WO2010058566A1 - 燃料電池の起動方法 - Google Patents
燃料電池の起動方法 Download PDFInfo
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- WO2010058566A1 WO2010058566A1 PCT/JP2009/006193 JP2009006193W WO2010058566A1 WO 2010058566 A1 WO2010058566 A1 WO 2010058566A1 JP 2009006193 W JP2009006193 W JP 2009006193W WO 2010058566 A1 WO2010058566 A1 WO 2010058566A1
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- fuel cell
- fuel
- cathode
- oxidant
- 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
- H01M8/04298—Processes for controlling fuel cells or fuel cell systems
- H01M8/04694—Processes for controlling fuel cells or fuel cell systems characterised by variables to be controlled
- H01M8/04858—Electric variables
- H01M8/04895—Current
- H01M8/0491—Current of fuel cell stacks
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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
- H01M8/02—Details
- H01M8/0202—Collectors; Separators, e.g. bipolar separators; Interconnectors
- H01M8/0267—Collectors; Separators, e.g. bipolar separators; Interconnectors having heating or cooling means, e.g. heaters or coolant flow channels
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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
- H01M8/04223—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids during start-up or shut-down; Depolarisation or activation, e.g. purging; Means for short-circuiting defective fuel cells
- H01M8/04225—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids during start-up or shut-down; Depolarisation or activation, e.g. purging; Means for short-circuiting defective fuel cells during start-up
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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
- H01M8/04223—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids during start-up or shut-down; Depolarisation or activation, e.g. purging; Means for short-circuiting defective fuel cells
- H01M8/04228—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids during start-up or shut-down; Depolarisation or activation, e.g. purging; Means for short-circuiting defective fuel cells during shut-down
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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
- H01M8/04298—Processes for controlling fuel cells or fuel cell systems
- H01M8/043—Processes for controlling fuel cells or fuel cell systems applied during specific periods
- H01M8/04302—Processes for controlling fuel cells or fuel cell systems applied during specific periods applied during start-up
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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
- H01M8/04298—Processes for controlling fuel cells or fuel cell systems
- H01M8/043—Processes for controlling fuel cells or fuel cell systems applied during specific periods
- H01M8/04303—Processes for controlling fuel cells or fuel cell systems applied during specific periods applied during shut-down
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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
- 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
- H01M8/04955—Shut-off or shut-down of fuel cells
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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
- H01M8/10—Fuel cells with solid electrolytes
- H01M2008/1095—Fuel cells with polymeric electrolytes
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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
- H01M2250/00—Fuel cells for particular applications; Specific features of fuel cell system
- H01M2250/20—Fuel cells in motive systems, e.g. vehicle, ship, plane
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T90/00—Enabling technologies or technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02T90/40—Application of hydrogen technology to transportation, e.g. using fuel cells
Definitions
- the present invention relates to a fuel cell startup method and a fuel cell power generation system that executes the method.
- Solid polymer fuel cells that use hydrogen or liquid organic compound reformed fuels, or solid polymer fuel cells that use liquid organic compounds such as methanol, ethanol, and dimethyl ether as fuel have low noise and low operating temperature ( About 70 to 80 ° C.), and it is easy to refuel. Therefore, a wide range of uses are expected as a portable power source, a power source for an electric vehicle, or a power source for an electric motorcycle, an assist type bicycle, a light vehicle such as a medical care wheelchair or a senior car.
- Non-Patent Documents 1 and 2 Non-Patent Documents 1 and 2. This degradation is believed to be due to a reverse current mechanism due to the local high potential state of the cathode.
- a method of supplying air to the cathode stepwise (Patent Document 1), and an operation of reducing the oxidant electrode potential gradient in the cell plane accompanying the start of oxidant supply at startup in the process of starting power generation in the fuel cell power generation system
- Patent Document 2 a starting method for a fuel cell power generation system
- Patent Document 3 a starting method comprising a plurality of steps such as a step of discharging a fuel cell without supplying fuel and an oxidant
- the inventors have started to develop a new start-up method different from the prior art in order to prevent oxidative deterioration of the cathode by the start-stop cycle.
- cathodic oxidative degradation is caused by a local potential difference when supplying an oxidant.
- the countermeasures against local potential difference at the time of supplying the oxidant are insufficient, and there is an essential problem in the prior art.
- Equation 1 a hydrogen oxidation reaction
- Equation 2 an oxygen reduction reaction
- Equation 3 a reaction is caused to compensate for the electrons necessary for oxygen reduction on the cathode by the oxidation reaction (Equations 3 and 4) of the cathode itself.
