JP2010168242A - Hydrogen generator and fuel cell system including the same - Google Patents

Abstract

A cooling operation in a stop process of a hydrogen generator is not optimized so as to be executed according to a situation when the stop process is executed.
A hydrogen generator comprising a reformer 16, a combustor 102a, a combustion air supply device 117, a controller 110, and a stop operation device 120, wherein the combustion air supply device 117 is stopped. In the process, by supplying combustion air to the combustor 102a, the combustor 102a is cooled, and the controller 110 has a stop operation device 120 by the operator rather than the cooling amount of the hydrogen generator 102 in the normal stop processing. The hydrogen generator configured to control the combustion air supply 117 so that the cooling amount of the hydrogen generator 102 in the stop process by the input operation is larger.
[Selection] Figure 1

Description

  The present invention relates to a hydrogen generator and a fuel cell system including the same, and more particularly to an apparatus that performs a stop process when an abnormality of the hydrogen generator is detected.

  Conventionally, a fuel cell system capable of high-efficiency small-scale power generation is easy to build a system for using thermal energy generated during power generation. Development is progressing as a power generation system. In the fuel cell system, fuel gas (hydrogen gas) and oxidant gas are supplied from the outside to the fuel cell, and electric power is generated by an electrochemical reaction between the supplied fuel gas and oxidant gas, and is generated by the reaction. This system recovers heat and stores it as hot water in a hot water storage tank, and effectively uses this hot water to supply heat to the outside.

  In such a fuel cell system, the hydrogen gas used for power generation is not provided with a general infrastructure for its supply facilities. For example, a raw material obtained from existing infrastructure such as city gas and LPG is used as a reformer. Steam reforming reaction to produce hydrogen-containing reformed gas, carbon monoxide contained in the reformed gas is sufficiently reduced by a transformer and purifier, and hydrogen production to produce fuel gas In general, the apparatus is provided in the fuel cell.

By the way, in the stop process of the hydrogen generator, the hydrogen generator is sealed, and more air is supplied from the burner blower that supplies the combustion air to the burner for heating the reforming catalyst than during the operation of the fuel cell. A hydrogen generator that forcibly cools the reforming catalyst has been proposed (see, for example, Patent Document 1).
Similarly, in the shutdown process of the hydrogen generator, the supply of raw material gas and water vapor is continued, the cooling operation to advance the endothermic reaction of the reforming reaction, and the rotational speed of the combustion fan are increased compared to the normal operation, and the excess A hydrogen generation apparatus has been proposed in which both a cooling operation for air cooling with exhaust gas containing fresh air is performed, and the temperature is rapidly reduced to a temperature at which carbon does not precipitate even when a purge operation using only a raw material gas is performed (for example, patents). Reference 2).
Japanese Patent Laid-Open No. 2-132770 JP 2005-162580 A

  However, the cooling operation during the stop process such as the hydrogen generator disclosed in Patent Document 1 and Patent Document 2 is a case of stopping the hydrogen generator for maintenance work and a case of normal stop that does not require maintenance. It is not optimized for each situation.

  The present invention has been made in view of the above problems, and an object of the present invention is to provide a hydrogen generator in which the cooling operation of the hydrogen generator is executed in accordance with the situation when the stop process is executed.

  In order to solve the above conventional problems, a hydrogen generator according to the present invention includes a reformer that generates a hydrogen-containing gas by a reforming reaction using raw materials, a combustor that heats the reformer, A hydrogen generator comprising a combustion air supplier for supplying combustion air to a combustor, and a controller, comprising a stop operator for stopping the operation of the hydrogen generator by an input operation by an operator, The controller cools the hydrogen generator in a stop process (hereinafter referred to as a stop process by an input operation) by an input operation to the stop controller by an operator rather than a cooling amount of the hydrogen generator in a normal stop process. The combustion air supplier is controlled so that the amount is larger.

  As a result, when the operation of the hydrogen generator is stopped by the operator's input operation to the stop operation device, the cooling amount of the hydrogen generator increases compared to the normal stop process, so the temperature of the hydrogen generator is lowered. Is promoted, and the maintenance work can be started more quickly.

  Further, in the hydrogen generator according to the present invention, the controller is configured so that the cooling amount of the hydrogen generator in the stop process by the input operation is more than the cooling amount of the combustor in the case of performing the normal stop process. So that at least one of the operation time and the operation amount of the combustion air supply device may be controlled.

  In the hydrogen generator according to the present invention, the controller increases the operation amount of the combustion air supplier in the stop process by the input operation, more than the operation amount of the combustion air supplier in the normal stop process. It may be configured to increase the cooling amount of the hydrogen generation device by controlling so as to cause the hydrogen generation device to control.

  Moreover, in the hydrogen generator according to the present invention, the controller is configured such that the controller is more operative than the operation time of the combustion air supplier in the normal stop process, and the combustion air supplier in the stop process by the input operation. It may be configured to increase the amount of cooling of the combustor by controlling so as to increase the operation time.

  In the hydrogen generator according to the present invention, the controller may be configured such that the temperature of the hydrogen generator when the stop process is completed by the input operation is greater than the temperature of the hydrogen generator when the normal stop process is completed. The combustion air supply device may be controlled so as to be low.

  Further, in the hydrogen generator according to the present invention, the controller is configured so that the hydrogen generator has a higher temperature in the normal stop process than in the stop process by the input operation. You may be comprised so that the starting process of a production | generation apparatus may be permitted.

  Further, in the hydrogen generator according to the present invention, the controller uses the operation amount of the combustion air supplier in the stop process by the input operation, and the operation amount of the combustion air supplier during a rated operation of the hydrogen generator. The combustion air supply device may be controlled so as to be forcibly increased to a predetermined operation amount that is greater than a predetermined value.

  Furthermore, in the hydrogen generator according to the present invention, the hydrogen generator includes a sealer for making a gas flow path including the reformer a closed space, and the hydrogen generator is the closed space formed by the sealer. When the internal pressure decreases, the sealing device is opened to perform a supplementary pressure process for supplying gas into the gas flow path, and the controller is more effective than the normal stop process. The stop process by the input operation may be configured to increase the frequency of the pressure compensation process.

  The fuel cell system according to the present invention includes a hydrogen generator and a fuel cell that generates power using a hydrogen-containing gas supplied from the hydrogen generator.

  According to the hydrogen generator and the fuel cell system including the hydrogen generator according to the present invention, when maintenance work is required, an operator inputs the stop operation device to stop the operation of the hydrogen generator more quickly. In addition, maintenance work on the hydrogen generator can be started.

  Hereinafter, preferred embodiments of the present invention will be described with reference to the drawings. In all the drawings, the same or corresponding parts are denoted by the same reference numerals, and redundant description may be omitted.

(Embodiment 1)
[Configuration of hydrogen generator]
FIG. 1 is a schematic diagram showing a schematic configuration of a hydrogen generator according to Embodiment 1 of the present invention. In addition, in FIG. 1, the up-down direction in a hydrogen generator is represented as the up-down direction in a figure, and the one part is abbreviate | omitted.

  As shown in FIG. 1, the hydrogen generator 102 according to Embodiment 1 of the present invention includes a combustion air supply device 117, a raw material gas supply device (raw material supply device) 112, a water supply device 105, and an oxidizing air supply device 116. , A controller 110, a remote controller 120, a housing package 111, and detectors 140 to 145, and the user operates the remote controller 120 to start and stop the operation of the hydrogen generator 102. It is configured to be able to. Each device such as the hydrogen generator 102 is accommodated in the package 111. The abnormality determiner 110a constitutes an abnormality detector, and determines various abnormalities based on the detection value of each detector (for example, a temperature detector). However, the abnormality determiner 110a functions as an abnormality detector for the failure of each detector, and an abnormality different from the failure of the detector is a determination target when determining the abnormality with the abnormality determiner 110a. The detector that outputs the detection value functions as an abnormality detector. Moreover, in this Embodiment 1, the remote control 120 comprises a stop operating device. As an input operation for stopping operation using the remote controller 120, for example, a mode in which an operator presses a button for stopping operation provided on the remote controller 120, or for operating stop input by operating the remote controller 120. In this state, an operation stop confirmation input is performed by a button operation or a touch operation on the screen.

  Here, the hydrogen generator 102 is formed in a cylindrical shape, and includes a container 1, an outer cylinder 2, and an inner cylinder 3 that share a central axis. The container 1 is composed of a stepped cylinder in which a large diameter portion is formed at the upper portion and a small diameter portion having a smaller diameter than the large diameter portion is formed at the lower portion. The lower end of the container 1 is closed by a bottom plate 5, and the upper end thereof is connected to the outer cylinder 2 via an annular plate member 6. A heat insulating member 4 is provided outside the container 1 so as to cover the container 1.

  The upper ends of the outer cylinder 2 and the inner cylinder 3 are closed by a lid member 7. On the other hand, the lower end of the outer cylinder 2 is opened, and the lower end of the inner cylinder 3 is closed by an inner cylinder bottom plate 8. A cylindrical radiation tube 9 is provided inside the inner tube 3.

  The upper end of the radiation tube 9 is closed by the lid member 7, and the lower end thereof is opened. A cylindrical space formed between the radiation cylinder 9 and the inner cylinder 3 constitutes a combustion exhaust gas flow path 10. A combustion exhaust gas outlet 11 is provided in the vicinity of the downstream end of the combustion exhaust gas channel 10 (upper part of the inner cylinder 3). An upstream end of the combustion exhaust gas path 59 is connected to the combustion exhaust gas outlet 11, and the downstream end thereof is opened to the outside of the package 111.

  A burner (combustor) 102 a is disposed inside the radiation tube 9 so as to penetrate the lid member 7 and extend downward. Further, an ignition detector 141 and a CO sensor 142 are provided inside the radiation tube 9. The ignition detector 141 is configured to detect the presence or absence of ignition in the burner 102a and to output a detection signal to the controller 110. The CO sensor 142 is monoxide contained in the combustion exhaust gas from the burner 102a. It is configured to detect the concentration of carbon and output a detection signal to the controller 110. Here, a flame rod is used as the ignition detector 141, and a CO concentration sensor is used as the CO sensor 142.

  The burner 102 a is connected to the downstream end of the combustion air supply path 56, and the upstream end is connected to the combustion air supplier 117. As the combustion air supply device 117, for example, fans such as a blower or a sirocco fan can be used.

  The source gas introduced into the source gas supply port 12 from the source gas supply unit 112 passes through the inside of the hydrogen generator 102 and is supplied as combustion fuel to the burner 102a through the bypass path 44 that bypasses the hydrogen utilization device 101. Is done. Thereby, in the burner 102a, the combustion fuel supplied from the raw material gas supply device 112 is burned with the combustion air supplied from the combustion air supply device 117, and combustion exhaust gas is generated. The generated flue gas flows out from the tip (lower end) of the radiation tube 9, hits the bottom wall of the inner cylinder bottom plate 8, reverses, flows upward from there through the flue gas passage 10, and is supplied to the flue gas passage 59. The The flue gas supplied to the flue gas path 59 flows through the flue gas path 59 and is discharged out of the hydrogen generator 102 (more precisely, the package 111).

  A raw material gas supply port 12 is provided in the upper part of the outer cylinder 2, and the raw material gas supply port 12 is connected to the downstream end of the raw material gas supply path 41. Here, a city gas mainly composed of methane is used as the source gas, and the upstream end of the source gas supply path 41 is connected to a city gas pipe (not shown). The source gas supply path 41 is provided with a first on-off valve (sealing device) 71, a source gas supply device 112, and a second on-off valve (sealing device) 72 from the upstream side. The first on-off valve 71 and the second on-off valve 72 are configured to allow / block the flow of the raw material gas flowing through the raw material gas supply path 41. For example, a valve such as an electromagnetic valve may be used. it can. The raw material gas supply unit 112 is a device that adjusts the flow rate of the raw material gas supplied to the hydrogen generator 102, and includes, for example, a combination of a booster pump and a flow rate adjustment valve, or a single flow rate adjustment valve.

  A water supply port 13 is provided in the upper part of the outer cylinder 2, and the downstream end of the reforming water supply path 57 is connected to the water supply port 13. A water supplier 105 is connected to the upstream end of the reforming water supply path 57. The water supplier 105 supplies the reforming water to the reforming water supply path 57 and adjusts the flow rate of the reforming water flowing through the reforming water supply path 57.

  A lower part of the cylindrical space between the outer cylinder 2 and the inner cylinder 3 forms a reforming catalyst housing space, and a reforming catalyst layer 14 filled with the reforming catalyst is formed in the reforming catalyst housing space. Has been. A preheating unit 15 for preheating the raw material gas and the reforming water is formed above the reforming catalyst housing space. A reformer 16 is composed of the reforming catalyst housing space, the reforming catalyst layer 14, and the preheating unit 15. As a result, the reformer 16 utilizes the heat transfer of the combustion exhaust gas generated by the burner 102 a and the raw gas (methane) supplied from the raw gas supplier 112 and the reformer supplied from the water supplier 105. The quality water is preheated by the preheating unit 15, and the preheated raw material gas and the reforming water are subjected to a steam reforming reaction in the reforming catalyst layer 14, thereby generating a hydrogen-containing gas containing hydrogen.

  Further, a space is formed between the bottom plate 5 and the inner cylinder bottom plate 8, and the space constitutes the buffer space portion 17. A temperature detector 143 is disposed at the center of the bottom plate 5 of the buffer space 17.

