JP4831947B2 - Fuel cell cogeneration system - Google Patents

Description

  The present invention relates to a cogeneration system including a high temperature operation type fuel cell such as a solid oxide fuel cell (SOFC) or a molten carbonate fuel cell (MCFC).

 Fuel cell systems that use high-temperature operating fuel cells, such as solid oxide fuel cells (SOFC) and molten carbonate fuel cells (MCFC) as power generation systems, reform and use hydrocarbon fuels. Is operated at a high temperature of 600 to 1000 ° C. or more, and MCFC is operated at a temperature of about 500 to 900 ° C. or more.

  In such a high temperature operation type fuel cell, not all of the supplied fuel is used for power generation in the cell, and about 60 to 80% of the fuel is used for power generation even during rated operation, and the remaining 20 to 40%. Is discharged out of the battery as unreacted fuel. Unreacted fuel burns in an off-gas combustion chamber or the like, and a part of the generated heat is used for maintaining the fuel cell system at a high temperature, reforming the supplied fuel, or the like. In the fuel cell, internal heat is generated during power generation, and the fuel cell system is maintained at a high temperature by the heat. The ratio of the amount of heat corresponding to the power generation reaction of the fuel cell to the amount of heat generated by the supplied fuel (the sum of the amount of heat corresponding to the power generated by the fuel cell and the amount of heat corresponding to the heat generated by the fuel cell) Called rate.

  Even when the fuel supply amount is the same, if the fuel utilization rate is different, the balance between the heat generated in the battery and the heat generated by off-gas combustion changes greatly. For example, it is possible to reduce the output of the fuel cell by reducing the fuel utilization rate while keeping the fuel supply amount the same as during rated operation, but in that case the internal heat generation in the cell will decrease and the battery temperature will decrease. However, since the amount of fuel burned off-gas increases, the temperature of the off-gas portion increases. However, the heat of the off-gas combustion part is not necessarily transmitted efficiently in the battery part. In that case, the battery temperature is lowered, and as a result, the heat self-sustaining operation may become difficult.

  Also, as with fuel, oxygen in the oxidant supplied to the fuel cell (including carbon dioxide in the case of MCFC) is not all used for power generation, and generally 20 to 40% is used. Called oxidant utilization.

The fuel cell temperature changes at the same time as the fuel cell temperature changes due to the fuel usage rate and oxidant usage rate, and the balance between the fuel supply amount and the oxidant supply amount. As a result, the exhaust gas temperature also changes. To do.
Therefore, when using exhaust gas through a heat exchanger for hot water supply, steam supply, heating, etc., if the exhaust gas temperature is too high and excessive steam or hot water is generated, or conversely, the exhaust gas temperature is too low, a sufficient amount Steam or heating energy may not be supplied.

Here, referring to FIG. 17, in a high temperature operation type fuel cell such as a solid oxide fuel cell (SOFC) or a molten carbonate fuel cell (MCFC), as an operation example when the supplied fuel is 100,
(1) Power generation output, (2) Available waste heat energy, and (3) Heat during power main heat operation (when you want to obtain power generation output as much as possible even if there is little waste heat available) (1) Power generation output in the ratio of energy required for self-sustainment and fuel reforming, and heat main operation (when power generation output is small, but want to increase the supply of hot water and steam as much as possible; Case B), ( 2) Available exhaust heat energy, (3) Ratio of energy required for heat self-supporting and fuel reforming,
Will be described.

  The fuel cell cogeneration system Sc of FIG. 17 includes the fuel cell 1 and the blower B interposed in the air supply line La, and the pure water interposed in the first water supply line Lw1 to produce reforming pure water. The heat of the second water supply line Lw2 for obtaining heat is exchanged with the heat of the exhaust system Hx, and the heat energy or steam is exchanged with the heat of the exhaust system Hx. It is comprised with the heat exchanger Hh which provides. In addition, a thermometer and a flow meter M1 are installed upstream of the system Sc in the first water supply line Lw1, and a gas meter M2 is installed upstream of the system Sc in the fuel gas supply line Lf. Yes. In FIG. 17, the symbol W indicates a power generation output line.

In the fuel cell cogeneration system Sc, assuming that the energy of the supplied fuel is 100, in the case of the electric main heat slave operation (A case) (1) The ratio of the power generation output (rated output power generation) is 40-50,
(2) The ratio of available exhaust heat energy is 20-30.
(3) The ratio of energy required for thermal independence and fuel reforming is 30-40
It is.
On the other hand, in the case of heat main power operation (case B) (1) The ratio of the power generation output (power generation output of 25 to 50% of the rating) is 20 to 30,
(2) The ratio of available waste heat energy is 40,
(3) The ratio of energy required for thermal independence and fuel reforming is 30-40
It is.

  A fuel cell cogeneration system generates electricity and heat. Here, depending on the characteristics of power demand and hot water supply demand of the facility (general household, office, hospital, etc.) where the fuel cell cogeneration system is installed, it should be the main electric heat subordinate operation or the main heat subordinate operation It should be different.

  Here, FIG. 18 is a graph showing the daily power demand (solid line) and heat demand (broken line) in ordinary households converted into electric energy, and FIG. 19 shows the daily power demand in hospitals and elderly welfare facilities. It is the graph which converted and showed electric power demand (solid line) and heat demand (broken line) to electric energy. 18 and 19, the two-dot chain line indicates the output of the fuel cell when the thermoelectric ratio cannot be changed.

In general households, heat demand increases from about 18:00, and there is much heat demand until around 23:00. In particular, since there is a bathing demand after 21:00, there is a demand pattern in which there is more heat demand than electric power demand. During other times, that is, from 11:00 (23:00) at midnight to 6:00 pm (18:00) the following day, especially from 5:00 to 18:00, there is much power demand but less heat demand (hot water supply, etc.) It becomes the demand pattern.
In general households, since the thermoelectric ratio cannot be changed throughout the day, the output of the fuel cell is also constant. From 18:00 to past 21:00, the power generation output of the fuel cell is insufficient with respect to the power demand, so that it depends on external power (purchased power).
Considering such a demand pattern, when a fuel cell is used in a general household, as shown in FIG. 18, from 18:00 to 23:00, the main heat recovery is mainly the heat recovery from the exhaust heat recovery. It is preferable to perform a subordinate operation and to perform a main power subordinate operation in which power generation is the main and exhaust heat recovery is subordinate in other time zones (from 23:00 to 18:00 on the next day).

As shown in FIG. 19, in hospitals and elderly welfare facilities, etc., there is a large amount of power demand during the daytime (between around 8 o'clock and around 18 o'clock) due to the use of medical equipment and nursing care equipment. It's too creepy. Contrary to this, meals have already been completed at night (from 18:00 to around 8:00 the next morning), and because it is intended for sick or elderly people, the turn-off time is fast and power is surplus, but heat (especially in the winter) Etc.)
That is, in hospitals and welfare facilities for the elderly, the main heating operation is performed during the daytime (between about 8 o'clock and around 18 o'clock) and the main heating operation is performed during the night (from 18 o'clock to around 8 o'clock the next morning). It is preferable to do.

  As described above, even in the same facility, whether to perform the electric main heat slave operation or the heat main electric slave operation varies depending on the time zone.

  Therefore, it is preferable that the thermoelectric ratio of the fuel cell cogeneration system (the ratio of the electric output and the heat output of the fuel cell cogeneration system to the same fuel supply amount) can be changed. In this way, if the thermoelectric ratio can be changed, it will lead to energy saving.

  However, when the thermoelectric ratio is changed in a high-temperature operation type fuel cell, there is a possibility that the heat balance is lost and the self-sustained operation cannot be performed.

  In a hybrid system of a high-temperature operating fuel cell such as a solid oxide fuel cell (SOFC) or a molten carbonate fuel cell (MCFC) and a micro gas turbine, the micro gas turbine maintains a constant power output of the fuel cell. The balance between the power generation output and heat output of the hybrid system is controlled by extracting the excess steam from the turbine while adjusting the opening of the flow adjustment valve. And the method of controlling the thermoelectric ratio of the whole system is proposed (for example, refer patent document 1).

  However, in the control method described above, the scale of the system is large because the target system is a hybrid system Sh of the high-temperature operating fuel cell 1 and the micro gas turbine TC as shown in FIG. Therefore, as a cogeneration system for small and medium-sized consumers such as home use and business use, the equipment scale is too large and it is difficult to introduce.