- the formation of such a local cell causes elution of the platinum catalyst of the cathode and oxidation of the conductive material, and the function of the cathode gradually decreases.
- PEFC power generation system a power generation system equipped with a polymer electrolyte fuel cell
- a PEFC power generation system when restarted after being stopped for a long period of time, or when the system is first started after installation at the customer site Since the anode is in an oxidized state, it becomes difficult to avoid cathodic oxidation deterioration due to local current or reverse current.
- Equation 1 The essential problem of such oxidative deterioration of the cathode is that the cathode is strongly pulled by the hydrogen oxidation reaction (Equation 1) on the anode and causes an oxygen reduction reaction (Equation 2).
- Equation 2 The first problem provided by the present invention is avoidance of Equation 2 at the time of fuel supply.
- the second problem provided by the present invention is avoidance of Equation 2 when supplying the oxidizing agent.
- Formula 2 is a key point in solving the first and second technical problems.
- the inventors have constructed a new activation method and a system for executing the method.
- (1) the cathode is covered with generated water, and the contact between the cathode and oxygen is cut off; and (2) an oxide layer is formed on the surface of the catalyst particles of the cathode, so that the voltage rise is substantially reduced.
- the first solution is a solid polymer type comprising a separator having an anode flow path for flowing fuel, a separator having a cathode flow path for supplying an oxidant, an electrode inserted between the separators, and an electrolyte membrane.
- a first step of supplying fuel to the fuel cell with the cathode covered with generated water a second step of forming an oxide layer on the cathode, and an oxidant gas to the fuel cell
- a fuel cell start-up method characterized by executing a third step of supplying and a fourth step of extracting a load current from the fuel cell.
- the second solving means determines whether or not the time difference between the latest stop time and the current time exceeds a predetermined time in the first step of the first solving means.
- a fuel cell starting method characterized by performing an operation of flowing a current to the fuel cell using an external current control means.
- the third solving means determines whether or not the voltage between the terminals of the fuel cell exceeds a predetermined voltage in the first step of the first solving means. If the voltage exceeds the predetermined voltage, the external current control is performed.
- a starting method for a fuel cell characterized in that an operation of passing a current through the fuel cell using the means is performed.
- the fourth solving means is a fuel cell starting method characterized in that in the second step of the first solving means, an operation of passing a current to the fuel cell using an external current control means is performed.
- the fifth solving means is a means for applying a DC voltage to the voltage across the terminals of the fuel cell among the fourth solving means, wherein the DC voltage is not less than 0.5V and not more than 0.8V.
- the start-up method of the fuel cell is characterized by being set as follows.
- the sixth solving means includes: a fuel supply system comprising a pipe and a switch for supplying fuel to the fuel cell; a pipe for discharging the fuel exhaust gas from the fuel cell; and a fuel cell.
- An oxidant distribution system comprising a pipe and a switch for supplying an oxidant, a pipe for discharging an oxidant exhaust gas from the fuel cell, an external current controller having a function of flowing current to the fuel cell, a switch and an external current It is to use a fuel cell system including an arithmetic circuit for operating a controller.
- the fuel cell start-up method of the present invention can prevent oxidative deterioration of the cathode without depending on the oxidation / reduction state of the anode, and can avoid a decrease in the output of the fuel cell.
- the cross-sectional structure of the single cell of this invention is shown.
- 2 shows a cross-sectional structure of a cell stack according to the present invention.
- 1 shows a configuration of a fuel cell power generation system of the present invention. It is an example of the starting sequence of this invention. It is an example of the starting sequence of this invention. It is an example of the starting sequence of this invention. It is an example of the starting sequence of this invention. It is an example of the starting sequence of this invention.
- the technical problem to be solved by the present invention is that the cathode is oxidatively deteriorated in the start-up process from supplying the fuel containing hydrogen to the fuel flow path, supplying the oxidant to the oxidant flow path, and taking out power to the outside. Is to prevent.
- the fuel is not limited to hydrogen, and the present invention can be applied to any gas or vapor (eg, methanol or dimethyl ether) that is oxidized at the anode.
- FIG. 1 shows a cross-sectional structure of a single cell of a fuel cell to which the present invention is applied.
- MEA membrane-electrode assembly
- This MEA has a three-layer structure in which the anode 101 is laminated on the upper surface of the electrolyte membrane 103 and the cathode 102 is laminated on the lower surface.
- the fuel-side separator 104 has a fuel channel 105 and is disposed so that the channel surface is in contact with the anode 101.
- the oxidant side separator 106 has an oxidant channel 107, and the channel surface 107 is in contact with the cathode 102.
