WO2022239108A1 - 燃料電池システム - Google Patents
燃料電池システム Download PDFInfo
- Publication number
- WO2022239108A1 WO2022239108A1 PCT/JP2021/017872 JP2021017872W WO2022239108A1 WO 2022239108 A1 WO2022239108 A1 WO 2022239108A1 JP 2021017872 W JP2021017872 W JP 2021017872W WO 2022239108 A1 WO2022239108 A1 WO 2022239108A1
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- Prior art keywords
- exhaust gas
- fuel cell
- anode
- anode exhaust
- temperature
- Prior art date
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- 239000000446 fuel Substances 0.000 title claims abstract description 267
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- VZSRBBMJRBPUNF-UHFFFAOYSA-N 2-(2,3-dihydro-1H-inden-2-ylamino)-N-[3-oxo-3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)propyl]pyrimidine-5-carboxamide Chemical class C1C(CC2=CC=CC=C12)NC1=NC=C(C=N1)C(=O)NCCC(N1CC2=C(CC1)NN=N2)=O VZSRBBMJRBPUNF-UHFFFAOYSA-N 0.000 description 1
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
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Images
Classifications
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- 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 disclosure relates to a fuel cell system with a steam generator.
- Patent Document 1 describes a reformer evaporator that is provided upstream of a reformer in a fuel cell system.
- This reformer evaporator is provided with a burner as a heat generating part.
- An evaporator tube is spirally wound around the outer periphery of the heat generating portion. Thermal energy from the combustion of the burner is transferred to the evaporator tube. This vaporizes the water in the evaporation tube.
- the present disclosure has been made to solve the problems described above, and aims to provide a fuel cell system that can obtain higher energy efficiency.
- a fuel cell system includes a steam generator that heats water to generate steam, a reformer that reacts the steam with hydrocarbons to generate reformed gas containing hydrogen, an anode and a cathode. and generating electrical energy through an electrochemical reaction between the reformed gas supplied to the anode and the oxidant supplied to the cathode; and the raw material containing the hydrocarbon; an ejector that supplies at least one of an anode circulating gas obtained by recovering a part of the anode exhaust gas discharged from the anode to the reforming section using the water vapor as a driving fluid, wherein the steam generator is an evaporation passage through which the water flows; an anode exhaust gas passage thermally connected to the evaporation passage through which the anode exhaust gas flows; and an auxiliary heating device for heating the water,
- the anode exhaust gas channel and the auxiliary heating device face each other with the evaporation channel interposed therebetween.
- FIG. 1 is a system diagram showing the configuration of a fuel cell system according to Embodiment 1;
- FIG. 2 is a cross-sectional view showing the internal structure of the steam generator in the fuel cell system according to Embodiment 1;
- FIG. 8 is a cross-sectional view showing the configuration of the inlet of the anode exhaust gas channel and its surroundings in the steam generator according to Modification 1-1 of Embodiment 1;
- FIG. 10 is a cross-sectional view showing the configuration of the inlet of the anode exhaust gas channel and its surroundings in the steam generator according to Modification 1-2 of Embodiment 1;
- FIG. 8 is a cross-sectional view showing the configuration of the inlet of the anode exhaust gas flow path and its surroundings in the steam generator according to Modification 1-3 of Embodiment 1;
- FIG. 2 is a system diagram showing the configuration of a fuel cell system according to Embodiment 2;
- FIG. 8 is a cross-sectional view showing the internal structure of a steam generator in a fuel cell system according to Embodiment 2;
- FIG. 10 is a system diagram showing the configuration of a fuel cell system according to Embodiment 3;
- FIG. 11 is a cross-sectional view showing the internal structure of a steam generator according to Modification 3-1 of Embodiment 3;
- FIG. 11 is a system diagram showing the configuration of a fuel cell system according to Embodiment 4;
- FIG. 1 is a system diagram showing the configuration of a fuel cell system according to this embodiment. First, the basic configuration of the fuel cell system 100 according to this embodiment will be described.
- the fuel cell system 100 includes a fuel cell stack 1, a reformer 2, a combustor 3, a steam generator 4, a water separator 5, a recovery branch 221, an oxidant heat exchanger 7, a water Equipment such as a pump 8, an ejector 9, a heat recovery cooler 10, an air blower 18, a raw material pretreatment device 19, and a water treatment device 14 are provided.
- Each device processes raw materials, oxidants, water, or fluids originating from these.
- air is used as the oxidizing agent.
- the fuel cell system 100 has a control section 90 .
- the control unit 90 controls the entire fuel cell system 100 including the devices described above.
- the control unit 90 has a microcomputer including a CPU (Central Processing Unit), a ROM (Read Only Memory), a RAM (Random Access Memory), and the like.
- the fuel cell system 100 has a plurality of systems 200 to 211 and 214 to 216, each serving as a flow path for fluid.
- Each of the systems 200-211 and 214-216 is configured using piping.
- the raw material system 200 is a system that serves as a distribution route for the raw material F00.
- the reforming raw material system 201 is a system that serves as a distribution channel for the raw material F01 for reforming.
- the fuel gas system 202 is a system that serves as a distribution route for the fuel gas F02.
- the oxidant system 203 is a system that serves as a distribution channel for the oxidant F03.
- the cathode exhaust gas system 204 is a system that serves as a distribution route for the cathode exhaust gas F04.
- the reformed gas system 205 is a system that serves as a distribution route for the reformed gas F05.
- the anode exhaust gas system 206 is a system that serves as a distribution route for the anode exhaust gas F06.
- the anode recovery gas system 207 is a system that serves as a distribution route for the anode recovery gas F07.
- the recycled combustion gas system 208 is a system that serves as a distribution route for the recycled combustion gas F08.
- the anode circulating gas system 209 is a system that serves as a flow path for the anode circulating gas F09.
- the circulating water system 210 is a system that serves as a distribution route for the circulating water F10.
- the steam system 211 is a system that serves as a flow path for the steam F11.
- the heat recovery system 214 is a system that serves as a flow path for the cooling medium F14.
- the flue gas system 215 is a system that serves as a distribution route for the flue gas F15.
- the auxiliary combustion fuel system 216 is a system that serves as a distribution route for the auxiliary combustion fuel F16.
- a raw material F00 such as city gas is supplied to the raw material system 200 from the outside.
- a raw material pretreatment device 19 is provided in the raw material system 200 .
- the raw material pretreatment device 19 is configured to remove unnecessary components such as sulfur components from the raw material F00.
- the raw material system 200 is connected to the suction port of the ejector 9 via a reformed raw material system 201 .
- the raw material system 200 branches into a reforming raw material system 201 and an auxiliary combustion fuel system 216 at its downstream end.
- a downstream end of the auxiliary combustion fuel system 216 is connected to the combustor 3 .
- part of the raw material F00 passes through the auxiliary combustion fuel system 216 and is supplied to the combustor 3 as the auxiliary combustion fuel F16.
- the ejector 9 is a circulator that circulates fluid.
- the ejector 9 has an inlet into which the drive fluid flows, a suction port into which the suction fluid flows, and an outlet into which mixed fluid of the drive fluid and the suction fluid flows out.
- a nozzle is formed inside the ejector 9 to eject the driving fluid.
- An inlet of the ejector 9 is connected to the steam system 211 .
- a suction port of the ejector 9 is connected to a reforming raw material system 201 and an anode circulation gas system 209 .
- An outflow port of the ejector 9 is connected to a fuel gas system 202 .
- the ejector 9 uses the water vapor F11 as a driving fluid and sucks at least one of the raw material F01 and the anode circulating gas F09 as a suction fluid.
- the suction fluid sucked into the ejector 9 flows out from the ejector 9 together with the steam F ⁇ b>11 that is the driving fluid, and is supplied to the reformer 2 through the fuel gas system 202 .
- the reformer 2 is configured to react the steam F11 with the hydrocarbons contained in the raw material F01 to generate a hydrogen-containing reformed gas F05.
- the reformer 2 serves as a reforming section in the fuel cell system 100 .
- the reformer 2 is thermally connected to the combustor 3 or integrated with the combustor 3 . Thereby, the reformer 2 is supplied with the heat required for the reforming reaction from the combustor 3 .
- the reformer 2 is connected to the anode 1 a of the fuel cell stack 1 via a reformed gas system 205 .
- the combustor 3 is configured to burn the cathode exhaust gas F04, the recycled combustion gas F08, or the auxiliary combustion fuel F16 to generate heat.
- the combustor 3 is connected to a flue gas system 215 .
- the gas burned in the combustor 3 is discharged to the outside via the combustion exhaust gas system 215 as the combustion exhaust gas F15.
- Air used as the oxidant F03 is supplied to the oxidant system 203 from the outside.
- An air blower 18 is provided in the oxidant system 203 .
- the air blower 18 is a fluid machine that pumps the oxidant F03.
- An oxidant heat exchanger 7 is provided in the oxidant system 203 .
- a downstream end of the oxidant system 203 is connected to the cathode 1 c of the fuel cell stack 1 .
- the oxidant heat exchanger 7 is thermally connected to the combustor 3 or reformer 2.
- the oxidant F03 that has passed through the oxidant heat exchanger 7 is heated by heat supplied from the combustor 3 or the reformer 2 . As a result, the temperature of the oxidant F03 supplied to the fuel cell stack 1 rises.
- the fuel cell stack 1 is a power generator in which a plurality of fuel cells are stacked.
- the fuel cell stack 1 has an anode 1a as a negative electrode, a cathode 1c as a positive electrode, and an electrolyte 1e.
- Anode 1a and cathode 1c are separated by electrolyte 1e.
- An electrochemical device composed of an anode 1a, a cathode 1c and an electrolyte 1e is incorporated in the fuel cell stack 1 using cell members such as flow paths and separators.
- the fuel cell stack 1 is configured to generate electrical energy through an electrochemical reaction between the reformed gas F05 supplied to the anode 1a and the oxidizing agent F03 supplied to the cathode 1c.
- the upstream end of the anode exhaust gas system 206 is connected to the outlet of the anode 1a.
- the anode exhaust gas system 206 passes through the anode exhaust gas flow path 302 of the steam generator 4 .
- a heat recovery cooler 10 is provided downstream of the anode exhaust gas flow path 302 in the anode exhaust gas system 206 .
- a downstream end of the anode exhaust gas system 206 is connected to an inlet of the water separator 5 .
- the upstream end of the cathode exhaust gas system 204 is connected to the outlet of the cathode 1c.
- a downstream end of the cathode exhaust gas system 204 is connected to the combustor 3 .
- Circulating water F10 flows through the circulating water system 210 .
- the circulating water F10 is recovered from the water separator 5 by the water pump 8 .
- a water treatment device 14 is provided in the circulating water system 210 .
- the water treatment device 14 is configured to remove unnecessary components such as ion components from the circulating water F10.
- water is basically self-sustaining, but raw material water may be added from the outside as needed.
- a water pump 8 is provided downstream of the water treatment device 14 in the circulating water system 210 .
- the water pump 8 is a fluid machine that pumps the circulating water F10.