  The hybrid system Sh (FIG. 20) is composed of a high-temperature operating fuel cell 1 such as SOFC or MCFC, a micro gas turbine TC composed of a turbine T and a compressor C, and a generator G driven by the turbine. The turbine T is rotated by the exhaust gas of 1 and the compressor C is driven by the rotational force of the turbine T. The compressor C compresses the intake air, and the compressed air compressed is supplied to the fuel cell 1 through the pressurized air supply line Lac. It is configured to be. Electric power is obtained from the power line W1 of the fuel cell 1 and the power line W2 of the generator G driven by the turbine TC.

Since the optimum of the gas turbine TC and the optimum of the fuel cell 1 do not coincide with each other, the compromise is set as the optimum point of the hybrid system Sh. However, when the conditions change, the operating conditions of the fuel cell 1 change, and as a result, the gas turbine TC The driving conditions will change drastically.
Therefore, cooperative operation control of the high-temperature operating fuel cell 1 and the micro gas turbine TC is difficult, and the thermoelectric ratio also needs to be complicatedly controlled.

  Furthermore, the exhaust heat of the hybrid system Sh (electric main heat slave system) cannot be used, for example, a large amount of steam is used in the manufacturing process of a factory (about 60 ° C. for hot water supply, In some cases, it is difficult to supply heat to consumers who have a large demand for heat, such as steam, which requires a larger amount of thermal energy.

  In a molten carbonate fuel cell (MCFC) capable of controlling the air supply pressure, cooling air is controlled by controlling the number of revolutions of a compressor that supplies fuel cooling air and controlling the air flow rate for battery cooling. Has been proposed (see, for example, Patent Document 2), in which the thermoelectric ratio is changed by changing the outlet temperature and changing the amount of exhaust heat (changing the amount of heat taken by the cooling air).

In addition, since the technology is also a hybrid system of a fuel cell and a micro gas turbine (because use of the technology is limited to a molten carbonate fuel cell system having an air compressor), the above-mentioned (for example, as in Patent Document 1) As described above, there is a problem that cooperative operation control between the fuel cell and the micro gas turbine is difficult.
Furthermore, since the auxiliary power is required for operation control of the turbine (compressor), energy saving performance is impaired.
And since it is a hybrid system of a fuel cell and a micro gas turbine, as in the above (for example, the above-described technique such as Patent Document 1), it is suitable for applications that require a large amount of heat (thermal main power usage). Is unsuitable.
Alternatively, with the change in air flow rate, the thermal self-supporting balance of the fuel cell may be lost, or the battery may be damaged due to oxidant withering at a low flow rate.
JP 2004-111130 A JP 2004-71279 A

  The present invention has been proposed in view of the above-described problems of the prior art, and provides a fuel cell cogeneration system that can change the thermoelectric ratio while maintaining the thermal self-sustaining operation state of the fuel cell and that is not large-scale. It is an object.

  As a result of various studies, the inventors have changed the state of off-gas combustion if the power generation output (for example, current density and / or fuel utilization rate) of the fuel cell cogeneration system is changed, and the flow rate of the exhaust gas of the fuel cell It was also found that the thermoelectric ratio can be controlled by varying various parameters such as temperature.

  According to the present invention, a high temperature operation type fuel cell (1), current density control means (3) for controlling the power generation output of the fuel cell (1), and fuel supply supplied to the fuel cell (1) A fuel adjustment valve (5) for controlling the amount, an oxidant adjustment valve (7) for controlling the amount of oxidant supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1) In the fuel cell cogeneration system, comprising: a heat recovery means (15) for supplying exhaust heat of the fuel cell (1) to the heat demand side, and a fuel cell system temperature measuring instrument (2); The means (3) is connected to the power demand (12) via the output power line (Le), and is disposed between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). An exhaust gas temperature sensor (17) is interposed, and the heat recovery hand The fuel is received in response to input signals from the heat utilization means utilizing the heat recovered in (15), the power demand (12), the current density control means (3), and the fuel cell system temperature measurement means (2). A control means (8) for controlling the regulating valve (5) and the oxidant regulating valve (7) is provided. The control means (8) measures heat demand and power demand (S1), and the ratio of heat demand increases. If so (S2), the current density control means (3) is throttled while the fuel supply amount is kept constant, thereby reducing the power generation output of the fuel cell (1).

  Further, according to the present invention, the high-temperature operation type fuel cell (1), the current density control means (3) for controlling the power generation output of the fuel cell (1), and the fuel supplied to the fuel cell (1) A fuel adjustment valve (5) for controlling the supply amount, an oxidant adjustment valve (7) for controlling an oxidant supply amount supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1) ) And a fuel cell cogeneration system comprising a heat recovery means (15) for supplying exhaust heat of the fuel cell (1) to the heat demand side, and a fuel cell system temperature meter (2). The control means (3) is connected to the power demand (12) via the output power line (Le), and between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). Is equipped with an exhaust gas temperature sensor (17), Receiving the input signals from the heat utilization means for utilizing the heat recovered by the means (15), the power demand (12), the current density control means (3), and the fuel cell system temperature measurement means (2); A control means (8) for controlling the fuel adjustment valve (5) and the oxidant adjustment valve (7) is provided. The control means (8) measures heat demand and power demand (S11), and the ratio of power demand is If it increases (S12), it has a function of increasing the power generation output of the fuel cell (1) by opening the current density control means (3) while keeping the fuel supply amount constant.

  According to the present invention, the high-temperature operating fuel cell (1), the current density control means (3) for controlling the power generation output of the fuel cell (1), and the fuel supplied to the fuel cell (1) A fuel adjustment valve (5) for controlling the supply amount, an oxidant adjustment valve (7) for controlling an oxidant supply amount supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1) ) And a fuel cell cogeneration system comprising a heat recovery means (15) for supplying exhaust heat of the fuel cell (1) to the heat demand side, and a fuel cell system temperature meter (2). The control means (3) is connected to the power demand (12) via an output power line (Le) having a D / D converter (9), and the off-gas combustion part (1a) of the fuel cell (1) and the heat Between the recovery means (15) (17) and an electric heater (19) are interposed, and the electric heater (19) is connected to the D / D converter (9) by a sub power line (Les) interposing a current control means (18). Input from the heat recovery means that uses the heat recovered by the heat recovery means (15), the power demand (12), the current density control means (3), and the fuel cell system temperature measurement means (2). In response to the signal, there is provided control means (8) for controlling the fuel adjustment valve (5) and the oxidant adjustment valve (7) and for turning on / off the current control means (18). And if the power demand is measured (S21) and there is a surplus of power demand (S22), it is determined whether or not the exhaust heat recovery amount is insufficient with respect to the heat demand (S23), and the exhaust heat with respect to the heat demand. If the recovered amount is insufficient, turn the current control means (18) Is dynamic (S24), if the heat recovery amount if greater than the heat demand (S26), and has a function of turning off the current control means (18).

  Furthermore, according to the present invention, the fuel cell (1) operated at high temperature, the current density control means (3) for controlling the power generation output of the fuel cell (1), and the fuel supplied to the fuel cell (1) A fuel adjustment valve (5) for controlling the supply amount, an oxidant adjustment valve (7) for controlling an oxidant supply amount supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1) ) And a fuel cell cogeneration system comprising a heat recovery means (15) for supplying exhaust heat of the fuel cell (1) to the heat demand side, and a fuel cell system temperature meter (2). The control means (3) is connected to the power demand (12) via the output power line (Le), and between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). Is provided with an exhaust gas temperature sensor (17), and the heat In response to input signals from the heat utilization means utilizing the heat recovered by the collecting means (15), the power demand (12), the current density control means (3), and the fuel cell system temperature measurement means (2). Control means (8) for controlling the fuel adjustment valve (5) and the oxidant adjustment valve (7) is provided, and the control means (8) measures heat demand and power demand (S31), and the ratio of heat demand (S32), the fuel adjustment valve (5) is opened while the current density and / or fuel utilization rate is kept constant, thereby increasing the fuel supply amount.

  And according to this invention, the fuel cell (1) of a high temperature operation type, the current density control means (3) which controls the electric power generation output of the fuel cell (1), and the fuel supplied to the fuel cell (1) A fuel adjustment valve (5) for controlling the supply amount, an oxidant adjustment valve (7) for controlling an oxidant supply amount supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1) ) And a fuel cell cogeneration system comprising a heat recovery means (15) for supplying exhaust heat of the fuel cell (1) to the heat demand side, and a fuel cell system temperature meter (2). The control means (3) is connected to the power demand (12) via the output power line (Le), and between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). Is equipped with an exhaust gas temperature sensor (17), Receiving the input signals from the heat utilization means for utilizing the heat recovered by the means (15), the power demand (12), the current density control means (3), and the fuel cell system temperature measurement means (2); A control means (8) for controlling the fuel adjustment valve (5) and the oxidant adjustment valve (7) is provided, the control means (8) measures the heat demand and the power demand (S41), and the ratio of the power demand is If it is reduced (S42), if the power demand is higher, the fuel adjustment valve (5) is throttled while the current density and / or fuel utilization rate is kept constant, thereby reducing the fuel supply amount.