- Gaskets 108 and 109 are provided on the outer peripheral portion of the separator so that the fuel and the oxidant do not leak to the outside and so that one reactant does not leak into the flow path of the other reactant.
- the separator material can be selected from any separator material such as a graphite separator made of a binder such as graphite and phenol resin, or a metal separator made of stainless steel or titanium as a base material. These separators may be subjected to a hydrophilic treatment, or composite separators added with a conductive material or a corrosion-resistant material may be used.
- the groove width and groove depth of the fuel flow path 105 can be set to optimum dimensions according to the fuel type and flow rate. If the groove width becomes too wide, the contact resistance between the separator and the MEA increases, so it is particularly desirable that the groove width is in the range of 1 to 5 mm and the depth is 0.3 to 5 mm. Similarly, for the oxidant channel 107, it is appropriate that the groove width is in the range of 1 to 5 mm and the depth is in the range of 0.3 to 5 mm.
- FIG. 2 illustrates a cross-sectional structure of a polymer electrolyte fuel cell stack having a rated output of 1 kW.
- the portion corresponding to the single cell in FIG. 1 is the single cell 201 in FIG.
- the gasket 205 By laminating the gasket 205, the electrolyte membrane of the MEA 202 (the portion where the cathode and anode of the electrolyte membrane are not formed), and the gasket 205 in this order between the two separators 204 and 219 and pressing them together, Leakage is prevented.
- a flow path for flowing cooling water is formed on the other surface of the separator 219 constituting the single cell, and a cooling cell 208 for removing heat from the single cell is formed.
- the cathode is composed of a catalyst layer and a gas diffusion layer.
- the catalyst layer is fixed to the surface of the electrolyte membrane. This may be applied to the gas diffusion layer.
- the catalyst layer is generally one in which platinum fine particles are supported on graphite powder, but other catalysts may be used.
- the graphite powder is bonded with an electrolyte binder to form a catalyst layer.
- a gas diffusion layer is provided on the catalyst layer.
- the anode is also composed of a catalyst layer and a gas diffusion layer.
- the catalyst layer supports platinum fine particles on graphite powder, or supports fine particles made of platinum alloyed with a promoter such as lutite that has the function of oxidizing and removing carbon monoxide generated during the process of fuel oxidation. And further bonded with an electrolyte binder. Other catalysts such as oxide catalysts may be used. After this catalyst layer is fixed to the other surface of the electrolyte membrane, a gas diffusion layer is provided on the catalyst layer. Moreover, the catalyst layer of the anode can be replaced with one applied to the gas diffusion layer.
- a plurality of single cells 201 are connected in series, current collecting plates 213 and 214 are installed at both ends, and further, tightened with an end plate 209 from the outside via an insulating plate 207. If the end plate is an insulating material, the insulating plate 207 can be omitted. Bolts 216, springs 217, and nuts 218 are used as fastening parts.
- the tightening structure is not limited to the structure shown in FIG. 2 as long as both end plates 209 can hold the compressive force in the inner direction.
- the cooling flow path surface of the cooling cell in contact with the current collector plates 213 and 214 is formed using the flat plate component 203.
- the fuel is supplied from the fuel supply connector 210 provided on the left end plate 209, passes through each single cell 201, and is provided on the opposite end plate 209 after the fuel is oxidized on the anode of the MEA.
- the fuel is discharged from the fuel discharge connector 222.
- hydrogen or a gas containing hydrogen is particularly effective as the fuel, but other organic vapors such as methanol and dimethyl ether and liquid organic fuels such as an aqueous methanol solution can be used.
- the oxidant is supplied from the oxidant supply connector 211 provided on the left end plate 209 shown in FIG. 8 and discharged from the oxidant discharge connector 223 of the opposite end plate 209. Air was supplied through piping from an air blower installed outside the battery.
- the cooling water is supplied from the cooling water supply connector 212 provided on the end plate 209 and discharged from the cooling water discharge connector 224 of the opposite end plate 209.
- the cooling water discharged from here is removed by the cold water in the heat exchanger, and is supplied again to the cooling water supply connector 212.
- a pump was used to circulate the cooling water. The heat exchanger and the pump are omitted from FIG.
- a cell stack composed of 25 single cells 201 was manufactured using the above-described component configuration.
- the cell stack was filled with helium gas equivalent to 50 kPa with respect to atmospheric pressure from the pipe connector of fuel, oxidant, and cooling water, and the internal pressure change was measured with a pressure sensor.
- the initial pressure of 50 kPa maintained a high pressure of 49.1 kPa even after 10 minutes, and it was confirmed that almost no leakage to the outside occurred.
