JP5765064B2 - Fuel cell wet state control device - Google Patents

Description

  The present invention relates to an apparatus for controlling the wet state of a fuel cell.

  In order to efficiently generate power in the fuel cell, it is important to maintain the electrolyte membrane in an appropriate wet state. That is, if the wet state of the electrolyte membrane is too high, flooding occurs or a purge operation at the time of stop is required in preparation for starting below zero. Moreover, if the electrolyte membrane is too wet, the voltage of the fuel cell stack drops and the output may be greatly reduced. Therefore, in Patent Document 1, the pressure regulating valve and the cathode compressor are controlled so that the cathode gas pressure and the cathode gas flow rate for maintaining the electrolyte membrane in an appropriate wet state are obtained. In particular, when the control is performed on the wet side in consideration of fuel consumption, the rotational speed is first reduced in order to reduce the cathode compressor field power consumption, and then the pressure control valve is opened to increase the pressure.

JP 2007-115488 A

  A parameter for controlling the wetness is the cooling water temperature. However, in the above-described method, the cooling water temperature is not controlled in order to adjust the wetness. For this reason, the present inventors have found that there is room for improving fuel consumption in wet control during transition.

  The present invention has been made paying attention to such conventional problems, and an object of the present invention is to keep the electrolyte membrane in an appropriate wet state while suppressing deterioration of fuel consumption including control of cooling water. It is an object to provide a wet state control device for a fuel cell that can be maintained.

  The present invention solves the above problems by the following means.

  The wet state control device for a fuel cell of the present invention includes a priority control unit that preferentially controls either the pressure or the flow rate of the cathode gas when adjusting the wet state of the fuel cell. Further, the control by the priority control unit further includes a water temperature control unit that controls the temperature of the cooling water when the wet state of the fuel cell cannot be adjusted. And it has further a complement control part which controls either the pressure or flow volume of cathode gas so that the response delay of the said water temperature control part may be supplemented.

  In general, the temperature of the fuel cell is achieved by controlling the cooling water. If the wetness is controlled by adjusting the temperature of the cooling water, there is an effect that the fuel consumption is excellent as compared with the case where the flow rate and pressure are adjusted. However, adjusting the temperature of the cooling water requires more time for response than adjusting the flow rate and pressure. Therefore, when the humidity control by temperature is given the highest priority, the control response is slow. On the other hand, if the priority order of control based on temperature is the slowest, other parameters can follow the deviation to the target value when the target value of wetness control is not reached due to control based on temperature. Therefore, by determining the priority order as described above, for example, during the dry operation for lowering the wet state, control is performed in the order of pressure → temperature → flow rate. By doing so, the pressure compensates the low responsiveness of the temperature, and the flow rate compensates the amount that cannot be covered by the temperature control with respect to the target value of the wetness. Therefore, when the wet state can be satisfied with the pressure and temperature, the increase in the flow rate of the compressor can be suppressed, and the fuel efficiency is improved as compared with the above-described conventional technology.

  Embodiments of the present invention and advantages of the present invention will be described in detail below with reference to the accompanying drawings.

FIG. 1 is a diagram showing an example of a system to which a wet state control device for a fuel cell according to the present invention is applied. FIG. 2 is a schematic diagram for explaining the reaction of the electrolyte membrane in the fuel cell stack. FIG. 3 is a block diagram showing functions related to the wet state control of the controller. FIG. 4 is a timing chart showing the operation of the wetting control device when the target wetting state decreases. FIG. 5 is a timing chart showing the operation of the wetting control device when the target wetting state increases. FIG. 6 is a block diagram illustrating functions related to the control of the controller in the second embodiment of the wet state control apparatus according to the present invention. FIG. 7 is a block diagram showing functions related to the control of the controller in the third embodiment of the wet state control device according to the present invention. FIG. 8 is a block diagram illustrating functions related to the control of the controller in the fourth embodiment of the wet state control device according to the present invention.

(First embodiment)
FIG. 1 is a diagram showing an example of a system to which a wet state control device for a fuel cell according to the present invention is applied.

  First, referring to FIG. 1, a basic system to which a wet state control device for a fuel cell according to the present invention is applied will be described.

The fuel cell stack 10 is supplied with reaction gas (cathode gas O ₂ , anode gas H ₂ ) while maintaining an appropriate temperature to generate electric power. Therefore, the cathode line 20, the anode line 30, and the cooling water circulation line 40 are connected to the fuel cell stack 10. The generated current of the fuel cell stack 10 is detected by the current sensor 101. The power generation voltage of the fuel cell stack 10 is detected by the voltage sensor 102.

A cathode gas O ₂ supplied to the fuel cell stack 10 flows through the cathode line 20. The cathode line 20 is provided with a compressor 21 and a cathode pressure regulating valve 22.

