JP3465198B2 - Method of operating a chemical reaction vessel at normal temperature and method of lowering the temperature of a fuel cell power plant - Google Patents

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a chemical plant having a single or a plurality of chemical reaction vessels, in order to reduce the loss of waiting time until the start of maintenance after the plant shutdown operation. Method and fuel cell power plant
Regarding the temperature decrease method .

[0002]

2. Description of the Related Art Japanese Patent Application Laid-Open No. 58-220907 discloses
In the forced cooling of the steam turbine, a method to effectively cool the turbine by reversely changing the gas flow direction inside the turbine to that under load so as not to damage the equipment is described. However, the technology described here is a general cooling method or normal temperature in a system having a reaction field in a container and a plurality of process input / output systems for the purpose of promoting or suppressing the reaction, such as a chemical reaction container. It does not give a solution as a slicing operation method.

Further, in Japanese Patent Laid-Open No. 3-276574, a reformer burner exhaust gas is swiftly circulated in a fuel cell power plant by circulating the exhaust gas cooled by a purge gas cooler to the reformer when the plant is cooled. It is disclosed that the system can be cooled.

[0004]

In the chemical industry, hydrogen gas production apparatus, fuel cell power plant, etc., which utilize ordinary chemical reaction processes, it is necessary to increase the chemical reaction rate to increase the yield. It is common sense that the temperature is generally raised to a temperature suitable for reaction control. However, the reaction temperature is often in the range of several hundreds of degrees higher than room temperature, and when maintenance or maintenance is required after operation is stopped, the temperature of the equipment is the temperature at which maintenance work can be performed with natural heat radiation. Generally, the waiting time until the temperature reaches room temperature is on the order of several days to a week, and the time loss is large, which is one of the factors that lowers the plant utilization rate.
In many chemical reactions, combustion is used as a heat source for the reaction, and in that case, purging operation after extinction of the combustion part, gas replacement operation, etc. are required to lower the temperature to a room temperature level. However, even if natural heat is released after the gas is filled for the above gas replacement, or even if forced cooling is performed at that time, there is an increase in costs such as a compressor as an additional pressurizing source, and an increase in the number of cylinders to cover the gas consumption. There was a factor, and there was a difficulty in clearing the circumstances around it. In addition, forced cooling in the process of reaching from the high temperature region to the normal temperature region also causes a temperature difference in the parts carelessly. Therefore, the thermal stress cannot be managed well and fatigue of the member and excessive thermal stress There was a problem that it contained a fatal problem of occurrence.

Further, the technique described in Japanese Patent Laid-Open No. 3-276574 uses exhaust gas cooled by a purge gas cooler, and has a drawback that extra equipment is required.

An object of the present invention is to reduce the standby time loss for cooling equipment in a chemical plant having a single or a plurality of chemical reaction vessels until the maintenance after the plant shutdown operation is started. Further on it is to propose a specific method to achieve the object of the fuel cell power generation system.

[0007]

[Means for Solving the Problems] The above object, compared to room temperature, intended for chemical reaction vessel in a chemical plant that utilizes a chemical reaction which is operated at high or low temperature region, usually
Used to supply and discharge chemical reaction groups to the chemical reaction vessel during operation.
Preliminarily install these pipes and chemical reaction vessels in the pipes used.
Used for said discharge so as to form a circulation channel containing
Piping and piping used for supply via a heat exchanger
To keep the room temperature after operation of the chemical reaction vessel
At the time of operation, a cooling or heating medium is passed through the circulation channel.
At the same time, the heat recovered in the cooling or heating medium is
It can be released to the outside of the system via a heat exchanger installed in the storage conduit.
It is achieved by the.

