JP5759597B2 - Control method of fuel cell system - Google Patents

Description

  The present invention relates to a control method for a fuel cell system, and more particularly to a technique for controlling the supply start timing of an oxygen-containing gas to a fuel cell stack.

In Patent Document 1, fuel gas (hydrogen) is supplied to the anode electrode of the fuel cell, and then oxidant gas (air) is supplied to the cathode electrode, thereby deteriorating the fuel cell (corrosion of separators, membrane electrodes, etc.). ) Is disclosed.
That is, when the fuel cell system is started up, hydrogen and oxygen coexist in the anode electrode. At this time, the presence of oxygen in the cathode electrode generates a potential to corrode carbon. After the concentration becomes sufficiently high, the supply of air (air) to the cathode electrode is started.
Then, the amount (concentration) of hydrogen gas in the anode electrode is estimated from the supply time of hydrogen to the anode electrode, and when the supply time reaches a predetermined value, the amount (concentration) of hydrogen gas becomes a predetermined value or more. The air supply to the cathode electrode is started.

JP 2006-0119153 A

  However, variations occur in the correlation between the actual hydrogen gas amount (concentration) in the anode and the supply time. For this reason, when the amount (concentration) of hydrogen gas is estimated based on the supply time of hydrogen, even if the amount (concentration) of hydrogen gas varies to the side where the amount of hydrogen gas (concentration) is small, In order not to start supplying oxygen-containing gas (air, pure oxygen, etc.) to the cathode, it is necessary to add sufficient time to start supply of oxygen-containing gas, and in turn start fuel cell power generation. Had the problem of being overly delayed.

  Therefore, an object of the present invention is to provide a control method for a fuel cell system that can prevent the start of the supply of oxygen-containing gas to the fuel cell stack from being delayed while avoiding the occurrence of corrosion in the fuel cell stack.

Therefore, a control method for a fuel cell system according to claim 1 is a fuel cell stack and a fuel process for reforming a hydrocarbon fuel to generate a hydrogen-containing reformed gas and supplying the reformed gas to the fuel cell stack. A combustion section for introducing an off-gas discharged from the fuel cell stack as fuel and heating a catalyst provided in the fuel processing section, an oxygen-containing gas supply section for supplying an oxygen-containing gas to the fuel cell stack, a method of controlling a fuel cell system wherein the switch to the off-gas fuel to be supplied to the combustion unit from the reformed gas, when the switching from the reformed gas of the fuel supplied to the combustion section to the off-gas, the combustion to perform the ignition operation by the ignition device provided in the section, the minimum value of the temperature of the combustion portion in a periodically time to then when starting the supply of the off-gas to the combustion section Because the temperature of the combustion section after switching the fuel supplied to the combustion section performs determination of ignition success off upon reaching a temperature higher than a threshold than the minimum value, the fuel supplied to the combustion portion of when it is determined ignition success Oite off after switching, the hydrogen concentration in the anode of the cell stack of the oxygen-containing gas by the oxygen-containing gas supply unit as becomes higher enough to start the supply of oxygen-containing gas The supply was started .

Since the off gas supplied as fuel to the combustion section is supplied to the combustion section after passing through the anode (fuel electrode) of the fuel cell stack, if the off gas ignition is successful in the combustion section, the fuel cell stack already has It shows that a sufficient amount of reformed gas (hydrogen) is supplied to the anode, and the hydrogen concentration in the anode is above a certain level.
Therefore, if the supply of the oxygen-containing gas to the fuel cell stack is started after the off-gas is successfully ignited in the combustion section, the supply of the oxygen-containing gas is promptly performed when the hydrogen concentration in the anode becomes higher than a certain level. Will be started.

According to a second aspect of the present invention, the step of starting the supply of the oxygen-containing gas determines whether or not a predetermined waiting time has elapsed since determination of successful off-gas ignition, and the predetermined waiting time is After the lapse of time, supply of the oxygen-containing gas by the oxygen-containing gas supply unit can be started.

According to a third aspect of the present invention, the oxygen-containing gas supply unit can supply an oxygen-containing gas as an oxidant to the cathode of the battery stack. According to a fourth aspect of the present invention, the oxygen-containing gas supply unit can supply an oxygen-containing gas as a bleed gas to the anode of the battery stack.

Further, as in claim 5 , the oxygen-containing gas supply unit includes a first oxygen-containing gas supply unit that supplies an oxygen-containing gas as an oxidant to the cathode of the battery stack, and a bleed gas to the anode of the battery stack. And a second oxygen-containing gas supply unit that supplies the oxygen-containing gas.

  According to the above invention, since the supply of oxygen-containing gas to the battery stack by the oxygen-containing gas supply unit can be started after the hydrogen concentration in the anode becomes sufficiently high, deterioration of the fuel cell (separator or membrane electrode) (Such as carbon corrosion), and the fact that the hydrogen concentration in the anode has become sufficiently high is detected based on the off-gas ignition judgment. It is possible to suppress the delay in the start of the supply of the oxygen-containing gas.

