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WO2013069973A1 - Système de pile à combustible et procédé de fonctionnement - Google Patents

Système de pile à combustible et procédé de fonctionnement Download PDF

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Publication number
WO2013069973A1
WO2013069973A1 PCT/KR2012/009371 KR2012009371W WO2013069973A1 WO 2013069973 A1 WO2013069973 A1 WO 2013069973A1 KR 2012009371 W KR2012009371 W KR 2012009371W WO 2013069973 A1 WO2013069973 A1 WO 2013069973A1
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WIPO (PCT)
Prior art keywords
fuel cell
reformed
heat exchanger
reformer
gas
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Ceased
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PCT/KR2012/009371
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English (en)
Korean (ko)
Inventor
권준택
이수재
전희권
노창수
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GS Caltex Corp
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GS Caltex Corp
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    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
    • H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
    • H01M8/04119—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying
    • H01M8/04126—Humidifying
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/04694—Processes for controlling fuel cells or fuel cell systems characterised by variables to be controlled
    • H01M8/04701—Temperature
    • H01M8/04708—Temperature of fuel cell reactants
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/04694—Processes for controlling fuel cells or fuel cell systems characterised by variables to be controlled
    • H01M8/04746—Pressure; Flow
    • H01M8/04776—Pressure; Flow at auxiliary devices, e.g. reformer, compressor, burner
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
    • H01M8/04694—Processes for controlling fuel cells or fuel cell systems characterised by variables to be controlled
    • H01M8/04828—Humidity; Water content
    • H01M8/04835—Humidity; Water content of fuel cell reactants
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
    • H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/10—Fuel cells with solid electrolytes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/066—Integration with other chemical processes with fuel cells
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/10—Fuel cells with solid electrolytes
    • H01M2008/1095—Fuel cells with polymeric electrolytes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/50—Fuel cells

Definitions

  • the present invention relates to a fuel cell system, and more particularly, a fuel cell system that does not require a separate membrane humidifier by allowing the fuel cell stack to be humidified by moisture contained in the reformed gas supplied to the fuel cell stack. It is about.
  • a fuel cell is a battery that generates power by supplying fuel (hydrogen gas or hydrocarbon) to the cathode and air (oxygen) to the anode from the outside.
  • the power generation method using a fuel cell is a method of directly converting an energy difference before and after the reaction into electrical energy through an electrochemical reaction between hydrogen and oxygen without undergoing a combustion (oxidation) reaction of the fuel.
  • the fuel cell is a clean power generation system that generates no NOx and SOx, and has no noise and vibration, and its thermal efficiency is 80% or more combined with the amount of electricity generation and heat recovery, and does not generate harmful gases such as NOx or SOx. Can be.
  • Conventionally known fuel cell systems include a mobile power generation system using hydrogen gas stored in a hydrogen bomb as a fuel, and a fuel cell system using a liquid fuel that is mobile and easily exchangeable.
  • a domestic power generation system using liquefied natural gas as fuel is a domestic power generation system using liquefied natural gas as fuel.
  • Patent Document 1 schematically shows a conventional domestic fuel cell system, which is disclosed in Japanese Patent Laid-Open No. 2003-187832 (Patent Document 1).
  • the fuel cell system includes a fuel processor 1 to 4 for reforming a hydrocarbon-based fuel such as city gas, LPG, kerosene, and the like into the fuel cell stack 5.
  • a fuel cell stack 5 for generating electricity by an electrochemical reaction using reformed gas, a power converter (not shown) for converting the generated direct current into an alternating current, and fuel gas, air, and water It is configured to include a pump and a peripheral device such as a valve and a sensor to supply the battery system.
  • a fuel converter includes a reformer 2 for reacting fuel gas with water vapor to generate hydrogen, and a CO transformer for removing carbon monoxide so that the generated gas does not poison the catalyst of the fuel cell stack. a shift converter 3 and a CO remover 4.