  The temperature detector 143 is configured to detect the temperature of the hydrogen-containing gas that has passed through the reformer 16 and output the detected temperature to the controller 110 as the temperature of the reformer 16. In the present embodiment, the temperature detector 143 is provided below the downstream end of the reformer 16, and is configured to detect the temperature of the hydrogen-containing gas after flowing through the reformer 16. However, the present invention is not limited to this, and the temperature of the hydrogen-containing gas that is provided inside the reforming catalyst layer 14 of the reformer 16 and flows through the reforming catalyst layer 14 of the reformer 16 may be detected. Good.

  In addition, a cylindrical space 18 is formed between the container 1 and the outer cylinder 2 so as to communicate with the buffer space portion 17, and the space 18 and the buffer space portion 17 are connected to the hydrogen-containing gas channel 19. Configure. As a result, the hydrogen-containing gas flowing through the reformer 16 flows out from the downstream end of the reforming catalyst layer 14 to the buffer space portion 17, hits the bottom wall of the bottom plate 5, and reverses to pass through the hydrogen-containing gas flow path 19. Circulate.

  A pair of partition plates 20 and 21 are arranged in the cylindrical space between the large diameter portion of the container 1 and the outer cylinder 2 above the hydrogen-containing gas flow path 19 with a predetermined interval in the axial direction. The pair of partition plates 20 and 21 divide the cylindrical space into a shift catalyst containing space 22, an air mixing unit 25, and an oxidation catalyst containing space 26.

  A shift catalyst layer 23 filled with a shift catalyst is formed in the shift catalyst storage space 22, and a shift converter 24 is configured from the shift catalyst storage space 22 and the shift catalyst layer 23. Further, the partition plate 20 is provided with a plurality of through holes 29 so as to allow the transformer 24 and the air mixing unit 25 to communicate with each other, and the through holes 29 constitute an outlet 29 of the transformer 24. As a result, the hydrogen-containing gas flowing through the hydrogen-containing gas flow path 19 flows into the transformer 24. Then, while the hydrogen-containing gas flows through the shift catalyst layer 23, carbon monoxide and water in the hydrogen-containing gas are converted by the shift reaction, and carbon monoxide is reduced. The hydrogen-containing gas with reduced carbon monoxide flows out from the outlet 29 of the transformer 24 to the air mixing unit 25.

  The container 1 forming the air mixing unit 25 is provided with an air supply port 30 for supplying air for carbon monoxide oxidation reaction. The air supply port 30 is connected to a downstream end of an oxidation air supply path 58, and an oxidation air supply 116 is connected to the upstream end of the air supply port 30. Thereby, the hydrogen-containing gas flowing out from the outlet 29 of the transformer 24 to the air mixing unit 25 is mixed with the air supplied from the oxidizing air supply unit 116.

  A temperature detector 144 is provided above the outlet 29 of the transformer 24 in the air mixing unit 25. The temperature detector 144 is configured to detect the temperature of the hydrogen-containing gas that has passed through the transformer 24 and output the detected temperature to the controller 110 as the temperature of the transformer 24. In the present embodiment, the temperature detector 144 is provided above the outlet 29 of the transformer 24 and configured to detect the temperature of the hydrogen-containing gas after flowing through the transformer 24. However, the temperature of the hydrogen-containing gas flowing through the shift catalyst layer 23 of the shift converter 24 may be detected by being provided inside the shift catalyst layer 23 of the shift converter 24.

  An oxidation catalyst layer 27 filled with an oxidation catalyst is formed in the oxidation catalyst housing space 26, and a purifier 28 is constituted by the oxidation catalyst housing space 26 and the oxidation catalyst layer 27. Further, the partition plate 21 is provided with a plurality of through holes 31 so as to communicate the air mixing unit 25 and the purifier 28, and the through holes 31 constitute the inlet 31 of the purifier 28. Further, a temperature detector 145 is provided below the inlet 31 of the purifier 28 in the air mixing unit 25. The temperature detector 145 is configured to detect the temperature of the mixed gas of hydrogen-containing gas and air flowing into the purifier 28 and output the detected temperature to the controller 110 as the temperature of the purifier 28. In the present embodiment, the temperature detector 145 is provided below the inlet 31 of the purifier 28 so as to detect the temperature of the fuel gas before flowing through the purifier 28. The present invention is not limited, and the temperature of the fuel gas that is provided inside the oxidation catalyst layer 27 of the purifier 28 and flows through the oxidation catalyst layer 27 of the purifier 28 may be detected.

  Further, a fuel gas outlet 32 is provided at the upper part of the container 1 constituting the oxidation catalyst housing space 26. An upstream end of the fuel gas supply path 42 is connected to the fuel gas outlet 32, and a hydrogen utilization device (for example, a fuel cell) 101 is connected to the downstream end of the fuel gas outlet 32. A fuel gas valve (sealing device) 79 is provided in the middle of the fuel gas supply path 42, and the upstream end of the bypass path 44 is connected to the upstream side thereof. The downstream end of the bypass path 44 is connected to the burner 102a. A bypass valve (sealing device) 80 is provided in the middle of the bypass path 44.

  Thus, the hydrogen-containing gas mixed with air in the air mixing unit 25 flows into the purifier 28 from the through hole 31 (the inlet 31 of the purifier 28) of the partition plate 21 and flows through the oxidation catalyst layer 27. In the meantime, carbon monoxide in the hydrogen-containing gas and oxygen in the air react to produce a fuel gas in which carbon monoxide is reduced to several ppm. The generated fuel gas flows from the fuel gas outlet 32 through the fuel gas supply path 42 and is supplied to the hydrogen utilization device 101.

  In the hydrogen generator 102 of the present embodiment, the configuration in which the transformer 24 and the purifier 28 are provided is adopted, but the carbon monoxide contained in the hydrogen-containing gas generated by the reformer 16 is further reduced. If it is not necessary to do so, a configuration in which the transformer 24 and the purifier 28 are not provided may be employed. For example, when the hydrogen using device 101 is a device that is not easily poisoned with respect to carbon monoxide (for example, a solid oxide fuel cell), the above configuration is adopted.

  An intake port 61 and an exhaust port 62 are provided at appropriate positions of the package 111. The intake port 61 and the exhaust port 62 are preferably provided as far as possible from each other so that the outside air can flow through the package 111. The exhaust port 62 is provided in the package 111 where flammable gas tends to stay. It is preferable to be provided in the upper part. A ventilation fan 119 is disposed in the vicinity of the exhaust port 62. The ventilation fan 119 can be a fan such as a sirocco fan.

  Thereby, the ventilation fan 119 sucks outside air from the intake port 61 and the sucked outside air is discharged from the exhaust port 62.

  A flammable gas sensor 140 is provided in the package 111. The combustible gas sensor 140 is configured to detect leakage (concentration) of combustible gas (for example, raw material gas or hydrogen gas) in the package 111 and output the detected concentration of combustible gas to the controller 110. ing. In the present embodiment, the combustible gas sensor 140 is provided in the vicinity of the ventilation fan 119 in the upper part of the package 111 where the combustible gas tends to stay.

  Further, a controller 110 is provided in the package 111. The controller 110 is configured by a computer such as a microcomputer, and includes an arithmetic processing unit including a CPU, a storage unit including a memory, a communication unit, and a clock unit having a calendar function (all of which are not shown). ) The arithmetic processing unit reads out a predetermined control program stored in the storage unit and executes it to perform various controls relating to the hydrogen generator 102. The arithmetic processing unit processes data stored in the storage unit and data input from the operation input unit, and in particular, an abnormality determination program read from the storage unit and detection values input from the detectors 140 to 145. If the abnormality determined to be abnormal belongs to the first abnormality or the second abnormality, the corresponding hydrogen generation apparatus 102 is stopped.

  Here, in this specification, the controller means not only a single controller but also a controller group in which a plurality of controllers cooperate to execute control of the hydrogen generator 102. For this reason, the controller 110 does not need to be composed of a single controller, and a plurality of controllers may be arranged in a distributed manner so that they cooperate to control the hydrogen generator 102. .

  In the present embodiment, the controller 110 is configured to determine whether or not the detection values input from the detectors 140 to 145 are abnormal. However, the present invention is not limited to this. 140-145 is good also as a structure which determines whether the physical quantity which each detects is abnormal by providing calculators, such as a microcomputer.

  The remote controller 120 includes a control unit (not shown) configured by a microcomputer, a communication unit (not shown), a display unit 120a, and a key operation unit 120b. The control unit controls the communication unit and the like. I have control. In addition, the remote controller 120 receives a control signal by the communication unit, and the control unit processes this and transmits it to the display unit 120a. In addition, an operation signal input from the key operation unit 120 b of the remote control 120 is transmitted to the controller 110 via the control unit and communication unit of the remote control 120 and received by the communication unit of the controller 110. When the operation is forcibly stopped to perform maintenance and inspection of the hydrogen generator 102, the user of the hydrogen generator 102 or a maintenance operator (operator) uses the remote controller 120 to stop the operation. By performing this input operation (stop command input), the controller 110 forcibly stops the operating hydrogen generator 102. The term “in operation” as used herein includes at least one of the startup process, the hydrogen supply operation, and the stop process of the hydrogen generator 102. The stop process (hereinafter referred to as forced stop process) of the hydrogen generator 102 when the stop input operation is performed with the remote controller 120 will be described later.

  In the following description, in order to simplify the description, the exchange of signals between the controller 110 and the remote controller 120 is described by omitting communication by both communication units and processing of the control unit in the remote controller 120.

[Operation of hydrogen generator]
Next, the startup process (startup operation) of the hydrogen generator 102 according to Embodiment 1 will be described with reference to FIG. The following operation is performed by the controller 110 controlling the hydrogen generator 102 when the user operates the remote controller 120.

  First, the first on-off valve 71 and the second on-off valve 72 are opened, and then the source gas supply unit 112 is operated so that the source gas is burned via the hydrogen generator 102 and the bypass path 44. 102a. Further, the combustion air is supplied from the combustion air supplier 117 via the combustion air supply path 56. In the burner 102a, the supplied source gas is combusted with combustion air, and combustion exhaust gas is produced | generated. At this time, the ignition detector 141 detects the presence or absence of ignition in the burner 102a and outputs a detection signal to the controller 110. In addition, the CO sensor 142 detects the concentration of carbon monoxide contained in the combustion exhaust gas from the burner 102 a and outputs the detected concentration of carbon monoxide to the controller 110.

  And it flows out from the front-end | tip (lower end) of the radiation cylinder 9 with the burner 102a, hits the bottom wall of the bottom plate 8 for inner cylinders, inverts, flows from there through the combustion exhaust gas flow path 10, and is supplied to the combustion exhaust gas path 59. The flue gas supplied to the flue gas path 59 flows through the flue gas path 59 and is discharged out of the hydrogen generator 102 (more precisely, the package 111). At this time, the reformer 16, the transformer 24, and the purifier 28 of the hydrogen generator 102 are heated by heat transfer from the combustion combustion exhaust gas.

  Then, based on the temperature detected by the temperature detector 143, when the controller 110 determines that the temperature of the preheating unit 15 has reached a temperature at which water can be evaporated (for example, 120 ° C.), the second opening / closing valve 72 is opened. At the same time, the operation of the water supply unit 105 is started, and the source gas is supplied from the source gas supply unit 112 to the preheating unit 15 of the reformer 16 of the hydrogen generator 102 via the source gas supply path 41. Reforming water is supplied from the water supply device 105 via the reforming water supply path 57. Then, the supplied water is heated in the preheating portion to become steam, and the steam and the raw material gas undergo a steam reforming reaction while flowing through the reforming catalyst layer 14 together with the heated raw material gas, thereby generating hydrogen. A hydrogen-containing gas is produced.

  Next, the hydrogen-containing gas generated by the reformer 16 flows out from the downstream end of the reforming catalyst layer 14 and flows through the hydrogen-containing gas channel 19. The hydrogen-containing gas that has flowed through the hydrogen-containing gas flow path 19 flows into the shifter 24, and while flowing through the shift catalyst layer 23, carbon monoxide and water in the hydrogen-containing gas are converted by the shift reaction. Carbon oxide is reduced. The hydrogen-containing gas with reduced carbon monoxide flows out from the outlet 29 of the transformer 24 to the air mixing unit 25. At this time, the temperature detector 144 detects the temperature of the hydrogen-containing gas flowing out from the outlet 29 of the transformer 24 and outputs the detected temperature to the controller 110.

  Next, the hydrogen-containing gas flowing out from the outlet 29 of the transformer 24 to the air mixing unit 25 is mixed with the air supplied from the oxidizing air supply unit 116. The hydrogen-containing gas mixed with air in the air mixing unit 25 flows into the purifier 28 from the inlet 31 of the purifier 28. At this time, the temperature detector 145 detects the temperature of the mixed gas of hydrogen-containing gas and air that flows into the purifier 28 and outputs the detected temperature to the controller 110.

  Next, while the mixed gas of hydrogen-containing gas and air flowing into the purifier 28 flows through the oxidation catalyst layer 27, carbon monoxide in the hydrogen-containing gas reacts with oxygen in the air, Fuel gas in which carbon monoxide is reduced to several ppm is generated. The generated fuel gas is supplied from the fuel gas outlet 32 to the fuel gas supply path 42.

