JP2008200656A - Dimethyl ether-reforming catalyst and its manufacturing method - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a dimethyl ether-reforming catalyst which prevents the uneven distribution of catalyst components and shows high activity at a reformation temperature of 300°C or lower, and also provide its manufacturing method. <P>SOLUTION: The dimethyl ether-reforming catalyst is a catalyst which steam-reforms a dimethyl ether at a temperature of 300°C or lower. The catalyst is formed in a prescribed shape by subjecting a mixture, which comprises particle powder comprising active metal and particle powder comprising zeolite, to compression molding. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

  The present invention relates to a dimethyl ether reforming catalyst that generates steam and reforms steam by adding water vapor to dimethyl ether and a method for producing the same.

  As one vision of the future society, the realization of a hydrogen energy society using hydrogen as an energy medium is attracting attention, and several promising hydrogen production methods are considered. Currently, the mainstream hydrogen production method produces hydrogen by a steam reforming method at a reaction temperature of 700 ° C. or higher using natural gas or liquefied petroleum gas as a raw material in the presence of a catalyst. In this manufacturing method, since impurities such as sulfur are included in the raw material, pretreatment of this impurity is necessary, and since the reaction temperature is high, it is necessary to use a material having excellent heat resistance for the reactor structural material.

  Thus, the conventional steam reforming requires a reaction temperature of 700 ° C. or more, and uses the combustion heat of fossil fuel as the heat source. When burning using hydrogen as an energy source, carbon dioxide, which is a global warming gas, is not produced. However, when hydrogen is produced, in addition to carbon dioxide produced during fuel reforming, Carbon dioxide is produced by the combustion of fossil fuels. Furthermore, when the combustion heat of fossil fuel is used as this heat source, air pollutants such as sulfur oxides are simultaneously generated in addition to the generation of carbon dioxide.

  In contrast, in steam reforming using dimethyl ether as a raw fuel, since dimethyl ether is a synthetic fuel, impurities such as sulfur are less than natural gas and liquefied petroleum gas. Further, in this steam reforming, it is shown that hydrogen generation is possible at a temperature of 400 ° C. or lower, and the possibility that hydrogen can be produced at a lower temperature than that of the conventional method is shown (for example, (See Patent Document 1).

In addition, many techniques have been disclosed regarding a method of generating hydrogen using oxygen-containing hydrocarbons that may reduce the environmental burden compared to conventional techniques. Among them, since the performance of the catalyst to be used affects the amount of hydrogen produced and the like when producing hydrogen, many techniques relating to the formation method of the catalyst have been disclosed. For example, a technique for forming a steam reforming catalyst by supporting an active metal on a solid acid using a coprecipitation method at the time of catalyst preparation is disclosed (for example, see Patent Document 2). Further, a technique for forming a steam reforming catalyst by applying an active metal sol on a solid acid has been disclosed (for example, see Patent Document 3). Furthermore, a steam reforming catalyst that can be used in a temperature range of 300 to 400 ° C. is formed by mixing a solid acid (γ alumina, etc.) and an active metal at a mixing ratio of 2 to 15 (solid acid / active metal). The technique to do is disclosed (for example, refer patent document 4). Further, a technique for forming a steam reforming catalyst using zeolite as a carrier and a technique for forming a steam reforming catalyst using a platinum group element as an active metal are disclosed (for example, Patent Documents 5-7). reference.).
Fukushima, et al., `` Hydrogen production with steam reforming of dimethyl ether at ether at the temperature less than 300 ℃ '', 15th World hydrogen Energy Conference 30D-03, 2004 JP 2005-95738 A JP 2005-170717 A JP 2005-66516 A Japanese Patent Laid-Open No. 2004-81901 JP 2003-47846 A JP 2003-47853 A

  In the steam reforming of dimethyl ether, it is known that the reaction proceeds at a relatively low temperature (reaction temperature of 200 to 500 ° C.), dimethyl ether is hydrolyzed to produce methanol, and the produced methanol is subjected to a steam reforming reaction to generate hydrogen. Is generated. Thus, since the reaction proceeds at a relatively low temperature, for example, effective use of industrial waste heat is required. For this purpose, it is possible to advance the reaction at the lowest possible temperature to widen the scope of application and to use industrial waste heat more efficiently. However, the hydrolysis reaction of dimethyl ether is difficult to proceed at a low temperature, and becomes a rate-limiting step within the reaction for producing hydrogen from dimethyl ether.

