JPH08195214A - Phosphoric acid fuel cell generating system - Google Patents

Abstract

PURPOSE: To readily hold catalyst temperature at the appropriate temperature so as to reduce the concentration of carbon monoxide in reformed gas without enlarging a system by providing a cooling pipe through which high-temperature water flows to a CO modifier and another cooling pipe through which low- temperature water flows to the CO modifier. CONSTITUTION: In a phosphoric acid fuel cell generating system, a cooling water supply pipe, leading to a CO converter 4 converting carbon monoxide in reformed gas into carbon dioxide, comprises two systems, i.e., a high- temperature cooling water supply line 13a and a low-temperature cooling water supply line 13b. The high-temperature cooling water supply line 13a is connected to a steam separator 6 via a pump 7 to supply high-temperature water (about 170 deg.C) to a high-temperature water cooling pipe 4c. The lowtemperature cooling water supply line 13b is connected to a higher heat recovery system 10 to supply low-temperature water (about 90 deg.C) to a low-temperature water cooling pipe 4d. Thus the temperature of a low-temperature CO modifying catalyst 4a can be readily held at the appropriate temperature.

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a phosphoric acid type fuel cell power generator for obtaining electric power by acting a reformed gas and an oxidizing gas.

[0002]

2. Description of the Related Art FIG. 7 is a system diagram of a conventional phosphoric acid fuel cell power generator shown in Japanese Patent Laid-Open No. 6-52880. In FIG. 7, 1 is a reformer for reacting fuel with steam to obtain hydrogen, and 2 and 3 are heat exchanges between the gas reformed by the reformer 1 (hereinafter referred to as reformed gas) and the fuel. A heat exchanger 4 for carrying out and preheating the fuel is a CO shifter for converting carbon monoxide contained in the reformed gas reformed by the reformer 1 into hydrogen, and is filled with a low temperature CO shift catalyst 4a. It is composed of a container 4b and a cooling pipe 4C for flowing cooling water for removing reaction heat. Reference numeral 5 is a phosphoric acid type fuel cell that obtains a direct current from hydrogen in the reformed gas and air as an oxidizing gas, and 6 supplies steam to the reformer 1 and cools the fuel cell 5 and the CO shift converter 4. A steam separator for obtaining high temperature water, a pump 7 for circulating cooling water for cooling the fuel cell 5 and the CO shifter 4, a desulfurizer 8 for removing sulfur contained in the fuel, and a fuel cell 5 for 9 An orthogonal converter 10 for converting the generated DC current into AC power is a high-level heat recovery device for recovering heat from the steam taken out from the steam separator 6. Reference numeral 11 is a water treatment device for condensed water. Reference numeral 12 is a cooling water supply pipe for the CO shift converter 4. 1
Condensers 4a and 14b are a combustion gas condenser and a reformed gas condenser, respectively.

Next, the operation will be described. The reformer 1 is
A reformed gas, which is a hydrogen-rich gas, is produced by using hydrocarbons such as LNG and steam supplied from the steam separator 6 as raw materials. This reformed gas contains a considerably large amount of carbon monoxide, and this carbon monoxide becomes a catalyst poison to the fuel cell 5. Therefore, it is necessary to reduce the carbon monoxide concentration (about 1% or less), and the CO shift converter 4 is used. CO transformer 4
The reaction inside is

CO + H ₂ O → CO ₂ + H ₂ (1)

This is an exothermic reaction represented by the formula (1) and has the effect of reducing the carbon monoxide concentration and simultaneously producing H ₂ . The reformed gas is cooled to the operating temperature (170 ° C. to 300 ° C.) of the low temperature CO shift catalyst in the CO shift converter 4 by the heat exchangers 2 and 3, and then introduced into the CO shift converter 4. The inlet of the reformed gas of the CO shift converter 4 is connected to the outlet of the heat exchanger 3, and the outlet of the reformed gas of the CO shift converter 4 is connected to the inlet of the fuel electrode 5a of the fuel cell 5. The heat of reaction of the fuel cell 5 is absorbed by the high temperature water from the steam separator 6 and introduced into the steam separator 6. A part of these heats is used to generate the steam supplied to the reformer 1 from the high temperature water. The remaining heat is taken out as steam and recovered by the high-level heat recovery device 10.