The compressor 21 is provided in the cathode line 20 upstream of the fuel cell stack 10. The compressor 21 is driven by a motor M. The compressor 21 adjusts the flow rate of the cathode gas O ₂ flowing through the cathode line 20. The flow rate of the cathode gas O ₂ is adjusted by the rotational speed of the compressor 21.

The cathode pressure regulating valve 22 is provided in the cathode line 20 downstream of the fuel cell stack 10. The cathode pressure regulating valve 22 adjusts the pressure of the cathode gas O ₂ flowing through the cathode line 20. The pressure of the cathode gas O ₂ is adjusted by the opening degree of the cathode pressure regulating valve 22.

The flow rate of the cathode gas O ₂ flowing through the cathode line 20 is detected by the cathode flow rate sensor 201. The cathode flow rate sensor 201 is provided downstream of the compressor 21 and upstream of the fuel cell stack 10.

The pressure of the cathode gas O ₂ flowing through the cathode line 20 is detected by the cathode pressure sensor 202. The cathode pressure sensor 202 is provided downstream of the compressor 21 and upstream of the fuel cell stack 10. Further, in FIG. 1, the cathode pressure sensor 202 is located downstream of the cathode flow sensor 201.

The anode gas H ₂ supplied to the fuel cell stack 10 flows through the anode line 30. An anode recirculation line 300 is juxtaposed with the anode line 30. The anode recirculation line 300 branches from the anode line 30 downstream of the fuel cell stack 10 and joins the anode line 30 upstream of the fuel cell stack 10. The anode line 30 is provided with a cylinder 31, an anode pressure regulating valve 32, an ejector 33, an anode pump 34, and a purge valve 35.

The cylinder 31 stores the anode gas H ₂ in a high pressure state. The cylinder 31 is provided on the uppermost stream of the anode line 30.

The anode pressure regulating valve 32 is provided downstream of the cylinder 31. The anode pressure regulating valve 32 adjusts the pressure of the anode gas H ₂ that is newly supplied from the cylinder 31 to the anode line 30. The pressure of the anode gas H ₂ is adjusted by the opening degree of the anode pressure regulating valve 32.

The ejector 33 is provided downstream of the anode pressure regulating valve 32. The ejector 33 is located at a portion where the anode recirculation line 300 joins the anode line 30. In the ejector 33, the anode gas H ₂ flowing through the anode recirculation line 300 is mixed with the anode gas H ₂ newly supplied from the cylinder 31.

The anode pump 34 is located downstream of the ejector 33. The anode pump 34 sends the anode gas H ₂ flowing through the ejector 33 to the fuel cell stack 10.

The purge valve 35 is provided in the anode line 30 downstream of the fuel cell stack 10 and further downstream of the branch portion of the anode recirculation line 300. When the purge valve 35 is opened, the anode gas H ₂ is purged.

The pressure of the anode gas H ₂ flowing through the anode line 30 is detected by an anode pressure sensor 301. The anode pressure sensor 301 is provided downstream of the anode pump 34 and upstream of the fuel cell stack 10.

  The cooling water supplied to the fuel cell stack 10 flows through the cooling water circulation line 40. The cooling water circulation line 40 is provided with a radiator 41, a three-way valve 42, and a water pump 43. In addition, a bypass line 400 is provided in parallel with the cooling water circulation line 40. The bypass line 400 branches from the upstream side of the radiator 41 and joins downstream of the radiator 41. For this reason, the cooling water flowing through the bypass line 400 bypasses the radiator 41.

  The radiator 41 cools the cooling water. The radiator 41 is provided with a cooling fan 410.

  The three-way valve 42 is located at the joining portion of the bypass line 400. The three-way valve 42 adjusts the flow rate of the cooling water flowing through the radiator side line and the flow rate of the cooling water flowing through the bypass line according to the opening degree. Thereby, the temperature of the cooling water is adjusted.

  The water pump 43 is located downstream of the three-way valve 42. The water pump 43 sends the cooling water that has flowed through the three-way valve 42 to the fuel cell stack 10.

  The temperature of the cooling water flowing through the cooling water circulation line 40 is detected by a water temperature sensor 401. The water temperature sensor 401 is provided upstream of the portion where the bypass line 400 branches.

  The controller inputs signals from the current sensor 101, voltage sensor 102, cathode flow rate sensor 201, cathode pressure sensor 202, anode pressure sensor 301, and water temperature sensor 401. The controller outputs a control signal to control the operations of the compressor 21, the cathode pressure regulating valve 22, the anode pressure regulating valve 32, the anode pump 34, the purge valve 35, the three-way valve 42, and the water pump 43.

With such a configuration, the fuel cell stack 10 is supplied with the reaction gas (cathode gas O ₂ , anode gas H ₂ ) while maintaining an appropriate temperature to generate electric power. The electric power generated by the fuel cell stack 10 is supplied to the battery 12 and the load 13 via the DC / DC converter 11.

  FIG. 2 is a schematic diagram for explaining the reaction of the electrolyte membrane in the fuel cell stack.