The above-mentioned problems are caused by the cathode gas outlet side of the fuel cell.
And the cathode gas inlet side of the cathode exhaust gas.
A part of the fuel cell is recycled to the fuel cell through a regulating valve.
Sword gas blower and first conduit on the cathode gas outlet side
Cathode that is communicated via the
A turbo compressor that compresses air using exhaust gas as a driving fluid
And the air compressed by the turbo compressor
The fuel cell caustic via the first valve and the regulating valve
A second pipeline for supplying gas to the gas inlet side, and a second pipeline for the second pipeline.
Between the turbo compressor and the first valve, the first
And a third conduit provided so as to communicate with the first conduit.
Reactions after Power Generation Stops at Naruto Fuel Cell Power Plant
In the case of lowering the temperature of the section, after the power generation is stopped, the first
Close the valve, operate the cathode gas blower, and stop.
From the turbo compressor to the third line and the first line
Air is sucked in through the conduit of
Mixed gas created by sucking gas from the cathode gas outlet of the pond
Part of this is circulated to the cathode of the fuel cell and the remaining mixture
It is achieved by discharging the combined gas to the outside of the system through the second conduit .

[0009]

In the present invention, a system for injecting a reactive group is utilized to promote the temperature difference between the heat generated by the reaction and the outside air caused by heat dissipation to the room temperature level after the reaction in the chemical reaction container is completed. Further, by controlling the temperature so that the temperature change rate falls within the limit value of the temperature change rate allowed by the chemical reaction container or its peripheral equipment, damage to the equipment can be prevented without giving a rapid temperature change to the equipment.

In the fuel cell power generation plant, when the temperature of the cell chemical reaction unit is lowered after the power plant is stopped, a forced circulation flow of a cooling medium is applied to the cell chemical reaction unit by using a rotary machine for recycling cathode gas. It is sent and the temperature reduction of the battery chemical reaction part is promoted.

[0011]

BEST MODE FOR CARRYING OUT THE INVENTION Embodiments of the present invention will be described below with reference to the drawings. FIG. 12 schematically shows an example of a general overall configuration of a chemical reaction plant which is the subject of the present invention. The illustrated chemical reaction plant is a source for supplying the chemical reaction group A.
Source 17B for supplying the reactive group from 17A and the chemically reactive group B
The reaction groups from the above are injected into the chemical reaction vessel 13 through the reaction group flow paths 18A and 18B.
Blowers 15A and 15B are respectively provided in the reaction group flow path on the outlet side of 7B, and the reaction group is pushed into the chemical reaction container 13 which is the chemical reaction field. Valves 16A and 16B are provided in the reaction group flow paths 18A and 18B between the supply source and the blower for controlling the flow rate of the reaction group. The reaction in the chemical reaction vessel 13 is, for example,

[0012]

[Equation 1] It is described by a reaction formula such as. The reaction product in the chemical reaction vessel 13 passes through the reaction product flow path 19 and the reaction product tank.
Recovered in 11. Here, blowers 15A and 15B and valves 16A and 16B
Is an accessory that is always used during normal operation.

The point of interest of the present invention is that the retained heat generated during the chemical reaction in the reaction vessel in the chemical reaction system can reasonably speed up the time required for the temperature change to the normal temperature at the time of normal natural heat dissipation after the operation is completed. It is devised so that the temperature level is the same as the above, and will be specifically described below.

FIG. 1 is a reference for explaining the principle of the present invention .
Here is an example: The figure shows that a new gas suction for heat exchange at normal temperature is newly introduced into the reaction group flow paths 18A, 18B for injecting the reaction groups from the chemical reaction group supply sources 17A, 17B into the reaction vessel 13 of the plant shown in FIG. The parts 23A and 23B are connected via the suction control valves 24A and 24B, and the reaction product flow path 19 is connected to the normal temperature heat exchange gas discharge part 21 via the discharge control valve 22. The gas suction portions 23A and 23B for heat exchange at room temperature are connected to the reaction base flow paths 18A and 18B on the upstream side of the blowers 15A and 15B. Inhalation control valve
24A and 24B are for controlling the gas flowing into the reaction base flow paths 18A and 18B from the gas intake portions 23A and 23B for heat exchange at room temperature, and the discharge control valve 22 is for heat exchange at room temperature from the reaction product flow path 19. It controls the gas flowing out to the use gas discharge part 21.

