Classifications

• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M8/00—Fuel cells; Manufacture thereof
  • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
  • H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
  • H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M8/00—Fuel cells; Manufacture thereof
  • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
  • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
  • H01M8/04313—Processes for controlling fuel cells or fuel cell systems characterised by the detection or assessment of variables; characterised by the detection or assessment of failure or abnormal function
  • H01M8/0438—Pressure; Ambient pressure; Flow
  • H01M8/04388—Pressure; Ambient pressure; Flow of anode reactants at the inlet or inside the fuel cell
• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M8/00—Fuel cells; Manufacture thereof
  • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
  • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
  • H01M8/04313—Processes for controlling fuel cells or fuel cell systems characterised by the detection or assessment of variables; characterised by the detection or assessment of failure or abnormal function
  • H01M8/0438—Pressure; Ambient pressure; Flow
  • H01M8/04395—Pressure; Ambient pressure; Flow of cathode reactants at the inlet or inside the fuel cell
• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M8/00—Fuel cells; Manufacture thereof
  • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
  • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
  • H01M8/04313—Processes for controlling fuel cells or fuel cell systems characterised by the detection or assessment of variables; characterised by the detection or assessment of failure or abnormal function
  • H01M8/04537—Electric variables
  • H01M8/04574—Current
  • H01M8/04589—Current of fuel cell stacks
• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M8/00—Fuel cells; Manufacture thereof
  • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
  • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
  • H01M8/04313—Processes for controlling fuel cells or fuel cell systems characterised by the detection or assessment of variables; characterised by the detection or assessment of failure or abnormal function
  • H01M8/04537—Electric variables
  • H01M8/04604—Power, energy, capacity or load
  • H01M8/04619—Power, energy, capacity or load of fuel cell stacks
• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M8/00—Fuel cells; Manufacture thereof
  • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
  • H01M8/04298—Processes for controlling fuel cells or fuel cell systems
  • H01M8/04694—Processes for controlling fuel cells or fuel cell systems characterised by variables to be controlled
  • H01M8/04746—Pressure; Flow
  • H01M8/04753—Pressure; Flow of fuel cell reactants
• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M8/00—Fuel cells; Manufacture thereof
  • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
  • H01M8/04082—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
  • H01M8/04104—Regulation of differential pressures
• • 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 an associated control method.
• Fuel cells are used to provide energy either for stationary applications, or in the aeronautical or automotive field
• the standard PEM (“Proton Exchange Membrane”) type fuel cells comprise elementary cells which consist in particular of a bipolar plate and an electrode / membrane assembly commonly called MEA ("Membrane Electrodes Assembly" in the English language).
• MEA Electrode Electrodes Assembly
• the electrochemical reactions which take place in the fuel cell make it possible to supply electrical energy.
• a cell is supplied with hydrogen at the anode, for example by a reformer or a hydrogen reservoir, and with oxygen at the cathode. usually by a group of air compression
• the aim is to achieve the best possible system performance.
• Optimizing the efficiency of such a system is sought by reducing the power losses generated by the various auxiliary elements, and by optimizing the operating efficiency of different components. More particularly, the efficiency of the system depends directly on the initial choice of the operating voltage chosen for the maximum power of the fuel cell Generally, the operating voltage chosen for the maximum power of the battery is about 0.6V, by compromise between compactness and cost of the battery
• Condensers are arranged at the outlet of the anode and the cathode of the fuel cell, making it possible to condense the outlet gases of the cell. It is important to be able to increase the temperature of the end of condensation at the outlet of the cell. temperature end of condensation, an average temperature representative of the temperatures at the outlet of the anode and cathodic condensers located at the outlet of the fuel cell
• On-stoichiometry is understood to mean Ra in hydrogen and by following stoichiometry Rc oxygen, an amount of reagents provided greater than the amount that would be strictly necessary for the reactions considered (stoechiomét ⁇ e 1)
• current density is meant the local intensity value per surface unit.
• the current density corresponds to the intensity delivered by the cell, divided by the active surface value of a battery cell plus the power delivered by the battery is low, the lower the battery density delivered by the battery is low
• An object of the invention is to optimize the operation of the cell and the temperatures at the end of anodic and cathodic condensations, for small current density values delimited by the cell.
• a fuel cell system comprising means for supplying hydrogen to the anode of the cell, means for supplying oxygen to the cathode of the cell, and a control unit.
• the system also comprises first control means for controlling the cell. supply of hydrogen to the anode of the cell and second means of controlling the supply of oxygen to the cathode of the cell.
• the system comprises the first means for determining hydrogen supraichiometry in the anodic oxidation half - reaction, and second means for determining an omet ⁇ e oxygen super - stoichi of the cathodic reduction half - reaction, said first and second means for controlling are adapted to adapt said hydrogen and oxygen stoichiometries to the stack depending on the power demanded from the stack.