The cooling water flowing through the cooling water supply pipe 12 of the CO shift converter 4 is a mixed fluid of high temperature water which is the supply water from the steam separator 6 and low temperature water which is the supply water from the high level heat recovery device 10. Is. The hot water from the steam separator 6 is circulated by the pump 7. The high-temperature water in the steam separator 6 serves as a cooling water for the fuel cell 5 and a steam supply source to the reformer 1, so that its temperature is maintained at about 170 ° C. The low-temperature water from the high-order heat recovery device 10 consists of water obtained by condensing the excess steam of the steam separator 6 and has a temperature of about 90 ° C. This condensed water flow rate has an upper limit, and the steam separator 6
Since its flow rate is smaller than that of the high temperature water from No. 1, the temperature of these mixed fluids is usually about 150 to 165 ° C.
The cooling water composed of the mixed fluid thus obtained is introduced into the CO shift converter 4, absorbs the heat generated in the low temperature CO shift catalyst 4a, and then is sent to the steam separator 6. Further, the condensed water collected by the condensers 14a and 14b is used as the water treatment device 11
Is supplied to the water vapor separator 6 via.

[0007]

C at the exit of the CO transformer 4
In order to reduce the O concentration, it is necessary to use the catalyst as effectively as possible. Regarding the reaction in the low-temperature CO shift catalyst 4a, when the temperature is low, the activity of the catalyst is low and the reaction rate becomes low. It has the characteristic that it does not drop much. Therefore, there is an optimum temperature depending on the concentration of carbon monoxide in the reformed gas, and the CO conversion reaction has a temperature that maximizes the CO conversion reaction as a whole.
It is necessary to construct a transformer. However, in the conventional phosphoric acid fuel cell power generator, the high-temperature water and the low-temperature water are mixed and supplied through one cooling water supply pipe, so that CO
It was difficult to obtain a temperature and temperature distribution that would allow the transformation reaction to proceed to the maximum.

For example, FIG. 8 shows a catalyst temperature distribution (dotted line) of a conventional CO shift converter. The figure also shows the ideal temperature distribution (solid line) that maximizes the amount of reaction per unit volume of the catalyst that is analytically obtained. The conditions at this time are defined as follows.

First, since the maximum operating temperature of the low temperature CO shift catalyst is about 300 to 320 ° C., the upper limit of the temperature is 3
It was set to 00 ° C. Secondly, in the conventional CO transformer,
Since the temperature of the catalyst is increased due to insufficient cooling at the inlet, it is assumed that the plant is configured so that the inlet temperature is 250 ° C. Thirdly, the fuel electrode inlet temperature of the fuel cell also has an upper limit, and it is necessary to suppress the temperature to about 200 ° C. Therefore, the temperature of the CO transformer outlet is set to 190 ° C here.

FIG. 9 is a diagram showing the distribution of the heat flux from the catalyst to the cooling water under the condition of FIG. 8. In order to achieve the optimum temperature distribution, in order to achieve the optimum temperature distribution, the vicinity of the gas inlet and the vicinity of the outlet are compared with the conventional example. It is necessary to take a large heat flux at. In particular, at the CO converter outlet, the temperature difference between the cooling water temperature (minimum 150 ° C) and the catalyst temperature (190 ° C) is small. Therefore, in order to obtain a large heat flux, the cooling pipes should be densely laid and the heat transfer area However, there is a problem in that the size of the device is increased and the cost is increased.

The present invention has been made to solve the above-mentioned problems. By supplying high-temperature water and low-temperature water to a CO transformer by separate cooling pipes, CO
Improving the temperature distribution of the shift converter catalyst layer,
The purpose is to easily reduce the O concentration. Another object of the present invention is to improve the temperature distribution of the CO shift converter catalyst layer and reduce the CO concentration at the CO shift outlet.