- a downstream end of the circulating water system 210 is connected to one end of the evaporation flow path 301 of the steam generator 4 .
- the upstream end of the steam system 211 is connected to the other end of the evaporation channel 301 .
- a downstream end of the steam system 211 is connected to an inlet of the ejector 9 .
- the steam generator 4 is configured to heat and vaporize water to generate steam.
- the steam generator 4 has an evaporation channel 301 , an anode exhaust gas channel 302 and an auxiliary heating device 303 .
- the circulating water F10 and steam F11 obtained by vaporizing the circulating water F10 flow through the evaporation flow path 301 .
- the anode exhaust gas F06 flows through the anode exhaust gas channel 302 .
- the anode exhaust gas channel 302 is thermally connected to the evaporation channel 301 .
- the auxiliary heating device 303 is configured to heat the circulating water F10 flowing through the evaporation passage 301 .
- the circulating water F10 flowing into the evaporation channel 301 is heated by heat exchange with the anode exhaust gas F06 flowing through the anode exhaust gas channel 302.
- the circulating water F10 is also heated by an auxiliary heating device 303 provided separately from the anode exhaust gas channel 302 .
- the heated circulating water F10 evaporates into steam F11 and flows out from the evaporation passage 301 to the steam system 211 .
- a detailed configuration of the steam generator 4 will be described later with reference to FIG.
- the heat recovery cooler 10 is a heat exchanger that exchanges heat between the anode exhaust gas F06 flowing out from the anode exhaust gas flow path 302 of the steam generator 4 and the cooling medium F14 flowing through the heat recovery system 214.
- the water separator 5 is a gas-liquid separator that separates the anode exhaust gas F06 into a gas component and a liquid component.
- a liquid outlet of the water separator 5 is connected to a circulating water system 210 on the upstream side of the water treatment device 14 via the water pipe 6 .
- a gas outlet of the water separator 5 is connected to the upstream end of the anode recovery gas system 207 .
- the anode recovery gas system 207 is branched into a recycling combustion gas system 208 and an anode circulation gas system 209 at a recovery branching portion 221 .
- a downstream end of the anode circulating gas system 209 is connected to the suction port of the ejector 9 .
- a recycled combustion gas flow meter 312 and a recycled combustion gas flow control valve 311 are provided in the recycled combustion gas system 208 .
- Recycled combustion gas flow meter 312 is configured to detect the flow rate of recycled combustion gas F08 flowing through recycled combustion gas system 208 .
- the recycled combustion gas flow control valve 311 is configured to adjust the flow rate of the recycled combustion gas F08.
- the recycled combustion gas flow rate adjustment valve 311 also functions as a shutoff section that shuts off the recycled combustion gas F08.
- a downstream end of the recycled combustion gas system 208 is connected to the combustor 3 .
- the oxidant F03 is circulated through the oxidant system 203 by the air blower 18 .
- the oxidant F03 is heated to a temperature suitable for operating the fuel cell stack 1 in the oxidant heat exchanger 7 and supplied to the cathode 1c of the fuel cell stack 1 .
- the oxidant F03 supplied to the cathode 1c consumes part of oxygen through an electrochemical reaction while being separated from the reformed gas F05 by the electrolyte 1e.
- the oxidizing agent F03 that has partially consumed the oxygen flows out from the cathode 1c as the cathode exhaust gas F04.
- the cathode exhaust gas F04 passes through the cathode exhaust gas system 204 and is supplied to the combustor 3 .
- Raw material F00 such as city gas is distributed in the raw material system 200 .
- Unnecessary components contained in the raw material F00 are removed by the raw material pretreatment device 19 .
- the raw material F00 that has passed through the raw material pretreatment device 19 is sucked into the ejector 9 as the raw material F01 for reforming.
- the raw material F01 sucked into the ejector 9 is mixed with the anode circulating gas F09 and water vapor F11, and flows out from the ejector 9 as the fuel gas F02.
- the fuel gas F02 passes through the fuel gas system 202 and is supplied to the reformer 2 .
- a part of the raw material F00 that has passed through the raw material pretreatment device 19 passes through the auxiliary combustion fuel system 216 and is supplied to the combustor 3 as the auxiliary combustion fuel F16.
- the fuel gas F02 supplied to the reformer 2 is reformed in the reformer 2 to become a reformed gas F05 containing hydrogen as a main component.
- the reformed gas F05 that has flowed out of the reformer 2 passes through the reformed gas system 205 and is supplied to the anode 1a of the fuel cell stack 1 .
- the reformed gas F05 supplied to the anode 1a consumes part of the fuel through an electrochemical reaction while being separated from the oxidant F03 by the electrolyte 1e.
- the reformed gas F05 that has partially consumed the fuel is discharged from the anode 1a as the anode exhaust gas F06.
- the anode exhaust gas F06 passes through the anode exhaust gas system 206 and flows into the anode exhaust gas channel 302 of the steam generator 4 .
- the anode exhaust gas F06 that has flowed out of the steam generator 4 flows into the heat recovery cooler 10.
- heat exchange is performed between the anode exhaust gas F06 and the cooling medium F14 flowing through the heat recovery system 214 . This further cools the anode exhaust gas F06.
- the cooled anode exhaust gas F 06 flows into the water separator 5 .
- the water separator 5 separates the anode exhaust gas F06 into a gas component and a liquid component.
- the gas component flows out from the water separator 5 to the anode recovery gas system 207 as the anode recovery gas F07.
- a part of the anode recovery gas F07 passes through the recycled combustion gas system 208 and is supplied to the combustor 3 as recycled combustion gas F08.
- Other anode recovery gas F07 passes through the anode circulation gas system 209 and is sucked into the ejector 9 as anode circulation gas F09.
- the anode circulating gas F09 sucked into the ejector 9 is mixed with the raw material F01 and water vapor F11 and supplied to the reformer 2 as the fuel gas F02.
- condensed water which is a liquid component, flows out from the water separator 5 and is supplied to the circulating water system 210 through the water pipe 6 .
- the circulating water F10 that has passed through the water treatment device 14 in the circulating water system 210 is supplied to the evaporation flow path 301 of the steam generator 4 .
- water is basically self-sustaining, but raw material water may be added from the outside as needed.
- the circulating water F10 is heated by heat exchange with the anode exhaust gas F06 or by the auxiliary heating device 303.
- the heated circulating water F10 evaporates into water vapor F11 and flows out from the steam generator 4 .
- the steam F11 flowing out from the steam generator 4 passes through the steam system 211 and flows into the ejector 9.
- the steam F11 that has flowed into the ejector 9 is ejected as a driving fluid from a nozzle provided inside the ejector 9 .
- the momentum possessed by the ejected water vapor F11 is given to the raw material F01 and the anode circulation gas F09.
- the raw material F01 and the anode circulating gas F09 are mixed with the water vapor F11 to become the fuel gas F02, which flows out from the ejector 9.
- the fuel gas F02 that has flowed out from the ejector 9 is supplied to the reformer 2 .
- a filter, a desulfurizer, etc. are used as the raw material pretreatment device 19 .
- a gas containing hydrocarbons is used as the raw material F00.
- Gases containing hydrocarbons include methane gas, propane gas, butane gas, natural gas, city gas, digestion gas containing methane gas as a main component, and the like.
- Various alcohols, petroleum-based raw materials, and the like can also be used as the raw material F00.
- the raw material F00 is a hydrophilic liquid raw material
- the raw material F00 may be mixed with the circulating water in advance.
- the raw material F00 is a hydrophobic liquid raw material
- the raw material F00 alone may be preheated and vaporized, or the raw material F00 and steam F11 may be preheated and vaporized while being mixed.
- a steam reforming reaction is performed.
- Typical reforming reactions when methane is used as a raw material are represented by equations (1) and (2).
- the reformer 2 is filled with a reforming catalyst.
- An endothermic reaction between methane and water vapor occurs in the reforming catalyst. This reaction produces hydrogen.
- the flow rate of steam supplied to the reformer 2 is expressed by the value of S/C.
- S/C is the mole fraction of water vapor (S) to carbon (C) contained in the fuel gas.
- the flow rate of steam supplied to the reformer 2 is set so that the S/C value is a constant value within the range of about 2.5 to 3.5.
- the reforming catalyst has a structure in which, for example, a Ni-based, Pt-based, or Ru-based catalyst is supported on a carrier such as Al 2 O 3 or MgO.
- the reforming reaction is not limited to this.
- an autothermal reforming reaction or a partial oxidation reforming reaction in which air is separately introduced into the reformer 2 may be used.
- the fuel cell stack 1 causes an electrochemical reaction between the reformed gas F05 supplied to the anode 1a and the oxidant F03 supplied to the cathode 1c while being separated from each other by the electrolyte 1e.
- electric energy is generated by giving and receiving electrons.
- a potential difference is generated in the fuel cell stack 1, and ion transfer via the electrolyte 1e and electron transfer within the circuit via the output terminals of both the anode 1a and the cathode 1c occur simultaneously.
- a direct current generated by movement of electrons in the circuit is output as power.
- the electrode material, operating temperature, etc. of the fuel cell stack 1 differ depending on the type of electrolyte 1e. Also, the type of ions that move through the electrolyte 1e differs depending on the type of the electrolyte 1e.
- the electrode reaction at the anode 1a is represented by Equation (3)
- the electrode reaction at the cathode 1c is represented by Equation (4).
- the oxygen corresponding to the electron transfer is consumed by the electrode reaction. Therefore, in the cathode 1c, the closer the cathode outlet is, the smaller the gas flow rate and the lower the oxygen partial pressure.
- internal reforming is possible in which the electrode reaction and the reforming reaction proceed simultaneously in the anode 1a. In this case, at the anode 1a, the reforming reaction of the residual methane that could not be reformed in the reformer 2 can proceed in the direction of hydrogen production.
- the ratio of the amount of hydrogen consumed in the electrode reaction of the anode 1a to the flow rate of hydrogen supplied from the reformer 2 or produced by internal reforming is 0.60 to 0.85. It often operates to be about the same. That is, the anode exhaust gas F06 at the anode outlet contains residual fuel. For example, the volume mole fraction of hydrogen contained in the anode exhaust gas F06 at the anode outlet is about 12%. Further, for example, the volume mole fraction of water vapor contained in the anode exhaust gas F06 at the anode outlet is about 60%.
- the fuel cell stack 1 is arranged so that the ratio of the amount of oxygen consumed in the electrode reaction of the cathode 1c to the flow rate of oxygen supplied through the oxidant system 203 is about 0.15 to 0.50. often works. That is, the cathode exhaust gas F04 at the cathode outlet contains residual oxygen. For example, the volume mole fraction of oxygen contained in the cathode exhaust gas F04 at the cathode outlet is about 16%.
- the temperature difference and enthalpy difference between the anode exhaust gas F06 and the circulating water F10, and the auxiliary heating device 303 are used as heat sources for the steam generator 4. This point also applies to fuel cell systems 100 in and after Embodiment 2, which will be described later.