- the cell stack was incorporated into the fuel cell power generation system so as to have the configuration shown in FIG.
- the cell stack 301 is arranged in the center of the system, and fuel is supplied from the reformer 302 to the cell stack 301 via the fuel distribution system 311.
- a flow rate controller 310 having a switch for starting or stopping the supply of fuel is provided.
- an organic fuel such as city gas or kerosene can be used.
- a mass flow controller or the like can be used in addition to a general valve.
- the reformer 302 may be changed to a pure hydrogen storage device.
- the fuel distribution system 312 on the discharge side can be omitted.
- Oxidants such as air and oxygen can be supplied to the fuel cell from the oxidant supply device 303 via the oxidant distribution system 314.
- a fan, a blower, an air cylinder, or the like can be used for the oxidant supply device 303.
- a flow rate controller 313 having a switch for starting or stopping the supply of fuel is provided.
- the flow rate controller 313 provided with a switch may be omitted.
- the oxidant After passing through the cathode flow path of the cell stack 301, the oxidant is discharged from the oxidant distribution system 315 as it is outside the cell stack 301, or is discharged after passing through the heat exchanger 304.
- the refrigerant of the heat exchanger 304 cold air supplied from a fan, circulating water from a water heater, or the like can be used.
- the external terminals (positive electrode and negative electrode) of the cell stack 301 are connected to the external current controller 316.
- the external current controller 316 includes a short circuit 307 or a DC power supply 308 in addition to a load device 306 such as an inverter that operates during normal operation. Inside the external current controller 316, operations of the load device 306, the short circuit 307, and the DC power supply 308 are controlled by the switch 305.
- either the short circuit 307 or the DC power supply 308 can be operated by the switch 305.
- power necessary for the operation of the short circuit 307 and the DC power supply 308 is supplied from a secondary battery or a power system.
- a signal is transmitted from the arithmetic circuit 320, and a flow rate controller including a reformer 302, an air supply device 303, and a switch for fuel and oxidant through a signal line 321.
- a flow rate controller including a reformer 302, an air supply device 303, and a switch for fuel and oxidant through a signal line 321.
- 310, 313, switch 305, load device 306, short circuit 307, and DC power supply 308 can be controlled.
- the first step is to form a water film (generated water) on the surface of the catalyst particles of the cathode and make it difficult for oxygen to reach the catalyst surface by the film.
- the water film can be easily formed by short-circuiting the external terminals of the cell stack while supplying fuel to the anode without supplying an oxidant to the cathode side. In this operation, it is sufficient to cover the surface of the cathode catalyst with the produced water in the form of an extremely thin film, so that very little oxygen is sufficient. This is different from the method that actively consumes oxygen.
- the anode potential increases due to the short circuit current, and the accompanying oxidation reaction of the catalyst and the conductive agent occurs.
- the anode potential is an electric double layer region of platinum (from 0.4 to 0.6 V based on the hydrogen equilibrium potential at the hydrogen concentration of the fuel). It must not exceed. This is because if the potential is kept higher than this, the oxidation reaction of carbon and the dissolution reaction of platinum proceed. Therefore, it is important to supply the fuel before the fuel contained in the anode channel is consumed.
- the switch 305 When necessary hydrogen is present in the anode flow path in advance, the switch 305 is simply operated, the short circuit 307 and the cell stack 301 are connected, and a short circuit current is caused to flow, so that a water film is formed on the cathode catalyst particle surface. Can be formed.
- a current consumption circuit incorporating a resistor can be used as the short circuit 307. Such a method can be realized in a PEFC power generation system driven by pure hydrogen. This is because the volume of fuel in the fuel cell is large and the short-circuit operation is completed with a small amount of energization that covers the surface of the cathode catalyst with the produced water in an extremely thin film form.
- the current value at the time of short-circuiting can be set to an arbitrary pattern depending on the resistance value of the short-circuit circuit 307 and the element specifications, and finally the short-circuiting is performed until the potential difference between the anode and the cathode becomes 0.1 V or less. More desirably, the short-circuit current is substantially zero, that is, the potential difference is substantially zero. This is because when the potential difference is higher than 0.1 V, the amount of the water film is insufficient, and the water evaporates into the gas phase existing in the cathode flow path. Further, it is more desirable that the short-circuit current is as large as possible because the generated water can be selectively formed on the catalyst surface with a small amount of energization.
- the current value is 1/10 or more of the rated current value, more preferably 25% or more.
- the current value is 0.01 mA / cm 2 or more, more preferably 0.025 mA / cm 2 or more.