• the temperature at the outlet of the condensers situated at the outlet of the fuel cell is then higher, which makes it possible to limit the vol ume of the condensers and to improve the efficiency of the system.
• the power demanded from the battery is a function of the current density requested from the battery
• the current density delivered by the battery is a parameter that is well known to handle, the power demand passing through a control intensity or current density.
• said first control means are adapted to maintain said constant hydrogen stoichiometry when the current density requested at the stack is lower than a first value, and increasing as a function of the current density requested at the stack when the current density requested at the stack is greater than said first value and lower than a second value greater than said first value.
• said second control means are adapted to maintain said constant oxygen stoichiometry when the density current requested to the stack is less than said first value, and increasing as a function of the current density requested from the stack when the current density requested from the stack is greater than said first value and lower than said second value.
• said first determination means comprise first connected computing means. a first flowmeter disposed at the inlet of the anode of the cell, and said second determination means comprise second calculation means connected to a second flowmeter arranged in an integer of the cathode of the cell;
• the system comprises a sensor for measuring the intensity delivered by the battery 1
• the corresponding current density is calculated from this mesuie intensity and the active surface of a battery cell.
• said first value is substantially equal to 0.2 A / cm 2
• said second value is substantially equal to 0.6 A / cm 2
• said first control means are adapted to maintain said on-stoichiometry in linearly increasing hydrogen law sque the current density requested to the stack is greater than the first adite value and lower than said second value De Pl us, said second control means are adapted to maintain said on-stoichiometry in linearly increasing oxygen law sque the current density requested to the stack is greater than said second value and lower than said first value
• a method of controlling a fuel cell system characterized by supplying the anode of the cell with hydrogen and oxygenating the same. cathode of the cell, so as to respectively adapt the superstoichiomét ⁇ es hydrogen of the half-anodic oxidation reaction and oxygen of the cathodic reduction half-reaction according to the power demanded pi pi
• the power demanded from the cell is a function of the current density required from the cell.
• said hydrogen stagnation is maintained constant when the density The current requested from the stack is less than a first value, and increasing as a function of the current density requested from the stack when the deny of current requested from the stack is greater than said first value and less than a second value.
• the constant oxygen stoichiometry is maintained when the required density of the stack is lower than the first value, and increasing as a function of the current density required at the first value. the stack obtains the current density requested from the stack is greater than said first value and lower than said second value
• FIG. 1 is a block diagram of a system according to one aspect.
• FIG. 2 illustrates a method according to one aspect of the invention
• FIG. 3 illustrates an adaptation of the anodic and cathodic over-stoichiometries according to one aspect of the invention.
• Fig 1 represents a system according to the invention, embarked in a motor vehicle
• the system comprises a fuel cell 1 comprising an anode portion A and a cathode portion C, a reformer 2 for supplying hydrogen fuel cell 1
• the system comprises also a burner 3 for heating the entire system, during the start-up phase, as well as regulating the temperature during nominal operation
• the fuel cell 1 is designed so that the voltage chosen for the maximum power
• the burner 3 also supplies the energy required for the reforming reaction and makes it possible to oxidize the hydriogen when it uses a return of the anode output gases from the fuel cell 1. also to provide the energy necessary for the vaporization of the water and the fuel necessary for the ieformer 2.
• the system also comprises an air compression unit 4, which supplies oxygen, generally in the form of compressed air, to the fuel cell 1, and the burner 3, respectively via ducts 5 and 6. air 4 also feeds into air a preferred oxidation reactor 7 via a conduit 8
• the system further comprises an electronic control unit 9 also used for other purposes such as vehicle stability control or braking, connected at reformer 2, the burner 3, the fuel cell 1 and the air compression unit 4 respectively by connections 10, 11, 12 and 13.
• the system also comprises a fuel supply device 14, comprising a fuel tank, connected to the electronic control unit 9 via a connection 15.
• This fuel supply device 14 supplies the burner 3 with fuel.
• a vaporizer 16 which vaporizes the water and the fuel input of the reloimeur 2
• the burner 3 and the vapo ⁇ sateui 16 are respectively fueled by conduits 17 and 18
• At the outlet of refoi die 2 are present two reaction reactors 19 and 20 of These two reactors 19 and 20, as well as the preferred oxidation reactor 7, allow the carbon monoxide content CO of the reformate fueling the fuel cell 1 to be considerably reduced because the monoxide of CO Carbon Poisons Fuel Cells
• Various heat exchangers 21, 22 and 23 are present to cool gas streams
• the system also includes various condensers 24, 25 and 26 for receiving water and sending it, respectively by conduits 27 28 and 29 in a water supply device 30, comprising a tank of water, allowing in particular food the vapo ⁇ sateui 16 in water through a conduit 31
• the outlet gases from the anode A are fed to the condenser 25 via a pipe 39.