  Further, according to the present invention, the high-temperature operation type fuel cell (1), the current density control means (3) for controlling the power generation output of the fuel cell (1), and the fuel supplied to the fuel cell (1) A fuel adjustment valve (5) for controlling the supply amount, an oxidant adjustment valve (7) for controlling an oxidant supply amount supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1) ) And a fuel cell cogeneration system comprising a heat recovery means (15) for supplying exhaust heat of the fuel cell (1) to the heat demand side, and a fuel cell system temperature meter (2). The control means (3) is connected to the power demand (12) via the output power line (Le), and between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). Is equipped with an exhaust gas temperature sensor (17), Receiving the input signals from the heat utilization means for utilizing the heat recovered by the means (15), the power demand (12), the current density control means (3), and the fuel cell system temperature measurement means (2); A control means (8) for controlling the fuel adjustment valve (5) and the oxidant adjustment valve (7) is provided, the control means (8) measures the heat demand and the power demand (S51), and the ratio of the heat demand is If it is increased (S52), the current density and / or the fuel utilization rate is decreased by adjusting the current density control means (3) within a range where the oxidant is not withered in the fuel cell (1) while increasing the fuel supply amount. It has a function to make it.

  According to the present invention, the high-temperature operating fuel cell (1), the current density control means (3) for controlling the power generation output of the fuel cell (1), and the fuel supplied to the fuel cell (1) A fuel adjustment valve (5) for controlling the supply amount, an oxidant adjustment valve (7) for controlling an oxidant supply amount supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1) ) And a fuel cell cogeneration system comprising a heat recovery means (15) for supplying exhaust heat of the fuel cell (1) to the heat demand side, and a fuel cell system temperature meter (2). The control means 3) is connected to the power demand (12) via the output power line (Le), and between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). An exhaust gas temperature sensor (17) is interposed to Receiving the input signals from the heat utilization means utilizing the heat recovered by the means (15), the power demand (12), the generated power adjustment means (3), and the fuel cell system temperature measurement means (2); A control means (8) for controlling the fuel adjustment valve (5) and the oxidant adjustment valve (7) is provided, the control means (8) measures the heat demand and the power demand (S61), and the ratio of the power demand is If it has decreased (S62), the current density and / or the fuel utilization rate are increased by adjusting the current density control means (3) within the range where fuel depletion does not occur in the fuel cell (1) while decreasing the fuel supply amount. It has a function to make it.

  Furthermore, according to the present invention, the fuel cell (1) operated at high temperature, the current density control means (3) for controlling the power generation output of the fuel cell (1), and the fuel supplied to the fuel cell (1) A fuel adjustment valve (5) for controlling the supply amount, an oxidant adjustment valve (7) for controlling an oxidant supply amount supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1) ) And a fuel cell cogeneration system comprising a heat recovery means (15) for supplying exhaust heat of the fuel cell (1) to the heat demand side, and a fuel cell system temperature meter (2). The control means (3) is connected to the power demand (12) via the output power line (Le), and between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). Is provided with an exhaust gas temperature sensor (17). A heat utilization means connected to an off-gas air supply line (21) having an oxidant valve (22) interposed in the gas combustion section (1a), and utilizing the heat recovered by the heat recovery means (15); The fuel adjustment valve (5), the oxidant adjustment valve (7), and the oxidant in response to input signals from the power demand (12), the current density control means (3), and the fuel cell system temperature measurement means (2). A control means (8) for controlling the valve (22) is provided, and the control means (8) judges whether the off-gas combustion state needs to shift to a lean side or to a stoichiometric side. (S72) If the shift to the lean side is necessary, the opening degree of the oxidizer valve (22) is increased (S73), and if the shift to the stoichiometric side is necessary, the opening degree of the oxidizer valve (22) is reduced. Have.

  And according to this invention, the fuel cell (1) of a high temperature operation type, the current density control means (3) which controls the electric power generation output of the fuel cell (1), and the fuel supplied to the fuel cell (1) A fuel adjustment valve (5) for controlling the supply amount, an oxidant adjustment valve (7) for controlling an oxidant supply amount supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1) ) And a fuel cell cogeneration system comprising a heat recovery means (15) for supplying exhaust heat of the fuel cell (1) to the heat demand side, and a fuel cell system temperature meter (2). The control means (3) is connected to the power demand (12) via the output power line (Le), and between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). Is equipped with an exhaust gas temperature sensor (17) The heat combustion means (1a) is connected to a fuel supply line (23) for an off-gas combustion part having a fuel valve (24) interposed therebetween, and uses heat recovered by the heat recovery means (15). Receiving the input signals from the power demand (12), the current density control means (3) and the fuel cell system temperature measurement means (2), the fuel adjustment valve (5) and the oxidant adjustment valve (7) The control means (8) for controlling the fuel valve (24) is provided. If the exhaust heat recovery amount is less than the heat demand (S81), the control means (8) opens the fuel valve (24) to perform off-gas combustion. When the fuel is supplied to the part (1a) (S82) and a predetermined time has elapsed (S83) and the amount of exhaust heat recovery exceeds the heat demand (S84), the fuel is supplied to the off-gas combustion part (1a). Has a function to stop.

  Further, according to the present invention, the high-temperature operation type fuel cell (1), the current density control means (3) for controlling the power generation output of the fuel cell (1), and the fuel supplied to the fuel cell (1) A fuel adjustment valve (5) for controlling the supply amount, an oxidant adjustment valve (7) for controlling an oxidant supply amount supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1) ) And a fuel cell cogeneration system comprising a heat recovery means (15) for supplying exhaust heat of the fuel cell (1) to the heat demand side, and a fuel cell system temperature meter (2). The control means (3) is connected to the power demand (12) via the output power line (Le), and is connected between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). The exhaust gas temperature sensor (17) is connected to the exhaust gas line (Lh). And a reheating burner (25) having a spark plug (25P), and a fuel supply line (26) having a fuel valve (27) connected to the reheating burner (25), In response to input signals from the heat utilization means utilizing the heat recovered by the recovery means (15), the power demand (12), the current density control means (3), and the fuel cell system temperature measurement means (2). Control means (8) for controlling the fuel adjustment valve (5), the oxidant adjustment valve (7), the fuel valve (27), and the spark plug (25P) is provided, and the control means (8) is for recovering exhaust heat. If the amount is below the heat demand (S91), the fuel valve (27) is opened, fuel is supplied to the reheating burner (25) and ignited by the spark plug (25P) (S92). S93), Exhaust heat recovery exceeds heat demand If Kitara (S94), cutting the fuel supply to turn off the fired burner (25) to follow (S95) has a function.

  According to the present invention having the above-described configuration, the fuel cell (1) and the power generation output adjusting means for controlling the power generation output (for example, current density and / or fuel utilization rate) of the fuel cell (1) ( For example, a power conditioner 3), fuel supply amount control means (fuel adjustment valve 5) for controlling the amount of fuel supplied to the fuel cell (1), and an oxidant (for example, air) supplied to the fuel cell (1) An oxidant supply amount control means (oxidant adjustment valve 7) for controlling the supply amount, and an exhaust system (Lh) of the fuel cell (1) to dissipate the fuel cell exhaust heat on the heat demand side (water heater, boiler, etc.) The heat recovery means (for example, the heat exchanger 15) supplied to the fuel cell (1) and the operating state monitoring means for monitoring the operating state of the fuel cell (1) (for example, a battery temperature sensor interposed in the fuel cell main body or an exhaust system) An intervening exhaust gas temperature sensor 17), Means (fuel cell cogeneration monitoring device, battery controller 8), and the control means (8) generates power output (eg, current density and / or fuel utilization) of the fuel cell (1) in response to fluctuations in heat demand. Rate) and / or control to change the exhaust gas temperature of the fuel cell (1), the thermoelectric ratio can be changed by the fuel cell (1) alone, and the apparatus and control method are greatly increased. Simplified.

  According to the present invention, it is possible to provide a fuel cell cogeneration system with a power generation output of 1 to 200 kW, which is a medium to small scale fuel cell cogeneration system that can change the thermoelectric ratio.

  Furthermore, according to the present invention, conventionally, a fuel cell system whose thermoelectric ratio cannot be changed unless it is configured as a hybrid type can cover the heat demand even when the heat supply capacity is insufficient for the heat demand. Can provide a system that can.

