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WO2013069973A1 - Fuel cell system and operating method - Google Patents

Fuel cell system and operating method 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
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
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PCT/KR2012/009371
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French (fr)
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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Filing date
Publication date
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Publication of WO2013069973A1 publication Critical patent/WO2013069973A1/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • 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

The present invention relates to a fuel cell system, and one embodiment of the present invention provides a fuel cell system which comprises a fuel cell stack for generating electricity by means of an electrochemical reaction upon receiving a supply of a reformed gas that has passed through a reformer, wherein the fuel cell stack is humidified by means of a water fraction contained in the reformed gas, and the temperature and humidity of the reformed gas supplied to the fuel cell stack can be controlled by adjusting the steam-to-carbon ratio (S/C) of the reforming water introduced into the reformer.

Description

연료전지 시스템 및 운전방법Fuel Cell System and Operation Method

본 발명은 연료전지 시스템에 관한 것으로, 더욱 상세하게는 연료전지 스택에 공급되는 개질가스에 함유된 수분에 의해 연료전지 스택의 가습이 이루어지도록 함으로써, 별도의 막가습기를 필요로 하지 않는 연료전지 시스템에 관한 것이다. 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.

인류가 사용하고 있는 에너지 중 대부분은 화석연료로부터 얻고 있다. 그러나, 이러한 화석연료의 사용은 대기오염 및 산성비, 지구 온난화 등의 환경에 심각한 악영향을 미치고 있으며, 에너지 효율도 낮은 등의 문제점이 있었다.Most of the energy that humans are using comes from fossil fuels. However, the use of such fossil fuel has a serious adverse effect on the environment, such as air pollution, acid rain, global warming, and has a problem such as low energy efficiency.

이러한 화석연료의 사용에 따른 문제점을 해결하기 위하여 근래에는 연료전지 시스템이 개발되고 있다.Recently, fuel cell systems have been developed to solve the problems caused by the use of fossil fuels.

연료전지는 통상의 전지(2차 전지)와는 달리, 음극에 연료(수소가스 또는 탄화수소)를, 양극에 공기(산소)를 외부로부터 공급하여 발전하는 전지로서 실제로는 발전장치라고 볼 수 있다.Unlike conventional batteries (secondary batteries), 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.

연료전지에 의한 발전 방법은 연료의 연소(산화) 반응을 거치지 않고, 수소와 산소의 전기화학적 반응을 거쳐 반응 전후의 에너지 차를 전기에너지로 직접 변환하는 방법이다.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.

이러한 연료전지는 NOx와 SOx가 발생되지 않으며, 소음과 진동이 없는 시스템으로서 열효율이 전기발전량과 열회수량을 합하여 80% 이상이면서도 NOx나 SOx 등 유해가스의 발생이 없는 클린(clean) 발전 시스템이라고 할 수 있다.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.

종래에 알려진 연료전지 시스템으로는 수소봄베에 저장한 수소가스를 연료로 이용하는 이동식 발전 시스템 등이 있고, 이동 가능하고 교환이 용이한 액체연료를 이용하는 연료전지 시스템도 있으며, LNG나 LPG와 같은 보편적인 액화천연가스를 연료로 이용하는 가정용 발전 시스템이 있다.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. There is a domestic power generation system using liquefied natural gas as fuel.

도 1은 종래의 가정용 연료전지 시스템을 개략적으로 도시한 것으로, 일본공개특허공보 특개2003-187832호(특허문헌 1)에 개시되었다.1 schematically shows a conventional domestic fuel cell system, which is disclosed in Japanese Patent Laid-Open No. 2003-187832 (Patent Document 1).

도 1에 도시된 바와 같이, 연료전지 시스템은 도시가스, LPG, 등유 등의 탄화수소계 연료를 연료전지 스택(5)에서 사용할 수 있도록 개질하는 연료변환장치(fuel processor)(1~4)와, 개질된 가스를 이용하여 전기화학 반응에 의해 전기를 생성하는 연료전지 스택(5)과, 생산된 직류전류를 교류전류로 변환하는 전력변환장치(미도시)와, 연료가스, 공기, 물을 연료전지 시스템에 공급하는 펌프와 밸브 및 센서 등의 주변기기를 포함하여 구성된다.As shown in FIG. 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.

여기서, 일반적으로 연료변환장치는 연료가스를 수증기와 반응시켜 수소를 생성하는 개질기(reformer)(2)와, 생성된 가스가 연료전지 스택의 촉매에 피독을 일으키지 않도록 일산화탄소를 제거하는 CO변성기(CO shift converter)(3) 및 CO제거기(CO remover)(4)를 포함하여 구성된다.In general, 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.

연료변환장치를 거쳐 CO가 필요한 수준까지 정화된 개질가스는 연료전지 스택(5)으로 공급되며, 연료전지 스택(5)을 구성하는 각 단위 셀의 연료극(anode)에서 수소가 수소이온(H+)과 전자(e-)로 분해되고, 이들은 각각 전해질막과 외부도선을 통해 공기극(cathod)으로 이동하여 공기극으로 공급된 공기 중의 산소와 결합하여 물을 생성하는 반응을 일으킨다.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.

여기서, 전자의 흐름에 의해 전류가 생성되고 물 생성반응에서 부수적으로 열이 발생하며, 발생된 전류는 직류로서 전력변환장치를 사용하여 교류로 전환하여 사용하고, 발생된 열은 소정의 열교환기를 사용하여 온수로서 축열 저장하고 필요에 따라 급탕 및 난방용으로 사용하게 된다.Here, 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.

이때, 연료전지 시스템의 운전중에 성능에 가장 직접적인 영향을 미치는 요인 중 하나는 연료전지 시스템의 핵심 구성요소인 막전극 어셈블리(Membrane Electrode Assembly, MEA)의 전해질막과 촉매층 내의 이오노머(ionomer)에 일정량 이상의 수분을 공급하여 함수율을 유지시킴으로써, 전해질막과 이오노머 자체가 보유하고 있는 이온전도도의 최대 성능을 얻는 것이다.At this time, 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. By supplying moisture to maintain the moisture content, the maximum performance of the ion conductivity possessed by the electrolyte membrane and the ionomer itself is obtained.

이를 위해, 연료변환장치를 통과한 개질가스는 일본공개특허공보 특개2011-086543(특허문헌 2)에 개시된 바와 같이, 가습기를 거쳐 수분을 포함한 상태로 연료전지 스택으로 들어가게 되는데, 가습기 및 가습기에 필요한 주변부품으로 인해 연료전지 시스템의 규격이 커지면서 구조가 복잡해지고 제작 및 유지 보수비용이 증가하게 되는 문제가 있다.To this end, the reformed gas passing through the fuel conversion device enters the fuel cell stack in a state containing moisture through a humidifier, as disclosed in Japanese Patent Laid-Open No. 2011-086543 (Patent Document 2), which is required for a humidifier and a humidifier. As peripheral components increase in size of fuel cell systems, there is a problem in that the structure becomes complicated and manufacturing and maintenance costs increase.

본 발명은 상술한 바와 같은 문제를 해결하기 위해 안출된 것으로, 본 발명의 일 실시예는 개질기에 투입되는 개질수의 S/C(Steam to Carbon ratio)를 조절하는 등으로 연료전지 스택으로 공급되는 개질가스의 온도 및 습도 제어가 가능하여, 종래의 막가습기 등 별도의 가습수단을 필요로 하지 않는 연료전지 시스템을 제공하는 것을 목적으로 한다.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.

또한, 개질기를 통과한 개질가스가 열교환기를 거쳐 연료전지 스택으로 유입되는 것을 특징으로 하는 연료전지 시스템을 제공한다.In addition, there is provided a fuel cell system, characterized in that the reformed gas passing through the reformer flows into the fuel cell stack via a heat exchanger.

아울러, 개질가스와 열교환한 냉각수는 개질기의 개질반응을 위한 개질수로 공급되는 것을 특징을 하는 연료전지 시스템을 제공한다.In addition, it provides a fuel cell system characterized in that the cooling water heat-exchanged with the reformed gas is supplied to the reformed water for the reforming reaction of the reformer.

본 발명은 하기와 같은 연료전지 시스템을 제공한다.The present invention provides a fuel cell system as follows.

1. 개질기를 통과한 개질가스를 공급받아 전기화학반응에 의해 전기를 생성하는 연료전지 스택을 포함하며, 상기 개질가스에 함유된 수분에 의해 상기 연료전지 스택의 가습이 이루어지되, 상기 개질기에 투입되는 개질수의 S/C(Steam to Carbon ratio)를 조절하여 상기 연료전지 스택으로 공급되는 개질가스의 온도 및 습도를 제어하는 것을 특징으로 하는 연료전지 시스템.1. 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.

2. 위 1에 있어서, 상기 S/C는 2.5~4.0의 범위에서 조절되는 것을 특징으로 하는 연료전지 시스템.2. The fuel cell system according to 1 above, wherein the S / C is controlled in a range of 2.5 to 4.0.

3. 위 1에 있어서, 상기 개질기로부터 개질가스를 공급받아 개질가스 중에 함유된 일산화탄소를 시프트 반응에 의해 감소시키는 CO변성기; 및 상기 CO변성기를 통과한 개질가스를 공급받아 개질가스 중에 함유된 일산화탄소를 선택적으로 산화시켜 제거하는 CO제거기를 더 포함하며, 상기 CO제거기의 운전온도는 100℃~180℃인 것을 특징으로 하는 연료전지 시스템.3. In the above 1, 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.