1 is a schematic configuration diagram of a fuel cell system in an embodiment. It is sectional drawing which shows the fuel processing system (FPS) in embodiment. It is a flowchart which shows the starting process of the fuel cell system in embodiment. 4 is a time chart showing burner fuel switching processing and bleed air / cathode air supply start timing at start-up in the embodiment.

Embodiments of the present invention will be described below.
FIG. 1 is a block diagram showing a configuration of a fuel cell system according to an embodiment.
The fuel cell system in this embodiment performs power generation using a hydrocarbon fuel such as kerosene as a raw fuel.

As shown in FIG. 1, a fuel cell system 1 includes a desulfurizer 2, a fuel processing system (hereinafter referred to as “FPS”) 3 as a fuel processing unit, and a polymer electrolyte fuel cell (hereinafter referred to as “PEFC”) stack. 4, an inverter 5, and a housing 6 for housing them.
The desulfurizer 2 removes sulfur from a hydrocarbon fuel supplied from the outside. The desulfurizer 2 includes a desulfurization catalyst and a heater. The heater heats the desulfurization catalyst to, for example, 150 ° C. to 300 ° C., and the desulfurization catalyst performs a desulfurization process of the hydrocarbon fuel. In addition, you may provide as a desulfurization catalyst what is used on temperature conditions about room temperature.

The FPS 3 reforms a hydrocarbon fuel to generate a hydrogen-containing reformed gas. The reformer (reformer) 7, the burner combustor (combustor) 8, and the transformer (transformer) 9 And a selective oxidizer (selective oxidizer) 11.
The reformer 7 generates a steam reformed gas containing hydrogen by subjecting the hydrocarbon-based fuel and steam after the desulfurization process to a steam reforming reaction using a reforming catalyst.
The burner combustor 8 heats the reforming catalyst of the reformer 7 with the heat generated by the combustion of the fuel, and supplies the amount of heat necessary for the steam reforming reaction.

The shift converter 9 performs an aqueous shift reaction of the steam reformed gas generated by the reformer 7 using a shift catalyst to generate a shift reformed gas in which the concentration of carbon monoxide CO is reduced.
Further, the selective oxidizer 11 causes the selective reforming reaction of the shift reformed gas generated by the converter 9 with a selective oxidation catalyst by supplying selective oxidization air to further reduce the concentration of carbon monoxide CO. A reformed gas used for power generation reaction is generated.
The PEFC stack 4 is formed by connecting a plurality of battery cells (single cells) in series, and generates power using the reformed gas generated by the FPS 3.

Each battery cell constituting the PEFC stack 4 includes an anode (fuel electrode) 4a, a cathode (air electrode) 4b, and an electrolyte (not shown) that is a solid polymer disposed between the anode 4a and the cathode 4b. The reforming gas (hydrogen) is supplied to the anode 4a and air (air) is supplied to the cathode 4b, so that the power generation reaction is performed.
The inverter 5 converts the DC current output from the PEFC stack 4 into an AC current.
The casing 6 accommodates the above-described desulfurizer 2, FPS 3, PEFC stack 4 and inverter 5 in a modular manner.

The fuel cell system 1 also includes a fuel line L1 for supplying hydrocarbon fuel (gas fuel such as LPG or city gas or liquid fuel such as kerosene) to the FPS 3 from the outside of the housing 6. . In the present embodiment, kerosene is used as the hydrocarbon fuel.
On the downstream side of the desulfurizer 2, the fuel line L 1 branches into a fuel line L 11 that supplies hydrocarbon fuel to the reformer 7 and a fuel line L 12 that supplies hydrocarbon fuel to the burner combustor 8.
The fuel line L11 and the fuel line L12 are provided with electromagnetic valves 12 and 13 for switching the supply of hydrocarbon fuel to the reformer 7 and the burner combustor 8.
In addition, it is also possible to connect the fuel line L12 directly to the burner combustor 8 without going through the desulfurizer, and to supply the hydrocarbon fuel that has not been desulfurized to the burner combustor 8.

Furthermore, a water line L2 for supplying water (raw water) used for steam reforming to the reformer 7 is connected to the fuel line L11 in the vicinity of the reformer 7.
An upstream side of the water line L2 is connected to a water tank 15, and the water line L2 is provided with an electromagnetic valve 14 for controlling supply / stop of water to the reformer 7.
The water tank 15 is connected with a water line L21 for supplying water from the outside of the housing 6 to the water tank 15 and a recovery water line L22 for recovering process water generated by the reaction in the PEFC stack 4. .

Further, the water tank 15 is connected with a recovered water line L23 for recovering water contained in the combustion gas (exhaust gas) discharged from the burner combustor 8.
Recovery of water from the combustion gas via the recovery water line L23 is performed when the reformed gas or off-gas is burned in the burner combustor 8.
This is because the combustion gas when the reformed gas or off-gas is combusted has less oil components and collects less impurities than the combustion gas when the hydrocarbon-based fuel is combusted in the burner combustor 8. This is because it can.