When maintenance of the chemical reaction vessel 13 is performed after the operation of the chemical reaction vessel 13 is completed in the apparatus having the above-mentioned configuration, the cooling medium (operating temperature is higher than normal temperature) from the heat exchange gas suction portions 23A and 23B at normal temperature. When the temperature is low, the temperature raising medium) is injected into the reaction vessel 13 via the reaction base flow paths 18A and 18B, so that the internal temperature of the chemical reaction vessel 13 is accelerated.
In addition, the injected cooling or temperature raising medium (hereinafter referred to as normal temperature medium) is recovered through the heat exchange gas discharge part 21 at normal temperature. The emission control valve 22 regulates the emission of the recovered gas. Here, valve 16A, suction control valve 24A, valve 16B
The suction control valve 24B and the suction control valve 24B have a degree of opening (opening and closing) so that they do not open at the same time in order to prevent mutual gas mixture.
Control is performed.

FIG. 2 shows a first embodiment of the present invention. Figure 1
Is not connected to the inlet side of the heat exchange gas suction portions 23A and 23B for normal temperature and the outlet side of the normal temperature heat exchange gas discharge portion 21, but in the first embodiment shown in FIG. The difference is that the inlet sides of the hour heat exchange gas suction portions 23A and 23B and the outlet side of the normal temperature heat exchange gas discharge portion 21 are connected . Tsuma
2 , in FIG. 2, the gas suction part 23 for heat exchange at room temperature is used.
No special equipment is provided to serve as A, 23B and the heat exchange gas discharge part 21 at room temperature, and the outlet side of the discharge control valve 22 and the inlet side of the suction control valves 24A, 24B are connected by the medium flow path 20. ing. In the figure, a heat exchanger 28 installed in the medium flow path 20.
Represents that the ambient temperature medium exchanges heat with the outside air while passing through the medium flow path 20, and releases the heat to the air or absorbs the heat from the air. Of course, when the medium flow path 20 is not long enough to release or absorb the heat of the ambient temperature medium due to the arrangement of the plant equipment, the heat exchanger may be actually provided. In any case, it is possible to shorten the time for shifting the temperature inside the chemical reaction container 13 to the normal temperature range.

[0017] Figure 3 and 4, a reference example in which a chemical reaction vessel in reference example of FIG. 1 is a multi-sequenced, both
The embodiment of FIG. 2 can be applied . FIG. 3 shows the flow of reactive groups during normal operation of the device. During normal operation, the suction control valves 24A and 24B are closed in order to prevent the room temperature medium from being injected into the reaction vessel from the heat exchange gas suction portions 23A and 23B, and
The discharge control valve 22 is closed to prevent the reaction group from flowing into the heat exchange gas discharge part 21. FIG. 4 shows the flow of the medium when the reaction container 13 is brought to room temperature after the operation is completed.
The valves 16A and 16B are closed to prevent injection of the reactive groups from the chemically reactive group supply sources 17A and 17B into the reactive group flow paths 18A and 18B, and the suction control valves 24A and 24B are opened to introduce the temperature-warming medium into the reaction vessel. ,
Further, the valve 12 is closed to prevent the ambient temperature medium from flowing into the reaction product tank 11, and the discharge control valve 22 is opened to guide the ambient temperature medium to the heat exchange gas discharge portion 21. When actually injecting the ambient temperature medium, a procedure such as purging the reaction group in the reaction group channel may be required.

Liquids, inert gases, air, and the like are considered as the temperature-increasing medium to be injected to bring the chemical reaction vessel to room temperature, and these are basically substances that do not impair the original purpose of the chemical reaction plant. There is no problem with.

As a method for injecting a medium for cooling or heating,
The blowers 15A and 15B shown in Fig. 1 that were used during normal operation are diverted and circulated and injected into the reaction vessel as shown in Fig. 2 , or a fan or blower dedicated to the injection of the cooling / heating medium is used. Circulating injection as shown in FIG. 2 by providing a rotary machine, but a temperature measuring means not shown in FIGS. 1 to 4 so that the chemical reaction container or peripheral equipment thereof is within the limit value of the rate of temperature change allowed. The blower 15A, 15B or the suction control valve 24A, 24B is adjusted by a temperature control mechanism (not shown). Further, the operation control of the rotating machine is performed within an allowable range in which the rotating machine is not mechanically damaged by the relative pressure difference inside the reaction vessel or inside and outside.

