JP2011032128A - Refining method of hydrogen, shipping equipment of hydrogen, and hydrogen station - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method for refining hydrogen, which can reduce the content of carbon monoxide in hydrogen. <P>SOLUTION: The refining method of hydrogen includes a refining step of removing carbon monoxide from a hydrogen-containing gas, using at least one step selected from the groups consisting of a methanation step of methanating carbon monoxide remaining in a hydrogen-containing gas refined by an adsorption method, by a catalyst, an adsorption step of making carbon monoxide adsorbed in an adsorbent, and an oxidation step of oxidizing carbon monoxide. <P>COPYRIGHT: (C)2011,JPO&INPIT

Description

  The present invention relates to a hydrogen purification method, a hydrogen shipping facility, and a hydrogen station.

  Conventionally, a method for reforming petroleum-based raw materials such as naphtha by a steam reforming reaction or the like is known as one of inexpensive and practical methods for producing a hydrogen-containing gas. The hydrogen-containing gas produced by such a method contains impurities such as water vapor, unreacted hydrocarbons, carbon monoxide and carbon dioxide in addition to hydrogen.

  As a method for purifying the hydrogen gas by removing the above-mentioned impurities from the hydrogen-containing gas, the Pressure Swing Adsorption method (PSA method), the Thermal Swing Adsorption method (TSA method), the Thermal Pressure Swing Adsorption method (TPSA method) and the like are used. The law is known. In the PSA method, for example, as shown in Patent Document 1 below, high-purity hydrogen gas is purified by allowing an adsorbent to adsorb impurities contained in a hydrogen-containing gas in a high-pressure adsorption tower.

Japanese Patent Laid-Open No. 10-212103

  In recent years, the spread of a fuel cell vehicle using hydrogen gas as a fuel has been demanded as a transportation means with a low environmental load in place of a conventional gasoline vehicle. For the spread of fuel cell vehicles, it is necessary to disseminate hydrogen stations for supplying hydrogen gas having a purity applicable to fuel cell vehicles to fuel cell vehicles and shipping facilities for supplying hydrogen gas to hydrogen stations. .

  When hydrogen gas is used in a fuel cell vehicle, it is required to remove impurities from the hydrogen gas to purify the hydrogen gas having a purity of preferably 99.99% by mass, more preferably 99.999% by mass or more. . Among impurities, particularly carbon monoxide (CO) is a catalyst poison of platinum (Pt) that is frequently used as an electrode catalyst for fuel cells. Therefore, it is required to remove as much carbon monoxide from hydrogen gas as possible. .

  When purifying high-purity hydrogen gas by the above-described PSA method, it is necessary to increase the pressure of the hydrogen-containing gas and to increase the number of stages of the purification apparatus as the carbon monoxide remaining in the hydrogen gas is reduced. However, the increase in the pressure of the hydrogen-containing gas results in an increase in the amount of hydrogen adsorbed on the adsorbent, so that the hydrogen gas recovery rate decreases. Further, in order to increase the purity of the hydrogen gas by the PSA method, a large amount of energy is required for increasing the pressure of the hydrogen-containing gas (compression of the hydrogen-containing gas). Furthermore, safety becomes a problem as the pressure of the hydrogen-containing gas increases. Further, if the apparatus is multistaged, the recovery rate of hydrogen gas is reduced, and the cost required for multistage and the complexity of the apparatus become problems. In this way, if excessive purification of hydrogen gas is attempted by the PSA method, the scale of the compressor for increasing the amount of adsorbent, enlarging the adsorbing tower, increasing the number of stages, and increasing the pressure of the hydrogen-containing gas Needs to be made.

  As described above, in terms of recovery rate, energy loss, safety, or cost, there is a problem in purifying hydrogen gas whose carbon monoxide content has been reduced to a level applicable to a fuel cell vehicle by the PSA method. was there. Therefore, it has been difficult to spread hydrogen shipping equipment and hydrogen stations to which the PSA method is applied.

  The present invention has been made in view of the above-described problems of the prior art, and includes a hydrogen purification method capable of reducing the content of carbon monoxide in hydrogen, and a hydrogen shipping facility to which the purification method is applied. And to provide a hydrogen station.