  • the reformed gas purified to the required level through the fuel converter is supplied to the fuel cell stack 5, and hydrogen is hydrogen ions (H +) at the anode of each unit cell constituting the fuel cell stack 5. They are decomposed into electrons (e-), which move to the cathode through the electrolyte membrane and the outer conductor, respectively, and combine with oxygen in the air supplied to the cathode to generate water.
  • a current is generated by the flow of electrons, and heat is incidentally generated in the water generation reaction, and the generated current is converted to alternating current using a power converter as a direct current, and the generated heat is used for a predetermined heat exchanger.
  • the heat storage is stored as hot water and used for hot water supply and heating as needed.
  • one of the factors that directly affect the performance during operation of the fuel cell system is a certain amount of more than a certain amount of ionomers in the electrolyte membrane and catalyst layer of the membrane electrode assembly (MEA), which is a key component of the fuel cell system.
  • MEA membrane electrode assembly
  • Patent Document 2 Japanese Patent Laid-Open No. 2011-086543
  • the present invention has been made to solve the problems described above, an embodiment of the present invention is supplied to the fuel cell stack by adjusting the steam to carbon ratio (S / C) of the reformed water is introduced into the reformer It is an object of the present invention to provide a fuel cell system capable of controlling the temperature and humidity of a reformed gas and which does not require a separate humidifying means such as a conventional membrane humidifier.
  • a fuel cell system characterized in that the reformed gas passing through the reformer flows into the fuel cell stack via a heat exchanger.
  • the present invention provides a fuel cell system as follows.
  • a fuel cell stack including a reformed gas supplied through a reformer and generating electricity by an electrochemical reaction, wherein the fuel cell stack is humidified by moisture contained in the reformed gas, and is charged into the reformer.
  • a fuel cell system characterized in that for controlling the temperature and humidity of the reformed gas supplied to the fuel cell stack by adjusting the steam to carbon ratio (S / C) of the reformed water.
  • CO reformer for receiving a reformed gas from the reformer to reduce the carbon monoxide contained in the reformed gas by a shift reaction; And a CO remover for selectively oxidizing and removing carbon monoxide contained in the reformed gas by receiving the reformed gas passing through the CO transformer, wherein the operating temperature of the CO remover is 100 ° C to 180 ° C. Battery system.
  • the fuel cell stack A fuel cell system, characterized in that it is temperature controlled by the cathode off gas discharged from, or temperature controlled by the exhaust gas discharged from the burner of the reformer, or temperature controlled by both the cathode off gas and the exhaust gas.
  • the reformed gas passing through the second heat exchanger is discharged from the fuel cell stack in the process of passing through the first heat exchanger
  • a fuel cell system characterized in that the temperature and humidity of the reformed gas is controlled by heat exchange with the cooling water and the cathode off gas, or the temperature and humidity of the reformed gas is controlled by heat exchange with any one of the coolant and the cathode off gas.
  • a fuel cell system wherein the reformed gas passing through the reformer passes through the first heat exchanger, the heat exchange with the cooling water and the cathode off gas discharged from the fuel cell stack to control the temperature and humidity of the reformed gas
  • a fuel cell system characterized in that the temperature and humidity of the reformed gas is controlled by heat exchange with any one of the cooling water and the cathode off gas.
  • the second heat exchanger is installed on a flow path provided with one of the cooling water and the cathode off gas discharged from the fuel cell stack, or the cooling water and the cathode off gas flows to the first heat exchanger, And a reformed water that receives heat from either of the coolant and the cathode off gas or the coolant and the cathode off gas in the second heat exchanger is supplied to the reformer.
  • the present invention provides a fuel cell operating method as follows.
  • the operating temperature of the CO remover is 100 ⁇ 180 fuel cell operating method.
  • the S / C of the reforming water is 2.5 ⁇ 4.0 fuel cell operating method.
  • the reformed water is temperature controlled by at least one of a cathode open gas discharged from a fuel cell stack and an exhaust gas discharged from a burner of the reformer.
  • the reformed water in the second heat exchanger is installed on the flow path is provided so that any one of the cooling water and the cathode open gas discharged from the fuel cell stack flows to the first heat exchanger.