In addition, a burner air supply line L31 for supplying air (combustion air) from an air supply blower 41 provided outside the housing 6 to the burner combustor 8 is provided.
The PEFC stack 4 is connected to the selective oxidizer 11 of the FPS 3 via the reformed gas supply line L4. The PEFC stack 4 passes the reformed gas that has passed through the selective oxidizer 11 to the reformed gas supply line L4. Through.
The PEFC stack 4 is connected to an offgas supply line L5 for discharging offgas containing hydrogen that has not contributed to the power generation reaction from the anode 4a. A burner combustor is connected to the downstream side of the offgas supply line L5. 8 is connected.

Further, a bypass line L14 is provided which branches from the middle of the reformed gas supply line L4 and is connected to the middle of the off gas supply line L5.
Then, an electromagnetic valve (bypass valve) 26 provided in the bypass line L14 and an electromagnetic valve (reformed gas supply valve) 27 provided in the reformed gas supply line L4 downstream from the branching portion of the bypass line L14 are controlled. By doing so, the reformed gas generated by the FPS 3 can be switched between a state in which it is supplied to the burner combustor 8 and a state in which the reformed gas is supplied to the PEFC stack 4 (a state in which off-gas is supplied to the burner combustor 8). It has become.

That is, when the electromagnetic valve 27 is closed and the electromagnetic valve 26 is opened, the reformed gas that has passed through the selective oxidizer 11 bypasses the PEFC stack 4 and is supplied to the burner combustor 8. On the other hand, when the electromagnetic valve 27 is opened and the electromagnetic valve 26 is closed, the reformed gas that has passed through the selective oxidizer 11 is supplied to the PEFC stack 4, and off-gas discharged from the PEFC stack 4 is supplied to the burner combustor 8 as fuel. Supplied.
Also, cathode air supply for supplying air (oxygen-containing gas) as an oxidant from an air supply blower 42 (first oxygen-containing gas supply unit) provided outside the housing 6 to the cathode 4 b of the PEFC stack 4. Line L32 is provided, and air (oxygen-containing gas) as bleed gas from an air supply blower 44 (second oxygen-containing gas supply unit) provided outside the housing 6 is supplied to the anode 4a of the PEFC stack 4. A bleed air supply line L34 for supply is provided.

The bleed air (bleed gas) is air (oxygen-containing gas) mixed with reformed gas (fuel gas) in order to supply oxygen for removing carbon monoxide CO to the anode 4a. If carbon monoxide CO is contained in the reformed gas, poisoning of the anode 4a occurs, so the selective oxidizer 11 reduces the concentration of carbon monoxide CO in the reformed gas (fuel gas), and The reformed gas is mixed with air to oxidize the carbon monoxide CO in the PEFC stack 4.
In this embodiment, the air supply blower 42 (first oxygen-containing gas supply unit) and the air supply blower 44 (second oxygen-containing gas supply unit) both supply air (air) to the PEFC stack 4. Instead of (air), pure oxygen can be supplied. The air supply blower 42 and the air supply blower 44 may be any device that supplies an oxygen-containing gas such as air or pure oxygen.

Further, a selective oxidation air supply line L33 for supplying air (selective oxidation air) from an air supply blower 43 provided outside the housing 6 to the selective oxidizer 11 is connected to the selective oxidizer 11. is there.
A control device (control unit) 30 incorporating a microprocessor controls the electromagnetic valves 12, 13, 14, 26, 27 and the air supply blowers 41, 42, 43, 44, and an igniter 22 described later. Control the operation of the fuel cell system.

Next, the structure of the FPS 3 will be described in detail. FIG. 2 is a cross-sectional view of the FPS 3. As shown in FIG. 2, the burner combustor (combustion unit) 8 is a burner unit that burns burner fuel (hydrocarbon fuel, reformed gas, offgas) with air. 19 and a combustion cylinder 21 for holding the burner flame.
The burner unit 19 is connected to a fuel line L12, a burner air line L31, a line where an off-gas supply line L5 and a bypass line L14 merge, and an igniter which is an ignition device capable of performing an ignition operation continuously. The burner fuel is ignited and burned by spark ignition of the igniter 22.

When using liquid hydrocarbon fuel such as kerosene, a carburetor (not shown) is disposed inside the fuel line L12 or the burner combustor 8, and liquid hydrocarbon fuel such as kerosene is vaporized by the vaporizer. Then, the fuel is supplied to the combustion cylinder 21.
The combustion cylinder 21 defines a burner combustion space S and is held by the combustion cylinder 21. The combustion cylinder 21 is provided with a combustion temperature sensor 23 for detecting the temperature TB (temperature of the combustion part) in the combustion cylinder 21.