- FIG. 2 is a cross-sectional view showing the internal structure of the steam generator of the fuel cell system according to this embodiment.
- the up-down direction in FIG. 2 represents the vertical up-down direction.
- the thick arrows in FIG. 2 represent the flow direction of the fluid.
- the steam generator 4 has a cylindrical shape as a whole.
- a central axis 4a of the steam generator 4 extends in the vertical direction.
- the steam generator 4 has an outer peripheral wall 4b and an inner peripheral wall 4c provided on the inner peripheral side of the outer peripheral wall 4b. Both the outer peripheral wall 4b and the inner peripheral wall 4c are formed in a cylindrical shape around the central axis 4a and extend along the vertical direction. An annular space is formed between the outer peripheral wall 4b and the inner peripheral wall 4c.
- a partition wall 4d is formed between the outer peripheral wall 4b and the inner peripheral wall 4c, that is, on the inner peripheral side of the outer peripheral wall 4b and on the outer peripheral side of the inner peripheral wall 4c.
- 4 d of partitions are formed in the cylindrical shape coaxial with the outer peripheral wall 4b and the inner peripheral wall 4c, and are extended along the up-down direction.
- a space formed between the outer peripheral wall 4b and the inner peripheral wall 4c is partitioned into an outer peripheral space 41 and an inner peripheral space 42 by the partition wall 4d. Both the outer peripheral space 41 and the inner peripheral space 42 are annular spaces.
- the upper end of the outer peripheral space 41 and the upper end of the inner peripheral space 42 are closed by the upper wall 4e.
- a lower end of the outer peripheral space 41 and a lower end of the inner peripheral space 42 are closed by a lower wall 4f. Both the upper wall 4e and the lower wall 4f are formed in an annular shape.
- the evaporation flow path 301 is provided in the inner peripheral space 42 .
- a heat transfer tube 301 a having a helical tube structure is formed in the inner peripheral space 42 .
- the heat transfer tube 301a has the central axis 4a as a spiral axis and extends spirally along the partition wall 4d.
- An evaporation channel inlet 301b serving as an inlet of the evaporation channel 301 is provided at the upper end of the heat transfer tube 301a.
- An evaporation channel outlet 301c serving as an outlet of the evaporation channel 301 is provided at the lower end of the heat transfer tube 301a.
- the heat transfer tube 301a is installed such that the height from the lower wall 4f monotonously decreases from the evaporation channel inlet 301b toward the evaporation channel outlet 301c.
- the heat transfer tube 301a is in close contact with the inner peripheral surface of the partition wall 4d. As a result, thermal energy is easily transferred between the heat transfer tube 301a and the partition wall 4d.
- the evaporation passage 301 is formed inside the heat transfer tube 301a. That is, the evaporation passage 301 is formed in a spiral shape with the central axis 4a as the spiral axis.
- the evaporation channel 301 extends obliquely with respect to the vertical direction.
- the evaporation channel 301 has a downward slope from the upstream side to the downstream side.
- the circulating water F10 that has flowed into the evaporation channel 301 from the evaporation channel inlet 301b gradually evaporates while flowing downward along the evaporation channel 301, and flows out as water vapor F11 from the evaporation channel outlet 301c.
- the auxiliary heating device 303 is a heating device that heats the circulating water F10 flowing through the evaporation flow path 301.
- the auxiliary heating device 303 is provided in the inner peripheral space 42 .
- the auxiliary heating device 303 is provided on the inner peripheral side of the evaporation passage 301, that is, between the evaporation passage 301 and the central axis 4a.
- Auxiliary heating device 303 is controlled by control unit 90 .
- the auxiliary heating device 303 has a plurality of electric heaters each formed in the shape of a straight pipe.
- the plurality of electric heaters are arranged on a circle around the central axis 4a.
- Each of the plurality of electric heaters is arranged parallel to the central axis 4a.
- the auxiliary heating device 303 may be formed in a cylindrical shape around the central axis 4a.
- a heat transfer promoting member 306 is filled around the evaporation passage 301 and the auxiliary heating device 303 in the inner peripheral space 42 . This facilitates transfer of thermal energy between the evaporation flow path 301 and the auxiliary heating device 303 .
- the evaporation passage 301 and the auxiliary heating device 303 are thermally connected to each other via the heat transfer promoting member 306 .
- the heat transfer promoting member 306 for example, metal particles, metal mesh, heat transfer cement, or the like is used.
- the anode exhaust gas channel 302 is provided in the outer peripheral space 41 .
- the entire outer peripheral space 41 serves as the anode exhaust gas channel 302 .
- the anode exhaust gas channel 302 is defined by the outer peripheral wall 4b, the partition wall 4d, the upper wall 4e and the lower wall 4f. That is, the outer peripheral wall 4 b , the partition wall 4 d , the upper wall 4 e and the lower wall 4 f serve as channel walls of the anode exhaust gas channel 302 .
- the anode exhaust gas channel 302 is thermally connected to the evaporation channel 301 via the partition wall 4d and the heat transfer tube 301a.
- the anode exhaust gas channel 302 is provided with heat transfer fins, such as offset fins, which are thermally connected to the partition wall 4d. This improves the heat transfer performance between the anode exhaust gas F06 and the partition wall 4d, so that the size of the steam generator 4 can be reduced.
- the steam generator 4 has an inflow pipe 307a forming an anode exhaust gas channel inlet 307 and an outflow pipe 308a forming an anode exhaust gas channel outlet 308.
- the anode exhaust gas F06 flows into the anode exhaust gas channel 302 through the inflow pipe 307a and flows out of the anode exhaust gas channel 302 through the outflow pipe 308a.
- the inflow pipe 307 a is connected to the lower portion of the anode exhaust gas flow path 302 .
- the inflow pipe 307 a penetrates the outer peripheral wall 4 b and extends along the radial direction of the steam generator 4 .
- the radial direction of the steam generator 4 is a direction along the radius of the steam generator 4 centering on the central axis 4a.
- the outflow pipe 308 a is connected to the upper end portion of the anode exhaust gas flow path 302 .
- the outflow pipe 308 a penetrates the outer peripheral wall 4 b and extends along the radial direction of the steam generator 4 .
- the outflow pipe 308a is arranged at a position symmetrical to the inflow pipe 307a with respect to the central axis 4a.
- the anode exhaust gas F06 flows through the anode exhaust gas channel 302 from the anode exhaust gas channel inlet 307 toward the anode exhaust gas channel outlet 308 .
- the circulating water F10 and water vapor F11 flow from top to bottom, while the anode exhaust gas F06 flows from bottom to top. That is, the flow of the anode exhaust gas F06 is countercurrent to the flow of the circulating water F10 and the water vapor F11.
- the anode exhaust gas channel 302 and the auxiliary heating device 303 face each other with the evaporation channel 301 interposed therebetween. That is, the evaporation channel 301 is sandwiched between the anode exhaust gas channel 302 and the auxiliary heating device 303 . As a result, the circulating water F10 flowing through the evaporation passage 301 is heated from both sides by the anode exhaust gas F06 and the auxiliary heating device 303 .
- a condensed water storage space 304 for storing condensed water is provided in the anode exhaust gas channel 302 below both the inflow pipe 307a and the outflow pipe 308a. That is, the condensed water storage space 304 is provided below both the anode exhaust gas channel inlet 307 and the anode exhaust gas channel outlet 308 .
- a condensed water discharge pipe 305 is connected to the bottom of the condensed water storage space 304 .
- the condensed water discharge pipe 305 extends downward through the lower wall 4f.
- the condensed water discharge pipe 305 is provided with a condensed water discharge valve 305a.
- a steam temperature sensor 20 is provided in the steam system 211 located downstream of the evaporation passage 301 .
- the water vapor temperature sensor 20 is configured to detect the temperature of the water vapor F11 that has flowed out from the evaporation passage 301 and output a detection signal to the control section 90 .
- An anode exhaust gas temperature sensor 21 is provided downstream of the anode exhaust gas flow path 302 in the anode exhaust gas system 206 .
- the anode exhaust gas temperature sensor 21 is configured to detect the temperature of the anode exhaust gas F06 flowing out from the anode exhaust gas channel 302 and output a detection signal to the control unit 90 .
- a water pump 8 supplies circulating water F ⁇ b>10 to the evaporation passage 301 of the steam generator 4 .
- the circulating water F10 uses the discharge pressure of the water pump 8 and gravity to flow through the evaporation channel 301 from the evaporation channel inlet 301b toward the evaporation channel outlet 301c.
- the anode exhaust gas flow path 302 of the steam generator 4 is supplied with the anode exhaust gas F06 discharged from the anode 1a. Thermal energy is transferred from the anode exhaust gas F06 flowing through the anode exhaust gas flow channel 302 to the circulating water F10 flowing through the evaporation flow channel 301 via the partition wall 4d and the heat transfer tube 301a. As a result, the circulating water F10 is vaporized into water vapor F11.
- the anode exhaust gas F06 that has flowed out of the anode exhaust gas channel 302 flows through the anode exhaust gas system 206 into the heat recovery cooler 10 .
- the control unit 90 Based on the detection signal from the anode exhaust gas temperature sensor 21, the control unit 90 acquires information on the temperature of the anode exhaust gas F06 flowing out from the anode exhaust gas flow path 302. The control unit 90 controls the auxiliary heating device 303 based on the temperature of the anode exhaust gas F06 flowing out from the anode exhaust gas channel 302 . Specifically, the control unit 90 operates the auxiliary heating device 303 when the temperature of the anode exhaust gas F06 detected by the anode exhaust gas temperature sensor 21 is below the lower limit threshold. The control unit 90 stops the auxiliary heating device 303 when the temperature of the anode exhaust gas F06 detected by the anode exhaust gas temperature sensor 21 exceeds the upper threshold value.
- the control of the auxiliary heating device 303 may be on/off control, or stepwise or continuous phase control. For example, when the temperature of the anode exhaust gas F06 detected by the anode exhaust gas temperature sensor 21 is between the lower limit threshold value and the upper limit threshold value, the control unit 90 gradually increases the output of the auxiliary heating device 303 according to the temperature. Or you may make it control continuously.
- the auxiliary heating device 303 When the auxiliary heating device 303 operates, the circulating water F10 flowing through the evaporation passage 301 is heated by the anode exhaust gas F06 and also by the auxiliary heating device 303. That is, the circulating water F10 flowing through the evaporation channel 301 is heated from both sides by the anode exhaust gas F06 flowing through the anode exhaust gas channel 302 and the auxiliary heating device 303 . Thereby, sufficient heat of vaporization is given to the circulating water F10.
- the anode exhaust gas temperature sensor 21 may be provided at or near the anode exhaust gas channel outlet 308 . Even in this case, the control unit 90 controls the auxiliary heating device 303 based on the temperature of the anode exhaust gas F06 detected by the anode exhaust gas temperature sensor 21 in the same manner as described above.
- the auxiliary heating device 303 is controlled based on the temperature of the anode exhaust gas F06 flowing out from the anode exhaust gas channel 302, but the control of the auxiliary heating device 303 is not limited to this.
