JP2007252988A - Catalyst for carbon monoxide methanation and methanation method of carbon monoxide using the catalyst - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a catalyst for removing carbon monoxide capable of selective and highly active methanation of carbon monoxide even at a low temperature. <P>SOLUTION: The catalyst for carbon monoxide methanation is made by depositing Ru and a metal other than Ru and the deposition amount of Ru and the metal other than Ru lies the range of 0.5 to 15 wt.% in the catalyst. The metal other than Ru is at least one kind of metal selected from 4B group, 6A group, 7A group and 8 group and, specifically, is at least one kind selected from Sn, Mo, W, Re, Pt, Pd, Rh, Ni and Co. When the sum of Ru and the metal other than Ru is 100 wt.%, the proportion of Ru lies in the range of 20 to 90 wt.%. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

  The present invention relates to a catalyst for removing carbon monoxide in a hydrogen-containing gas and a method for removing carbon monoxide using the catalyst. More particularly, the present invention relates to a carbon monoxide removal catalyst that can selectively methanate carbon monoxide with high activity even at low temperatures, and a carbon monoxide removal method using the catalyst.

In recent years, power generation using fuel cells has been attracting attention because of its low pollution and low energy loss, and research and development for practical use is being promoted.
Various types of fuel cells are known, depending on the type of fuel and electrolyte, operating temperature, etc. Among them, hydrogen-oxygen using hydrogen as a reducing agent (active material) and oxygen or air or the like as an oxidizing agent. The development of fuel cells (low temperature operation type fuel cells) is the most advanced.

  There are various types of hydrogen-oxygen fuel cells depending on the type of electrolyte, the type of electrodes, and the like, and typical examples include phosphoric acid fuel cells and solid polymer fuel cells. In such fuel cells, platinum catalysts are often used for electrodes. However, platinum used in the electrode is easily poisoned by carbon monoxide (hereinafter also referred to as CO). Therefore, if the fuel contains more than a certain level of CO, the power generation performance may be reduced or depending on the concentration. There is a serious problem that power generation becomes impossible.

The deterioration of the activity of the catalyst due to CO poisoning is particularly remarkable at low temperatures, and this problem becomes particularly serious in the case of a low temperature operation type fuel cell.
Therefore, pure hydrogen is preferable as a fuel for a fuel cell using such a platinum-based electrode catalyst. However, from a practical point of view, it is inexpensive and has excellent storage properties or is already equipped with a public supply system. Fuel, for example, methane, natural gas (LNG), petroleum gas (LPG) such as propane, butane, various hydrocarbon fuels such as naphtha, gasoline, kerosene, light oil, alcohol fuel such as methanol, city gas, It has become common to use hydrogen-containing gas obtained by steam reforming of other fuels for hydrogen production or the like, and fuel cell power generation systems incorporating such reforming equipment are being promoted. However, since these reformed gases generally contain a considerable concentration of CO in addition to hydrogen, this CO is converted into a harmless to the platinum-based electrode catalyst, and the CO concentration in the fuel is reduced. There is a strong demand for the development of technologies that can be used. For example, in a polymer electrolyte fuel cell, it is desirable to reduce the CO concentration to a low concentration of usually 100 ppm by volume or less, preferably 50 ppm by volume or less, more preferably 10 ppm by volume or less.

In order to solve the above problem, as one of means for reducing the concentration of CO in the fuel gas (hydrogen-containing gas in the reformed gas), a shift reaction represented by the following formula (1) (water gas shift) A technique using reaction) has been proposed.
_{CO + H 2 O = CO 2} + H 2 (1)
However, in the reaction using only this shift reaction, there is a limit to the reduction of the CO concentration due to restrictions on chemical equilibrium, and it is generally difficult to reduce the CO concentration to 1% or less.

Therefore, as a means for reducing the CO concentration to a lower concentration, a method has been proposed in which oxygen or an oxygen-containing gas (air or the like) is introduced into the reformed gas and CO is converted to CO ₂ . However, in this case, since a large amount of hydrogen is present in the reformed gas, hydrogen is also oxidized when attempting to oxidize CO, resulting in loss of hydrogen and insufficient removal of CO.

Recently, a method of converting CO to methane by methanation with hydrogen (hereinafter also referred to as methanation) has been reviewed. For example, in JP-A-3-93602 (Patent Document 1) and JP-A-11-86892 (Patent Document 2), a catalyst (Ru / γ-alumina catalyst) in which Ru is supported on a γ-alumina carrier, A method of contacting hydrogen gas containing CO is disclosed. However, if the hydrogen gas contains carbon dioxide (CO ₂ ),
There was also a methanation reaction of carbon dioxide, which was a side reaction. For this reason, the development of a catalyst having high activity of CO methanation reaction, which is the main reaction, and high selectivity (low carbon dioxide methanation reaction) is desired.