On the other hand, a cylindrical reformer casing 24 is disposed so as to surround the outside of the combustion cylinder 21, and an annular shape is provided between the outer peripheral surface of the combustion cylinder 21 and the inner peripheral surface of the reformer casing 24. A catalyst housing space SC is formed.
In the catalyst containing space SC, an annular reforming catalyst container 25 having gaps SR1, SR2 is inserted into the inner peripheral surface of the reformer casing 24 and the outer peripheral surface of the combustion cylinder 21, respectively. A gap SRE is provided between the end surface of the reforming catalyst container 25 on the burner combustor 8 side and the end surface of the reformer casing 24 on the burner combustor 8 side.

The reforming catalyst container 25 is filled with, for example, a reforming catalyst 25a mainly composed of nickel or ruthenium, and a raw material gas composed of a hydrocarbon-based fuel and steam after the desulfurization treatment is steamed by the reforming catalyst 25a. A reforming reaction is performed to generate a steam reformed gas containing hydrogen.
The reforming catalyst container 25 introduces the raw material gas from the lower end, and the steam reformed gas generated by the steam reforming reaction with the reforming catalyst 25 a is generated from the outer periphery of the reforming catalyst container 25 at the upper end side. 25, is led out to the annular space SC1 surrounding 25, flows outwardly from the reforming catalyst container 25, and is introduced into a transformer (transformer) 9 disposed below the reforming catalyst container 25.

On the other hand, the combustion gas generated in the combustion cylinder 21 passes through the annular space SR <b> 1 sandwiched between the outer peripheral surface of the combustion cylinder 21 and the inner peripheral surface of the reforming catalyst container 25 toward the end on the burner combustor 8 side. After the movement, the annular space SR2 sandwiched between the inner peripheral surface of the reformer casing 24 and the outer peripheral surface of the reforming catalyst container 25 so as to go around the end surface of the reforming catalyst container 25 on the burner combustor 8 side. After moving in the annular space SR2 away from the burner combustor 8 (downward in FIG. 2), the annular space SR2 is discharged to the outside through the annular space SRE1 surrounding the transformer 9.
Further, a steam generator 16 for evaporating the water in the water tank 15 is provided so as to surround the outside of the annular space SRE1, and the steam generated by the steam generator 16 is desulfurized to be introduced into the reforming catalyst 25a. It is mixed with the hydrocarbon-based fuel after treatment.

The reformed gas that has passed through the transformer (transformer section) 9 is added with selective oxidation air in the middle, and then introduced into the selective oxidizer 11 provided so as to surround the outside of the steam generator 16. Then, after the carbon monoxide concentration is reduced, it is supplied to the subsequent stage (the fuel cell stack 4 or the burner combustor 8).
The water in the water tank 15 is supplied to the steam generator 16 after heat exchange with the reformed gas immediately after being derived from the selective oxidizer 11.

  As described above, the high-temperature combustion gas generated in the combustion cylinder 21 (combustion section) flows along the inner peripheral surface and the outer peripheral surface of the reforming catalyst container 25, so that the reforming in the reforming catalyst container 25 is performed. The catalyst 25a and the raw material gas are heated to a temperature (for example, 400 ° C. to 800 ° C.) necessary for the endothermic reaction in the reforming catalyst 25a. Further, the heat of the combustion gas generated in the combustion cylinder 21 (combustion section) is used for heating the shift catalyst of the shift converter 9 and the selective oxidation catalyst of the selective oxidizer 11 and further used as a heat source in the steam generator 16. . That is, the burner combustor 8 is a combustion section that performs catalyst heating with combustion gas.

  The control device 30 inputs an ON / OFF signal of the start switch 31, a combustion temperature signal TB output from the combustion temperature sensor 23, and the like, while the electromagnetic valves 12, 13, 14, 26, 27 and the air supply blowers 41, 42 are input. , 43, 44, and further, by outputting an operation signal to the igniter 22, supply of fuel and air to the burner combustor 8, supply of hydrocarbon fuel and raw water to the reformer 7, ignition by the igniter 22 Operation, supply of reformed gas and air to the PEFC stack 4 are controlled.

FIG. 3 is a flowchart showing a control processing procedure (startup processing procedure) executed by the control device 30 when the fuel cell system 1 is started up. For example, the control device 30 starts the process shown in the flowchart of FIG. 3 when an ON operation signal of the start switch 31 is input.
First, the solenoid valve 13 and the air supply blower 41 are controlled to supply hydrocarbon fuel and air to the burner combustor 8 (S111), and the igniter 22 ignites and burns the hydrocarbon fuel. Thereby, the combustion exhaust gas of the burner combustor 8 heats the reforming catalyst 25a.

The reformed gas that can be supplied as fuel to the burner combustor 8 is not generated until the reformed gas is generated by the FPS 3, so carbonization such as kerosene that is the raw fuel of the reforming process is used as the burner fuel at the start-up. Using hydrogen-based fuel, heat of reforming is generated.
When the temperature of the reforming catalyst 25a is increased to a temperature necessary for the endothermic reaction due to combustion of the hydrocarbon-based fuel in the burner combustor 8, and the steam generator 16 reaches a temperature at which steam can be generated, the reformed gas is In order to start the production, the solenoid valves 12 and 14 are controlled to supply the hydrocarbon fuel desulfurized by the desulfurizer 2 and the raw water in the water tank 15 to the reformer 7 (S112). ).