  • the fuel cell operating method further comprising the step of being supplied to the reformer after receiving the heat by any one of.
  • the fuel cell stack includes a fuel cell stack supplied with reformed gas passing through a reformer to generate electricity by an electrochemical reaction, and the humidification of the fuel cell stack is controlled by moisture contained in the reformed gas.
  • the fuel cell system is provided to control the temperature and humidity of the reformed gas supplied to the fuel cell stack by adjusting the steam to carbon ratio (S / C) of the reformed water introduced into the reformer.
  • the S / C can be adjusted in the range of 2.5 ⁇ 4.0.
  • a CO transformer for receiving a reforming gas from the reformer to reduce the carbon monoxide contained in the reforming gas by a shift reaction; And a CO remover for selectively oxidizing and removing carbon monoxide contained in the reformed gas by receiving the reformed gas passed through the CO transformer.
  • the operating temperature of the CO remover is, for example, 100 ° C to 180 ° C.
  • a first heat exchanger is installed between the reformer and the fuel cell stack, or between the CO remover and the fuel cell stack, so that at least one of temperature and humidity of the reformed gas passing through the reformer is controlled. Can be.
  • reforming water that receives heat from the reforming gas in the first heat exchanger may be supplied to the reformer.
  • the flow rate (S / C) of the reformed water introduced into the reformer it is possible to control at least one of the temperature and humidity of the reformed gas supplied to the fuel cell stack. Can be.
  • the coolant may be supplied to the reformer after receiving heat from the reformed gas and used for the reforming reaction. There is an effect that the overall efficiency of the is improved.
  • FIG. 1 is a block diagram of a conventional fuel cell system.
  • FIG. 2 is a block diagram of a fuel cell system according to a first embodiment of the present invention.
  • FIG. 3 is a flow chart showing a method for controlling the temperature of the CO remover by controlling the flow rate of the reformed water.
  • Figure 4 is a flow chart illustrating a method for controlling the temperature of the CO remover by air cooling fan operation control.
  • FIG. 5 is a flow chart illustrating a method for controlling the temperature of the CO remover by controlling the burner gas amount.
  • FIG. 6 is a configuration diagram of a fuel cell system according to a second embodiment of the present invention.
  • FIG. 7 is a configuration diagram of a fuel cell system according to a third embodiment of the present invention.
  • FIG. 8 is a configuration diagram of a fuel cell system according to a fourth embodiment of the present invention.
  • FIG. 9 is a configuration diagram of a fuel cell system according to a fifth embodiment of the present invention.
  • FIG. 10 is a configuration diagram of a fuel cell system according to a sixth embodiment of the present invention.
  • FIG. 11 is a configuration diagram of a fuel cell system according to a seventh embodiment of the present invention.
  • FIG. 12 is a configuration diagram of a fuel cell system according to an eighth embodiment of the present invention.
  • FIG. 13 is a configuration diagram of a fuel cell system according to a ninth embodiment of the present invention.
  • 16 is a 50% load operation result of the output 1KW system as a third experimental example of the present invention.
  • 17 is a 30% load operation result of the output 1KW system as a fourth experimental example of the present invention.
  • FIG. 2 is a configuration diagram of a fuel cell system according to a first embodiment of the present invention.
  • the fuel cell system includes a reformer 10, a CO transformer 20, a CO remover 30, and a fuel cell stack 40.
  • natural gas which is mainly used as fuel gas, has a different content of sulfur (S) depending on the production region or gas refinery, but methane (CH4) is a main component of city gas.
  • methane CH4
  • THT tetra-hydro-thiophene
  • TBM tertiary-butylmercaptan
  • the sulfur component is preferably removed because the catalyst of the reformer 10 and the fuel cell stack 40 deteriorates even at a content of about several tens of ppm.
  • the fuel gas may first go through a desulfurizer (not shown), and the desulfurizer removes sulfur from the fuel gas by the following desulfurization reaction.
  • the reformer 10 reacts the fuel gas with steam to reform the reformed gas into a reformed gas mainly composed of hydrogen.
  • the reformer 10 generates hydrogen by the following methane-steam reforming reaction.