  In order to achieve the above object, a method for purifying hydrogen according to the present invention comprises a methanation step of methanating carbon monoxide remaining in a hydrogen-containing gas purified by an adsorption method using a catalyst, and using carbon monoxide as an adsorbent. It comprises a purification step for removing carbon monoxide from the hydrogen-containing gas by at least one step selected from the group consisting of an adsorption step for adsorption and an oxidation step for oxidizing carbon monoxide. The adsorption method is a method for purifying hydrogen gas by causing an adsorbent to adsorb impurities contained in the hydrogen-containing gas, such as a PSA method, a TSA method, or a TPSA method. In the PSA method, the adsorption / desorption of impurities with respect to the adsorbent is controlled by changing the pressure of the hydrogen-containing gas. In the TSA method, the adsorption / desorption of impurities with respect to the adsorbent is controlled by changing the temperature of the hydrogen-containing gas. In the TPSA method, the adsorption / desorption of impurities with respect to the adsorbent is controlled by fluctuations in the pressure and temperature of the hydrogen-containing gas.

  According to the present invention, it is possible to reduce the content of carbon monoxide in hydrogen as compared with the case of purifying hydrogen by the adsorption method alone. Further, according to the present invention, even if the carbon monoxide content in the hydrogen-containing gas purified by the adsorption method is not reduced to a level applicable to a fuel cell vehicle, It is possible to reduce the carbon monoxide content to such an extent that it can be applied to a fuel cell vehicle.

  In the said invention, it is preferable that the catalyst used at a methanation process contains at least 1 type chosen from the group which consists of nickel, cobalt, iron, ruthenium, and rhodium as an active metal. Thereby, the effect of this invention becomes remarkable.

  In the present invention, the adsorbent used in the adsorption step is preferably at least one selected from the group consisting of activated carbon, zeolite and alumina. Thereby, the effect of this invention becomes remarkable.

  In the present invention, copper is preferably supported on the adsorbent used in the adsorption step. Thereby, adsorption of carbon monoxide to the adsorbent is promoted.

  In the present invention, it is preferable to oxidize carbon monoxide in the oxidation step using a catalyst containing ruthenium or platinum. Thereby, the effect of this invention becomes remarkable.

  The hydrogen shipping facility according to the present invention includes a facility for carrying out the hydrogen purification method according to the present invention. Moreover, the hydrogen station which concerns on this invention is equipped with the equipment for enforcing the hydrogen purification method which concerns on the said invention. In the hydrogen shipping facility and the hydrogen station according to the present invention, it is possible to supply hydrogen with a carbon monoxide content reduced to such an extent that it can be applied to a fuel cell vehicle.

  ADVANTAGE OF THE INVENTION According to this invention, the hydrogen purification method which can reduce the content rate of the carbon monoxide in hydrogen, the hydrogen shipping equipment and hydrogen station which applied the said purification method can be provided.

  Hereinafter, a preferred embodiment of the present invention will be described in detail.

(PSA method)
Below, the case where PSA method is used as an adsorption method is demonstrated. In the hydrogen purification method according to the present embodiment, a hydrogen-containing gas purified by the PSA method is used. In the PSA method, adsorbents such as zeolite, carbon molecular sieve, and alumina are used alone or in combination. These adsorbents are installed in an adsorption tower, and a high-pressure hydrogen-containing gas compressed by a compressor is introduced into the adsorption tower. Alternatively, the pressure in the adsorption tower into which the hydrogen-containing gas has been introduced is increased. Thereby, impurities such as carbon monoxide, carbon dioxide, hydrocarbons and water contained in the hydrogen-containing gas are adsorbed by the adsorbent, and the hydrogen-containing gas from which the impurities have been removed is recovered. After recovering the hydrogen-containing gas, the pressure in the adsorption tower is reduced from a high pressure to a normal pressure to desorb impurities adsorbed on the adsorbent and regenerate the adsorbent.

  In this embodiment, it is preferable to obtain hydrogen gas having a purity of 99.99% by mass or more by purification by the PSA method. This makes it possible to reduce the content of carbon monoxide in the hydrogen gas to 0.2 mass ppm or less in the purification step described later.

  In the PSA method, the pressure of the hydrogen-containing gas in the adsorption tower may be 0.5 to 4.0 MPa. The temperature of the hydrogen-containing gas sent to the adsorption tower should just be 10-100 degreeC. In order to obtain hydrogen gas having a purity of 99.99% by mass or more by purification by the PSA method, the pressure of the hydrogen-containing gas in the adsorption tower is preferably adjusted to 1.5 MPa or more. Note that the pressure and temperature of the hydrogen-containing gas are not necessarily limited to the above numerical range.

