1C to the negative electrode terminal 1A is calculated. Further, the impedance calculator 66 calculates the total impedance Z of the fuel cell stack 1 by taking the sum of the internal impedance Z1 and the internal impedance Z2.
- the impedance measuring device 6 is connected to the fuel cell stack 1 and outputs AC currents I 1 and I 2 to the fuel cell stack 1, and the positive electrode of the fuel cell stack 1.
- the positive side AC potential difference V1 which is a potential difference obtained by subtracting the potential of the middle portion 1C from the potential of the side 1B
- the negative polarity which is a potential difference obtained by subtracting the potential of the middle portion 1C from the potential of the negative side 1A of the fuel cell stack 1.
- the controller 65 as an AC adjusting unit that adjusts the AC currents I1 and I2 based on the side AC potential difference V2, and the fuel based on the adjusted AC currents I1 and I2, the positive side AC potential difference V1, and the negative side AC potential difference V2
- the controller 65 is configured so that the positive-side AC potential difference V1 on the positive side of the fuel cell stack 1 and the negative-side AC potential difference V2 on the negative side substantially coincide with the alternating current I1 and the negative electrode applied by the positive-side AC power supply unit 63.
- the amplitude and phase of the alternating current I2 applied by the side alternating-current power supply unit 64 are adjusted.
- the amplitude of the positive-side AC potential difference V1 is equal to the amplitude of the negative-side AC potential difference V2, so that the positive terminal 1B and the negative terminal 1A are substantially equipotential (hereinafter, this is referred to as equipotential control). ). Therefore, since the alternating currents I1 and I2 for impedance measurement are prevented from flowing to the load device 5, the power generation by the fuel cell 10 is prevented from being affected.
- the measurement AC potential is superimposed on the voltage generated by the power generation, so that the positive side AC potential difference V1 and the negative side AC potential difference V2 themselves increase.
- the phases and amplitudes of the positive-side AC potential difference V1 and the negative-side AC potential difference V2 do not change, high-precision impedance measurement can be performed as in the case where the fuel cell 10 is not in the power generation state.
- an alternating current may be supplied to the fuel cell stack 1 from a predetermined current source, an output alternating voltage may be measured, and an impedance may be calculated based on the alternating current and the output alternating voltage.
- the power generation control unit 202 calculates the anode gas target flow rate and the stack target temperature using the measured values of the cathode gas flow rate and pressure, but the anode gas is calculated using the average values of the cathode gas flow rate and pressure.
- the target flow rate and the stack target temperature may be calculated.
- the membrane wet state detection unit 201 calculates the target water balance and outputs the target water balance to both the anode gas target flow rate calculation unit 220 and the stack target temperature calculation unit 230.
- the unit 201 may calculate the target discharge amount based on the target water balance, and output the target discharge amount to both instead of the target water balance.
- the priority control unit 201A is provided in the film wet state detection unit 201.
- the priority control unit 201A may be provided in the power generation control unit 202.
- the cathode gas flow rate estimating unit 240 is provided in the power generation control unit 202A.
- the cathode gas flow rate estimating unit 240 may be provided in the priority control unit 201A.
- the controller 200 may execute the following wetting control.
- the controller 200 determines whether or not to perform the dry operation based on the target water balance (target drainage amount). For example, the controller 200 determines whether or not the target water balance is smaller than a predetermined threshold (for example, zero), and executes the dry operation when the target water balance is smaller than the predetermined threshold.
- a predetermined threshold for example, zero
- the controller 200 decreases the anode gas flow rate to a predetermined lower limit flow rate by the reduction control, and then increases the cooling water flow rate to the predetermined upper limit flow rate by the temperature increase control to increase the temperature of the cathode gas. Raise. Even with such simple control, the dry operation can be completed early.