- a film of generated water can be formed on the cathode by the short-circuit operation in the first step described above.
- the hydrogen oxidation reaction according to Equation 1 proceeds upstream of the anode channel
- the oxygen reduction reaction according to Equation 2 proceeds for a short time at the opposite side of the channel via MEA (that is, the cathode surface).
- the electrons required for Equation 2 are not supplied by the oxidation reaction (Equations 3 and 4) of the cathode downstream of the cathode flow path, but are directly supplied from another adjacent single cell. This electron is the oxidation current of Equation 1 at the anode at the corresponding position.
- the reason why the electrons are supplied from the adjacent cells in this way is that the distance between the adjacent cells is smaller than the distance from the downstream position of the cathode flow channel of the same cell, and the electrical resistance becomes relatively small.
- the operation of the first step can be omitted.
- the omission is possible because it is known in advance that hydrogen is present in the anode flow path, the voltage between the terminals of the cell stack is close to zero, and more precisely, each cell voltage becomes 0.1 V or less. Therefore, it can be confirmed easily.
- the fuel supply may be temporarily stopped after forming a coating of generated water on the cathode.
- an oxide layer is formed on the surface of the cathode catalyst coated with the produced water.
- the purpose of this is to avoid a sudden rise in the potential of the cathode located upstream of the cathode channel at the same time as the generated water evaporates to the oxidant side when the oxidant is supplied to the cathode channel. It is said.
- the cathode potential rises rapidly, the oxidative degradation reaction of the downstream cathode proceeds according to equations 3 and 4.
- an oxide film on the surface of platinum particles when the cathode is composed of a platinum catalyst and a carbon conductive agent. If an oxide film is formed in advance in this way, the potential is unlikely to rise even if the generated water disappears due to evaporation.
- An important objective of the second step is to form a surface oxide on the cathode catalyst in a state where the surface of the cathode catalyst is covered with the produced water, in other words, in a state where the cell voltage is 0.1 V or less. . By simply applying the voltage, the generated water is not formed on the cathode, so this operation cannot be realized.
- the oxide film can be formed on the surface of the cathode catalyst by operating the switch 305 and connecting the cell stack 301 and the DC power source 308.
- the terminal voltage at this time is set according to the type of catalyst. For example, when a platinum catalyst is used, it is higher than the potential region of the electric double layer (which is 0.4 to 0.6 V based on the hydrogen equilibrium potential at the hydrogen concentration of the fuel) and is higher than the oxidation start potential of the conductive agent. (Approximately 0.9 V with respect to the hydrogen equilibrium potential) or less.
- Pt (OH) 2 (Formula 5) or PtO (Formula 6) can be formed on the surface layer of Pt by the reaction of the following formula.
- the oxidation reaction proceeds at the cathode, and the water electrolysis reaction (reaction that generates hydrogen gas from water) proceeds on the opposite surface (anode) of the MEA, so that the anode is not damaged. Therefore, in the second step, the supply of hydrogen to the anode may be continued from the first step, or the supply may be temporarily stopped.
- the cathode potential tends to approach the normal open circuit potential (1 to 1.1 V) after the oxidant is supplied in the third step described later. Therefore, in the fourth step, it is necessary to take out the current promptly after the oxidant is supplied. This current can be consumed by the short circuit 307 in FIG. 3, but it is desirable to quickly connect the load device 306 and the cell stack 301 because of loss due to Joule heat generation. Therefore, in the second step, by controlling the high cell voltage capable of forming an oxide film on the platinum particle surface, the power output from the cell stack in the subsequent third and fourth steps is made as small as possible. It becomes possible.
- the second step if the voltage between the terminals is controlled to be higher than the potential region of the electric double layer and lower than the oxidation start potential of the conductive agent, a large inrush current to the load device 306 can be suppressed. it can. As a result, damage to the load device 306 can be prevented, and an increase in the size of the load device 306 to cope with a large current can be avoided.
- the cathode potential is set in the electric double layer region by direct current polarization, the potential cannot be maintained unless a large current is supplied to the cell stack immediately after the oxidant is supplied. May cause damage.
- the cathode potential when the cathode potential is set to be equal to or higher than the oxidation start potential of the conductive agent, the conductive agent is oxidized by DC polarization, and the electron network of the cathode is destroyed. The same phenomenon occurs when DC polarization is omitted.
- the cathode catalyst is oxidized (Equations 5 and 6), but the cathode potential is adjusted to a potential that does not oxidize the conductive agent, thereby avoiding cathode deterioration when supplying the oxidizing agent. can do.