  As the hydrogen-containing gas before purification by the PSA method, for example, a reformed gas produced by a steam reforming reaction of a raw material such as petroleum hydrocarbon, natural gas, alcohols or ethers may be used. Specific examples of the reformed gas include naphtha, kerosene, gasoline, methane, ethane, propane, butane, pentane, methanol, and dimethyl ether.

(Purification process)
In this embodiment, carbon monoxide and other impurities remaining in the hydrogen-containing gas purified by the PSA method are removed in the purification step. In the purification process, carbon monoxide and other impurities are removed from the hydrogen-containing gas by using one or more processes selected from the group consisting of the following methanation process, adsorption process and oxidation process. In addition, when implementing combining a methanation process, an adsorption process, and an oxidation process, the order of a process is not specifically limited. Moreover, you may repeat at least any one among a methanation process, an adsorption process, and an oxidation process.

<Methanation process>
In the methanation step, carbon monoxide remaining in the hydrogen-containing gas purified by the PSA method is methanated using a catalyst. In the methanation step, carbon monoxide is methanated by hydrogen contained in the hydrogen-containing gas.

  The catalyst used in the methanation step preferably contains at least one selected from the group consisting of nickel, cobalt, iron, ruthenium and rhodium as the active metal. These active metals may be used by being supported on a carrier such as silica, alumina, titania or zirconia.

  The temperature of the hydrogen-containing gas in the methanation step may be about 150 to 400 ° C. The pressure of the hydrogen-containing gas in the methanation step may be about normal pressure to about 5 MPa. The temperature of the catalyst in the methanation step may be about 150 to 400 ° C.

  Conventionally, as shown in, for example, Japanese Patent Application Laid-Open No. 2006-290732 (hereinafter referred to as “Document 2”), a hydrogen-containing gas purified by methanation of carbon monoxide without being purified by the PSA method. There is known a method of using for a fuel cell. However, in the method of Document 2, since purification by the PSA method is not performed, the content of carbon monoxide in the hydrogen-containing gas before methanation is higher than that of the hydrogen-containing gas used in this embodiment. Therefore, the amount of hydrogen consumed by methanation of carbon monoxide is larger than that in the methanation process of this embodiment. Therefore, in the method of Document 2, the hydrogen recovery rate finally obtained is lower than that in the present embodiment. Moreover, in the method shown in Document 2, the amount of methane generated by methanation of carbon monoxide is larger than that in the methanation process of this embodiment. As a result, the gas finally obtained by the method of Document 2 has a lower hydrogen partial pressure than that of the present embodiment, making it difficult to use as a fuel for a fuel cell.

  On the other hand, in this embodiment, since carbon monoxide in the hydrogen-containing gas purified by the PSA method is methanated, the hydrogen gas recovery rate is higher than the method of Document 2 in which hydrogen is purified by methanation alone. . In the present embodiment, the amount of methane generated in the methanation step is also lower than that of the method of Document 2.

<Adsorption process>
In the adsorption step, carbon monoxide remaining in the hydrogen-containing gas purified by the PSA method is adsorbed on the adsorbent.

  The adsorbent used in the adsorption step is preferably at least one selected from the group consisting of activated carbon, zeolite and alumina. Thereby, the effect of this invention becomes remarkable.

  In this embodiment, it is preferable that copper or a copper compound is supported on the adsorbent. Thereby, adsorption of carbon monoxide to the adsorbent is promoted.

  The temperature of the hydrogen-containing gas in the adsorption step may be about −10 to 100 ° C. The pressure of the hydrogen-containing gas in the adsorption step may be about normal pressure to about 5 MPa.

  Conventionally, as shown in, for example, Japanese Patent No. 2607682 (hereinafter referred to as “Document 3”), a hydrogen-containing gas purified by adsorbing carbon monoxide on a gas diffusion electrode without being purified by the PSA method. There is known a method of using for a fuel cell. However, in the method of Document 2, since the hydrogen-containing gas purified by the PSA method is not used, the content of carbon monoxide in the hydrogen after purification is higher than that of this embodiment compared to this embodiment.

<Oxidation process>
In the oxidation step, carbon monoxide remaining in the hydrogen-containing gas purified by the PSA method is oxidized.

