JP2008103278A - Fuel cell system - Google Patents

Abstract

An object of the present invention is to provide a fuel cell system that is advantageous in dealing with changes in the fuel cell over time.
A fuel cell system includes: a fuel cell; a cumulative operation number determining unit for determining a cumulative operation number of the fuel cell; and a fuel cell based on the cumulative operation number of the fuel cell determined by the cumulative operation number determining unit. And a control unit 500 that performs power generation control. Since the control unit 500 performs power generation control of the fuel cell based on the cumulative number of fuel cell operations, the control unit 500 can cope with changes in the fuel cell over time.
[Selection] Figure 1

Description

  The present invention relates to a fuel cell system equipped with a fuel cell.

In a fuel cell system, the reforming rate decreases due to a decrease in catalyst activity over time as the fuel cell system is operated. Therefore, the reformer set temperature is corrected based on a predetermined correlation between the reformer set temperature and the cumulative operation time of the fuel cell power generator so that the reforming rate in the reformer is substantially constant. A method for operating a fuel cell system is disclosed.
JP 2001-126748 A

  It is possible to cope with a decrease in catalyst activity and the like over time, which decreases with the operation of the fuel cell system described above. However, it is not always sufficient to sufficiently cope with changes in the fuel cell over time.

  The present invention has been made in view of the above-described circumstances, and an object of the present invention is to provide a fuel cell system that is advantageous for coping with changes over time of the fuel cell.

  A fuel cell system according to aspect 1 includes: (a) a fuel cell; (b) cumulative operation number determination means for determining the cumulative operation number of the fuel cell; and (c) fuel cell accumulation determined by the cumulative operation number determination means. And a control unit that performs power generation control of the fuel cell based on the number of operations. The cumulative operation number determination means obtains the cumulative operation number of the fuel cell. The cumulative number of operation times of the fuel cell corresponds to changes with time in the constituent elements of the fuel cell. Since the control unit performs power generation control of the fuel cell based on the cumulative number of operation times of the fuel cell, the control unit can cope with the change with time of the fuel cell.

  A fuel cell system according to aspect 2 includes: (a) a fuel cell; (b) a cumulative operation number determination unit that determines the cumulative operation number of the fuel cell; and (c) a cumulative operation time determination unit that calculates the cumulative operation time of the fuel cell. And (d) control for performing power generation control of the fuel cell based on the cumulative operation number of the fuel cell determined by the cumulative operation number determination unit and the cumulative operation time of the fuel cell determined by the cumulative operation time determination unit It comprises the part. The cumulative operation number determination means obtains the cumulative operation number of the fuel cell. The accumulated operation time determining means obtains the accumulated operation time of the fuel cell. The cumulative number of operation times and the cumulative operation time of the fuel cell correspond to changes with time in the constituent elements of the fuel cell. Since the control unit performs power generation control of the fuel cell based on both the cumulative number of fuel cell operations and the cumulative operation time of the fuel cell, it can cope with changes in the fuel cell over time.

  ADVANTAGE OF THE INVENTION According to this invention, the fuel cell system advantageous to cope with a change with time can be provided.

  The fuel cell may be a type in which sheet-type cells are stacked in the thickness direction or a type in which a plurality of tube-type cells are mounted. The cumulative operation number determination means obtains the cumulative number of fuel cell operations (corresponding to the number of fuel cell activations). According to aspect 1, the control unit performs power generation control of the fuel cell based on the cumulative operation frequency of the fuel cell obtained by the cumulative operation frequency determining means. According to aspect 2, based on both the cumulative operation number of the fuel cell determined by the cumulative operation number determination means and the cumulative operation time of the fuel cell determined by the cumulative operation time determination means, the control unit Performs battery power generation control.

  In the present specification, as the power generation control, the flow rate per unit time of the reforming fuel to be the anode gas supplied to the fuel cell, the flow rate per unit time of the anode gas and the cathode gas, the fuel cell Examples include pressure of anode gas and / or cathode gas supplied to fuel, current control of fuel cell, voltage control of fuel cell, power control of fuel cell, control of supply amount of reforming fuel per unit time, etc. . In this case, the control unit, regarding the flow rate per unit time of the reforming fuel to be the anode gas supplied to the anode electrode of the fuel cell, the supply amount per unit time of the anode gas, the cathode gas, Examples of the control are based on the sum of the reference supply amount and the correction supply amount, or based on the product of the reference supply amount and the correction coefficient.

  Further, the control unit may control the current value generated by the fuel cell based on the sum of the reference current value and the correction current value or the product of the reference current value and the correction coefficient. Examples of the anode gas include hydrogen gas and hydrogen-containing gas. Examples of the cathode gas include oxygen gas, oxygen-containing gas, and air.

  According to the present invention, a reformer that generates reformed gas from the reforming fuel is provided, and the control unit is exemplified to perform power generation control of the fuel cell and control of the reformer. The reformer includes a reforming unit that generates reformed gas from the reforming fuel, a heating unit that heats the reforming unit, and a CO removal unit that oxidizes and reduces carbon monoxide contained in the reformed gas. An example is provided that includes an oxygen supply unit that supplies an oxygen component to the CO removal unit. In this case, the control of the reformer performed by the control unit based on the cumulative number of fuel cell operations and / or the cumulative operation time of the fuel cell determines the supply amount of oxygen component per unit time supplied to the CO removal unit. Control. Specifically, if the cumulative number of operations and / or the cumulative operation time of the fuel cell increase, it is estimated that the catalyst of the CO removal unit has deteriorated, so the oxygen component per unit time supplied to the CO removal unit The form which increases the supply amount of is preferable.

  The control of the reformer performed by the control unit is exemplified by a catalyst regeneration process for regenerating the catalyst carried on the CO removal unit. In this case, the catalyst regeneration treatment time and temperature can be mentioned. Specifically, a mode in which the catalyst regeneration process time is increased and the regeneration temperature is increased as the cumulative number of fuel cells and / or the cumulative operation time increases.

  According to the present invention, the reformer cumulative operation number determining means for determining the cumulative operation frequency of the reformer is provided, and the control unit accumulates the reformer determined by the reformer cumulative operation number determination means. A mode of performing power generation control of the fuel cell and / or control of the reformer based on the number of operations is exemplified.

  According to the present invention, the reformer accumulated operation time determining means for determining the accumulated operation time of the reformer is provided, and the control unit accumulates the reformer determined by the reformer accumulated operation frequency determination means. A mode of performing power generation control of the fuel cell and / or control of the reformer based on the number of operations and the cumulative operation time of the reformer determined by the reformer cumulative operation time determination unit is exemplified.

  In this case, the control of the reformer performed by the control unit based on the cumulative number of operation of the reformer and / or the cumulative operation time of the reformer is the supply of oxygen components per unit time supplied to the CO removal unit. The form which controls quantity is illustrated. Specifically, if the cumulative number of operation times of the reformer and / or the cumulative operation time of the reformer increases, it is estimated that the catalyst of the CO removal unit has deteriorated, and is supplied to the CO removal unit. A form in which the supply amount of the oxygen component per unit time is increased is preferable.

(Overall description of examples)
Embodiment 1 of the present invention will be specifically described below with reference to FIGS. The reformer according to the present embodiment is applied to a fuel cell system. As shown in FIG. 1, a fuel cell 1 includes a membrane electrode assembly in which a solid polymer membrane 10 having proton conductivity is sandwiched between an anode 11 (fuel electrode) and a cathode 12 (oxidant electrode) in the thickness direction. 13 is formed by assembling a plurality. Examples of the material of the solid polymer film 10 include a fluorocarbon resin (for example, perfluorosulfonic acid resin) or a hydrocarbon resin. The fuel cell 1 may be a system in which a plurality of sheet-like membrane electrode assemblies 13 are stacked in the thickness direction, or a system in which a plurality of tube-shaped membrane electrode assemblies 13 are arranged.