  As a catalyst for promoting hydrolysis of dimethyl ether, it is known that a substance having an acidic site on or inside a solid called a solid acid is effective. Specific examples of the solid acid include γ-alumina, zeolite, and heteropolyacid. In the case of using γ-alumina or zeolite, the strength of the acid is different, and when it is used for the dimethyl ether steam reforming reaction, an appropriate catalyst preparation method is required. In particular, when zeolite is used, since the zeolite has ion exchange properties, the catalyst preparation method using a metal solution has a problem that the ion exchange is performed and the function as a catalyst cannot be exhibited sufficiently. In addition, there is a problem that the function of the catalyst as a solid acid cannot be sufficiently exhibited by coating the surface of the solid acid with an active metal as in the conventional steam reforming catalyst described above. In addition, none of the conventional steam reforming catalysts described above can promote the reforming reaction by sufficiently proceeding the hydrolysis reaction of dimethyl ether at a low temperature (for example, 300 ° C. or lower).

  Accordingly, the present invention has been made to solve the above-described problems, and provides a dimethyl ether reforming catalyst that prevents uneven distribution of catalyst components and exhibits high activity at a reforming temperature of 300 ° C. or less, and a method for producing the same. For the purpose.

  In order to achieve the above object, according to one aspect of the present invention, there is provided a catalyst for steam reforming dimethyl ether under a temperature condition of 300 ° C. or less, which comprises mixing particle powder made of active metal and particle powder made of zeolite. Provided is a dimethyl ether reforming catalyst characterized in that a powder is formed into a predetermined shape by compression molding.

  According to this hydrogen generation catalyst, since the mixed powder of the particle powder made of active metal and the particle powder made of zeolite is formed by compression molding, the solid acid action of zeolite is sufficiently exhibited.

  According to another aspect of the present invention, there is provided a method for producing a catalyst for steam reforming dimethyl ether under a temperature condition of 300 ° C. or less, wherein a particle powder made of active metal and a particle powder made of zeolite are mixed in a predetermined manner. A method for producing a dimethyl ether reforming catalyst, comprising: a mixing step of mixing at a ratio to form a mixed powder; and a compression step of compressing the mixed powder at a predetermined pressure to form a predetermined shape. Is done.

  According to this method for producing a dimethyl ether reforming catalyst, the solid acid action of zeolite can be sufficiently exerted by compression molding a mixed powder of particle powder made of active metal and particle powder made of zeolite in the compression step. A dimethyl ether reforming catalyst is formed.

  ADVANTAGE OF THE INVENTION According to this invention, the dimethyl ether reforming catalyst which can prevent uneven distribution of a catalyst component and can show high activity at the reforming temperature of 300 degrees C or less, and its manufacturing method can be provided.

  Hereinafter, an embodiment of the present invention will be described with reference to the drawings.

  The dimethyl ether reforming catalyst according to an embodiment of the present invention is formed by compression molding a mixed powder of a particle powder made of active metal and a particle powder made of zeolite.

Zeolite is used as a component that particularly accelerates the hydrolysis reaction (see the following formula (1)) in the steam reforming reaction of dimethyl ether. The zeolite used here has a silica ratio (SiO ₂ / Al ₂ O ₃ ) contained in the zeolite of greater than 5 and 120 or less in terms of molar ratio. Specifically, it is preferable to use a FAU type, MFI type, KFI type, or mordenite type zeolite within the range of this molar ratio. The ratio of the silica to alumina (SiO ₂ / Al ₂ O ₃ ) contained in the zeolite is within the above range when the molar ratio of SiO ₂ / Al ₂ O ₃ is less than 5, and the effective activity. This is because a zeolite having a crystal lattice cannot be prepared, and when it is 120 or more, the active site for the reaction is lowered.