  In the present embodiment, in the oxidation step, it is preferable to oxidize carbon monoxide using a catalyst containing at least one of ruthenium and platinum. Ruthenium or platinum may be used by supporting it on one or more carriers selected from the group consisting of alumina, titania, silica, zirconia and the like.

  In the oxidation step, it is preferable to oxidize carbon monoxide by adding oxygen to the hydrogen-containing gas purified by the PSA method. Thereby, the oxidation of carbon monoxide in the hydrogen-containing gas is promoted.

  The temperature of the hydrogen-containing gas in the oxidation step may be about 50 to 300 ° C. The pressure of the hydrogen-containing gas in the oxidation step may be about normal pressure to about 5 MPa. The temperature of the catalyst in the oxidation step may be about 50 to 300 ° C.

  Conventionally, as shown in, for example, Japanese Patent Application Laid-Open No. 2000-169107 (hereinafter referred to as “Document 4”), a hydrogen-containing gas purified by methanation and oxidation of carbon monoxide without being purified by the PSA method. There is known a method of using for a fuel cell. However, since the method of Document 4 does not perform purification by the PSA method, the content of carbon monoxide in the hydrogen-containing gas before oxidation is higher than that of the hydrogen-containing gas used in this embodiment. Therefore, in the method of Document 4, the amount of carbon dioxide generated with the oxidation of carbon monoxide is larger than that in the oxidation process of the present embodiment. Therefore, in the method of Document 4, the content rate and partial pressure of carbon dioxide contained in the finally obtained hydrogen are higher than in the present embodiment. As a result, the gas finally obtained by the method of Document 4 has a lower hydrogen partial pressure than that of the present embodiment, making it difficult to use as a fuel for a fuel cell. Further, in the method of Document 4, since the amount of oxygen required for the oxidation of carbon monoxide is large, it is necessary to supply a large amount of oxygen to the hydrogen-containing gas as compared with the oxidation step of this embodiment. Therefore, not only the oxidation of carbon monoxide but also the oxidation (combustion) of hydrogen easily proceeds. Thereby, in the method of literature 4, compared with this embodiment, the recovery rate of hydrogen finally obtained becomes low. Further, the method of Document 4 is less safe than the present embodiment because a dangerous hydrogen oxidation reaction is likely to occur.

  On the other hand, in this embodiment, since carbon monoxide in the hydrogen-containing gas purified by the PSA method is oxidized, the amount of carbon dioxide and water generated in the oxidation process is smaller than that of the method of Document 4, and the amount of hydrogen gas The recovery rate is increased. Moreover, in this embodiment, compared with the method of the literature 4, the oxidation reaction of hydrogen does not occur easily, and the safety of purification improves.

  According to this embodiment, it becomes possible to reduce the content of carbon monoxide in hydrogen as compared with the method of purifying hydrogen by the PSA method alone and the methods of the above-mentioned documents 2 to 4. In the present embodiment, even if the carbon monoxide content in the hydrogen-containing gas purified by the PSA method is not reduced to a level applicable to a fuel cell vehicle, the methanation step, the adsorption step, or the In the oxidation step, the content of carbon monoxide in hydrogen can be reduced to a level that can be applied to a fuel cell vehicle. Specifically, in the present embodiment, the content of carbon monoxide in hydrogen can be reduced to 0.2 mass ppm or less. Hydrogen whose carbon monoxide content is reduced to 0.2 mass ppm or less is suitable as a fuel for fuel cell vehicles.

  When the reformed gas is purified by the PSA method alone and the carbon monoxide content in the hydrogen gas is reduced to about 1 ppm by mass as in the past, the hydrogen recovery is dependent on the reformed gas composition. The rate is about 85% by mass or more. However, when the reformed gas is purified by the PSA method alone and the carbon monoxide content in the hydrogen gas is reduced to less than 0.2 ppm by mass, the hydrogen is adsorbed on the adsorbent by increasing the pressure of the hydrogen-containing gas. Therefore, the hydrogen recovery rate is reduced to about 70% by mass or less. On the other hand, in this embodiment, even if the pressure of the hydrogen-containing gas is set low by purification by the PSA method, carbon monoxide can be removed in the subsequent purification step, so that the hydrogen recovery rate is not reduced without reducing the hydrogen recovery rate. It becomes possible to reduce the carbon monoxide content to such an extent that it can be applied to a fuel cell vehicle.