  The temperature detectors 143 to 145 provided in the reformer 16, the transformer 24, and the purifier 28 of the hydrogen generator 102 have predetermined temperatures (for example, the reformer 16 has a temperature of 600 to 650 ° C., the transformer). 24 is 200 to 250 ° C. and the purifier 28 is 130 to 170 ° C.), the controller 110 determines that the carbon monoxide in the fuel gas has been sufficiently reduced, and the controller 110 generates hydrogen. The activation process of the device 102 is terminated.

  Next, the hydrogen supply operation (operation operation) of the hydrogen generator 102 according to Embodiment 1 will be described.

  First, the controller 110 opens the fuel gas valve 79 when the temperature detectors 143 to 145 provided in the reformer 16, the transformer 24, and the purifier 28 of the hydrogen generator 102 reach a predetermined temperature. Then, the fuel gas is supplied from the hydrogen generator 102 to the hydrogen using device 101. Note that while the carbon monoxide in the fuel gas is not sufficiently reduced, the fuel gas valve 79 is closed, and the fuel gas generated by the hydrogen generator 102 is not supplied to the hydrogen utilization device 101 and bypassed. It is supplied to the burner 102 a via the path 44. In addition, while the gas produced | generated by the hydrogen production | generation apparatus 102 as mentioned above is not supplied to the hydrogen utilization apparatus 101, but is supplied to the burner 102a via the bypass path 44, it is bypassed by control of the controller 110. Valve 80 is open. When carbon monoxide in the fuel gas is sufficiently reduced and the fuel gas is supplied to the hydrogen utilization device 101, the fuel gas valve 79 and the bypass valve 80 are also opened under the control of the controller 110, The combustion of the fuel gas introduced into the burner 102a through the bypass path 44 maintains the temperature of the hydrogen generator 102 at an appropriate temperature for generating a high-quality hydrogen-containing gas having a low carbon monoxide concentration.

  Next, normal stop processing (stop operation) of the hydrogen generator 102 according to Embodiment 1 will be described. The normal stop process here is different from the stop process (abnormal stop process) or the forced stop process that is executed when an abnormality is detected by the abnormality detector during the operation of the hydrogen generator 102. Refers to processing. For example, this is a stop process executed when it is no longer necessary to use hydrogen in the hydrogen-using device 101. Specifically, when the hydrogen-using device is a hydrogen tank, the hydrogen generator 102 is connected to the hydrogen tank. An example is a stop process that is executed when the capacity of the hydrogen tank becomes full during the hydrogen supply operation. In addition, when the hydrogen using device is a fuel cell, a stop process executed in advance when the power demand of the power load drops below a predetermined threshold that does not require the power generation operation of the fuel cell or preset For example, a stop process that is executed at the stop time that has been executed is given.

  In the present invention, the stop process (stop operation) is defined as an operation from when the controller 110 outputs a stop signal until the fuel cell system 100 completes the stop process. It should be noted that after the normal stop process of the hydrogen generator 102 is completed, the controller 110 is operating, and the operation of parts other than the controller 110 is stopped. An activation command is output by 110, and the process shifts to a standby state where the activation process can be started promptly.

  Hereinafter, a normal stop process (stop operation) of the hydrogen generator 102 according to Embodiment 1 will be described with reference to FIG. FIG. 2 is a flowchart showing an example of normal stop processing in the hydrogen generator 102 according to Embodiment 1 of the present invention.

  First, when a stop command is output by the controller 110, the operation of the booster pump as the raw material gas supply unit 112 is stopped, and the water supply unit 105 stops its operation. Further, the oxidizing air supply 116 stops its operation. Thereby, the supply of the source gas and water to the hydrogen generator 102 is stopped, and the supply of the oxidizing air to the air mixing unit 25 is stopped. Then, the first on-off valve 71 and the second on-off valve 72 provided on the source gas supply path 41 are closed, the fuel gas valve 79 and the bypass valve 80 are closed (step S101), and the inside of the hydrogen generator 102 is inside. Shut off from outside air (sealing operation of hydrogen generator).

  As a result, the combustion of the burner 102a continues until the bypass valve 80 is closed in step S101, but when the bypass valve 80 is closed in step S101 and the supply of fuel gas to the burner 102a is stopped, the burner 102a is burned. In 102a, combustion of fuel gas and combustion air stops.

  Note that the combustion air supplier 117 continues to supply the combustion air to the burner 102a even after the combustion in the burner 102a is stopped. As a result, the combustion air supplied to the burner 102a removes heat from the burner 102a and the reformer 16 while passing through the internal space of the radiant tube 9, the combustion exhaust gas passage 10 and the like, and the burner 102a and the reformer 16 are reformed. The apparatus 16 or the like, that is, the entire hydrogen generator 102 is cooled (cooling operation of the hydrogen generator 102).

  During the cooling operation, the temperature detector 143 provided in the reformer 16 of the hydrogen generator 102 detects the temperature t1 of the reformer 16 (step S102), and the detected temperature t1 is on standby. When the temperature is equal to or lower than the possible temperature (for example, 500 ° C.) (Yes in Step S103), the combustion air supplier 117 stops the supply of the combustion air to the burner 102a (Step S104), and performs the cooling operation of the hydrogen generator 102. Complete. Note that the standby temperature is a temperature at which the hydrogen generator 102 can enter a standby state, and is defined as an upper limit temperature at which carbon deposition does not occur even when only the raw material gas is supplied to the hydrogen generator 102, for example. .

  When the cooling operation of the hydrogen generator 102 to the standby temperature is completed, the hydrogen generator 102 shifts to a standby state (step S105). The standby state is a state where the next hydrogen generator 102 is awaiting the start of operation. For example, when a predetermined activation request is generated, an activation command is output from the controller 110, and It is defined as a state that shifts to execution of the next startup process. Examples of the activation request include, for example, that the user operates the key operation unit 120b of the remote controller 120 to make an operation start request, or that the hydrogen using device 101 needs to use hydrogen. . For this reason, when the startup process is output from the controller 110 when the hydrogen generator 102 is in the standby state, the startup process of the hydrogen generator 102 is performed.

  In the standby state, the hydrogen generator 102 is naturally allowed to cool. At this time, the temperature detector 143 provided in the reformer 16 of the hydrogen generator 102 detects the temperature of the reformer 16 (step). S106), when the detected temperature is equal to or lower than the FP purge temperature (eg, 300 ° C.) lower than the standby temperature (Yes in Step S107), the first on-off valve 71, the second on-off valve 72, and the bypass valve 80 Open the respective valves, the raw material gas (purge gas) is supplied from the raw material gas supplier 112 to the hydrogen generator 102 (step S108), and the reactor (reformer 16 and the like) provided in the hydrogen generator 102 The gas such as water vapor is purged by the source gas and scavenged from the hydrogen generator 102 (the purge process for the hydrogen generator 102 (hereinafter referred to as FP (Fu)). l Processor) purge process start)). The scavenged gas is sent to the burner 102a through the bypass path 44 and burned in the burner 102a (step S109). By this FP purge process, it is possible to suppress the condensation of water vapor in the hydrogen generator 102 and the deterioration of the catalyst such as the reforming catalyst. Note that, even if the temperature rise of the reformer 16 due to the combustion operation in the burner 102a during the purge process for the hydrogen generator 102 is added to the purge temperature, the raw material gas in the reformer 16 does not carbon deposit. Defined as temperature.

  Then, the controller 110 measures an elapsed time T1 from the start of the FP purge process (step S110), and when the elapsed time T1 becomes equal to or longer than the FP purge time J1 (Yes in step S111), the source gas is supplied. The vessel 112 is stopped, the first on-off valve 71, the second on-off valve 72, and the bypass valve 80 are closed (FP purge process is completed) (step S112), and the normal stop process is ended. The purge time is defined as the time necessary for at least the water vapor in the hydrogen generator 102 to be scavenged.

  As described above, in the hydrogen generator 102 according to the first embodiment, when the operation is stopped in a normal state, a stop process (for example, a hydrogen generator) that protects at least the function of the hydrogen generator 102 is provided. (Sealing operation for shutting off 102 from the outside air) is executed, and the apparatus is promptly shifted to a standby state. Even when the cooling operation is performed, the exhaust heat recovery operation is performed only until the temperature of the hydrogen generator 102 can be restarted (that is, until the temperature of the reformer 16 is equal to or lower than the standby temperature). It is configured to perform the minimum necessary cooling operation such as. Therefore, it is possible to quickly shift to the standby state, and the next start-up process depends on the elapsed time since the shift to the standby state, and the equipment temperature (for example, the reformer 16) constituting the hydrogen generator 102 changes to the ambient temperature ( The temperature required to raise the temperature of the hydrogen generator 102 is reduced, the time required for the startup process is shortened, and the startup performance of the hydrogen generator 102 is improved.

  In addition, in the stop process of the hydrogen generator 102 according to the first embodiment, the cooling operation of the hydrogen generator 102 is configured to be performed, but it is appropriate to shift the hydrogen generator 102 to the standby state. The stop operation is not limited to this, and the cooling operation may not be performed. For example, the hydrogen generator 102 is provided with a combustion fuel supply path that branches from the source gas supply path 41 and supplies the source gas directly as combustion fuel to the burner 102a. The burner 102a may be configured to burn using the combustion fuel via the combustion fuel supply path. In the startup process of the hydrogen generator 102 configured as described above, it is not necessary to allow only the raw material gas to flow through the hydrogen generator 102 in the temperature raising process of the hydrogen generator 102, so the above cooling operation is executed. There is no need.

  Next, the forced stop process of the hydrogen generator 102 according to Embodiment 1 will be described with reference to FIG. FIG. 3 is a flowchart showing the main operation of the forced stop process in the hydrogen generator 102 according to Embodiment 1 of the present invention.

  When a user of the hydrogen generator 102 or a maintenance operator (operator) operates the remote controller 120 and a stop command signal is input to the controller 110, as shown in FIG. In addition, the supply of the source gas and water to the hydrogen generator 102 is stopped and the sealing operation of the hydrogen generator 102 is executed (see steps S100 and S101 in FIG. 2), so that the combustion operation in the burner 102a is stopped. (Step S200).

  The combustion air supply device 117 continues the supply of the combustion air to the burner 102a even after the combustion in the burner 102a is stopped by the control of the controller 110, and executes the cooling operation of the hydrogen generator 102 (step S201). ). In the cooling operation, unlike the normal stop process, the temperature detected by the temperature detector 143 provided in the reformer 16 of the hydrogen generator 102 becomes equal to or lower than the standby temperature (for example, 500 ° C.). Is also continued (steps S202 to S204).

  Then, when the temperature detected by the temperature detector 143 becomes equal to or lower than the purge temperature while the cooling operation of the hydrogen generator 102 is continued, the FP purge process is executed as in the case of the normal stop process (steps S205 to S210). When the FP purge process is completed, the combustion air supplier 117 is stopped (step S211), and the FP cooling operation is completed. Then, the forced stop process is completed, and the controller 110 shifts the hydrogen generator 102 to a start-up disapproval state (step S212). Here, the transition to the start disapproval state means that even if the user operates the remote controller 120 and inputs a start command so as to start the operation of the hydrogen generator 102, the arithmetic processing unit of the controller 110 This means that the above-described hydrogen generator 102 is not permitted to be activated, and the activation command is not output.

  In the cooling operation of the hydrogen generator 102 in the forced stop process, it is preferable to control the amount of combustion air supplied to the burner 102a to be larger than the supply amount during the rated operation of the hydrogen generator 102. Specifically, in the cooling operation of the hydrogen generator 102 in the forced stop process, the controller 110 controls the combustion air supplier 117 so as to be larger than the operation amount during the rated operation of the hydrogen generator 102. Thereby, the temperature of the hydrogen generator 102 decreases more quickly, and it becomes easy to shift to the maintenance work. The rated operation of the hydrogen generator 102 is defined as an operation that supplies the maximum amount of hydrogen that can be stably supplied during the hydrogen supply operation of the hydrogen generator 102.

  Here, when the forced stop process is compared with the normal stop process, in the forced stop process, the temperature of the reformer 16 becomes a temperature at which the FP purge process can be performed after the temperature of the reformer 16 becomes equal to or lower than the standby temperature. Instead of waiting for the hydrogen generator 102 to cool by natural cooling as in a normal stop process, the burner 102a by the combustion air supplier 117 is included in the period until it reaches (the temperature below the FP purge temperature). The difference is that the cooling operation of the hydrogen generator 102 is continued and the hydrogen generator 102 is controlled to cool more quickly.

  In other words, in the hydrogen generator 102 according to the first embodiment, the forced stop process is controlled so that the cooling amount of the hydrogen generator 102 is increased as compared with the normal stop process. The temperature of the device in the apparatus 102 can be lowered more quickly to such an extent that the maintenance worker does not burn or the like, and the shift to the maintenance work can be speeded up.

  On the other hand, the normal stop process is controlled so that the cooling amount of the hydrogen generator 102 is reduced as compared with the forced stop process. Therefore, depending on the elapsed time after shifting to the standby state, The equipment temperature (for example, the reformer 16) constituting the hydrogen generator 102 is higher than the ambient temperature (outside air temperature), and the energy required to raise the temperature of the hydrogen generator 102 is reduced. Startability may be improved.

  In the first embodiment, the forced stop process is controlled so as to increase the cooling operation time of the hydrogen generator 102 by the combustion air supply device 117 as compared with the normal stop process. Although the control is performed so that the cooling amount of the hydrogen generator 102 is increased, the present invention is not limited to this, and the cooling amount of the hydrogen generator 102 is increased by controlling the amount of combustion air supplied to the burner 102a to be increased. You may control so. Specifically, the operation amount of the combustion air supplier 117 during the cooling operation of the hydrogen generator 102 during the forced stop process is larger than the operation amount during the cooling operation of the hydrogen generator 102 during the normal stop process. This is realized by the controller 110 controlling the combustion air supplier 117.