  Moreover, it is preferable that the average particle diameter (median diameter) of the particle powder of zeolite is 5-300 micrometers. The range of the particle size is preferable when the average particle size is smaller than 5 μm, it is difficult to homogenize the zeolite, and when the average particle size is larger than 300 μm, the particles are uniformly distributed without being unevenly distributed with the active metal particle powder. It is because it becomes difficult to mix.

  The active metal is used as a component that particularly accelerates a steam reforming reaction (see the following formula (2)) in which methanol produced by the hydrolysis reaction (see the following formula (1)) is converted into hydrogen and carbon dioxide. The active metals are Cu (copper), Zn (zinc), Al (aluminum), Ce (cerium), Zr (zirconium), Ag (silver), Fe (iron), Mn (manganese) and Ti (titanium). It is composed of at least three of these metals. For example, it is preferable that three types of Cu, Zn, and Al include any one of Zr, Ag, Fe, Mn, and Ti.

  The average particle diameter (median diameter) of the active metal particle powder is preferably 5 to 300 μm. The range of the particle size is preferable when the average particle size is smaller than 5 μm, it is difficult to make the active metal uniform, and when it is larger than 300 μm, it is uniformly distributed without being unevenly distributed with the particle powder made of zeolite. It is because it becomes difficult to mix.

  The dimethyl ether reforming catalyst is formed by compression molding a mixed powder of the above-described particle powder made of active metal and particle powder made of zeolite. Here, the dimethyl ether reforming catalyst is configured such that the weight of the zeolite contained in the catalyst is 5 to 50%, more preferably 5 to 40% with respect to the weight of the dimethyl ether reforming catalyst. Composed. The reason why the weight ratio of the zeolite is set in this range is that when the weight of the zeolite is less than 5%, the hydrolysis reaction of dimethyl ether cannot be promoted and sufficient catalytic activity cannot be obtained. Further, when the weight of the zeolite exceeds 50%, side reactions (see the following formulas (3) and (4)) proceed simultaneously with the hydrolysis reaction of dimethyl ether on the zeolite, leading to catalyst poisoning, This is because the catalytic activity is lowered.

Moreover, the bulk density of the dimethyl ether reforming catalyst formed by compression molding is 0.7 to 1.5 g / cm ³ . The reason for setting the bulk density in this range is that when the bulk density is less than 0.7 g / cm ³ , the mechanical strength of the catalyst is insufficient and the shape during molding cannot be maintained, and 1.5 g This is because when it exceeds / cm ³ , the amount of the catalyst that does not contribute to the catalytic reaction increases without contacting with the raw material components such as dimethyl ether.

  Here, the reforming reaction of dimethyl ether by the dimethyl ether reforming catalyst will be described.

In the dimethyl ether reforming catalyst described above, the dimethyl ether hydrolysis reaction (formula (1)) is first promoted by the zeolite having a solid acid action to produce methanol. Subsequently, the methanol produced by this hydrolysis reaction (formula (1)) produces hydrogen and carbon dioxide mainly by a steam reforming reaction (formula (2)) with an active metal.
CH ₃ OCH ₃ + H ₂ O → 2CH ₃ OH Formula (1)
CH ₃ OH + H ₂ O → 3H ₂ + CO ₂ Formula (2)

By using the dimethyl ether reforming catalyst according to the present invention, the above-described dimethyl ether reforming reaction can be advanced under a temperature condition of 200 to 300 ° C. More preferably, the above-described reforming reaction of dimethyl ether proceeds under a temperature condition of 225 to 300 ° C. When the temperature condition is lower than 200 ° C., the hydrolysis reaction and steam reforming reaction of dimethyl ether do not proceed sufficiently. When the temperature condition is higher than 300 ° C., the shift reaction represented by the formula (3) or the formula ( Side reactions such as the methanation reaction shown in 4) are likely to proceed, making it difficult to separate hydrogen gas and shortening the catalyst life.
CO ₂ + H ₂ → CO + H ₂ O Formula (3)
CO + 3H ₂ → CH ₄ + H ₂ O Formula (4)