  As shown in FIG. 1, the reformer 2 includes a combustion section 30 formed of a combustion burner, a reforming section 34 heated by the combustion section 30, and a cylindrical combustion passage 32 facing the combustion section 30. The combustion passage 33 that communicates with the combustion passage 32, the cylindrical combustion passage 35 that communicates with the combustion passage 33, the cylindrical evaporation portion 36 that evaporates the raw material water, and the cylindrical CO oxidation removal portion 37 (CO removal) Part).

  As shown in FIGS. 1 and 2, the reforming section 34 is disposed between the combustion passage 32 and the combustion passage 33, and has an inner passage 34i, an outer passage 34p, and a turn-up portion 34m. A cylindrical combustion passage 33 is arranged so as to surround the reforming section 34. The combustion passage 35 is a cylindrical passage that is folded back from the combustion passage 33. A cylindrical heat insulating portion 31 is disposed between the cylindrical combustion passages 33 and 35. Further, a cylindrical evaporator 36 is arranged so as to surround the combustion passage 35. The combustion passage 35 is disposed on the inner peripheral side of the evaporator 36. The evaporator 36 is heated by the combustion gas that passes through the combustion passage 35. A CO oxidation removing unit 37 is arranged so as to surround the evaporation unit 36. Therefore, the evaporation unit 36 and the CO oxidation removal unit 37 are mutually heat-exchanged.

  During the steady operation of the reformer 2, the CO oxidation removing unit 37 is higher in temperature than the evaporation unit 36, so the CO oxidation removing unit 37 applies heat to the evaporation unit 36. Note that until the temperature of the CO oxidation removal unit 37 reaches about 100 ° C. during the start-up operation and after all the water in the evaporation unit 36 of the evaporation unit 36 is vaporized during the stop operation, the CO oxidation removal unit is removed from the evaporation unit 36. 37 is heated. On the outer periphery of the CO oxidation removing portion 37, a heat insulating cylindrical heat insulating layer 39 is disposed.

  The reforming unit 34 includes a ceramic carrier that supports a reforming catalyst 34e that promotes a reforming reaction. The active temperature range of the reforming catalyst 34e is generally 500 to 800 ° C., but is not limited thereto. If the temperature of the reforming unit 34 deviates greatly from the activation temperature range, the reforming reaction of the reforming unit 34 may be impaired. The reforming unit 34 performs steam reforming based on the reforming fuel and steam based on the following formula (1) to generate reformed gas containing hydrogen as a main component. The reformed gas contains carbon monoxide. In the reforming part 34, the reaction based on the formula (2) also occurs.

  Further, as shown in FIG. 1, the reformer 2 includes a heat exchange unit 4 disposed below the reforming unit 34, a CO shift unit 5 disposed below the heat exchange unit 4, and a CO shift unit. 5 and a warm-up unit 47 disposed between the heat exchange unit 4. Here, the heat exchange unit 4 is provided downstream of the evaporation unit 36, and the CO shift unit 5 is provided downstream of the heat exchange unit 4.

  The CO shift unit 5 promotes a shift reaction using steam based on the following equation (2), and reduces CO contained in the reformed gas. The CO shift unit 5 includes a ceramic carrier that supports a shift catalyst 5e (for example, a copper-zinc catalyst). The active temperature range of the shift catalyst 5e is generally 200 to 300 ° C., but is not limited thereto. If the temperature of the CO shift unit 5 greatly deviates from the activation temperature range, the shift reaction of the CO shift unit 5 may be impaired, and carbon monoxide may not be sufficiently purified. The concentration of CO contained in the reformed gas purified by the CO shift unit 5 is generally 0.2 to 1% in terms of molar ratio, although it depends on the reforming fuel. It is not something that can be done. The CO shift unit 5 has a passage 5i, a passage 5v, and a turning portion 5m. The outlet 5p of the CO shift unit 5 and the oxidation air pipe 75 are connected by a purification pipe 400 via the second junction area M2.

As shown in FIG. 1, the CO oxidation removal unit 37 is disposed downstream of the CO shift unit 5, and CO contained in the reformed gas that has passed through the CO shift unit 5 is converted into carbon dioxide as the following formula ( Based on 3), the oxidation reaction to be reduced by oxidation is promoted. The CO oxidation removing unit 37 includes a ceramic carrier that supports a selective oxidation catalyst 37e (for example, ruthenium-based). The active temperature range of the selective oxidation catalyst 37e is generally 100 to 200 ° C. However, it is not limited to this. If the temperature of the CO oxidation removing unit 37 is greatly deviated from the activation temperature range, the oxidation reaction in the CO oxidation removing unit 37 may be impaired. The concentration of CO contained in the reformed gas purified by the CO oxidation removing unit 37 is generally 10 ppm or less in terms of molar ratio. However, it is not limited to this.
Formula (1) ... CH ₄ + H ₂ O → 3H ₂ + CO
Formula (2) ... CO + H ₂ O → H ₂ + CO ₂
Formula (3) ... CO + 1 / 2O ₂ → CO ₂

  According to the present embodiment, since the CO shift unit 5 is arranged upstream of the CO oxidation removal unit 37, it is executed in the order of Expression (2) → Expression (3).

  Next, the piping system will be described. As shown in FIG. 1, a fuel pipe 62 connected to the fuel supply source 61 via a valve 25a is provided. The fuel of the fuel supply source 61 may be gaseous fuel, liquid fuel, or pulverized fuel. Specifically, hydrocarbon fuel and alcohol fuel are exemplified. Examples include city gas, LPG, kerosene, methanol, ethanol, dimethyl ether, and biogas. The fuel pipe 62 is connected to the combustion fuel pipe 62 connected to the combustion section 30 of the reforming section 34 via the valve 25a and the pump 27a, and to the inlet 4i of the heat exchange section 4 via the pump 27b, the desulfurizer 62x and the valve 25b. A reforming fuel pipe 62 (reforming fuel supply unit) is provided. An air pipe 72 (oxygen supply unit) connected to the air supply source 71 is provided. The air pipe 72 includes a combustion air pipe 73 connected to the combustion section 30 of the reforming section 34 via the pump 27c, and an oxidation air pipe 75 connected to the inlet 37i of the CO oxidation removal section 37 via the pump 27d and the valve 25d. And have.

  As shown in FIG. 1, a reforming water pipe 82 (reforming water supply unit) that connects the water tank 81 and the inlet 36i of the evaporation unit 36 via a pump 27m and a valve 25m is provided. An anode gas pipe 100 that connects the outlet 37p of the CO oxidation removing unit 37 and the inlet 11i of the anode 11 of the fuel cell 1 via a valve 25e is provided. The outlet 37p of the CO oxidation removing unit 37 is formed on the upper side of the CO oxidation removing unit 37 in the height direction. An off-gas pipe 110 that connects the outlet 11p of the anode 11 of the fuel cell 1 and the combustion unit 30 via a valve 25f is provided. The off-gas pipe 110 causes the combustion part 30 to discharge the anode off-gas after the power generation reaction. A bypass pipe 150 that connects the off-gas pipe 110 and the anode gas pipe 100 via a valve 25h is provided.

  As shown in FIG. 1, a cathode gas pipe 200 communicating with an air supply source 71 and an inlet 12i of the cathode electrode 12 of the fuel cell 1 via a pump 27k and a valve 25k is provided. A combustion exhaust gas pipe 250 for releasing the combustion exhaust gas burned in the reforming unit 34 to the outside is provided. A steam pipe 300 is provided that connects the outlet 36p of the evaporation section 36 and the reforming fuel pipe 62 via the first merge region M1. The upper end portion 300e of the water vapor pipe 300 is connected to the outlet 36p. The lower end portion 300f of the steam pipe 300 is connected to the merge area M1.