Abstract
Description
燃料電池は、燃料極としてのアノード電極と、酸化剤極としてのカソード電極と、これら電極に挟まれるように配置される電解質膜と、から構成されている。燃料電池のアノード電極には、燃料として、水素を含有するアノードガスが供給される。燃料電池のカソード電極には、酸化剤として、酸素を含有するカソードガスが供給される。
カソード電極: 4H++4e-+O2 → 2H2O ・・・(2)
これら(1)(2)の電極反応によって、燃料電池は1V(ボルト)程度の起電力を生じる。
なお、本実施形態ではアノードガス湿潤要求流量を用いてスタック目標温度を算出した。このような算出手法では、アノードガス目標流量として負荷要求流量が選択されているときには、アノードガス湿潤要求流量と実際のアノードガス流量とが大きく乖離してドライ操作に余計な時間を要する場合がある。
Claims (11)
- 燃料電池の電解質膜に燃料を供給する燃料供給手段と、前記電解質膜に酸化剤を供給する酸化剤供給手段と、前記酸化剤供給手段による酸化剤の供給と前記燃料供給手段による燃料の供給とを制御して前記燃料電池の発電を制御する発電制御手段と、を備えた燃料電池システムにおいて、
前記電解質膜の湿潤状態を検出する湿潤状態検出手段と、
前記燃料供給手段により前記燃料電池に供給される燃料の流量を調整する流量調整手段と、
前記酸化剤供給手段により前記燃料電池に供給される酸化剤の温度を調整する温度調整手段と、を含み、
前記発電制御手段は、前記湿潤状態検出手段から出力される信号により前記電解質膜の水分を減らすときには、前記電解質膜の水分を増やすときに比べて、前記燃料の流量を減少させるとともに、前記湿潤状態検出手段からの信号に応じて前記酸化剤の温度を上昇させる、
ことを特徴とする燃料電池システム。 - 請求項1に記載の燃料電池システムであって、
前記発電制御手段は、前記電解質膜の水分を減らすときには、前記流量調整手段による前記燃料の流量を減らす制御を、前記温度調整手段による前記酸化剤の温度を高くする制御よりも優先して実行する、
燃料電池システム。 - 請求項1又は請求項2に記載の燃料電池システムであって、
前記発電制御手段は、前記電解質膜の水分を減らすときには、前記燃料の流量を減少させるとともに、前記湿潤状態検出手段からの信号により前記電解質膜の湿潤度と目標値との差分が小さくなるように前記酸化剤の温度を上昇させる、
燃料電池システム。 - 請求項3に記載の燃料電池システムであって、
前記温度調整手段は、前記燃料電池に冷媒を供給する冷却装置を含み、
前記発電制御手段は、
前記温度調整手段の動作と前記流量調整手段の動作とを制御する順位を設定する優先制御部と、
前記燃料電池の温度と前記電解質膜の湿潤度とに基づいて、前記燃料電池に供給される燃料の流量を減少させる流量演算部と、
前記燃料の流量と前記電解質膜の湿潤度とに基づいて、前記燃料電池の温度を制御する温度演算部と、を含み、
前記優先制御部は、前記電解質膜の水分を減らすドライ操作を実行する場合には、前記燃料電池の温度よりも低いウェット操作時の温度を前記燃料電池の温度として前記流量演算部に設定する、
燃料電池システム。 - 請求項4に記載の燃料電池システムであって、
前記ウェット操作時の温度は、前記冷却装置が前記燃料電池の温度を調整できる範囲の下限値に設定される、
燃料電池システム。 - 請求項5に記載の燃料電池システムであって、
前記流量演算部は、前記ドライ操作を実行する場合には、前記燃料電池に供給される燃料の流量を減少させる減少速度を、前記ウェット操作時の温度の代わりに前記燃料電池の温度を用いたときの減少速度に比べて大きくし、
前記温度演算部は、前記燃料電池に供給される燃料の流量が減少するほど、前記燃料電池の温度を低下させ、かつ、前記電解質膜の湿潤度が大きくなるほど、前記燃料電池の温度を上昇させる、
燃料電池システム。 - 請求項1から請求項6までのいずれか1項に記載の燃料電池システムであって、
前記燃料供給手段は、
前記燃料電池から排出される燃料を前記燃料電池に循環させる循環通路と、
前記循環通路に設けられ、前記燃料電池に循環される燃料の循環流量を調整する循環ポンプと、を備え、
前記発電制御手段は、前記電解質膜の水分を減らすときには、前記燃料の循環流量を減らすことにより、前記循環通路を介して前記燃料電池を循環する燃料に含まれる水分を少なくする、
燃料電池システム。 - 請求項1から請求項7までのいずれか1項に記載の燃料電池システムであって、
前記燃料電池は、
当該燃料電池を冷却するための冷媒を通す冷媒流路と、
前記電解質膜の一方の面に対して酸化剤を通す酸化剤流路と、
前記電解質膜の他方の面に対して前記酸化剤通路に流れる酸化剤の向きとは反対の向きに燃料を通す燃料流路と、を含み、
前記温度調整手段は、前記冷媒流路に前記冷媒を供給し、
前記燃料供給手段は、前記燃料流路の一端から排出される燃料を前記燃料流路の他端に循環させる、
燃料電池システム。 - 請求項1から請求項6までのいずれか1項に記載の燃料電池システムであって、
前記湿潤状態検出手段は、前記燃料電池のインピーダンスを検出し、当該インピーダンスを前記電解質膜の湿潤度に関する信号として前記発電制御手段に出力する、
燃料電池システム。 - 請求項7に記載の燃料電池システムであって、
前記燃料電池は、積層電池により構成され、
前記湿潤状態検出手段は、前記積層電池のインピーダンスを測定する測定装置を含み、
前記測定装置は、
前記積層電池に接続されて該積層電池に交流電流を出力する交流電源部と、
前記積層電池の正極側の電位から該積層電池の中途部分の電位を引いて求めた電位差である正極側交流電位差と、前記燃料電池の負極側の電位から前記中途部分の電位を引いて求めた電位差である負極側交流電位差とに基づいて、交流電流を調整する交流調整部と、