In order to solve the above problems, a catalyst in which a Ru compound and an alkali metal compound and / or an alkaline earth metal compound are supported on an inorganic oxide carrier has been proposed. (Patent Document 3: JP 2002-68707 A)
Japanese Patent Laid-Open No. 3-93602 JP-A-11-86892 JP 2002-68707 A

However, the above-described conventional catalysts, particularly low temperature operation type fuel cell electrode catalysts, have problems such as insufficient activity and sometimes a rapid increase in reaction temperature.
That is, even when the reaction temperature is low, a catalyst and a removal method that can efficiently remove carbon monoxide in a hydrogen-containing gas with high selectivity and activity of the methanation reaction of carbon monoxide, which is the main reaction. It was desired to provide.

  Under these circumstances, the present inventors diligently studied to solve the above problems, and as a result, the reaction temperature of the catalyst in which a metal other than Ru is supported together with Ru as an active component on the metal oxide support is low. Even in this case, high activity and selectivity were exhibited in the methanation reaction of CO, and in addition, the shift reaction described above was accompanied and the CO removal effect was improved, and the present invention was completed.

That is, the configuration of the present invention is as follows.
[1] A metal other than Ru and Ru is supported on a metal oxide support,
A catalyst for carbon monoxide methanation, wherein the supported amount of metal other than Ru and Ru is in the range of 0.5 to 15% by weight in the catalyst.
[2] The catalyst for carbon monoxide methanation according to [1], wherein the metal other than Ru is one or more metals selected from Group 4B, Group 6A, Group 7A and Group 8.
[3] The metal other than Ru is at least one selected from the group consisting of Sn, Mo, W, Re, Pt, Pd, Rh, Ni and Co [1] or [2] Catalyst for carbon monoxide methanation.
[4] The catalyst for carbon monoxide methanation [1] to [3], wherein the ratio of Ru is in the range of 20 to 90% by weight when the total of the metals other than Ru and Ru is 100% by weight.
[5] The metal oxide support is one or more oxides selected from NiO, CoO (including Co ₃ O ₄ ), CeO ₂ , ZrO ₂ , Al ₂ O ₃ , TiO ₂ , SiO ₂ , or these A catalyst for carbon monoxide methanation [1] to [4], which is a composite oxide.
[6] The catalyst for carbon monoxide methanation having a CO adsorption amount in the range of ³ to 20 cm ³ / g-Cat [1] to [5].
[7] The catalyst for carbon monoxide methanation [1] to [6], wherein the average particle diameter of the metal other than Ru and Ru determined from CO adsorption is in the range of 0.5 to 5 nm.
[8] A carbon monoxide methanation method comprising contacting the methanation catalyst of [1] to [5] with a carbon monoxide gas-containing hydrogen gas.
[9] The method for methanation of carbon monoxide, wherein the temperature (reaction temperature) at the time of contact is in the range of 120 to 200 ° C.

  According to the present invention, the carbon monoxide methanation reaction, which is the main reaction, is selected even when the reaction temperature is low because a predetermined amount of metal other than Ru is supported together with Ru on the inorganic oxide support. It is possible to provide a catalyst and a removal method that have a high rate and activity and can effectively remove carbon monoxide in a hydrogen-containing gas.

Hereinafter, modes for carrying out the present invention will be described.
In the carbon monoxide methanation catalyst according to the present invention, Ru and a metal other than Ru are supported on a metal oxide support. The metal other than Ru is preferably one or more metals selected from Group 4B, Group 6A, Group 7A and Group 8.
Among them, the group 4B metal is selected from the group consisting of Sn, the group 6A metal is Mo, W, the group 7A metal is Re, and the group 8 metal is Pt, Pd, Rh, Ni and Co. One or more metals are preferably used.

The reason why each of the above metals is preferable is not clear, but in the case of Sn, it is conceivable to improve the activity by promoting the elimination of the carbon species adsorbed on Ru.
In the case of Mo and W, it is considered that active hydrogen is generated by dissociative adsorption of H ₂ and promotes hydrogenation to improve the activity. In the case of Re, it is considered that the activity is improved by promoting the adsorption and desorption of the carbon species to Ru. In the case of Pt, Pd, Rh, Ni, and Co, it is considered that the activity is improved by dissociating and adsorbing CO and H ₂ .

In this way, by supporting these metals together with Ru, an excellent effect that has not existed in the past is exhibited.
The amount of the metal supported other than Ru and Ru is preferably in the range of 0.5 to 15% by weight, more preferably 1.0 to 10% by weight, based on the catalyst weight.

When the loading amount of metals other than Ru and Ru is smaller than the lower limit of the above range, the activity is insufficient. When the loading amount of the metal other than Ru and Ru exceeds the above range, CO ₂ methanation occurs although the activity is high, the selectivity is lowered, and as a result, the effect of removing CO becomes insufficient.

Of metals other than Ru and Ru, the ratio of Ru is 20 to 90% by weight when the total is 100% by weight.
Furthermore, it is preferable that it exists in the range of 25 to 60 weight%.
If the ratio of Ru in the metal other than Ru and Ru is within the above range, adsorption and desorption of carbon species, H ₂
The dissociative adsorption of CO and the dissociative adsorption of CO are promoted in a coordinated manner, have high activity even when the reaction temperature is low, and can suppress side reactions, so that a highly selective catalyst can be obtained.