[0012]

A phosphoric acid fuel cell power generator according to claim 1 of the present invention is a cooling pipe through which high-temperature water supplied from a steam separator flows and low-temperature water supplied from a high-level heat recovery device. The CO transformer is configured so as to have both cooling pipes through which the CO flows.

A phosphoric acid fuel cell power generator according to a second aspect of the present invention has both a cooling pipe through which high temperature water supplied from a steam separator flows and a cooling pipe through which low temperature water supplied from a condenser flows. Thus, the CO transformer is configured.

A phosphoric acid fuel cell power generator according to a third aspect of the present invention is the phosphoric acid fuel cell power generator according to the first or second aspect, wherein a cooling pipe through which low temperature water flows is provided inside the CO transformer. , And are densely arranged near the inlet and outlet of the reformed gas.

A phosphoric acid fuel cell power generator according to a fourth aspect of the present invention is the phosphoric acid fuel cell power generator according to any one of the first to third aspects, wherein at the time of low load power generation, C
It is configured to shut off the low temperature water supplied to the O-transformer.

A phosphoric acid fuel cell power generator according to a fifth aspect of the present invention is the phosphoric acid fuel cell power generator according to any one of the first to fourth aspects, wherein the reformed gas temperature sensor is provided at the CO transformer outlet. Or a catalyst temperature sensor is also provided in the CO shift converter, and the supply amount of low-temperature water supplied to the CO shift converter is adjusted according to the temperature.

A phosphoric acid fuel cell power generator according to claim 6 of the present invention is the phosphoric acid fuel cell power generator according to any one of claims 1 to 5, wherein a carbon monoxide concentration sensor is provided at the CO transformer outlet. Is provided, and the supply amount of low-temperature water supplied to the CO shift converter is adjusted according to the concentration.

[0018]

According to the phosphoric acid fuel cell power generator of claim 1 of the present invention, the high-temperature water introduced from the steam separator as the cooling water for the CO shift converter and the low-temperature water from the high-level heat recovery device are separately provided. To facilitate the improvement of the temperature and temperature distribution of the catalyst in the CO shift converter so as to promote the catalytic reaction.

According to the phosphoric acid fuel cell power generator of claim 2 of the present invention, the high temperature water introduced from the steam separator as the cooling water for the CO shift converter and the low temperature water from the condenser are separately supplied. By doing so, it becomes easy to improve the temperature and temperature distribution of the catalyst in the CO shift converter so as to promote the catalytic reaction.

According to the phosphoric acid fuel cell power generator of claim 3 of the present invention, the cooling pipe for low-temperature water in which the low-temperature water flows is CO
Inside the shift converter, they are densely arranged near the inlet and outlet of the reformed gas, so that the catalyst in those portions can be sufficiently cooled, and the temperature distribution of the catalyst in the CO shifter accelerates the reaction. Thus, the concentration of carbon monoxide in the reformed gas at the outlet of the CO shift converter is reduced.

According to the phosphoric acid fuel cell power generator of claim 4 of the present invention, since low-temperature water does not flow at the time of low-load power generation, CO due to excessive cooling of the low-temperature CO shift catalyst
It is possible to prevent an increase in the carbon monoxide concentration in the reformed gas at the outlet of the shift converter.

According to the phosphoric acid fuel cell power generator of claim 5 of the present invention, the temperature of the reformed gas at the outlet of the CO shifter or the catalyst temperature in the CO shifter is measured, and the high-level heat recovery device is measured by the temperature. Alternatively, the heat exchange in the CO transformer can be optimally controlled by adjusting the flow rate of the cold water from the condenser.

According to the phosphoric acid fuel cell power generator of claim 6 of the present invention, the carbon monoxide concentration in the reformed gas at the outlet of the CO shift converter is measured, and the high-level heat recovery device or By adjusting the flow rate of cold water from the condenser, the heat exchange in the CO transformer can be optimally controlled.