By supplying hydrocarbon fuel and raw water to the reformer 7, the FPS 3 generates reformed gas. Immediately after the introduction of the hydrocarbon fuel, the reformed gas derived from the FPS 3 is allowed. When carbon monoxide CO exceeding the capacity is included or a trace amount of hydrocarbon-based fuel that could not be reformed may be included, if such reformed gas is supplied to the PEFC stack 4 The PEFC stack 4 will be deteriorated (poisoned).
Therefore, at the beginning of the fuel processing of the FPS 3, the reformed gas derived from the FPS 3 is not supplied to the PEFC stack 4, but the PEFC stack 4 is bypassed and supplied to the burner combustor 8 as fuel.

Specifically, when the FPS 3 generates reformed gas by supplying hydrocarbon-based fuel and raw material water, first, the electromagnetic valve 13 is used to shift the burner fuel from the hydrocarbon-based fuel to the reformed gas. And the supply of hydrocarbon fuel to the burner combustor 8 is stopped (S113). Subsequently, the electromagnetic valve 27 is closed and the electromagnetic valve 26 is opened, and the reformed gas derived from the FPS 3 is supplied directly to the burner combustor 8 via the bypass line L14 (S114).
Further, the air supply blower 41 is controlled to control the amount of air to be optimal for the combustion of the reformed gas, and the reformed gas is ignited by continuous spark ignition by the igniter 22.

Here, prior to the start of supply of the reformed gas to the burner combustor 8, it is preferable to start the ignition operation by the igniter 22.
The electromagnetic valve 26 is controlled to open to start supplying reformed gas to the burner combustor 8, and then the electromagnetic valve 13 is controlled to stop supplying hydrocarbon fuel to the burner combustor 8. In this case, only the reformed gas can be obtained through a transition from the state in which only the hydrocarbon-based fuel is supplied to the burner combustor 8 to the state in which the hydrocarbon-based fuel and the reformed gas are supplied to the burner combustor 8. Will be shifted to a state in which is supplied to the burner combustor 8.

Here, even after the electromagnetic valve 26 is opened and the supply of the reformed gas to the burner combustor 8 is started, the electromagnetic valve 27 is held in the closed state, so that the reformed gas derived from the FPS 3 is used in the PEFC stack. 4, the PEFC stack 4 is bypassed and supplied to the burner combustor 8. Even if the reformed gas contains carbon monoxide CO or hydrocarbon fuel, the PEFC stack 4 Will not deteriorate.
The reformed gas that bypasses the PEFC stack 4 until the reforming process and the selective oxidation process in the FPS 3 become stable and the carbon monoxide CO and hydrocarbon fuel contained in the reformed gas are within the allowable amount. Is continuously supplied to the burner combustor 8 as fuel. Here, the allowable amount (allowable concentration) of carbon monoxide CO and hydrocarbon-based fuel in the reformed gas is an amount (concentration) that does not cause deterioration even when continuously supplied to the PEFC stack 4.

Switching from the state in which the reformed gas is supplied to the burner combustor 8 as the fuel to the state in which the reformed gas is supplied to the PEFC stack 4 is determined by starting the reforming process in the FPS 3 It is performed based on whether or not the elapsed time from the input has reached a preset reforming treatment stabilization time (S115).
That is, when the elapsed time is less than the reforming treatment stabilization time, it is determined that the reformed gas may contain carbon monoxide CO or hydrocarbon fuel exceeding the allowable amount, and PEFC The state where the reformed gas that bypasses the stack 4 is supplied as fuel to the burner combustor 8 is continued.

On the other hand, the reforming process is stabilized when the elapsed time reaches the reforming process stabilization time, and the content (concentration) of carbon monoxide CO or hydrocarbon fuel in the reformed gas derived from FPS3 is allowed. It is determined that the level is within the level, and supply of the reformed gas to the PEFC stack 4 is started (S116).
Specifically, by closing the electromagnetic valve 26, the supply of the reformed gas to the burner combustor 8 via the bypass line L14 is stopped, and the electromagnetic valve 27 is opened and the reformed gas derived from the FPS 3 is opened. Is supplied to the PEFC stack 4 via the reformed gas supply line L4.

However, when the supply of reformed gas (fuel gas, hydrogen) to the PEFC stack 4 is started, the supply of cathode air and bleed air by the air supply blowers 42 and 44 is not started, but a start determination described later is awaited. The supply of cathode air and bleed air is started.
As described above, since the cathode air is not supplied to the cathode 4b, even if the supply of the reformed gas to the PEFC stack 4 is started, the hydrogen in the reformed gas is hardly consumed and unreacted. The fuel (off gas) is discharged from the PEFC stack 4 and supplied to the burner combustor 8 through the off gas supply line L5.