In the reference example shown in FIG. 5, the gas discharge portion 21 for heat exchange at room temperature described in FIGS.
FIG. 13 is a diagram showing a case in which 11 is also used.

Further, in another reference example shown in FIG.
It is the figure which showed the case where only one of the reaction group flow paths 18A and 18B is used to accelerate the temperature of the chemical reaction vessel to the room temperature level, as compared with the reference example shown in FIGS. For example, when using the B line (the unused line in the broken line) causes a problem of flammable gas or toxic gas leakage, when the normal temperature medium is injected only in the A system without utilizing the system. Is shown.

FIG. 7 shows a characteristic part of the second embodiment. When the temperature of the outer surface of the chemical reaction container is largely separated from the outside air temperature, convection of the outside air may be used to accelerate heat exchange on the outer surface. That is, when the chemical reaction container is installed indoors, the intake port 71 is provided at a lower position of the building, preferably lower than the chemical reaction container, as shown in FIG. The exhaust port 72 is provided at a higher position than that, and heat exchange is promoted by convection of the outside air to shorten the normal temperature time.

FIG. 8 shows a characteristic part of the third embodiment. The present embodiment is an example in which an outer container 81 is provided outside the reaction container 13 in order to effectively perform heat radiation on the outer surface of the container. Figure 8
As shown in, the surface area of the inner chemical reaction vessel 13 is increased, and after the operation is completed, the outer vessel 81 is removed to promote heat exchange on the outer surface of the inner reaction vessel.
Further, with this configuration, it is possible to improve heat retention during normal operation. Further, it becomes possible to increase the safety against leakage of flammable gas and toxic gas.

[0024] As in the third embodiment, the chemical outer container 81 on the outside of the reaction vessel 13 is provided another embodiment in the outer container enclosing the gas is interchangeable with the container outside with reference to FIG. 9 Explain. The fourth embodiment shown in FIG. 9 (a) is a case where intake and exhaust ports can be provided in the upper and lower parts of the outer container.
In this case, when passing through the cooling medium, the upper port is used as an exhaust port. The convection is generated due to the difference in temperature with the gas outside the container, and the flow facilitates heat exchange on the outer surface of the reaction container 13. External gas as a refrigerant is introduced from the lower port. When passing through the temperature raising medium, the lower port is used as a discharge port to improve heat circulation and supply and discharge of the medium to promote heat exchange of the container.

FIG. 9B shows the fifth embodiment. In this embodiment, the forced circulation of the enclosed gas in the outer reaction vessel 81 promotes the normalization of the temperature of the reaction vessel 13, and the inlet and outlet of the enclosed gas are on opposite sides of the reaction vessel 13 at the bottom of the outer vessel 81. This is an example of providing and forcibly circulating .

A sixth embodiment shown in FIG. 9 (c) is a reaction vessel using the main process system shown in FIGS.
9 shows an example in which a method of feeding a room temperature medium into the chamber 13 and a method of promoting heat exchange on the outer surface of the reaction vessel 13 shown in FIG. 9B are combined.

Next, a seventh embodiment in which the present invention is applied to a molten carbonate fuel cell power generation system will be described.