  • the reforming reaction is an endothermic reaction, and the necessary heat is supplied from a heating burner (not shown) installed at one side of the reformer 10, and the heating burner is burned by receiving burner gas and air.
  • the burner gas for combustion supplied to the heating burner is preferably the same hydrocarbon-based fuel as the fuel gas supplied to the reformer 10.
  • the CO concentration of the reformed gas produced by the reforming reaction is about 10-15%, and in the case of the polymer fuel cell (PEMFC), the CO concentration needs to be lowered further due to the electrode characteristics.
  • the reformed gas from the reformer 10 enters the CO transformer 20, where the CO transformer 20 converts CO in the reformed gas into carbon dioxide and generates hydrogen through a CO modification reaction below.
  • the CO content in the reformed gas is reduced to less than 1%, more preferably to about 0.5%.
  • the CO denaturation reaction is governed by the equilibrium, and the reaction composition is determined by temperature and pressure. It is an exothermic reaction in the direction of producing a low temperature is advantageous.
  • an endothermic reaction which is an endothermic reaction, consumes hydrogen to generate CO. If necessary, the CO concentration is reduced through two steps, a high-temperature water-gas shift (HTS) reaction and a low-temperature water-gas shift (LTS) reaction.
  • HTS high-temperature water-gas shift
  • LTS low-temperature water-gas shift
  • the HTS reactor reduces the CO concentration by 10% or more to 5% or less using a Cr / Fe-based catalyst at around 500 ° C.
  • the CO concentration is reduced to about 0.5 using a Cu-based catalyst at around 200 ° C. Can be reduced to about%.
  • the CO remover 30 removes and purifies CO to ppm by the selective oxidation reaction as follows.
  • Selective oxidation reactions are generally performed on reformed gases containing 0.5 to 1% of CO.
  • a ratio of about 1 to 3 is added to the air containing a small amount of oxygen to selectively react only CO without oxidizing the excess hydrogen in the reformed gas requires a high conversion catalyst.
  • the temperature of the catalyst layer may increase during the reaction.
  • the reaction temperature is increased, the oxidation reaction of hydrogen and the reverse water gas shift reaction may occur, and thus the CO selective oxidative property may be lowered, so that the oxygen distribution is uniformed to reduce the consumption of hydrogen and the selective oxidation of CO. Therefore, recently, a multistage air supply system is used, or a reactor having a different catalyst for each stage may be used.
  • the catalyst of the CO remover 30 is, for example It is desirable to be able to use continuously at an operating temperature of 100 °C ⁇ 180 °C, such as, if the operating temperature of the CO remover 30 is lower than 100 °C may not occur the catalytic reaction, if it exceeds 180 °C methanation as follows Because the reaction appears.
  • a heat exchanger (C) between the CO transformer 20 and the CO remover 30 may be used.
  • the operation temperature of the CO remover 30 is increased to 100 ° C. or more at which water vaporizes, thereby requiring a separate heat exchanger.
  • Moisture can be prevented from condensing, and the humidification (RH%) condition of the fuel cell stack 40 is 80% to 120% using moisture contained in the reformed gas that has passed through the CO remover 30. Can be controlled.
  • the reformed gas passing through the CO remover 30 contains moisture which is not condensed in the CO remover 30, and thus, when the reformed gas is supplied to the fuel cell stack 40, Humidification of the fuel cell stack 40 is made.
  • the reformed gas purified to the required level CO (carbon monoxide) by the above-described method is supplied to the fuel cell stack 40.
  • a first heat exchanger 50 is installed between the CO remover 30 and the fuel cell stack 40 to cool the reformed gas passing through the CO remover 30.
  • the first heat exchanger 50 is supplied with cooling water from inside or outside the fuel cell system.
  • the first heat exchanger 50 may include, for example, a chamber having a cooling water inlet and an outlet, and a capillary tube installed in the chamber, and the reformed gas passing through the CO remover 30 may be formed in a first heat exchange along the capillary tube. Pass the flag 50.