• the outlet gases from the condenser 25 then feed the combustion chamber 3 through a pipe 40.
• the outlet gases from the cathode portion C of the fuel cell 1 are fed to the condenser 26 through a conduit 41, before being mixed, through a conduit 42, to the exit gases of the exchanger 23
• the mixture is then fed to the turbine 4
• the device of The water supply 30 is also controlled by the electronic control unit 9 via a connection 43.
• the electronic control unit 9 comprises a first module 44 for controlling the supply of hydrogen in the cell, for example by acting on the reformer 2, as well as a second module 45 for controlling the oxygen supply of the cathode of the battery, for example by acting on the air compression group 4
• the electronic control unit 9 furthermore comprises a first module 46 for determining an over-stoichiometry Ra in hydrogen of the anodic oxidation half-reaction, and a second module 47 for determining an on-stoichiometry Rc in oxygen of the cathodic reduction half-reaction.
• the first and second modules 46 and 47 determine the respective over-stoichiometries Ra and Rc, as a function of the different flow rates feeding the battery 1, supplied for example by respective flow meters 48 and 49.
• the flowmeter 48 is located at the inlet of the supply in hydrogen from the anode A of the pile
• the flow meter 49 is located at the inlet of the oxygen supply of the cathode C of the cell 1.
• the flow meters 48 and 49 are respectively connected to the electronic control unit 9 by connections 50 and 51. Electrical energy supplied by the battery with an output cable 52 is measured by a current sensor 53 connected to the electronic control unitc 9 by a connection 54 the electronic control unit calculates the current density corresponding to the intensity provided by the sensor 53.
• the power demanded from the battery 1 is, for example, a function of the current density requested from the battery 1.
• the first and second control means 44 and 45 test (step 60) if the current density requested at the stack 1 is lower than the first value If the current density demanded at the cell 1 is lower than the first value, the first and second control means 44 and 45 maintain the over-stoichiometry Ra and Rc constant as a function of the current density requested at the cell 1 (step 61). If the current density requested at the stack 1 is greater than or equal to the first value, the first and second control means 44 and 45 test (step 62) if the current density requested at the stack 1 is less than the second value. .
• the first and second control means 44 and 45 maintain the increasing on-stoichiometry Ra and Rc as a function of the density of the current requested on stack 1 (step 63).
• the first and second control means 44 and 45 maintain the over-stoichiometry Ra and Rc constant as a function of the current density requested at the stack 1
• the super-stoichiometry Ra in hydrogen of the anodic oxidation half-reaction has a value of 1, 30, and the super-stoichiometry Rc in oxygen of the cathodic reduction half-reaction has a value of 1.8. .
• the invention makes it possible to adapt the respective super-stoichiometries Ra and Rc, as a function of the current density delivered by the fuel cell 1.
• FIG. 3 An example of such an adaptation of the superstoichiometries as a function of the current density required of the stack is illustrated in FIG. 3.
• the first current density value is 0.2 A / cm 2
• the second current density value is 0.6 A / cm 2 .
• the burner 3 can only be fed with the gases coming from the anode outlet of the fuel cell 1, or, if the reformer 2 needs more thermal energy, the burner 3 can also be powered. by fuel.
• the expression of the efficiency of the system then varies according to the supply of the burner 3.
• the invention makes it possible to increase the efficiency of the fuel cell system by about 2 to 5%, and to reduce by 2 to 4% the consumption of the air supply device of the fuel cell system. low power demand on the stack.
• condensation end temperature is increased from 4 to 8 0 C, which makes it possible to reduce the volume of the outlet condensers of the fuel cell.

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• Life Sciences & Earth Sciences (AREA)
• Engineering & Computer Science (AREA)
• Manufacturing & Machinery (AREA)
• Sustainable Development (AREA)
• Sustainable Energy (AREA)
• Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Electrochemistry (AREA)
• General Chemical & Material Sciences (AREA)
• Fuel Cell (AREA)

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• 2005
  • 2005-02-01 FR FR0500966A patent/FR2881577B1/fr not_active Expired - Fee Related
• 2006
  • 2006-01-19 JP JP2007552686A patent/JP2008529228A/ja active Pending
  • 2006-01-19 US US11/815,283 patent/US20080131743A1/en not_active Abandoned
  • 2006-01-19 WO PCT/FR2006/050028 patent/WO2006082331A1/fr active Application Filing
  • 2006-01-19 EP EP06709414A patent/EP1846972A1/de not_active Withdrawn

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