- the control is performed in the range of the cathode potential of 0.5 to 0.8 V in consideration of the cell voltage variation due to the influence of the history during stoppage or storage. When the cell voltage variation is small, the life of the fuel cell can be further extended by controlling the cathode potential to 0.6 to 0.8V.
- the oxidant is supplied in the third step, and the load from the fuel cell in the fourth step.
- An operation of taking out current can be performed.
- the supply amount of the oxidizing agent may be increased stepwise, or an oxidizing agent having a flow rate corresponding to the rated power generation may be supplied at a time. It is more preferable that the time interval between the third step and the fourth step be performed at the same time as the oxidant gas passes through the cathode flow path of the cell stack or almost immediately before entering the cathode flow path.
- load current is taken out from the fuel cell.
- the condition is that fuel is supplied to the fuel cell before the load current is extracted. This may be continued fuel supply from the first step, or after the fuel supply is temporarily stopped in the second and third steps, the fuel supply is resumed immediately before the start of the fourth step. Also means good.
- the cell stack 301 and the short circuit 307 are temporarily connected, and the power from the cell stack 301 is temporarily connected to the short circuit 307.
- the method of consumption can also be taken.
- the calorific value is large, it is desirable to promptly connect the cell stack 301 and the load device 306.
- the first to fourth steps of the present invention oxygen reduction inhibition by water coating and catalyst surface protection by oxide are realized, and cathode oxidation deterioration due to reverse current and local current is effectively avoided. .
- the first step can be omitted.
- FIG. 4 is a typical example of a start-up sequence when it is unclear whether or not the cathode is covered with generated water. It is assumed that the cathode channel is filled with air.
- the short circuit (307 in FIG. 3) is turned on and fuel is supplied.
- Switching to the short circuit 307 uses the switch 305 of FIG. By this operation, the cathode can be covered and protected with generated water.
- the short circuit 307 is turned off and the first step is completed.
- the DC power supply (DC power supply 308 in FIG. 3) is turned on.
- the cathode set potential at this time is set to a potential that does not oxidize the conductive agent, although an oxide film is formed on the cathode catalyst based on the anode potential (Equations 5 and 6).
- the average voltage for forming the oxide was set to 0.7 V per unit cell. When the current becomes nearly zero, the end point of the oxide formation reaction is known. Therefore, the DC power supply 308 is turned off, and the second step ends.
- an oxidant is supplied to the fuel cell (cell stack) 301 of FIG.
- the fuel is continuously supplied from the first step.
- the supply of fuel may be stopped at the end of the first step, and the fuel may be supplied again simultaneously with the supply of the oxidant in the third step.
- the reformed gas of 70% hydrogen and 30% carbon dioxide was used as fuel, and air was used as oxidant.
- These supply flow rates were respectively set to a fuel flow rate and an air flow rate supplied when a rated output of 1 kW was obtained.
- the rated current was 60 A, the fuel utilization rate was 85%, and the oxidant utilization rate was 55%.
- the fourth step is executed as soon as possible or substantially at the same time, and the load current is taken out from the cell stack 301.
- a load device load device 306 in FIG. 3
- a short circuit 307 such as a resistance circuit may be temporarily substituted.
- FIG. 5 is a typical example of a start-up sequence that can be applied when it is known that the cathode is covered with generated water. Assume that the anode channel is filled with fuel, and the cathode channel is filled with air.
- the first step can be omitted because the surface of the cathode is covered with the generated water.
- This predetermined time can be confirmed by supplying fuel to the anode from the storage state and checking whether the cell voltage of the fuel cell rises. Increasing the cell voltage by supplying fuel means that the cathode potential is high. If the cell voltage rise exceeds the electric double layer region (corresponding to a cell voltage of 0.4 to 0.6 V), it is determined that the generated water is completely peeled from the cathode. At least the predetermined time is set within a time during which the cell voltage does not exceed 0.6V. In consideration of long-term durability, it is desirable to set the predetermined time within a time during which the cell voltage increase can be kept below 0.4V.
- the first step short circuit on, fuel supply, short circuit off is executed as in FIG.
- FIG. 6 is an example of a startup sequence focusing on the cell voltage, that is, the voltage between terminals.
- the cell voltage that is, the voltage between terminals.
- it is determined whether or not produced water exists on the cathode by monitoring the voltage between the terminals. You may measure the voltage of each cell and judge the presence or absence of produced water about all the cells. If fuel is present at the anode, the cathode potential is measured based on the fuel and it is confirmed that it is below a predetermined voltage. As a result, it can be determined that the produced water is covering and protecting the cathode.