- the control unit 90 may control the auxiliary heating device 303 based on the temperature detected by the water vapor temperature sensor 20, that is, the temperature of the water vapor F11 flowing out from the evaporation passage 301. Further, the control unit 90 may control the auxiliary heating device 303 based on both the temperature of the anode exhaust gas F06 flowing out from the anode exhaust gas channel 302 and the temperature of the water vapor F11 flowing out from the evaporation channel 301. good.
- the anode exhaust gas temperature sensor 21 may be provided upstream of the anode exhaust gas flow path 302 in the anode exhaust gas system 206 .
- the controller 90 calculates the thermal energy of the anode exhaust gas F06 based on the detection signal of the anode exhaust gas temperature sensor 21 and the operating condition signal of the fuel cell system 100 input to the controller 90 .
- the control unit 90 compares the thermal energy of the anode exhaust gas F06 with the thermal energy required for vaporizing the circulating water F10, and if the thermal energy required for vaporizing the circulating water F10 is insufficient, the deviation
- the output of the auxiliary heating device 303 is controlled accordingly.
- the controller 90 does not need to operate the auxiliary heating device 303 when the heat energy required for vaporizing the circulating water F10 can be obtained from the anode exhaust gas F06.
- the controller 90 operates the auxiliary heating device 303.
- the condensed water generated by the condensation of the anode exhaust gas F06 is stored in the condensed water storage space 304 provided below the anode exhaust gas channel inlet 307 .
- the condensed water stored in the condensed water storage space 304 is appropriately discharged via the condensed water discharge valve 305a.
- the condensed water is desirably discharged automatically based on the amount of condensed water in the condensed water storage space 304 .
- the condensed water discharge valve 305 a may be configured to open using the weight of the condensed water in the condensed water storage space 304 .
- the condensed water discharge pipe 305 may be provided with a U-shaped pipe so that the condensed water is discharged due to the head difference of the condensed water.
- the condensed water discharge valve 305a may be opened and closed by a timer so that the condensed water is periodically discharged.
- the anode exhaust gas F06 flowing out from the anode exhaust gas channel 302 further gives thermal energy to the cooling medium F14 in the heat recovery cooler 10, and flows into the water separator 5.
- the temperature of the anode exhaust gas F06 that has flowed into the water separator 5 becomes a predetermined temperature below the dew point.
- the control unit 90 controls the temperature of the anode exhaust gas F06 that has passed through the heat recovery cooler 10 or the temperature of the anode exhaust gas F06 in the water separator 5. to control the flow rate of the cooling medium F14.
- the temperature of the anode exhaust gas F06 that has passed through the heat recovery cooler 10 or the temperature of the anode exhaust gas F06 inside the water separator 5 is detected by a temperature sensor (not shown).
- the moisture contained in the anode exhaust gas F06 is liquefied based on the saturated vapor pressure at the temperature of the anode exhaust gas F06.
- the liquefied water becomes water droplets, is separated from the anode exhaust gas F06, and is stored in the lower portion of the water separator 5 as condensed water.
- the condensed water stored in the water separator 5 passes through the water pipe 6 and is supplied to the circulating water system 210 as circulating water F10.
- the circulating water F10 is supplied to the steam generator 4 by the water pump 8 according to the flow rate of the water vapor F11 required for the fuel gas F02.
- the anode recovery gas F07 is split at the recovery branching portion 221 into the recycled combustion gas F08 that flows through the recycled combustion gas system 208 and the anode circulation gas F09 that flows through the anode circulation gas system 209 .
- the recycled combustion gas F08 is supplied to the combustor 3 through the recycling combustion gas flow meter 312 and the recycling combustion gas flow control valve 311 .
- the degree of opening of the recycled combustion gas flow control valve 311 is controlled by the controller 90 based on the flow rate signal from the recycled combustion gas flow meter 312, for example.
- the recycled combustion gas F08 and the anode circulating gas F09 are distributed in the recovery branch section 221 at an appropriate flow rate ratio based on the operating conditions of the fuel cell system 100 . Therefore, high efficiency of the fuel cell system 100 is realized.
- the combustor 3 is supplied with the recycled combustion gas F08, the cathode exhaust gas F04 discharged from the cathode 1c, and the auxiliary combustion fuel F16. These gases are combusted in the combustor 3 . A part of the thermal energy of the combusted gas is supplied to the reformer 2 as thermal energy required for the reforming reaction. Thereby, the temperature of the reformer 2 rises to the temperature required for the reforming reaction. The temperature required for the reforming reaction in the reformer 2 is 600° C., for example.
- Another part of the thermal energy of the combusted gas is supplied to the oxidant F03 in the oxidant heat exchanger 7.
- the temperature of the oxidant F03 rises to a temperature at which the cathode 1c of the fuel cell stack 1 can operate.
- the temperature of the oxidizing agent F03 increases from 25°C, which is the temperature of the outside air, to 600°C.
- the gas burned in the combustor 3 gives heat energy to the reformer 2 and the oxidant heat exchanger 7, and then is discharged to the outside through the flue gas system 215 as flue gas F15.
- the anode circulating gas F09 passes through the anode circulating gas system 209 and is sucked into the ejector 9 .
- the anode circulating gas F09 sucked into the ejector 9 is mixed with the water vapor F11 and the raw material F01, and flows out from the ejector 9 as the fuel gas F02.
- the fuel gas F02 is supplied to the reformer 2 through the fuel gas system 202 .
- the fuel cell system 100 includes a solid oxide fuel cell using city gas as a raw material, and operates at a fuel utilization rate of 75%, a cell voltage of 0.84V, and a current of 24A. Under this condition, the enthalpy per output of the fuel cell stack 1 is ⁇ 3081 J/s ⁇ kW in the anode exhaust gas F06 at the anode outlet.
- the heat of vaporization required to turn the circulating water F10 into steam F11 is estimated at 247 J/s kW.
- the temperature of the anode exhaust gas F06 after applying thermal energy to the circulating water F10 in the steam generator 4 exceeds 150° C. according to the heat balance calculation.
- the heat energy required for converting the circulating water F10 into steam F11 in the steam generator 4 can be covered by heat exchange between the circulating water F10 and the anode exhaust gas F06.
- the temperature of the anode exhaust gas F06 in the water separator 5 is, for example, 60°C.
- the saturated vapor pressure at this temperature is approximately 0.025 MPa.
- the volume mole fraction of water vapor contained in the anode exhaust gas F06 at the anode outlet is about 60%.
- the volume mole fraction of water vapor contained in the anode exhaust gas F06 in the water separator 5 decreases to about 20% as the flow rate of water vapor decreases to about 1/2 due to condensation of water vapor.
- the anode exhaust gas F06 flows out from the water separator 5 as the anode recovery gas F07.
- the anode recovery gas F07 that has flowed out of the water separator 5 is distributed to the recycled combustion gas F08 and the anode circulation gas F09 at roughly the same flow rate in the recovery branching section 221 .
- the flow rate of the anode circulating gas F09 is about 1/4 of the flow rate of the anode exhaust gas F06 at the anode outlet. Further, the flow rate of water vapor contained in the anode circulating gas F09 is approximately 8% of the flow rate of water vapor contained in the anode exhaust gas F06 at the anode outlet. The flow rate of water vapor contained in the anode exhaust gas F06 at the anode outlet is only about 15% of the flow rate of water vapor required for the reformer 2 or the fuel cell stack 1 . In order to make up for the shortage of water vapor, the steam generator 4 vaporizes the circulating water F10 to generate water vapor F11 of about 0.5 MPa.
- the operation of the fuel cell system 100 when increasing the output of the fuel cell stack 1 will be described.
- the flow rates of the oxidizing agent F03, the raw material F01, and the water vapor F11, which are gases required for the cell reaction increase according to the output load conditions under the control of the control unit 90.
- the controller 90 increases the flow rate of the steam F11 prior to increasing the flow rate of the raw material F01. That is, when increasing the output of the fuel cell stack 1, it is first necessary to increase the flow rate of the water vapor F11, that is, the flow rate of the circulating water F10. Along with this, the steam generator 4 requires heat of vaporization corresponding to the increase in the flow rate of the circulating water F10.
- the auxiliary heating device 303 when the flow rate of the circulating water F10 increases, the temperature of the anode exhaust gas F06 detected by the anode exhaust gas temperature sensor 21 decreases, so the auxiliary heating device 303 operates. That is, the auxiliary heating device 303 gives auxiliary heat energy to the circulating water F10 in the evaporation passage 301 . As a result, the auxiliary heating device 303 compensates for the heat of vaporization corresponding to the increase in the flow rate of the circulating water F10.
- the heat of vaporization of the circulating water F10 can be covered by the thermal energy from the anode exhaust gas F06.
- the auxiliary heating device 303 is stopped.
- the circulating water F10 flowing through the evaporation channel 301 is heated from one side only by the anode exhaust gas F06 flowing through the anode exhaust gas channel 302 .
- the operation of the fuel cell system 100 when increasing the output of the fuel cell stack 1 is not limited to the above example. If the heat of vaporization of the circulating water F10 is insufficient depending on the operating conditions of the fuel cell system 100, the auxiliary heating device 303 may operate continuously or intermittently. Further, when the amount of increase in the output of the fuel cell stack 1 is small and the increase in the heat of vaporization of the circulating water F10 can be covered by the heat energy from the anode exhaust gas F06, the auxiliary heating device 303 does not need to operate. good.
- the thermal energy of the anode exhaust gas F06 flowing through the anode exhaust gas system 206 can be used to turn the circulating water F10 into steam F11. Therefore, the flow rate of the recycled combustion gas F08 supplied to the combustor 3 can be decreased, and the flow rate of the anode circulating gas F09 returned to the reformer 2 via the ejector 9 can be increased. Therefore, according to this embodiment, the fuel cell system 100 with high energy efficiency can be realized.
- the anode exhaust gas channel 302 and the auxiliary heating device 303 face each other with the evaporation channel 301 interposed therebetween. Therefore, the circulating water F10 flowing through the evaporation passage 301 can be heated from both sides. Therefore, according to the present embodiment, the heat loss can be reduced, so that the fuel cell system 100 with higher energy efficiency can be realized.
- the condensed water can be stored in the condensed water storage space 304.
- the flow of the anode exhaust gas F06 can be prevented from being obstructed by the condensed water, so that the generation of pulsation in the anode exhaust gas F06 can be suppressed.
- the waste heat of the anode exhaust gas F06 can be used to turn the circulating water F10 into steam F11. Therefore, according to the present embodiment, the thermal energy of the fuel cell system 100 can be effectively used, so the fuel cell system 100 with high energy efficiency can be realized.
- the thermal energy obtained from the anode exhaust gas F06 may be insufficient for the thermal energy required as the heat of vaporization of the circulating water F10.
- the auxiliary heating device 303 can compensate for thermal energy with good responsiveness. Therefore, in this embodiment, a wide range of operating conditions for the fuel cell system 100 can be accommodated.