  In the first embodiment, the remote controller 120 constitutes a stop operation device. However, the present invention is not limited to this, and a stop operation for forcibly stopping the operation of the hydrogen generator 102 is performed separately from the remote controller 120. A vessel may be provided.

(Embodiment 2)
FIG. 4 is a schematic diagram showing a schematic configuration of the hydrogen generator according to Embodiment 2 of the present invention. In FIG. 4, the vertical direction in the hydrogen generator is shown as the vertical direction in the drawing, and a part thereof is omitted.

  As shown in FIG. 4, the hydrogen generator 102 according to Embodiment 2 of the present invention has the same basic configuration as the hydrogen generator 102 according to Embodiment 1, but is cooled in the middle of the combustion exhaust gas path 59. The difference is that the device 121 is provided.

  As the cooler 121, a heat exchanger, a radiator, or the like can be used. For example, when a heat exchanger is used as the cooler 121, the primary flow path of the heat exchanger and the combustion exhaust gas path 59 are connected, and water is passed through the secondary flow path of the heat exchanger. The combustion exhaust gas discharged from the burner 102a is cooled by exchanging heat with the water flowing through the secondary flow path of the heat exchanger while flowing through the primary flow path of the heat exchanger. Constitute. Then, in the stop process of the hydrogen generator 102, the controller 110 performs the heat exchanger 2 during the cooling operation period of the hydrogen generator 102 in which the burner 102 a stops burning and the combustion air supplier 117 is operating. Control to allow water to flow through the next channel. Thereby, it is possible to suppress the temperature of the exhaust air that is heat recovered from the hydrogen generator 102 and discharged to the outside of the hydrogen generator 102 (outside of the package 111) via the combustion exhaust gas path 59 from being excessively increased. . In the hydrogen generator 102 according to the second embodiment, carbon monoxide contained in the hydrogen-containing gas generated by the reformer 16 is further reduced in the same manner as the hydrogen generator 102 according to the first embodiment. When it is not necessary to reduce, you may employ | adopt the form which does not provide the transformer 24 and the purifier 28. FIG.

  Note that the cooling operation period of the hydrogen generator 102 by the combustion air supply device 117 when the combustion of the burner 102a is stopped is, in the case of the hydrogen generator 102 according to the second embodiment, the burner 102a in the normal stop process. In the cooling operation period in which the combustion air supply device 117 is operated until the temperature of the reformer 16 becomes equal to or lower than the standby temperature after the combustion is stopped, or in the forced stop processing, the combustion air supply device 117 is reformed after the combustion of the burner 102a is stopped. This refers to the cooling operation period in which the operation is performed until the temperature of the vessel 16 becomes the purge temperature or less.

  In addition, the hydrogen generator 102 is controlled so that the amount of cooling during the forced stop process is larger than that during the normal stop process. At this time, the burner 102a during the cooling operation period of the hydrogen generator 102 is controlled. When the amount of combustion air supplied (the amount of operation of the combustion air supply device 117) is controlled to be larger than that during normal stop processing, the amount of heat recovered by the air flowing through the combustion exhaust gas flow channel 102 increases. For this reason, the controller 110 can control to increase the flow rate of the water flowing through the secondary flow path of the heat exchanger when the forced stop process is performed rather than the normal stop process. preferable. That is, the controller 110 causes the cooling amount of the exhaust air by the cooler 121 when performing the forced stop process to be larger than the cooling amount of the exhaust air by the cooler 121 when performing the normal stop process. It is preferable to control the cooler 121.

  Even the hydrogen generator 102 according to the second embodiment configured as described above has the same effects as the hydrogen generator 102 according to the first embodiment. Further, in the hydrogen generator 102 according to the second embodiment, it is possible to suppress the temperature of the exhaust air discharged from the combustion exhaust gas path 59 from being excessively increased during the cooling operation period of the hydrogen generator 102. Therefore, the hydrogen generator 102 can be stopped more safely.

(Embodiment 3)
The fuel cell system according to Embodiment 3 of the present invention includes the hydrogen generator 102 according to Embodiment 1. Hereinafter, the fuel cell system according to Embodiment 3 will be described in detail.

[Configuration of fuel cell system]
FIG. 5 is a schematic diagram showing a schematic configuration of a fuel cell system according to Embodiment 3 of the present invention. In FIG. 5, the vertical direction in the fuel cell system is represented as the vertical direction in the figure.

  As shown in FIG. 5, a fuel cell system 100 according to Embodiment 3 of the present invention includes a fuel cell 101, a hydrogen generator 102, an oxidant gas supply device 103, a cooling water tank 104, a condensed water tank 105, heat exchange. A heat sink (heat radiator) 106, a first pump (first transmitter) 107, a second pump (second transmitter) 108, a hot water storage tank 109, a controller 110, a remote controller 120, and a package 111 comprising a housing. The fuel cell system 100 can be started and stopped when the user operates the remote controller 120. In the present embodiment, the package 111 is formed so as to extend in the vertical direction, and each device such as the fuel cell 101 is disposed inside the package 111.

  In the third embodiment, remote controller 120 constitutes a stop operating device. As an input operation for stopping operation using the remote controller 120, for example, a mode in which an operator presses a button for stopping operation provided on the remote controller 120, or for operating stop input by operating the remote controller 120. In this state, an operation stop confirmation input is performed by a button operation or a touch operation on the screen.

  The hydrogen generator 102 includes a reformer 16, a transformer 24, a purifier 28 (see FIG. 1), and a burner 102a, and the raw material gas supply port 12 (see FIG. 1) of the reformer 16 of the hydrogen generator 102. 1) is connected to the downstream end of the source gas supply path 41. Here, a city gas mainly composed of methane is used as the source gas, and the upstream end of the source gas supply path 41 is connected to a city gas pipe (not shown). The source gas supply path 41 is provided with a first on-off valve 71, a booster pump 112a, a flow rate adjustment valve 112b, and a second on-off valve 72 from the upstream side. The first on-off valve 71 and the second on-off valve 72 are configured to allow / block the flow of the raw material gas flowing through the raw material gas supply path 41. For example, a valve such as an electromagnetic valve may be used. it can. The booster pump 112a is configured to increase the pressure of the source gas flowing through the source gas supply path 41, and the flow rate adjustment valve 112b is configured to adjust the flow rate of the source gas flowing through the source gas supply path 41. In addition, the booster pump 112a and the flow rate adjustment valve 112b constitute the raw material gas supplier 112. Here, the booster pump 112a and the flow rate adjusting valve 112b constitute the raw material gas supply unit 112, but the present invention is not limited to this, and the raw material gas supply unit 112 may be configured only by the booster pump 112a. That is, the booster pump 112a may be configured to increase the pressure of the source gas and adjust the flow rate.

  The burner 102a is connected to the downstream end of the off-fuel gas path 43 so that excess fuel gas not used in the fuel cell 101 is supplied to the burner 102a as off-fuel gas. Also, the downstream end of the cathode purge gas discharge path 50 is connected to the burner 102a, and the scavenged oxidation gas is obtained by the cathode purge process of the fuel cell 101 that is performed when the fuel cell system 100 described later is started or stopped. A gas (hereinafter referred to as cathode purge gas) present in the agent gas flow path 101b is supplied to the burner 102a. Furthermore, the downstream end of the combustion air supply path 56 is connected to the burner 102a, and the combustion air supply device 117 is connected to the upstream end.

  As a result, the burner 102a is supplied with the raw material gas supplied through a flow path (not shown) (or the off-fuel gas supplied from the fuel cell 101 via the off-fuel gas path 43, or the cathode purge gas discharge path 50 from the fuel cell 101). The cathode purge gas supplied via the combustion air is burned by the combustion air supplied from the combustion air supply device 117 via the combustion air supply path 56. As the combustion air supply device 117, for example, fans such as a blower or a sirocco fan can be used.

  Further, the downstream end of the reforming water supply path 57 is connected to the water supply port 13 (see FIG. 1) of the reformer 16 of the hydrogen generator 102, and the upstream end thereof is connected to the second condensed water tank 105B. Connected to the bottom of the. Further, a third pump 113 that adjusts the flow rate of the reforming water (condensed water) that flows through the reforming water supply path 57 is provided in the middle of the reforming water supply path 57. In the present embodiment, the condensate is supplied directly from the second condensate tank 105B to the reformer 16 of the hydrogen generator 102. However, the present invention is not limited to this, and the first condensate tank 105A is not limited thereto. The condensate stored in the second condensate tank 105 </ b> B may be supplied to the cooling water tank 104 and stored in the cooling water tank 104. It is good also as a structure supplied to the reformer of the hydrogen production | generation apparatus 102 with the cooling water.

  Further, the upstream end of the oxidizing air supply path 58 is connected to the purifier 28 of the hydrogen generator 102, and the downstream end thereof is connected to the oxidizing air supply 116. The oxidizing air supply unit 116 is configured to supply air used for the oxidation reaction in the purifier. For example, fans such as a blower and a sirocco fan can be used as the oxidizing air supply 116.

  The reformer 16 utilizes the heat transfer of the combustion exhaust gas generated by the burner 102a, the source gas (methane) supplied from the source gas supply unit 112 via the source gas supply path 41, and the first By performing a reforming reaction with the condensed water supplied from the condensed water tank 105A, a hydrogen-rich hydrogen-containing gas (reformed gas) is generated. Further, the transformer 24 reduces the carbon monoxide contained in the reformed gas by subjecting the reformed gas generated in the reformer 16 to a shift reaction. In the purifier 28, the carbon monoxide in the reformed gas whose carbon monoxide has been reduced by the transformer 24 reacts with the oxidizing air supplied from the oxidizing air supply 116 via the oxidizing air supply path 58. By doing so, fuel gas in which carbon monoxide is reduced to 10 ppm or less is generated. In the present embodiment, methane is used as the raw material gas. However, the present invention is not limited to this, and examples thereof include gases containing hydrocarbons such as ethane and propane, gases containing gaseous alcohol, and the like. A gas containing an organic compound composed of at least carbon and hydrogen can be used. Further, in the hydrogen generator 102 in the fuel cell system 100 according to the third embodiment, the embodiment in which the transformer 24 and the purifier 28 are provided is adopted, but is included in the hydrogen-containing gas generated by the reformer 16. If it is not necessary to further reduce the carbon monoxide to be produced, a configuration in which the transformer 24 and the purifier 28 are not provided may be adopted. For example, when the hydrogen using device 101 is a device that is not easily poisoned with respect to carbon monoxide (for example, a solid oxide fuel cell), the above configuration is adopted.

  The upstream end of the fuel gas supply path 42 is connected to the fuel gas outlet 32 (see FIG. 1) of the purifier 28 of the hydrogen generator 102, and a first switch consisting of a three-way valve is provided in the middle. (Sealing device) 73 is provided, and the downstream end of the fuel gas supply path 42 is connected to the upstream end of the fuel gas channel 101 a of the fuel cell 101. Specifically, the fuel gas supply path 42 includes a first fuel gas supply path 42 a and a second fuel gas supply path 42 b, and the upstream end of the first fuel gas supply path 42 a is connected to the hydrogen generator 102. It is connected to the fuel gas outlet 32 of the purifier 28, and its downstream end is connected to the first port 73 a of the first switch 73. The upstream end of the second fuel gas supply path 42 b is connected to the third port 73 c of the first switch 73, and the downstream end is connected to the upstream end of the fuel gas channel 101 a of the fuel cell 101. ing. Note that the upstream end of the fuel gas bypass path 44 is connected to the second port 73 b of the first switch 73, and the downstream end thereof is connected in the middle of the off-fuel gas path 43.

  The upstream end of the off-fuel gas path 43 is connected to the downstream end of the fuel gas passage 101 a of the fuel cell 101, and the downstream end is connected to the burner 102 a of the hydrogen generator 102. A fourth on-off valve 75 for permitting / blocking the flow of fuel gas or the like flowing through the off-fuel gas path 43 is provided upstream of the connection point of the off-fuel gas path 43 with the fuel gas bypass path 44. It has been. In addition, a first condenser 114 is provided on the downstream side of the connection point between the off-fuel gas path 43 and the fuel gas bypass path 44, and the primary flow path 114 a of the off-fuel gas path 43 and the first condenser 114 is provided. And are connected. The first condenser 114 is configured to separate unreacted fuel gas and moisture by condensing water vapor and liquefying it into water. The upstream end of the first condensed water path 45 formed so as to extend in the vertical direction is connected to the downstream side of the first condenser 114 in the off fuel gas path 43. The downstream end is connected to the upper part (here, the upper end surface) of the second condensed water tank 105B. Further, a seventh on-off valve 78 is provided on the downstream side of the connection point of the off-gas fuel gas path 43 with the fuel gas bypass path 44.

  As a result, the fuel gas generated by the hydrogen generator 102 is supplied to the fuel gas channel 101a of the fuel cell 101, and the fuel gas supplied to the fuel gas channel 101a flows through the fuel gas channel 101a. In the meantime, it is supplied to the anode (not shown) of each cell and subjected to an electrochemical reaction. Further, surplus fuel gas that has not been used in the fuel cell 101 flows into the off-fuel gas path 43 as off-gas. While the surplus fuel gas that has flowed into the off-fuel gas path 43 flows through the primary flow path 114a of the first condenser 114, the water vapor contained in the fuel gas is condensed and liquefied into water. Then, the surplus fuel gas separated by the first condenser 114 is supplied to the burner 102a as an off gas, and is burned by the burner 102a as described above. On the other hand, the water separated by the first condenser 114 is supplied to the second condensed water tank 105 </ b> B via the first condensed water path 45.