  As shown in FIG. 1, the outlet 5 p of the CO shift unit 5 and the inlet 37 i of the CO oxidation removing unit 37 are connected by a purification pipe 400. The reformed gas (containing hydrogen and carbon monoxide) discharged from the outlet 5p of the CO shift unit 5 flows upward in the direction of the arrow W2 through the purification pipe 400, passes through the second merge region M2, and is discharged from the CO oxidation removal unit 37. It is supplied to the inlet 37i. The inlet 37 i is formed on the lower side in the height direction of the CO oxidation removing unit 37.

  Next, a case where the fuel cell system is started will be described. In this case, combustion air is supplied to the combustion unit 30 via the combustion air pipe 73 by the pump 27c. Further, the combustion fuel is supplied to the combustion unit 30 through the combustion fuel pipe 62 by the valve 25a and the pump 27a. As a result, the combustion section 30 is ignited and heated, and as a result, the reforming section 34 is heated so as to be suitable for the reforming reaction. The reformer 34 and the evaporator 36 are also heated to a high temperature.

  Thereafter, the reformed water is supplied from the water tank 81 and the reformed water pipe 82 to the inlet 36i of the high-temperature evaporator 36 through the pump 27m and the valve 25m. The reformed water is steamed in the high temperature evaporation section 36. The generated water vapor reaches the first merge region M1 from the outlet 36p of the evaporation section 36 through the water vapor pipe 300. The first merge region M1 is a region where the steam or condensed water flowing through the steam pipe 300 and the reforming fuel flowing through the reforming fuel pipe 62 merge. On the other hand, the reforming fuel is supplied to the inlet 4i of the heat exchanging section 4 through the reforming fuel pipe 62 and the first junction region M1 by the valve 25a, the pump 27b, and the valve 25b. Accordingly, in the first merge region M1, the reforming fuel in the reforming fuel pipe 62 and the steam in the steam pipe 300 are merged and mixed. The merged mixed fluid is supplied to the inlet 4 i of the heat exchange unit 4. The mixed fluid passes through the first passage 4 a on the low temperature side of the heat exchange unit 4. At this time, heat exchange is performed with the high-temperature reformed gas flowing through the second passage 4c on the high temperature side of the heat exchange unit 4. For this reason, the mixed fluid before the reforming reaction is heated. The mixed fluid flows into the outer passage 34p of the reforming portion 34, flows in the direction of arrow A1, flows into the inner passage 34i through the turn-up portion 34m, and flows in the direction of arrow A2. At this time, the mixed fluid in which the steam (or condensed water) and the reforming fuel are mixed becomes a hydrogen-rich reformed gas by the reforming reaction shown in (1). This reformed gas contains carbon monoxide.

  Further, the high-temperature reformed gas that has undergone the reforming reaction flows from the reforming section 34 into the heat exchanging section 4. That is, the high-temperature reformed gas passes through the second passage 4c on the high temperature side of the heat exchange unit 4 from the reforming unit 34, thereby heating the mixed fluid in the first passage 4a on the low temperature side. Further, the reformed gas flows into the CO shift unit 5 from the inlet 5 i of the CO shift unit 5 through the warm-up unit 47. In the CO shift unit 5, a shift reaction using water vapor is performed as shown in the above formula (2). As a result, the carbon monoxide contained in the reformed gas is reduced and the reformed gas is purified.

Further, the reformed gas in which carbon monoxide is reduced in the CO shift unit 5 flows from the outlet 5p of the CO shift unit 5 through the purification pipe 400 in the direction of the arrow W2, and reaches the second merge region M2. Further, the reformed gas joins the oxidizing air (oxygen component, selective oxidizing air used for the selective reaction in the CO oxidation removing unit 37) in the oxidizing air pipe 75 (oxygen supply unit) in the second merging zone M2. To do. The second merge region M2 is a region where the reformed gas flowing through the purification pipe 400 and the oxidation air flowing through the oxidation air pipe 75 merge. The merged reformed gas flows into the CO oxidation removing unit 37 from the inlet 37i. In the CO oxidation removing unit 37, an oxidation reaction (CO + 1 / 2O ₂ → CO ₂ ) using oxygen is performed as shown in the above formula (3). As a result, carbon monoxide contained in the reformed gas is further reduced. The oxidation reaction is exothermic.

  The reformed gas purified in this way is supplied as an anode gas from the outlet 37p of the CO oxidation removing unit 37 to the inlet 11i of the anode electrode 11 of the fuel cell 1 through the anode gas pipe 100 and the valve 25e. The air functioning as the cathode gas is supplied to the inlet 12i of the cathode electrode 12 of the fuel cell 1 through the cathode gas pipe 200 by the pump 27k and the valve 25k. As a result, a power generation reaction occurs in the fuel cell 1 and electric energy is generated. The off-gas after the power generation reaction of the anode gas may include hydrogen that has not undergone the power generation reaction. For this reason, the off gas is supplied to the combustion unit 30 of the reforming unit 34 through the off gas pipe 110 and burned, and becomes a heat source of the combustion unit 30.

  In addition, at the time of starting the reforming apparatus 2, the stability of the reformed gas composition may not always be sufficient. For this reason, the valve 25e and the valve 25f are closed when the reformer 2 is started. In this state, the reformed gas discharged from the outlet 37p of the CO oxidation removal unit 37 passes through the valve 25h and is sent to the combustion unit 30 via the bypass pipe 150 and the offgas pipe 110, and becomes a heat source for the combustion unit 30. . As time elapses from the start of the reforming device 2, the composition of the reformed gas becomes stable. In this case, the valve 25h is closed and the valves 25e and 25h are opened. For this reason, the reformed gas discharged from the outlet 37p of the CO oxidation removing unit 37 is supplied as an anode gas to the inlet 11i of the anode electrode 11 of the fuel cell 1 through the anode gas pipe 100 and the valve 25e to generate a power generation reaction. used.

  As shown in FIG. 1, a CO shift unit temperature detector 55 that detects a temperature T11 on the upstream side (inlet side of the passage 5i) of the CO shift unit 5 is provided. A temperature detector 39 for detecting the temperature T31 of the CO shift unit 5 is provided. A CO oxidation removal unit temperature detector 38 for detecting the upstream temperature T12 of the CO oxidation removal unit 37 is provided. Further, a reforming part temperature detector 31t for detecting the temperature T1 on the outlet side of the inner part 34 of the reforming part 34 is provided. The temperature T1 controls the temperature of the reforming unit 34, and is used for controlling the combustion of the combustion unit 30. A temperature detector 65 that detects the temperature T2 of the first merge region M1 where the steam and the reforming fuel merge is provided.

  According to the present embodiment, as shown in FIG. 3, the control unit 500 includes an input processing circuit 500a, a CPU 500b, a memory 500c formed of a writable / readable non-volatile memory, a readable memory 500d, And an output processing circuit 500e. An activation switch 504 that activates the fuel cell system is provided. A stop switch 505 for stopping the power generation operation of the fuel cell system is provided. A regeneration switch 506 for starting the regeneration process of the catalyst 37e of the CO oxidation removing unit 377 is provided.

  The signals of the start switch 504, stop switch 505, regeneration switch 506, reforming unit temperature detector 31t, CO oxidation removal unit temperature detector 38, CO shift unit temperature detector 55, and temperature detector 65 are input to the control unit 500. Is done. Further, the control unit 500 controls the valves 25a, 25b, 25d, 25e, 25f, 25h, 25k, 25m and the pumps 27a, 27b, 27c, 27d, 27m, 27k. The pumps 27a, 27b, 27c, 27d, 27m, and 27k function as a conveyance source.