In addition to the above characteristics, the catalyst for carbon monoxide methanation according to the present invention in which the ratio of Ru in the metal other than Ru and Ru falls within the above range shows an increase in CO ₂ when the reaction temperature is low. This also causes a high CO removal effect.

Next, as the metal oxide support used in the present invention, one or more oxides selected from NiO, CoO (including Co ₃ O ₄ etc.), CeO ₂ , ZrO ₂ and Al ₂ O ₃ , A composite oxide is particularly preferable.
Specifically, ZrO ₂ —CoO, ZrO ₂ —NiO, ZrO ₂ —CeO ₂ , ZrO ₂ —CoO—NiO, NiO—CoO, CoO—CeO ₂ , NiO—CoO—CeO ₂ , ZrO ₂ —NiO—CoO— _{CeO 2, Al 2 O 3 -Co} 3 O 4, Al 2 O 3 -CeO 2 -CoO, Al 2 O 3 -NiO,
Examples thereof include TiO ₂ —CoO, TiO ₂ —NiO, and TiO ₂ —SiO ₂ —Co ₃ O ₄ .

  When the composite oxide contains at least one of Ni and Co oxides in an amount of approximately 10% by weight or more, preferably 30% by weight or more, high activity can be obtained even when the reaction temperature is low.

  Further, when at least one of the oxides of Zr, Al, Ti, and Si is contained in an amount of approximately 20% by weight or more, preferably 50% by weight or more, the specific surface area is improved, and thus high activity can be obtained. .

When the Ce oxide is contained in an amount of 3.0% by weight or more, preferably 10.0% by weight or more, the selectivity is excellent and the runaway reaction accompanied by heat generation due to the methanation of CO ₂ is suppressed. can do. Among them, CoO—NiO—ZrO ₂ —CeO ₂ , CoO—NiO—CeO ₂ , ZrO ₂ —CeO ₂ —NiO, TiO ₂ —CeO ₂ —CoO, ZrO ₂ —CeO ₂ —
A composite oxide containing CeO ₂ such as CoO has a remarkable effect of improving selectivity and suppressing a runaway reaction accompanied by heat generation.

The catalyst for carbon monoxide methanation according to the present invention preferably has a CO adsorption amount of ³ to 20 cm ³ / g-Cat, more preferably 8 to 20 cm ³ / g-Cat.
When the amount of CO adsorption is less than the lower limit of the above range, sufficient adsorption cannot be obtained because CO adsorption and activation are insufficient. When the amount of CO adsorption exceeds the above upper limit, it is difficult to adsorb, and even if adsorbed, the activity is too high and a runaway reaction accompanied by heat generation may occur.

  The amount of CO adsorption in the present invention is determined by using a catalyst analyzer (BEL-CAT, manufactured by Nippon Bell Co., Ltd.), reducing the catalyst at 400 ° C. for 30 minutes in the device, and performing CO adsorption by the pulse method. Can be measured.

  The amount of CO adsorption depends on the metal particle diameter and metal, and increases as the number of small metal particles increases. The metal particle diameter can be adjusted by controlling the reduction conditions (lower temperature is preferable if the temperature can be reduced), the type of metal, the type of support, and the specific surface area.

  Moreover, it is preferable that the average particle diameter of the supported Ru and Ru other than Ru obtained from the CO adsorption amount obtained above is in the range of 0.5 to 5 nm, more preferably 0.8 to 4 nm. If the average particle diameter of the metal exceeds the upper limit of the above range, sufficient adsorption cannot be obtained because CO adsorption and activation are insufficient. It is difficult to carry a metal whose average particle diameter is less than the lower limit of the above range.

  In addition, the average particle diameter of the metal calculated | required from CO adsorption amount calculates the average atomic weight and average atomic radius of a supported metal from the ratio of the supported metal, and is described in a catalyst analyzer (BEL-CAT) instruction manual. It can be calculated using a calculation formula.

The specific surface area of the catalyst is preferably in the range of 30 to 200 m ² / g, more preferably 60 to 120 m ² / g.
When the specific surface area of the catalyst is less than the lower limit of the above range, the activity is insufficient and it becomes difficult to operate at a high SV (superficial velocity). Even if the specific surface area of the catalyst is larger than the upper limit of the above range, the activity and selectivity tend to decrease greatly when operated for a long time.

The pore volume of the catalyst is preferably in the range of 0.10 to 0.45 ml / g, more preferably 0.15 to 0.30 ml / g.
When the pore volume of the catalyst is less than the lower limit of the above range, sufficient activity may not be obtained.

Increasing the pore volume of the catalyst beyond the upper limit of the above range is difficult to obtain in the composition range of the present invention.
The pore volume depends on the specific surface area of the oxide carrier and neutralizes the metal salt to form a gel. The pore volume is adjusted by controlling the gel size, aging conditions, and the like.

