JP2001180912A - Hydrogen refining equipment - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a hydrogen refining equipment in which the CO concentration in the reforming gas containing hydrogen and water can be reduced by CO transforming reaction with high stability and linger life even if the start-up and shut-down operations are repeated many times, and also the start-up time can be shortened. SOLUTION: A carbon monoxide transforming medium is divided into some parts by using a noble metal catalyst and provided with either a radiation space or a cooling space in the middle between each part.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a hydrogen purifying apparatus for use in fuel such as a fuel cell, and more particularly to a method for removing carbon monoxide from reformed gas.

[0002]

2. Description of the Related Art Generally, a fuel cell uses, as a hydrogen source, a reformed gas obtained by reforming a hydrocarbon, alcohol, ether, or the like. However, in a polymer electrolyte fuel cell operating at a low temperature of 100 ° C. or less, the platinum catalyst used for the electrode is poisoned by carbon monoxide (hereinafter referred to as CO) contained in the reformed gas. If the poisoning of the platinum catalyst occurs, the reaction of hydrogen is hindered, and the power generation efficiency of the fuel cell is significantly reduced. Therefore, it is necessary to remove CO to 100 ppm or less, preferably 10 ppm or less.

[0003] Generally, to remove CO, CO
The CO and steam are reacted in the CO shift section provided with the shift catalyst to convert the CO into hydrogen and reduce the CO concentration to a concentration of several thousand ppm to about 1%. Thereafter, a small amount of air is added, and CO is removed by a CO selective oxidation catalyst to a level of several ppm which does not adversely affect the fuel cell.

At this time, in order to sufficiently remove CO, it is necessary to add oxygen having a concentration of about 1 to 3 times the CO concentration. However, hydrogen is consumed in accordance with the amount of oxygen. When the CO concentration is high, the amount of added oxygen also increases, and the consumed hydrogen increases, so that the efficiency of the entire apparatus is greatly reduced. Therefore, it is necessary to sufficiently reduce CO in the CO shift section.

Conventionally, for CO conversion, a copper-zinc catalyst or a copper-chromium catalyst usable at 150 to 300 ° C. as a low-temperature CO conversion catalyst has been used. An iron-chromium catalyst that functions as described above is used. These CO conversion catalysts have been used only as low-temperature catalysts or as a combination of high-temperature and low-temperature catalysts, depending on applications such as chemical plants and hydrogen generators for fuel cells.

[0006]

As described above, when a copper-based low-temperature CO conversion catalyst is used, high catalytic activity can be obtained, but it is necessary to activate it by performing a reduction treatment before use. In such an activation treatment, since the catalyst generates heat during the treatment, it is necessary to perform the treatment over a long period of time, for example, by adjusting the supply amount of the reducing gas so that the catalyst does not reach the heat-resistant temperature or higher.

The once activated CO shift catalyst is
When oxygen is mixed in, for example, when the apparatus is stopped, the oxygen is re-oxidized and deteriorated, so that measures to prevent the oxidation have been required. Furthermore, since the low-temperature CO conversion catalyst has low heat resistance and cannot rapidly heat the catalyst at the time of starting the apparatus, it is necessary to take measures such as gradually increasing the temperature.

On the other hand, when only the high-temperature CO shift catalyst is used, the heat resistance is high and the temperature can be slightly increased. However, C
Since the O shift reaction is an equilibrium reaction depending on temperature, the CO shift catalyst for high temperature, which functions only at high temperature, has a CO concentration of 1%.
It was difficult to: For this reason, the efficiency of the CO purification unit connected later has been reduced.

As described above, the conventional method requires a long time to start the metamorphic section and is complicated to handle. Therefore, there are many problems in applications in which starting and stopping are frequently repeated.

[0010]

SUMMARY OF THE INVENTION The present invention has been made in consideration of the above problems of the hydrogen purifying apparatus, and facilitates the activation treatment of the CO conversion catalyst, and eliminates the influence of oxygen contamination when the operation is repeatedly started and stopped. To provide a hydrogen purifier that operates stably for a long period of time.