  Next, the technical idea of the inventors will be described with reference to FIG.

As described above, the fuel cell stack 10 is supplied with the reaction gas (cathode gas O ₂ , anode gas H ₂ ) to generate power. The fuel cell stack 10 is configured by stacking hundreds of membrane electrode assemblies (MEA) in which a cathode electrode catalyst layer and an anode electrode catalyst layer are formed on both surfaces of an electrolyte membrane. FIG. 2A shows one MEA. In this example, the cathode gas is supplied to the MEA (cathode in) and discharged from the diagonal side (cathode out), while the anode gas is supplied (anode in) and discharged from the diagonal side (anode out). Has been.

  In each membrane electrode assembly (MEA), the following reaction proceeds in accordance with the load in the cathode electrode catalyst layer and the anode electrode catalyst layer to generate power.

As shown in FIG. 2 (B), as the reaction gas (cathode gas O ₂ ) flows through the cathode flow path, the reaction of the above equation (1-1) proceeds and water vapor is generated. Then, the relative humidity increases on the downstream side of the cathode channel. As a result, the relative humidity difference between the cathode side and the anode side increases. With this relative humidity difference as the driving force, water is back-diffused and the anode upstream side is humidified. This moisture further evaporates from the MEA to the anode channel, and humidifies the reaction gas (anode gas H ₂ ) flowing through the anode channel. Then, it is transported downstream of the anode and humidifies the MEA downstream of the anode.

  In order to generate electric power efficiently by the above reaction, the electrolyte membrane needs to be in an appropriate wet state.

Therefore, the present inventors paid attention to the flow rate and pressure of the cathode gas O ₂ and the temperature of the fuel cell stack 1.

That is, by increasing the flow rate of the cathode gas O _2, water to be discharged together with the cathode gas O ₂ increases. Therefore, the wet state of the electrolyte membrane can be reduced. On the other hand, Reducing the flow rate of the cathode gas O _2, water to be discharged together with the cathode gas O ₂ is reduced. Therefore, the wet state of the electrolyte membrane can be increased.

The cathode gas O ₂ pressure decreases when the opening of the cathode pressure regulating valve 22 increases. Therefore, by lowering the pressure of the cathode gas O ₂ to increase the opening of the cathode pressure regulating valve 22, the cathode gas O ₂ is likely to be discharged. As a result, the moisture discharged together with the cathode gas O ₂ also increases. Therefore, the wet state of the electrolyte membrane can be reduced. On the other hand, the pressure of the cathode gas O ₂ increases when the opening of the cathode pressure regulating valve 22 decreases. Thus, by raising the pressure of the cathode gas O ₂ to reduce the opening of the cathode pressure regulating valve 22, the cathode gas O ₂ is less likely to be discharged. As a result, the moisture discharged together with the cathode gas O ₂ is also reduced. Therefore, the wet state of the electrolyte membrane can be increased.

As the temperature of the fuel cell stack 1 increases, the amount of water contained in the cathode gas O ₂ increases. As a result, the moisture discharged together with the cathode gas O ₂ also increases. Therefore, the wet state of the electrolyte membrane can be reduced. On the other hand, when the temperature of the fuel cell stack 1 is lowered, the amount of water contained in the cathode gas O ₂ is reduced. As a result, the moisture discharged together with the cathode gas O ₂ is also reduced. Therefore, the wet state of the electrolyte membrane can be increased.

The inventors have obtained such findings. Further, if the rotation speed of the compressor 21 is increased in order to increase the flow rate of the cathode gas O ₂ , power consumption increases and fuel consumption deteriorates. Therefore, it is desirable to keep the rotation speed of the compressor 21 as low as possible. The inventors have completed the present invention based on such an idea. Specific contents will be described below.

  FIG. 3 is a block diagram showing functions related to the wet state control of the controller.

  Each block shown in the block diagram represents each function of the controller as a virtual unit, and each block does not mean physical existence.

  The wet state control device controls the operation of the compressor 21, the cathode pressure regulating valve 22, the anode pressure regulating valve 32, the anode pump 34, the purge valve 35, the three-way valve 42, and the water pump 43 to wet the electrolyte membrane of the fuel cell stack 10. Control the state. Specifically, the wet state control device includes a wet state decrease unit 100 and a wet state increase unit 200.

The wet state decreasing unit 100 is a control unit that is executed when the target drainage amount Q _{H2O — out} increases, that is, when the wet state decreases. The wet state reduction unit 100 includes a target pressure calculation block B101, a target temperature calculation block B102, and a target flow rate calculation block B103.

Target pressure calculation block B101 is a target wastewater Q _{H2 O} _ _out, and the lowest stack temperature T _min, the minimum cathode flow rate Q _min, on the basis, calculates the target pressure P _target.

The target drainage amount Q _{H2O — out} [NL / min] is obtained by the following equation (2). Here, NL indicates a normal liter, that is, a liter in a normal state.