  In the catalyst for carbon monoxide methanation according to the present invention, the support component and the active component are in the above-mentioned range, the specific surface area and pore volume of the catalyst are in the above-mentioned range, and used for carbon monoxide methanation. If possible, there is no particular limitation, and it can be produced by a conventionally known method. In addition, as the various oxide sols and silica sources, silicic acid solutions obtained by dealkalizing water glass can be preferably used.

  For example, zirconium salt, nickel salt, cobalt salt, cerium salt, aluminum salt, titanium salt, silicate aqueous solution of one or more metal salts, preferably two or more mixed metal salt aqueous solutions are prepared as a carrier component raw material.

  As the nickel salt, nickel nitrate, nickel sulfate, nickel chloride, nickel acetate, nickel carbonate or the like is used, and as the cobalt salt, cobalt nitrate, cobalt sulfate, cobalt chloride, cobalt acetate or the like is used. As the cerium salt, cerium nitrate, cerium chloride, cerium sulfate, etc. are used. Zirconium nitrate, zirconium chloride, zirconyl chloride, zirconium sulfate, zirconium acetate, zirconyl nitrate, zirconyl sulfate, zirconium carbonate, etc. are used as the zirconium salt, and aluminum chloride, aluminum sulfate, aluminum nitrate, etc. are used as the aluminum salt. As the salt, titanium tetrachloride, titanium sulfate or the like is used, and as the silicate, water glass or the like is mainly used. This is mixed as needed so that it may become a desired oxide composition.

The mixed salt aqueous solution preferably has a total oxide concentration in the range of 7.5% by weight or less.
When the concentration of the mixed salt aqueous solution exceeds 7.5% by weight as the total oxide, the resulting catalyst has a small specific surface area, and sufficient activity may not be obtained.

Next, an aqueous solution of a basic compound is added to the mixed salt aqueous solution to neutralize it, and it is aged as necessary to prepare a hydrogel.
Examples of basic compounds that can be used include aqueous alkali metal solutions such as NaOH, KOH, Na ₂ CO ₃ , ammonia, tetramethylammonium hydroxide, and the like.

The temperature for aging is usually preferably in the range of 30 to 100 ° C., and the time is usually about 0.5 to 24 hours.
The hydrogel is then filtered and washed. The washing method is not particularly limited as long as it can remove by-produced salt such as sodium chloride, and a conventionally known method can be adopted. For example, a method of sufficiently applying warm water, a method of applying ammonia water, an ultrafiltration membrane method and the like can be suitably employed.

The carrier is then prepared from the hydrogel, and there are two main methods:
One is a method in which the washed gel is dried and fired, and the obtained mixed oxide powder is pulverized as necessary and molded with a tablet molding machine or the like.

  Another method is to add a molding aid such as cellulose to the washed gel as necessary, adjust the moisture, heat and concentrate, knead, knead, etc., and then form a pellet with an extruder, etc. In this method, the pellets are formed into a spherical shape with a malmerizer, a rolling granulator or the like, then dried and fired. Both of these can be employed without any particular limitation.

The carrier obtained by firing is then loaded with a ruthenium component and a component other than ruthenium in order to carry a metal other than Ru and Ru.
The loading method is not particularly limited as long as a predetermined amount of a ruthenium component and a component other than ruthenium can be loaded. Usually, a ruthenium salt aqueous solution having a volume corresponding to the pore volume of the carrier and a salt other than ruthenium are used. A mixed aqueous solution with an aqueous solution is prepared, impregnated into a carrier, and then dried.

  As the ruthenium salt, ruthenium chloride, ruthenium nitrate or the like is used. As the metal salt other than Ru, it is preferable to use a salt of one or more metals selected from Group 4B, Group 6A, Group 7A and Group 8. Among these, metal salts such as 4B group Sn, 6A group Mo, W, 7A group Re, 8 group Pt, Pd, Rh, Ni and Co can be preferably used.

  Specifically, tin chloride, tin acetate, tin sulfate, tin oxalate, molybdenum chloride, ammonium molybdate, ammonium tungstate, rhenium chloride, ammonium perrhenate, chloroplatinic acid, dichlorotetraamineplatinum, palladium nitrate, chloride Palladium, rhodium nitrate, rhodium chloride, nickel nitrate, nickel sulfate, nickel chloride, cobalt nitrate, cobalt chloride, cobalt sulfate and the like are preferably used.

  The concentration of the mixed salt aqueous solution is usually a predetermined amount, that is, a concentration that can be supported so that the total content of metals other than Ru and Ru in the obtained catalyst is 0.5 to 15% by weight. When the concentration of the aqueous solution is low, or when the loading amount is large, the impregnation and drying can be repeated.

  The drying conditions are not particularly limited, but are usually dried at 80 to 200 ° C. After drying, the catalyst for carbon monoxide methanation can be obtained by reduction at 100 to 700 ° C., preferably 150 to 400 ° C. in a reducing gas atmosphere.