In order to achieve this object, the hydrogen purifying apparatus of the present invention comprises a supply section for a reformed gas containing hydrogen and water and a catalytic reaction chamber provided with a carbon monoxide conversion catalyst having a noble metal. A hydrogen purification device disposed downstream of a reformed gas supply unit, wherein the catalyst reaction chamber is divided into a plurality of stages, and at least one of a heat radiating unit and a cooling unit is provided at an intermediate portion of each stage of the catalyst reaction chamber. It is characterized by being installed.

At this time, it is effective that the carbon monoxide conversion catalyst contains at least platinum and cerium oxide. At this time, the particle size of the cerium oxide is 0.1 μm to
It is effective that the thickness is 15 μm.

[0013] The temperature of the carbon monoxide conversion catalyst disposed in the first stage is set to 300 ° C with respect to the flow direction of the reformed gas.
It is effective to carry out the above-mentioned carbon monoxide modification reaction while maintaining the temperature at 450 ° C.

The temperature of the carbon monoxide conversion catalyst is as follows:
It is effective that the lower part is lower than the upper part in the flow direction of the reformed gas.

Further, the volume of the carbon monoxide conversion catalyst is
It is effective to make the lower part larger than the upper part in the flow direction of the reformed gas.

It is effective that the amount of the noble metal carried by the catalyst for carbon monoxide conversion is larger in the lower part than in the upper part in the flow direction of the reformed gas.

It is effective that a catalyst having copper as a component is provided in at least one stage of the carbon monoxide conversion catalyst in the second and subsequent stages with respect to the flow direction of the reformed gas.

It is effective that a catalyst having a noble metal as a component is provided downstream of the catalyst having copper as a component.

It is effective that a diffusion section or a mixing section of the reformed gas is provided between each stage of the catalyst reaction chamber.

It is effective that a plurality of tubes are used to connect the respective stages of the catalyst reaction chamber.

It is also effective to control the operation of the cooling unit by controlling the temperature of the catalyst for carbon monoxide conversion. At this time, it is effective to control the temperature of the catalyst for carbon monoxide conversion by installing a water supply unit in the cooling unit and controlling the flow rate of the cooling water. It is also effective to install an air fan in the cooling unit and control the operation of the cooling fan by controlling the temperature of the catalyst.

Further, it is effective to heat at least one of fuel, water, reformed gas and combustion air introduced into the hydrogen purifier with the heat recovered in the cooling section.

[0023]

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

(Embodiment 1) FIG. 1 is a sectional view showing a configuration of a hydrogen purifying apparatus according to Embodiment 1 of the present invention. In FIG. 1, reference numeral 1 denotes a first catalyst body, and 2 denotes a second catalyst body, which are installed in a first reaction chamber 3 and a second reaction chamber 4, respectively. 5
Is a reformed gas inlet from which a reformed gas is introduced. The reformed gas reacted by the first catalyst body 1 and the second catalyst body 2 is discharged from the reformed gas outlet 6. The first reaction chamber 3 and the second reaction chamber 4 were separated so that heat was released between the first catalyst body 1 and the second catalyst body 2. Further, a diffusion plate 7 was provided on the upstream side of each catalyst body. Further, in order to keep the reactor at a constant temperature, the outer periphery of a necessary portion was covered with a heat insulating material 8 made of ceramic wool. Here, as the first catalyst body 1 and the second catalyst body 2, a cordierite honeycomb coated with a catalyst in which cerium oxide supported platinum was used.

Next, the operation and characteristics of the hydrogen purifier of the present embodiment will be described. Fuels for generating the reformed gas to be supplied to the hydrogen purifier include natural gas, methanol, gasoline and the like. The reforming method includes steam reforming by adding steam and partial reforming by adding air. In this embodiment, a case where a reformed gas obtained by steam reforming a natural gas is used will be described.