前記調整された交流電流、前記正極側交流電位差及び前記負極側交流電位差に基づいて、前記燃料電池のインピーダンスを演算する演算部と、を含む、
燃料電池システム。 - 燃料電池の電解質膜に燃料を供給する燃料供給手段と、前記電解質膜に酸化剤を供給する酸化剤供給手段と、前記酸化剤供給手段による酸化剤の供給と前記燃料供給手段による燃料の供給とを制御して前記燃料電池の発電を制御する発電制御手段と、を備えた燃料電池システムの制御方法であって、
前記電解質膜の湿潤状態を検出する湿潤状態検出ステップと、
前記燃料供給手段により前記燃料電池に供給される燃料の流量を調整する流量調整ステップと、
前記酸化剤供給手段により前記燃料電池に供給される酸化剤の温度を調整する温度調整ステップと、を含み、
前記電解質膜の湿潤状態に関する信号により前記電解質膜の水分を減らすときには、前記電解質膜の水分を増やすときに比べて、前記燃料の流量を減少させるとともに、前記電解質膜の湿潤状態を示す信号に応じて前記酸化剤の温度を上昇させる発電制御ステップと、
を含むことを特徴とする燃料電池システムの制御方法。
Priority Applications (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US15/561,179 US10020523B2 (en) | 2015-03-27 | 2015-03-27 | Fuel cell system and control method for fuel cell system |
EP15887473.5A EP3276724B1 (en) | 2015-03-27 | 2015-03-27 | Fuel cell system and fuel cell system control method |
PCT/JP2015/059712 WO2016157320A1 (ja) | 2015-03-27 | 2015-03-27 | 燃料電池システム及び燃料電池システムの制御方法 |
KR1020177030402A KR101892889B1 (ko) | 2015-03-27 | 2015-03-27 | 연료 전지 시스템 및 연료 전지 시스템의 제어 방법 |
CN201580078391.1A CN107431226B (zh) | 2015-03-27 | 2015-03-27 | 燃料电池系统以及燃料电池系统的控制方法 |
CA2981161A CA2981161C (en) | 2015-03-27 | 2015-03-27 | Fuel cell system and control method for fuel cell system |
JP2017508851A JP6432675B2 (ja) | 2015-03-27 | 2015-03-27 | 燃料電池システム及び燃料電池システムの制御方法 |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/JP2015/059712 WO2016157320A1 (ja) | 2015-03-27 | 2015-03-27 | 燃料電池システム及び燃料電池システムの制御方法 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2016157320A1 true WO2016157320A1 (ja) | 2016-10-06 |
Family
ID=57005713
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2015/059712 WO2016157320A1 (ja) | 2015-03-27 | 2015-03-27 | 燃料電池システム及び燃料電池システムの制御方法 |
Country Status (7)
Country | Link |
---|---|
US (1) | US10020523B2 (ja) |
EP (1) | EP3276724B1 (ja) |
JP (1) | JP6432675B2 (ja) |
KR (1) | KR101892889B1 (ja) |
CN (1) | CN107431226B (ja) |
CA (1) | CA2981161C (ja) |
WO (1) | WO2016157320A1 (ja) |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2019102430A (ja) * | 2017-12-01 | 2019-06-24 | パナソニックIpマネジメント株式会社 | 燃料電池システム |
WO2019242189A1 (zh) * | 2018-06-21 | 2019-12-26 | 中山大洋电机股份有限公司 | 一种燃料电池及其控制方法 |
JP7132088B2 (ja) * | 2018-11-02 | 2022-09-06 | 株式会社Soken | 燃料電池システム |
CN113036188B (zh) * | 2021-05-25 | 2021-08-03 | 北京亿华通科技股份有限公司 | 一种燃料电池系统的控制方法 |
Citations (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2004165058A (ja) * | 2002-11-14 | 2004-06-10 | Nissan Motor Co Ltd | 燃料電池システムの制御装置 |