As the reducing atmosphere gas, hydrogen gas or a mixed gas of hydrogen gas and inert gas such as nitrogen gas is usually used.
If the temperature during the reduction is less than 100 ° C., the reduction of the active metal becomes insufficient and sufficient activity may not be obtained.

If the temperature at the time of reduction exceeds 700 ° C., sintering occurs, the specific surface area of the resulting catalyst is small, and the activity may be insufficient.
Although the time for reduction varies depending on the temperature, it is usually 0.5 to 12 hours.

  Further, the shape of the catalyst for carbon monoxide methanation is not particularly limited, and can be appropriately selected depending on the reaction method, reaction conditions, etc. The fine powder can be used as it is, and the fine powder is used after being pressure-molded. It is also possible to suitably use a honeycomb or pellet extruded product, or a pellet made into a spherical shape (bead shape).

Next, the carbon monoxide methanation method according to the present invention will be described.
The methanation method for carbon monoxide according to the present invention is characterized in that the methanation catalyst is brought into contact with a hydrogen gas containing carbon monoxide gas. As the methanation catalyst, the aforementioned catalyst is used.

As the carbon monoxide gas-containing hydrogen gas, a fuel gas (hydrogen-containing gas in the reformed gas) is used, and this gas usually contains hydrogen gas, carbon monoxide gas, carbon dioxide gas, water vapor, and the like. May contain methane.
The hydrogen gas concentration in the fuel gas used in the present invention is 71 to 89 vol%, the carbon monoxide gas concentration is 0.3 to 1.0 vol%, the carbon dioxide gas concentration is 10 to 25 vol%, and the methane gas concentration is 0 to 3.0 vol. % (Gas composition). Furthermore, it contains water vapor at a ratio of 20 vol% to 70 vol% with respect to the gas in the fuel.

  The temperature at which the methanation catalyst and carbon monoxide gas-containing hydrogen gas are brought into contact (hereinafter referred to as reaction temperature) is preferably in the range of 100 to 250 ° C, more preferably 130 to 190 ° C.

When the reaction temperature is less than 100 ° C., the water vapor contained in the reaction gas is condensed and it is difficult to carry out the reaction continuously.
When the reaction temperature exceeds 250 ° C., it becomes the temperature range of the CO shift reaction (CO + H ₂ O → CO ₂ + H ₂ ), and carbon monoxide that can be converted by the CO shift reaction is methanated by the methanation reaction. The hydrogen concentration contained in the fuel gas is significantly reduced.

The fuel gas treated by such a carbon monoxide methanation method according to the present invention has a carbon monoxide gas concentration of 20 ppm or less.
[Example]
EXAMPLES Hereinafter, although an Example demonstrates this invention more concretely, this invention is not limited by these Examples.
[Example 1]
Preparation of catalyst for methanation (1 ) Zirconyl nitrate solution (ZrO ₂ concentration: 25.0%) 168.00 g, cerium nitrate-6
50.20 g of hydrate, 100.89 g of cobalt nitrate hexahydrate and 46.71 g of nickel nitrate hexahydrate were dissolved in 2800 g of water to obtain a mixed aqueous solution (1).

86.51 g of sodium hydroxide was dissolved in 3200 g of water, and the mixed aqueous solution (1) was added thereto while stirring to prepare a hydrogel slurry, and then aged at 80 ° C. for 2 hours.
The aged hydrogel is filtered, washed with sufficient warm water, dried at 120 ° C for one day, and then baked in the air at 550 ° C for 1 hour to obtain a composite oxide powder (1). It was.

Next, the complex oxide powder (1) is filled into a tablet molding machine, pressure-molded at 50 kg / cm ² , pulverized, and the particle size is adjusted to 20 to 42 mesh to obtain the methanation catalyst carrier (1). Prepared.
Ruthenium chloride and palladium chloride were dissolved so that the metal weight ratio was Ru: Pd = 1: 0.8 and the metal concentration was 10% by weight to prepare an impregnation solution (1). 23.56 g of impregnation solution (1) was absorbed into 50 g of support (1) for methanation catalyst, stirred well, allowed to stand for 1 hour, dried at 120 ° C. for 8 hours, and then adjusted to pH 10-11. Stir in 2 L of the prepared sodium hydrogen carbonate solution, wash with sufficient warm water, dry at 120 ° C. for 5 hours, perform reduction treatment in a hydrogen stream at 400 ° C. for 1.5 hours, Nation catalyst (1) was prepared. The active component, the content of each carrier component, the specific surface area and the pore volume were measured, and the results are shown in the table.
The catalyst for activity test methanation (1) (4.2 ml) was filled into a stainless steel reaction tube with an inner diameter of 12 mm, and again for 1 hour under a flow of hydrogen-nitrogen mixed gas (H ₂ concentration 10 VOL%) at a catalyst layer temperature of 400 ° C. Then, after reducing the catalyst layer temperature to 120 ° C., the reaction gas mixture (carbon monoxide 0.6 vol%, carbon dioxide 20.0 vol%, methane 2.0 vol%, hydrogen 51.37 vol%) , Water vapor 33.3 Vol%) is circulated so that SV = 2,500 h ^−1, and the product gas in a steady state after about 1 hour is analyzed by gas chromatography and an infrared spectroscopic gas densitometer. The results of measuring the tube outlet CO concentration, CO ₂ concentration, and CH ₄ concentration are shown in the table.