The composition of steam reformed natural gas is as follows:
Although it varies depending on the reaction temperature in the reforming catalyst, as an average value excluding water vapor, about 80% of hydrogen, carbon dioxide and carbon monoxide (hereinafter referred to as CO) are about 10%, respectively.
%included. The reformed gas introduced from the reformed gas inlet 5 is
First, it reacts on the first catalyst body 1, and the CO concentration is reduced to 1 to 2%. The reformed gas that has passed through the first catalyst 1 reacts in the second catalyst 2 until the CO concentration becomes about 0.1 to 0.8%, and is discharged from the reformed gas outlet 6. The reformed gas after the reaction is further supplied to the fuel cell unit through a CO purifying unit for removing CO and the like.

Next, the operation principle of the present apparatus will be described. The CO shift reaction is a temperature-dependent equilibrium reaction,
In terms of equilibrium theory, the lower the temperature, the lower the CO concentration. However, since the reaction rate on the catalyst decreases at low temperatures, the CO conversion catalyst exhibits such a characteristic that the CO concentration takes a minimum value with respect to the temperature as shown in practice in FIG. Therefore, the higher the low-temperature activity of the catalyst, the lower the concentration of CO can be reduced. Generally, a copper-based catalyst such as a copper-zinc catalyst or a copper-chromium catalyst used as a CO shift catalyst has a high low-temperature activity and can perform a CO shift reaction at about 150 ° C. to 300 ° C. Several hundred to several thousand p
pm. However, after the copper-based catalyst has been charged into the reactor, it is necessary to activate hydrogen gas and a reducing gas such as a reformed gas as an initial operation. Further, since the heat resistance of the copper-based catalyst is as low as about 300 ° C., the reducing gas is diluted or supplied or the reaction is gradually performed at a small flow rate so that the heat of reaction during activation does not exceed the heat-resistant temperature. The content of copper in the catalyst also affects the time required for activation, but about tens of percent by weight is necessary to ensure life reliability.
The activation takes a long time.

In addition, the CO shift reaction usually requires reaction conditions in which the gas flow rate (space velocity: SV) per catalyst volume is 1000 or less per hour, and a large amount of catalyst is required to increase the heat capacity. Sometimes it takes a long time to raise the temperature of the catalyst. Therefore, it is conceivable to use heating from the outside of the reaction chamber together with an electric heater or the like, or to increase the temperature of the supplied reformed gas to increase the heating rate. However, since a copper-based catalyst has a low heat-resistant temperature, rapid heating to a locally high temperature is not desirable.

When the apparatus is stopped, the pressure inside the reaction chamber decreases as the temperature of the apparatus decreases, and a small amount of external air is mixed. Therefore, when the device is repeatedly stopped and started over a long period of time, the copper-based catalyst gradually deteriorates. Therefore, means for preventing oxygen from being mixed is required, and the apparatus becomes complicated.

On the other hand, when a noble metal catalyst is used as the CO conversion catalyst as in the present apparatus, long-term activation or reduction treatment is not required. In addition, since heat resistance is high, and there is no problem even when a high-temperature portion of about 500 ° C. is generated locally at the time of startup, heating can be rapidly performed by supplying a high-temperature reformed gas, and the apparatus can be started quickly. it can. Also,
Since even a small amount of air hardly deteriorates, it is not particularly necessary to provide an antioxidant.

The characteristics of the CO shift reaction are affected by the temperature distribution from the upstream to the downstream of the shift catalyst. C
On the upstream side where the O concentration is high, it is preferable to set the reaction temperature to a high temperature, and the downstream side affected by the equilibrium concentration of CO is preferably a low temperature. Therefore, when the CO conversion catalyst body is divided into a plurality of stages as in the present apparatus, and a heat radiating portion or a cooling portion is arranged in the middle of each stage to adjust the heat radiating amount or the cooling amount,
CO can be reduced with a smaller amount of catalyst.