  Now, according to the present embodiment, when the temperature T11 of the CO shift unit 5 is low and lower than the activation temperature range thereof, the CO shift unit 5 is heated to maintain the CO shift unit 5 in the activation temperature range. The control unit 500 works to make it happen. The control unit 500 functions as a temperature adjusting unit that adjusts the temperature of the CO shift unit 5 and maintains the temperature of the CO shift unit 5 in the activation temperature range.

  A signal of the temperature T11 of the CO shift unit 5 detected by the CO shift unit temperature detector 55, a signal of the temperature T12 of the CO oxidation removal unit 37 detected by the CO oxidation removal unit temperature detector 38, and a reforming unit temperature detector A signal of the temperature T1 of the inner part 34 of the reforming unit 34 detected by 31t and a signal of the temperature T2 of the first merge region M1 detected by the temperature detector 65 are input to the control unit 500, respectively. The controller 500 controls the flow rate of air (oxygen-containing gas, oxygen component) supplied from the oxidation air pipe 75 (oxygen supply unit) to the CO oxidation removal unit 37. Thereby, the temperature of the CO shift part 5 arrange | positioned upstream of the CO oxidation removal part 37 is controlled.

  Specifically, when the temperature T11 of the CO shift unit 5 is low and lower than the activation temperature range, the control unit 500 supplies the air (oxygen) supplied from the oxidation air pipe 75 to the CO oxidation removal unit 37. The flow rate of the component, oxygen-containing gas) is controlled to increase. Thereby, the reaction in the CO oxidation removing unit 37 is promoted. Since this reaction is an oxidation reaction and is a reaction accompanied by heat generation, the amount of heat generated in the CO oxidation removal unit 37 increases. Accordingly, the amount of heat transferred from the relatively high temperature CO oxidation removal unit 37 to the relatively low temperature evaporation unit 36 is controlled. This is because the CO oxidation removal unit 37 and the evaporation unit 36 are adjacent to each other so that the CO oxidation removal unit 37 is positioned outside the evaporation unit 36 as shown in FIG.

  During normal operation of the reformer 2, the evaporation unit 36 evaporates the reformed water. Therefore, the evaporator 36 is generally maintained in a temperature range of about 100 ° C. due to the latent heat of evaporation of the reformed water. . And since the high temperature reformed gas which passed through the CO shift part 5 is supplied to the CO oxidation removal part 37 from the inlet 37i, the temperature of the CO oxidation removal part 37 becomes high. For this reason, the CO oxidation removal unit 37 is on the relatively high temperature side, and the evaporation unit 36 is on the relatively low temperature side. Therefore, the amount of heat that the CO oxidation removing unit 37 gives to the evaporation unit 36 increases. As a result, the amount of heat given to the reforming water in the evaporation section 36 increases. Therefore, vaporization is promoted in the evaporation section 36, the liquid phase moisture ratio is relatively decreased, and the gas phase moisture ratio is relatively increased.

  Here, in the heat exchanging section 4, the high-temperature reformed gas flowing through the second passage 4c and the mixed fluid flowing through the first passage 4a exchange heat with each other as described above. When the ratio of gas-phase moisture contained in the mixed fluid is relatively increased, the amount of latent heat of vaporization for vaporizing liquid-phase moisture is reduced, and the low-temperature gas is reduced from the reformed gas on the high temperature side. The amount of heat transferred to the mixed fluid on the side is reduced, and as a result, the temperature of the heat exchange unit 4 is relatively increased. Therefore, the temperature of the reformed gas heading toward the CO shift unit 5 through the second passage 4c of the heat exchange unit 4 relatively increases. Accordingly, the temperature T11 of the CO shift unit 5 is relatively increased.

  On the other hand, when the ratio of the liquid phase moisture contained in the mixed fluid flowing through the first passage 4a is relatively increased, the amount of latent heat of vaporization for vaporizing the liquid phase moisture is large. Thus, in the heat exchange unit 4, the amount of heat transferred from the reformed gas in the second passage 4c on the high temperature side to the mixed fluid in the first passage 4a on the low temperature side increases, and as a result, the temperature of the heat exchange unit 4 increases. Relatively decreases. Therefore, the temperature of the reformed gas toward the CO shift unit 5 through the second passage 4c of the heat exchange unit 4 relatively decreases. Accordingly, the temperature T11 of the CO shift unit 5 relatively decreases.

  Conversely, when the temperature T11 of the CO shift unit 5 is excessively high and exceeds the active temperature range, or even when the temperature is close to the upper limit of the active temperature range, the temperature T11 is controlled to be relatively lowered. Part 500 works. That is, when the temperature T11 of the CO shift unit 5 is excessively high, the control unit 500 controls the pump 27d to reduce the flow rate of the air supplied from the oxidation air pipe 75 to the inlet 37i of the CO oxidation removal unit 37. . For this reason, the oxidation reaction in the CO oxidation removing unit 37 is suppressed, and the heat generation amount is suppressed. Accordingly, the amount of heat given to the evaporation unit 36 by the CO oxidation removing unit 37 is reduced. As a result, the amount of heat given to the reforming water in the evaporation section 36 is reduced. Therefore, in the evaporation part 36, the liquid-phase water ratio increases relatively, and the vapor-phase water ratio decreases relatively. In this case, in the heat exchanging unit 4, the amount of heat transferred from the high temperature side reformed gas flowing through the second passage 4c to the low temperature side mixed fluid flowing through the first passage 4a increases. As a result, the temperature of the heat exchange unit 4 is relatively lowered. Therefore, the temperature of the reformed gas that goes to the CO shift unit 5 via the heat exchange unit 4 is relatively lowered, and the temperature T11 of the CO shift unit 5 is relatively lowered.

  As described above, according to this embodiment, when the temperature T11 of the CO shift unit 5 is low, the flow rate of the air (oxygen-containing gas) supplied from the oxidation air pipe 75 to the CO oxidation removal unit 37 is increased. As a result, the temperature T11 of the CO shift unit 5 rises, and the CO shift unit 5 is well maintained at a temperature suitable for its activation temperature range. When the temperature T11 of the CO shift unit 5 is high, the temperature T11 of the CO shift unit 5 is decreased by decreasing the flow rate of air (oxygen-containing gas) supplied from the oxidation air pipe 75 to the CO oxidation removal unit 37. In addition, the CO shift unit 5 is well maintained at a temperature suitable for the activation temperature range. In controlling the air flow rate, the conveying capacity of the pump 27d and / or the opening of the valve 25d in the oxidation air pipe 75 are controlled.

(The main part of an Example)
Now, according to the present embodiment, the control unit 500 functions as an accumulated operation number determination means for obtaining the accumulated operation number of the fuel cell 1. Further, the control unit 500 functions as a cumulative operation time determination unit that calculates the cumulative operation time of the fuel cell 1. The control unit 500 performs power generation control of the fuel cell 1 based on the cumulative number of operations of the fuel cell 1 obtained by the cumulative operation number determining means. Specifically, the control unit 500 controls the flow rate of the reforming fuel per unit time supplied to the inlet 4 i of the reformer 2, and consequently the flow rate of the anode gas supplied to the anode electrode 11 of the fuel cell 1. To control.

  FIG. 4 conceptually shows the reference supply flow rate Vα1 (relative display) with respect to the supply flow rate (supply amount) of the reforming fuel supplied to the reformer 2 per unit time. The reference supply flow rate Vα1 is related to the power generation output of the fuel cell 1 and is determined according to the power generation output (250 W, 500 W, 750 W, 1 kW) of the power generation operation of the fuel cell 1, and the cumulative operation of the fuel cell 1. It is set regardless of the number of times and the cumulative operation time of the fuel cell 1. In addition, when the power generation output is 250 W, 500 W, 750 W, and 1 kW, values for linear interpolation are used.