  • the coolant is introduced into the chamber through the inlet of the coolant, receives heat from the reformed gas flowing through the capillary tube in the process of passing through the first heat exchanger 50, and opens the first heat exchanger 50 through the coolant outlet.
  • the cooling water is supplied to the reformer 10 through the water supply passage 51 as reforming water and used for the steam reaction of the reformer 10.
  • the operating temperature of the CO remover 30 is 100 ° C. or more (100 ° C. in which water is vaporized). ° C ⁇ 180 ° C), it will be described below how to control the operating temperature of the CO remover (30).
  • the controller 70 may control the amount of reformed water supplied to the first heat exchanger 50 so that the operating temperature of the CO remover 30 maintains an appropriate range (eg, 100 ° C. to 180 ° C.). There is, but it is preferable to adjust in the range of S / C 2.5 ⁇ 4.0.
  • the efficiency of the reformer 10 is reduced due to lack of water, while the humidification (RH%) of the reformed gas supplied to the fuel cell stack 40 falls below 80%, and the S / C When it exceeds 4.0, the excess water supply reduces the efficiency of the entire fuel cell system as the heater for steaming the reformed water is operated inside the reformer, while reducing the efficiency of the reformed gas supplied to the fuel cell stack 40. This is because humidification increases to more than 120%.
  • FIG. 3 is a flowchart illustrating a method of controlling the temperature of the CO remover 30 by controlling the flow rate of the reformed water.
  • the temperature of the CO remover 30 is measured (S10). At this time, the temperature measurement is made by a temperature sensor (not shown) installed in the CO remover 30, the measured value is sent to the controller (70).
  • the controller 70 determines whether the measured temperature of the CO remover 30 is within an appropriate temperature range (for example, 100 ° C. to 180 ° C.) (S20). At this time, the appropriate temperature range is preferably input in advance to the controller (70).
  • an appropriate temperature range for example, 100 ° C. to 180 ° C.
  • the controller 70 reduces the flow rate (S / C) of the reformed water supplied to the first heat exchanger 50 (S40), and if it exceeds the normal operating temperature range, the flow rate of the reformed water is exceeded.
  • Increase (S50) the increase and decrease of the reformed water may be set in advance to be determined corresponding to the measured temperature of the CO remover 30, and further, until the temperature of the CO remover 30 reaches the normal operating temperature range. It is also possible to circulate the reformed gas passed through) back to the reformer 10 through a recirculation line.
  • Figure 4 is a flow chart illustrating a method for controlling the temperature of the CO remover by the air cooling fan operation control.
  • an air cooling fan (not shown) installed in the CO remover 30 may be used to control the operating temperature of the CO remover 30 to an appropriate range.
  • the controller 70 determines whether the measured temperature of the CO remover 30 is within an appropriate temperature range (for example, 100 ° C. to 180 ° C.) (S20). At this time, the appropriate temperature range is preferably input in advance to the controller (70).
  • an appropriate temperature range for example, 100 ° C. to 180 ° C.
  • the controller 70 decreases the number of revolutions of the air cooling fan installed in the CO remover 30 (S40 ').
  • the number of revolutions of the air cooling fan is increased (S50). ').
  • the amount of increase and decrease of the rotation speed of the air cooling fan may be set in advance so as to correspond to the measured temperature of the CO remover 30, and further, the CO remover until the temperature of the CO remover 30 reaches a normal operating temperature range. It is also possible to circulate the reformed gas passed through 30 back to the reformer 10 through a recirculation line.
  • FIG. 5 is a flowchart illustrating a method of controlling the temperature of the CO remover by controlling the burner gas amount.
  • the operating temperature range control of the CO remover 30 can be achieved by adjusting the amount of burner gas supplied to a heating burner (not shown) installed in the reformer 10.
  • the temperature of the CO remover 30 is measured (S10). At this time, the temperature measurement is made by a temperature sensor (not shown) installed in the CO remover 30, the measured value is sent to the controller (70).
  • the controller 70 determines whether the measured temperature of the CO remover 30 is within an appropriate temperature range (for example, 100 ° C. to 180 ° C.) (S20). At this time, the appropriate temperature range is preferably input in advance to the controller (70).