[0024]

【Example】

Example 1. Hereinafter, Embodiment 1 of the present invention will be described with reference to FIG. 1, 2, 3, 4, 5, 6, 7,
8, 9, 10, 11, 14a, and 14b are the same as the conventional device shown in FIG. The cooling water supply pipe to the CO shift converter 4 has two systems, a high temperature cooling water supply pipe 13a and a low temperature cooling water supply pipe 13b. The high temperature cooling water supply pipe 13a is
It is connected to the water vapor separator 6 through a pump 7 and supplies high temperature water to the high temperature water cooling pipe 4c. The low-temperature cooling water supply pipe 13b is connected to the high-level heat recovery device 10,
The low temperature water is supplied to the low temperature water cooling pipe 4d.

Next, the operation will be described. According to the configuration of the first embodiment, the cooling water of the CO shift converter 4 has two systems, that is, the high temperature water from the steam separator 6 and the low temperature water from the high level heat recovery device 10. The hot water from the steam separator 6 is about 170
While the low-temperature water from the high-level heat recovery device 10 is supplied at about 90 ° C., while the low-temperature water is supplied to the CO shift converter 4 at about 90 ° C., the low-temperature water cooling pipe 4d and the low-temperature CO shift catalyst are used for this low-temperature water. The temperature difference with 4a is large, and the heat exchange in the CO shift converter 4 can be improved. On the other hand, the high temperature water from the steam separator 6 can promote the heat exchange of the low temperature CO shift conversion catalyst 4a while preventing the temperature drop of the low temperature CO shift catalyst 4a, and as a result, the catalyst temperature can be easily maintained at an appropriate temperature. Therefore, the carbon monoxide concentration in the reformed gas at the CO shifter outlet can be reduced without increasing the size of the device.

Example 2. Next, a second embodiment of the present invention will be described with reference to FIG. In FIG. 2, 1, 2, 3, 4,
5, 6, 7, 8, 9, 10, 11, 14a, 14b are
This is the same as the conventional device shown in FIG. The cooling water supply pipe to the CO shift converter 4 has two systems, a high temperature cooling water supply pipe 13a and a low temperature cooling water supply pipe 13c, and the high temperature cooling water supply pipe 13a is connected to the steam separator 6 through a pump 7. The high temperature water is supplied to the high temperature water cooling pipe 4c. The low-temperature cooling water supply pipe 13c is connected to the condensers 14a and 14b through the water treatment device 11, and the low-temperature water cooling pipe 4
Supply low temperature water to d.

Next, the operation will be described. According to the configuration of the second embodiment, the cooling water for the CO shift converter 4 is composed of the high temperature water from the steam separator 6 and the low temperature water from the condensers 14a and 14b.
Have a lineage. The hot water from the steam separator 6 is about 17
The CO converter 4 is supplied at 0 ° C. while the condenser 1 is supplied.
The low-temperature water supplied from 4a and 14b through the water treatment device 11 is supplied at about 90 ° C. for degassing (main carbon dioxide), so that the temperature difference with the catalyst is large, and The heat exchange can be improved. On the other hand, the high-temperature water from the steam separator 6 can promote the heat exchange of the CO shift catalyst 4a while preventing the temperature drop of the CO shift catalyst 4a, and as a result, the catalyst temperature can be easily maintained at an appropriate temperature. The carbon monoxide concentration in the reformed gas at the outlet of the CO shift converter can be reduced without increasing the size of the device.

Example 3. Next, a third embodiment of the present invention will be described with reference to FIG. In FIG. 3, 1, 2, 3, 4,
5, 6, 7, 8, 9, 10, 11, 13a, 13b, 1
4a and 14b are the same as those in the first embodiment (FIG. 1) described above. The cooling pipe 4d-1 for low temperature water in the CO transformer 4 is
The transformer 4 is densely arranged near the inlet and outlet of the reformed gas, and the other parts are sparsely arranged.