- the voltage between terminals can be easily determined. Therefore, the product of the threshold value of each cell voltage and the number of cells may be used as the reference voltage of the voltage between terminals. In addition, what is necessary is just to add the voltage measuring device for measuring the voltage between the terminals of the fuel cell 301 when performing this measurement.
- the predetermined voltage is set within a range in which the average cell voltage does not exceed at least the electric double layer region (corresponding to a cell voltage of 0.4 to 0.6 V). This is because it is determined that the generated water is completely removed from the cathode. That is, the predetermined voltage is set within a time during which the cell voltage does not exceed 0.6V. In consideration of long-term durability, it is desirable to set the predetermined time within a time during which the cell voltage increase can be kept below 0.4V. More preferably, the average cell voltage is set to a voltage that is 0.1 V or less (less than the product of 0.1 V and the number of cells).
- the first operation of the sequence shown in FIG. 6 is to measure the voltage between terminals and determine whether or not the value is at a predetermined value.
- This predetermined value corresponds to the above-described reference voltage.
- the first step can be omitted when the inter-terminal voltage is less than or equal to a predetermined value. Thereafter, the cell stack can be activated by sequentially executing operations corresponding to steps 2, 3, and 4 in FIG.
- the procedure shown in FIG. 4 was selected as the standard activation method, and the start-stop cycle test of the previous cell stack was performed.
- the fuel cell power generation test was performed with a fuel utilization rate of 85%, an oxidant utilization rate of 55%, a current of 60 A, and a power generation time of 5 hours.
- the stop operation was performed by using the short circuit 307 of FIG.
- the value of the current flowing through the short circuit is 0 for the cell voltage.
- the resistance value was set so that the rated current would flow at 8V.
- the cooling water inlet temperature was set to 30 ° C., and the battery was rapidly cooled. Then, after confirming that it became 30 degreeC after about 1 hour, the cooling water inlet temperature was heated up again to 70 degreeC, and the previous electric power generation test was restarted. As described above, the start-stop cycle test by repeating power generation and cooling was performed 200 times.
- the reduction rate of the output was only less than 0.1% after 200 cycle tests with respect to the initial rated output.
- the above-mentioned stopping method was the same, and after the anode was purged with nitrogen immediately after the stopping operation, 200 start-stop cycle tests were performed by the start-up method in which the first step was omitted from the start-up sequence in FIG. As a result, the output decreased by 8% of the initial value after 200 cycle tests.
- the start-stop cycle test was performed 200 times by the start-up method in which the stop method was the same and the second step was omitted from the start-up sequence in FIG. As a result, the output decreased by 5% of the initial value after 200 cycle tests.
- This starting method is a particularly effective method for starting a polymer electrolyte fuel cell using a fuel containing hydrogen.