  Further, when supplementing the shortage heat demand, when additional fuel supply or a reheating burner (25) is used, additional fuel is supplied to the high temperature off-gas combustion section (1a), or it is driven in the high temperature exhaust gas. Since the burning burner (25) is burned, a small amount of fuel is required to make up for the shortage of heat demand.

  Embodiments of the present invention will be described below with reference to the accompanying drawings.

  First, a first embodiment (embodiment including the whole) will be described with reference to FIG.

  The system of the first embodiment of FIG. 1 (hereinafter, the fuel cell cogeneration system is simply referred to as a system) is operated at a high temperature such as a solid oxide fuel cell (SOFC) or a molten carbonate fuel cell (MCFC). Type fuel cell 1 and a power conditioner 3 which is a power generation output adjusting means for controlling the power generation output (for example, current density and / or fuel utilization rate) of the fuel cell 1.

  The system includes a fuel supply line 4 that supplies fuel to the fuel cell 1 and an oxidant supply line 6 that supplies an oxidant (for example, air) of the fuel cell 1, and the fuel supply line 4 includes the fuel cell 1. A fuel supply amount control means (fuel adjustment valve) 5 for controlling the fuel supply amount to be supplied, and an oxidant for controlling an oxidant (for example, air) supply amount to be supplied to the fuel cell 1 in the oxidant supply line 6. Supply amount control means (oxidant adjusting valve) 7 is interposed.

An exhaust system Lh is connected to the off-gas combustion part 1a of the fuel cell, and the exhaust system Lh exchanges heat from the fuel cell exhaust heat with, for example, tap water (tap water) so that the heat demand side (water heater, boiler, etc.) ) Is provided with, for example, a water heater (hereinafter referred to as a heat exchanger) 15 which is a heat recovery means for supplying the heat recovery line Lb to the heat recovery line Lb. An exhaust gas temperature sensor 17 for measuring the exhaust gas temperature is interposed in the area between 1a.
The fuel cell 1 is also provided with a fuel cell system temperature measuring device 2 for directly measuring the temperature of each part in the fuel cell 1.

  The output power line Le of the fuel cell 1 is connected to the power demand 12, and the output power line Le is sequentially connected from the fuel cell 1 side to the power conditioner 3, D / D which is a means for controlling the current density and / or the fuel utilization rate. A converter 9 and an inverter 11 are interposed.

  The system includes a control means (a complex of a fuel cell cogeneration monitoring device and a fuel cell control unit) 8, and an exhaust gas temperature sensor 17 and an input signal by the fuel cell system temperature measuring instrument 2 and the input signal line Li 1. The line Li2 is a means for using heat (steam or hot water), for example, a bath operation panel (not shown) or the like and the input signal line Li3, and the power demand is connected by the input signal line Li4.

  Further, the control means (hereinafter, the control means is referred to as a control unit) 8 includes the fuel adjustment valve 5 and the output signal line Lo1, the oxidant adjustment valve 7 and the output signal line Lo2, the power conditioner 3 and the output signal line Lo3. Connected with.

  The control unit 8 performs control to vary the power generation output (for example, current density and / or fuel utilization rate) and / or the exhaust gas temperature of the fuel cell 1 in response to fluctuations in heat demand. It is configured.

  That is, the control unit 8 also obtains information from the fuel cell system temperature measuring instrument 2 and can change the exhaust heat recovery amount while maintaining the heat self-sustainability of the fuel cell 1. Both heat recovery amounts are controlled.

Next, a second embodiment will be described with reference to FIGS.
In the second embodiment, the control method in the apparatus of FIG. 1, that is, the fuel supply amount is made constant, and the current density and / or the fuel utilization rate is reduced to cope with the increase in heat demand (control the exhaust heat recovery amount). ) An embodiment relating to a control method.
Specifically, in the second embodiment, the current density and / or the fuel utilization rate are maintained while keeping the fuel supply amount of the fuel cell constant when the ratio of the heat demand among the demand amounts of power and heat increases. By reducing the power generation amount, the power generation amount is reduced, but by increasing the proportion of the fuel combusted in the off-gas combustion section, the exhaust gas temperature rises and the exhaust heat recovery amount is increased.

  First, in step S1, the control unit 8 measures heat demand and power demand based on information from the input signal line Li3 for heat demand information and the input signal line Li4 for power demand information.

  In the next step S2, the control unit 8 determines whether or not the heat demand exceeds the power demand (a considerable amount), that is, the heat demand ratio has increased, and if the heat demand ratio has increased (step S2). NO), the process proceeds to step S3, and if the heat demand ratio is not increased (NO in step S2), the process proceeds to step S4.

  In step S3, with the fuel supply amount kept constant, the power conditioner 3 is squeezed to reduce the power generation output of the fuel cell 1, and then the process returns to step S1 again to repeat step S1 and subsequent steps.

  In step S4, the control unit 8 determines whether or not to end the control, and if it is ended (YES in step S4), the control is ended as it is. On the other hand, if the control is continued (NO in step S4), the process returns to step S1 and repeats step S1 and subsequent steps.

In the second embodiment of FIGS. 1 and 2, as described above, if the fuel supply amount is kept constant and the current density and / or fuel utilization rate is reduced when the heat demand ratio increases, the off-gas combustion unit The proportion of fuel that burns increases.
And if the ratio of the fuel combusted in an off-gas combustion part increases, naturally the amount of exhaust heat will also increase and the amount of exhaust heat recovery can also be increased.

Next, a third embodiment will be described with reference to FIGS. 1 and 3.
The third embodiment is an embodiment relating to a control method different from the second embodiment in the apparatus of FIG. 1, that is, a control method that copes with an increase in power demand by increasing the current density and / or fuel utilization rate. .
Specifically, when the power demand ratio increases, the fuel gas that burns off gas while increasing the power output by increasing the current density and / or fuel utilization rate while keeping the fuel supply amount of the fuel cell constant. This is a control to reduce the amount of exhaust heat recovery by reducing the ratio of.

A third embodiment will be described below with reference to FIG.
First, in step S11 of FIG. 3, the control unit 8 measures heat demand and power demand based on information from the input signal line Li3 for heat demand information and the input signal line Li4 for power demand information.

  In the next step S12, the control unit 8 determines whether or not the power demand exceeds (a considerable amount) the heat demand, that is, whether the power demand ratio has increased, and if the power demand ratio has increased (step S12). NO), the process proceeds to step S13, and if the power demand ratio is not increased (NO in step S12), the process proceeds to step S14.

  In step S13, with the fuel supply amount kept constant, the power conditioner 3 is opened to increase the power generation output of the fuel cell 1, and then the process returns to step S11 again to repeat step S11 and subsequent steps.

  In step S14, the control unit 8 determines whether or not to end the control, and if it is ended (YES in step S14), the control is ended as it is. On the other hand, if the control is to be continued (NO in step S14), the process returns to step S11 and step S11 and subsequent steps are repeated again.

  In the third embodiment of FIGS. 1 and 3, as described above, if the fuel supply amount is made constant when the power demand increases and the current density and / or fuel utilization rate is increased, the off-gas combustion unit The proportion of fuel that burns decreases. And if the ratio of the fuel combusted in an off-gas combustion part decreases, naturally the amount of exhaust heat will also decrease and the amount of exhaust heat recovery can also be decreased.

Next, a fourth embodiment will be described with reference to FIGS.
In the fourth embodiment shown in FIGS. 4 and 5, in the state where electricity is surplus, when the exhaust heat recovery amount is insufficient with respect to the heat demand, the power generated by the fuel cell is used to interpose the exhaust heat system. In this embodiment, for example, an electric heater is operated to heat the exhaust gas to satisfy the insufficient heat demand.

  The apparatus of the fourth embodiment in FIG. 4 is different from the apparatus of the first to third embodiments (FIG. 1) in that an electric heater 19 is provided in the region between the heat exchanger 15 of the exhaust system Lh and the exhaust gas temperature sensor 17. In this embodiment, the electric heater 19 and the D / D converter 9 are connected by the sub power line Les, and the current control means 18 is interposed in the sub power line Les.

The control unit 8 is configured to control the ON / OFF of the electric heater 19 and the supply current by the current control means 18.
That is, in the fourth embodiment, the electric power supplied to the electric heater 19 is the electric power generated by the fuel cell 1.

Based on FIG. 5, the control method of 4th Embodiment is demonstrated with reference also to FIG.
First, in step S21, the control unit 8 measures heat demand and power demand based on information from the input signal line Li3 for heat demand information and the input signal line Li4 for power demand information.