FIG. 10 is a system diagram of the molten carbonate fuel cell power plant during normal operation. The molten carbonate fuel cell power plant shown in the figure has a reformer (reformer) 117, a fuel cell 111 connected to the reformer 117 via pipes 124 and 125, and a cathode on the cathode side of the fuel cell 111. A turbo compressor 115 having a drive fluid inlet side connected through an exhaust gas channel 118, a pipe line 120 connecting a discharge side of the turbo compressor 115 and a reformer 117 through a valve 119, and the cathode exhaust gas channel 118. A cathode blower 112 connected to the suction side, and a regulating valve 11 for connecting the discharge side of the cathode blower 112 and the cathode side of the electric battery 111.
The conduit 121 connected via 3 and the conduit 1 on the downstream side of the valve 119.
20 and a conduit 122 connecting the discharge side conduit 121 of the cathode blower 112 via a valve 114, a conduit 123 connecting the conduit 122 and the reformer 117, and a drive fluid inlet side of the turbo compressor 115. A conduit 126 connecting the cathode exhaust gas flow path 118 and the discharge-side conduit 120 of the turbo compressor 115,
An exhaust heat recovery boiler (HRSG) 116 connected to the driving fluid outlet side of the turbo compressor 115 via a pipe 127, and a pipe 1
It is configured to include a transmission line 129 connected to the fuel cell 111, and a pipe line 128 connecting the 27 and the pipe line 120 on the downstream side of the valve 119 to form a turbo compressor bypass system.

In the molten carbonate fuel cell power plant having the above structure, the process gas obtained by mixing the hydrocarbon fuel and steam is supplied to the reformer 117, where it is reformed into hydrogen, and the generated hydrogen passes through the pipe 124. Then, it is injected into the anode side of the fuel cell 111. In addition, the turbo compressor 115
The air compressed by is mixed with carbon dioxide supplied from the reformer 117 through the pipe 123 through the valves 119 and 114, and is injected into the cathode side of the fuel cell 111 through the adjustment valve 113. The gas on the anode side and the gas on the cathode side react electrochemically to generate electricity. Since the anode exhaust gas after the reaction contains 10% of hydrogen, the anode exhaust gas is sent to the reformer 117 via the pipe 125 and used as a fuel there. A part of the cathode exhaust gas of the fuel cell 111 is boosted by the cathode blower 112 through the cathode exhaust gas passage 118, is recycled to the fuel cell 111 through the adjusting valve 113, and the rest drives the turbine of the turbo compressor 115 and discharges it. It is discharged to the heat recovery boiler 116.

FIG. 11 shows the flow of each gas showing the case where the temperature inside the fuel cell is cooled by utilizing the cathode side system after the operation of the power plant is completed. After the operation ends, the turbo compressor 115 is stopped and the valve 119 is closed. By operating the cathode blower 112 , the outside air is taken in from the air intake of the turbo compressor 115, and is sent to the fuel cell 111 through the inside of the stopped turbo compressor 115, the pipelines 126, 118, 121, and the adjusting valve 113. Due to this air flow, the cathode side system and the fuel cell 111 are cooled by the forced circulation flow. Further, it goes without saying that the cooling effect is enhanced by forming a mixed portion of the outside air and the cooling medium.

Further, a temperature measuring device 101 at the cathode side inlet and outlet of the fuel cell 111 and a pressure detector 1 for detecting the inter-electrode differential pressure.
02 is provided, and a control means (not shown) for controlling the valve 113 or the cathode blower 112 by using the output temperature signal and pressure signal as input is provided. This control means controls the valve 113 so that the pressure / temperature change rate of the fuel cell due to the circulating flow sent to the fuel cell does not deviate from the above limit value based on the limit value of the pressure resistance inside the cell and the limit value of the temperature change rate. Or mosquito
To control the Sword blower 112. Therefore, even after forcibly cooling the fuel cell 111 or other equipment after the operation of the power plant, it is possible to prevent the fuel cell 111 and other equipment from abruptly changing the temperature and causing excessive thermal stress. It became possible. In addition, as the operation end of the control means,
In addition to the valve 113, the valve 114 may be added. Further, the limit value of the temperature change rate may be changed at the electrolyte melting point / freezing point temperature as a boundary.

[0032]

According to the present invention, after the reaction operation of the chemical reaction container is completed, the temperature in the container is rapidly changed to the normal temperature level, so that the maintenance and inspection of the chemical reaction container can be started earlier. For example, in a chemical reaction plant such as a fuel cell plant, useless waiting time can be shortened.

[Brief description of drawings]

FIG. 1 is a system diagram of a reference example for explaining the principle of the present invention.

FIG. 2 is a system diagram showing a first embodiment of the present invention.