  • an appropriate temperature range for example, 100 ° C. to 180 ° C.
  • the amount of heat source supplied to the reformer is increased by increasing the amount of burner gas supplied to the heating burner by the controller 70 (S40 "), and if the temperature exceeds the normal operating temperature range, the burner is supplied to the heating burner. Reduce the amount of gas (S50 ").
  • the increase and decrease amount of the burner gas may be set in advance to correspond to the measured temperature of the CO remover 30, and further, the CO remover 30 until the temperature of the CO remover 30 reaches a normal operating temperature range. It is also possible to circulate the reformed gas passed back to the reformer 10 through a recirculation line.
  • FIG. 6 is a configuration diagram of a fuel cell system according to a second embodiment of the present invention.
  • the controller 70 is omitted for convenience.
  • the fuel cell system according to the second embodiment of the present invention is almost similar to the first embodiment described above, except that the reformed water supplied from the water tank 60 to the first heat exchanger 50 is a burner of the reformer 10. There is a difference in that the temperature is controlled by the exhaust gas discharged from 11 and the cathode off gas of the fuel cell stack 40 or by either the exhaust gas and the cathode off gas.
  • the water tank 60 stores the condensed water in the fuel cell system, or supplies the water supplied from the outside, or stores the condensed water and the supplied water together.
  • the water tank 60 is heated by a separate heater (not shown), heat exchanged with the exhaust gas of the burner 11, or heat exchanged with the cathode off gas of the fuel cell stack 40, or exhaust gas and By heat-exchanging with both the cathode off-gas, the temperature of the reformed water supplied from the water tank 60 to the first heat exchanger 50 is adjusted, and the temperature and humidity in the process of passing the reformed gas through the first heat exchanger 50. Is adjusted and supplied to the fuel cell stack 40.
  • the operation temperature control of the CO remover 30, as described above can be made by adjusting the flow rate of the reformed water, the operation control of the air cooling fan, or the gas amount control of the burner (11).
  • FIG. 7 is a configuration diagram of a fuel cell system according to a third embodiment of the present invention.
  • the fuel cell system according to the third embodiment of the present invention is almost similar to the first embodiment described above, except that a knock-out drum 80 is installed at one side of the first heat exchanger 50. Thus, there is a difference in that the amount of humidification supplied to the fuel cell stack 40 can be controlled by the knock-out drum 80.
  • the operation temperature control of the CO remover 30 can be made by adjusting the flow rate of the reformed water, the operation control of the air cooling fan, or the gas amount control of the burner 11 as described above.
  • FIG. 8 is a configuration diagram of a fuel cell system according to a fourth embodiment of the present invention.
  • the exhaust gas is discharged from the burner 11 of the reformer 10 in the course of passing the reformed gas through the first heat exchanger 50.
  • the heat exchange with the gas thereby controlling the temperature and humidity of the reformed gas supplied to the fuel cell stack 40.
  • the operation temperature control of the CO remover 30 may be performed by adjusting the flow rate of the reformed water, controlling the operation of the air cooling fan, or controlling the gas amount of the burner 11.
  • FIG. 9 is a configuration diagram of a fuel cell system according to a fifth embodiment of the present invention.
  • the fuel cell system according to the fifth embodiment of the present invention is almost similar to the fourth embodiment described above, except that the second heat exchanger 52 is installed in the flow path between the first heat exchanger 50 and the burner 11. There is a difference in that.
  • the exhaust gas of the burner 11 first enters the first heat exchanger 56 after heat exchange with the reformed water while passing through the second heat exchanger 52, and from the exhaust gas in the second heat exchanger 52.
  • the reformed water received with heat is supplied to the reformer 10 and used for steam reaction.
  • the operation temperature control of the CO remover 30 can be made by adjusting the flow rate of the reformed water, the operation control of the air cooling fan, or the gas amount control of the burner 11 as described above.
  • FIG. 10 is a configuration diagram of a fuel cell system according to a sixth embodiment of the present invention.