  The oxidant gas supply unit 103 is configured to be able to supply an oxidant gas (here, air) to the oxidant gas flow path 101b of the fuel cell 101. For example, a fan such as a blower or a sirocco fan is used. Can be used. An upstream end of an oxidant gas supply path 46 is connected to the oxidant gas supply device 103, and a downstream end thereof is connected to the oxidant gas flow path 101 b of the fuel cell 101.

  The third on-off valve 74 is configured to open and close the oxidant gas supply path 46, and for example, a valve such as an electromagnetic valve can be used.

  Further, the downstream end of the purge gas supply path 49 is connected to the oxidant gas supply path 46 downstream of the third on-off valve 74, and the upstream end thereof is connected to the flow rate adjusting valve 112 b of the source gas supply path 41 and the second end. It is connected to the part between the on-off valve 72. The purge gas supply path 49 is configured to allow a source gas as a purge gas or a supplemental gas to flow therethrough, and a sixth on-off valve 77 is provided in the middle thereof. The sixth on-off valve 77 is configured to open and close the purge gas supply path 49, and for example, a valve such as an electromagnetic valve can be used.

  The upstream end of the off-oxidant gas path 47 is connected to the downstream end of the oxidant gas flow path 101 b of the fuel cell 101, and the downstream end is opened to the outside of the fuel cell system 100. A fifth on-off valve 76 that opens and closes the off-oxidant gas path 47 is provided in the middle of the off-oxidant gas path 47. The upstream end of the cathode purge gas discharge path 50 is connected between the upstream end of the off-oxidant gas path 47 and the fifth on-off valve 76, and the downstream end of the hydrogen generator 102 is connected as described above. It is connected to the burner 102a. Further, a ninth on-off valve 81 is provided in the cathode purge gas discharge path 50.

  Further, a second condenser 115 is provided downstream of the fifth on-off valve 76 in the off-oxidant gas path 47, and the off-oxidant gas path 47 and the primary flow path 115 a of the second condenser 115 are provided. It is connected. The second condenser 115 condenses the water vapor in the off-oxidant gas flowing through the off-oxidant gas path 47 and liquefies it into water, thereby surplus off-oxidant gas and moisture that have not been used in the fuel cell 101. Are configured to separate. The off-oxidant gas path 47 on the downstream side of the second condenser 115 extends vertically downward and is connected to the first condensed water tank 105A.

  As a result, the oxidant gas is supplied from the oxidant gas supply unit 103 to the oxidant gas flow path 101b of the fuel cell 101 via the oxidant gas supply path 46, and the oxidant gas supplied to the oxidant gas flow path 101b. The agent gas is supplied to the cathode (not shown) of each cell while passing through the oxidant gas flow path 101b and is subjected to an electrochemical reaction. Further, the surplus oxidant gas that has not been used for the electrochemical reaction in the fuel cell 101 flows into the off-oxidant gas path 47 together with the water generated by the electrochemical reaction. The excess oxidant gas that has flowed into the off-oxidant gas path 47 is condensed into water by the water vapor contained in the oxidant gas being condensed while flowing through the secondary flow path 115b of the second condenser 115. The Then, excess oxidant gas discharged from the second condenser 115 is introduced into the first condensed water tank 105A via the off-oxidant gas path 47, and then from an exhaust port provided in the first condensed water tank 105A. It is discharged and finally discharged outside the fuel cell system 100 (outside the package 111). On the other hand, the water separated by the second condenser 115 is supplied to the first condensed water tank 105A. The water supplied to the first condensed water tank 105A is supplied to the second condensed water tank 105B when a predetermined amount is accumulated.

  In the fuel cell 101, the fuel gas supplied from the fuel gas flow path 101a to the anode of each cell and the oxidant gas supplied from the oxidant gas flow path 101b to the cathode of each cell are electrochemically generated. It reacts to generate electricity and heat. Excess fuel gas that has not been used for the electrochemical reaction in the fuel cell 101 flows through the off-fuel gas path 43 and is stored in the second condensed water tank 105B.

  In addition, the fuel cell 101 collects heat generated by the electrochemical reaction between the fuel gas and the oxidant gas, and a cooling water flow through which cooling water (first heat medium) for cooling the fuel cell 101 flows. A path 101c is provided. The downstream end of the cooling water supply path 51 is connected to the upstream end of the cooling water flow path 101c, and the upstream end is connected to the lower part of the cooling water tank 104 for storing cooling water. In addition, the upstream end of the cooling water discharge path 52 is connected to the downstream end of the cooling water flow path 101 c, and the downstream end is connected to the lower end surface of the cooling water tank 104.

  A heat exchanger 106 is provided at an appropriate position of the cooling water path (first heat medium path), for example, a cooling water path other than the cooling water flow path 101 c in the fuel cell 101, and the cooling water supply path 51 and the heat exchanger 106 are connected to each other. The primary flow path 106a is connected. In the present embodiment, the heat exchanger 106 is provided in the cooling water supply path 51 as an example. The heat exchanger 106 can exchange heat between cooling water flowing through the primary flow path 106a and hot water (second heat medium) flowing through the secondary flow path 106b described later. It is configured as follows. The cooling water supply path 51, the primary flow path 106a of the heat exchanger 106, the cooling water flow path 101c of the fuel cell 101, and the cooling water discharge path 52 constitute a cooling water path (first heat medium path).

  Further, a temperature detector 137 is provided in the vicinity of the upstream end of the cooling water discharge path 52. The temperature detector 137 is configured to detect the temperature of the cooling water flowing through the cooling water path and output the detected temperature to the controller 110. In the present embodiment, a temperature detector 147 is provided in the cooling water supply path 51 downstream from the heat exchanger 106 to detect the temperature of the cooling water discharged from the cooling water passage 101c flowing into the fuel cell 101. The detected temperature is output to the controller 110. Note that the temperature detector that detects the temperature of the cooling water is not limited to the above-described configuration, and may be either the temperature detector 137 or the temperature detector 147, and on the cooling water path (first heat medium path). If it exists, it may be provided at any location.

  Furthermore, a first pump (first delivery device) 107 for adjusting the flow rate of the cooling water flowing through the cooling water path is provided at an appropriate position of the cooling water path (here, the cooling water supply path 51). Yes. In addition, although the pump which can adjust flow volume is used as the 1st sending device of this invention here, it is not limited to this, The flow regulator which adjusts flow volume combining a pump and a flow regulating valve is used. May be.

  As a result, the cooling water flowing through the cooling water supply path 51 passes through the primary flow path 106a of the heat exchanger 106 and the hot water and heat flowing through the secondary flow path 106b of the heat exchanger 106. Replace and cool. The cooled cooling water is supplied to the cooling water passage 101c of the fuel cell 101. The cooling water supplied to the cooling water channel 101 c recovers heat generated in the fuel cell 101 and cools the fuel cell 101. Then, the cooling water recovered from the exhaust heat of the fuel cell 101 is supplied to the cooling water tank 104.

  Here, the hot water storage tank 109 is formed so as to extend in the vertical direction, and a water supply path 53 for supplying city water is connected to a lower portion of the hot water storage tank 109, and an upper portion of the hot water storage tank 109 is connected to the hot water storage tank 109. Is connected to a hot water supply channel 54 for supplying hot water to the user. The hot water supply channel 54 is connected to a heat load that uses the hot water (not shown). Examples of the thermal load include hot water supply equipment, heating equipment, and air conditioning equipment.

  In addition, an upstream end of the hot water storage passage 55 is connected to a lower end surface of the hot water storage tank 109, and a downstream end thereof is connected to an upper portion of the hot water storage tank 109. The hot water path 55 is provided with a second pump (second transmitter) 108, a first condenser 114, a second condenser 115, and a heat exchanger 106 in order from the upstream side. The secondary flow path 114b of the first condenser 114, the secondary flow path 115b of the second condenser 115, and the secondary flow path 106b of the heat exchanger 106 are respectively connected.

  As a result, the hot water flowing through the hot water path 55 passes through the primary flow path 114a of the first condenser 114 while flowing through the secondary flow path 114b of the first condenser 114. Heat exchange with the oxidant gas flowing through the primary flow path 115a of the second condenser 115 while flowing through the secondary flow path 115b of the second condenser 115. Heated. The stored hot water flowing through the secondary flow path 115b of the second condenser 115 flows through the primary flow path 106a of the heat exchanger 106 while flowing through the secondary flow path 106b of the heat exchanger 106. Heat is exchanged with cooling water. The heated hot water is supplied to the upper end of the hot water tank 109 through the hot water passage 55. With such a configuration, the hot water storage tank 109 stores water having a low temperature close to the city water temperature in the lower part, and stores a heat medium heated by the heat exchanger 106 or the like in the upper part. It becomes a hot water storage tank.

  Further, the fuel cell system 100 includes a temperature detector 146 that detects the temperature of hot water after passing through the heat exchanger 106 in the hot water path 55, and a hot water path 55 that is downstream of the temperature detector 146. The hot water storage tank 109 and the hot water storage bypass serve as the hot water storage bypass path 207 that bypasses the hot water storage tank 109 and connects to the hot water storage water path 55 upstream of the first condenser 114, and the hot water inflow destination after passing through the heat exchanger 106. And a switcher 206 that switches to and from the path 207.

  In addition, an inverter 118 is electrically connected to the fuel cell 101 by appropriate wiring, and a direct current generated by the fuel cell 101 is converted into an alternating current, and power is supplied to an electric power load outside the fuel cell system 100. It is configured to supply. In addition, a system power supply is connected to the electrical path through which the current output from the inverter 118 flows (not shown) via a system interconnection point. That is, the output power of the fuel cell 101 and the power from the system power supply are grid-connected at the grid connection point.

  An intake port 61 and an exhaust port 62 are provided at appropriate positions of the package 111. The intake port 61 and the exhaust port 62 are preferably provided as far away from each other as possible so that the outside air can flow through the entire package 111. The exhaust port 62 may be a city gas mainly composed of methane, hydrogen, or the like. It is preferable that the flammable gas, which is lighter than oxygen, is provided on the upper portion of the package 111 where it is likely to stay. A ventilation fan 119 is disposed in the vicinity of the exhaust port 62. The ventilation fan 119 can be a fan such as a sirocco fan.

  Thereby, the ventilation fan 119 sucks outside air from the intake port 61 and the sucked outside air is discharged from the exhaust port 62.

  A combustible gas sensor 140 is provided in the package 111 of the fuel cell system 100. The combustible gas sensor 140 detects leakage (concentration) of combustible gas (for example, raw material gas or hydrogen gas) in the fuel cell system 100 (package 111), and supplies the detected combustible gas concentration to the controller 110. It is configured to output. In the present embodiment, the combustible gas sensor 140 is an upper part of the package 111 in which a combustible gas that is lighter than oxygen such as city gas or hydrogen, which is mainly composed of methane, is located in the vicinity of the ventilation fan 119. Is provided.

  The controller 110 is configured by a computer such as a microcomputer, and includes an arithmetic processing unit including a CPU, a storage unit including a memory, a communication unit, and a clock unit having a calendar function (all of which are not shown). ) The arithmetic processing unit reads out a predetermined control program stored in the storage unit and executes it, thereby performing various controls relating to the fuel cell system 100. The arithmetic processing unit processes data stored in the storage unit and data input from the operation input unit.

  Here, in this specification, the controller means not only a single controller but also a controller group in which a plurality of controllers cooperate to execute control of the fuel cell system 100. For this reason, the controller 110 does not need to be composed of a single controller, and a plurality of controllers may be arranged in a distributed manner so as to control the fuel cell system 100 in cooperation with each other. .

  The remote controller 120 includes a control unit (not shown) configured by a microcomputer, a communication unit (not shown), a display unit 120a, and a key operation unit 120b. The control unit controls the communication unit and the like. I have control. In addition, the remote controller 120 receives a control signal by the communication unit, and the control unit processes this and transmits it to the display unit 120a. In addition, an operation signal input from the key operation unit 120 b of the remote control 120 is transmitted to the controller 110 via the control unit and communication unit of the remote control 120 and received by the communication unit of the controller 110. Then, when the operation is forcibly stopped to perform maintenance and inspection of the fuel cell system 100, or the user or the maintenance operator of the fuel cell system 100 performs an input operation for stopping the operation via the remote controller 120. By performing (stop command input), the controller 110 forcibly stops the fuel cell system 100. The term “during operation” as used herein includes at least one of the start process, the power generation operation, and the stop process of the fuel cell system 100. A stop process of the fuel cell system 100 (hereinafter referred to as a forced stop process) when a stop input operation is performed with the remote controller 120 will be described later.

  In the following description, in order to simplify the description, the exchange of signals between the controller 110 and the remote controller 120 is described by omitting communication by both communication units and processing of the control unit in the remote controller 120.

[Operation of fuel cell system]
Next, startup processing (startup operation) of the fuel cell system 100 according to Embodiment 3 will be described with reference to FIG. The following operation is performed by the controller 110 controlling the fuel cell system 100 by the user operating the remote controller 120.