4. 위 1에 있어서, 상기 개질기와 상기 연료전지 스택의 사이에 제1열교환기가 설치되어, 상기 개질기를 통과한 개질가스의 온도 및 습도 조절이 이루어지는 것을 특징으로 하는 연료전지 시스템.4. The fuel cell system according to 1 above, wherein a first heat exchanger is installed between the reformer and the fuel cell stack to control the temperature and humidity of the reformed gas passing through the reformer.

5. 위 4에 있어서, 상기 제1열교환기 내에서 상기 개질가스로부터 열을 전달받은 개질수(reforming water)가 상기 개질기로 공급되는 것을 특징으로 하는 연료전지시스템.5. The fuel cell system as set forth in 4 above, wherein reforming water which receives heat from the reforming gas in the first heat exchanger is supplied to the reformer.

6. 위 5에 있어서, 상기 개질수는, 시스템 내부의 응축수를 저장하거나, 또는 외부로부터 공급되는 공급수를 저장하거나, 또는 응축수와 공급수를 모두 저장하는 물탱크로부터 공급되며, 상기 연료전지 스택으로부터 배출되는 캐소드 오프 가스에 의해 온도 조절되거나, 또는 상기 개질기의 버너로부터 배출되는 배기가스에 의해 온도 조절되거나, 또는 캐소드 오프 가스와 배기가스 모두에 의해 온도 조절되는 것을 특징으로 하는 연료전지 시스템.6. In the above 5, wherein the reformed water is supplied from a water tank for storing condensate in the system, or to supply the supply from the outside, or to store both the condensate and the supply water, 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.

7. 위 5에 있어서, 상기 제1열교환기의 일측에 넉-아웃(knock-out) 드럼이 설치되어 상기 스택으로 공급되는 개질가스의 가습량이 조절되는 것을 특징으로 하는 연료전지 시스템.7. The fuel cell system as set forth in 5 above, wherein a knock-out drum is installed at one side of the first heat exchanger to adjust a humidification amount of the reformed gas supplied to the stack.

8. 위 4에 있어서, 상기 개질기를 통과한 개질가스가 상기 제1열교환기를 거치는 과정에서, 상기 개질기의 버너로부터 배출되는 배기가스와 열교환되어 개질가스의 온도 및 습도조절이 이루어지는 것을 특징으로 하는 연료전지 시스템.8. The fuel according to 4 above, wherein the reformed gas passing through the reformer is heat-exchanged with the exhaust gas discharged from the burner of the reformer in the course of passing through the first heat exchanger, thereby controlling temperature and humidity of the reformed gas. Battery system.

9. 위 8에 있어서, 상기 제1열교환기와 상기 개질기의 버너 사이에 제2열교환기가 설치되고, 상기 제2열교환기 내에서 상기 개질기의 버너로부터 배출되는 배기가스로부터 열을 전달받은 개질수가 상기 개질기로 공급되는 것을 특징으로 하는 연료전지 시스템.9. The reformer according to the above 8, wherein a second heat exchanger is installed between the first heat exchanger and the burner of the reformer, and the reformed water received heat from exhaust gas discharged from the burner of the reformer in the second heat exchanger. Fuel cell system, characterized in that supplied to.

10. 위 8에 있어서, 상기 개질기와 상기 제1열교환기 사이에 제2열교환기가 설치되고, 상기 제2열교환기 내에서 상기 개질가스로부터 열을 전달받은 개질수가 상기 개질기로 공급되는 것을 특징으로 하는 연료전지 시스템.10. The method according to the above 8, wherein a second heat exchanger is installed between the reformer and the first heat exchanger, and the reformed water that receives heat from the reforming gas in the second heat exchanger is supplied to the reformer. Fuel cell system.

11. 위 4에 있어서, 상기 개질기와 상기 제1열교환기 사이에 제2열교환기가 설치되고, 상기 제2열교환기를 통과한 개질가스가 상기 제1열교환기를 거치는 과정에서, 상기 연료전지 스택으로부터 배출되는 냉각수 및 캐소드 오프 가스와 열교환되어 개질가스의 온도 및 습도 조절이 이루어지거나, 냉각수와 캐소드 오프 가스 둘 중 어느 하나와 열교환되어 개질가스의 온도 및 습도 조절이 이루어지는 것을 특징으로 하는 연료전지 시스템.11. In the above 4, wherein a second heat exchanger is installed between the reformer and the first heat exchanger, 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.

12. 위 4에 있어서, 상기 개질기를 통과한 개질가스가 상기 제1열교환기를 거치는 과정에서, 상기 연료전지 스택로부터 배출되는 냉각수 및 캐소드 오프 가스와 열교환되어 개질가스의 온도 및 습도 조절이 이루어지거나, 냉각수와 캐소드 오프 가스 둘 중 어느 하나와 열교환되어 개질가스의 온도 및 습도 조절이 이루어지는 것을 특징으로 하는 연료전지 시스템.12. In the above 4, 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.

13. 위 12에 있어서, 상기 연료전지 스택로부터 배출되는 냉각수 및 캐소드 오프 가스, 또는 냉각수와 캐소드 오프 가스 둘 중 어느 하나가 상기 제1열교환기로 유동하도록 마련되는 유로 상에 제2열교환기를 설치하고, 상기 제2열교환기 내에서 냉각수 및 캐소드오프 가스, 또는 냉각수와 캐소드 오프 가스 둘 중 어느 하나로부터 열을 전달받은 개질수가 상기 개질기로 공급되는 것을 특징으로 하는 연료전지 시스템.13. In the above 12, wherein 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.

14. 위 3에 있어서, 상기 CO제거기의 일측에 구비되는 공냉팬의 작동을 제어하여 상기 CO제거기의 운전온도를 제어하는 것을 특징으로 하는 연료전지 시스템.14. The fuel cell system of 3 above, wherein the operation temperature of the CO remover is controlled by controlling an operation of an air cooling fan provided at one side of the CO remover.

15. 위 3에 있어서, 상기 CO제거기를 통과한 개질가스의 온도를 측정하여 상기 개질기의 버너에 공급되는 버너가스량을 조절함으로써, 상기 CO제거기의 운전온도를 제어하는 것을 특징으로 하는 연료전지 시스템.15. The fuel cell system as set forth in 3 above, by measuring the temperature of the reformed gas passing through the CO remover and controlling the amount of burner gas supplied to the burner of the reformer, thereby controlling the operating temperature of the CO remover.

또한, 본 발명은 하기와 같은 연료전지 운전 방법을 제공한다.In addition, the present invention provides a fuel cell operating method as follows.

1. 수분을 포함하는 개질가스를 상기 수분의 기화 온도 이상으로 운전되는 CO 제거기에 통과시키는 단계; 및 상기 수분으로 연료전지 스택의 가습 조건을 제어하는 단계를 포함하는 연료전지 운전 방법.1. passing a reforming gas comprising moisture through a CO remover operated above the vaporization temperature of the moisture; And controlling the humidification condition of the fuel cell stack with the moisture.

2. 위 1에 있어서, 개질기에 투입되는 개질수의 S/C (Steam to Carbon ratio)를 조절하여 상기 CO 제거기의 운전 온도를 조절하는 단계를 더 포함하는 연료전지 운전 방법.2. The method of 1 above, further comprising the step of adjusting the operating temperature of the CO remover by adjusting the S / C (Steam to Carbon ratio) of the reformed water introduced into the reformer.

3. 위 1에 있어서, 상기 CO 제거기의 공냉팬의 작동을 제어하여 상기 CO 제거기의 운전 온도를 조절하는 단계를 더 포함하는 연료전지 운전 방법.3. The method of 1 above, further comprising the step of controlling the operation temperature of the CO remover by controlling the operation of the air cooling fan of the CO remover.

4. 위 1에 있어서, 개질기에 설치된 버너에 공급되는 가스량을 조절하여 상기 CO 제거기의 운전 온도를 조절하는 단계를 더 포함하는 연료전지 운전 방법.4. The fuel cell operating method of 1 above, further comprising adjusting an operating temperature of the CO remover by adjusting an amount of gas supplied to a burner installed in the reformer.

5. 위 1에 있어서, 상기 CO 제거기의 운전 온도는 100~180인 연료전지 운전 방법.5. In the above 1, the operating temperature of the CO remover is 100 ~ 180 fuel cell operating method.

6. 위 2에 있어서, 상기 개질수의 S/C는 2.5~4.0인 연료전지 운전 방법.6. In the above 2, the S / C of the reforming water is 2.5 ~ 4.0 fuel cell operating method.

7. 위 1에 있어서, 상기 CO 제거기가 상기 수분의 기화 온도 이상으로 운전되어 상기 연료전지 스택으로 공급되는 개질가스의 온도 및 습도가 제어됨으로써 상기 연료전지의 가습 조건이 제어되는 연료전지 운전 방법.7. The fuel cell operating method of 1 above, wherein the CO remover is operated at a temperature higher than the vaporization temperature of the moisture to control the temperature and humidity of the reformed gas supplied to the fuel cell stack to control humidification conditions of the fuel cell.

8. 위 1에 있어서, 상기 수분을 포함하는 개질가스는 연료가 개질기에서 수증기와 반응한 후 CO 변성기에서 시프트 반응에 의해 일산화탄소가 감소된 것인 연료전지 운전 방법.8. The method according to the above 1, wherein the reformed gas containing water is reduced carbon monoxide by the shift reaction in the CO reformer after the fuel reacts with water vapor in the reformer.

9. 위 1에 있어서, 상기 CO 제거기를 통과한 개질가스를 상기 연료전지 스택에 투입하기 전에 제1 열교환기에 통과시켜 상기 개질가스의 온도 및 습도 중 적어도 하나를 조절하는 단계를 더 포함하는 연료전지 운전 방법.9. The fuel cell of 1 above, further comprising adjusting at least one of a temperature and a humidity of the reformed gas by passing the reformed gas passing through the CO remover through a first heat exchanger before inputting the reformed gas into the fuel cell stack. Driving way.