That is, by switching from the state in which the PEFC stack 4 is bypassed and the reformed gas is supplied to the burner combustor 8 to the state in which the reformed gas is supplied to the PEFC stack 4, the fuel supplied to the burner combustor 8 is The reformed gas is switched to off gas.
At the time of switching the burner fuel, an ignition operation is performed by the igniter 22 provided in the burner combustor 8 to ignite and burn off gas. Here, it is determined whether or not the ignition of the off gas is successful (S117).

Then, after the off-gas is successfully ignited in the burner combustor 8, the air supply blowers 42 and 44 (oxygen-containing gas supply unit) are operated to start the supply of cathode air and bleed air (S118).
To switch the burner fuel from the reformed gas to the off-gas, first, the supply of the reformed gas to the burner combustor 8 is stopped, and the reformed gas supplied to the burner combustor 8 is changed to the fuel cell stack 4 (anode 4a). ) And off-gas discharged as an unreacted component from the anode 4 a is supplied to the burner combustor 8.

For this reason, when switching from the reformed gas to the off-gas, the flame formation stops, so that the off-gas is stably supplied to the burner combustor 8 so that the flame due to the combustion of the off-gas is continuously formed. It is detected as whether or not ignition has succeeded.
The above ignition determination is performed in order to determine the supply start timing of bleed air / cathode air. As will be described later, the supply of bleed air / cathode air is started after determining successful ignition. .

When the fuel cell system is started up, hydrogen and oxygen coexist in the anode 4a. If oxygen is present in the cathode 4b at this time, a potential to corrode carbon is generated. Therefore, supply of the reformed gas (hydrogen) causes the inside of the anode 4a. After the hydrogen concentration becomes sufficiently high, it is preferable to start supplying air to the cathode 4b with a delay. In addition, when bleed air is supplied to the anode 4a simultaneously with the start of supply of the reformed gas to the anode 4a, a state in which hydrogen and oxygen coexist in the anode 4a is promoted.
On the other hand, if the supply of cathode air and bleed air is started after the hydrogen concentration in the anode 4a is high in advance, the bleed air reacts with hydrogen immediately after being introduced into the anode 4a and becomes water. Therefore, the situation where hydrogen and oxygen coexist in the anode 4a can be prevented, and if cathode air is introduced after the hydrogen concentration in the anode 4a becomes high, the generation of a potential that causes corrosion is prevented. be able to.

Therefore, by delaying the start of introduction of the cathode air / anode air with respect to the start of introduction of the reformed gas (hydrogen) to the anode 4a, the cathode air / anode air is introduced after the hydrogen concentration in the anode 4a becomes high. In addition, hydrogen and oxygen coexist in the anode 4a, and the situation where oxygen is present in the cathode 4b is prevented with respect to the anode 4a in which hydrogen and oxygen coexist.
In the present application, from the start of introduction of the reformed gas (hydrogen) to the anode 4a, the fact that the hydrogen concentration in the anode 4a has become sufficiently high is detected based on the successful ignition of the offgas in the burner combustor 8.

That is, the off gas supplied to the burner combustor 8 is the reformed gas that has passed through the anode 4a. In a state where the hydrogen concentration in the off gas maintains a low value or varies greatly, the burner combustor At 8, the flame cannot be formed continuously and the ignition success is not judged.
On the other hand, if the supply of the reformed gas to the anode 4a is continued, the air in the reformed gas supply line L4, the anode 4a, and the off-gas supply line L5 downstream from the electromagnetic valve 27 is discharged, and the burner combustor 8 is discharged. As a result, the hydrogen concentration in the off-gas introduced is maintained at a high level, so that the flame can be continuously formed, and the ignition success is determined.

That is, successful ignition of off gas in the burner combustor 8 indicates that the hydrogen concentration of the off gas is stabilized at a high value, and further, the hydrogen concentration of off gas supplied to the burner combustor 8 is high. A stable value indicates that the hydrogen concentration in the anode 4a has increased.
Therefore, if the supply of cathode air and anode air is started after the off-gas is successfully ignited in the burner combustor 8, the hydrogen concentration in the anode 4a becomes high. After eliminating the coexistence of oxygen, the cathode air and the anode air are supplied, so that it is possible to prevent the occurrence of a potential for corrosion.

Here, when estimating whether or not the hydrogen concentration in the anode 4a has become sufficiently high based on the elapsed time from the start of supply of the reformed gas to the anode 4a, it is ensured that there are various variations. Under the condition that the hydrogen concentration in the anode 4a increases relatively quickly, it is necessary to wait for the elapse of time when the hydrogen concentration becomes high, and the start of supply of cathode air / anode air, that is, the start of power generation is delayed excessively. turn into.
On the other hand, in the determination of the off-gas ignition in the burner combustor 8, since the success of the ignition is determined substantially synchronously with the increase in the hydrogen concentration in the anode 4a, the hydrogen in the anode 4a is relatively early. Under the condition where the concentration is high, the start of supply of cathode air and anode air can be advanced, and the start of supply of cathode air and anode air can be prevented from being delayed excessively.