  FIG. 5 conceptually shows the cumulative number of activations of the fuel cell 1 (corresponding to the cumulative number of operations, relative display) and the corrected supply flow rate Vβ1 (corrected supply amount, relative display). FIG. 6 schematically shows the relationship between the cumulative operation time (relative display) of the fuel cell 1 and the corrected supply flow rate Vβ2 (corrected supply amount, relative display). The target supply flow rate V of the reforming fuel supplied to the reformer 2 is set based on the sum of the reference supply flow rate Vα1, the corrected supply flow rate Vβ1, and the corrected supply flow rate Vβ2 (V = Vα1 + Vβ1 + Vβ2). As a result, the flow rate of the anode gas in which the reforming fuel is reformed is controlled.

  By the way, FIG. 7 shows an example of a flowchart executed by the control unit 500 in measuring the cumulative number of activations and the cumulative operation time of the fuel cell 1 and further measuring the cumulative number of activations and the cumulative operation time of the reformer 2. . As shown in FIG. 7, the control unit 500 reads the start switch 504 of the fuel cell system that starts the power generation operation of the fuel cell 1 (step S2), and determines whether the start switch 504 is operated to the start side (step S2). S4). The controller 500 waits until the start switch 504 is operated to the start side. If the activation switch 504 is activated on the activation side (YES in step S4), the control unit 500 increments the cumulative number counter NA for the reformer 2 by 1 (step S6), and a predetermined area of the memory 500c. It writes in (accumulation number storage part for reformer 2) (step S8).

  Further, the control unit 500 reads the cumulative operation time accumulation timer for the reformer 2 up to the present time written in the memory 500c (step S10) and accumulates it in the accumulated operation time for the reformer 2. Then, measurement of the accumulated operation time is started (step S12).

  Further, the control unit 500 stands by until a generated current equal to or higher than the threshold value of the fuel cell 1 is read (steps S14 and S16). If the power generation current of the fuel cell 1 is detected to be equal to or greater than the threshold value, the power generation operation has been performed, so the cumulative number counter NB for the fuel cell 1 is increased by 1 (step S18), and a predetermined area (fuel cell) of the memory 500c 1 (accumulated number storage unit for 1) is written (step S20).

  If the generated current of the fuel cell 1 is not detected beyond the threshold value even after the predetermined time has elapsed, the power generation operation of the fuel cell 1 is not executed, so the program is set to proceed to step S34.

  Further, the control unit 500 reads the accumulated timer for the accumulated operation time for the fuel cell 1 written in the memory 500c (step S22) and accumulates the operation time for the accumulated operation time for the fuel cell 2. Thus, the measurement of the cumulative operation time is started (step S24). Further, the control unit 500 reads the operation status of the stop switch 505 of the fuel cell system (step S26). It is determined whether or not the stop switch 505 of the fuel cell system is operated to the stop side (step S28). If the stop switch 505 is not operated to the stop side, it waits until it is operated.

  When the stop switch 505 is operated to the stop side (YES in Step S28), the power generation operation of the fuel cell system is ended, and thus the control unit 500 ends the measurement of the cumulative operation time for the reformer 2 and Then, the measurement of the cumulative operation time for the fuel cell 1 is ended (step S30). Next, the control unit 500 writes the cumulative operation time for the reformer 2 in a predetermined area (the cumulative operation time storage unit for the reformer 2) of the memory 500c, and the cumulative operation time for the fuel cell 1 is written. The data is written in a predetermined area (accumulated operation time storage unit for the fuel cell 1) of the memory 500c (step S32). The controller 500 performs other controls (step S34) and returns to the main routine.

  Steps S <b> 2 to S <b> 8 function as cumulative activation number determination means (cumulative operation number determination means) regarding the reformer 2. Steps S <b> 14 to S <b> 20 function as cumulative activation number determination means (cumulative operation number determination means) related to the fuel cell 1. Steps S <b> 10 to S <b> 32 function as cumulative operation time determination means for the reformer 2. Steps S <b> 12 to S <b> 32 function as cumulative operation time determination means related to the fuel cell 1. Note that the flowchart is not limited to this.

  The cumulative number counters NA and NB described above are not reset unless a predetermined operation is performed. Therefore, it is possible to measure the cumulative number of activations of the reformer 2 and the cumulative number of activations of the fuel cell 1. Similarly, since the cumulative timer described above is not reset unless a predetermined operation is performed, the cumulative operation time of the reformer 2 and the cumulative operation time of the fuel cell 1 can be measured.

  As described above, according to this embodiment, the cumulative number of activations of the reformer 2 and the cumulative number of activations of the fuel cell 1 are measured independently of each other. The cumulative operation time of the reformer 2 and the cumulative operation time of the fuel cell 1 are measured independently of each other.

  According to the present embodiment, when the condition for detecting the generated current of the fuel cell 1 equal to or greater than the threshold is satisfied (steps S14 and S16), the cumulative number of activations of the fuel cell 1 and the cumulative operation time of the fuel cell are counted. The However, even if the reformer 2 is operated, if the generated current of the fuel cell 1 is not detected above the threshold value, both the cumulative number of activations of the reformer 2 and the cumulative operation time of the reformer 2 are measured. The However, the cumulative number of activations of the fuel cell 1 and the cumulative operation time of the fuel cell 1 are not counted. If the generated current of the fuel cell 1 is not detected above the threshold value even after the predetermined time has elapsed, the operation proceeds to a system stop operation.

  Even when the reforming device 2 is operated as described above, if the generated current of the fuel cell 1 is not detected beyond the threshold value, the fuel supply is performed before the power generation operation is performed although the reforming device 2 is operated. There is a case where the supply of reforming fuel is stopped due to circumstances on the source 61 side. Alternatively, there is a case where the fuel cell system is stopped before the reformer 2 is operated but before generating power.

  FIG. 8 shows a flowchart executed during normal power generation operation of the fuel cell 1. As shown in FIG. 8, the control unit 500 reads the state of the power generation operation of the fuel cell 1 (step SB2), and determines whether the fuel cell 1 is in a normal power generation operation (step SB4). If fuel cell 1 is in a normal power generation operation (YES in step SB4), control unit 500 adds Vα1, Vβ1, and Vβ2V to set V (V = Vα1 + Vβ1 + Vβ2) (step SB6). More specifically, the reforming fuel carrying capacity of the pump 27b and / or the opening of the valves 25a and 25b are controlled.

  Further, the control unit 500 outputs the flow rate command signal to the pump 27b, the valves 25a, 25b, etc. (step S8), executes other processing (step SB10), and accordingly, for the combustion supplied to the combustion unit 30 The flow rate per unit time of fuel and the flow rate per unit time of combustion air supplied to the combustion unit 30 are controlled, and the process returns to the main routine. Note that the flowchart is not limited to this.

According to the present embodiment, the value of S / C relating to the reforming water and the reforming fuel is defined, and is set to be S / C = 3.0 to 3.3. Here, the value of S / C means (number of moles of H ₂ O contained in reforming water) / (number of moles of carbon component contained in reforming fuel). The value of S / C corresponds to the amount of H ₂ O supplied to the reforming unit 34 via the evaporation unit 36. Here, when the flow rate of the reforming water supplied to the evaporation unit 36 is insufficient and the value of S / C is not appropriate, there is a possibility that coking in which carbon precipitates may occur in the reforming unit 34 and the like. There is a possibility of impairing the properties, which is not preferable. Accordingly, since the cumulative number of startups of the fuel cell 1 and the cumulative operation time of the fuel cell 1 are taken into consideration, if the flow rate V per unit time of the reforming fuel supplied to the reformer 2 changes, the S / Since the C parameter of the C value changes, the flow rate of the reforming water supplied to the evaporation unit 36 of the reformer 2 is set correspondingly. In addition, in order to control the flow volume of the reforming water supplied to the evaporation part 36, the conveyance capability of the pump 27m and the opening degree of the valve 25m are controlled.