Next, the operation will be described. CO transformer 4
High temperature water flows through the high temperature water cooling pipe 4c, and low temperature water flows through the low temperature water cooling pipe 4d-1. As shown in FIG. 9, in order to optimize the catalyst temperature distribution, it is necessary to rapidly cool the catalyst at the reforming gas inlet and outlet of the CO shift converter 4.
The cooling pipe 4d-1 for low temperature water is densely arranged at the inlet and outlet of the reformed gas to achieve rapid cooling of the catalyst.

Example 4. Next, a fourth embodiment of the present invention will be described with reference to FIG. In FIG. 4, 1, 2, 3, 4,
5, 6, 7, 8, 9, 10, 11, 13a, 13b, 1
4a and 14b are the same as those in the first embodiment described above. 15
Is a cutoff valve provided in the low-temperature cooling water supply pipe 13b for supplying low-temperature water from the high-level heat recovery device 10 to the CO shift converter 4, and 16 is the recovery water of the high-level heat recovery device 10 to the steam separator 6. It is a shutoff valve provided in the supply pipe 16a.

Next, the operation will be described. During high-load power generation, the shutoff valve 15 is opened and the shutoff valve 16 is closed to supply low-temperature water from the high-level heat recovery device 10 to the CO shift converter 4. The operation in this case is the same as that in the first embodiment. At the time of low-load power generation, the shutoff valve 15 is closed and the shutoff valve 16 is opened, so that the low-temperature water from the high-level heat recovery device 10 is discharged from the CO shift converter 4
Is not supplied to the steam separator 6 and returned to the steam separator 6. During low load power generation, the flow rate of the reformed gas is small, so the calorific value of the catalyst is small, and when cooled like the high load power generation, the temperature of the catalyst drops too much, so the low temperature water is supplied to the CO shift converter 4. Stop.

Example 5. Next, a fifth embodiment of the present invention will be described with reference to FIG. In FIG. 5, 1, 2, 3, 4,
5, 6, 7, 8, 9, 10, 11, 13a, 13b, 1
4a and 14b are the same as those in the first embodiment described above. 17
Is a temperature sensor attached near the reformed gas outlet of the CO shift converter 4. 18 is C from the high-level heat recovery device 10
It is a flow rate control valve provided in the middle of the low temperature cooling water supply pipe 13b to the O-transformer 4. Reference numeral 19 is a control device that controls the opening degree of the flow rate control valve 18 according to the output of the temperature sensor 17.

Next, the operation will be described. CO transformer 4
When the temperature of the temperature sensor 17 installed near the reformed gas outlet of the high temperature is high, the control device 19 increases the opening degree of the flow rate control valve 18, and the low temperature supplied from the high-level heat recovery device 10 to the CO shift converter 4 is low. The flow rate of water is increased to improve the cooling capacity of the CO shift converter 4 for the catalyst. Conversely, when the temperature of the temperature sensor 17 is low, the control device 19 causes the flow control valve 1
The opening degree of 8 is reduced, the flow rate of the low-temperature water supplied from the high-order heat recovery device 10 to the CO shift converter 4 is reduced, and the cooling capacity of the CO shift converter 4 for the catalyst is reduced. The low temperature water not used as the cooling water is sent to the steam separator 6. As a result, the temperature distribution of the CO shift catalyst 4a in the CO shifter 4 can always be maintained at an appropriate temperature, and the carbon monoxide concentration in the reformed gas at the CO shifter outlet can be reduced.

Embodiment 6 FIG. Next, a sixth embodiment of the present invention will be described with reference to FIG. In FIG. 6, 1, 2, 3, 4,
5, 6, 7, 8, 9, 10, 11, 13a, 13b, 1
4a and 14b are the same as those in the first embodiment described above. 20
Is a carbon monoxide concentration sensor attached near the reformed gas outlet of the CO shift converter 4. Reference numeral 21 is a flow rate control valve provided in the middle of the low-temperature cooling water supply pipe 13b from the high-level heat recovery device 10 to the CO shift converter 4. Reference numeral 22 is a control device that controls the opening degree of the flow rate control valve 21 according to the output of the carbon monoxide concentration sensor 20.