The space velocity SV can be increased at a higher temperature. However, when the temperature is too high, the reverse reaction of the reforming reaction starts to proceed, and methane is generated, so that the amount of hydrogen in the reformed gas decreases. Affects the efficiency of the device. Therefore, the temperature of the first catalyst 1 is preferably 450 ° C. or less. Conversely, if the temperature of the first catalyst body is low, the space velocity SV needs to be reduced, so the temperature of the first catalyst body is preferably set to 300 ° C. or higher. At this time, the temperature of the first catalyst body is set to 30
Even if it is lower than 0 ° C., it works if the space velocity SV is made small, but since the temperature difference between the first catalyst body 1 and the second catalyst body 2 becomes small, the effect of dividing into plural stages is weakened, and Only the volume of the reactor may increase.

Further, the temperature of the second catalyst 2 is changed to the first catalyst 1
If the temperature is higher than the above, the CO reduced in the first catalyst body 1 increases again by the reverse reaction, so that the temperature is preferably lower than that of the first catalyst body 1. This means that the number of catalyst
The same applies to the case of multiple stages.

The lower the catalyst temperature, the lower the space velocity SV, the higher the characteristics obtained. At the same time, the higher the space velocity SV, the more difficult the methanation at high temperatures. Preferably, the volume is smaller than that of the catalyst body.

Further, the material of the CO conversion catalyst preferably contains cerium oxide and platinum, and high characteristics are obtained. The particle size of cerium oxide is 0.1 μm to 15 μm.
μm is preferred, and when the particle size is larger than this, the dispersibility of platinum decreases, and it becomes difficult to obtain sufficient characteristics,
When the size is small, the life characteristics are apt to be deteriorated, such as peeling off from the honeycomb or other equipment, or the pellet being easily broken.

In the present embodiment, the first reaction chamber 3 and the second reaction chamber 4 are simply separated from each other, and a tube for radiating heat is provided in the middle. Even higher characteristics can be obtained by, for example, forcibly cooling with a fan or controlling the amount of cooling according to the catalyst temperature.

It is preferable that a diffusion section or a mixing section is provided in the middle of each stage of the catalyst body. In a large-volume CO-converting catalyst, a temperature distribution tends to be formed in the cross-sectional direction.
Concentration tends to vary. Therefore, by providing the mixing section or the diffusion section, the lower catalyst effectively functions, and higher characteristics can be obtained.

Further, it is preferable that the amount of the noble metal carried by the shift catalyst is increased in the lower stage than in the upper stage. When the amount of the noble metal carried is large, methanation tends to proceed, and this tendency is more remarkable as the catalyst temperature rises. On the other hand, the higher the amount of the noble metal carried, the higher the low-temperature activity. For this reason, by increasing the amount of the noble metal carried in the lower catalyst body in which the methanation reaction does not easily proceed, high characteristics can be obtained with a smaller catalyst volume.

In the present embodiment, a catalyst in which platinum is supported on cerium oxide is used as a noble metal catalyst. However, a noble metal such as rhodium, palladium, ruthenium, etc.
As a carrier, zirconium oxide, magnesium oxide, zinc oxide, titanium oxide, or silicon oxide can be used.

In the present embodiment, a platinum conversion salt is supported on cerium oxide and coated on a cordierite honeycomb to prepare a CO conversion catalyst. However, a noble metal catalyst is supported on pellet-shaped alumina to form a CO conversion catalyst. A catalyst body can also be produced. Further, as the honeycomb base material, a metal such as stainless steel or ceramic wool can be used.

In this embodiment, the example in which natural gas is used as fuel and steam reforming has been described. However, when another fuel is used, partial reforming in which air is added to partially oxidize fuel is performed. The present device can also be adapted when performing.

(Embodiment 2) A second embodiment of the present invention will be described. In this embodiment, as shown in FIG. 3, a cooling water supply pipe 19 is provided between the first reaction chamber 13 and the second reaction chamber 14, and most of the functions and effects are similar to those of the first embodiment. It is. Therefore, the present embodiment will be described focusing on different points.

FIG. 3 is a diagram showing a sectional configuration of the present embodiment. Since the CO conversion reaction is an equilibrium reaction, CO can be further reduced when the proportion of the reactant steam is large. In the present example, the cooling water supply pipe 19 is provided in the cooling unit, so that not only cooling by the latent heat of evaporation of water but also equilibrium in the CO shift reaction becomes advantageous, and CO can be reduced more efficiently.