- the auxiliary heating device 303 can be stopped when the heat energy required as the heat of vaporization of the circulating water F10 can be obtained from the anode exhaust gas F06. Therefore, it is not necessary to continuously supply energy to the auxiliary heating device 303 . Therefore, according to this embodiment, the fuel cell system 100 with high energy efficiency can be realized.
- FIG. 3 is a cross-sectional view showing the configuration of the inlet of the anode exhaust gas flow path and its surroundings in the steam generator according to Modification 1-1 of the present embodiment.
- the inflow pipe 307a has an end face 307a1.
- the end surface 307 a 1 faces the anode exhaust gas channel 302 .
- the end face 307a1 is formed perpendicular to the pipe axis of the inflow pipe 307a.
- the end surface 307a1 is formed on a surface different from the inner wall surface 4b1 of the outer peripheral wall 4b.
- the inflow pipe 307a is inserted into the anode exhaust gas channel 302, so the end surface 307a1 protrudes toward the inside of the anode exhaust gas channel 302 with respect to the inner wall surface 4b1.
- the end surface 307a1 is separated from the partition wall 4d.
- the anode exhaust gas F06 flows into the anode exhaust gas channel 302 through the inflow pipe 307a, flows upward through the anode exhaust gas channel 302, and flows out of the steam generator 4.
- the condensed water mainly flows down along the inner wall surface 4b1 of the outer peripheral wall 4b and moves to the condensed water storage space 304.
- the end surface 307a1 of the inflow pipe 307a is formed on a different surface from the inner wall surface 4b1, so that the condensed water flowing down along the inner wall surface 4b1 is less likely to enter the inflow pipe 307a. Therefore, it is possible to prevent the flow of the anode exhaust gas F06 from being obstructed by the condensed water, so that it is possible to suppress the generation of pulsation in the anode exhaust gas F06.
- the end surface 307a1 of the inflow pipe 307a protrudes toward the inside of the anode exhaust gas channel 302 with respect to the inner wall surface 4b1, so that the infiltration of the condensed water into the inflow pipe 307a is more reliably prevented. can be prevented. Therefore, it is possible to more reliably prevent pulsation from occurring in the anode exhaust gas F06.
- FIG. 4 is a cross-sectional view showing the configuration of the inlet of the anode exhaust gas channel and its surroundings in the steam generator according to Modification 1-2 of the present embodiment.
- the end surface 307a1 of the inflow pipe 307a is formed on a different surface from the inner wall surface 4b1 and is formed obliquely with respect to the pipe axis of the inflow pipe 307a.
- the end surface 307a1 is inclined with respect to the inner wall surface 4b1 so as to move away from the inner wall surface 4b1 toward the upper side. Therefore, in this modified example, it is more difficult for the condensed water to enter the inflow pipe 307a as compared with the configuration of the modified example 1-1.
- FIG. 5 is a cross-sectional view showing the configuration of the inlet of the anode exhaust gas flow path and its surroundings in the steam generator according to Modification 1-3 of the present embodiment.
- a dew condensation water guide plate 313 is formed above the anode exhaust gas channel inlet 307 in the anode exhaust gas channel 302 .
- One end 313 a of the condensed water guide plate 313 is joined to the inner wall surface 4 b 1 at a position above the anode exhaust gas channel inlet 307 .
- Condensed water guide plate 313 is inclined such that the further away from inner wall surface 4b1, that is, the closer to other end 313b of dew condensed water guide plate 313, the lower the height.
- a gap is formed between the other end portion 313b of the condensed water guiding plate 313 and the partition wall 4d.
- the other end 313b may be joined to the partition wall 4d.
- the inflow pipe 307a and the anode exhaust gas channel inlet 307 of this modified example have the same configuration as that shown in FIG.
- the condensed water guiding plate 313 is formed with at least one through hole 313c.
- Each of the through holes 313c penetrates the condensed water guide plate 313 along the thickness direction of the condensed water guide plate 313 .
- the through hole 313c becomes a part of the channel of the anode exhaust gas F06, so that the anode exhaust gas F06 that has flowed into the anode exhaust gas channel 302 can easily flow upward.
- the through hole 313c may not be formed in the condensed water guiding plate 313 when the flow path for the anode exhaust gas F06 is sufficiently secured.
- the fuel cell system 100 includes the steam generator 4, the reformer 2, the fuel cell stack 1, and the ejector 9.
- the steam generator 4 is configured to heat the circulating water F10 to generate steam F11.
- the reformer 2 is configured to react the steam F11 and hydrocarbons to produce a reformed gas F05 containing hydrogen.
- the fuel cell stack 1 has an anode 1a and a cathode 1c.
- the fuel cell stack 1 is configured to generate electrical energy through an electrochemical reaction between the reformed gas F05 supplied to the anode 1a and the oxidizing agent F03 supplied to the cathode 1c.
- the ejector 9 ejects at least one of the raw material F01 containing hydrocarbons and the anode circulating gas F09 obtained by recovering a part of the anode exhaust gas F06 discharged from the anode 1a into the reformer 2 using steam F11 as a driving fluid.
- the steam generator 4 includes an evaporation passage 301 through which the circulating water F10 flows, an anode exhaust gas passage 302 that is thermally connected to the evaporation passage 301 and through which the anode exhaust gas F06 flows, and an auxiliary heating that heats the circulating water F10.
- the anode exhaust gas channel 302 and the auxiliary heating device 303 face each other with the evaporation channel 301 interposed therebetween.
- the reformer 2 is an example of a reforming section.
- the circulating water F10 is an example of water.
- the anode exhaust gas channel 302 and the auxiliary heating device 303 can heat the circulating water F10 flowing through the evaporation channel 301 from both sides. Therefore, according to the present embodiment, the heat loss can be reduced, so that the fuel cell system 100 with higher energy efficiency can be realized.
- the evaporation flow path 301 extends obliquely with respect to the vertical direction.
- the evaporation channel 301 has a downward slope from the upstream side to the downstream side. According to this configuration, the circulating water F10 can be circulated through the evaporation flow path 301 using gravity.
- the anode exhaust gas channel 302 extends along the vertical direction.
- the steam generator 4 has an outer peripheral wall 4b, an inflow pipe 307a and an outflow pipe 308a.
- the outer peripheral wall 4b extends along the vertical direction.
- the outer peripheral wall 4 b defines the anode exhaust gas flow path 302 .
- the inflow pipe 307a is connected to the anode exhaust gas channel 302 through the outer peripheral wall 4b.
- the anode exhaust gas F06 flows in from the inflow pipe 307a.
- the outflow pipe 308a is connected to the anode exhaust gas channel 302 above the inflow pipe 307a.
- the anode exhaust gas F06 flows out from the outflow pipe 308a.
- a condensed water storage space 304 for storing condensed water is provided in the anode exhaust gas channel 302 below the inflow pipe 307a.
- the outer peripheral wall 4b is an example of a channel wall.
- the inflow pipe 307a has an end face 307a1 facing the anode exhaust gas channel 302.
- the end surface 307a1 protrudes toward the inside of the anode exhaust gas channel 302 from the inner wall surface 4b1 of the outer peripheral wall 4b. According to this configuration, it is possible to prevent the condensed water from entering the inflow pipe 307a, thereby preventing pulsation from occurring in the anode exhaust gas F06.
- a condensed water guide plate 313 that guides condensed water is provided above the inflow pipe 307a in the anode exhaust gas flow path 302 . According to this configuration, it is possible to prevent the condensed water from entering the inflow pipe 307a, thereby preventing pulsation from occurring in the anode exhaust gas F06.
- the auxiliary heating device 303 has an electric heater. With this configuration, the output of the auxiliary heating device 303 can be easily adjusted.
- the fuel cell system 100 further includes an anode exhaust gas temperature sensor 21 that detects the temperature of the anode exhaust gas F06, and a controller 90.
- the controller 90 controls the auxiliary heating device 303 based on the temperature of the anode exhaust gas F06.
- the heat energy obtained from the anode exhaust gas F06 is insufficient for the heat energy required as the heat of vaporization of the circulating water F10, the heat energy can be supplemented by the auxiliary heating device 303. .
- the fuel cell system 100 further includes a water vapor temperature sensor 20 that detects the temperature of the water vapor F11, and a controller 90.
- the controller 90 controls the auxiliary heating device 303 based on the temperature of the steam F11.
- the heat energy obtained from the anode exhaust gas F06 is insufficient for the heat energy required as the heat of vaporization of the circulating water F10, the heat energy can be supplemented by the auxiliary heating device 303. .
- FIG. 6 is a system diagram showing the configuration of the fuel cell system according to this embodiment.
- FIG. 7 is a cross-sectional view showing the internal structure of the steam generator in the fuel cell system according to this embodiment.
- This embodiment differs from the first embodiment in that the auxiliary heating device 303 has an auxiliary combustor 50 and a combustion exhaust gas flow path 314 .
- Components having the same functions and actions as those of the first embodiment are given the same reference numerals, and descriptions thereof are omitted.
- an auxiliary combustor 50 is provided above the steam generator 4 .
- the auxiliary combustor 50 forms part of the auxiliary heating device 303 .
- the auxiliary combustor 50 is arranged on the central axis 4 a of the steam generator 4 .
- the auxiliary combustor 50 faces the anode exhaust gas flow path 302 with the evaporation flow path 301 interposed therebetween.
- the auxiliary combustion fuel system 216 branches into an auxiliary combustion fuel system 217 and an auxiliary combustion fuel system 218 .
- Auxiliary combustion fuel system 217 is connected to combustor 3 .
- Auxiliary combustion fuel system 218 is connected to auxiliary combustor 50 .
- the auxiliary combustion fuel F16 flowing through the auxiliary combustion fuel system 216 is divided into auxiliary combustion fuel F17 and auxiliary combustion fuel F18.
- the auxiliary combustion fuel F17 flows through the auxiliary combustion fuel system 217 and is supplied to the combustor 3 .
- the auxiliary combustion fuel F18 flows through the auxiliary combustion fuel system 218 and is supplied to the auxiliary combustor 50 .
- a flue gas flow path 314 is provided between the auxiliary combustor 50 and the outside of the steam generator 4 .
- the combustion exhaust gas flow path 314 is arranged on the inner peripheral side of the inner peripheral space 42 .
- a partition wall 315 partitions the combustion exhaust gas flow path 314 and the inner peripheral space 42 .
- the partition wall 315 is formed in a cylindrical shape around the central axis 4a.
- the flue gas channel 314 is thermally connected to the evaporation channel 301 via the partition wall 315, the heat transfer promoting member 306, and the heat transfer tube 301a.
- the flue gas flow path 314 forms part of the auxiliary heating device 303 .
- the combustion exhaust gas channel 314 faces the anode exhaust gas channel 302 with the evaporation channel 301 interposed therebetween.
- the auxiliary combustion fuel F18 and combustion-supporting gas such as air are ignited by an igniter or the like and burned to generate high-temperature flue gas.
- the high-temperature flue gas passes through the flue gas passage 314 and gives thermal energy to the circulating water F10 flowing through the evaporation passage 301 .