  As described above, according to this embodiment, even when the fuel cell 1 (catalyst, etc.) changes with time, the flow rate V per unit time of the reforming fuel supplied to the reforming device 2. Is set to V = Vα1 + Vβ1 + Vβ2 in consideration of the cumulative number of activations of the fuel cell 1 and the cumulative operation time of the fuel cell 1. For this reason, the power generation performance of the fuel cell system can be obtained satisfactorily. For this reason, it is possible to cope with changes with time of the fuel cell 1 or the reformer 2. Note that, with respect to the flow rate V per unit time of the reforming fuel supplied to the reformer 2, the corrected supply flow rate Vβ2 related to the cumulative operation time may be eliminated and V = Vα1 + Vβ1. V = Vα1 + Vβ2 may be set.

  9 to 11 show a second embodiment. Since the present embodiment has basically the same configuration and operational effects as the first embodiment, FIGS. 1 to 3, 7 and 8 are applied mutatis mutandis. Also in the present embodiment, the control unit 500 functions as cumulative activation number determination means (cumulative operation number determination means) for obtaining the cumulative activation number (cumulative operation number) of the fuel cell 1. Further, the control unit 500 functions as a cumulative operation time determination unit that calculates the cumulative operation time of the fuel cell 1. The control unit 500 performs power generation control of the fuel cell 1 based on the cumulative number of operations of the fuel cell 1 obtained by the cumulative operation number determining means. Specifically, the control unit 500 controls the flow rate of the cathode gas supplied to the cathode electrode of the fuel cell 1 per unit time.

  In FIG. 9, the cumulative operation time is based on the reference supply flow rate Mα1 (relative display) for the supply flow rate (supply amount) per unit time of the cathode gas (generally air) supplied to the cathode electrode of the fuel cell 1. Indicate. The reference supply flow rate Mα1 is related to the power generation output of the fuel cell 1 and is determined according to the power generation output (250 W, 500 W, 750 W, 1 kW) of the power generation operation of the fuel cell 1. It is set regardless of the number of times and the cumulative operation time of the fuel cell 1.

  FIG. 10 conceptually shows the cumulative number of activations of the fuel cell 1 (corresponding to the cumulative number of operations) and the corrected supply flow rate Mβ1 (corrected supply amount, relative display). FIG. 11 conceptually shows the relationship between the cumulative operation time of the fuel cell 1 and the corrected supply flow rate Mβ2 (corrected supply amount, relative display).

  The target supply flow rate M of the cathode gas supplied to the cathode electrode of the fuel cell 1 is set based on the sum of the reference supply flow rate Mα1, the corrected supply flow rate Mβ1, and the corrected supply flow rate Mβ2 (M = Mα1 + Mβ1 + Mβ2). Specifically, the pump 27k and the valve 27k in the cathode gas pipe 200 are controlled according to the supply flow rate M of the cathode gas.

  Thus, when the supply flow rate M of the cathode gas supplied to the cathode electrode of the fuel cell 1 is controlled, the supply flow rate of the anode gas supplied to the anode electrode of the fuel cell 1 is controlled to correspond to this. 500. That is, the flow rate per unit time of the reforming fuel supplied to the reformer 2 and the flow rate of reforming water per unit time supplied to the evaporator 36 are controlled. In some cases, M = Mα1 + Mβ1. Alternatively, M = Mα1 + Mβ2 may be set.

  12 to 13 show a third embodiment. Since the present embodiment has basically the same configuration and operational effects as the first embodiment, FIGS. 1 to 3, 7 and 8 are applied mutatis mutandis. Also in the present embodiment, the control unit 500 functions as cumulative activation number determination means (cumulative operation number determination means) for obtaining the cumulative activation number (cumulative operation number) of the fuel cell 1. Further, the control unit 500 functions as a cumulative operation time determination unit that calculates the cumulative operation time of the fuel cell 1. The control unit 500 performs power generation control of the fuel cell 1 based on the cumulative number of operations of the fuel cell 1 obtained by the cumulative operation number determining means. Specifically, the control unit 500 controls the current value generated by the fuel cell 1.

  FIG. 12 conceptually shows the relationship between the power generation output and the reference current value Iα1 for the current value (ampere) generated by the fuel cell 1. Although the reference current value Iα1 is related to the power generation output of the fuel cell 1, it is set regardless of the cumulative number of activations and the cumulative operation time of the fuel cell 1. FIG. 13 conceptually shows the relationship between the cumulative number of activations of the fuel cell 1 and the correction current value Iβ1 (correction current value, relative display). FIG. 14 conceptually shows the relationship between the cumulative operation time of the fuel cell 1 and the correction current value Iβ2 (correction current value, relative display). According to this embodiment, the target current value I generated by the fuel cell 1 is set based on the sum of the reference current value Iα1, the correction current value Iβ1, and the correction current value Iβ2 (I = Iα1 + Iβ1 + Iβ2).

  Here, if the cumulative number of activations of the fuel cell 1 and the cumulative operation time of the fuel cell 1 increase, the power generation voltage gradually decreases and the generated power tends to decrease. In this regard, according to this embodiment, even when the fuel cell 1 or the reformer 2 changes over time, the cumulative activation of the fuel cell 1 is performed in setting the target current value I generated by the fuel cell 1. In consideration of the number of times and the cumulative operation time of the fuel cell 1, I = Iα1 + Iβ1 + Iβ2 is set and the power generation current of the fuel cell 1 is increased, so that necessary power is secured. For this reason, it is possible to cope with changes over time of the fuel cell 1 or the reformer 2. The corrected current value Iβ2 related to the cumulative operation time of the fuel cell 1 may be abolished and I = Iα1 + Iβ1. Alternatively, I = Iα1 + Iβ2.

  15 to 17 show a fourth embodiment. Since the present embodiment has basically the same configuration and operational effects as the first embodiment, FIGS. 1 to 3, 7 and 8 are applied mutatis mutandis. Also in the present embodiment, the control unit 500 functions as a cumulative activation number determination means for obtaining the cumulative activation number of the fuel cell 1. Further, the control unit 500 functions as a cumulative operation time determination unit that calculates the cumulative operation time of the fuel cell 1. Based on the cumulative number of operations of the fuel cell 1 determined by the cumulative number of operations determination means, the control unit 500 performs power generation control of the fuel cell 1 and the control unit 500 supplies the CO oxidation removal unit 37 to the unit of unit time. Control the flow rate of air. Specifically, the conveyance capacity of the pump 27d and the opening degree of the valve 25d are controlled.

  By the way, in order to reduce the carbon monoxide contained in the anode gas, it is preferable to increase the flow rate of air supplied to the CO oxidation removing unit 37 per unit time. However, at the beginning of the installation of the fuel cell system, the reformer 2 and the catalyst carried on the fuel cell 1 are also sufficiently activated, so there is no need to increase the amount of air. Furthermore, when the flow rate of the air is increased, the average efficiency of the fuel cell system may be reduced. Further, when the flow rate of the air is increased, the oxidation reaction of the reformed gas having a high reaction rate is likely to be locally generated and locally becomes high temperature, which may cause aggregation of the catalyst, that is, sintering. . For this reason, according to the present embodiment, the flow rate of air supplied to the CO oxidation removing unit 37 per unit time is set to be suppressed. When the cumulative number of activations and the cumulative operation time of the reformer 2 and / or the fuel cell 1 increase, the flow rate of air supplied to the CO oxidation removal unit 37 per unit time is increased accordingly. Yes. As a result, the progress of sintering deterioration can be delayed as much as possible. Further explanation will be added.

  FIG. 15 comfortably shows the relationship between the reference flow rate Uα (relative display) and the power generation output with respect to the flow rate of air supplied to the CO oxidation removing unit 37 per unit time. Although the reference flow rate Uα is related to the power generation output of the fuel cell 1, it is set regardless of the cumulative number of activations and the cumulative operation time of the fuel cell 1. FIG. 16 conceptually shows the relationship between the cumulative number of activations of the fuel cell 1 and the corrected flow rate Uβ1 (corrected supply amount, relative display). FIG. 17 conceptually shows the relationship between the cumulative operation time of the fuel cell 1 and the corrected flow rate Uβ2 (corrected supply amount, relative display).