(Embodiment 3) A third embodiment of the present invention will be described. In the present embodiment, as shown in FIG. 4, a connecting portion between the first reaction chamber 13 and the second reaction chamber 14 is constituted by a plurality of pipes, and a cooling fan 29 is further provided. For the most part, it is similar to the first embodiment. Therefore, the present embodiment will be described focusing on different points.

FIG. 5 is a diagram showing a sectional configuration of the present embodiment. Although the efficiency of cooling depends on the surface area of the tube, in this example, since the number of connecting portions is plural, cooling can be performed efficiently and the length of the connecting portion can be shortened, so that the device can be downsized. . Further, since the cooling fan 29 is provided, cooling can be performed more efficiently. In addition, the second catalyst body 22
By operating, stopping, or controlling the number of revolutions of the cooling fan according to the temperature, the catalyst temperature can always be maintained at the optimum value.

The air exchanged and heated in the cooling section is used for heating the air and fuel in the combustion section for heating the reforming section, the raw material used for reforming, and water, thereby improving the efficiency of the apparatus. be able to.

(Embodiment 4) A fourth embodiment of the present invention will be described. In the present embodiment, as shown in FIG. 5, a copper-based catalyst body 32 is provided downstream of a noble metal catalyst body 31, and most of the functions and effects are similar to those of the first embodiment. Therefore, the present embodiment will be described focusing on different points.

FIG. 5 is a diagram showing a sectional configuration of the present embodiment. In the second reaction chamber 34, a copper-based catalyst body 32 in which a cordierite honeycomb is coated with a copper-based catalyst is installed. Here, the copper-based catalyst refers to a CO conversion catalyst containing copper as an active component, and includes a copper-zinc catalyst, a copper-chromium catalyst, or a material containing these as a main component, alumina,
What added silica, zirconia, etc. is also contained in a copper catalyst. Copper-based catalyst 3 capable of CO conversion at low temperature
By installing 2, the CO concentration after passing through the second stage can be further reduced. Further, since the noble metal catalyst body 31 having high heat resistance is provided at the first stage, the copper-based catalyst having relatively low heat resistance is not exposed to high temperature even at the time of startup, and the influence of deterioration is reduced.

Although not provided in this example, it is preferable to provide a noble metal catalyst downstream of the copper-based catalyst. When the apparatus is stopped or when the apparatus is stopped for a long period of time, a small amount of air may be mixed in from the outside, and the copper-based catalyst gradually deteriorates due to the mixing of air. Hydrogen and CO are adsorbed on the noble metal catalyst even when stopped, and if the noble metal catalyst is installed so as to sandwich the copper-based catalyst between the upstream side and the downstream side, a small amount of oxygen is consumed on the noble metal catalyst, Deterioration of the copper-based catalyst can be suppressed.

[0050]

(Example 1) Platinum-supported cerium oxide powder was prepared by mixing powders having the same diameter and lengths of 20 mm and 60 m, respectively.
m to form a first catalyst body 1 and a second catalyst body 2 by coating on a cordierite honeycomb, and as shown in FIG.
They were installed in the first reaction chamber and the second reaction chamber, respectively. From the reformed gas inlet 5, a reformed gas containing 8% of carbon monoxide, 8% of carbon dioxide, 20% of steam and the balance of hydrogen was introduced at a flow rate of 10 liters per minute. The temperature of the first catalyst 1 and the temperature of the second catalyst 2 were set to 400 ° C. and 250 ° C., respectively, and the CO concentration of the gas discharged from the reformed gas outlet 6 was measured by gas chromatography.
m. Thereafter, after the atmosphere in the reaction chamber was replaced with nitrogen, air was supplied, reformed gas was supplied again, and the composition of the reaction gas was measured. As a result, the CO concentration was 3000 ppm.
Further, the same operation was repeated 50 times, and the CO concentration was measured in the same manner, and it was 3200 ppm.