  Moreover, it is preferable to set the value (henceforth S / DME) of the supply molar flow rate of the vapor | steam with respect to the supply molar flow rate of dimethyl ether to 3-10, and a more preferable range is 3-6. The value of S / DME within this range is preferable because when S / DME is less than 3, the stoichiometric amount is not satisfied, the steam becomes insufficient, and the side reaction proceeds. This is because much energy is required to bear the latent heat of vaporization of water, and energy efficiency is reduced.

  Next, the manufacturing method of a dimethyl ether reforming catalyst is demonstrated.

  First, a particle powder made of active metal having the above average particle size and a particle powder made of zeolite are prepared, and both are mixed at a predetermined mixing ratio to obtain a mixed powder uniformly mixed. Examples of the mixing method include a method of mixing while grinding the mixed powder in a mortar, a method of stirring using a stirrer, and a method of diffusing and mixing using a nonpolar solvent. Among these mixing methods, from the viewpoint of easy and uniform mixing, it is preferable to employ a method of mixing while grinding the mixed powder in a mortar or the like, and a method of stirring using a stirrer or the like.

Subsequently, the mixed powder in which the particle powder made of active metal and the particle powder made of zeolite are uniformly mixed is compressed at a predetermined pressure to form a predetermined shape. Examples of the forming method include a tableting method and an extrusion method in which the mixed powder is compressed and pressed into a predetermined shape, and a granulation method in which a thickener is added to the powder and kneaded. It is preferable to use a tablet method or an extrusion method. In particular, when compacting by a tableting method, it is preferable to apply a pressure of 1.0 to 2.5 t / cm ² as the load pressure, and a more preferable load pressure is 1.0 to 2.0 t / cm ² . By applying a pressure in the range of this weighted pressure, the dimethyl ether reforming catalyst in the above-described bulk density range can be formed. In order to easily form the dimethyl ether reforming catalyst in the above-described bulk density range, it is preferable to pressurize from one side when pressurizing. Further, although not particularly limited, examples of the shape of the dimethyl ether reforming catalyst to be formed include a columnar shape, a spherical shape, and a honeycomb shape.

  As described above, the dimethyl ether reforming catalyst of one embodiment is formed by compression molding a mixed powder of particle powder made of active metal and particle powder made of zeolite, so that the zeolite is, for example, a metal solution or the like Can be avoided. As a result, ion exchange in the zeolite having ion exchange properties can be prevented, so that the function as a catalyst can be sufficiently exhibited by the solid acid action of the zeolite.

  Furthermore, by limiting the average particle size of the particle powder made of active metal and the particle powder made of zeolite to a predetermined range, a uniformly mixed powder can be formed, and the catalytic function of each of the active metal and zeolite Can be formed.

  Next, the dimethyl ether reforming catalyst according to the present invention in which a mixed powder of active metal particle powder and zeolite particle powder is formed into a predetermined shape by compression molding is excellent under a temperature condition of 300 ° C. or less. It demonstrates that it has the modification characteristic of a dimethyl ether.

  Here, FIG. 1 is an explanatory view showing the steps of the method for producing a dimethyl ether reforming catalyst used in Example 1, Comparative Example 1 and Comparative Example 2. FIG.

(Example 1)
In Example 1, a dimethyl ether reforming catalyst (sample 1) is produced by the manufacturing method according to the present invention, in which a mixed powder obtained by mixing particle powder made of active metal and particle powder made of zeolite is formed into a predetermined shape by compression molding. did.