10. 위 9에 있어서, 상기 제1 열교환기 내에서 상기 개질가스의 열을 전달받은 개질수를 개질기로 공급하는 단계를 더 포함하는 연료전지 운전 방법.10. The method of claim 9, further comprising the step of supplying the reformed water received from the reformed gas heat in the first heat exchanger to a reformer.

11. 위 10에 있어서, 상기 개질수는 연료전지 시스템의 응축수 및 외부 공급수 중 적어도 하나를 저장하는 물탱크로부터 공급되는 것인 연료전지 운전 방법.11. The fuel cell operating method according to the above 10, wherein the reformed water is supplied from a water tank storing at least one of condensate and external supply water of a fuel cell system.

12. 위 10에 있어서, 상기 개질수는 연료전지 스택에서 배출되는 캐소드 오픈 가스 및 상기 개질기의 버너에서 배출되는 배기가스 중 적어도 하나에 의해 온도 조절되는 것인 연료전지 운전 방법.12. The method of claim 10, wherein 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.

13. 위 1에 있어서, 상기 CO 제거기를 통과한 개질가스가 상기 연료전지 스택에 투입되기 전에, 상기 개질가스의 습도를 넉-아웃(knock-out) 드럼으로 조절하는 단계를 더 포함하는 연료전지 운전 방법.13. The fuel cell of 1 above, further comprising adjusting the humidity of the reformed gas to a knock-out drum before the reformed gas passing through the CO remover is introduced into the fuel cell stack. Driving way.

14. 위 9에 있어서, 상기 개질가스가 상기 제1 열교환기를 통과할 때 개질기의 버너로부터 배출되는 배기가스와 열교환하여 온도 및 습도 중 적어도 하나의 조절이 이루어지는 연료전지 운전 방법.14. The fuel cell operating method according to the above 9, wherein the reformed gas is heat-exchanged with the exhaust gas discharged from the burner of the reformer when the reformed gas passes through the first heat exchanger, thereby controlling at least one of temperature and humidity.

15. 위 9에 있어서, 상기 개질가스를 상기 제1 열교환기에 통과시키기 전에 제2 열교환기에 통과시켜 상기 개질가스의 열을 상기 제2 열교환기의 개질수에 전달시키고 상기 개질수를 개질기로 공급하는 단계를 더 포함하는 연료전지 운전 방법.15. The method according to the above 9, wherein the reformed gas is passed through a second heat exchanger before passing the reformed gas to the first heat exchanger to transfer heat of the reformed gas to the reformed water of the second heat exchanger, and to supply the reformed water to the reformer. The fuel cell operating method further comprising the step.

16. 위 9에 있어서, 상기 개질가스를 상기 제1 열교환기에 통과시키기 전에 제2 열교환기에 통과시키고, 상기 제2 열교환기 내에서 개질수가 개질기의 버너에서 배출되는 배기가스의 열을 전달받도록 한 후 상기 개질수를 상기 개질기로 공급시키는 단계를 더 포함하는 연료전지 운전 방법.16. The method according to the above 9, after passing the reformed gas to the second heat exchanger before passing through the first heat exchanger, the reformed water in the second heat exchanger after receiving the heat of the exhaust gas discharged from the burner of the reformer And supplying the reformed water to the reformer.

17. 위 15에 있어서, 상기 개질가스가 상기 제2 열교환기를 통과한 후 상기 제1 열교환기를 통과할 때 연료전지 스택에서 배출되는 냉각수 및 캐소드 오픈 가스 중 어느 하나에 의해 온도 및 습도 중 적어도 하나의 조절이 되는 것인 연료전지 운전 방법.17. The method according to the above 15, wherein the reformed gas passes through the second heat exchanger and then passes through the first heat exchanger, at least one of temperature and humidity by any one of cooling water and cathode open gas discharged from the fuel cell stack. Fuel cell operation method that is controlled.

18. 위 9에 있어서, 상기 개질가스가 상기 제1 열교환기를 통과할 때 상기 연료전지 스택에서 배출되는 냉각수 및 캐소드 오픈 가스 중 어느 하나에 의해 온도 및 습도 중 적어도 하나의 조절이 되는 것인 연료전지 운전 방법.18. The fuel cell of 9 above, wherein the reformed gas is controlled by at least one of temperature and humidity by any one of a coolant and a cathode open gas discharged from the fuel cell stack when the reformed gas passes through the first heat exchanger. Driving way.

19. 위 18에 있어서, 상기 연료전지 스택에서 배출되는 냉각수 및 캐소드 오픈 가스 중 어느 하나가 상기 제1 열교환기로 유동하도록 마련되는 유로 상에 설치된 제2 열교환기 내에서 개질수가 상기 냉각수 및 캐소드 오픈 가스 중 어느 하나에 의해 열을 전달 받은 후 개질기로 공급되도록 하는 단계를 더 포함하는 연료전지 운전 방법.19. In the above 18, wherein 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.

본 발명의 일 실시예에 의하면, 개질기를 통과한 개질가스를 공급받아 전기화학반응에 의해 전기를 생성하는 연료전지 스택을 포함하며, 상기 개질가스에 함유된 수분에 의해 상기 연료전지 스택의 가습이 이루어지되, 상기 개질기에 투입되는 개질수의 S/C(Steam to Carbon ratio)를 조절함으로써, 상기 연료전지 스택으로 공급되는 개질가스의 온도 및 습도를 제어할 수 있는 연료전지 시스템이 제공된다.According to an embodiment of the present invention, 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. Although made, 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.

여기서, 상기 S/C는 2.5~4.0의 범위에서 조절될 수 있다.Here, the S / C can be adjusted in the range of 2.5 ~ 4.0.

또한, 상기 개질기로부터 개질가스를 공급받아 개질가스 중에 함유된 일산화탄소를 시프트 반응에 의해 감소시키는 CO 변성기; 및 상기 CO 변성기를 통과한 개질가스를 공급받아 개질가스 중에 함유된 일산화탄소를 선택적으로 산화시켜 제거하는 CO 제거기를 더 포함할 수 있는데, 상기 CO 제거기의 운전온도는 예컨대 100℃~180℃이다.In addition, 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.

이때, 상기 개질기와 상기 연료전지 스택의 사이에, 또는 상기 CO 제거기와 상기 연료전지 스택의 사이에 제1열교환기가 설치되어, 상기 개질기를 통과한 개질가스의 온도 및 습도 중 적어도 하나의 조절이 이루어질 수 있다.In this case, 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.

아울러, 상기 제1열교환기 내에서 상기 개질가스로부터 열을 전달받은 개질수(reforming water)가 상기 개질기로 공급될 수 있다.In addition, reforming water that receives heat from the reforming gas in the first heat exchanger may be supplied to the reformer.

본 발명의 바람직한 일 실시예에 따른 연료전지 시스템에 의하면, 개질기에 투입되는 개질수의 유량(S/C)을 조절함으로써, 연료전지 스택으로 공급되는 개질가스의 온도 및 습도 중 적어도 하나를 제어할 수 있다.According to the fuel cell system according to the preferred embodiment of the present invention, by controlling 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.

또한, 연료전지 스택의 가습을 위한 별도의 막가습기를 필요로 하지 않고, 종래 CO 변성기와 CO 제거기 사이에 설치된 열교환기가 불필요하게 되며, 따라서 전체 시스템을 컴팩트하게 제작할 수 있고, 제작 및 유지 보수 비용을 절감할 수 있다.In addition, there is no need for a separate membrane humidifier for humidifying the fuel cell stack, and a heat exchanger installed between the conventional CO transformer and the CO remover is unnecessary, thus making the whole system compact and reducing the manufacturing and maintenance costs. Can be saved.

아울러, 개질기와 연료전지 스택 사이에, 또는 CO 제거기와 연료전지 스택 사이에, 설치되는 열교환기에서 냉각수가 개질가스로부터 열을 전달받은 후 개질기에 공급되어 개질반응에 이용될 수 있으므로, 연료전지 시스템의 전체 효율이 향상되는 효과가 있다.In addition, between the reformer and the fuel cell stack, or between the CO remover and the fuel cell stack, in the heat exchanger installed, 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.

도 1은 종래의 연료전지 시스템의 구성도.1 is a block diagram of a conventional fuel cell system.

도 2는 본 발명의 제1실시예에 따른 연료전지 시스템의 구성도.2 is a block diagram of a fuel cell system according to a first embodiment of the present invention.

도 3은 개질수의 유량 제어에 의한 CO제거기 온도 제어방법을 도시한 순서도.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.

도 4는 공냉팬 작동 제어에 의한 CO제거기 온도 제어방법을 도시한 순서도.Figure 4 is a flow chart illustrating a method for controlling the temperature of the CO remover by air cooling fan operation control.

도 5는 버너 가스량 제어에 의한 CO제거기 온도 제어방법을 도시한 순서도.5 is a flow chart illustrating a method for controlling the temperature of the CO remover by controlling the burner gas amount.

도 6은 본 발명의 제2실시예에 따른 연료전지 시스템의 구성도.6 is a configuration diagram of a fuel cell system according to a second embodiment of the present invention.

도 7은 본 발명의 제3실시예에 따른 연료전지 시스템의 구성도.7 is a configuration diagram of a fuel cell system according to a third embodiment of the present invention.

도 8은 본 발명의 제4실시예에 따른 연료전지 시스템의 구성도.8 is a configuration diagram of a fuel cell system according to a fourth embodiment of the present invention.