On the other hand, when the increase in the hydrogen concentration in the anode 4a is slow, the timing for determining the success of off-gas ignition is also delayed, and the increase in the hydrogen concentration is waited for a longer time, so that the hydrogen concentration in the anode 4a is sufficient. The supply of cathode air and anode air is not started in a state where it is not high.
The supply of the cathode air and the anode air may be started at the same time when the off-gas ignition success in the burner combustor 8 is determined, or when a preset waiting time TD has elapsed from the determination of successful ignition. You may start with.

The waiting time TD is preliminarily adapted in accordance with, for example, the timing for determining the success of ignition depending on the method for determining the success of off-gas ignition, and the difference in the hydrogen concentration in the anode 4a when determining the success of ignition. The
The off-gas ignition determination in the burner combustor 8 can be performed based on the temperature (combustion part temperature) TB in the combustion cylinder 21 detected by the temperature sensor 23.

Specifically, when the temperature in the combustion cylinder 21 that has decreased due to the transition from the reformed gas to the off-gas is no longer transiently formed, the temperature rises to a temperature that matches the stable combustion state of the off-gas, that is, When the temperature in the combustion cylinder 21 exceeds the threshold after switching to the off gas, or when the temperature exceeding the threshold is continued for a predetermined time or more, the success of the off gas ignition can be determined.
Moreover, after switching to off gas, when the temperature in the combustion cylinder 21 rises and changes at a speed exceeding the threshold, it is possible to determine the success of off gas ignition.

Further, from the time when the reformed gas is switched to off-gas, the minimum value of the temperature in the combustion cylinder 21 in the period up to that time is obtained at each periodic sampling timing, and the temperature reaches a temperature higher than the threshold value than this minimum value. At that point, a successful off-gas ignition can be determined.
The temperature can be detected at a plurality of locations by a plurality of temperature sensors 23 to determine the success of ignition. Further, based on a state quantity other than the temperature, for example, the pressure in the combustion cylinder 21 or the component concentration of the combustion exhaust gas. Successful ignition can also be determined, and various known ignition determination methods can be employed as appropriate.

Further, if the success of ignition of off gas in the burner combustor 8 cannot be determined even after the maximum determination time has elapsed from the time of switching to off gas, an ignition failure is determined, and an alarm failure is determined when ignition failure is determined. (Warning) may be issued, and the supply of air, hydrocarbon fuel, and raw water to the desulfurizer 2 and FPS 3 may be stopped to reset the fuel cell system.
FIG. 4 is a time chart schematically showing the startup process in the above embodiment. When the system is started at time t1, first, hydrocarbon fuel such as kerosene is supplied to the burner combustor 8 as burner fuel.

When it is determined at time t2 that the temperature of the reforming catalyst has been raised to the target temperature by the combustion heat of the hydrocarbon fuel in the burner combustor 8, the reformer 7 receives the hydrocarbon fuel and Water is supplied to start the reforming process.
However, the reformed gas obtained at the beginning of reforming may contain carbon monoxide CO or hydrocarbon fuel beyond the allowable amount, and is not suitable for supplying to the anode 4a (PEFC stack 4). Then, the bypass line L14 is opened and supplied to the burner combustor 8 as burner fuel.

At time t3 when the stabilization time Tst has elapsed from the start of reforming, the reformed gas is in a stable supply state. In other words, carbon monoxide CO and hydrocarbon fuel contained in the reformed gas are allowed. It is presumed that the level is within the level, the bypass line L14 is closed, and the supply of reformed gas (hydrogen) to the PEFC stack 4 (anode 4a) is started.
By supplying reformed gas (hydrogen) to the PEFC stack 4 (anode 4a), the off-gas discharged from the PEFC stack 4 (anode 4a) is supplied as fuel to the burner combustor 8, and the off-gas is successfully ignited. It is determined based on the temperature rise change in the burner combustor 8 or the like.

When it is determined at time t4 that ignition of off-gas is successful, supply of bleed air to the anode 4a and cathode to the cathode 4b at the same time or when the waiting time TD has elapsed from time t4 (time t5). Start supplying air.
Here, during the delay time from the start of supply of reformed gas (hydrogen) to the PEFC stack 4 (anode 4a) (time t3) to the start of supply of bleed air / cathode air (time t4 or time t5), Since the hydrogen concentration in the anode 4a is sufficiently increased and reacts with hydrogen immediately even if bleed air is supplied, it is possible to prevent hydrogen and oxygen from coexisting in the anode 4a, so that corrosion occurs even if cathode air is supplied. Never become a potential.

  Further, the success of the off-gas ignition in the burner combustor 8 is based on the premise that the hydrogen concentration in the off-gas supplied to the burner combustor 8 is stably high. When the ignition is successful, the hydrogen concentration in the anode 4a is Since it can be estimated that it is sufficiently high, the supply of bleed air and cathode air can be started immediately when the hydrogen concentration in the anode 4a becomes sufficiently high, while preventing the occurrence of corrosion, Power generation can be started as soon as possible.