Next, the operation will be described. Flow control valve 2
If the opening degree of 1 is increased or decreased, CO
The flow rate of low-temperature water supplied to the transformer 4 increases or decreases. At this time, the cooling capacity for the catalyst of the CO shift converter 4 increases or decreases. The temperature distribution of the catalyst changes and the carbon monoxide concentration sensor 2
The 0 output changes. The control device 22 has a function of automatically determining the opening degree of the flow rate control valve 21 so that the output of the carbon monoxide concentration sensor 20 becomes minimum. The low temperature water not used as the cooling water is sent to the steam separator 6. As a result, the temperature distribution of the CO shift catalyst 4a in the CO shifter 4 can always be maintained at an appropriate temperature, and the carbon monoxide concentration in the reformed gas at the CO shifter outlet can be reduced.

[0036]

In the phosphoric acid fuel cell power generator according to claim 1 of the present invention, the cooling pipe through which the high temperature water supplied from the steam separator flows and the cooling pipe through which the low temperature water supplied from the high level heat recovery device flows. Since the CO shifter is configured to have both of the above, it is possible to easily improve the temperature or temperature distribution of the CO shifter catalyst layer and reduce the CO concentration at the CO shifter outlet without increasing the size of the device. There is an effect that can be.

The phosphoric acid fuel cell power generator according to claim 2 of the present invention has both a cooling pipe through which high temperature water supplied from the steam separator flows and a cooling pipe through which low temperature water supplied from the condenser flows. Since the CO transformer is configured as
It is possible to improve the temperature or temperature distribution of the shift converter catalyst layer and reduce the CO concentration at the CO shift outlet without increasing the size of the apparatus. Further, since the temperature of the CO transformer cooling water can be lowered by using the condensed water necessary for the continuous operation of the plant, unlike the case where new water is supplied for cooling, it is possible to prevent the deterioration of the thermal efficiency. .

A phosphoric acid fuel cell power generator according to claim 3 of the present invention is the phosphoric acid fuel cell power generator of claim 1 or 2, wherein the low temperature heat is supplied from a high-level heat recovery device or a condenser. Since the cooling pipe through which water flows is densely arranged in the vicinity of the inlet and the outlet of the reformed gas inside the CO shift converter, the temperature distribution of the CO shift catalyst can be maintained optimally. The effect is that the carbon monoxide concentration in the reformed gas at the outlet can be reduced.

A phosphoric acid fuel cell power generator according to a fourth aspect of the present invention is the phosphoric acid fuel cell power generator according to any one of the first to third aspects, wherein at the time of low load power generation, C
Since the low-temperature water supplied to the O-transformer is cut off, it is possible to prevent an increase in the concentration of carbon monoxide in the reformed gas at the CO-transformer outlet due to excessive cooling of the CO-transformer catalyst. Play.

A phosphoric acid fuel cell power generator according to a fifth aspect of the present invention is the phosphoric acid fuel cell power generator according to any one of the first to fourth aspects, wherein a reformed gas temperature sensor is provided at the CO transformer outlet. Or a catalyst temperature sensor is also provided in the CO shift converter, and the supply amount of the cooling water supplied to the CO shift converter is adjusted according to the temperature, so that the heat exchange in the CO shift converter is optimally controlled. There is an effect that can be.

A phosphoric acid fuel cell power generator according to claim 6 of the present invention is the phosphoric acid fuel cell power generator according to any one of claims 1 to 5, wherein a carbon monoxide concentration sensor is provided at the CO transformer outlet. Is provided, and the amount of cooling water supplied to the CO transformer is adjusted according to the concentration,
It is possible to optimally control the heat exchange in the CO shift converter.

[Brief description of drawings]

FIG. 1 is a system diagram showing a first embodiment of the present invention.

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

FIG. 3 is a system diagram showing a third embodiment of the present invention.

FIG. 4 is a system diagram showing a fourth embodiment of the present invention.