도 9는 본 발명의 제5실시예에 따른 연료전지 시스템의 구성도.9 is a configuration diagram of a fuel cell system according to a fifth embodiment of the present invention.

도 10은 본 발명의 제6실시예에 따른 연료전지 시스템의 구성도.10 is a configuration diagram of a fuel cell system according to a sixth embodiment of the present invention.

도 11은 본 발명의 제7실시예에 따른 연료전지 시스템의 구성도.11 is a configuration diagram of a fuel cell system according to a seventh embodiment of the present invention.

도 12는 본 발명의 제8실시예에 따른 연료전지 시스템의 구성도.12 is a configuration diagram of a fuel cell system according to an eighth embodiment of the present invention.

도 13은 본 발명의 제9실시예에 따른 연료전지 시스템의 구성도.13 is a configuration diagram of a fuel cell system according to a ninth embodiment of the present invention.

도 14는 본 발명의 제1실험예로서 출력 1KW 시스템의 100% 부하 운전결과.14 is a 100% load operation result of the output 1KW system as a first experimental example of the present invention.

도 15는 본 발명의 제2실험예로서 출력 1KW 시스템의 75% 부하 운전결과.15 is a 75% load operation result of the output 1KW system as a second experimental example of the present invention.

도 16은 본 발명의 제3실험예로서 출력 1KW 시스템의 50% 부하 운전결과.16 is a 50% load operation result of the output 1KW system as a third experimental example of the present invention.

도 17은 본 발명의 제4실험예로서 출력 1KW 시스템의 30% 부하 운전결과.17 is a 30% load operation result of the output 1KW system as a fourth experimental example of the present invention.

이하, 본 발명인 연료전지 시스템의 바람직한 실시예들을 첨부된 도면을 참조하여 설명하기로 한다. 이 과정에서 도면에 도시된 선들의 두께나 구성요소의 크기 등은 설명의 명료성과 편의상 과장되게 도시되어 있을 수 있다.Hereinafter, exemplary embodiments of the present invention fuel cell system will be described with reference to the accompanying drawings. In this process, the thickness of the lines or the size of the components shown in the drawings may be exaggerated for clarity and convenience of description.

또한, 후술되는 용어들은 본 발명에서의 기능을 고려하여 정의된 용어들로서 이는 사용자, 운용자의 의도 또는 관례에 따라 달라질 수 있다. 그러므로, 이러한 용어들에 대한 정의는 본 명세서 전반에 걸친 내용을 토대로 하여 내려져야 할 것이다.In addition, terms to be described below are terms defined in consideration of functions in the present invention, which may vary according to the intention or convention of a user or an operator. Therefore, definitions of these terms should be made based on the contents throughout the specification.

아울러, 아래의 실시예는 본 발명의 권리범위를 한정하는 것이 아니라 본 발명의 청구범위에 제시된 구성요소의 예시적인 사항에 불과하며, 본 발명의 명세서 전반에 걸친 기술사상에 포함되고 청구범위의 구성요소에서 균등물로서 치환 가능한 구성요소를 포함하는 실시예는 본 발명의 권리범위에 포함될 수 있다.In addition, the following examples are not intended to limit the scope of the present invention but merely illustrative of the components set forth in the claims of the present invention, which are included in the technical spirit throughout the specification of the present invention and constitute the claims Embodiments that include a substitutable component as an equivalent in the element may be included in the scope of the present invention.

제1실시예First embodiment

도 2는 본 발명의 제1실시예에 따른 연료전지 시스템의 구성도이다.2 is a configuration diagram of a fuel cell system according to a first embodiment of the present invention.

도 2에 도시된 바와 같이, 본 발명의 제1실시예에 따른 연료전지 시스템은 개질기(10)와 CO변성기(20), CO제거기(30), 및 연료전지 스택(40)을 포함한다.As shown in FIG. 2, the fuel cell system according to the first embodiment of the present invention includes a reformer 10, a CO transformer 20, a CO remover 30, and a fuel cell stack 40.

여기서, 연료가스로 주로 사용되는 천연가스(NG)는 생산지역 또는 가스정제 공장에 따라 황(S) 성분의 함량이 각기 다르기는 하나, 통상적으로 도시가스는 메탄(CH4)이 주성분이며, 안전을 이유로 부취제(ordorant)인 황(S) 성분을 함유한 THT(tetra-hydro-thiophene), TBM(tertiary-butylmercaptan) 성분이 약4ppm 정도 첨가된 형태로 공급된다.Here, natural gas (NG), 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. For this reason, tetra-hydro-thiophene (THT) and tertiary-butylmercaptan (TBM) containing sulfur (S) as an odorant are supplied in the form of about 4 ppm added.

이 경우, 황 성분은 수십 ppm 정도의 함량으로도 개질기(10)와 연료전지 스택(40)의 촉매를 열화시키므로 제거해 주는 것이 바람직하다.In this case, 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.

따라서, 연료가스가 개질기(10)에 투입되기 전에, 탈황기(미도시)를 먼저 거칠 수 있으며, 탈황기는 다음의 탈황반응에 의해 연료가스로부터 황을 제거한다.Thus, before the fuel gas is introduced into the reformer 10, it may first go through a desulfurizer (not shown), and the desulfurizer removes sulfur from the fuel gas by the following desulfurization reaction.

HC + S → HCHC + S → HC

개질기(10)는 연료가스를 수증기와 반응시켜 수소가 주성분인 개질가스로 개질하는 것으로, 다음의 메탄-수증기 개질반응에 의해 수소를 생성한다.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.

Figure PCTKR2012009371-appb-I000001
Figure PCTKR2012009371-appb-I000001

Figure PCTKR2012009371-appb-I000002
Figure PCTKR2012009371-appb-I000002

이때의 개질반응은 흡열반응이며, 이에 필요한 열은 개질기(10)의 일측에 설치되는 가열버너(미도시)에서 공급되는데, 가열버너는 버너가스와 공기를 공급받아 연소시킨다.At this time, 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.

이때, 가열버너에 공급되는 연소용 버너가스는 개질기(10)에 공급되는 연료가스와 동일한 탄화수소계 연료인 것이 바람직하다.At this time, 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.

개질반응에 의해 생성된 개질가스의 CO농도는 10~15%정도이며, 고분자 연료전지(PEMFC)의 경우 전극 특성 때문에 CO농도를 더 낮출 필요가 있다.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.

이에 따라, 개질기(10)에서 나온 개질가스는 CO변성기(20)로 들어가며, 이때 CO변성기(20)는 아래의 CO변성반응을 통해 개질가스 중의 CO를 이산화탄소로 변성시키고 더불어 수소를 생성한다.Accordingly, 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.

Figure PCTKR2012009371-appb-I000003
Figure PCTKR2012009371-appb-I000003

위와 같은 CO변성반응에 의해 개질가스 중의 CO함량은 1% 이하, 더바람직하게는 0.5% 정도까지 감소한다.As a result of the above CO denaturation reaction, the CO content in the reformed gas is reduced to less than 1%, more preferably to about 0.5%.

CO 변성반응은

Figure PCTKR2012009371-appb-I000004
를 생성하는 쪽으로 진행될 경우, CO를 제거할 뿐만 아니라 추가로 수소를 생산할 수 있다는 장점을 가지고 있다.CO denaturation
Figure PCTKR2012009371-appb-I000004
Proceeding to produce the, it not only removes CO, but also has the advantage of producing additional hydrogen.

일반적으로 CO변성반응은 평형에 지배를 받아 온도와 압력에 의해 반응 조성이 결정되어 지며,

Figure PCTKR2012009371-appb-I000005
를 생성하는 방향으로 발열반응이어서 저온에서 유리하다.In general, the CO denaturation reaction is governed by the equilibrium, and the reaction composition is determined by temperature and pressure.
Figure PCTKR2012009371-appb-I000005
It is an exothermic reaction in the direction of producing a low temperature is advantageous.

반면에, 고온에서는 흡열반응인 역반응이 진행되어 수소를 소모하여 CO를 생성한다. 필요에 따라서는 고온 수성가스 변환(high-temperature water-gasshift ; HTS) 반응 및 저온 수성가스 변환(low-temperature water-gas shift ; LTS) 반응의 두 단계를 거쳐 CO농도를 감소시킨다.On the other hand, at high temperatures, 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 반응기는 500℃ 부근에서 Cr/Fe 계열의 촉매를 이용하여 10% 이상의 CO 농도를 5% 이하로 저감시키며, 이어지는 LTS 반응기에서는 200℃ 부근에서 Cu 계열의 촉매를 이용하여 CO의 농도를 약 0.5% 정도로 감소시킬 수 있다.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. In the subsequent LTS reactor, the CO concentration is reduced to about 0.5 using a Cu-based catalyst at around 200 ° C. Can be reduced to about%.

이어, CO제거기(30)에서 아래와 같은 선택적 산화 반응에 의해 CO를 ppm 단위까지 제거 및 정화하게 된다.Subsequently, the CO remover 30 removes and purifies CO to ppm by the selective oxidation reaction as follows.

Figure PCTKR2012009371-appb-I000006
Figure PCTKR2012009371-appb-I000006

선택적 산화 반응은 일반적으로 0.5~1% 정도의 CO를 포함하는 개질가스에

Figure PCTKR2012009371-appb-I000007
비가 약 1~3 정도 되게 미량의 산소를 포함하는 공기를 첨가하여, 개질가스 중에 과량으로 존재하는 수소를 산화하지 않고 CO만을 선택적으로 반응시키므로 고전환율의 촉매를 필요로 한다.Selective oxidation reactions are generally performed on reformed gases containing 0.5 to 1% of CO.
Figure PCTKR2012009371-appb-I000007
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.