The amount of generated water Q _{H2O — in} [NL / min] inside the fuel cell is obtained by the following equation (3).

The target water balance Q _{net — water} [NL / min] is set so as to realize the target wet state of the electrolyte membrane determined according to the operation state (load state) of the fuel cell.

Target pressure calculation block B101 is thus the target wastewater Q _{H2 O} _ _out determined by the, and the minimum stack temperature T _min, the minimum cathode flow rate Q _min, on the basis, determine the target pressure P _target. Specifically, the target pressure P _target is obtained by the following equations (4-1) and (4-2).

Here, the minimum stack temperature T _min is the stack temperature when the wet state of the fuel cell stack is maximized. As described above, in order to increase the wet state of the electrolyte membrane, the temperature of the fuel cell stack 1 is lowered. Note that if the temperature of the fuel cell stack 1 is too low, power generation failure due to condensed water may occur. On the other hand, when it is too high, the deterioration of the fuel cell stack 1 is accelerated. Therefore, the stack temperature when the wet state of the fuel cell stack is maximized is the lowest stack temperature within a range in which the performance of the fuel cell stack can be ensured by comprehensively considering these. Similarly, the minimum cathode flow rate Q _min is a cathode flow rate when the wet state of the fuel cell stack is maximized. As described above, the cathode flow rate is decreased to increase the wet state of the electrolyte membrane. If the cathode flow rate is too low, power generation failure may occur due to insufficient supply amount. On the other hand, if it is too high, the sound vibration performance may be deteriorated. Therefore, the cathode flow rate when the wet state of the fuel cell stack is minimized is the lowest cathode flow rate within a range in which the performance of the fuel cell stack can be ensured by comprehensively considering these. These are set in advance according to the operating state of the fuel cell through experiments.

P _{sat — min} is a saturated water vapor pressure with respect to the minimum stack temperature T _min , and the above equation (4-2) is obtained based on the Antoine equation.

As described above, the target pressure calculation block B101 obtains the target wastewater Q _{H2 O} _ _out, and the lowest stack temperature T _min, the minimum cathode flow rate Q _min, on the basis of the target pressure P _target. The target pressure calculation block B101 corresponds to the priority control unit in the claims.

Target temperature calculation block B102 obtains the target wastewater Q _{H2 O} _ _out, and the pressure P _sens detected by the cathode pressure sensor 202, and the lowest cathode flow Q _min, on the basis of the target temperature T _target. Specifically, it is obtained by the following equations (5-1) and (5-2). Equation (5-1) is obtained by reverse lookup of Antoine's equation.

P _{sat — target} is a target saturated water vapor pressure. In the present embodiment, the pressure P _sens is detected by the cathode pressure sensor 202. However, the pressure loss of the fuel cell stack may be obtained in advance by experiments and estimated based on the pressure loss.

As described above, the target temperature calculation block B102 obtains the target wastewater Q _{H2 O} _ _out, and the actual pressure P _sens, and minimum cathode flow rate Q _min, on the basis of the target temperature T _target. The target temperature calculation block B102 corresponds to the water temperature control unit in the claims.

The target flow rate calculation block B103 calculates the target cathode flow rate Q _target based on the target drainage amount Q _{H2O — out} , the pressure P _sens detected by the cathode pressure sensor 202, and the water temperature T _sens detected by the water temperature sensor 401. Ask. Specifically, it is obtained by the following equations (6-1) and (6-2).

P _{sat — sens} is a saturated water vapor pressure at the water temperature T _sens detected by the water temperature sensor 401.

As described above, the target flow rate calculation block B103 is a target wastewater Q _{H2 O} _ _out, and the actual pressure P _sens, and the actual water temperature T _sens, on the basis, determine a target cathode flow Q _target. The target flow rate calculation block B103 corresponds to the complementary control unit in the claims.

The wet state increasing unit 200 is a control unit that is executed when the target drainage amount Q _{H2O — out} decreases, that is, when the wet state increases. The wet state increasing unit 200 includes a target flow rate calculation block B203, a target temperature calculation block B202, and a target pressure calculation block B201.

Target flow rate calculation block B203 obtains the target wastewater Q _{H2 O} _ _out, and the maximum stack temperature T _max, and the minimum cathode pressure P _min, based on the target cathode flow Q _target. Specifically, it is obtained by the following equations (7-1) and (7-2).