  In the next step S22, the control unit 8 determines whether there is surplus power with respect to the power demand. If there is surplus power (YES in step S22), the process proceeds to step S23. The process proceeds to step S27 (NO in step S22).

  In step S23, the control unit 8 determines whether or not the exhaust heat recovery amount is insufficient for the heat demand, and if the exhaust heat recovery amount is insufficient for the demand (YES in step S23). The process proceeds to step S24, and if the exhaust heat recovery amount is not insufficient with respect to the demand (NO in step S23), the process proceeds to step S27.

  In step S24, the electric current control means 18 is operated, the electric power generated by the fuel cell 1 is input to the electric heater 19 interposed in the exhaust heat line Lh via the D / D converter 9, and the process proceeds to step S25.

  In step S25, the control unit 8 determines whether or not the exhaust heat recovery amount exceeds the heat demand. If the exhaust heat recovery amount exceeds the heat demand (YES in step S25), the control unit 8 proceeds to step S26 and exceeds it. If not (NO in step S25), the loop of step S25 is repeated until it exceeds.

  In step S26, the current control means 18 is turned off, the process returns to step S21, and step S21 and subsequent steps are repeated again.

  In step S27, the control unit 8 determines whether or not to end the control, and if it is ended (YES in step S27), the control is ended as it is. On the other hand, if the control is continued (NO in step S27), the process returns to step S21 and repeats step S21 and subsequent steps.

Next, a fifth embodiment will be described with reference to FIGS. 1 and 6.
In the second to fourth embodiments, the fuel supply amount is kept constant and the thermoelectric ratio is changed. In the fifth to eighth embodiments, the fuel supply amount is changed to recover the exhaust heat. The amount is controlled.

The fifth embodiment is a control method for increasing the exhaust heat recovery rate by increasing the fuel supply amount while keeping the current density and / or fuel utilization rate of the fuel cell constant when the heat demand ratio increases.
In the case of the fifth embodiment, the demand for electricity is not necessarily increased.

  First, in step S31 of FIG. 6, the control unit 8 measures heat demand and power demand based on information from the input signal line Li3 for heat demand information and the input signal line Li4 for power demand information.

  In the next step S32, the control unit 8 determines whether the heat demand exceeds (a considerable amount) the power demand, that is, whether the heat demand ratio has increased, and if the heat demand ratio has increased (step S32). NO), the process proceeds to step S33, and if the ratio of heat demand is not increased (NO in step S32), the process proceeds to step S34.

In step S33, with the current density and / or fuel utilization rate kept constant, the fuel adjustment valve 5 is opened and the fuel supply amount is increased. Then, the process returns to step S31 again and repeats step S31 and subsequent steps.
If the fuel supply amount is increased while maintaining the power generation output, the amount of fuel gas for off-gas combustion increases and the exhaust gas temperature rises. As a result, the exhaust heat recovery amount can be increased.

  When the fuel supply amount is increased, the fuel cell 1 is maintained in a self-sustained operation state, and oxidant depletion (a phenomenon in which the amount of oxidant supplied with respect to the fuel amount is insufficient, and “oxidant depletion” occurs). It is important to increase the fuel supply amount in such a range that the fuel cell is not damaged).

  In step S34, the control unit 8 determines whether or not to end the control, and if it is ended (YES in step S34), the control is ended as it is. On the other hand, if the control is to be continued (NO in step S34), the process returns to step S31 and repeats step S31 and subsequent steps.

Next, a sixth embodiment will be described with reference to FIGS. 1 and 7.
In the sixth embodiment, when the heat demand ratio decreases, the fuel cell current density and / or the fuel utilization rate remain constant, and the fuel supply amount is decreased to maintain off-gas combustion while maintaining the power generation output. This is an embodiment in which the amount of fuel gas to be increased is increased to lower the exhaust gas temperature, and as a result, the exhaust heat recovery amount is decreased. In the case of the sixth embodiment, the electricity demand does not necessarily fluctuate.

  First, in step S41 of FIG. 7, the control unit 8 measures heat demand and power demand based on information from the input signal line Li3 for heat demand information and the input signal line Li4 for power demand information.

  In the next step S42, the control unit 8 determines whether or not the power demand exceeds the heat demand (a considerable amount), that is, whether or not the power demand ratio has decreased, and if the power demand ratio has decreased ( If YES in step S42), the process proceeds to step S43, and if the power demand ratio is not increased (NO in step S42), the process proceeds to step S44.

In step S43, with the current density and / or fuel utilization rate kept constant, the fuel adjustment valve 5 is throttled to reduce the fuel supply amount, and then the process returns to step S41 again to repeat step S41 and subsequent steps.
If the fuel supply amount is decreased while maintaining the power generation output, the amount of fuel gas that burns off-gas decreases, the exhaust gas temperature decreases, and as a result, the exhaust heat recovery amount can be decreased.

  When the fuel supply amount is decreased, the fuel cell 1 is maintained in a self-sustained operation state and the fuel cell is exhausted (a phenomenon in which the fuel supply amount to the oxidant is insufficient. It is important to reduce the amount of fuel supplied to the extent that does not occur.

  In step S44, the control unit 8 determines whether or not to end the control, and if it is ended (YES in step S44), the control is ended as it is. On the other hand, if the control is continued (NO in step S44), the process returns to step S41 and repeats step S41 and subsequent steps.

Next, a seventh embodiment will be described with reference to FIGS. 1 and 8.
In the fifth embodiment, the output (current density and / or fuel utilization rate) is constant, but in the seventh embodiment of FIGS. 1 and 8, when the heat demand increases, the fuel supply amount of the fuel cell is increased. In this control, the output (current density and / or fuel utilization rate) is reduced within the range where oxidant depletion does not occur in the fuel cell, and the amount of exhaust heat recovery is increased by increasing the off-gas combustion rate while reducing the power generation output. .

    First, in step S51 of FIG. 8, the control unit 8 measures heat demand and power demand based on information from the input signal line Li3 for heat demand information and the input signal line Li4 for power demand information.

  In the next step S52, the control unit 8 determines whether or not the power demand ratio has increased, and if the power demand ratio has increased (YES in step S52), the process proceeds to step S53, where the power demand ratio is If not increased (NO in step S52), the process proceeds to step S54.

In step S53, the power conditioner 3 is adjusted to decrease the current density and / or the fuel utilization rate within a range in which the fuel cell 1 does not oxidize with increasing the fuel supply amount, and then the process returns to step S51. Step S51 and subsequent steps are repeated again.
By reducing the current density and / or fuel utilization, the power generation output is reduced and the off-gas combustion rate is increased. As the off-gas combustion rate increases, the amount of exhaust heat recovery increases.

  In step S54, the control unit 8 determines whether or not to end the control, and if it is ended (YES in step S54), the control is ended as it is. On the other hand, if the control is to be continued (NO in step S54), the process returns to step S51 and repeats step S51 and subsequent steps.

Next, an eighth embodiment: FIG. 1 and a flowchart will be described with reference to FIGS.
In the sixth embodiment, the output (current density and / or fuel utilization rate) is constant, but in the eighth embodiment of FIGS. 1 and 9, when the heat demand decreases, the fuel supply amount of the fuel cell is decreased. In this control, the output (current density and / or fuel utilization rate) is increased within a range where fuel depletion does not occur in the fuel cell, and the amount of exhaust heat recovery is decreased by increasing the power generation output and decreasing the off-gas combustion rate.

  First, in step S61 of FIG. 9, the control unit 8 measures heat demand and power demand based on information from the input signal line Li3 for heat demand information and the input signal line Li4 for power demand information.

  In the next step S62, the control unit 8 determines whether or not the power demand ratio has decreased. If the power demand ratio has decreased (YES in step S62), the process proceeds to step S63, where the power demand ratio is If not lowered (NO in step S62), the process proceeds to step S64.

In step S63, the power conditioner 3 is adjusted to increase the current density and / or the fuel utilization rate within a range where fuel depletion does not occur in the fuel cell 1 while reducing the fuel supply amount, and then the process returns to step S61. Step S61 and subsequent steps are repeated again.
By increasing the current density and / or fuel utilization, the power generation output increases and the off-gas combustion rate decreases. As the off-gas combustion rate decreases, the amount of exhaust heat recovery decreases.

  In step S64, the control unit 8 determines whether or not to end the control, and if it is ended (YES in step S64), the control is ended as it is. On the other hand, if the control is to be continued (NO in step S64), the process returns to step S61 and repeats step S61 and subsequent steps.

Next, a ninth embodiment will be described with reference to FIGS. 10 and 11.
The off gas is a fuel gas that has not contributed to the power generation reaction of the fuel cell 1 and is generated in the off gas combustion portion downstream of the fuel cell. And when off-gas burns, the temperature of exhaust gas further rises.
Therefore, if the amount of off-gas is varied, the amount of exhaust heat recovery can be adjusted.