The preferred embodiment of the present invention has been described in detail above, but the present invention is not limited to the above embodiment.
For example, in the above embodiment, kerosene is exemplified as the hydrocarbon fuel used in the burner combustor 8 (combustion unit), but in addition, biofuel using gasoline, naphtha, light oil, methanol, ethanol, dimethyl ether, and biomass is used. Further, the hydrocarbon fuel is not limited to the liquid fuel, and may be a gaseous fuel such as city gas.

Moreover, in the said embodiment, although it was set as the fuel cell system 1 provided with the PEFC stack 4, the fuel cell system provided with the solid oxide fuel cell (SOFC) stack may be sufficient.
Further, for example, the reformer 7 and the transformer 9 are integrally formed, the reformer 7, the transformer 9 and the selective oxidation unit 11 are integrally formed, or the desulfurizer 2 and the reformer. 7 and the transformer 9 can be integrally formed.

Further, the burner combustor 8 is used for heating a shift catalyst (for example, a mixed oxide of Fe—Cr) provided in the transformer 9, and the reformed gas and PEFC that have passed through the selective oxidizer 11 are supplied to the burner combustor 8. The off gas discharged from the stack 4 (anode 4a) may be supplied as fuel.
Further, in the above embodiment, the air supply blower 42 (first oxygen-containing gas supply unit) for supplying cathode air to the cathode 4b and the air supply blower 44 (second oxygen supply) for supplying bleed air to the anode 4a. Even though the fuel cell system is configured to include the containing gas supply unit, the bleed air is not supplied (the air supply blower 44 and the bleed air supply line L34 (second oxygen-containing gas supply unit) are not provided). Good.

  In a fuel cell system that does not supply bleed air, the cathode air supply is started after determining the success of the off-gas ignition in the burner combustor 8, and at this time, hydrogen and oxygen are mixed in the anode 4a. Since the coexisting state is eliminated and the hydrogen concentration in the anode 4a is high, corrosion does not occur even if cathode air is supplied to the cathode 4b.

  DESCRIPTION OF SYMBOLS 1 ... Fuel cell system 1, 3 ... Fuel processing system (FPS, fuel processing part), 4 ... Solid polymer fuel cell (PEFC) stack, 4a ... Anode, 4b ... Cathode, 7 ... Reformer (reforming part) ), 8 ... Burner combustor (combustion section), 9 ... Transformer (modification section), 11 ... Selective oxidizer (selective oxidation section), 21 ... Combustion cylinder, 22 ... Igniter (ignition device), 23 ... Combustion temperature sensor , 30 ... Control device (control unit), 42, 44 ... Air supply blower (oxygen-containing gas supply unit)

Claims (5)

A fuel cell stack, a fuel processing unit that reforms a hydrocarbon-based fuel to generate a hydrogen-containing reformed gas, supplies the reformed gas to the fuel cell stack, and off-gas discharged from the fuel cell stack as fuel A control method for a fuel cell system, comprising: a combustion unit that is introduced as a catalyst that heats a catalyst provided in the fuel processing unit; and an oxygen-containing gas supply unit that supplies an oxygen-containing gas to the fuel cell stack,
The fuel supplied to the combustion section is switched from reformed gas to off-gas,
When switching from the reformed gas of the fuel supplied to the combustion section to off, the to perform the ignition operation by the ignition device provided in the combustion unit, the periodically from the time of starting the supply of the off-gas to the combustion unit Find the minimum value of the temperature of the combustion part in the period until then,
After switching the fuel to be supplied to the combustion section, when the temperature of the combustion section reaches a temperature higher than a threshold value than the minimum value, a determination of successful ignition of off-gas is performed,
When it is determined ignition success Oite off after switching the fuel supplied to the combustion unit, said oxygen-containing gas as the hydrogen concentration in the anode of the cell stack is increased enough to start the supply of oxygen-containing gas A control method for a fuel cell system, wherein supply of oxygen-containing gas by a supply unit is started . Starting the supply of the oxygen-containing gas,
Determine whether a predetermined waiting time has elapsed since the determination of successful off-gas ignition,
Wherein after a predetermined waiting time has elapsed, the starting the supply of oxygen-containing gas with an oxygen-containing gas supply unit, the control method of the fuel cell system according to claim 1. The control method of a fuel cell system according to claim 1 or 2 , wherein the oxygen-containing gas supply unit supplies an oxygen-containing gas as an oxidant to the cathode of the battery stack. The control method of a fuel cell system according to claim 1 or 2 , wherein the oxygen-containing gas supply unit supplies an oxygen-containing gas as a bleed gas to the anode of the battery stack. The oxygen-containing gas supply unit includes a first oxygen-containing gas supply unit that supplies an oxygen-containing gas as an oxidant to the cathode of the battery stack, and a second oxygen that supplies an oxygen-containing gas as a bleed gas to the anode of the battery stack. The control method of the fuel cell system of Claim 1 or 2 containing a containing gas supply part.