As the particle powder made of active metal, active metal particle powder having an average particle diameter (median diameter) of 250 μm made of oxides of copper, zinc and aluminum was used. Further, as the particle powder made of zeolite, a zeolite particle powder having an average particle diameter (median diameter) of 250 μm in which the ratio of silica to alumina (SiO ₂ / Al ₂ O ₃ ) is 55 in molar ratio was used. And both particle powder was mix | blended so that the weight of the zeolite contained in the sample 1 with respect to the weight of the sample 1 might be 10%, and it mixed uniformly by stirring using a stirrer, and was set as mixed powder.

Subsequently, the uniformly mixed powder was filled into a SUS (stainless steel) container having a diameter of 20 mm and a height of 100 mm, and a pressure of 1.5 t / cm ² was applied from one direction. The compression molded sample was cut into Sample 1. The produced sample 1 had a cylindrical shape with a diameter of 3 mm and a height of 5 mm, and a bulk density of 1.1 g / cm ³ .

  Subsequently, about 5 g of the prepared sample 1 was placed in a reaction tube composed of a SUS tube (stainless steel tube), filled with quartz wool before and after that, and dimethyl ether and water vapor so that S / DME was 5. A mixed gas mixed with was supplied to the reaction tube. The pressure condition was 0.02 MPa (gauge pressure). And the hydrogen production amount when the temperature in the predetermined point inside the sample 1 was 225 degreeC, 250 degreeC, and 275 degreeC was measured. The measurement result will be described later.

(Comparative Example 1)
In Comparative Example 1, a dimethyl ether reforming catalyst (sample 2) was prepared by using an impregnation method in which a solution in which an active metal was dissolved was impregnated into zeolite to prepare a catalyst.

First, a solution in which copper nitrate trihydrate, zinc nitrate hexahydrate and ammonium nitrate were dissolved in water was prepared so that the weight of zeolite contained in sample 2 was 10% with respect to the weight of sample 2. Into this solution, a zeolite particle powder having an average particle diameter (median diameter) of 250 μm in which the ratio of silica to alumina (SiO ₂ / Al ₂ O ₃ ) is 55 in terms of molar ratio is charged, and the zeolite particle powder is impregnated with the solution. I let you. Subsequently, the zeolite particle powder impregnated with the solution was heated to about 100 ° C. to evaporate water to obtain a zeolite particle powder to which a powdery active metal adhered. The obtained zeolite particle powder to which the active metal was adhered was filled into a SUS (stainless steel) container having a diameter of 20 mm and a height of 100 mm, and a pressure of 1.5 t / cm ² was applied from one direction. The compression molded sample was cut into Sample 2. The prepared sample 2 had a cylindrical shape with a diameter of 3 mm and a height of 5 mm, and a bulk density of 0.9 g / cm ³ .

  Using the sample 2 thus prepared, the amount of hydrogen generation was measured by the same measurement method and measurement conditions as in Example 1. The measurement result will be described later.

(Comparative Example 2)
In Comparative Example 2, a dimethyl ether reforming catalyst (sample 3) was prepared by separately forming a cylindrical active metal and a cylindrical zeolite and mixing them at a predetermined mixing ratio.

As the particle powder made of active metal, active metal particle powder having an average particle diameter (median diameter) of 250 μm made of oxides of copper, zinc and aluminum was used. This active metal particle powder was filled in a SUS (stainless steel) container having a diameter of 20 mm and a height of 100 mm, and a pressure of 1.5 t / cm ² was applied from one direction. The compression molded sample was cut. The formed active metal particle powder formed body had a cylindrical shape with a diameter of 3 mm and a height of 5 mm, and a bulk density of 1.2 g / cm ³ .

Further, as the particle powder made of zeolite, a zeolite particle powder having an average particle diameter (median diameter) of 250 μm in which the ratio of silica to alumina (SiO ₂ / Al ₂ O ₃ ) is 55 in molar ratio was used. This zeolite particle powder was filled in a SUS (stainless steel) container having a diameter of 20 mm and a height of 100 mm, and a pressure of 1.5 t / cm ² was applied from one direction. The compression molded sample was cut. The formed zeolite particle powder formed body had a cylindrical shape with a diameter of 3 mm and a height of 5 mm, and a bulk density of 0.8 g / cm ³ .