As the selectivity, the increase / decrease in CO ₂ from 20.0 Vol% of carbon dioxide in the reaction gas is shown in the table, and the case where the increase / decrease in CO ₂ is small is evaluated as being excellent in selectivity.
Similarly, the reaction was carried out at 140 ° C. and 160 ° C., and the results are shown in the table.
[Example 2]
Preparation of catalyst for methanation (2) In Example 1, ruthenium chloride and palladium chloride were dissolved so that the metal weight ratio was Ru: Pd = 1: 0.4, and the metal concentration was 10% by weight. A methanation catalyst (2) was prepared in the same manner except that (2) was prepared and 18.13 g of the impregnation solution (2) was absorbed. The active component, the content of each carrier component, the specific surface area and the pore volume were measured, and the results are shown in the table.
Activity test An activity test was conducted in the same manner as in Example 1, and the CO concentration, CO ₂ concentration and CH ₄ concentration were shown in the table.
[Example 3]
Preparation of catalyst for methanation (3) In Example 1, ruthenium chloride and palladium chloride were dissolved so that the metal weight ratio was Ru: Pd = 1: 1.6, and the metal concentration was 10% by weight. A methanation catalyst (3) was prepared in the same manner except that (3) was prepared and 34.76 g of the impregnation solution (3) was absorbed. The active component, the content of each carrier component, the specific surface area and the pore volume were measured, and the results are shown in the table.
Activity test An activity test was conducted in the same manner as in Example 1, and the CO concentration, CO ₂ concentration and CH ₄ concentration were shown in the table.
[Example 4]
Preparation of catalyst for methanation (4) In Example 1, Ru: Pd: Pt = 1: 0.6: 0.4 in terms of metal weight ratio of ruthenium chloride, palladium chloride and chloroplatinic acid, and the metal concentration was 10 wt. The methanation catalyst (4) was prepared in the same manner except that the impregnation solution (4) was prepared and 26.32 g of the impregnation solution (4) was absorbed. The active component, the content of each carrier component, the specific surface area and the pore volume were measured, and the results are shown in the table.
Activity test An activity test was conducted in the same manner as in Example 1, and the CO concentration, CO ₂ concentration and CH ₄ concentration were shown in the table.
[Example 5]
Preparation of catalyst for methanation (5) 154.47 g of aluminum nitrate nonahydrate, 50.20 g of cerium nitrate hexahydrate, 100.89 g of cobalt nitrate hexahydrate, and nickel nitrate hexahydrate 46 .71 g was dissolved in 2780 g of water to obtain a mixed aqueous solution (2).
242.01 g of sodium hydroxide was dissolved in 3220 g of water, and the mixed aqueous solution (2) was added thereto while stirring to prepare a hydrogel slurry, and then aged at 80 ° C. for 2 hours.

The aged hydrogel is filtered, washed with sufficient warm water, dried at 120 ° C for one day,
Subsequently, it baked in air | atmosphere at 550 degreeC for 1 hour, and composite oxide powder (2) was obtained. Next, the complex oxide powder (2) is filled into a tablet molding machine, pressure-molded at 50 kg / cm ² , then pulverized, and the particle size is adjusted to 20 to 42 mesh to adjust the carrier for methanation catalyst (2). Was prepared.

Ruthenium chloride, palladium chloride, tin chloride dihydrate is dissolved so that the metal weight ratio is Ru: Pd: Sn = 1: 0.4: 0.6, and the metal concentration is 10% by weight. A methanation catalyst (5) was prepared in the same manner as in Example 1 except that (5) was prepared and 26.32 g of the impregnation solution (5) was absorbed into 50 g of the methanation catalyst support (2). The active component, the content of each carrier component, the specific surface area and the pore volume were measured, and the results are shown in the table.
Activity test An activity test was conducted in the same manner as in Example 1, and the CO concentration, CO ₂ concentration and CH ₄ concentration were shown in the table.
[Example 6]
Preparation of catalyst for methanation (6) 149.47 g of titanium tetrachloride (TiO2: 28.1%) solution, 21.28 g of cerium chloride heptahydrate and 152.28 g of cobalt chloride hexahydrate into 2840 g of water It was made to melt | dissolve and mixed aqueous solution (3) was obtained.

60.50 g of sodium hydroxide was dissolved in 3200 g of water, and a mixed aqueous solution (3) was added thereto while stirring to prepare a hydrogel slurry, followed by aging at 80 ° C. for 2 hours.
The aged hydrogel was filtered, washed with sufficient warm water, dried at 120 ° C. for one day, and then baked in the air at 550 ° C. for 1 hour to obtain a composite oxide powder (3). It was. Next, the complex oxide powder (3) is filled into a tablet molding machine, pressure-molded at 50 kg / cm ² , then pulverized, and the particle size is adjusted to 20-42 mesh to support the methanation catalyst carrier (3). Was prepared.