  Regarding the target flow rate U of the air supplied to the CO oxidation removing unit 37 per unit time, the cumulative number of activations of the fuel cell 1 and the cumulative operation time of the fuel cell 1 are considered. That is, the air flow rate U is set based on the sum of the reference flow rate Uα2, the corrected flow rate Uβ2, and the corrected flow rate Uβ3 (U = Uα2 + Uβ2 + Uβ3). In accordance with the target flow rate U of air, the control unit 500 controls the conveyance capacity of the pump 27d and / or the opening of the valve 25d.

  According to the present embodiment, even when the fuel cell 1 and / or the reformer 2 change over time, the target flow rate U of air supplied to the CO oxidation removal unit 37 per unit time is U = Since it is set to Uα2 + Uβ2 + Uβ3, it is possible to cope with a change with time of the fuel cell 1 or the reformer 2. The corrected flow rate Uβ3 may be abolished and set based on U = Uα2 + Uβ2.

  18 to 20 show the fifth embodiment. This embodiment has basically the same configuration and function as the first embodiment. Also in the present embodiment, the control unit 500 functions as cumulative activation number determination means (cumulative operation number determination means) for obtaining the cumulative activation number (cumulative operation number) of the fuel cell 1. Further, the control unit 500 functions as a cumulative operation time determination unit that calculates the cumulative operation time of the fuel cell 1. The control unit 500 performs power generation control of the fuel cell 1 based on the cumulative number of operations of the fuel cell 1 obtained by the cumulative operation number determining means. Specifically, the control unit 500 controls the temperature T1. As described above, the temperature T1 is the temperature on the outlet side of the inner portion 34 of the reforming portion 34. In this case, the conversion rate at which the reforming fuel is converted to hydrogen changes depending on the temperature T1, and the flow rate of the anode gas in which the amount of generated hydrogen is reformed is controlled.

  FIG. 18 conceptually shows the relationship between the power generation output and the reference value T1α1 of the temperature T1 (° C.) for the temperature T1. Although the reference value T1α1 is related to the power generation output of the fuel cell 1, the reference value T1α1 is set regardless of the cumulative number of activations and the cumulative operation time of the fuel cell 1. FIG. 19 conceptually shows the relationship between the cumulative number of activations of the fuel cell 1 and the correction value T1β1 (relative display). FIG. 20 conceptually shows the relationship between the cumulative operation time of the fuel cell 1 and the correction value T1β2 (relative display). According to this embodiment, the temperature T1 is set based on the sum of the reference value T1α1, the correction value T1β1, and the correction value T1β2 (T1 = T1α1 + T1β1 + T1β2). Note that the correction current value T1β2 related to the cumulative operation time of the fuel cell 1 may be abolished and T1 = T1α1 + T1β1. Alternatively, T1 = T1α1 + T1β2.

  21 to 23 show a sixth embodiment. This embodiment has basically the same configuration and function as the first embodiment. Also in the present embodiment, the control unit 500 functions as cumulative activation number determination means (cumulative operation number determination means) for obtaining the cumulative activation number (cumulative operation number) of the fuel cell 1. Further, the control unit 500 functions as a cumulative operation time determination unit that calculates the cumulative operation time of the fuel cell 1. The control unit 500 performs power generation control of the fuel cell 1 based on the cumulative number of operations of the fuel cell 1 obtained by the cumulative operation number determining means. Specifically, the controller 500 controls the temperature T11 (° C.).

  FIG. 21 conceptually shows the relationship between the power generation output and the reference value T11α1 of the temperature T11 for the temperature T11. Although the reference value T11α1 is related to the power generation output of the fuel cell 1, it is set regardless of the cumulative number of activations and the cumulative operation time of the fuel cell 1. FIG. 22 conceptually shows the relationship between the cumulative number of activations of the fuel cell 1 and the correction value T11β1 (relative display). FIG. 23 conceptually shows the relationship between the cumulative operation time of the fuel cell 1 and the correction value T11β2 (relative display). According to this embodiment, the temperature T11 is set based on the sum of the reference value T11α1, the correction value T11β1, and the correction value T11β2 (T11 = T11α1 + T11β1 + T11β2). Note that the correction current value T11β2 related to the cumulative operation time of the fuel cell 1 may be abolished and T11 = T11α1 + T11β1. Alternatively, T11 = T11α1 + T11β2 may be set.

24 to 26 show a seventh embodiment. This embodiment has basically the same configuration and function as the first embodiment. Also in the present embodiment, the control unit 500 functions as cumulative activation number determination means (cumulative operation number determination means) for obtaining the cumulative activation number (cumulative operation number) of the fuel cell 1. Further, the control unit 500 functions as a cumulative operation time determination unit that calculates the cumulative operation time of the fuel cell 1. The control unit 500 performs power generation control of the fuel cell 1 based on the cumulative number of operations of the fuel cell 1 obtained by the cumulative operation number determining means. Specifically, the control unit 500 controls the cathode air utilization rate M of the fuel cell. More specifically, the flow rate per unit time of the cathode gas (air) is controlled by controlling the cathode air utilization rate M (%).
Target flow rate of cathode gas (air) = current value × predetermined value (initial value 8000) ÷ cathode air utilization rate

  FIG. 24 conceptually shows the relationship between the power generation output and the reference value Mα1 of the cathode air utilization rate M for the cathode air utilization rate M of the fuel cell. Although the reference value Mα1 is related to the power generation output of the fuel cell 1, it is set regardless of the cumulative number of activations and the cumulative operation time of the fuel cell 1. FIG. 25 conceptually shows the relationship between the cumulative number of activations of the fuel cell 1 and the correction value Mβ1 (relative display). FIG. 26 conceptually shows the relationship between the cumulative operation time of the fuel cell 1 and the correction value Mβ2 (relative display). According to this embodiment, the cathode air utilization rate M of the fuel cell is set based on the sum of the reference value Mα1, the correction value Mβ1, and the correction value Mβ2 (M = Mα1 + Mβ1 + Mβ2). Note that M = Mα1 + Mβ1 may be used. Alternatively, M = Mα1 + Mβ2 may be set.

  27-29 show Example 8. FIG. This embodiment has basically the same configuration and function as the first embodiment. Also in the present embodiment, the control unit 500 functions as cumulative activation number determination means (cumulative operation number determination means) for obtaining the cumulative activation number (cumulative operation number) of the fuel cell 1. Further, the control unit 500 functions as a cumulative operation time determination unit that calculates the cumulative operation time of the fuel cell 1. The control unit 500 performs power generation control of the fuel cell 1 based on the cumulative number of operations of the fuel cell 1 obtained by the cumulative operation number determining means. Specifically, the control unit 500 controls the maximum input current value K input from the fuel cell to an inverter connected to the output side of the fuel cell. The input current maximum value K is a ratio (%) to a predetermined value.

  FIG. 27 conceptually shows the relationship between the power generation output and the reference value Kα1 of the input current maximum value K with respect to the input current maximum value K (%). Although the reference value Kα1 is related to the power generation output of the fuel cell 1, it is set regardless of the cumulative number of activations and the cumulative operation time of the fuel cell 1. FIG. 28 conceptually shows the relationship between the cumulative number of activations of the fuel cell 1 and the correction value Kβ1 (relative display). FIG. 29 conceptually shows the relationship between the cumulative operation time of the fuel cell 1 and the correction value Kβ2 (relative display). According to this embodiment, the maximum input current value K is set based on the sum of the reference value Kα1, the correction value Kβ1, and the correction value Kβ2 (K = Kα1 + Kβ1 + Kβ2). Note that K = Kα1 + Kβ1 may be used. Alternatively, K = Kα1 + Kβ2 may be set.