  Then, the active metal particle powder formed body and the zeolite particle powder formed body are mixed with each formed body, that is, the zeolite in the sample 3 with respect to the weight of the dimethyl ether reforming catalyst (sample 3). The mixture was blended so that the weight of the formed particle powder was 10%, and mixed uniformly by stirring with a stirrer.

  Using the sample 3 thus prepared, the amount of hydrogen generation was measured by the same measurement method and measurement conditions as in Example 1. The measurement result will be described later.

(Summary of Example 1, Comparative Example 1 and Comparative Example 2)
FIG. 2 is a characteristic diagram showing the measurement results of the amount of hydrogen generation in Example 1, Comparative Example 1, and Comparative Example 2 described above. Here, the vertical axis in FIG. 2 indicates the amount of hydrogen produced per catalyst per unit time and unit weight. In addition, this hydrogen production amount is converted into the volume in a standard state (1 atm, 0 degreeC).

  As shown in FIG. 2, when the sample 1 in Example 1 was used, it became clear that the amount of hydrogen generation was larger in the measured temperature conditions than in the case of Comparative Example 1 and Comparative Example 2. . In addition, it was found that when the sample 2 produced by using the impregnation method in Comparative Example 2 was used, the catalyst was particularly inactive under the measured temperature conditions. This is considered to be caused by impregnating the zeolite particle powder into the solution by the impregnation method, thereby causing ion exchange in the zeolite and failing to exhibit the solid acid action inherent in the zeolite. On the other hand, the sample 1 in Example 1 is not immersed in a solution, and the active metal and the zeolite are integrally formed with a predetermined bulk density only by compression formation. It is considered that the effect could be fully exhibited.

  In addition, from the results of Example 1 and Comparative Example 2, as compared with Comparative Example 2, the active metal particle powder formed body and the zeolite particle powder formed body were mixed with each other to constitute a dimethyl ether reforming catalyst. As shown in Example 1, it was revealed that the dimethyl ether reforming catalyst was formed by compression molding a mixed powder obtained by mixing particle powder made of active metal and particle powder made of zeolite. .

  Next, in the dimethyl ether reforming catalyst according to the present invention in which the mixed powder of the particle powder made of active metal and the particle powder made of zeolite is formed into a predetermined shape by compression molding, the catalyst with respect to the weight of the dimethyl ether reforming catalyst It is explained that it is preferable that the weight of the zeolite contained in is within the range of the present invention.

(Example 2)
In Example 2, the same dimethyl ether reforming catalyst (sample 1) as that prepared in Example 1 was used. The amount of hydrogen produced when the temperature at a predetermined point inside the sample 1 was 225 ° C., 250 ° C., 275 ° C., and 300 ° C. was measured using the same measurement method and measurement conditions as in Example 1. The measurement result will be described later.

(Example 3)
In Example 3, a dimethyl ether reforming catalyst (Sample 5) was produced in the same manner as in Example 1 described above. In addition, it produced so that the weight of the zeolite contained in the sample 5 might be 25% with respect to the weight of the sample 5. The amount of hydrogen produced when the temperature at a predetermined point inside the sample 5 was 225 ° C., 250 ° C., 275 ° C., and 300 ° C. was measured using the same measurement method and measurement conditions as in Example 1. The measurement result will be described later.

Example 4
In Example 4, a dimethyl ether reforming catalyst (Sample 6) was produced in the same manner as in Example 1 described above. In addition, it produced so that the weight of the zeolite contained in the sample 6 might be 50% with respect to the weight of the sample 6. The amount of hydrogen produced when the temperature at a predetermined point inside the sample 6 was 225 ° C., 250 ° C., 275 ° C. was measured using the same measurement method and measurement conditions as in Example 1. The measurement result will be described later.