  • the second heat exchanger 52 is installed in the flow path between the first heat exchanger 50 and the burner 11, whereas the fuel cell system according to the sixth embodiment of the present invention has a second embodiment. There is a difference in that the heat exchanger 52 is installed in the flow path between the first heat exchanger 50 and the CO remover 30.
  • the reformed water received from the reformed gas in the second heat exchanger 52 is supplied to the reformer 10 is used for the steam reaction.
  • the operation temperature control of the CO remover 30 can be made by adjusting the flow rate of the reformed water, the operation control of the air cooling fan, or the gas amount control of the burner 11 as described above.
  • FIG. 11 is a configuration diagram of a fuel cell system according to a seventh embodiment of the present invention.
  • the fuel cell system according to the seventh embodiment of the present invention is reformed gas. Heat exchanges with the coolant and the cathode off gas discharged from the fuel cell stack 40 in the course of passing through the first heat exchanger 50 or with either the coolant and the cathode off gas. There is a difference.
  • a second heat exchanger 52 is installed in the flow path between the first heat exchanger 50 and the CO remover 30, and the reformed water received from the reformed gas while passing through the second heat exchanger 54 is reformed 10. Is supplied.
  • the operation temperature control of the CO remover 30 can be made by adjusting the flow rate of the reformed water, the operation control of the air cooling fan, or the gas amount control of the burner 11 as described above.
  • FIG. 12 is a configuration diagram of a fuel cell system according to an eighth embodiment of the present invention.
  • the fuel cell system according to the eighth embodiment of the present invention has the form in which the second heat exchanger is removed in the seventh embodiment, and the temperature and humidity of the reformed gas are discharged from the fuel cell stack 40 and cathode off. It can be controlled by gas, or by either coolant and cathode off gas.
  • the operation temperature control of the CO remover 30 can be made by adjusting the flow rate of the reformed water, the operation control of the air cooling fan, or the gas amount control of the burner 11 as described above.
  • FIG. 13 is a configuration diagram of a fuel cell system according to a ninth embodiment of the present invention.
  • any one of the cooling water and the cathode off gas discharged from the fuel cell stack 40 or the cooling water and the cathode off gas is first heat exchanged in the eighth embodiment.
  • the second heat exchanger 52 is installed on the flow path entering the machine 50.
  • any one of the cooling water and the cathode off gas, or both the cooling water and the cathode off gas is discharged from the fuel cell stack 40 and then passes through the second heat exchanger 52 and then through the first heat exchanger 50.
  • the cooling water and the cathode off gas discharged from the fuel cell stack 40, or any one of the cooling water and the cathode off gas heat exchange with the reformed water in the second heat exchanger 55, the reformed water to the reformer 10 The supplied gas is used for the steam reaction, and the reformed gas is supplied to the fuel cell stack 40 by adjusting temperature and humidity in the course of passing through the first heat exchanger 50.
  • the operation temperature control of the CO remover 30 may be performed by adjusting the flow rate of the reformed water, controlling the operation of the air cooling fan, or controlling the gas amount of the burner 11.
  • Fig. 14 shows the 100% load operation result of the output 1KW system as the first experimental example of the present invention.
  • the amount of reformed water supplied to the reformer 10 via the heat exchanger 50 was maintained in the range of 2.5 to 4.0 (S / C; steam-carbon ratio), and the temperature of the reformed gas passed through the CO remover 30 was 115. It was -160 degreeC.
  • the temperature of the reformed gas supplied to the fuel cell stack 40 through the heat exchanger 50 was measured at 60 ⁇ 80 °C, the flow rate was 20 ⁇ 25lpm, the relative humidity (RH) is 80 ⁇ 120% Was measured.
  • Fig. 15 shows a 75% load operation result of the output 1KW system as the second experimental example of the present invention.
  • the amount of reformed water supplied to the reformer 10 through the heat exchanger 50 was maintained in the range of 2.5 to 4.0 (S / C; steam-carbon ratio), and the temperature of the reformed gas passed through the CO remover 30 was 110. It was -150 degreeC.