Here, the maximum stack temperature T _max is a stack temperature when the wet state of the fuel cell stack is minimized. As described above, in order to lower the wet state of the electrolyte membrane, the temperature of the fuel cell stack 1 is increased. Note that if the temperature of the fuel cell stack 1 is too low, power generation failure due to condensed water may occur. On the other hand, when it is too high, the deterioration of the fuel cell stack 1 is accelerated. Therefore, the stack temperature when the wet state of the fuel cell stack is minimized is the highest stack temperature within a range in which the performance of the fuel cell stack can be ensured by comprehensively considering these. Similarly, the minimum cathode pressure P _min is a cathode pressure when the wet state of the fuel cell stack is minimized. As described above, the cathode pressure is decreased to lower the wet state of the electrolyte membrane. If the cathode pressure is too low, performance may deteriorate due to insufficient pressure. On the other hand, if it is too high, it may not be realized with a compressor. Therefore, the cathode pressure when the wet state of the fuel cell stack is minimized is the lowest cathode pressure within a range in which the performance of the fuel cell stack can be ensured by comprehensively considering these. These are set in advance according to the operating state of the fuel cell through experiments.

As described above, the target flow rate calculation block B203 is a target wastewater Q _{H2 O} _ _out, and the maximum stack temperature T _max, and the minimum cathode pressure P _min, on the basis, determine a target cathode flow Q _target. The target flow rate calculation block B203 corresponds to the priority control unit in the claims.

Target temperature calculation block B202 obtains the target wastewater Q _{H2 O} _ _out, and the lowest cathode pressure P _min, and detected flow rate Q _sens cathode flow rate sensor 201, based on the target temperature T _target. Specifically, it is obtained by the following equations (8-1) and (8-2). Equation (8-1) is obtained by reverse lookup of Antoine's equation.

P _{sat — target} is a target saturated water vapor pressure.

As described above, the target temperature calculation block B202 is a target wastewater Q _{H2 O} _ _out, and the lowest cathode pressure P _min, and a flow rate Q _sens detected by the cathode flow rate sensor 201, based on the target temperature T _target Ask. The target temperature calculation block B202 corresponds to the water temperature control unit in the claims.

Target pressure calculation block B201 is a target wastewater Q _{H2 O} _ _out, and the flow rate Q _sens detected by the cathode flow rate sensor 201, a water temperature T _sens detected by the water temperature sensor 401, based on the target cathode pressure P _target Ask. Specifically, the target cathode pressure P _target is obtained by the following equations (9-1) and (9-2).

P _{sat — sens} is a saturated water vapor pressure with respect to the water temperature T _sens detected by the water temperature sensor 401, and the equation (9-2) is obtained based on the Antoine equation.

As described above, the target pressure calculation block B201 obtains the target wastewater Q _{H2 O} _ _out, the actual flow rate Q _sens, and the actual water temperature T _sens, based on the target cathode pressure P _target. The target pressure calculation block B201 corresponds to the complementary control unit in the claims.

  FIG. 4 is a timing chart showing the operation of the wetting control device when the target wetting state decreases.

  When the above control logic is executed, when the target wet state decreases, the wetness control device operates as follows.

  When the target wet state decreases at time t11, the wet state reducing unit 100 of the wet control device starts operating.

The target pressure P _target is set based on the target drainage amount Q _{H2O — out} , the minimum stack temperature T _min, and the minimum cathode flow rate Q _min . The target temperature T _target is set based on the target drainage amount Q _{H2O — out} , the actual pressure P _sens, and the minimum cathode flow rate Q _min . The target cathode flow rate Q _target is set based on the target drainage amount Q _{H2O — out} , the actual pressure P _sens, and the actual water temperature T _sens .

Since the target pressure P _target is set based on the stack temperature (minimum stack temperature T _min ) and the cathode flow rate (minimum cathode flow rate Q _min ) when the wet state is _maximized , it is most likely to fluctuate. Therefore, first, the target pressure P _target is preferentially lowered. Then, the cathode pressure regulating valve 22 is controlled so that this target pressure P _target is realized. Then, the cathode pressure decreases almost without a response delay.

If the adjustment cannot be made by changing the target pressure P _target alone, the target temperature T _target starts to fluctuate at time t12. That is, a limit value (minimum cathode flow rate Q _min ) is used for setting the target temperature T _target . The sensor detection value P _sens of the cathode pressure adjusted as described above is fed back. For this reason, the amount that cannot be adjusted only by the cathode pressure is adjusted by changing the temperature of the cooling water. Note that the temperature of the cooling water hardly changes even if the target value changes, and a response delay is likely to occur. The temperature of the cooling water is detected by the water temperature sensor 401, and this temperature is fed back to determine the cathode flow rate, so that the response delay of the cooling water temperature is complemented by the cathode flow rate.

If the target temperature T _target cannot be adjusted even by changing the target temperature T _target , the target cathode flow rate Q _target starts to fluctuate at time t13. That is, the pressure P _sens detected by the cathode pressure sensor 202 and the water temperature T _sens detected by the water temperature sensor 401 are fed back to determine the cathode flow rate, so that the target pressure P _target and the target temperature T _target are changed. The amount that cannot be adjusted by is supplemented by the cathode flow rate.

  FIG. 5 is a timing chart showing the operation of the wetting control device when the target wetting state increases.

  When the target wet state increases at time t21, the wet state increasing unit 200 of the wet control device starts operating.