- the combustion exhaust gas that has given thermal energy to the circulating water F10 is discharged outside the steam generator 4 .
- the flow rate of the auxiliary combustion fuel F18 By adjusting the flow rate of the auxiliary combustion fuel F18, the heat quantity of the flue gas is controlled. Other operations are the same as those of the first embodiment.
- the auxiliary combustor 50 may have a structure in which air is introduced by natural intake. In this case, although it becomes difficult to change the combustion air ratio, the structure of the auxiliary combustor 50 becomes simple. Further, the auxiliary combustor 50 may be supplied with air through an air supply system separately provided. In this case, an arbitrary combustion air ratio can be obtained by controlling the flow rate ratio of the auxiliary combustion fuel F18 and air. This makes it possible to control the temperature of the adiabatic flame, so that the amount of heat energy transferred to the circulating water F10 can be controlled more accurately.
- the following effects are obtained in addition to the effects obtained by the first embodiment. That is, in the present embodiment, the auxiliary combustor 50 is used in the auxiliary heating device 303 , so that the raw material F00 necessary for the fuel cell stack 1 can be used to generate the thermal energy necessary for the steam generator 4 . Therefore, the efficiency of the fuel cell system 100 can be improved.
- the auxiliary combustor 50 is used as the auxiliary heating device 303, compared to the configuration in which an electric heater is used as the auxiliary heating device 303, power consumption is reduced particularly when starting the fuel cell system 100. can be suppressed. Therefore, the fuel cell system 100 can also be applied to an emergency power supply. Note that the operation of the fuel cell system 100 at startup will be described in a third embodiment, which will be described later.
- the auxiliary heating device 303 includes the auxiliary combustor 50 and the flue gas channel 314 through which the flue gas generated in the auxiliary combustor 50 flows. have. With this configuration, power consumption in the auxiliary heating device 303 can be suppressed.
- Embodiment 3 A fuel cell system and an operating method thereof according to Embodiment 3 will be described. This embodiment mainly relates to the operation of the fuel cell system 100 when it is started.
- FIG. 8 is a system diagram showing the configuration of the fuel cell system according to this embodiment.
- the fuel cell stack 1 is provided with a stack temperature sensor 22 .
- Stack temperature sensor 22 is configured to detect a representative temperature of fuel cell stack 1 .
- the reformer 2 is provided with a reformer temperature sensor 24 .
- the reformer temperature sensor 24 is configured to detect a representative temperature of the reformer 2 .
- Other configurations are the same as those of the first embodiment shown in FIGS.
- the oxidant F03 discharged from the air blower 18 flows through the oxidant system 203, passes through the oxidant heat exchanger 7 and the cathode 1c, and is supplied to the combustor 3 as the cathode exhaust gas F04. Also, part of the raw material F00 flows through the auxiliary combustion fuel system 216 and is supplied to the combustor 3 as the auxiliary combustion fuel F16. In the combustor 3, the cathode exhaust gas F04 and the auxiliary combustion fuel F16 are ignited by an igniter or the like and combusted to generate combustion gas.
- the combustion gas generated in the combustor 3 raises the temperature of the reformer 2 and the oxidant heat exchanger 7, passes through the combustion exhaust gas system 215, and is discharged as the combustion exhaust gas F15.
- the oxidant F03 heated in the oxidant heat exchanger 7 is supplied to the cathode 1c, and the temperature of the fuel cell stack 1 is raised by the sensible heat of the oxidant F03 itself.
- the auxiliary heating device 303 of this embodiment shall be an electric heater.
- the temperature of the steam generator 4 is increased.
- the water pump 8 When the temperatures of the fuel cell stack 1 and the reformer 2 rise to a temperature at which water vapor does not condense, for example 150°C, the water pump 8 is activated to supply the circulating water F10 to the steam generator 4.
- the circulating water F10 circulates downward through the evaporation flow path 301 using the discharge pressure of the water pump 8 and gravity.
- the circulating water F10 flowing through the evaporation passage 301 receives heat from the auxiliary heating device 303 and evaporates into water vapor F11.
- the steam F11 is supplied to the reformer 2 and the anode 1a by the ejector 9 as fuel gas F02 at startup.
- the anode exhaust gas F06 discharged from the anode 1a flows upward through the anode exhaust gas channel 302 of the steam generator 4 and flows out from the anode exhaust gas channel outlet 308.
- the anode exhaust gas F06 In the temperature rising process of the steam generator 4, the anode exhaust gas F06 is in a steam-rich state. If the anode exhaust gas flow path 302 has a low temperature portion, water vapor in the anode exhaust gas F06 will condense. However, even if the water vapor in the anode exhaust gas F06 is condensed, the condensed water is stored in the condensed water storage space 304 provided in the lower part of the anode exhaust gas channel 302 and discharged through the condensed water discharge pipe 305. be done.
- the raw material system 200 and the reforming raw material system 201 to start supplying raw material F01.
- the flow rate of raw material F01 at the start of supply is controlled in consideration of S/C.
- the value of S/C at rated operating conditions is, for example, in the range of 2.5 to 3.5.
- the flow rate of the raw material F01 at the start of supply is set so that the S/C value is larger than the S/C value in the rated operation state.
- a transient temperature distribution is formed in the reformer 2 at startup.
- the flow rate of the raw material F01 at the start of supply is set to a value of S/C of about 8.0, for example. After that, the flow rate of steam F11 and the flow rate of raw material F01 are appropriately controlled.
- the supply of the raw material F01 is started before the temperature of the fuel cell stack 1 rises to a temperature at which the oxidation reaction of the component members constituting the fuel cell stack 1 progresses, for example 300°C.
- the supply of the raw material F01 is started under temperature conditions such that the temperature of the reformer 2 is 450° C. or higher and the temperature of the fuel cell stack 1 is 300° C. or lower.
- the flow rate of the auxiliary combustion fuel F16 supplied to the combustor 3 and the flow rate of the oxidant F03 supplied to the combustor 3 as the cathode exhaust gas F04 are adjusted to achieve combustion.
- the combustion temperature of the combustor 3 and the input energy of the combustor 3 are controlled.
- the flow rate of each of the oxidizing agent F03, raw material F01, and water vapor F11, which are gases necessary for the cell reaction, is set to a predetermined flow rate.
- the temperature of the fuel cell stack 1 is raised to a temperature at which power generation is possible, for example, 600.degree. After the temperature of the fuel cell stack 1 has risen to a temperature at which power generation is possible, the respective flow rates of the oxidizing agent F03, raw material F01, and steam F11 are controlled to predetermined flow rates.
- power generation in the fuel cell stack 1 is started by a method such as current control or power control, and the fuel cell system 100 shifts to a predetermined rated operating state.
- the flow rate of the anode exhaust gas F06 increases and the temperature of the anode exhaust gas F06 rises. This increases the enthalpy of the anode exhaust gas F06. Therefore, in the steam generator 4, the heat energy given to the circulating water F10 from the anode exhaust gas F06 increases.
- the control unit 90 controls the auxiliary heating device 303 based on the temperature of the anode exhaust gas F06 detected by the anode exhaust gas temperature sensor 21. Specifically, the controller 90 controls the auxiliary heating device 303 so that the amount of heat generated by the auxiliary heating device 303 decreases as the temperature of the anode exhaust gas F06 rises. As a result, the amount of heat generated by the auxiliary heating device 303 decreases as the temperature of the anode exhaust gas F06 rises. Therefore, it is possible to prevent excessive heat energy from being applied to the circulating water F10. In this way, the thermal energy given to the circulating water F10 is adjusted.
- control unit 90 may control the auxiliary heating device 303 based on the temperature of the steam F11 detected by the steam temperature sensor 20. Specifically, the controller 90 controls the auxiliary heating device 303 so that the amount of heat generated by the auxiliary heating device 303 decreases as the temperature of the steam F11 rises. Even in this way, it is possible to prevent excessive heat energy from being applied to the circulating water F10.
- the anode exhaust gas F06 that has passed through the steam generator 4 further gives thermal energy to the cooling medium F14 flowing through the heat recovery system 214 in the heat recovery cooler 10 .
- the temperature of the anode exhaust gas F06 flowing into the water separator 5 is lowered to a predetermined temperature below the dew point.
- the moisture contained in the anode exhaust gas F06 is liquefied based on the saturated vapor pressure at the temperature of the anode exhaust gas F06.
- the liquefied water becomes water droplets and is separated from the anode exhaust gas F06 and stored in the lower portion of the water separator 5 .
- the anode recovery gas F07 is split at the recovery branching portion 221 into the recycled combustion gas F08 that flows through the recycled combustion gas system 208 and the anode circulation gas F09 that flows through the anode circulation gas system 209 .
- Recycled combustion gas F08 is supplied to combustor 3 through recycled combustion gas system 208 .
- the auxiliary combustion fuel F16 supplied by the auxiliary combustion fuel system 216 and the cathode exhaust gas F04 supplied by the cathode exhaust gas system 204 are mainly burned.
- the flow rate of the raw material F01 increases, so the combustion fuel supplied to the combustor 3 increases. Therefore, after the supply of the raw material F01 is started, the flow rate of the auxiliary combustion fuel F16, the flow distribution ratio of the recycled combustion gas F08 in the recovery branch section 221, and the flow rate of the oxidant F03 are appropriately controlled.
- the anode recovery gas F07 that has flowed through the anode recovery gas system 207 is split into the recycled combustion gas F08 and the anode circulation gas F09 at the recovery branching section 221, but this is not restrictive.
- the entire amount of the anode recovery gas F07 that has flowed through the anode recovery gas system 207 may be circulated to the recycling combustion gas system 208 as the recycled combustion gas F08.
- the auxiliary heating device 303 is controlled by the controller 90 so that the supply of steam F11 to the reformer 2 and the anode 1a is started during a specific period.
- the above specific period is a period after the temperature of the fuel cell stack 1 rises to the first temperature and before the temperature of the fuel cell stack 1 rises to the second temperature.
- the first temperature is a temperature at which water vapor does not condense inside the fuel cell stack 1, and is, for example, 150.degree.
- the second temperature is the temperature at which the oxidation reaction of the component members forming the fuel cell stack 1 proceeds, and is 300° C., for example.
- the thermal energy required to generate the required flow rate of water vapor F11 is supplied from the auxiliary heating device 303 to the evaporation passage 301 when the fuel cell system 100 is started.
- the thermal energy supplied from the anode exhaust gas channel 302 to the evaporation channel 301 increases. Therefore, the amount of heat generated by the auxiliary heating device 303 is reduced under the control of the control unit 90 .
- the thermal energy required to generate water vapor F11 is supplied to evaporation channel 301 from both auxiliary heating device 303 and anode exhaust gas channel 302 .
- the thermal energy supplied from the anode exhaust gas channel 302 to the evaporation channel 301 further increases. Therefore, the auxiliary heating device 303 is stopped under the control of the controller 90 . Thereby, the thermal energy required to generate the water vapor F11 is given from the anode exhaust gas channel 302 to the evaporation channel 301 .