FIG. 5 is a system diagram showing a fifth embodiment of the present invention.

FIG. 6 is a system diagram showing a sixth embodiment of the present invention.

FIG. 7 is a system diagram of a conventional phosphoric acid fuel cell power generator.

FIG. 8 is a heat flux flow distribution diagram of a CO shift converter catalyst layer.

FIG. 9 is a heat flux distribution diagram of a CO shift converter catalyst layer.

[Explanation of symbols]

1 reformer, 2 heat exchanger, 3 heat exchanger, 4 CO shift converter, 4a low temperature CO shift catalyst, 4b container, 4c high temperature water cooling pipe, 4d, 4d-1 low temperature water cooling pipe, 5
Fuel cell, 6 steam separator, 10 high-level heat recovery device,
11 water treatment device, 13a high temperature cooling water supply pipe, 13
b, 13c low temperature cooling water supply pipe, 14 condenser, 15
Shut-off valve, 16 Shut-off valve, 17 Temperature sensor, 18, 21
Flow rate control valve, 19, 22 Control device, 20 Carbon monoxide concentration sensor.

Claims (6)

[Claims] 1. A CO shifter for reacting carbon monoxide in the reformed gas obtained by the reformer with steam in the presence of a catalyst to convert it into carbon dioxide, and a reformed gas passed through the CO shifter. And a fuel cell that obtains electric power by acting an oxidizing gas, a steam separator that obtains high-temperature water for cooling the fuel cell and steam that is necessary for the reformer, and is connected to this steam separator, and a surplus In a phosphoric acid fuel cell power generator including a high-level heat recovery device that obtains condensed water from steam, the CO shift converter encloses the catalyst, and one end of the CO shift converter is connected to the outlet side of the reformer, A container having the other end connected to the fuel electrode side of the cell; a cooling pipe for high-temperature water, which is installed in the container to cool the catalyst and through which the high-temperature water supplied from the steam separator flows; To cool the above container To be installed, phosphoric acid fuel cell power generation apparatus characterized by comprising a cold water cooling pipes condensed water recovered by the high heat recovery device flows. 2. A CO shifter for converting carbon monoxide in the reformed gas obtained by the reformer with steam in the presence of a catalyst to convert it into carbon dioxide, and the reformed gas passed through the CO shifter. And a fuel cell that obtains electric power by acting an oxidizing gas, a steam separator that obtains high-temperature water for cooling the fuel cell and a steam required for the reformer, and a gas discharged from the fuel cell In a phosphoric acid fuel cell power generation device including a condenser for obtaining condensed water, the CO shifter encloses the catalyst and has one end connected to an outlet side of the reformer, and a fuel electrode of the fuel cell. A container having the other end connected to a side, a cooling pipe for high temperature water, which is installed in the container to cool the catalyst, and through which high temperature water supplied from the water vapor separator flows, and to cool the catalyst. Installed in the container, Phosphoric acid fuel cell power generation apparatus characterized by comprising a cold water cooling pipe through which the condensed water supplied from the condenser. 3. The low-temperature water cooling pipes are densely arranged on the inlet side and the outlet side of the reformed gas with respect to the container, and are sparsely arranged on other portions. The phosphoric acid fuel cell power generator according to claim 2. 4. The phosphoric acid according to claim 1, wherein the cooling water of the cooling pipe for low temperature water is not flowed during low load power generation of the phosphoric acid fuel cell power generator. Type fuel cell power generator. 5. A control device for changing the flow rate of the cooling water flowing through the cooling pipe for low temperature water according to the reformed gas temperature near the CO shifter outlet or the CO shifter catalyst temperature. The phosphoric acid fuel cell power generator according to any one of claims 1 to 4. 6. A CO sensor is provided in a flow path of the reformed gas passing through the CO shift converter, and a control device is provided for changing a flow rate of cooling water flowing through the cooling pipe for low temperature water according to an output of the CO sensor. The phosphoric acid fuel cell power generator according to any one of claims 1 to 5.