The target cathode flow rate Q _target is set based on the target drainage amount Q _{H2O — out} , the maximum stack temperature T _max, and the minimum cathode pressure P _min . Target temperature T _target is the target wastewater Q _{H2 O} _ _out, and the lowest cathode pressure P _min, and the actual flow rate Q _sens, is set based on. The target cathode pressure P _target is set based on the target drainage amount Q _{H2O — out} , the actual flow rate Q _sens, and the actual water temperature T _sens .

Since the target flow rate Q _target is set based on the stack temperature (maximum stack temperature T _max ) and the cathode pressure (minimum cathode pressure P _min ) when the wet state is minimized, it is most likely to fluctuate. Therefore, first, the target flow rate Q _target is preferentially lowered. Then, the compressor 21 is controlled so that the target flow rate Q _target is realized. Then, the cathode flow rate decreases almost without a response delay.

If the adjustment cannot be made by changing the target flow rate Q _target alone, the target temperature T _target starts to fluctuate at time t22. That is, a limit value (minimum cathode pressure P _min ) is used for setting the target temperature T _target . The sensor detection value Q _sens of the cathode flow rate adjusted as described above is fed back. For this reason, the amount that the cathode flow rate alone cannot be adjusted is adjusted by changing the temperature of the cooling water. Note that the temperature of the cooling water hardly changes even if the target value changes, and a response delay is likely to occur. The temperature of the cooling water is detected by the water temperature sensor 401, and this temperature is fed back to determine the cathode pressure, so that the response delay in the temperature of the cooling water is complemented by the cathode pressure.

Even if the target temperature T _target is changed and cannot be adjusted, the target cathode pressure P _target starts to fluctuate at time t23. That is, the flow rate Q _sens detected by the cathode flow rate sensor 201 and the water temperature T _sens detected by the water temperature sensor 401 are fed back to determine the cathode pressure, so that the target flow rate Q _target and the target temperature T _target are changed. The amount that cannot be adjusted by is supplemented by the cathode pressure.

  According to this embodiment, when the target wet state of the fuel cell is changed and the wet state is lowered, the target pressure is first lowered and the cathode pressure regulating valve 22 is opened. Next, the target cooling water temperature is raised and the three-way valve 42 is controlled. Finally, the target flow rate is increased and the rotation speed of the compressor 21 is increased. By doing in this way, the raise of the rotational speed of the compressor 21 will be suppressed as much as possible. As the rotation speed of the compressor increases, the power consumption increases and the fuel consumption deteriorates. However, in this embodiment, since the increase in the rotation speed of the compressor 21 is suppressed as much as possible, the power consumption is suppressed and the fuel consumption is improved. To do.

  Further, according to the present embodiment, when the target wet state of the fuel cell is changed and the wet state is increased, the target flow rate is first decreased to decrease the rotational speed of the compressor 21. Next, the target cooling water temperature is lowered to control the three-way valve 42. Finally, the target pressure is increased and the cathode pressure regulating valve 22 is closed. By doing in this way, the rotational speed of the compressor 21 will fall as early as possible. As described above, as the rotational speed of the compressor increases, power consumption increases and fuel consumption deteriorates. In other words, the lower the rotational speed of the compressor, the lower the power consumption and the better the fuel consumption. In the present embodiment, the rotational speed of the compressor 21 is reduced as early as possible, so that fuel efficiency is improved.

  Furthermore, in this embodiment, the control logic of the target pressure calculation block B101 and the target pressure calculation block B201 is the same. The control logic of the target temperature calculation block B102 and the target temperature calculation block B202 is also the same. Further, the control logic of the target flow rate calculation block B103 and the target flow rate calculation block B203 is the same. By changing only the signals input to these control blocks, the wet state of the fuel cell is lowered and dried, or the wet state of the fuel cell is increased and wetted. Although the control logic is the same as described above, the wet state of the fuel cell can be controlled by changing the control order of pressure, temperature, and flow rate only by changing the input value.

(Second Embodiment)
FIG. 6 is a block diagram illustrating functions related to the control of the controller in the second embodiment of the wet state control apparatus according to the present invention.

  In the following description, parts having the same functions as those described above are denoted by the same reference numerals, and redundant description is omitted as appropriate.

The three-way valve 42 is not controlled depending on the operation mode. Further, there is a possibility that the three-way valve 42 cannot be controlled due to some trouble. In such a case, the target pressure calculation block B101 calculates the target pressure P _target using the water temperature T _sens detected by the water temperature sensor 401 instead of the minimum stack temperature T _min . The target flow rate calculation block B203 calculates the target pressure P _target using the water temperature T _sens detected by the water temperature sensor 401 instead of the maximum stack temperature T _max .