- the fuel cell system 100 when the fuel cell system 100 is activated, it is possible to continuously raise the temperature while forming the necessary gas atmosphere. Therefore, according to the present embodiment, it is possible to stably generate water vapor with little pulsation according to the temperature rising conditions of the fuel cell system 100 . Moreover, according to the present embodiment, the fuel cell system 100 with a high degree of freedom and high energy efficiency can be realized.
- FIG. 9 is a cross-sectional view showing the internal structure of a steam generator according to modification 3-1 of the present embodiment. As shown in FIG. 9 , the steam generator 4 has a first channel member 316 and a second channel member 317 .
- the first flow path member 316 is formed in a cylindrical shape around the central axis 4a.
- a groove 316 a is formed in the outer peripheral surface of the first flow path member 316 .
- the groove 316a extends spirally with the central axis 4a as the spiral axis.
- the second flow path member 317 is formed in a cylindrical shape around the central axis 4a.
- the second channel member 317 has an inner diameter equal to the outer diameter of the first channel member 316 .
- the inner peripheral surface of the second channel member 317 is joined to the outer peripheral surface of the first channel member 316 .
- An evaporation channel 301 is formed inside the groove 316a. At the upper end of the evaporation channel 301, an evaporation channel inlet 301b is provided. At the lower end of the evaporation channel 301, an evaporation channel outlet 301c is provided.
- the first channel member 316 and the second channel member 317 are arranged on the outer peripheral side of the flue gas channel 314 and on the inner peripheral side of the anode exhaust gas channel 302 .
- the inner peripheral surface of the first flow path member 316 faces the flue gas flow path 314 .
- the evaporation channel 301 is thermally connected to the flue gas channel 314 via the first channel member 316 .
- the outer peripheral surface of the second channel member 317 faces the anode exhaust gas channel 302 .
- the evaporation channel 301 is thermally connected to the anode exhaust gas channel 302 via the second channel member 317 .
- the circulating water F10 flowing through the evaporation flow path 301 is given heat energy from the combustion exhaust gas flowing through the combustion exhaust gas flow path 314 via the first flow path member 316 . Further, the circulating water F10 is given thermal energy from the anode exhaust gas F06 flowing through the anode exhaust gas channel 302 via the second channel member 317 .
- both the flue gas flowing through the flue gas flow path 314 and the anode flue gas F06 flowing through the anode flue gas flow path 302 transfer heat energy to the circulating water F10 via a single member. transmitted.
- the heat transfer characteristics of the steam generator 4 can be improved because the heat resistance is reduced in any heat transfer path. Therefore, a small-sized steam generator 4 with high responsiveness can be realized, so that a high-performance fuel cell system 100 can be realized.
- the fuel cell system 100 further includes the stack temperature sensor 22 that detects the temperature of the fuel cell stack 1 and the controller 90 .
- the control unit 90 controls the auxiliary heating device 303 so that the supply of the steam F11 to the reformer 2 is started during a specific period.
- the specific period is after the temperature of the fuel cell stack 1 rises to the first temperature and before the temperature of the fuel cell stack 1 rises to a second temperature higher than the first temperature.
- the first temperature is 150°C and the second temperature is 300°C.
- the supply of the water vapor F11 can be started before the oxidation reaction of the component members constituting the fuel cell stack 1 proceeds.
- Embodiment 4 A fuel cell system and an operating method thereof according to Embodiment 4 will be described.
- This embodiment mainly relates to the operation when the fuel cell system 100 is stopped.
- the configuration of the fuel cell system 100 according to this embodiment is the same as the configuration of the fuel cell system 100 according to Embodiment 3 shown in FIG. That is, the fuel cell system 100 according to the present embodiment has a stack temperature sensor 22 and a reformer temperature sensor 24, like the fuel cell system 100 according to the third embodiment.
- the operation of the fuel cell system 100 executed under the control of the control unit 90 when the fuel cell system 100 is stopped will be described.
- the control unit 90 reduces the output of the fuel cell stack 1 to stop the power generation of the fuel cell stack 1 .
- the control unit 90 reduces the supply amount of the raw material F01 and stops the supply of the raw material F01.
- the control unit 90 operates the auxiliary heating device 303 at the same time as the supply amount of the raw material F01 starts to decrease.
- the auxiliary heating device 303 of this embodiment shall be an electric heater.
- the control unit 90 fully closes the recycled combustion gas flow control valve 311 when the flow rate of the raw material F01 becomes less than the threshold value. As a result, the supply of the recycled combustion gas F08 to the combustor 3 is cut off, and combustion in the combustor 3 is stopped.
- the water pump 8 remains in operation.
- the circulating water F10 is supplied to the evaporation passage 301 of the steam generator 4 by the water pump 8 .
- the anode exhaust gas F06 is supplied to the anode exhaust gas channel 302 of the steam generator 4 via the anode exhaust gas channel 302 .
- Thermal energy is applied to the circulating water F10 in the evaporation channel 301 from the anode exhaust gas channel 302 and the auxiliary heating device 303 . Thereby, in the steam generator 4, the steam F11 is stably generated.
- the fuel gas F02 flowing through the fuel gas system 202 is the water vapor F11 and the anode circulating gas F09.
- the fuel gas F02 undergoes a slight CH4 production reaction as the temperature drops, but most of the H2 component remains and becomes the anode exhaust gas F06 to generate steam. supplied to vessel 4.
- the anode exhaust gas F06 that has flowed out of the steam generator 4 is cooled in the heat recovery cooler 10 and flows into the water separator 5 .
- water vapor in the anode exhaust gas F06 is condensed into condensed water, which is separated from the gas components of the anode exhaust gas F06.
- the gas component of the anode exhaust gas F06 flows out from the water separator 5 and flows into the anode recovery gas system 207 as the anode recovery gas F07. Since the recycled combustion gas flow rate adjustment valve 311 is fully closed, the entire amount of the anode recovery gas F07 directly becomes the anode circulation gas F09.
- the steam F11 generated by the steam generator 4 serves as a driving fluid, and the anode circulating gas F09 is sucked.
- the water vapor F11 and the anode circulating gas F09 flow out from the ejector 9 as the fuel gas F02 and are supplied to the reformer 2 and the fuel cell stack 1 through the fuel gas system 202 . That is, in the fuel cell system 100 at this point, the gas in the anode system circulates while the generation, supply and condensation of water vapor are repeated.
- the flow rate of the oxidant F03 supplied to the cathode 1c is set to an appropriate flow rate according to conditions such as the rate of temperature drop of the fuel cell stack 1 and the reformer 2. Due to the transfer of sensible heat due to the circulation of the oxidant F03, the temperatures of the fuel cell stack 1 and the reformer 2 are lowered.
- the anode system is purged with the oxidizing agent F03, or Open the closed loop of the anode system to the atmosphere.
- the temperature of the fuel cell stack 1 is acquired based on the detection signal of the stack temperature sensor 22 .
- the temperature of the reformer 2 is acquired based on the detection signal of the reformer temperature sensor 24 .
- the purging of the anode system is performed by introducing the oxidant F03 into the fuel gas system 202 under the control of the controller 90 .
- a route for introducing the oxidant F03 into the fuel gas system 202 is not shown in FIG.
- the closed-loop opening of the anode system to the atmosphere is performed by opening the recycled combustion gas flow control valve 311 under the control of the control unit 90 .
- the raw material F00 may be introduced into the fuel gas system 202 and purged with the raw material F00. Further, after purging the anode system with the oxidizing agent F03 or the raw material F00, the anode system may be cut off from the atmosphere to form a closed loop.
- control unit 90 stops the auxiliary heating device 303 and the water pump 8. This stops the generation of water vapor. Through the above procedure, the fuel cell system 100 is stopped.
- the steam generator 4 can generate a required flow rate of steam without starting the combustor 3 .
- the generated water vapor circulates through the anode system by the driving force of the ejector 9 . That is, water vapor serves as a medium, and the gas composition immediately after the fuel cell system 100 is stopped is generally maintained. Therefore, the temperature of the reformer 2 and the fuel cell stack 1 can be lowered in a reducing atmosphere by the fuel gas F02 and the reformed gas F05. As a result, the temperature of each device of the fuel cell system 100 can be efficiently lowered while maintaining the gas atmosphere in each system of the fuel cell system 100 .
- the fuel cell system 100 further includes the water separator 5, the recovery branch section 221, and the recycled combustion gas flow control valve 311.
- the water separator 5 is configured to separate the anode exhaust gas F06 into condensed water and the anode recovery gas F07.
- the recovery branch part 221 is configured to split the anode recovery gas F07 into a recycled combustion gas F08 supplied to the combustor 3 thermally connected to the reformer 2 and an anode circulation gas F09. there is
- the recycled combustion gas flow control valve 311 is configured to cut off the supply of the recycled combustion gas F08 to the combustor 3 .
- the control unit 90 stops the generation of electric energy in the fuel cell stack 1, closes the recycled combustion gas flow rate adjustment valve 311, and controls the auxiliary heating device 303 to reduce the flow rate of the steam F11.
- the temperature of the reformer 2 and the fuel cell stack 1 is lowered.
- the recycled combustion gas flow rate adjustment valve 311 is an example of a cutoff section.
- the fuel cell system 100 further includes an anode exhaust gas temperature sensor 21 that detects the temperature of the anode exhaust gas F06.
- the controller 90 controls the auxiliary heating device 303 based on the temperature of the anode exhaust gas F06. According to this configuration, it is possible to prevent excessive heat energy from being applied to the circulating water F10.
- the fuel cell system 100 further includes a water vapor temperature sensor 20 that detects the temperature of the water vapor F11.
- the controller 90 controls the auxiliary heating device 303 based on the temperature of the steam F11. According to this configuration, it is possible to prevent excessive heat energy from being applied to the circulating water F10.
- the controller 90 may open the recycled combustion gas flow control valve 311 after the temperature of the fuel cell stack 1 has decreased to the second temperature. After the temperature of the fuel cell stack 1 has decreased to the second temperature, the control unit 90 introduces the oxidant F03 or the raw material F00 into the anode system, for example, the fuel gas system 202 passing through the reformer 2 and the anode 1a. You may do so.
- FIG. 10 is a system diagram showing the configuration of the fuel cell system according to this embodiment.
- the fuel cell stack 1 is provided with a circulation heat exchanger 23 .
- the circulation heat exchanger 23 is arranged between the steam generator 4 and the heat recovery cooler 10 of the anode exhaust gas system 206 and between the recovery branch 221 of the anode circulation gas system 209 and the ejector 9.
- Other configurations are the same as those of the second embodiment shown in FIG.
- the circulation heat exchanger 23 heat is exchanged between the anode exhaust gas F06 flowing through the anode exhaust gas system 206 and the anode circulating gas F09 flowing through the anode circulating gas system 209.
- the anode circulating gas F09 obtains heat energy from the anode exhaust gas F06 flowing out of the steam generator 4 in the circulating heat exchanger 23 . This increases the temperature of the anode circulating gas F09.