  If the content of carbon monoxide in hydrogen is reduced to 0.2 mass ppm or less by the PSA method alone, the hydrogen-containing gas in the PSA method is adjusted to a pressure higher than about 4.0 MPaG, or a refining device is installed in multiple stages. It is necessary to make it. However, as the hydrogen-containing gas is compressed at a higher pressure, the energy required for the compression increases, and the equipment (adsorption tower, compressor, etc.) for carrying out the PSA method increases in size, which increases the costs associated with purification. Multi-stage purification equipment is also expensive. In addition, the safety of the purification decreases as the pressure increases. On the other hand, in this embodiment, compared with the method of purifying hydrogen by the PSA method alone, it is possible to reduce the cost associated with purification and improve the safety of purification.

  The hydrogen shipping facility according to the present embodiment includes a facility for performing the hydrogen purification method according to the present embodiment. The hydrogen station according to the present embodiment includes equipment for performing the hydrogen purification method according to the present embodiment. That is, the hydrogen shipping facility and the hydrogen station according to the present embodiment include a facility for performing a methanation process, an adsorption process, or an oxidation process using a hydrogen-containing gas purified by the PSA method. For example, the hydrogen shipping facility supplies purified hydrogen gas to a hydrogen station for a fuel cell vehicle. The hydrogen station is installed along a road, for example, and supplies hydrogen directly to a fuel cell vehicle or the like.

  The hydrogen shipping facility and hydrogen station according to this embodiment reduce the cost and energy consumption associated with hydrogen purification and improve the safety of the purification compared to the shipping facility and hydrogen station that purify hydrogen by the PSA method alone. It is possible to make it. Therefore, the hydrogen shipping facility and the hydrogen station according to the present embodiment are easy to spread.

  The preferred embodiments of the hydrogen purification method, the hydrogen shipping facility, and the hydrogen station according to the present invention have been described above in detail, but the present invention is not limited to the above embodiments. For example, instead of the PSA method, carbon monoxide and other impurities remaining in the hydrogen-containing gas purified by the TSA method or TPSA method may be removed in the purification step. Also in this case, the same effects as those of the above-described embodiment can be obtained.

  EXAMPLES Hereinafter, although this invention is demonstrated more concretely based on an Example and a comparative example, this invention is not limited to a following example.

(Comparative Example 1)
Using naphtha as a raw material, a hydrogen-containing gas was produced by a steam reforming reaction. This hydrogen-containing gas was purified by the PSA method. In the PSA method, the hydrogen-containing gas was pressurized and the pressure of the hydrogen-containing gas was adjusted to 3.0 MPa. In the PSA method, the temperature of the pressurized hydrogen-containing gas was adjusted to 40 ° C. Hereinafter, the hydrogen-containing gas purified by the PSA method in Comparative Example 1 is referred to as “hydrogen-containing gas 1”.

  The composition of the hydrogen-containing gas 1 was analyzed by gas chromatography. The composition of the hydrogen-containing gas 1 is shown in Table 1. As shown in Table 1, the hydrogen concentration in the hydrogen-containing gas 1 was 99.99% by mass or more. On the other hand, the concentration of carbon monoxide remaining as an impurity in the hydrogen-containing gas 1 was 0.70 ppm.

Example 1
Carbon monoxide contained in the hydrogen-containing gas 1 was methanated using a commercially available 50% by mass nickel / silica catalyst to obtain hydrogen gas of Example 1. In methanation, a hydrogen-containing gas 1 at 300 ° C. was reacted under normal pressure. The 50 mass% nickel / silica catalyst means a catalyst having silica as a carrier and carrying 50 mass% of nickel with respect to the total mass of the catalyst.

(Example 2)
Carbon monoxide contained in the hydrogen-containing gas 1 was methanated using a 2% by mass Ru / alumina catalyst to purify the hydrogen gas of Example 2. In methanation, a hydrogen-containing gas 1 at 270 ° C. was reacted under normal pressure.

(Example 3)
Carbon monoxide contained in the hydrogen-containing gas 1 was methanated using a 2% by mass Rh / alumina catalyst to purify the hydrogen gas of Example 3. In the methanation, a hydrogen-containing gas 1 at 250 ° C. was reacted under normal pressure.