Ruthenium chloride, perrhenic acid, and molybdenum chloride are dissolved in a weight ratio of Ru: Re: Mo = 1: 0.4: 0.6 and the metal concentration is 10% by weight to prepare an impregnation solution (6). Then, a methanation catalyst (6) was prepared in the same manner as in Example 1 except that 26.32 g of the impregnation solution (6) was absorbed into 50 g of the support (3) for methanation catalyst. The active component, the content of each carrier component, the specific surface area and the pore volume were measured, and the results are shown in the table.
Activity test An activity test was conducted in the same manner as in Example 1, and the CO concentration, CO ₂ concentration and CH ₄ concentration were shown in the table.
[Example 7]
Preparation of catalyst for methanation (7) 149.47g of titanium tetrachloride (TiO2: 28.1%) solution, 21.66g of cerium chloride heptahydrate, 101.52g of cobalt chloride hexahydrate and chlorinated -50.91 g of hexahydrate was dissolved in 2852 g of water to obtain a mixed aqueous solution (4).

60.57 g of sodium hydroxide was dissolved in 3200 g of water, and a mixed aqueous solution (4) was added thereto with stirring to prepare a hydrogel slurry, and then aged at 80 ° C. for 2 hours.
The aged hydrogel was filtered, washed with sufficient warm water, dried at 120 ° C for one day and night, and then calcined at 550 ° C for 1 hour in the air to obtain a composite oxide powder (4). It was. Next, the complex oxide powder (4) is filled into a tablet molding machine, pressure-molded at 50 kg / cm ² , then pulverized, and the particle size is adjusted to 20 to 42 mesh to support the methanation catalyst carrier (4). Was prepared.

Ruthenium chloride and tungstic acid are dissolved so that the weight ratio is Ru: W = 1: 1.2 and the metal concentration is 10% by weight to prepare an impregnation solution (7), and 29.10 g of the impregnation solution (7) A methanation catalyst (7) was prepared in the same manner as in Example 1 except that 50 g of the methanation catalyst support (4) was absorbed. The active component, the content of each carrier component, the specific surface area and the pore volume were measured, and the results are shown in the table.
Activity test An activity test was conducted in the same manner as in Example 1, and the CO concentration, CO ₂ concentration and CH ₄ concentration were shown in the table.
[Example 8]
Preparation of catalyst for methanation (8 ) Zirconyl nitrate solution (ZrO ₂ concentration: 25.0%) 124.00 g, cerium nitrate-6
Hydrate 25.10 g and cobalt nitrate hexahydrate 147.46 g were dissolved in water 2640 g to obtain a mixed aqueous solution (5).

Sodium hydroxide 61.30 g and water glass (SiO ₂ concentration: 24.0%) were added to water 320
It melt | dissolved in 0g, mixed aqueous solution (5) was added to this with stirring, the hydrogel slurry was prepared, and it age | cure | ripened at 80 degreeC for 2 hours.

The aged hydrogel was filtered, washed with sufficient warm water, dried at 120 ° C for one day and night, and then baked in the air at 550 ° C for 1 hour to obtain a composite oxide powder (5). It was. Next, the complex oxide powder (5) is filled into a tablet molding machine, pressure-molded at 50 kg / cm ² , then pulverized, and the particle size is adjusted to 20 to 42 mesh to adjust the carrier for methanation catalyst (5). Was prepared.

Ruthenium chloride, rhodium chloride, and nickel chloride are dissolved so that the weight ratio is Ru: Rh: Ni = 1: 0.2: 1, and the metal concentration is 10% by weight to prepare an impregnation solution (8). A methanation catalyst (8) was prepared in the same manner as in Example 1 except that 29.10 g of the solution (8) was absorbed into 50 g of the support (5) for methanation catalyst. The active component, the content of each carrier component, the specific surface area and the pore volume were measured, and the results are shown in the table.
Activity test An activity test was conducted in the same manner as in Example 1, and the CO concentration, CO ₂ concentration and CH ₄ concentration were shown in the table.
[Example 9]
Preparation of catalyst for methanation (8) Zirconyl nitrate solution (ZrO ₂ concentration: 25.0%) 80.00 g, cerium nitrate hexahydrate 25.10 g, cobalt nitrate hexahydrate 124.17 g and nickel nitrate -62.28 g of hexahydrate was dissolved in 2640 g of water to obtain a mixed aqueous solution (6).

Sodium hydroxide 61.30 g and water glass (SiO ₂ concentration: 24.0%) were added to water 320
It melt | dissolved in 0g, mixed aqueous solution (6) was added to this, stirring, and the hydrogel slurry was prepared, and it matured at 80 degreeC for 2 hours then.