FIG. 3 is a system diagram of a reference example to which the present invention can be applied .

FIG. 4 is a system diagram showing an example of opening and closing a valve in the reference example shown in FIG.

FIG. 5 is a system diagram of another reference example to which the present invention can be applied .

FIG. 6 is a system diagram of still another reference example to which the present invention can be applied .

FIG. 7 is a conceptual diagram showing a characteristic part of a second exemplary embodiment of the present invention.

FIG. 8 is a conceptual diagram showing a characteristic part of a third exemplary embodiment of the present invention.

FIG. 9 is a fourth to sixth modification of the third embodiment of the present invention.
It is a conceptual diagram which shows the characteristic part of an Example .

FIG. 10 is a system diagram of a fuel cell power plant during normal operation.

11 is a diagram showing a seventh embodiment in which the present invention is applied to the fuel cell power plant shown in FIG.

FIG. 12 is a system diagram showing a configuration example of a general chemical reaction plant to which the present invention is applied.

[Explanation of Codes] 11 Reaction Product Recovery Tank 12
Valve 13 Chemical reaction vessel 14
A, 14B Regulator valve 15A, 15B Blower 16
A, 16B Valve 17A, 17B Reactive group supply source 18
A, 18B Reaction group flow path 19 Reaction product flow path 20
Medium flow path 21 Heat exchange gas discharge part at normal temperature 22
Emission control valves 23A, 23B Gas suction part for heat exchange at normal temperature 24
A, 24B Intake control valve 28 Heat exchanger 71
Intake port 72 Exhaust port 81
Outer container 101 Temperature measuring device 111
Fuel cell 112 Cathode blower 113
Regulator valve 114 Valve 115
Turbo compressor 116 Exhaust heat recovery boiler 117
Reformer 118 Cathode exhaust gas passage 119
Valve 120-128 Pipeline 129
power line

Front page continuation (72) Inventor Tadashi Yoshida 3-1-1, Sachimachi, Hitachi City, Ibaraki Hitachi Ltd. Hitachi Factory (72) Inventor Nobuhiro Kiyoki, 502 Kandachimachi, Tsuchiura, Ibaraki Hitachi Machinery Co., Ltd. In the laboratory (56) Reference JP 63-254677 (JP, A) JP 60-65471 (JP, A) JP 61-179067 (JP, A) JP 62-259356 (JP, A) ) Japanese Patent Laid-Open No. 61-176077 (JP, A) Actual development 61-204365 (JP, U) (58) Fields investigated (Int.Cl. ⁷ , DB name) B01J 19/00 H01M 8/00-8 / twenty four

Claims (13)