  First, at the start of the starting process, the third on-off valve 74, the fifth on-off valve 76, and the sixth on-off valve 77 are respectively set so as not to flow through the source gas and the oxidant gas oxidant gas supply path 46. Keep the valve closed. Further, the first switch 73 communicates the first port 73a with the second port 73b so that fuel gas in which carbon monoxide is not sufficiently reduced is not supplied to the fuel gas passage 101a of the fuel cell 101. And the 3rd port 73c is interrupted | blocked. Subsequently, the first on-off valve 71 opens the valve, and the source gas is supplied to the source gas supply path 41.

  Next, the second on-off valve 72 opens the valve. As a result, the source gas bypasses the hydrogen generator 102 and is supplied from the source gas supply unit 112 to the burner 102a through a flow path (not shown). Further, combustion air is supplied from the combustion air supplier 117 to the burner 102 a via the combustion air supply path 56. In the burner 102a, the supplied source gas is combusted with combustion air, and combustion exhaust gas is produced | generated. The generated flue gas flows through the flue gas passage 10 (see FIG. 1) provided in the hydrogen generator 102, heats the reformer 16, the transformer 24, and the purifier 28, and then the fuel cell system. 100 (package 111) is discharged outside. At this time, the reformer 16, the transformer 24, and the purifier 28 of the hydrogen generator 102 are heated by heat transfer from the combustion exhaust gas.

  Next, the source gas is supplied from the source gas supply unit 112 to the reformer 16 of the hydrogen generator 102 via the source gas supply path 41, and the reforming water supply path 57 from the first condensed water tank 105A. The reforming water (condensed water) is supplied via the. Then, the supplied water is heated to become water vapor, and the raw material gas and water vapor react to generate a hydrogen-containing gas containing hydrogen. The generated hydrogen-containing gas passes through the transformer 24 and the purifier 28 of the hydrogen generator 102 and is sent out from the hydrogen generator 102 as fuel gas with reduced carbon monoxide. The delivered fuel gas is introduced from the fuel gas outlet 32 (see FIG. 1) of the purifier 28 of the hydrogen generator 102 into the first fuel gas supply path 42a.

  The fuel gas introduced into the first fuel gas supply path 42a is divided into the first fuel gas supply path 42a, the fuel gas bypass path 44, and the off fuel gas path 43 (more precisely, the fuel gas bypass path 44 and the off fuel gas path 43 flows through the off-fuel gas path 43) downstream of the junction with 43 and is supplied to the burner 102 a. When the fuel gas is supplied to the burner 102a, the direct supply of the raw material gas bypassing the hydrogen generator 102 from the raw material gas supplier 112 to the burner 102a is stopped.

  Next, when the temperature detector 143 (see FIG. 1) provided in the reformer 16 of the hydrogen generator 102 reaches a predetermined temperature (for example, 500 ° C.), the sixth open / close valve 77 and the ninth open / close valve 81. Opens the valve, and the source gas flows through the purge gas supply path 49 and the oxidant gas supply path 46 (more precisely, the path downstream of the third on-off valve 74 of the oxidant gas supply path 46). Then, the hydrogen that is supplied to the oxidant gas flow path 101b of the fuel cell 101 and enters the oxidant gas flow path 101b through the electrolyte from the fuel gas flow path 101a during the stop period of the fuel cell system 100 is caused by the source gas. Purge (cathode purge process during start-up process of the fuel cell system 100). The cathode purge gas and the source gas scavenged by the cathode purge process flow through the cathode purge gas discharge path 50, are supplied to the burner 102a, and are burned. When at least the amount of source gas necessary for sending the gas sealed in the oxidant gas flow path 101b to the burner 102a is supplied before starting the cathode purge process, the sixth on-off valve 77 and the ninth on-off valve 81 is closed to finish the cathode purge process.

  Then, the temperature detectors 143 to 145 (see FIG. 1) provided in the reformer 16, the transformer 24, and the purifier 28 of the hydrogen generator 102 are set to a predetermined temperature (for example, the reformer 16 is 600 to 650 ° C., the transformer 24 is 200 to 250 ° C., and the purifier 28 is 130 to 170 ° C.), the controller 110 finishes the startup process of the fuel cell system 100 and shifts to the power generation process (power generation operation). To do.

  Next, power generation processing (power generation operation) of the fuel cell system 100 according to Embodiment 3 will be described.

  First, the controller 110 detects that the temperatures detected by the temperature detectors 143 to 145 provided in the reformer 16, the transformer 24, and the purifier 28 of the hydrogen generator 102 are respectively predetermined temperatures (for example, reforming). When the vessel 16 reaches a predetermined temperature within 600 to 650 ° C., the transformer 24 reaches a predetermined temperature within 200 to 250 ° C., and the purifier 28 reaches a predetermined temperature within 130 to 170 ° C.), the transformer 24 and the purifier 28 Thus, it is determined that the carbon monoxide has been sufficiently reduced, and a power generation processing start signal is output.

  Then, the 3rd on-off valve 74, the 4th on-off valve 75, and the 5th on-off valve 76 open each valve. In addition, the first switch 73 causes the first port 73a to communicate with the third port 73c, blocks the second port 73b, and starts the operation of the oxidant gas supplier 103.

  As a result, the fuel gas generated by the hydrogen generator 102 flows through the first fuel gas supply path 42 a and the second fuel gas supply path 42 b (that is, the fuel gas supply path 42), and the fuel gas of the fuel cell 101. Supplied to the channel 101a. Further, the oxidant gas is supplied from the oxidant gas supply device 103 through the oxidant gas supply path 46 and supplied to the oxidant gas flow path 101 b of the fuel cell 101.

  The fuel gas and the oxidant gas supplied to the fuel gas channel 101a and the oxidant gas channel 101b of the fuel cell 101 are supplied to the anode and cathode of each cell, respectively, and react electrochemically to form water. Is generated, generating electricity and heat. The generated electricity is converted from a direct current to an alternating current by an inverter 118 and supplied to an electric power load outside the fuel cell system 100.

  Excess fuel gas that has not been used in the fuel cell 101 is supplied to the off-fuel gas path 43 as off-fuel gas. While the surplus fuel gas supplied to the off-fuel gas path 43 flows through the primary flow path 114a of the first condenser 114, water vapor contained in the fuel gas is condensed and liquefied into water. The surplus fuel gas that has passed through the first condenser 114 is supplied to the burner 102a as off-fuel gas, and is burned in the burner 102a as described above. On the other hand, the water separated by the first condenser 114 is supplied to the second condensed water tank 105 </ b> B via the off fuel gas path 43.

  Further, surplus oxidant gas that has not been used in the electrochemical reaction in the fuel cell 101 is supplied to the oxidant gas path 47. The excess off-oxidant gas supplied to the off-oxidant gas path 47 is condensed into water by the water vapor contained in the oxidant gas being condensed while flowing through the primary flow path 115a of the second condenser 115. Is done. The surplus oxidant gas that has passed through the second condenser 115 is finally discharged out of the fuel cell system 100 through the exhaust port of the first condensed water tank 105A. On the other hand, the water separated by the second condenser 115 is supplied to the first condensed water tank 105 </ b> A via the off-oxidant gas path 47.

  Further, by operating the first pump 107, cooling water is supplied from the cooling water tank 104 to the cooling water flow path 101c of the fuel cell 101 via the cooling water path (more precisely, the cooling water supply path 51). Is done. Specifically, the cooling water flows from the cooling water tank 104 through the cooling water supply path 51 and is supplied to the primary flow path 106 a of the heat exchanger 106. The cooling water supplied to the primary flow path 106a of the heat exchanger 106 is stored in hot water flowing through the secondary flow path 106b of the heat exchanger 106 while flowing through the primary flow path 106a of the heat exchanger 106. It is cooled by exchanging heat. Then, the cooled cooling water flows through the cooling water supply path 51 and is supplied to the cooling water channel 101 c of the fuel cell 101. The cooling water supplied to the cooling water channel 101 c recovers heat generated in the fuel cell 101 and cools the fuel cell 101. The cooling water recovered from the exhaust heat of the fuel cell 101 flows through the cooling water discharge path 52 and is supplied to the cooling water tank 104.

  On the other hand, the hot water supplied from the lower part (here, the lower end surface) of the hot water tank 109 to the hot water path 55 is the secondary flow path 114b of the first condenser 114 and the secondary flow path 115b of the second condenser 115. During the flow, the heat exchange with the surplus fuel gas and oxidant gas flowing through the primary flow path 114a of the first condenser 114 and the primary flow path 115a of the second condenser 115 is performed, respectively. The The heated hot water is supplied to the secondary flow path 106b of the heat exchanger 106 and passes through the primary flow path 106a of the heat exchanger 106 while flowing through the secondary flow path 106b of the heat exchanger 106. It is further heated by exchanging heat with the flowing cooling water. The heated hot water is supplied to the upper part of the hot water tank 109 through the hot water path 55 and supplied to the heat load from the hot water supply path 54.

  Next, normal stop processing (stop operation) of the fuel cell system 100 according to Embodiment 3 will be described. The normal stop process here is different from a stop process (abnormal stop process) or a forced stop process executed when an abnormality is detected by the abnormality detector during operation of the fuel cell system 100. Refers to processing. For example, a stop process that is executed when the power demand of the power load falls below a predetermined threshold that does not require the power generation operation, a stop process that is executed when a preset stop time is reached, and the like. .

  First, in the present invention, a stop process (stop operation) is defined as an operation from when the controller 110 outputs a stop signal until the fuel cell system 100 completes the stop process. It should be noted that after the completion of the stop process of the fuel cell system 100, the controller 110 is operating, the operation of the parts other than the controller 110 is stopped, and when an activation request is generated, the controller 110 A start command is output, and a transition is made to a standby state in which start processing can be started immediately. As a case where the controller 110 outputs a stop process, for example, the power demand of the power load is equal to or less than a predetermined threshold (the power demand of load power detected by a load power detector (not shown) is equal to or less than a predetermined threshold. A stop signal is output. The power generation of the fuel cell 101 is stopped by setting the output of the inverter 118 to zero and electrically disconnecting the electric circuit on the outlet side of the inverter 118.

  Hereinafter, normal stop processing (stop operation) of the fuel cell system 100 according to Embodiment 3 will be described with reference to FIGS. 6A, 6B, and 7. FIG. FIG. 6A is a flowchart showing the main operation of normal stop processing in the fuel cell system according to Embodiment 3 of the present invention. FIG. 6B is a flowchart showing the main operation of normal stop processing in the fuel cell system according to Embodiment 3 of the present invention. FIG. 7 is a flowchart showing the exhaust heat recovery operation of the fuel cell in the normal stop process of the fuel cell system according to Embodiment 3 of the present invention.

  First, the operation of the oxidant gas supply device 103 is stopped, the supply of the oxidant gas to the oxidant gas flow path 101b is stopped (step S300), and the third on-off valve 74 and the fifth on-off valve 76 are closed. Then, the oxidant gas flow path 101b of the fuel cell 101 is shut off from the outside air (step S301).

  Further, the first switch 73 communicates the first port 73a with the second port 73b, shuts off the third port 73c, and the fourth on-off valve 75 closes the valve (step S302). Thereby, the flow path between the third port 73c of the first switch 73 and the fourth on-off valve 75, that is, the second fuel gas supply path 42b, the fuel gas flow path 101a of the fuel cell 101, and the off-fuel gas. The fuel gas is confined in the flow path up to the fourth on-off valve 75 in the path 43, and mixing of air or the like into the fuel gas flow path 101a from the outside is suppressed, so that deterioration of the anode can be suppressed.

  In addition, the booster pump 112a, the third pump 113, and the oxidizing air supply unit 116 are stopped, and the supply of the raw material gas, the reforming water, and the oxidizing air to the hydrogen generator 102 is stopped (step S303). Further, the first on-off valve 71 and the second on-off valve 72 close the valves (step S304).

  As a result, the supply of the raw material gas, the reforming water and the oxidizing air to the hydrogen generator 102 is stopped, and the supply of the fuel gas from the hydrogen generator 102 to the fuel gas channel 101a of the fuel cell 101 is stopped. As a result, the supply of off gas from the fuel cell 101 to the burner 102a is stopped, and combustion in the burner 102a is stopped. Then, since the supply of the fuel gas and the oxidant gas to the fuel cell 101 is stopped by the series of operations, the power generation is also stopped. On the other hand, since the operation of the combustion air supply device 117 continues, the hydrogen generator 102 is air-cooled, and the temperature of the hydrogen generator 102 decreases with time.

  Next, when the detected temperature (step S305) of the temperature detector 143 provided in the reformer 16 of the hydrogen generator 102 becomes equal to or lower than the cathode purge temperature (Yes in step S306), the fifth on-off valve 76 and the sixth on-off opening / closing. The valve 77 and the ninth on-off valve 81 are opened (step S307), the first on-off valve 71 and the second on-off valve 72 are opened, and the operation of the booster pump 112a is started (at the time of stop processing of the fuel cell system 100). Start of cathode purge process) (step S308). Here, the cathode purge temperature is a temperature that is lower than the heat resistant temperature of the catalyst used in the reformer 16 even if the temperature increase of the hydrogen generator 102 during the cathode purge process during the stop process is added (for example, 600 ° C). At the start of the cathode purge process during the stop process, the inside of the reformer 16 of the hydrogen generator 102 is in a state where the raw material gas and water vapor sealed in the internal space remain immediately after the stop, so the stop process At the time of cathode purge treatment, the possibility of carbon deposition from the raw material is reduced.