In the ninth embodiment shown in FIGS. 10 and 11, an oxidant (air) is added to the off-gas combustion section, and the flow rate is adjusted to determine whether the off-gas combustion is lean or stoichiometric. . That is, if the oxidant flow rate is increased, the combustion state shifts to the lean combustion side, the exhaust temperature becomes lower, and the exhaust heat recovery amount decreases.
On the other hand, if the oxidant flow rate is decreased, the combustion state shifts to the stoichiometric combustion side, the exhaust gas temperature becomes high, and the exhaust heat recovery amount increases.

  As shown in FIG. 10, the system has a configuration in which an off-gas air supply line 21 is provided in the off-gas combustion unit 1a and an oxidizer valve is provided in the off-gas air supply line 21 as compared with the configuration of the first embodiment in FIG. (Air adjustment valve) 22 is interposed, and the other configuration is the same as in FIG.

By adjusting the opening degree of the oxidizer valve 22, lean combustion or stoichiometric combustion can be selected. In lean combustion, exhaust gas has a high flow rate at a low temperature, and in stoichiometric combustion, exhaust gas has a high temperature and a small flow rate.
That is, the amount of exhaust heat recovery can be adjusted depending on whether off-gas combustion in the off-gas combustion unit 1a is lean combustion or stoichiometric combustion.

  Parameters for determining whether off-gas combustion is lean combustion or stoichiometric combustion include power demand, heat demand, the structure of the heat exchanger (heat exchange water heater) 15 interposed in the exhaust system Lh, and the exhaust side Lh. And a temperature difference between the hot water supply side Lb and the like.

A control method according to the ninth embodiment will be described with reference to FIG.
First, in step S71, the control unit 8 determines whether or not the control of the second, third, fifth to eighth embodiments is being performed, and the second, third, fifth to eighth embodiments are controlled. If the control is being performed (YES in step S71), the process proceeds to step S72. If the control in the second, third, and fifth to eighth embodiments is not being performed (NO in step S71), the process proceeds to step S75.

  In step S72, the control unit determines the off-gas combustion state based on the exhaust gas temperature information (Li2) from the exhaust gas temperature sensor 17, the hot water supply information from the hot water supply line Lb (Li3), the power demand information from the power demand 12 (Li4), and the like. It is determined whether it is OK, whether it is necessary to shift to the lean combustion side, or whether it is necessary to shift to the stoichiometric side.

  If the off-gas combustion state is OK, the process proceeds to step S75. If it is necessary to shift to the lean combustion side, the process proceeds to step S73. If it is necessary to shift to the stoichiometric side, the process proceeds to step S74.

In step S73, the opening degree of the oxidant valve 22 is increased, the amount of oxidant (air) supplied to the off-gas combustion unit 1a is increased, and the process proceeds to step S75.
By increasing the amount of oxidant (air) supplied to the off-gas combustion unit 1a, the off-gas combustion unit 1a becomes lean combustion, and the exhaust gas temperature is lowered. Therefore, the recovery obtained by the heat exchanger 15 interposed in the exhaust gas line The amount of heat decreases.

In step S74, the opening degree of the oxidant valve 22 is reduced, the amount of oxidant (air) supplied to the off-gas combustion unit 1a is decreased, and the process proceeds to step S75.
By reducing the amount of oxidant (air) supplied to the off-gas combustion section 1a, the off-gas combustion section 1a becomes stoichiometric combustion, and the exhaust gas temperature rises. Therefore, it is obtained by the heat exchanger 15 interposed in the exhaust gas line. The amount of heat recovered increases.

  In step S75, the control unit 8 determines whether or not to end the control. If the control unit 8 has ended (YES in step S75), the control is ended as it is. On the other hand, if not finished (NO in step S75), the process returns to step S71, and step S71 and subsequent steps are repeated again.

Next, a tenth embodiment will be described with reference to FIGS. 12 and 13.
The tenth embodiment shown in FIGS. 12 and 13 increases the exhaust heat recovery amount by supplying fuel corresponding to the insufficient heat demand to the off-gas combustion unit when the heat recovery amount is lower than the heat demand, thereby reducing the shortage. It is an embodiment to supplement.

  As shown in FIG. 12, the system is configured by providing an off-gas combustion unit fuel supply line 23 in the off-gas combustion unit 1a with respect to the configuration of the first embodiment of FIG. 1 is provided with a fuel valve (flow rate adjusting valve) 24, and the other configuration is the same as in FIG.

It is to be noted that lean combustion or stoichiometric combustion can be selected by adjusting the opening of the fuel valve 24. In lean combustion, exhaust gas can be made at a low temperature and a large flow rate. In stoichiometric combustion, exhaust gas at a high temperature and a small flow rate can be selected. It can be.
That is, the amount of exhaust heat recovery can be adjusted depending on whether off-gas combustion in the off-gas combustion unit 1a is lean combustion or stoichiometric combustion.

  Parameters for determining whether off-gas combustion is lean combustion or stoichiometric combustion include power demand, heat demand, the structure of the heat exchanger (heat exchange water heater) 15 interposed in the exhaust system Lh, and the exhaust side Lh. And a temperature difference between the hot water supply side Lb and the like.

Based on FIG. 13, the control method of the tenth embodiment will be described with reference to FIG.
First, in step S81, the control unit 8 determines whether or not the heat recovery amount is below the heat demand. If it is below (YES in step S81), the control unit 8 proceeds to step S82, and if not below ( The process proceeds to step S86 (NO in step S81).

  In step S82, the fuel valve 24 interposed in the fuel supply line 23 is opened, and fuel is supplied to the off-gas combustion unit 1a.

In the next step S83, the control unit 8 monitors until a predetermined time elapses, and when the predetermined time elapses, the process proceeds to step S84. In step S84, the control unit 8 determines whether or not the exhaust heat recovery amount has exceeded the heat demand.
If the amount of exhaust heat recovery exceeds the heat demand (YES in step S84), the process proceeds to step S85, and if not yet exceeded (NO in step S84), the loop of step S84 is repeated.

  In step S85, the fuel valve 24 is closed and the fuel supply to the off-gas combustion unit 1a is stopped, and then the process proceeds to the next step S86. In step S86, the control unit 8 determines whether or not to end the control. If the control unit 8 ends the control (YES in step S86), the control ends as it is. On the other hand, if not finished yet (NO in step S86), the process returns to step S81 and repeats step S81 and subsequent steps.

Next, an eleventh embodiment will be described with reference to FIGS. 14 and 15.
In the eleventh embodiment shown in FIGS. 14 and 15, as shown in the configuration of FIG. 14, the heat exchanger 15 is disposed upstream of the heat exchanger 15 (example shown) in the exhaust gas flow path Lh of the fuel cell 1 or inside the heat exchanger 15. A burning burner 25 is interposed.

  A fuel supply line 26 having a fuel flow rate adjusting valve 27 interposed is connected to the reheating burner 25, and an ignition plug 25P provided in the reheating burner 25 when the amount of energy recovered by exhausting the fuel cell 1 falls below the heat demand. By igniting the fuel, the fuel supplied by the reheating burner 25 is combusted to increase the amount of heat energy recovered from the exhaust, and the control method therefor.

  Here, the exhaust gas temperature immediately before the reheating burner 25 is high, and oxygen is sufficiently contained in the exhaust gas. Therefore, even if the flow rate of fuel supplied to the reheating burner 25 is small, sufficient combustion heat is generated to meet the shortage heat demand.

Based on FIG. 15, the control method of the eleventh embodiment will be described with reference also to FIG.
First, in step S91, the control unit 8 determines whether or not the heat recovery amount is lower than the heat demand. If it is lower (YES in step S91), the process proceeds to step S92. The process proceeds to step S96 (NO in step S91).

  In step S92, the fuel valve 27 provided in the fuel supply line 26 is opened, fuel is supplied to the reheating burner 25 and ignited by the spark plug 25P of the reheating burner 25, and then the process proceeds to step S93.

In the next step S93, the control unit 8 monitors until a predetermined time elapses, and when the predetermined time elapses, the process proceeds to step S94. In step S94, the control unit 8 determines whether or not the exhaust heat recovery amount has exceeded the heat demand.
If the amount of exhaust heat recovery exceeds the heat demand (YES in step S94), the process proceeds to step S95, and if not yet exceeded (NO in step S94), the loop of step S94 is repeated.