또한, 선택적 산화 반응은 발열 반응이므로 반응 중 촉매층의 온도가 증가할 수 있다. 반응 온도가 증가하면 수소의 산화 반응 및 역수성가스 전환반응이 일어나 CO 선택 산화성이 저하될 수 있으므로 산소 분포를 균일화해야만 수소의 소모를 줄이고 CO의 선택적 산화가 가능하다. 때문에, 최근에는 다단계의 공기 공급 시스템을 사용하거나, 각 단마다 촉매를 달리한 반응기를 제작하여 사용하기도 한다.In addition, since the selective oxidation reaction is an exothermic reaction, the temperature of the catalyst layer may increase during the reaction. When 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.

이때, CO제거기(30)의 촉매는 예를 들어

Figure PCTKR2012009371-appb-I000008
등과 같이 운전온도 100℃~180℃에서 연속 사용 가능한 것이 바람직한데, CO제거기(30)의 운전온도가 100℃ 보다 낮으면 촉매반응이 일어나지 않을 수 있고, 180℃를 초과할 경우에는 아래와 같은 메탄화반응이 나타나기 때문이다.At this time, the catalyst of the CO remover 30 is, for example
Figure PCTKR2012009371-appb-I000008
It is desirable to be able to use continuously at an operating temperature of 100 ℃ ~ 180 ℃, such as, if the operating temperature of the CO remover 30 is lower than 100 ℃ may not occur the catalytic reaction, if it exceeds 180 ℃ methanation as follows Because the reaction appears.

Figure PCTKR2012009371-appb-I000009
Figure PCTKR2012009371-appb-I000009

Figure PCTKR2012009371-appb-I000010
Figure PCTKR2012009371-appb-I000010

또한, 종래에는 CO제거기(30)의 촉매 반응부에 응축이 발생하고 수막에 의해 반응면적이 줄어들어 CO가 발생되는 것을 방지하기 위해, CO변성기(20)와 CO제거기(30) 사이에 열교환기(도 1 참조)가 설치되어 CO변성반응 후 남은 증기(steam)를 제거하였으나, 본 발명에서는 CO제거기(30)의 운전온도를 수분이 기화되는 100℃ 이상으로 높여서 운전함에 따라, 별도의 열교환기를 필요로 하지 않고 수분이 응축되는 것을 방지할 수 있으며, 이때 CO제거기(30)를 거친 개질가스에 함유된 수분을 이용하여 연료전지 스택(40)의 가습(RH%) 조건을 80%~120%로 제어할 수 있다.In addition, conventionally, in order to prevent condensation from occurring in the catalytic reaction part of the CO remover 30 and CO 2 is generated by reducing the reaction area by the water film, a heat exchanger (C) between the CO transformer 20 and the CO remover 30 may be used. 1) is installed to remove steam remaining after the CO denaturation reaction, but in the present invention, 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.

즉, 본 발명의 실시예에 의하면, CO제거기(30)를 통과한 개질가스에는 CO제거기(30)에서 응축되지 않은 수분이 함유되어 있으며, 따라서 연료전지 스택(40)으로 개질가스가 공급될 때 연료전지 스택(40)의 가습이 이루어지게 되는 것이다.That is, according to the embodiment of the present invention, 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.

이때, 개질기에 투입되는 개질수의 S/C(Steam to Carbon ratio)를 조절함으로써, 연료전지 스택으로 공급되는 개질가스의 온도 및 습도를 제어할 수 있다.At this time, by adjusting the steam to carbon ratio (S / C) of the reformed water introduced into the reformer, it is possible to control the temperature and humidity of the reformed gas supplied to the fuel cell stack.

또한, CO제거기(30)의 온도가 정상운전 온도범위에 도달할 때까지, CO제거기(30)를 통과한 개질가스를, 재순환라인을 통해 다시 개질기(10)로 순환시키는 것도 물론 가능하다.In addition, it is also possible to circulate the reformed gas passed through the CO remover 30 to the reformer 10 again through a recirculation line until the temperature of the CO remover 30 reaches a normal operating temperature range.

한편, 전술한 방법으로 CO(일산화탄소)가 필요한 수준까지 정화된 개질가스는 연료전지 스택(40)으로 공급된다.On the other hand, the reformed gas purified to the required level CO (carbon monoxide) by the above-described method is supplied to the fuel cell stack 40.

이때, CO제거기(30)와 연료전지 스택(40) 사이에는 제1열교환기(50)가 설치되어, CO제거기(30)를 통과한 개질가스의 냉각이 이루어진다.At this time, 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.

그리고, 제1열교환기(50)에는 연료전지 시스템의 내부 또는 외부에서 냉각수의 공급이 이루어진다.The first heat exchanger 50 is supplied with cooling water from inside or outside the fuel cell system.

이때, 제1열교환기(50)는 예를 들어, 냉각수 입구와 출구를 갖춘 챔버와, 챔버 내에 설치되는 모세관으로 이루어질 수 있으며, CO제거기(30)를 통과한 개질가스는 모세관을 따라 제1열교환기(50)를 통과한다.In this case, 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.

이때 냉각수는 냉각수 입구를 통해 챔버로 유입되고, 제1열교환기(50)를 통과하는 과정에서 모세관을 통해 유동하는 개질가스로부터 열을 전달받게 되며, 냉각수 출구를 통해 제1열교환기(50)를 나온 냉각수는 수분 공급로(51)를 통해 개질기(10)에 개질수(reforming water)로 공급되어 개질기(10)의 수증기 반응에 사용된다.At this time, 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.

여기서, CO제거기(30)의 촉매 반응부에 응축이 발생하고 수막에 의해 반응면적이 줄어들어 CO가 발생되는 것을 방지하기 위해, CO제거기(30)의 운전온도를 수분이 기화되는 100℃ 이상(100℃~180℃)으로 제어할 필요가 있는데, 이하 CO제거기(30)의 운전온도를 제어하는 방법을 설명하기로 한다.Here, in order to prevent condensation from occurring in the catalytic reaction part of the CO remover 30 and the reaction area is reduced by the water film, CO is generated, 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).

먼저, CO제거기(30)의 운전온도가 적정범위(예를 들어,100℃~180℃)를 유지하도록, 제1열교환기(50)에 공급되는 개질수의 공급량을 제어기(70)로 조절할 수 있는데, S/C 2.5~4.0의 범위에서 조절하는 것이 바람직하다.First, 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.

이는, S/C 2.5 미만의 경우 물 부족으로 개질기(10)의 효율이 감소하는 한편, 연료전지 스택(40)으로 공급되는 개질가스의 가습(RH%)이 80% 이하로 떨어지고, S/C 4.0을 초과할 경우에는 과량의 물 공급으로 인해 개질기 내부에서 개질수의 증기화를 위한 히터가 작동됨에 따라 연료전지 시스템 전체의 효율이 감소하는 한편, 연료전지 스택(40)으로 공급되는 개질가스의 가습이 120% 이상으로 높아지기 때문이다.If the S / C less than 2.5, 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%.

도 3은 이처럼 개질수의 유량을 제어함으로써 CO제거기(30)의 온도를 제어하는 방법을 도시한 순서도이다.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.

도 3에 도시된 바와 같이, 먼저 CO제거기(30)의 온도를 측정한다(S10). 이때, 온도측정은 CO제거기(30) 내에 설치된 온도센서(미도시)에 의해 이루어지며, 측정된 값은 제어기(70)로 보내진다.As shown in FIG. 3, first, 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).

다음, 측정된 CO제거기(30)의 온도가 적정 온도범위(예를 들어, 100℃~180℃) 내에 있는지 제어기(70)에서 판단한다(S20). 이때, 적정 온도범위는 제어기(70)에 미리 입력되어 있는 것이 바람직하다.Next, 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).

정상운전 온도범위 내이면 정상적으로 운전이 계속되고, 정상운전 온도범위 밖이면 다시 온도범위 미만인지 판단한다(S30).If it is within the normal operating temperature range, operation continues normally, and if it is outside the normal operating temperature range, it is again determined whether the temperature range is lower (S30).

정상운전 온도범위 미만이면 제어기(70)에 의해, 제1열교환기(50)에 공급되는 개질수의 유량(S/C)을 감소시키고(S40), 정상운전 온도범위를 초과하면 개질수의 유량을 증가시킨다(S50). 이때, 개질수의 증감량은 측정된 CO제거기(30)의 온도에 대응하여 결정되도록 미리 설정될 수 있으며 또한, CO제거기(30)의 온도가 정상운전 온도범위에 도달할 때까지 CO제거기(30)를 통과한 개질가스를 재순환라인을 통해 다시 개질기(10)로 순환시키는 것도 가능하다.If it is less than the normal operating temperature range, 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). At this time, 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.

도 4는 공냉팬 작동 제어에 의한 CO제거기 온도 제어방법을 도시한 순서도이다.Figure 4 is a flow chart illustrating a method for controlling the temperature of the CO remover by the air cooling fan operation control.

이에 따르면, CO제거기(30)의 운전온도를 적절한 범위로 제어함에 있어서 CO제거기(30)에 설치되는 공냉팬(미도시)을 이용할 수 있다.According to this, 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.

즉, 도 4에 도시된 바와 같이, 먼저 CO제거기(30)의 온도를 측정한다(S10). 이때, 온도측정은 CO제거기(30) 내에 설치된 온도센서(미도시)에 의해 이루어지며, 측정된 값은 제어기(70)로 보내진다.That is, as shown in Figure 4, first measuring the temperature of the CO remover (30) (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).