  As a result, the source gas (purge gas) flows from the source gas supply path 41 through the purge gas supply path 49, and the oxidant gas supply path 46 (precisely, the purge gas supply path 49 and the oxidant gas supply path 46 join together). Is supplied to the oxidant gas flow path 101b of the fuel cell 101 via the oxidant gas supply path 46) on the downstream side of the unit. Then, the oxidant gas present in the oxidant gas flow path 101b is purged by the purge gas, and the off-oxidant gas path 47 (to be precise, the path upstream of the fifth on-off valve 76 in the off-oxidant gas path 47). And the cathode purge gas discharge path 50 is supplied to the burner 102a. The oxidant gas and source gas supplied to the burner 102a are combusted in the burner 102a (step S309).

  Then, the elapsed time T2 after the start of the cathode purge process in the stop process is measured (step S310), and when the elapsed time T2 becomes equal to or longer than the cathode purge time J2 (Yes in step S311), the booster pump 112a. The first on-off valve 71 and the second on-off valve 72 are closed (step S312), and the fifth on-off valve 76, the sixth on-off valve 77, and the ninth on-off valve 81 are closed (of the fuel cell system 100). End of cathode purge process during stop process) (step S313). The cathode purge time is defined as the time required for scavenging at least the oxidant gas in the oxidant gas flow path 101b of the fuel cell 101 from the oxidant gas flow path 101b.

  Thereby, a closed flow path formed by the third on-off valve 74, the sixth on-off valve 77, the fifth on-off valve 76, and the ninth on-off valve 81, that is, the downstream side from the sixth on-off valve 77 of the purge gas supply path 49. , The downstream side of the third open / close valve 74 of the oxidant gas supply path 46, the fifth open / close valve 76 of the oxidant gas flow path 101b, the off-oxidant gas path 47, and the ninth open / close of the cathode purge gas discharge path 50. Purge gas is confined in the flow path to the valve 81 (hereinafter referred to as purge gas sealing flow path), and the entry of air or the like into the oxidant gas flow path 101b from the outside is suppressed.

  On the other hand, the combustion air supplier 117 supplies combustion air to the burner 102a even after combustion in the burner 102a in the cathode purge process is stopped. Thereby, the reformer 16 and the like of the hydrogen generator 102 are also cooled by the combustion air flowing through the combustion exhaust gas path 59 (see FIG. 1) (cooling operation of the hydrogen generator 102).

  During the cooling operation after the completion of the cathode purge process during the stop process of the fuel cell system 100, the temperature detector 143 provided in the reformer 16 of the hydrogen generator 102 is the temperature of the reformer 16. (Step S314), and when the detected temperature is equal to or lower than the standby temperature (for example, 500 ° C.) (Yes in step S315), the combustion air supply device 117 supplies the combustion air to the burner 102a. The process is stopped (step S316), and the cooling process of the hydrogen generator 102 is completed.

  On the other hand, in the stop process of the fuel cell system 100, not only the above-described series of stop processes, but also a predetermined cooling operation (exhaust heat recovery operation) is executed in parallel in the cooling system of the fuel cell 101. Specifically, as shown in FIG. 7, even after the power generation of the fuel cell 101 is stopped, the operations of the first pump 107 and the second pump 108 are continued (step S400), and the hot water is used as a heat exchanger. In 106, heat is exchanged with the cooling water, and the residual heat held by the fuel cell 101 is recovered.

  Then, the controller 110 detects when the temperature detected by the temperature detector 143 provided in the reformer 16 is equal to or lower than the cathode purge temperature and the cathode purge process is started during the stop process (step S401). Then, the operation of the first pump 107 is stopped (step S402). When the cathode purge process during the stop process is completed (step S403), the operation of the first pump 107 is resumed (step S404), and the temperature t1 of the reformer 16 becomes equal to or lower than the standby temperature in step S315 of FIG. 6B. (Step S405), and when the cooling operation of the hydrogen generator 102 by the combustion air supply 117 is stopped in step S316 of FIG. 6B, the first pump 107 and the second pump 108 are also stopped. The operation is stopped (step S406).

  When the cooling operation of the hydrogen generator 102 up to the standby temperature and the cooling operation of the fuel cell executed along with this cooling operation are completed, the fuel cell system 100 shifts to a standby state (step of FIG. 6B). S317, step S407 of FIG. 7). The standby state is a state where the next fuel cell system 100 is waiting to start operation. For example, when a predetermined activation request is generated, an activation command is output from the controller 110, and It is defined as a state that shifts to execution of the next startup process. Examples of the activation request include, for example, that the power demand of the power load is equal to or higher than the lower limit of the power generation output of the fuel cell system, or that the user operates the key operation unit 120b of the remote controller 120 to make a power generation start request. To do.

  In the standby state, the hydrogen generator 102 is naturally cooled because the combustion air supply 117 is stopped. At that time, the hydrogen generator 102 is supplied to the reformer 16 of the hydrogen generator 102 as shown in FIG. 6B. When the provided temperature detector 143 detects the temperature t1 of the reformer 16 again (step S318), and the detected temperature t1 is lower than the FP purge temperature (for example, 300 ° C.) lower than the standby-enabled temperature. (Step S319), the first on-off valve 71, the second on-off valve 72, and the seventh on-off valve 78 are opened, and the booster pump 112a is activated (the purge process (FP (Fuel) for the hydrogen generator 102). (Processor) Start of Purging Process) (Step S320).

  Thereby, the raw material gas (purge gas) is supplied from the raw material gas supply device 112 to the hydrogen generating device 102, and the gas such as water vapor existing in the reactor such as the reformer 16 provided in the hydrogen generating device 102 is the raw material gas. , Purged from the hydrogen generator 102, and sent to the burner 102a. The gas sent to the burner 102a is burned by the burner 102a (step S321). By this FP purge process, it is possible to suppress the condensation of water vapor in the hydrogen generator 102 and the deterioration of the catalyst such as the reforming catalyst. Note that the FP purge temperature is not changed even if the temperature rise of the reformer 16 due to the combustion operation in the burner 102a during the FP purge process for the hydrogen generator 102 is added. It is defined as the temperature at which no precipitation occurs.

  Then, the elapsed time T3 from the start of the FP purge process is measured (step S322). When the elapsed time T3 becomes equal to or longer than the FP purge time J3 (step S323), the booster pump 112a is stopped and the first opening / closing is performed. The valve 71, the second on-off valve 72, and the seventh on-off valve 78 are closed (end of the FP purge process) (step S324). The FP purge time is defined as the time required for at least the water vapor in the hydrogen generator 102 to be scavenged.

  As described above, in the fuel cell system 100 according to the third embodiment, when the operation is stopped in a normal state, at least a stop process that protects at least the function of the fuel cell 101 (for example, the fuel cell system 100). The cathode purge process at the time of the stop process) is executed, and the apparatus quickly shifts to the standby state. Even when the cooling operation is performed, the exhaust heat recovery operation is performed only until the temperature of the hydrogen generator 102 can be restarted (that is, until the temperature of the reformer 16 is equal to or lower than the standby temperature). It is configured to perform the minimum necessary cooling operation such as. Therefore, it is possible to quickly shift to the standby state, and in the next start-up process, depending on the elapsed time after shifting to the standby state, the temperature of the device such as the fuel cell 101 is higher than the ambient temperature (outside air temperature). The energy required to raise the temperature of 101 is reduced, the time required for the startup process is shortened, and the startup performance of the fuel cell system 100 is improved.

  In the stop process of the fuel cell system 100 according to the third embodiment, the cooling operation of the hydrogen generator 102, the cathode purge process and the exhaust heat recovery operation of the fuel cell 101 are executed. The present invention is not limited to this as long as it is an appropriate stop operation for shifting the battery system 100 to the standby state.

  Next, the forced stop process of the fuel cell system 100 according to Embodiment 3 will be described with reference to FIG. FIG. 8 is a flowchart showing the main operation of the main stop process in the fuel cell system 100 according to Embodiment 3 of the present invention.

  When a user of the fuel cell system 100 or a maintenance operator operates the remote controller 120 and a stop command signal is input to the controller 110, the controller 110 outputs a stop command, as shown in FIG. As a stop process for the hydrogen generator 102 as in the normal stop process of the fuel cell system 100, first, the supply of the source gas and water is stopped and the sealing operation of the hydrogen generator 102 (steps S100 and S101 in FIG. 2). By executing (see), the combustion operation in the burner 102a is stopped (step S500). Further, as the stop operation for the fuel cell 101, the oxidant gas supply device 103 and the like are stopped, and the on-off valves are closed (see steps S300 to S304 in FIG. 6A) (step S501). Thereby, in the burner 102a of the hydrogen generator 102, the combustion of the fuel gas and the combustion air is stopped, and the power generation of the fuel cell 101 is stopped.

  On the other hand, the combustion air supply device 117 continues the supply of the combustion air to the burner 102a even after the combustion in the burner 102a is stopped by the control of the controller 110, and executes the cooling operation of the hydrogen generator 102 (step). S502). When the detected temperature t1 of the temperature detector 143 provided in the reformer 16 of the hydrogen generator 102 is equal to or lower than the cathode purge temperature (step S503), the cathode purge process in the stop process is executed (step S503). 6A and 6B (see step S306 to step S313) (step S504). At this time, the operation of the first pump 107 is stopped, and the exhaust heat recovery operation of the fuel cell 101 is stopped (step S513).

  Then, after the cathode purge process in the stop process is completed (step S505) and the combustion operation in the burner 102a is completed, the operation of the first pump is resumed and the exhaust heat recovery operation of the fuel cell 101 is resumed ( Step S514). Next, even if the temperature t1 of the reformer 16 detected by the temperature detector 143 falls below the standby temperature (step S506), unlike the normal stop process, the operation of the combustion air supply device 117 is continued. (Step S507) Further, the operations of the first pump 107 and the second pump 108 are continued (Step S515).

  Next, when the temperature t1 of the reformer 16 detected by the temperature detector 143 falls below the FP purge temperature (step S508), the FP purge process (see steps S106 to S112 in FIG. 2) is started (see FIG. 2). Step S509). Thereafter, when the FP purge process is completed (step S510), the controller 110 stops the operations of the combustion air supply device 117, the first pump 107, and the second pump 108 (steps S511 and S516), and the forced stop process. Is completed, and the fuel cell system 100 is shifted to the activation disapproval state (step S517). Here, the transition to the activation disapproval state means that even if the user operates the remote controller 120 and inputs an activation command so that the user starts the operation of the fuel cell system 100, the arithmetic processing unit of the controller 110 This means that the above-described fuel cell system 100 is not permitted to be activated and the activation command is not output. In other words, in the third embodiment, the controller 110 controls the controller 110 even if a user or the like erroneously operates the key operation unit 120b of the remote controller 120 to transmit an activation command to the communication unit of the controller 110. The device 110 is configured not to permit activation of the fuel cell system 100.

  In the cooling operation of the hydrogen generator 102 in the forced stop process, it is preferable to control the amount of combustion air supplied to the burner 102a to be larger than the supply amount during the rated operation of the hydrogen generator 102. Specifically, in the cooling operation of the hydrogen generator 102 in the forced stop process, the controller 110 controls the combustion air supplier 117 so as to be larger than the operation amount during the rated operation of the fuel cell system 100. As a result, the temperature of the hydrogen generator 102, which is a device constituting the fuel cell system 100, decreases more quickly, and it becomes easier to proceed to maintenance work. Here, the rated operation of the fuel cell system 100 is defined as an operation that generates power at the maximum output that can be stably output during the power generation operation of the fuel cell system 100.

  In the exhaust heat recovery operation of the fuel cell 101 in the normal stop process and the forced stop process, the hot water temperature control shown in FIG. 9 is performed in parallel with this operation. FIG. 9 is a flowchart showing an outline of hot water storage control in the fuel cell system 100 according to Embodiment 3 of the present invention.

  The control of the hot water temperature is performed so that hot water having a hot water storage lower limit temperature (for example, 60 ° C.) or higher is stored in the hot water storage tank 109. Specifically, as shown in FIG. 9, the temperature detector 146 detects the temperature t3 of the hot water after passing through the heat exchanger 106 (step S600), and the hot water temperature t3 is equal to or higher than the hot water storage lower limit temperature. (Yes in step S601), the controller 110 controls the switch 206 so that the stored hot water flows into the hot water storage tank 109 (step S602). On the other hand, when the temperature t3 of the hot water storage is lower than the hot water storage lower limit temperature (No in step S601), the controller 110 controls the switch 206 so as to be on the hot water bypass path 207 side (step S603).

  Here, when the forced stop process is compared with the normal stop process, in the forced stop process, the temperature of the reformer after the temperature of the reformer becomes equal to or lower than the standby temperature (FP purge temperature). In the period until the temperature reaches the following temperature), the cooling operation of the hydrogen generator 102 by the combustion air supply device 117 is not waited for the hydrogen generator 102 to cool by natural cooling as in the normal stop process. The exhaust heat recovery operation of the fuel cell 101 by the first pump 107 and the second pump 108 is continued, and the hydrogen generator 102 and the fuel cell 101 are cooled more quickly.

  For this reason, in the fuel cell system 100 according to the third embodiment, the forced stop process is controlled so that the cooling amount of the fuel cell 101 and the hydrogen generator 102 is increased as compared with the normal stop process. Thus, the temperature of the equipment in the fuel cell system 100 can be lowered more quickly to such an extent that the maintenance worker does not burn or the like, and the shift to the maintenance work can be made quicker.