(57) [Claims] 1. A method for normalizing a temperature of a chemical reaction container in a chemical plant that uses a chemical reaction operating in a high temperature or low temperature region as compared with normal temperature, in which a chemical reaction group is supplied to and discharged from the chemical reaction container during normal operation. The pipes used for the exhaust pipe and the pipe used for the supply in advance so as to form a circulation flow path including the pipes and the chemical reaction vessel through a heat exchanger. The cooling or heating medium is passed through the circulation channel during normal temperature operation after the end of the operation of the chemical reaction container, and the heat recovered in the cooling or heating medium is transferred to the pipe. A method for normalizing the temperature of a chemical reaction vessel, characterized in that the chemical reaction vessel is discharged to the outside of the system through a heat exchanger installed in the passage. 2. The method for normalizing the temperature of a chemical reaction container according to claim 1, wherein an inert gas and / or air is used as a cooling or heating medium. . 3. The method for normalizing the temperature of the chemical reaction container according to claim 1 or 2, wherein the chemical reaction container has an outside and an outside.
A container is provided, and intake and exhaust ports are formed in the upper and lower parts of the outer container,
When using a cooling medium uses mouth provided above the outer container as an exhaust port, also when using the medium for heating the mouth that is provided under the outer container and an exhaust port
A method for operating a chemical reaction container at room temperature, which is characterized by using the same. 4. The method for normalizing the temperature of a chemical reaction container according to claim 1, wherein a cooling or heating medium is used for driving a fluid used for feeding a reaction group during normal operation. The method for normalizing the temperature of a chemical reaction container, characterized in that the chemical reaction container is fed through a rotary machine. 5. The method for normalizing the temperature of a chemical reaction container according to claim 4, wherein the temperature of the chemical reaction container and / or the cooling or temperature raising medium fed into the chemical reaction container is detected, and the detected temperature is detected. Is used to control the temperature and / or the flow rate of the cooling or heating medium, and a method for normalizing the temperature of the chemical reaction container. 6. The method for normalizing the temperature of a chemical reaction container according to claim 4, wherein the machine is operated by the internal pressure of the chemical reaction container or the relative pressure difference between the inside and the outside of the chemical reaction container caused by passing a medium for cooling or heating. A method for operating a chemical reaction container at room temperature, which comprises operating a rotating machine within an allowable range that does not cause mechanical damage. 7. The method for normalizing the temperature of a chemical reaction container according to claim 1, wherein the chemical reaction container is installed indoors.
If we, the normal temperature of operation of the completion of the run of the chemical reaction vessel, a building top and sides or bottom which is formed in the ventilation holes give rise to convection and building external air to room temperature reduction by utilizing convection A method for operating a chemical reaction container at room temperature, which is characterized in that 8. The method for normalizing the temperature of a chemical reaction container according to claim 1, wherein the chemical reaction container is duplicated in advance, and the chemical reaction container is operated at a normal temperature after completion of operation of the chemical reaction container. A method for normalizing a temperature of a chemical reaction container, which comprises removing an outer container. 9. The method for normalizing the temperature of a chemical reaction container according to claim 1, wherein the chemical reaction container is duplicated into an inner container and an outer container, and the outer surface area of the inner container is increased by providing fins or the like. A chemical reaction container characterized by the above. 10. A cathode gas outlet side and a cathode gas inlet side of a fuel cell are connected to control a part of cathode exhaust gas.
Cathode gas recycled to the fuel cell through a valve
A sub-blower and a first conduit on the cathode gas outlet side
Cathode exhaust gas that is communicated and supplied through the pipe
A turbo compressor that compresses air as the driving fluid,
Air compressed by the turbocompressor has a first valve
And the cathode gas of the fuel cell through the adjusting valve
And a second pipe line for supplying the second pipe line
The first line between the vocompressor and the first valve
In the method of lowering the temperature of the electrochemical reaction part of the fuel cell power plant having the third conduit provided so as to communicate with, after the power generation is stopped, the first valve is closed, The cathode gas
Operate the sub-blower and stop the turbo compressor.
Intake air from the chamber through the third and first conduits
Gas from the cathode gas outlet side of the fuel cell.
A part of the mixed gas formed by sucking the gas
And the remaining mixed gas is circulated through the second conduit.
And releasing it outside the system . 11. The method for lowering the temperature of a fuel cell power plant according to claim 10 , wherein the fuel cell is circulated to the cathode of the fuel cell.
A method for lowering the temperature of a fuel cell power plant, wherein the mixed gas to be circulated is introduced into the fuel cell by controlling the flow rate of the mixed gas based on a condition of pressure resistance inside the cell and limitation of a temperature change rate. 12. The temperature decreasing method for a fuel cell power plant according to claim 10 , wherein the fuel cell unit
The flow rate of the mixed gas circulated in the sword is controlled by the rotation control of the rotating machine or the control valve in the cathode gas recycle system, or the control valve on the external supply / discharge system as the operating end, and the differential pressure between the electrodes of the fuel cell and / or A temperature decreasing method for a fuel cell power plant, wherein the temperature difference between the cell inlet and outlet and / or the cell outlet temperature and / or the cell inlet temperature is controlled as a controlled variable. 13. The temperature decreasing method for a fuel cell power plant according to claim 10 , wherein the fuel cell is a molten carbonate type, and the temperature change rate is limited with respect to the electrolyte melting point / freezing point temperature. A method for lowering the temperature of a fuel cell plant, which comprises changing a value.