다음, 측정된 CO제거기(30)의 온도가 적정 온도범위(예를 들어, 100℃~180℃) 내에 있는지 제어기(70)에서 판단한다(S20). 이때, 적정 온도범위는 제어기(70)에 미리 입력되어 있는 것이 바람직하다.Next, 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).

정상운전 온도범위 내이면 정상적으로 운전이 계속되고, 정상운전 온도범위 밖이면 다시 온도범위 미만인지 판단한다(S30).If it is within the normal operating temperature range, operation continues normally, and if it is outside the normal operating temperature range, it is again determined whether the temperature range is lower (S30).

정상운전 온도범위 미만이면 제어기(70)에 의해, CO제거기(30)에 설치된 공냉팬의 회전수를 감소시키고(S40'), 정상운전 온도범위를 초과하면 공냉팬의 회전수를 증가시킨다(S50'). 이때, 공냉팬의 회전수 증감량은 측정된 CO제거기(30)의 온도에 대응하여 결정되도록 미리 설정될 수 있으며 또한, CO제거기(30)의 온도가 정상운전 온도범위에 도달할 때까지 CO제거기(30)를 통과한 개질가스를 재순환라인을 통해 다시 개질기(10)로 순환시키는 것도 가능하다.When the temperature is less than the normal operating temperature, the controller 70 decreases the number of revolutions of the air cooling fan installed in the CO remover 30 (S40 '). When the temperature exceeds the normal temperature range, the number of revolutions of the air cooling fan is increased (S50). '). At this time, 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.

도 5는 버너 가스량 제어에 의한 CO제거기 온도 제어방법을 도시한 순서도이다.5 is a flowchart illustrating a method of controlling the temperature of the CO remover by controlling the burner gas amount.

이에 따르면, CO제거기(30)의 운전온도 범위 제어가, 개질기(10)에 설치된 가열버너(미도시)에 공급되는 버너가스량을 조절함으로써 이루어질 수 있다.According to this, 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.

즉, 도 5에 도시된 바와 같이, 먼저 CO제거기(30)의 온도를 측정한다(S10). 이때, 온도측정은 CO제거기(30) 내에 설치된 온도센서(미도시)에 의해 이루어지며, 측정된 값은 제어기(70)로 보내진다.That is, as shown in FIG. 5, first, 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).

다음, 측정된 CO제거기(30)의 온도가 적정 온도범위(예를 들어, 100℃~180℃) 내에 있는지 제어기(70)에서 판단한다(S20). 이때, 적정 온도범위는 제어기(70)에 미리 입력되어 있는 것이 바람직하다.Next, 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).

정상운전 온도범위 내이면 정상적으로 운전이 계속되고, 정상운전 온도범위 밖이면 다시 온도범위 미만인지 판단한다(S30).If it is within the normal operating temperature range, operation continues normally, and if it is outside the normal operating temperature range, it is again determined whether the temperature range is lower (S30).

정상운전 온도범위 미만이면 제어기(70)에 의해 가열버너에 공급되는 버너가스의 양을 늘려서 개질기에 공급되는 열원의 양을 늘리고(S40"), 정상운전 온도범위를 초과하면 가열버너에 공급되는 버너가스의 양을 줄인다(S50").If the temperature is less than the normal operating temperature, 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 ").

이때, 버너가스의 증감량은 측정된 CO제거기(30)의 온도에 대응하도록 미리 설정될 수 있으며 또한, CO제거기(30)의 온도가 정상운전 온도범위에 도달할 때까지 CO제거기(30)를 통과한 개질가스를 재순환라인을 통해 다시 개질기(10)로 순환시키는 것도 가능하다.At this time, 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.

이처럼, CO제거기(30)의 운전온도를 제어함으로써, 연료전지 스택(40)으로 공급되는 개질가스의 온도 조절이 가능하고, 개질가스의 이슬점(dewpoint)이 조절됨에 따라 개질가스의 습도가 조절되는 효과도 볼 수 있다.As such, by controlling the operating temperature of the CO remover 30, it is possible to adjust the temperature of the reformed gas supplied to the fuel cell stack 40, and the humidity of the reformed gas is controlled as the dew point of the reformed gas is adjusted. You can see the effect.

제2실시예Second embodiment

도 6은 본 발명의 제2실시예에 따른 연료전지 시스템의 구성도이며 이하, 제어기(70)의 도시는 편의상 생략하였음을 미리 밝혀둔다.FIG. 6 is a configuration diagram of a fuel cell system according to a second embodiment of the present invention. Hereinafter, the controller 70 is omitted for convenience.

본 발명의 제2실시예에 따른 연료전지 시스템은 전술한 제1실시예와 거의 유사하며 다만, 물탱크(60)로부터 제1열교환기(50)로 공급되는 개질수가, 개질기(10)의 버너(11)로부터 배출되는 배기가스 및 연료전지 스택(40)의 캐소드 오프 가스에 의해 온도 조절되거나, 배기가스와 캐소드 오프 가스 둘 중 어느 하나에 의해 온도 조절된다는 점에서 차이가 있다.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.

이때, 물탱크(60)에는 연료전지 시스템 내의 응축수가 저장되거나,또는 외부로부터 공급된 공급수가 저장되거나, 또는 응축수와 공급수가 함께 저장된다.In this case, 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.

이때, 물탱크(60)는 별도의 히터(미도시)에 의해 가열되거나, 버너(11)의 배기가스와 열교환하거나, 또는 연료전지 스택(40)의 캐소드 오프 가스와 열교환하거나, 또는 배기가스 및 캐소드 오프 가스 모두와 열교환함으로써, 물탱크(60)로부터 제1열교환기(50)로 공급되는 개질수의 온도가 조절되고, 개질가스가 제1열교환기(50)를 통과하는 과정에서 온도 및 습도가 조절되어 연료전지 스택(40)으로 공급된다.In this case, 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.

이때, CO제거기(30)의 운전온도 제어는, 개질수의 유량 조절, 공냉팬의 작동 제어, 또는 버너(11) 가스량 제어에 의해 이루어질 수 있음은 전술한 바와 같다.At this time, 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).

제3실시예Third embodiment

도 7은 본 발명의 제3실시예에 따른 연료전지 시스템의 구성도이다.7 is a configuration diagram of a fuel cell system according to a third embodiment of the present invention.

본 발명의 제3실시예에 따른 연료전지 시스템은 전술한 제1실시예와 거의 유사하며, 다만 제1열교환기(50)의 일측에 넉-아웃 드럼(knock-out drum)(80)이 설치되어, 연료전지 스택(40)으로 공급되는 가습량이 넉-아웃 드럼(80)에 의해 조절될 수 있다는 점에서 차이가 있다.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.

이때, CO제거기(30)의 운전온도 제어가, 개질수의 유량 조절, 공냉팬의 작동 제어, 또는 버너(11) 가스량 제어에 의해 이루어질 수 있음은 전술한 바와 같다.At this time, 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.

제4실시예Fourth embodiment

도 8은 본 발명의 제4실시예에 따른 연료전지 시스템의 구성도이다.8 is a configuration diagram of a fuel cell system according to a fourth embodiment of the present invention.

본 발명의 제4실시예에 따른 연료전지 시스템에서는, 전술한 실시예들과는 달리, 제1열교환기(50)를 개질가스가 통과하는 과정에서, 개질기(10)의 버너(11)로부터 배출되는 배기가스와 열교환이 이루어지며, 이에 의해 연료전지 스택(40)으로 공급되는 개질가스의 온도 및 습도 조절이 이루어진다는 점에서 차이가 있다.In the fuel cell system according to the fourth embodiment of the present invention, unlike the above-described embodiments, 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. There is a difference in that the heat exchange with the gas, thereby controlling the temperature and humidity of the reformed gas supplied to the fuel cell stack 40.

이때, CO제거기(30)의 운전온도 제어는, 개질수의 유량 조절, 공냉팬의 작동 제어, 또는 버너(11) 가스량 제어에 의해 이루어질 수 있다.In this case, 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.

제5실시예Fifth Embodiment

도 9는 본 발명의 제5실시예에 따른 연료전지 시스템의 구성도이다.9 is a configuration diagram of a fuel cell system according to a fifth embodiment of the present invention.

본 발명의 제5실시예에 따른 연료전지 시스템은 전술한 제4실시예와 거의 유사하며, 다만 제1열교환기(50)와 버너(11) 사이의 유로에 제2열교환기(52)가 설치된다는 점에서 차이가 있다.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.

이때, 버너(11)의 배기가스는 먼저 제2열교환기(52)를 거치면서 개질수와 열교환한 이후에 제1열교환기(56)로 들어가게 되며, 제2열교환기(52)에서 배기가스로부터 열을 전달받은 개질수는 개질기(10)에 공급되어 수증기 반응에 이용된다.At this time, 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.

이때, CO제거기(30)의 운전온도 제어가, 개질수의 유량 조절, 공냉팬의 작동 제어, 또는 버너(11) 가스량 제어에 의해 이루어질 수 있음은 전술한 바와 같다.At this time, 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.

제6실시예Sixth embodiment

도 10은 본 발명의 제6실시예에 따른 연료전지 시스템의 구성도이다.10 is a configuration diagram of a fuel cell system according to a sixth embodiment of the present invention.

전술한 제5실시예에서는 제2열교환기(52)가 제1열교환기(50)와 버너(11) 사이의 유로에 설치된 반면에, 본 발명의 제6실시예에 따른 연료전지 시스템은 제2열교환기(52)가 제1열교환기(50)와 CO제거기(30) 사이의 유로에 설치된다는 점에서 차이가 있다.In the above-described fifth embodiment, 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.