Example 4
Carbon monoxide contained in the hydrogen-containing gas 1 was methanated using a 5% by mass Fe / activated carbon catalyst to purify the hydrogen gas of Example 4. In methanation, a hydrogen-containing gas 1 at 350 ° C. was reacted under normal pressure.

(Example 5)
A hydrogen-containing gas 1 at normal temperature and normal pressure was treated with an adsorbent in which CuCl was supported on commercially available activated carbon. Thereby, carbon monoxide in the hydrogen-containing gas 1 was adsorbed by the adsorbent, and the hydrogen gas of Example 5 was purified.

(Example 6)
A hydrogen-containing gas 1 at room temperature and normal pressure was treated with an adsorbent in which CuCl was supported on a commercially available zeolite. Thereby, carbon monoxide in the hydrogen-containing gas 1 was adsorbed by the adsorbent, and the hydrogen gas of Example 6 was purified.

(Example 7)
A hydrogen-containing gas 1 at normal temperature and normal pressure was treated with an adsorbent in which CuCl was supported on commercially available alumina. Thereby, carbon monoxide in the hydrogen-containing gas 1 was adsorbed by the adsorbent, and the hydrogen gas of Example 7 was purified.

(Example 8)
A hydrogen-containing gas 1 at normal temperature and pressure was treated with a commercially available zeolitic adsorbent. Thereby, carbon monoxide in the hydrogen-containing gas 1 was adsorbed on the adsorbent, and the hydrogen gas of Example 8 was purified.

Example 9
A hydrogen-containing gas 1 at normal temperature and normal pressure was treated with a commercially available activated carbon-based adsorbent. Thereby, carbon monoxide in the hydrogen-containing gas 1 was adsorbed by the adsorbent, and the hydrogen gas of Example 9 was purified.

(Example 10)
Using a 0.5 mass% Ru / alumina catalyst, a hydrogen-containing gas 1 at 200 ° C. to which oxygen was added was reacted under normal pressure. Thereby, carbon monoxide in the hydrogen-containing gas 1 was oxidized to purify the hydrogen gas of Example 10.

(Example 11)
Using a 0.5 mass% Ru-0.1 mass% Pt / alumina catalyst, a hydrogen-containing gas 1 at 180 ° C. to which oxygen was added was reacted under normal pressure. Thereby, carbon monoxide in the hydrogen-containing gas 1 was oxidized to purify the hydrogen gas of Example 11.

(Example 12)
Using a 0.5 mass% Pt-0.1 mass% Ni / alumina catalyst, a hydrogen-containing gas 1 at 180 ° C. to which oxygen was added was reacted under normal pressure. Thereby, carbon monoxide in the hydrogen-containing gas 1 was oxidized to purify the hydrogen gas of Example 12.

  Each composition of the hydrogen-containing gas purified by the PSA method in Comparative Example 1 and the purified hydrogen gas of Examples 1 to 12 was analyzed by gas chromatography. The analysis results are shown in Table 1. In addition, “%” and “ppm” described in Table 1 are based on mass.

  The content of carbon monoxide in the hydrogen gas of Examples 1 to 12 was less than 0.2 mass ppm, and was confirmed to be smaller than that of Comparative Example 1.

Claims (7)

It comprises a methanation step for methanating carbon monoxide remaining in a hydrogen-containing gas purified by an adsorption method with a catalyst, an adsorption step for adsorbing the carbon monoxide on an adsorbent, and an oxidation step for oxidizing the carbon monoxide. A purification step of removing the carbon monoxide from the hydrogen-containing gas by at least one step selected from the group;
Hydrogen purification method. The catalyst used in the methanation step contains at least one selected from the group consisting of nickel, cobalt, iron, ruthenium and rhodium as an active metal.
The method for purifying hydrogen according to claim 1. The adsorbent used in the adsorption step is at least one selected from the group consisting of activated carbon, zeolite and alumina.
The method for purifying hydrogen according to claim 1 or 2. Copper is supported on the adsorbent,
The method for purifying hydrogen according to claim 3. In the oxidation step, the carbon monoxide is oxidized using a catalyst containing ruthenium or platinum.
The method for purifying hydrogen according to any one of claims 1 to 4. A facility for carrying out the method for purifying hydrogen according to any one of claims 1 to 5,
Hydrogen shipping equipment. A facility for carrying out the method for purifying hydrogen according to any one of claims 1 to 5,
Hydrogen station.