In step S95, the burner burner is turned off and the supplied fuel is cut, and then the process proceeds to the next step S96.
In step S96, the control unit 8 determines whether or not to end the control. If the control unit 8 is to end (YES in step S96), the control ends as it is. On the other hand, if not finished yet (NO in step S96), the process returns to step S91 and repeats step S91 and subsequent steps.

Next, a twelfth embodiment will be described with reference to FIG.
In the cogeneration system including one or more of the fourth embodiment, the tenth embodiment, and the eleventh embodiment, the twelfth embodiment of FIG. 16 starts with the fuel cell side when the heat demand ratio increases. When the heat supply ratio is increased by using one or more control methods other than the fourth embodiment, the tenth embodiment, and the eleventh embodiment, and the heat demand cannot be compensated, the fourth embodiment, the tenth embodiment It is an embodiment that covers the shortage of heat demand by using one or more system configurations and control methods other than the embodiment and the eleventh embodiment.
The fourth embodiment is a type that consumes part of the power generation output, and the tenth and eleventh embodiments are types that supply energy (fuel) from the outside.
Hereinafter, the control method of the twelfth embodiment will be described with reference to FIG.

  First, in step S101, the control unit 8 measures heat demand and power demand based on information from the input signal line Li3 for heat demand information and the input signal line Li4 for power demand information.

  In the next step S102, the control unit 8 determines whether or not the heat demand ratio is increased. If the heat demand ratio is increased (YES in step S102), the process proceeds to step S103, where the heat demand ratio is increased. If not (NO in step S102), the process proceeds to step S107.

  In step S103, the control of the second, third, fifth to ninth embodiments is performed to increase the exhaust heat recovery amount, and the process proceeds to the next step S104, where it is monitored until a predetermined time elapses. If the predetermined time has elapsed (YES in step S104), the process proceeds to step S105.

  In step S105, the control unit 8 determines whether or not the recovered heat quantity remains below the demand, and if the recovered heat quantity still remains below the demand (YES in step S105), the process proceeds to step S106. After performing one or more controls of the fourth embodiment, the tenth embodiment, and the eleventh embodiment, the process returns to step S101 and repeats the steps after step S101 again.

  On the other hand, if the heat demand has already been exceeded (NO in step S105), the process proceeds to step S107, and the control unit 8 determines whether or not to end the control. If the control is to be terminated (YES in step S107), the process is terminated as it is, and if it is not yet terminated (NO in step S107), the process returns to step S101, and step S101 and subsequent steps are repeated again.

  It should be noted that the illustrated embodiment is merely an example, and is not a description to limit the technical scope of the present invention.

The block diagram which shows the structure of 1st Embodiment of this invention. The flowchart which shows the control method of 2nd Embodiment of this invention. The flowchart which shows the control method of 3rd Embodiment of this invention. The block diagram which shows the structure of 4th Embodiment of this invention. The flowchart which shows the control method of 4th Embodiment of this invention. The flowchart which shows the control method of 5th Embodiment of this invention. The flowchart which shows the control method of 6th Embodiment of this invention. The flowchart which shows the control method of 7th Embodiment of this invention. The flowchart which shows the control method of 8th Embodiment of this invention. The block diagram which shows the structure of 9th Embodiment of this invention. The flowchart which shows the control method of 9th Embodiment of this invention. The block diagram which shows the structure of 10th Embodiment of this invention. The flowchart which shows the control method of 10th Embodiment of this invention. The block diagram which shows the structure of 11th Embodiment of this invention. The flowchart which shows the control method of 11th Embodiment of this invention. The flowchart which shows the control method of 12th Embodiment of this invention. The block diagram which showed the structure of the general high temperature operation method fuel cell cogeneration system. The graph which showed the daily change of the electric power and hot water supply demand in the fuel cell system utilized at a general household. A graph showing daily changes in demand for electric power, hot water, and steam in a fuel cell system used in hospitals and welfare facilities for the elderly. The block diagram which was the prior art, and showed the structure of the hybrid system which combined the high temperature operation method fuel cell and the micro gas turbine.

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 ... Fuel cell 2 ... Fuel cell operating condition determination means / Battery monitoring device 3 ... Current density control means / Power conditioner 4 ... Fuel supply system 5 ... Fuel supply amount control means / Fuel adjustment Valve 6 ... Oxidant supply system 7 ... Oxidant supply amount control means / Oxidant adjustment valve 8 ... Fuel cell control means / control unit 9 ... DC / DC converter 11 ... Bidirectional inverter 12 ... Electric power demand 15 ... Heat exchanger 17 ... Exhaust gas temperature sensor 19 ... Electric heater 21 ... Off-gas combustion part air supply line 22 ... Oxidant valve / air regulating valve 23 .... Fuel supply line 24 for off-gas combustion section ... Fuel valve / flow rate adjustment valve 25 ... Reheating burner Li ... Input signal line Lo ... Control signal line Le ... Output power line

Claims (10)