이때, CO제거기(30)를 통과한 개질가스는, 제2열교환기(52)를 거치는 과정에서 개질수와 열교환하고, 이어서 제1열교환기(50)를 거치는 과정에서 버너(11)의 배기가스와 열교환한 이후에 연료전지 스택(40)으로 공급되며, 제2열교환기(52)에서 개질가스로부터 열전달받은 개질수는 개질기(10)에 공급되어 수증기 반응에 이용된다.At this time, the reformed gas passing through the CO remover 30, the heat exchange with the reformed water in the process of passing through the second heat exchanger 52, and then the exhaust gas of the burner 11 in the process of passing through the first heat exchanger (50) After the heat exchange with the fuel cell stack 40 is supplied to the fuel cell stack 40, 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.

따라서, 개질가스가 제1열교환기(50)를 거치는 과정에서 버너(11)의 배기가스에 의해 승온됨에 따라, 연료전지 스택(40)으로 공급되는 개질가스의 수분응축이 더욱 방지되는 효과가 있으며 이때, CO제거기(30)의 운전온도 제어가, 개질수의 유량 조절, 공냉팬의 작동 제어, 또는 버너(11) 가스량 제어에 의해 이루어질 수 있음은 전술한 바와 같다.Therefore, as the reformed gas is heated by the exhaust gas of the burner 11 in the course of passing through the first heat exchanger 50, the condensation of the reformed gas supplied to the fuel cell stack 40 is further prevented. At this time, 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.

제7실시예Seventh embodiment

도 11은 본 발명의 제7실시예에 따른 연료전지 시스템의 구성도이다.11 is a configuration diagram of a fuel cell system according to a seventh embodiment of the present invention.

전술한 제6실시예에서는 개질가스가 제1열교환기(50)를 거치는 과정에서 버너(11)의 배기가스와 열교환하는 반면에, 본 발명의 제7실시예에 따른 연료전지 시스템은, 개질가스가 제1열교환기(50)를 거치는 과정에서 연료전지 스택(40)으로부터 배출되는 냉각수 및 캐소드 오프 가스(cathode off gas)와 열교환하거나, 또는 냉각수와 캐소드 오프 가스 둘 중 어느 하나와 열교환한다는 점에서 차이가 있다.In the sixth embodiment described above, while the reformed gas exchanges heat with the exhaust gas of the burner 11 in the course of passing through the first heat exchanger 50, 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.

이때, 제1열교환기(50)와 CO제거기(30) 사이의 유로에는 제2열교환기(52)가 설치되며, 제2열교환기(54)를 거치면서 개질가스로부터 열전달받은 개질수가 개질기(10)로 공급된다.In this case, 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.

이때, CO제거기(30)의 운전온도 제어가, 개질수의 유량 조절, 공냉팬의 작동 제어, 또는 버너(11) 가스량 제어에 의해 이루어질 수 있음은 전술한 바와 같다.At this time, 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.

제8실시예Eighth Embodiment

도 12는 본 발명의 제8실시예에 따른 연료전지 시스템의 구성도이다.12 is a configuration diagram of a fuel cell system according to an eighth embodiment of the present invention.

본 발명의 제8실시예에 따른 연료전지 시스템은, 전술한 제7실시예에서 제2열교환기가 삭제된 형태이며, 개질가스의 온도 및 습도는 연료전지 스택(40)으로부터 배출되는 냉각수 및 캐소드 오프 가스에 의해 제어되거나, 또는 냉각수와 캐소드 오프 가스 둘 중 어느 하나에 의해 제어될 수 있다.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.

이때, CO제거기(30)의 운전온도 제어가, 개질수의 유량 조절, 공냉팬의 작동 제어, 또는 버너(11) 가스량 제어에 의해 이루어질 수 있음은 전술한 바와 같다.At this time, 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.

제9실시예Ninth Embodiment

도 13은 본 발명의 제9실시예에 따른 연료전지 시스템의 구성도이다.13 is a configuration diagram of a fuel cell system according to a ninth embodiment of the present invention.

본 발명의 제9실시예에 따른 연료전지 시스템은, 전술한 제8실시예에서 연료전지 스택(40)으로부터 배출된 냉각수 및 캐소드 오프 가스, 또는 냉각수와 캐소드 오프 가스 둘 중 어느 하나가 제1열교환기(50)로 들어가는 유로 상에 제2열교환기(52)가 설치된다.In the fuel cell system according to the 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.

이때, 냉각수 및 캐소드 오프 가스, 또는 냉각수와 캐소드 오프 가스 둘 중 어느 하나는 연료전지 스택(40)으로부터 배출된 후 제2열교환기(52)를 거쳐 제1열교환기(50)를 통과하게 된다.In this case, 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.

이때, 연료전지 스택(40)으로부터 배출된 냉각수 및 캐소드 오프 가스, 또는 냉각수와 캐소드 오프 가스 둘 중 어느 하나는 제2열교환기(55)에서 개질수와 열교환하고, 개질수는 개질기(10)에 공급되어 수증기 반응에 이용되며, 개질가스는 제1열교환기(50)를 거치는 과정에서 온도 및 습도가 조절되어 연료전지 스택(40)으로 공급된다.At this time, 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.

이때, CO제거기(30)의 운전온도 제어는, 개질수의 유량 조절, 공냉팬의 작동 제어, 또는 버너(11) 가스량 제어에 의해 이루어질 수 있다.In this case, 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.

이하, 도 14 내지 도 17을 참조하여 본 발명의 실시예에 따른 연료전지 시스템의 실험예들을 소개하기로 한다. 아래와 같이 다양한 부하조건에서 본발명의 일실시예에 따른 연료전지 시스템을 운전한 결과, 별도의 막가습기 없이도 개질수의 유량을 조절함으로써, 연료전지 스택(40)으로 공급되는 개질가스가 연료전지 스택(40)의 정상운전을 위해 필요한 습기를 포함하게 됨을 확인하였다.Hereinafter, experimental examples of a fuel cell system according to an exemplary embodiment of the present invention will be described with reference to FIGS. 14 to 17. As a result of operating the fuel cell system according to an embodiment of the present invention under various load conditions as described below, the reformed gas supplied to the fuel cell stack 40 is controlled by adjusting the flow rate of the reformed water without a separate membrane humidifier. It was confirmed that the moisture contained for the normal operation of (40) was included.

제1실험예Experimental Example

도 14는 본 발명의 제1실험예로서 출력 1KW 시스템의 100% 부하 운전결과를 나타내고 있다.Fig. 14 shows the 100% load operation result of the output 1KW system as the first experimental example of the present invention.

열교환기(50)를 거쳐 개질기(10)로 공급되는 개질수의 공급량은 2.5~4.0(S/C;스팀-카본비) 범위를 유지하였고, CO제거기(30)를 거친 개질가스의 온도는 115~160℃였다.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.

여기서, 열교환기(50)를 거쳐 연료전지 스택(40)으로 공급되는 개질가스의 온도는 60~80℃로 측정되었고, 유량은 20~25lpm이었으며, 이때 상대습도(RH)는 80~120%로 측정되었다.Here, the temperature of the reformed gas supplied to the fuel cell stack 40 through the heat exchanger 50 was measured at 60 ~ 80 ℃, the flow rate was 20 ~ 25lpm, the relative humidity (RH) is 80 ~ 120% Was measured.

제2실험예Experimental Example

도 15는 본 발명의 제2실험예로서 출력 1KW 시스템의 75% 부하 운전결과를 나타내고 있다.Fig. 15 shows a 75% load operation result of the output 1KW system as the second experimental example of the present invention.

열교환기(50)를 거쳐 개질기(10)로 공급되는 개질수의 공급량은 2.5~4.0(S/C;스팀-카본비) 범위를 유지하였고, CO제거기(30)를 거친 개질가스의 온도는 110~150℃였다.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.

여기서, 열교환기(50)를 거쳐 연료전지 스택(40)으로 공급되는 개질가스의 온도는 55~75℃로 측정되었고, 유량은 15~20lpm이었으며, 이때 상대습도(RH)는 80~120%로 측정되었다.Here, the temperature of the reformed gas supplied to the fuel cell stack 40 via the heat exchanger 50 was measured at 55 ~ 75 ℃, the flow rate was 15 ~ 20lpm, the relative humidity (RH) is 80 ~ 120% Was measured.

제3실험예Experimental Example

도 16은 본 발명의 제3실험예로서 출력 1KW 시스템의 50% 부하 운전결과를 나타내고 있다.Fig. 16 shows the 50% load operation result of the output 1KW system as the third experimental example of the present invention.

열교환기(50)를 거쳐 개질기(10)로 공급되는 개질수의 공급량은 2.5~4.0(S/C;스팀-카본비) 범위를 유지하였고, CO제거기(30)를 거친 개질가스의 온도는 107~150℃였다.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.

여기서, 열교환기(50)를 거쳐 연료전지 스택(40)으로 공급되는 개질가스의 온도는 50~70℃로 측정되었고, 유량은 10~15lpm이었으며, 이때 상대습도 43-28(RH)는 80~120%로 측정되었다.Here, the temperature of the reformed gas supplied to the fuel cell stack 40 through the heat exchanger 50 was measured at 50 ~ 70 ℃, the flow rate was 10 ~ 15lpm, the relative humidity 43-28 (RH) is 80 ~ Measured at 120%.

제4실험예Experimental Example 4

도 17은 본 발명의 제4실험예로서 출력 1KW 시스템의 30% 부하 운전결과를 나타내고 있다.17 shows a 30% load operation result of an output 1KW system as a fourth experimental example of the present invention.