  By adopting the present embodiment, it is possible to cope with an operation mode in which the three-way valve 42 is not controlled or a case where the three-way valve 42 cannot be controlled due to some trouble. Also in this embodiment, when the target wet state of the fuel cell is changed and the wet state is lowered, the target pressure is first lowered and the cathode pressure regulating valve 22 is opened. Next, the target flow rate is increased and the rotation speed of the compressor 21 is increased. As a result, an increase in the rotational speed of the compressor 21 is suppressed as much as possible, power consumption is suppressed, and fuel efficiency is improved. Further, when the target wet state of the fuel cell is changed and the wet state is raised, the target flow rate is first lowered to lower the rotational speed of the compressor 21. Next, the target pressure is increased and the cathode pressure regulating valve 22 is closed. As a result, the rotational speed of the compressor 21 decreases as early as possible, power consumption is suppressed, and fuel efficiency is improved.

(Third embodiment)
FIG. 7 is a block diagram showing functions related to the control of the controller in the third embodiment of the wet state control device according to the present invention.

Depending on the operation mode, the cathode pressure regulating valve 22 is not controlled. Further, the cathode pressure regulating valve 22 may not be controlled due to some trouble. In such a case, the target flow rate calculation block B203, in place of the minimum cathode pressure P _min, to obtain a target cathode flow rate Q _target using the detected pressure P _sens cathode pressure sensor 202. The target temperature calculation block B202, in place of the minimum cathode pressure P _min, obtaining the target temperature T _target using the detected pressure P _sens cathode pressure sensor 202.

  By adopting the present embodiment, it is possible to cope with an operation mode in which the cathode pressure regulating valve 22 is not controlled or a case where the cathode pressure regulating valve 22 cannot be controlled due to some trouble. Also in this embodiment, when the target wet state of the fuel cell is changed and the wet state is lowered, first, the target cooling water temperature is raised and the three-way valve 42 is controlled. Next, the target flow rate is increased and the rotation speed of the compressor 21 is increased. Since it becomes like this, the raise of the rotational speed of the compressor 21 will be suppressed as much as possible, and a fuel consumption will improve. Further, when the target wet state of the fuel cell is changed and the wet state is raised, the target flow rate is first lowered to lower the rotational speed of the compressor 21. Next, the target cooling water temperature is lowered to control the three-way valve 42. As a result, the rotation speed of the compressor 21 is reduced as early as possible, and the fuel efficiency is improved.

(Fourth embodiment)
FIG. 8 is a block diagram illustrating functions related to the control of the controller in the fourth embodiment of the wet state control device according to the present invention.

The compressor 21 is not controlled depending on the operation mode. Further, there is a possibility that the compressor 21 cannot be controlled due to some trouble. In such a case, the target pressure calculation block B101 obtains the target cathode pressure P _target using the flow rate Q _sens detected by the cathode flow rate sensor 201 instead of the minimum cathode flow rate Q _min . The target temperature calculation block B102 obtains the target temperature T _target using the flow rate Q _sens detected by the cathode flow rate sensor 201 instead of the minimum cathode flow rate Q _min .

  By adopting the present embodiment, it is possible to cope with an operation mode in which the compressor 21 is not controlled or when the compressor 21 cannot be controlled due to some trouble.

  The embodiment of the present invention has been described above. However, the above embodiment only shows a part of application examples of the present invention, and the technical scope of the present invention is limited to the specific configuration of the above embodiment. Absent.

  For example, the wet state of the fuel cell may be the water balance of the fuel cell (for example, defined as “water balance = generated water−discharged water”) or the resistance of the electrolyte membrane of the fuel cell. It may represent a wet state of another fuel cell.

  Further, instead of the temperature of the cooling water, the temperature of the fuel cell itself or the temperature of air may be used.

In still above embodiments, the target pressure calculation block B101, when setting the target pressure P _target, the stack temperature when the maximum wet state (minimum stack temperature T _min) and a cathode flow (minimum cathode flow rate Q _min ) Is used. The target temperature calculation block B 102, when setting the target temperature T _target, using a cathode flow rate when the maximum wet state (minimum cathode flow Q _min). The target flow rate calculation block B 203, when setting the target flow rate Q _target, using the stack temperature (the maximum stack temperature T _max) and the cathode pressure (minimum cathode pressure P _min) at the time of the wet state to the minimum. The target temperature calculation block B 202, when setting the target temperature T _target, using a cathode pressure at the time of the wet state to the lowest (minimum cathode pressure P _min). If the limit values (maximum value, minimum value) are used in this way, the greatest effect is obtained. However, a value smaller than the maximum value and larger than the minimum value may be used. Even if it does in this way, a suitable effect is acquired.

  Furthermore, the above embodiments can be appropriately combined.