(Example 2) In Example 1, the temperature of the first catalyst was increased to 250 ° C, 275 ° C, 300 ° C, 400 ° C, 450 ° C.
° C and 475 ° C, and the CO concentration discharged from the reformed gas outlet 6 was measured in the same manner as in Example 1, and found to be 7000 ppm, 7200 ppm, 3100 ppm,
3000 ppm, 3100 ppm, and 3500 ppm. When the methane concentration in the gas was measured,
No methane is detected below 00 ° C, and 0.5% at 450 ° C.
% At 475 ° C.

(Example 3) A catalyst body was prepared from samples in which the particle diameters of the cerium oxide powder in Example 1 were different. The particle size of cerium oxide is 0.05 μm, 0.1 μm, 5 μm, respectively.
m, 15 μm and 17 μm were used. When the CO concentration discharged from the reformed gas outlet 6 was measured in the same manner as in Example 1, they were 2900 ppm, 3000 ppm, 3
It was 400 ppm, 3500 ppm, and 5000 ppm. Thereafter, the reaction chamber was replaced with nitrogen, air was supplied, reformed gas was supplied again, and the composition of the reaction gas was measured.
00 ppm, 3400 ppm, 3500 ppm, 510
It was 0 ppm. Repeat the same operation 50 times,
When the CO concentration was measured in the same manner, 9000 ppm, 31
00 ppm, 3500 ppm, 3600 ppm, 800
It was 0 ppm.

Comparative Example 1 As shown in FIG. 6 of Example 1, the connection between the first reaction chamber and the second reaction chamber was removed to form one reaction chamber. A noble metal catalyst 41 was prepared by supporting the same catalyst as in Example 1 on a cordierite honeycomb having a length of 80 mm, and was installed in the reaction chamber 42. Reformed gas inlet 4
From 3, carbon monoxide 8%, carbon dioxide 8%, steam 20
%, The remainder being hydrogen, was introduced at a flow rate of 10 liters per minute. When the temperature of the catalyst 41 was changed and the concentration of carbon monoxide discharged from the reformed gas outlet 44 was measured by gas chromatography, the minimum value of the CO concentration was 7000 ppm. Thereafter, the reaction chamber was replaced with nitrogen, air was supplied, reformed gas was supplied again, and the composition of the reaction gas was measured at the same temperature.
It was 100 ppm. Further, the same operation was repeated 50 times, and the CO concentration was measured in the same manner, and it was 7200 ppm.

(Comparative Example 2) A copper-zinc catalyst was installed in the reaction chamber 42 instead of the noble metal catalyst body 41 used in Comparative Example 1, and the same measurement as in Comparative Example 1 was performed. The CO concentration of the discharged gas was 1000 ppm. Thereafter, the reaction chamber was replaced with nitrogen, air was supplied, reformed gas was supplied again, and the composition of the reaction gas was measured. As a result, the CO concentration was 200 ppm. Further, the same operation was repeated 50 times, and the CO concentration was measured in the same manner to be 22000 ppm.

[0055]

As is clear from the comparison between the evaluation results of the apparatus of the above embodiment and the apparatus of the comparative example, according to the present invention, the heat resistance of the CO conversion catalyst is improved, and even when the apparatus is repeatedly started and stopped. A stable operation of the hydrogen purifier could be provided.

[Brief description of the drawings]

FIG. 1 is a cross-sectional view illustrating a configuration of a hydrogen purifying apparatus according to a first embodiment of the present invention.

FIG. 2 is a diagram showing a general relationship between the operating temperature of a shift catalyst and the concentration of carbon monoxide after passing through the catalyst.

FIG. 3 is a cross-sectional view illustrating a configuration of a hydrogen purifying apparatus according to a second embodiment.

FIG. 4 is a cross-sectional view illustrating a configuration of a hydrogen purifying apparatus according to a third embodiment.

FIG. 5 is a cross-sectional view illustrating a configuration of a hydrogen purifying apparatus according to a fourth embodiment.