  In the third embodiment, in the forced stop process, the cooling operation time of the hydrogen generator 102 by the combustion air supply device 117 and the first pump 107 and the second pump 108 are compared with those in the normal stop process. The amount of cooling of the fuel cell 101 and the hydrogen generator 102 is controlled to be increased by controlling the exhaust heat recovery operation time of the fuel cell 101 to be increased. However, the present invention is not limited to this, and is supplied to the burner 102a. It is also possible to adopt a form in which control is performed so that the flow rate of at least one of the cooling air passing through the heat exchanger 106 and the cooling water passing through the heat exchanger 106 and the hot water storage water increases. Specifically, the amount of operation of the combustion air supply device 117 is controlled to be larger than that during the cooling operation of the hydrogen generation device 102 in the normal stop process, and at least one of the first pump 107 and the second pump 108 is controlled. This is realized by controlling the operation amount to be larger than that during the exhaust heat recovery operation of the fuel cell 101 in the normal stop process.

  In the third embodiment, the remote controller 120 constitutes a stop operation device. However, the present invention is not limited to this, and a stop operation for forcibly stopping the operation of the fuel cell system 100 separately from the remote controller 120. A vessel may be provided.

(Embodiment 4)
By the way, during the stop process, the hydrogen generator 102 performs a sealing operation to close the inlet and the outlet of the combustible gas path of the hydrogen generator 102 so that the gas path including the reformer 16 is closed. However, after that, the internal force decreases as the temperature of the hydrogen generating apparatus 102 decreases, and as a result, the inside of the hydrogen generating apparatus 102 becomes excessively negative pressure, which may damage the constituent members. Therefore, in the hydrogen generator 102 according to the fourth embodiment, when the internal pressure of the hydrogen generator 102 is equal to or less than a predetermined pressure threshold P1 that is larger than the negative pressure limit value of the hydrogen generator 102, It is comprised so that the supplementary pressure process which replenishes gas may be implemented.

  In the hydrogen generator 102 according to the fourth embodiment, the cooling per unit time in the cooling operation of the hydrogen generator 102 during the forced stop process is greater than the cooling operation of the hydrogen generator 102 during the normal stop process. Configured to increase the amount. Accordingly, since the temperature decrease rate of the hydrogen generator 102 is faster and the pressure decrease is faster than in the normal stop process, the frequency of the pressure increasing process is increased more than the frequency of the pressure reducing process in the normal stop process. It is characterized by doing. The details will be described below.

  First, the configuration of the hydrogen generator 102 according to Embodiment 4 is the same as that of the hydrogen generator 102 according to Embodiment 1 shown in FIG. As for the normal stop process, the cooling operation of the hydrogen generator 102 is executed in the same manner as in the first embodiment, and the supplemental pressure process is further executed. The supplementary pressure process will be described later.

  The cooling operation in the normal stop process of the hydrogen generator 102 according to the fourth embodiment is the same as the cooling operation of the hydrogen generator 102 according to the first embodiment (see steps S100 to S105 in FIG. 2). .

  Next, the pressure compensation process of the hydrogen generator 102 according to the fourth embodiment will be described with reference to FIG. FIG. 10 is a flowchart showing an example of the pressure compensation process executed in the hydrogen generator 102 according to the fourth embodiment.

  As shown in FIG. 10, after the start of the stop process, the sealing operation of the hydrogen generator 102 is performed (step S900). Specifically, at least one of the first on-off valve 71 and the second on-off valve 72 provided on the source gas supply path 41 is closed, and the fuel gas valve 79 and the bypass valve 80 are closed.

  Next, a pressure value detected by a pressure detector (not shown) provided in a gas path including the hydrogen generator 102 that becomes a closed space by the sealing operation is a predetermined pressure threshold value P1 (for example, If it is equal to or less than −5 kPa with respect to the atmospheric pressure (Yes in step S901), the controller 110 closes the first on-off valve 71 and the second on-off valve 72 while the fuel gas valve 79 and the bypass valve 80 are closed. The source gas supply unit 112 is opened and the source gas is supplied from the source gas supply path 41 by controlling the source gas supply unit 112 (step S902). Then, when the pressure becomes equal to or higher than the atmospheric pressure, the controller 110 stops the gas supply from the source gas supplier 112 to the gas path including the hydrogen generator 102, and the first opening / closing valve 71 and the second opening / closing valve The valve 72 is closed and the compensation process is terminated.

  Then, the controller 110 executes step S901 periodically (for example, every 30 sec) even after execution of the above-described pressure-compensating operation. If the pressure in the gas path decreases to a level that requires pressure-compensation, the controller 110 performs the above-mentioned compensation as appropriate. Execute pressure processing.

  Note that when the execution of the supplementary pressure operation is determined, the detected pressure value of the pressure detector that directly detects the pressure value in the gas path is used. However, the temperature detection in the gas path that correlates with the pressure value is performed. A configuration may be adopted in which the pressure compensation process is executed based on the temperature detected by a temperature detector (for example, the temperature detector 143) and the elapsed time after the start of the stop process correlated with the pressure value measured by the clock unit. .

  Next, the forced stop process in the hydrogen generator 102 according to Embodiment 4 will be described. The forced stop process is performed in the same flow (see FIG. 3) as the cooling operation of the hydrogen generator 102 according to Embodiment 1, but the flow rate of the combustion air supplied to the burner 102a is the normal stop process. It is controlled to be larger than the cooling operation of the hydrogen generator. Specifically, the controller 110 sets the operation amount of the combustion air supply device 117 to a predetermined operation amount that is larger than the operation amount of the combustion air supply device 117 in the cooling operation of the hydrogen generator 102 in the normal stop process. To control.

  As described above, in the forced stop process, the cooling operation is performed so that the cooling rate of the hydrogen generator 102 is higher than that in the normal stop process. Therefore, the temperature decrease of the hydrogen generator 102 is lower than that in the normal stop process. The speed of the gas passage including the hydrogen generator 102 is increased, and the frequency at which the pressure is reduced to a level that requires supplementary pressure increases. Therefore, in the forced stop process of the hydrogen generator 102 according to the fourth embodiment, excessive pressure reduction in the hydrogen generator 102 is performed by executing the above-described supplementary pressure operation more frequently than the normal stop process. Is suppressed, and the hydrogen generator 102 is protected.

  The hydrogen generator according to the present invention and the fuel cell system including the hydrogen generator are more promptly operated when an operator inputs an operation to the stop operating device to stop the operation of the hydrogen generator when maintenance work is required. It becomes possible to start the maintenance work of the generator.

FIG. 1 is a schematic diagram showing a schematic configuration of a hydrogen generator according to Embodiment 1 of the present invention. FIG. 2 is a flowchart showing an example of normal stop processing in the hydrogen generator 102 according to Embodiment 1 of the present invention. FIG. 3 is a flowchart showing the main operation of the forced stop process in the hydrogen generator according to Embodiment 1 of the present invention. FIG. 4 is a schematic diagram showing a schematic configuration of the hydrogen generator according to Embodiment 2 of the present invention. FIG. 5 is a schematic diagram showing a schematic configuration of a fuel cell system according to Embodiment 3 of the present invention. FIG. 6A is a flowchart showing the main operation of normal stop processing in the fuel cell system according to Embodiment 3 of the present invention. FIG. 6B is a flowchart showing the main operation of normal stop processing in the fuel cell system according to Embodiment 3 of the present invention. FIG. 7 is a flowchart showing the exhaust heat recovery operation of the fuel cell in the normal stop process of the fuel cell system according to Embodiment 3 of the present invention. FIG. 8 is a flowchart showing the main operation of the forced stop process in the fuel cell system according to Embodiment 3 of the present invention. FIG. 9 is a flowchart showing an outline of hot water storage control in the fuel cell system according to Embodiment 3 of the present invention. FIG. 10 is a flowchart showing an example of the compensation pressure process executed in the hydrogen generator according to the fourth embodiment.

DESCRIPTION OF SYMBOLS 1 Container 2 Outer cylinder 3 Inner cylinder 4 Heat insulation member 5 Bottom plate 6 Plate member 7 Lid member 8 Inner cylinder bottom plate 9 Radiation cylinder 10 Combustion exhaust gas flow path 11 Combustion exhaust gas outlet 12 Raw material gas supply port 13 Water supply port 14 Reforming catalyst layer DESCRIPTION OF SYMBOLS 15 Preheating part 16 Reformer 17 Buffer space part 18 Space 19 Hydrogen containing gas flow path 20 Partition plate 21 Partition plate 22 Conversion catalyst accommodation space 23 Transformation catalyst layer 24 Transformation device 25 Air mixing part 26 Oxidation catalyst accommodation space 27 Oxidation catalyst layer 28 Purifier 29 Outlet (through hole)
30 Air supply port 31 Inlet (through hole)
32 Fuel gas outlet 41 Raw material gas supply path 42 Fuel gas supply path 42a First fuel gas supply path 42b Second fuel gas supply path 43 Off-fuel gas path 44 Fuel gas bypass path 45 First condensed water path 46 Oxidant gas supply path 47 Oxidant gas discharge path 48 Second condensate water path 49 Purge gas supply path 50 Cathode purge gas discharge path 51 Cooling water supply path 52 Cooling water discharge path 53 Water supply path 54 Hot water supply path 55 Hot water supply path 56 Combustion air supply path 57 Reforming water supply path 58 Selective oxidation air supply path 59 Combustion exhaust gas path 61 Intake port 62 Exhaust port 71 First on-off valve (sealing device)
72 Second on-off valve (sealing device)
73 1st switch 73a 1st port 73b 2nd port 73c 3rd port 74 3rd on-off valve 75 4th on-off valve 76 5th on-off valve 77 6th on-off valve 78 7th on-off valve 79 Fuel gas valve (sealing device) )
80 Bypass valve (sealing device)
81 9th on-off valve 100 Fuel cell system 101 Fuel cell (hydrogen utilization equipment)
101a Fuel gas channel 101b Oxidant gas channel 101c Cooling water channel 102 Hydrogen generator 102a Burner (combustor)
103 Oxidant gas supply device 104 Cooling water tank 105 Condensed water tank 106 Heat exchanger (radiator)
107 1st pump (1st delivery device)
108 Second pump (second transmitter)
109 Hot water storage tank 110 Controller 111 Package 112 Raw material gas supply (raw material supply)
112a Booster pump 112b Flow control valve 113 Third pump 114 First condenser 114a Primary flow path 114b Secondary flow path 115 Second condenser 115a Primary flow path 115b Secondary flow path 116 Selective oxidation air supply 117 Combustion air supply 118 Inverter 119 Ventilation fan 120 Remote control (stop operation device)
120a Display unit 120b Key operation unit 121 Radiator (cooler)
140 Combustible gas sensor 141 Ignition detector 142 CO sensor 143 Temperature detector 144 Temperature detector 145 Temperature detector 146 Temperature detector 147 Temperature detector 206 Switcher 207 Bypass path

Claims (9)

A reformer that generates a hydrogen-containing gas by a reforming reaction using a raw material, a combustor that heats the reformer, a combustion air supplier that supplies combustion air to the combustor, and a controller; A hydrogen generator comprising:
A stop operator for stopping the operation of the hydrogen generator by an input operation by an operator;
The controller is configured so that the cooling amount of the hydrogen generating device in the stop processing by the input operation to the stop operating device by the operator is larger than the cooling amount of the hydrogen generating device in the normal stop processing. A hydrogen generator that controls the combustion air supply.   The controller supplies the combustion air supply device so that the cooling amount of the hydrogen generator in the stop process by the input operation is larger than the cooling amount of the combustor in the case of performing the normal stop process. The hydrogen generation apparatus according to claim 1, wherein at least one of an operation time and an operation amount is controlled.   The controller is configured to control the operation amount of the combustion air supply unit in the stop process by the input operation to be larger than the operation amount of the combustion air supply unit in the normal stop process. The hydrogen generation device according to claim 2, wherein the hydrogen generation device is configured to increase a cooling amount.   The controller controls the combustor so as to increase an operation time of the combustion air supply unit in the stop process by the input operation rather than an operation time of the combustion air supply unit in the normal stop process. The hydrogen generator according to claim 2, wherein the hydrogen generator is configured to increase a cooling amount.   The controller controls the combustion air supply device so that the temperature of the hydrogen generator when the stop process is completed by the input operation is lower than the temperature of the hydrogen generator when the normal stop process is completed. The hydrogen generator according to claim 1, which is controlled.   The controller is configured to permit the start-up process of the hydrogen generator in a state where the temperature of the hydrogen generator is higher in the case of the normal stop process than in the case of the stop process by the input operation. The hydrogen generator according to claim 1, wherein   The controller forcibly sets the operation amount of the combustion air supply device to a predetermined operation amount larger than the operation amount of the combustion air supply device during rated operation of the hydrogen generator in the stop process by the input operation. The hydrogen generator according to claim 1, wherein the combustion air supplier is controlled so as to be increased. A sealing device for making the gas flow path including the reformer a closed space;
When the pressure in the closed space formed by the sealer decreases, the hydrogen generation device opens the sealer and performs a supplementary pressure process for supplying gas into the gas flow path. Configured,
2. The hydrogen generator according to claim 1, wherein the controller is configured to increase the frequency of the supplementary pressure process in the stop process by the input operation rather than in the normal stop process. A hydrogen generator according to claim 1;
A fuel cell system comprising: a fuel cell that generates power using a hydrogen-containing gas supplied from the hydrogen generator.

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