DESCRIPTION OF SYMBOLS 10 Fuel cell stack 20 Cathode line 21 Compressor 22 Cathode pressure regulation valve 201 Cathode flow sensor 202 Cathode pressure sensor 30 Anode line 40 Cooling water circulation line 400 Bypass line 41 Radiator 42 Three-way valve 43 Water pump 401 Water temperature sensor 100 Wet state reduction part B101 Target pressure Calculation block (priority control unit)
B102 Target temperature calculation block (water temperature control unit)
B103 Target flow rate calculation block (complementary control unit)
200 Wet state increasing part B201 Target pressure calculation block (complementary control part)
B202 Target temperature calculation block (water temperature control unit)
B203 Target flow rate calculation block (priority control unit)

Claims (11)

A priority control unit that preferentially controls either the pressure or the flow rate of the cathode gas when adjusting the wet state of the fuel cell;
A water temperature control unit for controlling the temperature of the cooling water when the wet state of the fuel cell cannot be adjusted by the control by the priority control unit;
A complementary control unit that controls either the pressure or the flow rate of the cathode gas so as to complement the response delay of the water temperature control unit;
A wet state control device for a fuel cell. The wet state control device for a fuel cell according to claim 1,
When lowering the wet state of the fuel cell and drying it,
The priority control unit preferentially lowers the pressure of the cathode gas,
The water temperature control unit raises the temperature of the cooling water when the wet state of the fuel cell cannot be adjusted by the control by the priority control unit,
The complement control unit controls the flow rate of the cathode gas so as to complement the response delay of the water temperature control unit.
Fuel cell wet state control device. In the fuel cell wet state control device according to claim 1 or 2,
When lowering the wet state of the fuel cell and drying it,
The priority control unit lowers the pressure of the cathode gas based on the flow rate of the cathode gas supplied when the fuel cell is in a higher wet state than the current state and the temperature of the cooling water,
The water temperature control unit raises the temperature of the cooling water based on the actual pressure of the cathode gas and the flow rate of the cathode gas supplied when the wet state is higher than the current state,
The complementary control unit controls the flow rate of the cathode gas based on the pressure of the cathode gas and the actual temperature of the cooling water.
Fuel cell wet state control device. In the fuel cell wet state control device according to claim 3,
The flow rate of the cathode gas to be supplied when the wet state is higher than the present is the lowest flow rate within the range where the performance of the fuel cell can be secured,
The temperature of the cooling water supplied when the wet state is higher than the present is the lowest temperature within the range in which the performance of the fuel cell can be secured.
Fuel cell wet state control device. In the fuel cell wet state control device according to claim 3 or 4,
When the water temperature control unit does not operate and when the wet state of the fuel cell is lowered and dried, the priority control unit replaces the temperature of the cooling water supplied when the wet state is higher than the current state, Use actual cooling water temperature,
Fuel cell wet state control device. In the fuel cell wet state control device according to any one of claims 3 to 5,
When the complementary control unit does not operate and the wet state of the fuel cell is lowered and dried, the priority control unit and the water temperature control unit supply the cathode gas to be supplied when the wet state is higher than the current state. Instead of the flow rate, use the actual flow rate of the cathode gas.
Fuel cell wet state control device. The wet state control device for a fuel cell according to any one of claims 1 to 6,
When increasing the wet state of the fuel cell,
The priority control unit preferentially decreases the flow rate of the cathode gas,
The water temperature control unit lowers the temperature of the cooling water when the wet state of the fuel cell cannot be adjusted by the control by the priority control unit,
The complement control unit controls the pressure of the cathode gas so as to complement the response delay of the water temperature control unit.
Fuel cell wet state control device. The wet state control device for a fuel cell according to any one of claims 1 to 7,
When increasing the wet state of the fuel cell,
The priority control unit lowers the flow rate of the cathode gas based on the cathode gas pressure and the temperature of the cooling water supplied when the fuel cell is in a lower wet state than the present,
The water temperature control unit lowers the temperature of the cooling water based on the actual flow rate of the cathode gas and the pressure of the cathode gas supplied when the fuel cell is in a lower wet state than the present,
The complementary control unit controls the pressure of the cathode gas based on the flow rate of the cathode gas and the actual temperature of the cooling water.
Fuel cell wet state control device. The wet state control device for a fuel cell according to claim 8,
The pressure of the cathode gas to be supplied when the wet state is lower than the present is the lowest pressure within a range in which the performance of the fuel cell can be secured,
The temperature of the cooling water supplied when the wet state is lower than the present is the highest temperature within a range in which the performance of the fuel cell can be secured.
Fuel cell wet state control device. The wet state control device for a fuel cell according to claim 8 or 9,
When the water temperature control unit does not operate and when the wet state of the fuel cell is increased and wetted, the priority control unit replaces the temperature of the cooling water supplied when the wet state is lower than the current state, Use actual cooling water temperature,
Fuel cell wet state control device. The wet state control device for a fuel cell according to any one of claims 8 to 10,
When the complementary control unit does not operate and when the wet state of the fuel cell is increased and wetted, the priority control unit and the water temperature control unit provide the cathode gas to be supplied when the wet state is lower than the current level. Instead of the pressure, the actual pressure of the cathode gas is used.
Fuel cell wet state control device.

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