- the anode recovery gas F07 immediately after flowing out of the water separator 5 is saturated steam, whereas the anode circulation gas F09 that has passed through the circulation heat exchanger 23 has thermal energy obtained from the anode exhaust gas F06. becomes superheated steam. Therefore, it is possible to prevent condensation from occurring in the piping from the circulation heat exchanger 23 to the ejector 9 in the anode circulation gas system 209 . Therefore, the pulsation of the anode circulating gas F09 flowing through the anode circulating gas system 209 is suppressed, and a stable fuel cell system 100 can be realized.
- each component of the fuel cell system 100 is surrounded by heat insulating material. As a result, heat radiation from each component device to the outside is suppressed.
- the cathode exhaust gas F04 is entirely supplied to the combustor 3 and used as a combustion-supporting gas, but the present invention is not limited to this.
- the cathode exhaust gas F04 is branched on the upstream side of the combustor 3, a part of the cathode exhaust gas F04 is supplied to the combustor 3, and the remaining cathode exhaust gas passes through at least one of the reformer 2 and the oxidant heat exchanger 7. You may make it heat.
- the cathode exhaust gas F04 may be branched inside the combustor 3, and the cathode exhaust gas F04 may be divided into those which are combusted together with the recycled combustion gas F08 or the auxiliary combustion fuel F16 and those which are not combusted. Furthermore, you may combine these. This makes it possible to realize combustion conditions with an appropriate air ratio.
- the timing of starting the operation of the auxiliary heating device 303 and the timing of the operation of the water pump 8 are not limited to the above contents.
- the auxiliary heating device 303 may be operated.
- water can be used as the cooling medium F14 that flows through the heat recovery system 214.
- the cooling medium F14 may be a refrigerant or a heat storage material as long as it can take thermal energy from the anode exhaust gas F06.
- the water treatment device 14 for example, an ion exchange device using an ion exchange resin can be used.
- the water treatment device 14 may use a permeable membrane, or may be only a filter depending on the required specifications. Also, if there is no need, the water treatment device 14 may not be installed.
- the evaporation flow path 301 is formed in a spiral shape with a space between each round.
- the evaporation channel 301 may be formed in a spiral shape that is in close contact with no gaps. In this case, since the heat transfer area per unit length in the axial direction of the steam generator 4 is increased, the heat transfer performance of the steam generator 4 is improved.
- the condensation temperature of the anode exhaust gas F06 in the water separator 5 is approximately 60°C.
- the condensation temperature of the anode exhaust gas F06 in the water separator 5 is not limited to this, and may be other temperatures.
- the condensation temperature of the anode exhaust gas F06 in the water separator 5 is desirably set so that the amount of condensed water per hour of the anode exhaust gas F06 in the water separator 5 is equal to or higher than the flow rate of the circulating water F10. In this case, it becomes unnecessary to supply water to the fuel cell system 100 from the outside after the fuel cell system 100 is activated. Therefore, the fuel cell system 100 can be water independent, and the operating cost of the fuel cell system 100 can be reduced.
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Abstract
Description
実施の形態1に係る燃料電池システムについて説明する。図1は、本実施の形態に係る燃料電池システムの構成を示す系統図である。まず、本実施の形態に係る燃料電池システム100の基本構成について説明する。
CO+H2O ⇔ CO2+H2 ・・・(2)
1/2 O2+2e- → O2- ・・・(4)
実施の形態2に係る燃料電池システムについて説明する。図6は、本実施の形態に係る燃料電池システムの構成を示す系統図である。図7は、本実施の形態に係る燃料電池システムにおける蒸気発生器の内部構造を示す断面図である。本実施の形態は、補助加熱装置303が補助燃焼器50及び燃焼排ガス流路314を有している点で、実施の形態1と異なっている。なお、実施の形態1と同様の機能及び作用を有する構成要素については、同一の符号を付してその説明を省略する。
実施の形態3に係る燃料電池システム及びその運転方法について説明する。本実施の形態は、主に燃料電池システム100の起動時の動作に関する。図8は、本実施の形態に係る燃料電池システムの構成を示す系統図である。
実施の形態4に係る燃料電池システム及びその運転方法について説明する。本実施の形態は、主に燃料電池システム100の停止時の動作に関する。本実施の形態に係る燃料電池システム100の構成は、図8に示した実施の形態3に係る燃料電池システム100の構成と同様である。すなわち、本実施の形態に係る燃料電池システム100は、実施の形態3に係る燃料電池システム100と同様に、スタック温度センサ22及び改質器温度センサ24を有している。
実施の形態5に係る燃料電池システム及びその運転方法について説明する。図10は、本実施の形態に係る燃料電池システムの構成を示す系統図である。
Claims (15)
- 水を加熱して水蒸気を発生させる蒸気発生器と、
前記水蒸気と炭化水素とを反応させ、水素を含む改質ガスを生成する改質部と、
アノードとカソードとを有し、前記アノードに供給された前記改質ガスと、前記カソードに供給された酸化剤と、の電気化学反応によって電気エネルギを発生させる燃料電池スタックと、
前記炭化水素を含む原料と、前記アノードから排出されたアノード排ガスの一部を回収したアノード循環ガスと、の少なくとも一方を、前記水蒸気を駆動流体として用いて前記改質部に供給するエジェクタと、
を備え、
前記蒸気発生器は、
前記水が流通する蒸発流路と、
前記蒸発流路と熱的に接続され、前記アノード排ガスが流通するアノード排ガス流路と、
前記水を加熱する補助加熱装置と、を有しており、
前記アノード排ガス流路及び前記補助加熱装置は、前記蒸発流路を挟んで互いに対向している燃料電池システム。 - 前記蒸発流路は、上下方向に対して斜めに延伸しており、
前記蒸発流路には、上流側から下流側に向かって下り勾配が生じている請求項1に記載の燃料電池システム。 - 前記アノード排ガス流路は、上下方向に沿って延伸しており、
前記蒸気発生器は、
上下方向に沿って延伸し、前記アノード排ガス流路を画定する流路壁と、
前記流路壁を貫通して前記アノード排ガス流路に接続され、前記アノード排ガスが流入する流入管と、
前記流入管よりも上方で前記アノード排ガス流路に接続され、前記アノード排ガスが流出する流出管と、
を有しており、
前記アノード排ガス流路において前記流入管よりも下方には、結露水を溜める結露水貯留空間が設けられている請求項1又は請求項2に記載の燃料電池システム。 - 前記流入管は、前記アノード排ガス流路に面した端面を有しており、
前記端面は、前記流路壁の内壁面よりも、前記アノード排ガス流路の内部側に突出している請求項3に記載の燃料電池システム。 - 前記アノード排ガス流路において前記流入管よりも上方には、結露水を誘導する結露水誘導板が設けられている請求項3に記載の燃料電池システム。
- 前記補助加熱装置は、電気ヒータを有している請求項1~請求項5のいずれか一項に記載の燃料電池システム。
- 前記補助加熱装置は、補助燃焼器と、前記補助燃焼器で発生した燃焼排ガスが流通する燃焼排ガス流路と、を有している請求項1~請求項5のいずれか一項に記載の燃料電池システム。
- 前記アノード排ガスの温度を検出するアノード排ガス温度センサと、
制御部と、
をさらに備え、
前記制御部は、前記アノード排ガスの温度に基づいて前記補助加熱装置を制御する請求項1~請求項7のいずれか一項に記載の燃料電池システム。 - 前記水蒸気の温度を検出する水蒸気温度センサと、
制御部と、
をさらに備え、
前記制御部は、前記水蒸気の温度に基づいて前記補助加熱装置を制御する請求項1~請求項7のいずれか一項に記載の燃料電池システム。 - 前記燃料電池スタックの温度を検出するスタック温度センサをさらに備え、
前記制御部は、燃料電池システムを起動するとき、前記改質部への前記水蒸気の供給が特定の期間に開始されるように前記補助加熱装置を制御し、
前記特定の期間は、前記燃料電池スタックの温度が第1温度まで上昇した後であって、かつ前記燃料電池スタックの温度が前記第1温度より高い第2温度まで上昇するよりも前である請求項8又は請求項9に記載の燃料電池システム。 - 前記燃料電池スタックの温度を検出するスタック温度センサと、
制御部と、
をさらに備え、
前記制御部は、燃料電池システムを起動するとき、前記改質部への前記水蒸気の供給が特定の期間に開始されるように前記補助加熱装置を制御し、
前記特定の期間は、前記燃料電池スタックの温度が第1温度まで上昇した後であって、かつ前記燃料電池スタックの温度が前記第1温度より高い第2温度まで上昇するよりも前である請求項1~請求項7のいずれか一項に記載の燃料電池システム。 - 前記第1温度は150℃であり、前記第2温度は300℃である請求項10又は請求項11に記載の燃料電池システム。
- 前記アノード排ガスを凝縮水とアノード回収ガスとに分離する水分離器と、
前記アノード回収ガスを、前記改質部に熱的に接続された燃焼器に供給されるリサイクル燃焼ガスと、前記アノード循環ガスと、に分流させる回収分岐部と、
前記燃焼器への前記リサイクル燃焼ガスの供給を遮断する遮断部と、
をさらに備え、
前記制御部は、燃料電池システムを停止するとき、前記燃料電池スタックにおける前記電気エネルギの発生を停止させ、前記遮断部を閉じ、前記補助加熱装置を制御して前記水蒸気の流量を確保し、前記改質部及び前記燃料電池スタックを降温させる請求項10~請求項12のいずれか一項に記載の燃料電池システム。 - 前記制御部は、前記燃料電池スタックの温度が前記第2温度まで低下した後に、前記遮断部を開放する請求項13に記載の燃料電池システム。
- 前記制御部は、前記燃料電池スタックの温度が前記第2温度まで低下した後に、前記改質部及び前記アノードを通るアノード系統に、前記酸化剤又は前記原料を導入する請求項13又は請求項14に記載の燃料電池システム。
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JP2006076850A (ja) * | 2004-09-10 | 2006-03-23 | Nippon Oil Corp | 改質装置および方法ならびに燃料電池システム |
JP2011009195A (ja) * | 2009-05-28 | 2011-01-13 | Toto Ltd | 固体電解質型燃料電池 |
JP2011204390A (ja) * | 2010-03-24 | 2011-10-13 | Osaka Gas Co Ltd | 固体酸化物形燃料電池システム及びこれを備えたコージェネレーションシステム |
JP6824485B1 (ja) * | 2020-03-30 | 2021-02-03 | 三菱電機株式会社 | 燃料電池システム |
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JP2006076850A (ja) * | 2004-09-10 | 2006-03-23 | Nippon Oil Corp | 改質装置および方法ならびに燃料電池システム |
JP2011009195A (ja) * | 2009-05-28 | 2011-01-13 | Toto Ltd | 固体電解質型燃料電池 |
JP2011204390A (ja) * | 2010-03-24 | 2011-10-13 | Osaka Gas Co Ltd | 固体酸化物形燃料電池システム及びこれを備えたコージェネレーションシステム |
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