열교환기(50)를 거쳐 개질기(10)로 공급되는 개질수의 공급량은 2.5~4.0(S/C;스팀-카본비) 범위를 유지하였고, CO제거기(30)를 거친 개질가스의 온도는 105~150℃였다.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.

여기서, 열교환기(50)를 거쳐 연료전지 스택(40)으로 공급되는 개질가스의 온도는 50~65℃로 측정되었고, 유량은 7~10lpm이었으며, 이때 상대습도(RH)는 80~120%로 측정되었다.Here, the temperature of the reformed gas supplied to the fuel cell stack 40 via the heat exchanger 50 was measured at 50 ~ 65 ℃, the flow rate was 7 ~ 10lpm, the relative humidity (RH) is 80 ~ 120% Was measured.

{부호의 설명}{Description of the sign}

10 : 개질기 11 : 버너10: reformer 11: burner

20 : CO변성기 30 : CO제거기20: CO transformer 30: CO remover

40 : 연료전지 스택 50 : 제1열교환기40 fuel cell stack 50 first heat exchanger

51 : 수분공급로 52 : 제2열교환기51: water supply passage 52: second heat exchanger

60 : 물탱크 70 : 제어기60: water tank 70: controller

80 : 넉-아웃 드럼80: knock-out drum

Claims (19)

수분을 포함하는 개질가스를 상기 수분의 기화 온도 이상으로 운전되는 CO 제거기에 통과시키는 단계; 및 상기 수분으로 연료전지 스택의 가습 조건을 제어하는 단계를 포함하는 연료전지 운전 방법.Passing a reforming gas comprising moisture through a CO remover operated above the vaporization temperature of the moisture; And controlling the humidification condition of the fuel cell stack with the moisture. 청구항 1에 있어서, 개질기에 투입되는 개질수의 S/C (Steam to Carbon ratio)를 조절하여 상기 CO 제거기의 운전 온도를 조절하는 단계를 더 포함하는 연료전지 운전 방법.The fuel cell operating method of claim 1, further comprising adjusting an operating temperature of the CO remover by adjusting a steam to carbon ratio (S / C) of the reformed water introduced into the reformer. 청구항 1에 있어서, 상기 CO 제거기의 공냉팬의 작동을 제어하여 상기 CO 제거기의 운전 온도를 조절하는 단계를 더 포함하는 연료전지 운전 방법.The method of claim 1, further comprising controlling an operation temperature of the CO remover by controlling an operation of an air cooling fan of the CO remover. 청구항 1에 있어서, 개질기에 설치된 버너에 공급되는 가스량을 조절하여 상기 CO 제거기의 운전 온도를 조절하는 단계를 더 포함하는 연료전지 운전 방법.The fuel cell operating method of claim 1, further comprising adjusting an operating temperature of the CO remover by adjusting an amount of gas supplied to a burner installed in the reformer. 청구항 1에 있어서, 상기 CO 제거기의 운전 온도는 100~180인 연료전지 운전 방법.The method of claim 1, wherein the operating temperature of the CO remover is 100 ~ 180 fuel cell operating method. 청구항 2에 있어서, 상기 개질수의 S/C는 2.5~4.0인 연료전지 운전 방법.The fuel cell operating method according to claim 2, wherein the S / C of the reformed water is 2.5 to 4.0. 청구항 1에 있어서, 상기 CO 제거기가 상기 수분의 기화 온도 이상으로 운전되어 상기 연료전지 스택으로 공급되는 개질가스의 온도 및 습도가 제어됨으로써 상기 연료전지의 가습 조건이 제어되는 연료전지 운전 방법.The fuel cell operating method of claim 1, wherein the CO remover is operated at a temperature higher than the vaporization temperature of the moisture to control the temperature and humidity of the reformed gas supplied to the fuel cell stack, thereby controlling humidification conditions of the fuel cell. 청구항 1에 있어서, 상기 수분을 포함하는 개질가스는 연료가 개질기에서 수증기와 반응한 후 CO 변성기에서 시프트 반응에 의해 일산화탄소가 감소된 것인 연료전지 운전 방법.The method of claim 1, wherein the reformed gas containing water is reduced in carbon monoxide by a shift reaction in a CO reformer after the fuel reacts with water vapor in a reformer. 청구항 1에 있어서, 상기 CO 제거기를 통과한 개질가스를 상기 연료전지 스택에 투입하기 전에 제1 열교환기에 통과시켜 상기 개질가스의 온도 및 습도 중 적어도 하나를 조절하는 단계를 더 포함하는 연료전지 운전 방법.The method of claim 1, further comprising adjusting at least one of a temperature and a humidity of the reformed gas by passing the reformed gas passing through the CO remover into the first heat exchanger before introducing the reformed gas into the fuel cell stack. . 청구항 9에 있어서, 상기 제1 열교환기 내에서 상기 개질가스의 열을 전달받은 개질수를 개질기로 공급하는 단계를 더 포함하는 연료전지 운전 방법.The fuel cell operating method of claim 9, further comprising supplying reformed water that receives heat of the reformed gas to a reformer in the first heat exchanger. 청구항 10에 있어서, 상기 개질수는 연료전지 시스템의 응축수 및 외부 공급수 중 적어도 하나를 저장하는 물탱크로부터 공급되는 것인 연료전지 운전 방법.The method of claim 10, wherein the reformed water is supplied from a water tank storing at least one of condensate and external feed water of the fuel cell system. 청구항 10에 있어서, 상기 개질수는 연료전지 스택에서 배출되는 캐소드 오픈 가스 및 상기 개질기의 버너에서 배출되는 배기가스 중 적어도 하나에 의해 온도 조절되는 것인 연료전지 운전 방법.The method of claim 10, wherein 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. 청구항 1에 있어서, 상기 CO 제거기를 통과한 개질가스가 상기 연료전지 스택에 투입되기 전에, 상기 개질가스의 습도를 넉-아웃(knock-out) 드럼으로 조절하는 단계를 더 포함하는 연료전지 운전 방법.The method of claim 1, further comprising adjusting a humidity of the reformed gas to a knock-out drum before the reformed gas passing through the CO remover is introduced into the fuel cell stack. . 청구항 9에 있어서, 상기 개질가스가 상기 제1 열교환기를 통과할 때 개질기의 버너로부터 배출되는 배기가스와 열교환하여 온도 및 습도 중 적어도 하나의 조절이 이루어지는 연료전지 운전 방법.The method of claim 9, wherein when the reformed gas passes through the first heat exchanger, at least one of temperature and humidity is controlled by heat exchange with exhaust gas discharged from a burner of the reformer. 청구항 9에 있어서, 상기 개질가스를 상기 제1 열교환기에 통과시키기 전에 제2 열교환기에 통과시켜 상기 개질가스의 열을 상기 제2 열교환기의 개질수에 전달시키고 상기 개질수를 개질기로 공급하는 단계를 더 포함하는 연료전지 운전 방법.The method of claim 9, wherein passing the reformed gas through a second heat exchanger before passing the reformed gas to the first heat exchanger to transfer heat of the reformed gas to the reformed water of the second heat exchanger and supplying the reformed water to the reformer. Fuel cell operation method further comprising. 청구항 9에 있어서, 상기 개질가스를 상기 제1 열교환기에 통과시키기 전에 제2 열교환기에 통과시키고, 상기 제2 열교환기 내에서 개질수가 개질기의 버너에서 배출되는 배기가스의 열을 전달받도록 한 후 상기 개질수를 상기 개질기로 공급시키는 단계를 더 포함하는 연료전지 운전 방법.The method according to claim 9, wherein the reformed gas is passed through a second heat exchanger before passing through the first heat exchanger, and the reformed water in the second heat exchanger after receiving the heat of the exhaust gas discharged from the burner of the reformer. And supplying water from the reformer to the reformer. 청구항 15에 있어서, 상기 개질가스가 상기 제2 열교환기를 통과한 후 상기 제1 열교환기를 통과할 때 연료전지 스택에서 배출되는 냉각수 및 캐소드 오픈 가스 중 어느 하나에 의해 온도 및 습도 중 적어도 하나의 조절이 되는 것인 연료전지 운전 방법.The method according to claim 15, wherein at least one of temperature and humidity is controlled by any one of the coolant and the cathode open gas discharged from the fuel cell stack when the reformed gas passes through the second heat exchanger and then passes through the first heat exchanger. Fuel cell operation method. 청구항 9에 있어서, 상기 개질가스가 상기 제1 열교환기를 통과할 때 상기 연료전지 스택에서 배출되는 냉각수 및 캐소드 오픈 가스 중 어느 하나에 의해 온도 및 습도 중 적어도 하나의 조절이 되는 것인 연료전지 운전 방법.The method of claim 9, wherein at least one of temperature and humidity is controlled by any one of a cooling water and a cathode open gas discharged from the fuel cell stack when the reformed gas passes through the first heat exchanger. . 청구항 18에 있어서, 상기 연료전지 스택에서 배출되는 냉각수 및 캐소드 오픈 가스 중 어느 하나가 상기 제1 열교환기로 유동하도록 마련되는 유로 상에 설치된 제2 열교환기 내에서 개질수가 상기 냉각수 및 캐소드 오픈 가스 중 어느 하나에 의해 열을 전달 받은 후 개질기로 공급되도록 하는 단계를 더 포함하는 연료전지 운전 방법.The method according to claim 18, wherein any one of the cooling water and the cathode open gas in the second heat exchanger provided on the flow path 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 operation method further comprising the step of being supplied to the reformer after receiving the heat by one.
PCT/KR2012/009371 2011-11-08 2012-11-08 Fuel cell system and operating method Ceased WO2013069973A1 (en)

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