JP2005093111A (ja) * | 2003-09-12 | 2005-04-07 | Nissan Motor Co Ltd | 燃料電池システムの制御装置 |
WO2008056617A1 (fr) * | 2006-11-06 | 2008-05-15 | Toyota Jidosha Kabushiki Kaisha | Système de pile à combustible |
JP2009187689A (ja) * | 2008-02-04 | 2009-08-20 | Toyota Motor Corp | 燃料電池システム |
JP2009245826A (ja) * | 2008-03-31 | 2009-10-22 | Equos Research Co Ltd | 燃料電池スタック及び燃料電池システム |
JP2011014429A (ja) * | 2009-07-03 | 2011-01-20 | Toyota Motor Corp | 燃料電池システム |
JP2011028937A (ja) * | 2009-07-23 | 2011-02-10 | Nissan Motor Co Ltd | 燃料電池システム及び燃料電池システムの運転方法 |
JP2012109182A (ja) * | 2010-11-19 | 2012-06-07 | Nissan Motor Co Ltd | 燃料電池システム |
WO2012114432A1 (ja) * | 2011-02-21 | 2012-08-30 | トヨタ自動車株式会社 | 燃料電池 |
JP2014044846A (ja) * | 2012-08-27 | 2014-03-13 | Toyota Motor Corp | 燃料電池の制御方法および燃料電池システム |
WO2014057868A1 (ja) * | 2012-10-09 | 2014-04-17 | 日産自動車株式会社 | 積層電池のインピーダンス測定装置 |
WO2014141752A1 (ja) * | 2013-03-12 | 2014-09-18 | 日産自動車株式会社 | インピーダンス測定装置及びインピーダンス測定装置の制御方法 |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7862935B2 (en) * | 2005-05-17 | 2011-01-04 | Gm Global Technology Operations, Inc. | Management via dynamic water holdup estimator in a fuel cell |
JP2009259758A (ja) * | 2008-03-26 | 2009-11-05 | Toyota Motor Corp | 燃料電池システム及び燃料電池の運転方法 |
JP5156797B2 (ja) * | 2010-06-17 | 2013-03-06 | 本田技研工業株式会社 | 燃料電池システム |
CA2825935C (en) | 2011-03-01 | 2016-06-28 | Nissan Motor Co., Ltd. | Setting and control of target wet state in fuel cell system |
-
2015
- 2015-03-27 WO PCT/JP2015/059712 patent/WO2016157320A1/ja active Application Filing
- 2015-03-27 CA CA2981161A patent/CA2981161C/en active Active
- 2015-03-27 US US15/561,179 patent/US10020523B2/en active Active
- 2015-03-27 EP EP15887473.5A patent/EP3276724B1/en active Active
- 2015-03-27 KR KR1020177030402A patent/KR101892889B1/ko active IP Right Grant
- 2015-03-27 CN CN201580078391.1A patent/CN107431226B/zh active Active
- 2015-03-27 JP JP2017508851A patent/JP6432675B2/ja active Active
Patent Citations (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2004165058A (ja) * | 2002-11-14 | 2004-06-10 | Nissan Motor Co Ltd | 燃料電池システムの制御装置 |
JP2005093111A (ja) * | 2003-09-12 | 2005-04-07 | Nissan Motor Co Ltd | 燃料電池システムの制御装置 |
WO2008056617A1 (fr) * | 2006-11-06 | 2008-05-15 | Toyota Jidosha Kabushiki Kaisha | Système de pile à combustible |
JP2009187689A (ja) * | 2008-02-04 | 2009-08-20 | Toyota Motor Corp | 燃料電池システム |
JP2009245826A (ja) * | 2008-03-31 | 2009-10-22 | Equos Research Co Ltd | 燃料電池スタック及び燃料電池システム |