- the present invention can also be applied to a fuel cell using such a liquid fuel.
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Abstract
Description
この劣化は、カソードの局所的な高電位状態による逆電流メカニズムによるものと考えられている。
1/2O2+2H++2e-→H2O …式2
Pt→Pt2++2e- …式3
C+2H2O→CO2+4H++4e- …式4
されていることを特徴とする燃料電池の起動方法である。
Pt+H2O→PtO+2H++2e- …式6
さらにインバータを交流式電子負荷装置に接続し、セルスタックの電力を消費できるようにした。
8Vのときに定格電流が流れるように抵抗値を設定した。
また、各のステップを実行する機器や周辺回路,制御機器は、それらを実行できれば良いので、任意に選定することができる。本起動方法は、水素を含む燃料を用いる固体高分子形燃料電池の起動に特に有効な方法である。
102 カソード
103 電解質膜
104 燃料流路を有するセパレータ
105 燃料流路
106 酸化剤流路を有するセパレータ
107 酸化剤流路
108 アノード側ガスケット
109 カソード側ガスケット
201 単セル
202 膜-電極接合体(MEA)
203 冷却水流路に対面する平板部品
204 本発明のセパレータ(単セル用)
205 ガスケット(シール)
207 絶縁板
208 冷却セル
209 端板
210 燃料供給用コネクタ
211 酸化剤供給用コネクタ
212 冷却水供給用コネクタ
213,214 集電板
216 ボルト
217 ばね
218 ナット
219 冷却水流路を有するセパレータ
222 燃料排出用コネクタ
223 酸化剤排出用コネクタ
224 冷却水排出用コネクタ
301 セルスタック
302 燃料製造装置(改質器)
303 酸化剤供給装置
304 熱交換器
305 切替器
306 負荷装置
307 短絡回路
308 直流電源
310 流量制御器
311 燃料流通系統(供給側)
312 燃料流通系統(排出側)
313 流量制御器
314 酸化剤流通系統(供給側)
315 酸化剤流通系統(排出側)
316 外部電流制御器
320 演算回路
321 信号線
Claims (6)
- 燃料を流通させるアノード流路を有するセパレータと、酸化剤を供給するカソード流路を有するセパレータと、前記セパレータの間に挿入された電極と電解質膜からなる固体高分子形燃料電池の起動方法において、
カソードが生成水によって被覆された状態にて燃料電池に燃料を供給する第一ステップと、
カソードに酸化物層を形成する第二ステップと、
燃料電池に酸化剤ガスを供給する第三ステップと、
燃料電池から負荷電流を取り出す第四ステップを実行することを特徴とする燃料電池の起動方法。 - 前記第一ステップにおいて、最新の停止時刻と現在の時刻との時間差が所定時間を超えたか否かを判断し、所定時間を超えた場合に、外部電流制御手段を用いて燃料電池に電流を流す操作を行うことを特徴とする請求項1に記載の燃料電池の起動方法。
- 前記第一ステップにおいて、燃料電池の端子間電圧が所定電圧を超えたか否かを判断し、所定電圧を超えた場合に、外部電流制御手段を用いて燃料電池に電流を流す操作を行うことを特徴とする請求項1に記載の燃料電池の起動方法。
- 前記第二ステップにおいて、外部電流制御手段を用いて燃料電池に電流を流す操作を行うことを特徴とする請求項1に記載の燃料電池の起動方法。
- 前記外部電流制御手段が、燃料電池の端子間電圧に直流電圧を印加する手段であって、前記直流電圧が0.5以上0.8V以下に設定されていることを特徴とする請求項4に記載
の燃料電池の起動方法。 - 燃料を流通させるアノード流路を有するセパレータと、酸化剤を供給するカソード流路を有するセパレータと、前記セパレータの間に挿入された電極と電解質膜からなる固体高分子形燃料電池の起動方法を実行する燃料電池システムにおいて、
前記燃料電池に燃料を供給する配管と開閉器と、前記燃料電池から燃料排ガスを排出する配管からなる燃料流通系統と、
前記燃料電池に酸化剤を供給する配管と開閉器と、前記燃料電池から酸化剤排ガスを排出する配管からなる酸化剤流通系統と、
前記燃料電池に電流を流す機能を具備した外部電流制御器と、
前記開閉器と前記外部電流制御器を操作する演算回路
からなる請求項1記載の燃料電池システム。
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JP2010539143A JP5483599B2 (ja) | 2008-11-19 | 2009-11-18 | 燃料電池の起動方法 |
EP09827347.7A EP2360763A4 (en) | 2008-11-19 | 2009-11-18 | METHOD FOR STARTING BATTERY OF FUEL CELLS |
US12/920,432 US8647784B2 (en) | 2008-11-19 | 2009-11-18 | Fuel cell stack start method preventing cathode deterioration |
CN200980105941.9A CN101953011B (zh) | 2008-11-19 | 2009-11-18 | 燃料电池的起动方法 |
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US (1) | US8647784B2 (ja) |
EP (1) | EP2360763A4 (ja) |
JP (1) | JP5483599B2 (ja) |
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WO (1) | WO2010058566A1 (ja) |
Cited By (2)
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WO2012079472A1 (zh) * | 2010-12-17 | 2012-06-21 | 北京北方微电子基地设备工艺研究中心有限责任公司 | 半导体设备 |
CN109216735A (zh) * | 2017-07-07 | 2019-01-15 | 奥迪股份公司 | 燃料电池的切断 |
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JP6122406B2 (ja) * | 2013-09-27 | 2017-04-26 | 本田技研工業株式会社 | 燃料電池スタック |
US10375901B2 (en) | 2014-12-09 | 2019-08-13 | Mtd Products Inc | Blower/vacuum |
KR101703607B1 (ko) * | 2015-07-08 | 2017-02-22 | 현대자동차 주식회사 | 촉매 활성화 시동 장치 및 이를 이용한 촉매 활성화 시동 방법 |
JP6700105B2 (ja) * | 2016-05-31 | 2020-05-27 | 日立造船株式会社 | 燃料電池システム |
CN108075154B (zh) * | 2016-11-17 | 2020-04-07 | 中国科学院大连化学物理研究所 | 一种氢空质子交换膜燃料电池无增湿条件启动及运行方法 |
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US8647784B2 (en) | 2014-02-11 |
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JP5483599B2 (ja) | 2014-05-07 |
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