(Other)
The present invention is not limited to the above-described embodiments, and can be modified as appropriate without departing from the scope of the invention. The controller 500 is determined based on the sum of the reference supply amount and the correction supply amount, but is not limited thereto, and may be controlled based on the product of the reference supply amount and the correction coefficient. In the above-described embodiment, as shown in FIG. 1, the evaporation unit 36 and the CO oxidation removal unit 37 are integrated with the reforming unit 34, but may be separated from the reforming unit 34 in terms of distance. . The CO shift unit 5 may be separated from the reforming unit 34 in terms of distance.

  The present invention can be used in, for example, fuel cell systems for vehicles, stationary devices, electronic devices, electric devices, and portable devices.

1 is a system diagram of a fuel cell system according to Embodiment 1 having a reformer and a fuel cell. FIG. FIG. 4 is an enlarged view of the vicinity of the reformer according to the first embodiment. It is a block diagram which shows notionally the relationship of a control part. It is a graph which shows reference | standard supply flow volume V (alpha) 1 (relative display) about the supply flow rate per unit time of the fuel for a reforming supplied to a reformer. 6 is a graph conceptually showing the relationship between the cumulative number of fuel cell activations (relative display) and the corrected supply flow rate Vβ1 (relative display). It is a graph which shows notionally the relationship between the accumulation operation time (relative display) of a fuel cell, and correction | amendment supply flow volume V (beta) 2 (relative display). It is a flowchart which shows the process 1 which a control part performs. It is a flowchart which shows the process 2 which a control part performs. It is a graph which shows reference | standard supply flow rate M (alpha) 1 (relative display) about the supply flow rate per unit time of the cathode gas supplied to the cathode electrode of a fuel cell. 6 is a graph conceptually showing the relationship between the cumulative number of fuel cell activations (relative display) and the corrected supply flow rate Mβ1 (relative display). It is a graph which shows notionally the relationship between the accumulation operation time (relative display) of a fuel cell, and correction supply flow rate Mβ2 (relative display). It is a graph which shows notionally the relation between a power generation output and a standard electric current value (relative display) about the electric current value which a fuel cell generates. It is a graph which shows notionally the relationship between the accumulation | activation count (relative display) of a fuel cell, and correction | amendment electric current value I (beta) 1 (relative display). It is a graph which shows notionally the relationship between the accumulation operation time (relative display) of a fuel cell, and correction | amendment electric current value I (beta) 2 (relative display). It is a graph which shows notionally the relation between the standard flow (relative display) and the power generation output about the flow of the air supplied to a CO oxidation removal part per unit time. 6 is a graph conceptually showing the relationship between the cumulative number of fuel cell activations (relative display) and the corrected flow rate Uβ1 (relative display). It is a graph which shows notionally the relationship between the accumulation operation time (relative display) of a fuel cell, and correction | amendment flow volume U (beta) 2 (relative display). It is a graph which shows standard value T1 alpha 1 (relative display) about temperature T1. 6 is a graph conceptually showing the relationship between the cumulative number of fuel cell activations (relative display) and the correction value T1β1 (relative display). It is a graph which shows notionally the relationship between the accumulation operation time (relative display) of fuel cell, and correction value T1β2 (relative display). It is a graph which shows standard value T11 alpha 1 (relative display) about temperature T11. It is a graph which shows notionally the relationship between the accumulation | activation count (relative display) of a fuel cell, and correction value T11 (beta) 1 (relative display). It is a graph which shows notionally the relationship between the cumulative operation time (relative display) of fuel cell, and correction value T11β2 (relative display). It is a graph which shows standard value Malpha1 (relative display) about cathode air utilization. It is a graph which shows notionally the relationship between the cumulative start count (relative display) of a fuel cell, and the correction value Mβ1 (relative display) of the cathode air utilization rate. It is a graph which shows notionally the relationship between the cumulative operation time (relative display) of a fuel cell, and the correction value Mβ2 (relative display) of the cathode air utilization rate. It is a graph which shows the reference value K (alpha) 1 (relative display) about the input current maximum value. It is a graph which shows notionally the relationship between the cumulative start count (relative display) of the fuel cell and the correction value Kβ1 (relative display) of the maximum input current value. It is a graph which shows notionally the relationship between the cumulative operation time (relative display) of a fuel cell, and the correction value Kβ2 (relative display) of the maximum input current value.

Explanation of symbols

  DESCRIPTION OF SYMBOLS 1 is a fuel cell, 2 is a reformer, 30 is a combustion part, 31 is a heat insulation part, 34 is a reforming part, 36 is an evaporation part, 37 is a CO oxidation removal part, 4 is a heat exchange part, 5 is a CO shift part , 62 is a fuel pipe, 72 is an air pipe (oxygen supply unit), 81 is a water tank, 82 is a reforming water pipe (reforming water supply unit), 100 is an anode gas pipe, 200 is a cathode gas pipe, and 300 is water vapor. Piping, 400 is purification piping, 500 is a control unit (cumulative operation number determination means, cumulative operation time determination means), 31t is a reforming unit temperature detector, 38 is a CO oxidation removal unit temperature detector, and 55 is a CO shift unit temperature. A detector 65 is a temperature detector.

Claims (9)

(A) a fuel cell;
(B) Cumulative operation number determination means for obtaining the cumulative operation number of the fuel cell;
(C) A fuel cell system comprising: a control unit that performs power generation control of the fuel cell based on the cumulative operation frequency of the fuel cell determined by the cumulative operation frequency determining means. (A) a fuel cell;
(B) Cumulative operation number determination means for obtaining the cumulative operation number of the fuel cell;
(C) cumulative operating time determining means for determining the cumulative operating time of the fuel cell;
(D) Power generation control of the fuel cell based on the cumulative operation number of the fuel cell determined by the cumulative operation number determination unit and the cumulative operation time of the fuel cell determined by the cumulative operation time determination unit A fuel cell system comprising: a control unit that performs the operation.   3. The fuel cell system according to claim 1, wherein the control unit controls a supply amount per unit time of at least one of the anode gas and the cathode gas. In one of Claims 1-3, the reformer which produces | generates reformed gas from the fuel for reforming is provided,
The control unit performs power generation control of the fuel cell, control of the reformer, and control of a supply amount of reforming fuel per unit time.   5. The reformer according to claim 4, wherein the reforming device oxidizes carbon monoxide contained in the reformed gas, a reformer that generates reformed gas from the reforming fuel, a heating unit that heats the reformer. A fuel cell system comprising: a CO removing unit that reduces the amount of oxygen and an oxygen supply unit that supplies an oxygen component to the CO removing unit.   6. The fuel cell system according to claim 5, wherein the control unit controls a supply amount per unit time sent to the CO removing unit. In Claim 5 or 6, a reformer cumulative operation number determination means for obtaining the cumulative operation number of the reformer is provided,
The control unit performs power generation control of the fuel cell and / or control of the reformer based on the cumulative number of operations of the reformer determined by the reformer cumulative operation frequency determination unit. A fuel cell system. In Claims 5 to 7, reforming device cumulative operation time determining means for obtaining the cumulative operation time of the reforming device is provided,
The controller is configured to determine the total number of reformer operation times determined by the reformer cumulative operation number determination unit, and the total reformer operation time determined by the reformer cumulative operation time determination unit. Based on the above, the fuel cell system performs power generation control of the fuel cell and / or control of the reformer.   9. The supply amount per unit time according to claim 1, wherein the control unit supplies at least one of a reforming fuel, an anode gas, and a cathode gas serving as an anode gas supplied to the fuel cell. Is controlled based on the sum of the reference supply amount and the correction supply amount or the product of the reference supply amount and the correction coefficient.

Images