The aged hydrogel was filtered, washed with sufficient warm water, dried at 120 ° C. for one day, and then baked in the air at 550 ° C. for 1 hour to obtain a composite oxide powder (6). It was. Next, the complex oxide powder (6) is filled into a tablet molding machine, pressure-molded at 50 kg / cm ² , then pulverized, and the particle size is adjusted to 20 to 42 mesh to adjust the carrier for methanation catalyst (6). Was prepared.

Ruthenium chloride, chloroplatinic acid, and cobalt chloride were dissolved so that the weight ratio was Ru: Pt: Co = 1: 0.2: 1 and the metal concentration was 10% by weight to prepare an impregnation solution (9). A methanation catalyst (9) was prepared in the same manner as in Example 1 except that 29.10 g of the impregnation solution (9) was absorbed into 50 g of the support (6) for methanation catalyst. The active component, the content of each carrier component, the specific surface area and the pore volume were measured, and the results are shown in the table.
Activity test An activity test was conducted in the same manner as in Example 1, and the CO concentration, CO ₂ concentration and CH ₄ concentration were shown in the table.
[Comparative Example 1]
Preparation of catalyst for methanation (R1) In Example 1, the support for methanation catalyst (1) was used without supporting a metal. Activity test An activity test was conducted in the same manner as in Example 1, and the CO concentration, CO ₂ concentration and CH ₄ concentration were shown in the table.
[Comparative Example 2]
Preparation of catalyst for methanation (R2) A catalyst for methanation (R2) was prepared in the same manner as in Example 1 except that 26.32 g of a ruthenium chloride aqueous solution having a concentration of 1.0% by weight as Ru was absorbed. The active component, the content of each carrier component, the specific surface area and the pore volume were measured, and the results are shown in the table.
Activity test An activity test was conducted in the same manner as in Example 1, and the CO concentration, CO ₂ concentration and CH ₄ concentration were shown in the table.
[Comparative Example 3]
Preparation of catalyst for methanation (R3) In Example 1, ruthenium chloride and palladium chloride were dissolved so that the metal weight ratio was Ru: Pd = 1: 0.66, and the metal concentration was 10% by weight. A catalyst for methanation (R3) was prepared in the same manner except that the step of preparing (R3) and absorbing 166.67 g of the impregnation solution (R3) and then drying was repeated four times. The active component, the content of each carrier component, the specific surface area and the pore volume were measured, and the results are shown in the table.
Activity test An activity test was conducted in the same manner as in Example 1, and the CO concentration, CO ₂ concentration and CH ₄ concentration were shown in the table.
[Comparative Example 4]
Preparation of catalyst for methanation (R4) In Example 1, ruthenium chloride and palladium chloride were dissolved so that the metal weight ratio was Ru: Pd = 1: 0.80, and the metal concentration was 1.0 wt%. A catalyst for methanation (R4) was prepared in the same manner except that the impregnation solution (R4) was prepared, and the step of absorbing and drying 22.60 g of the impregnation solution (R4) was repeated four times. The active component, the content of each carrier component, the specific surface area and the pore volume were measured, and the results are shown in the table.
Activity test An activity test was conducted in the same manner as in Example 1, and the CO concentration, CO ₂ concentration and CH ₄ concentration were shown in the table.

Claims (9)

A metal other than Ru and Ru is supported on a metal oxide support,
A catalyst for carbon monoxide methanation, wherein the supported amount of metal other than Ru and Ru is in the range of 0.5 to 15% by weight in the catalyst. The catalyst for carbon monoxide methanation according to claim 1, wherein the metal other than Ru is one or more metals selected from Group 4B, Group 6A, Group 7A and Group 8. 3. The monoxide according to claim 1, wherein the metal other than Ru is at least one selected from the group consisting of Sn, Mo, W, Re, Pt, Pd, Rh, Ni, and Co. 4. Catalyst for carbon methanation. The carbon monoxide according to any one of claims 1 to 3, wherein the ratio of Ru is in the range of 20 to 90 wt% when the total of the metals other than Ru and Ru is 100 wt%. Catalyst for methanation. The metal oxide support is one or more oxides selected from NiO, CoO (including Co ₃ O ₄ ), CeO ₂ , ZrO ₂ , Al ₂ O ₃ , TiO ₂ , SiO ₂ , or a composite oxide thereof. The catalyst for carbon monoxide methanation according to any one of claims 1 to 4, wherein The carbon monoxide methanation catalyst according to claim 1, wherein the CO adsorption amount is in the range of ³ to 20 cm ³ / g-Cat. The catalyst for carbon monoxide methanation according to claim 1, wherein the average particle diameter of the metal other than Ru and Ru determined from CO adsorption is in the range of 0.5 to 5 nm. A methanation method for carbon monoxide, comprising contacting the methanation catalyst according to any one of claims 1 to 5 with a hydrogen gas containing carbon monoxide gas. 9. The carbon monoxide methanation method according to claim 8, wherein the temperature (reaction temperature) at the time of contacting is in the range of 120 to 200 ° C.