FIG. 6 is a diagram showing a cross-sectional configuration of a hydrogen purification device of Comparative Example 1.

[Explanation of symbols]

 1,11,21 First catalyst 2,2,22 Second catalyst 3,13,23,33 First reaction chamber 4,14,24,34 Second reaction chamber 5,15,25,35,43 Quality gas inlet 6,16,26,36,44 Reformed gas outlet 7,17,27,37,45 Diffusion plate 8,18,28,38,46 Heat insulator 19 Cooling water supply pipe 29 Cooling fan 31,41 Precious metal Catalyst 32 Copper-based catalyst 42 Reaction chamber

Continued on the front page (72) Inventor Kunihiro Ukai 1006 Kadoma Kadoma, Osaka Prefecture Matsushita Electric Industrial Co., Ltd. (72) Inventor Toshiyuki Shono 1006 Oji Kadoma Kadoma City, Osaka Matsushita Electric Industrial Co., Ltd. (72) Invention Person Koichiro Kitagawa 6-2-61 Imafukunishi, Joto-ku, Osaka City, Osaka Prefecture Matsushita Seiko Co., Ltd. (72) Inventor Tetsuya Ueda 1006 Kadoma, Kadoma, Osaka Prefecture Matsushita Electric Industrial Co., Ltd. F-term (reference) 4G040 EA02 EA03 EA06 EB12 EB23 EB32.

Claims (12)

[Claims] 1. A hydrogen supply apparatus comprising: a supply section for a reformed gas containing hydrogen and water; and a catalytic reaction chamber provided with a catalyst for converting carbon monoxide having a noble metal disposed downstream of the reformed gas supply section. A hydrogen purifier, wherein the catalytic reaction chamber is divided into a plurality of stages, and at least one of a heat radiating unit and a cooling unit is provided in an intermediate portion of each stage of the catalytic reaction chamber. 2. The hydrogen purification apparatus according to claim 1, wherein the catalyst for carbon monoxide conversion contains at least platinum and cerium oxide. 3. The temperature of the catalyst for carbon monoxide conversion arranged in the first stage is maintained at 300 ° C. or higher and 450 ° C. with respect to the flow direction of the reformed gas, and the carbon monoxide denaturing reaction is carried out. The hydrogen purification apparatus according to claim 1, wherein the hydrogen purification is performed. 4. The hydrogen purification according to claim 1, wherein the temperature of the carbon monoxide conversion catalyst is lower in the lower part than in the upper part with respect to the flow direction of the reformed gas. apparatus. 5. The hydrogen purification according to claim 1, wherein the volume of the carbon monoxide conversion catalyst is larger in the lower part than in the upper part with respect to the flow direction of the reformed gas. apparatus. 6. The method according to claim 1, wherein the amount of the noble metal carried on the catalyst for carbon monoxide conversion is larger in the lower part than in the upper part with respect to the flow direction of the reformed gas. Hydrogen purification equipment. 7. The catalyst according to claim 1, wherein a catalyst having copper as a component is installed in at least one stage of the carbon monoxide conversion catalyst in the second and subsequent stages with respect to the flow direction of the reformed gas. Item 6. A hydrogen purifier according to Item 6. 8. A downstream side of a catalyst having copper as a component,
The hydrogen purifier according to claim 7, further comprising a catalyst having a noble metal as a component. 9. The apparatus according to claim 1, wherein a diffusion section or a mixing section of the reformed gas is provided between each stage of the catalyst reaction chamber.
The hydrogen purification apparatus according to claim 8. 10. The catalyst reaction chamber according to claim 1, wherein a plurality of tubes connect the respective stages of the catalyst reaction chamber.
A hydrogen purifier according to item 1. 11. The hydrogen purifier according to claim 1, wherein the operation of the cooling unit is controlled by the temperature of the carbon monoxide conversion catalyst. 12. The method according to claim 1, wherein at least one of fuel, water, reformed gas, and combustion air introduced into the hydrogen purifier is heated by the heat recovered in the cooling unit. The hydrogen purifying apparatus according to claim 1.