(Comparative Example 3)
In Comparative Example 3, a dimethyl ether reforming catalyst (Sample 7) was produced in the same manner as in Example 1 described above. In addition, it produced so that the weight of the zeolite contained in the sample 7 might be 75% with respect to the weight of the sample 7. The amount of hydrogen produced when the temperature at a predetermined point inside the sample 7 was 225 ° C., 250 ° C., 275 ° C., and 300 ° C. was measured using the same measurement method and measurement conditions as in Example 1. The measurement result will be described later.

(Summary of Examples 2 to 4 and Comparative Example 3)
FIG. 3 is a characteristic diagram showing the measurement results of the amount of hydrogen generation in Examples 2 to 4 and Comparative Example 3 described above. Here, the vertical axis in FIG. 3 indicates the amount of hydrogen produced per catalyst per unit time and unit weight. In addition, this hydrogen production amount is converted into the volume in a standard state (1 atm, 0 degreeC).

  As shown in FIG. 3, when Sample 1 and Sample 5 in Example 2 and Example 3 were used, it was found that a good hydrogen production amount was obtained under the measured temperature conditions. Further, when the sample 6 in Example 4 was used, the hydrogen generation amount distribution was convex upward, but it was found that a good hydrogen generation amount was obtained under relatively low temperature conditions.

  On the other hand, in sample 7 prepared so that the weight of zeolite contained in the dimethyl ether reforming catalyst was 75% with respect to the weight of the dimethyl ether reforming catalyst, it was found that the catalyst was particularly inactive under the measured temperature conditions. .

  Although the present invention has been specifically described above with reference to the embodiments, the present invention is not limited to these embodiments, and various modifications can be made without departing from the scope of the invention.

Explanatory drawing which showed the process of the manufacturing method of the dimethyl ether reforming catalyst used in Example 1, the comparative example 1, and the comparative example 2. FIG. The characteristic view which shows the measurement result of the hydrogen production amount in Example 1, Comparative Example 1, and Comparative Example 2. The characteristic view which shows the measurement result of the hydrogen production amount in Example 2-Example 4 and Comparative Example 3.

Claims (9)

A catalyst for steam reforming dimethyl ether under a temperature condition of 300 ° C. or lower,
A dimethyl ether reforming catalyst, wherein a mixed powder of a particle powder made of an active metal and a particle powder made of zeolite is formed into a predetermined shape by compression molding. The dimethyl ether reforming catalyst according to claim 1, wherein a bulk density of the catalyst is 0.7 to 1.5 g / cm ³ .   The dimethyl ether reforming catalyst according to claim 1 or 2, wherein a weight of the zeolite contained in the catalyst with respect to a weight of the catalyst is 5 to 50%.   The dimethyl ether modified according to any one of claims 1 to 3, wherein the active metal includes at least three of Cu, Zn, Al, Ce, Zr, Ag, Fe, Mn, and Ti. Quality catalyst. 5. The ratio of silica to alumina (SiO ₂ / Al ₂ O ₃ ) contained in the zeolite is greater than 5 and 120 or less in terms of molar ratio. 6. Dimethyl ether reforming catalyst. A method for producing a catalyst for steam reforming dimethyl ether under a temperature condition of 300 ° C. or less,
A mixing step of mixing powder particles made of active metal and particle powders made of zeolite at a predetermined mixing ratio to make a mixed powder;
A compression step of compressing the mixed powder at a predetermined pressure to form a predetermined shape.   The method for producing a dimethyl ether reforming catalyst according to claim 6, wherein the weight of the zeolite contained in the mixed powder is 5 to 50% with respect to the weight of the mixed powder.   The method for producing a dimethyl ether reforming catalyst according to claim 6 or 7, wherein the active metal contains at least three or more of Cu, Zn, Al, Ce, Zr, Ag, Fe, Mn and Ti. . 9. The ratio of silica to alumina (SiO ₂ / Al ₂ O ₃ ) contained in the zeolite is greater than 5 and 120 or less in terms of molar ratio. 9. A method for producing a dimethyl ether reforming catalyst.

Images