JP2011014429A (ja) * | 2009-07-03 | 2011-01-20 | Toyota Motor Corp | 燃料電池システム |
JP2011028937A (ja) * | 2009-07-23 | 2011-02-10 | Nissan Motor Co Ltd | 燃料電池システム及び燃料電池システムの運転方法 |
JP2012109182A (ja) * | 2010-11-19 | 2012-06-07 | Nissan Motor Co Ltd | 燃料電池システム |
WO2012114432A1 (ja) * | 2011-02-21 | 2012-08-30 | トヨタ自動車株式会社 | 燃料電池 |
JP2014044846A (ja) * | 2012-08-27 | 2014-03-13 | Toyota Motor Corp | 燃料電池の制御方法および燃料電池システム |
WO2014057868A1 (ja) * | 2012-10-09 | 2014-04-17 | 日産自動車株式会社 | 積層電池のインピーダンス測定装置 |
WO2014141752A1 (ja) * | 2013-03-12 | 2014-09-18 | 日産自動車株式会社 | インピーダンス測定装置及びインピーダンス測定装置の制御方法 |
Also Published As
Publication number | Publication date |
---|---|
US20180048003A1 (en) | 2018-02-15 |
KR20170125988A (ko) | 2017-11-15 |
CA2981161C (en) | 2018-07-17 |
EP3276724B1 (en) | 2019-03-06 |
JPWO2016157320A1 (ja) | 2018-02-01 |
KR101892889B1 (ko) | 2018-08-28 |
JP6432675B2 (ja) | 2018-12-05 |
US10020523B2 (en) | 2018-07-10 |
CN107431226B (zh) | 2019-06-21 |
CA2981161A1 (en) | 2016-10-06 |
CN107431226A (zh) | 2017-12-01 |
EP3276724A1 (en) | 2018-01-31 |
EP3276724A4 (en) | 2018-06-20 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
JP6477896B2 (ja) | 燃料電池システムの制御装置及び燃料電池システムの制御方法 | |
US10312537B2 (en) | Control method for fuel cell system and fuel cell system | |
CA2940020C (en) | Fuel cell system and control method for fuel cell system | |
JP5522309B2 (ja) | 燃料電池システム | |
JP6432675B2 (ja) | 燃料電池システム及び燃料電池システムの制御方法 | |
JP5812118B2 (ja) | 燃料電池システム | |
US10164275B2 (en) | Fuel cell system | |
JP6540407B2 (ja) | 燃料電池システムの湿潤制御装置及び湿潤制御方法 | |
JP6512047B2 (ja) | 燃料電池システムの湿潤制御装置及び湿潤制御方法 | |
JP6540408B2 (ja) | 燃料電池システムの湿潤制御装置及び湿潤制御方法 | |
WO2016125231A1 (ja) | 燃料電池システム及び燃料電池システムの制御方法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 15887473 Country of ref document: EP Kind code of ref document: A1 |
|
ENP | Entry into the national phase |
Ref document number: 2017508851 Country of ref document: JP Kind code of ref document: A |
|
WWE | Wipo information: entry into national phase |
Ref document number: 15561179 Country of ref document: US |
|
ENP | Entry into the national phase |
Ref document number: 2981161 Country of ref document: CA |
|
REEP | Request for entry into the european phase |
Ref document number: 2015887473 Country of ref document: EP |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
ENP | Entry into the national phase |
Ref document number: 20177030402 Country of ref document: KR Kind code of ref document: A |