High temperature operation type fuel cell (1), current density control means (3) for controlling the power generation output of the fuel cell (1), and fuel adjustment for controlling the amount of fuel supplied to the fuel cell (1) A fuel cell interposed between a valve (5), an oxidant adjusting valve (7) for controlling the amount of oxidant supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1). In the fuel cell cogeneration system including the heat recovery means (15) for supplying the exhaust heat of (1) to the heat demand side and the fuel cell system temperature measuring instrument (2), the current density control means (3) outputs An exhaust gas temperature sensor (17) is connected between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). Is installed, and the heat recovery means (15) Receiving the input signals from the heat utilization means for utilizing the generated heat, the power demand (12), the current density control means (3), and the fuel cell system temperature measurement means (2), the fuel adjustment valve (5) Control means (8) for controlling the oxidant adjusting valve (7) is provided, and the control means (8) measures heat demand and power demand (S1), and if the ratio of heat demand is increased (S2). The fuel cell cogeneration system has a function of reducing the power generation output of the fuel cell (1) by restricting the current density control means (3) while keeping the fuel supply amount constant. High temperature operation type fuel cell (1), current density control means (3) for controlling the power generation output of the fuel cell (1), and fuel adjustment for controlling the amount of fuel supplied to the fuel cell (1) A fuel cell interposed between a valve (5), an oxidant adjusting valve (7) for controlling the amount of oxidant supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1). In the fuel cell cogeneration system including the heat recovery means (15) for supplying the exhaust heat of (1) to the heat demand side and the fuel cell system temperature measuring instrument (2), the current density control means (3) outputs An exhaust gas temperature sensor (17) is connected between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). Is installed, and the heat recovery means (15) Receiving the input signals from the heat utilization means for utilizing the generated heat, the power demand (12), the current density control means (3), and the fuel cell system temperature measurement means (2), the fuel adjustment valve (5) Control means (8) for controlling the oxidant adjusting valve (7) is provided, and the control means (8) measures heat demand and power demand (S11), and if the ratio of power demand is increased (S12). The fuel cell cogeneration system has a function of increasing the power generation output of the fuel cell (1) by opening the current density control means (3) while keeping the fuel supply amount constant. High temperature operation type fuel cell (1), current density control means (3) for controlling the power generation output of the fuel cell (1), and fuel adjustment for controlling the amount of fuel supplied to the fuel cell (1) A fuel cell interposed between a valve (5), an oxidant adjusting valve (7) for controlling the amount of oxidant supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1). In the fuel cell cogeneration system including the heat recovery means (15) for supplying the exhaust heat of (1) to the heat demand side and the fuel cell system temperature measuring instrument (2), the current density control means (3) is D / D converter (9) is connected to power demand (12) via an output power line (Le), and is connected between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). Between the exhaust gas temperature sensor (17) and the electric heater (19) is interposed, and the electric heater (19) is connected to the D / D converter (9) through a sub power line (Les) interposed with current control means (18), and the heat recovery means ( The fuel adjustment by receiving input signals from the heat utilization means utilizing the heat recovered in 15), the power demand (12), the current density control means (3), and the fuel cell system temperature measurement means (2) A control means (8) for controlling the valve (5) and the oxidant adjusting valve (7) and turning on and off the current control means (18) is provided, and the control means (8) measures heat demand and power demand ( S21) If there is a surplus in power demand (S22), it is determined whether the exhaust heat recovery amount is insufficient with respect to the heat demand (S23), and the exhaust heat recovery amount is insufficient with respect to the heat demand. If the current control means (18) is activated (S24), If the amount of recovered if exceeded heat demand (S26), the fuel cell cogeneration system characterized by having a function of turning off the current control means (18). High temperature operation type fuel cell (1), current density control means (3) for controlling the power generation output of the fuel cell (1), and fuel adjustment for controlling the amount of fuel supplied to the fuel cell (1) A fuel cell interposed between a valve (5), an oxidant adjusting valve (7) for controlling the amount of oxidant supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1). In the fuel cell cogeneration system including the heat recovery means (15) for supplying the exhaust heat of (1) to the heat demand side and the fuel cell system temperature measuring instrument (2), the current density control means (3) outputs An exhaust gas temperature sensor (17) is connected between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). Is installed, and the heat recovery means (15) Receiving the input signals from the heat utilization means for utilizing the generated heat, the power demand (12), the current density control means (3), and the fuel cell system temperature measurement means (2), the fuel adjustment valve (5) Control means (8) for controlling the oxidant adjusting valve (7) is provided, and the control means (8) measures heat demand and power demand (S31), and if the ratio of heat demand is increased (S32). The fuel cell cogeneration system has a function of increasing the fuel supply amount by opening the fuel adjustment valve (5) while keeping the current density and / or the fuel utilization rate constant. High temperature operation type fuel cell (1), current density control means (3) for controlling the power generation output of the fuel cell (1), and fuel adjustment for controlling the amount of fuel supplied to the fuel cell (1) A fuel cell interposed between a valve (5), an oxidant adjusting valve (7) for controlling the amount of oxidant supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1). In the fuel cell cogeneration system including the heat recovery means (15) for supplying the exhaust heat of (1) to the heat demand side and the fuel cell system temperature measuring instrument (2), the current density control means (3) outputs An exhaust gas temperature sensor (17) is connected between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). Is installed, and the heat recovery means (15) Receiving the input signals from the heat utilization means for utilizing the generated heat, the power demand (12), the current density control means (3), and the fuel cell system temperature measurement means (2), the fuel adjustment valve (5) Control means (8) for controlling the oxidant adjusting valve (7) is provided, and the control means (8) measures heat demand and power demand (S41), and if the ratio of power demand is reduced (S42). ), A fuel cell cogeneration system having a function of reducing the fuel supply amount by restricting the fuel adjustment valve (5) while keeping the current density and / or the fuel utilization rate constant if the power demand exceeds. High temperature operation type fuel cell (1), current density control means (3) for controlling the power generation output of the fuel cell (1), and fuel adjustment for controlling the amount of fuel supplied to the fuel cell (1) A fuel cell interposed between a valve (5), an oxidant adjusting valve (7) for controlling the amount of oxidant supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1). In the fuel cell cogeneration system including the heat recovery means (15) for supplying the exhaust heat of (1) to the heat demand side and the fuel cell system temperature measuring instrument (2), the current density control means (3) outputs An exhaust gas temperature sensor (17) is connected between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). Is installed, and the heat recovery means (15) Receiving the input signals from the heat utilization means for utilizing the generated heat, the power demand (12), the current density control means (3), and the fuel cell system temperature measurement means (2), the fuel adjustment valve (5) Control means (8) for controlling the oxidant adjusting valve (7) is provided, and the control means (8) measures heat demand and power demand (S51), and if the ratio of heat demand is increased (S52). The fuel cell (1) has a function of adjusting the current density control means (3) and reducing the current density and / or the fuel utilization rate within a range where oxidant withering does not occur in the fuel cell (1) while increasing the fuel supply amount. Fuel cell cogeneration system. High temperature operation type fuel cell (1), current density control means (3) for controlling the power generation output of the fuel cell (1), and fuel adjustment for controlling the amount of fuel supplied to the fuel cell (1) A fuel cell interposed between a valve (5), an oxidant adjusting valve (7) for controlling the amount of oxidant supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1). In the fuel cell cogeneration system comprising the heat recovery means (15) for supplying the exhaust heat of (1) to the heat demand side and the fuel cell system temperature measuring instrument (2), the current density control means 3) is the output power. An exhaust gas temperature sensor (17) is connected between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). Heat recovery by the heat recovery means (15) Receiving the input signals from the heat utilization means for utilizing the generated heat, the power demand (12), the generated power adjustment means (3), and the fuel cell system temperature measurement means (2), the fuel adjustment valve (5) Control means (8) for controlling the oxidant adjusting valve (7) is provided, and the control means (8) measures heat demand and power demand (S61), and if the ratio of power demand is reduced (S62). ), A function of increasing the current density and / or the fuel utilization rate by adjusting the current density control means (3) within a range in which fuel depletion does not occur in the fuel cell (1) while reducing the fuel supply amount. Fuel cell cogeneration system. High temperature operation type fuel cell (1), current density control means (3) for controlling the power generation output of the fuel cell (1), and fuel adjustment for controlling the amount of fuel supplied to the fuel cell (1) A fuel cell interposed between a valve (5), an oxidant adjusting valve (7) for controlling the amount of oxidant supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1). In the fuel cell cogeneration system including the heat recovery means (15) for supplying the exhaust heat of (1) to the heat demand side and the fuel cell system temperature measuring instrument (2), the current density control means (3) outputs An exhaust gas temperature sensor (17) is connected between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). Is installed in the off-gas combustion section (1a). Connected to an off-gas air supply line (21) having an agent valve (22) interposed therebetween, heat utilization means for utilizing the heat recovered by the heat recovery means (15), the power demand (12), and current In response to input signals from the density control means (3) and the fuel cell system temperature measurement means (2), the fuel adjustment valve (5), the oxidant adjustment valve (7), and the oxidant valve (22) are controlled. Control means (8) is provided, and the control means (8) determines whether the off-gas combustion state needs to be shifted to the lean side or the stoichiometric side (S72). If it is necessary to shift, the opening of the oxidizer valve (22) is increased (S73), and if it is necessary to shift to the stoichiometric side, the fuel has a function of reducing the opening of the oxidizer valve (22). Battery cogeneration system. High temperature operation type fuel cell (1), current density control means (3) for controlling the power generation output of the fuel cell (1), and fuel adjustment for controlling the amount of fuel supplied to the fuel cell (1) A fuel cell interposed between a valve (5), an oxidant adjusting valve (7) for controlling the amount of oxidant supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1). In the fuel cell cogeneration system including the heat recovery means (15) for supplying the exhaust heat of (1) to the heat demand side and the fuel cell system temperature measuring instrument (2), the current density control means (3) outputs An exhaust gas temperature sensor (17) is connected between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15). And the off-gas combustion part (1a) Connected to a fuel supply line (23) for an off-gas combustion section with a fuel valve (24) interposed therebetween, and a heat utilization means for utilizing the heat recovered by the heat recovery means (15) and the power demand (12) And the fuel adjustment valve (5), the oxidant adjustment valve (7), and the fuel valve (24) in response to input signals from the current density control means (3) and the fuel cell system temperature measurement means (2). A control means (8) for controlling is provided, and if the exhaust heat recovery amount is less than the heat demand (S81), the control means (8) opens the fuel valve (24) to supply fuel to the off-gas combustion section (1a). Supplying (S82), and after a predetermined time has passed (S83), if the amount of exhaust heat recovery exceeds the heat demand (S84), it has a function of stopping the supply of fuel to the off-gas combustion unit (1a). Characteristic fuel cell cogeneration System. High temperature operation type fuel cell (1), current density control means (3) for controlling the power generation output of the fuel cell (1), and fuel adjustment for controlling the amount of fuel supplied to the fuel cell (1) A fuel cell interposed between a valve (5), an oxidant adjusting valve (7) for controlling the amount of oxidant supplied to the fuel cell (1), and an exhaust system (Lh) of the fuel cell (1). In the fuel cell cogeneration system including the heat recovery means (15) for supplying the exhaust heat of (1) to the heat demand side and the fuel cell system temperature measuring instrument (2), the current density control means (3) outputs It is connected to the electric power demand (12) via the electric power line (Le), and the exhaust gas line (Lh) between the off-gas combustion part (1a) of the fuel cell (1) and the heat recovery means (15) Exhaust gas temperature sensor (17) and spark plug (25P) A refueling burner (25) having a fuel supply line (26) interposed between the refueling burner (25) and a fuel valve (27) is connected to the reheating burner (25). The fuel regulating valve (5) receives input signals from the heat utilization means utilizing the recovered heat, the power demand (12), the current density control means (3), and the fuel cell system temperature measuring means (2). And a control means (8) for controlling the oxidant adjusting valve (7), the fuel valve (27), and the spark plug (25P), and the control means (8) has an exhaust heat recovery amount less than the heat demand. If this is the case (S91), the fuel valve (27) is opened and fuel is supplied to the reheating burner (25) and ignited by the spark plug (25P) (S92). If it exceeds the heat demand (S94) The fuel cell cogeneration system, comprising a fuel supply to cut (S95) functions erase the fired burner (25) follow.

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