  • the temperature of the reformed gas supplied to the fuel cell stack 40 via the heat exchanger 50 was measured at 55 ⁇ 75 °C, the flow rate was 15 ⁇ 20lpm, the relative humidity (RH) is 80 ⁇ 120% Was measured.
  • Fig. 16 shows the 50% load operation result of the output 1KW system as the third experimental example of the present invention.
  • the amount of reformed water supplied to the reformer 10 through the heat exchanger 50 was maintained in the range of 2.5 to 4.0 (S / C; steam-carbon ratio), and the temperature of the reformed gas passed through the CO remover 30 was 107. It was -150 degreeC.
  • the temperature of the reformed gas supplied to the fuel cell stack 40 through the heat exchanger 50 was measured at 50 ⁇ 70 °C, the flow rate was 10 ⁇ 15lpm, the relative humidity 43-28 (RH) is 80 ⁇ Measured at 120%.
  • the amount of reformed water supplied to the reformer 10 via the heat exchanger 50 was maintained in the range of 2.5 to 4.0 (S / C; steam-carbon ratio), and the temperature of the reformed gas passed through the CO remover 30 was 105. It was -150 degreeC.
  • the temperature of the reformed gas supplied to the fuel cell stack 40 via the heat exchanger 50 was measured at 50 ⁇ 65 °C, the flow rate was 7 ⁇ 10lpm, the relative humidity (RH) is 80 ⁇ 120% Was measured.

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Abstract

La présente invention concerne un système de pile à combustible et un mode de réalisation de la présente invention propose un système de pile à combustible qui comprend un empilement de piles à combustible pour générer de l'électricité au moyen d'une réaction électrochimique lors de la réception d'une alimentation d'un gaz reformé qui est passé à travers un reformeur, l'empilement de piles à combustible étant humidifié au moyen d'une fraction d'eau contenue dans le gaz reformé, et la température et l'humidité du gaz reformé introduit dans l'empilement de piles à combustible pouvant être régulées par ajustement du rapport vapeur-à-carbone (S/C) de l'eau de reformage introduite dans le reformeur.
PCT/KR2012/009371 2011-11-08 2012-11-08 Système de pile à combustible et procédé de fonctionnement Ceased WO2013069973A1 (fr)

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KR1020110116076A KR101295237B1 (ko) 2011-11-08 2011-11-08 연료전지 시스템

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Publication number Priority date Publication date Assignee Title
US11251443B2 (en) 2015-12-18 2022-02-15 Cummins Enterprise, Llc Fuel cell system, operating method thereof and fuel cell power plant

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KR102701211B1 (ko) * 2021-09-09 2024-08-29 엘지전자 주식회사 연료전지 장치 및 그 제어방법

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JP2003252605A (ja) * 2001-12-28 2003-09-10 Matsushita Electric Ind Co Ltd 水素生成装置および燃料電池発電システム
JP2005071740A (ja) * 2003-08-22 2005-03-17 Fuji Electric Holdings Co Ltd 燃料電池発電システムとその運転方法
KR20090043354A (ko) * 2007-10-29 2009-05-06 삼성전자주식회사 연료전지의 연료처리장치

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JP2003187832A (ja) 2001-12-19 2003-07-04 Sanyo Electric Co Ltd 燃料電池システム
EP1323669A3 (fr) * 2001-12-28 2004-07-21 Matsushita Electric Industrial Co., Ltd. Dispositif de génération d'hydrogène et système de pile à combustible

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JP2003252605A (ja) * 2001-12-28 2003-09-10 Matsushita Electric Ind Co Ltd 水素生成装置および燃料電池発電システム
JP2005071740A (ja) * 2003-08-22 2005-03-17 Fuji Electric Holdings Co Ltd 燃料電池発電システムとその運転方法
KR20090043354A (ko) * 2007-10-29 2009-05-06 삼성전자주식회사 연료전지의 연료처리장치

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11251443B2 (en) 2015-12-18 2022-02-15 Cummins Enterprise, Llc Fuel cell system, operating method thereof and fuel cell power plant

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