JP4772552B2 - Carbon monoxide selective methanation catalyst, hydrogen generator and fuel cell system - Google Patents

Description

  The present invention relates to a carbon monoxide selective methanation catalyst, a hydrogen generator, and a fuel cell system.

  In a conventional fuel cell system, methane, propane gas, kerosene, naphtha or the like is used as fuel to obtain a reformed gas containing hydrogen. The reformed gas contains about 1 to 2% carbon monoxide (CO). In order to remove this CO, the fuel cell system is provided with a CO removal unit equipped with a CO selective oxidation catalyst and a CO selective methanation catalyst (hereinafter referred to as a methanation catalyst). These CO removal units are required to remove CO contained in the reformed gas to about 100 ppm or less that does not affect the power generation efficiency of the power generation stack of the fuel cell.

  Conventionally, in many fuel cell systems, a CO removing unit using a CO selective oxidation catalyst is employed. However, this method requires a pump, piping and the like related to oxygen supply. For this reason, the installation of the CO removal unit by the CO selective oxidation catalyst is unsuitable for a fuel cell system for mobile use that requires compactness of the device itself. For this reason, it has been proposed to adopt a CO removal unit using a methanation catalyst that does not require the aforementioned auxiliary devices such as pumps and pipes for mobile systems.

  As a specific example of the methanation catalyst, Patent Document 1 discloses that a metal selected from ruthenium (Ru), rhodium (Rh), nickel (Ni) and a combination thereof is a beta zeolite, a mordenite type. A catalyst supported on a support selected from zeolite and Y-type zeolite is disclosed.

  In a fuel cell system equipped with a CO removal unit using such a methanation catalyst, when a general fuel such as methane, propane gas, kerosene, or naphtha is used, both the reforming unit and the CO removal unit operate normally, and power generation It has become clear that a reformed gas from which CO has been removed up to 100 ppm or less required by the stack can be obtained constantly for a long time.

  On the other hand, when considering a portable fuel cell system, it is considered preferable to use dimethyl ether (hereinafter referred to as DME), which has low toxicity and has a distribution record as a spray pressurizing agent. However, the catalyst described in Patent Document 1 has low selectivity to CO when a fuel containing DME is used, particularly when pure DME or a mixture of DME and methanol is used as the fuel. The amount of CO in the reformed gas could not be sufficiently reduced over a long period of time.

By the way, Patent Document 2 discloses a ruthenium compound and an alkali metal compound for the purpose of providing a method for removing carbon monoxide in a hydrogen-containing gas having a high selectivity for the methanation reaction of carbon monoxide, which is the main reaction. And / or using a catalyst in which an alkaline earth metal compound is supported on a refractory inorganic oxide carrier and methanating carbon monoxide. However, Patent Document 2 does not discuss catalyst characteristics when a fuel containing DME is used.
US Patent Application Publication No. 2005/0096212 JP 2002-68707 A

  An object of the present invention is to provide a long-life carbon monoxide selective methanation catalyst, a hydrogen generator, and a fuel cell system having excellent CO selectivity and CO removal performance.

  The carbon monoxide selective methanation catalyst of the present invention comprises hydrogen, carbon monoxide and carbon dioxide produced by steam reforming a fuel containing dimethyl ether, comprising a carrier and ruthenium and potassium supported on the carrier. The carbon monoxide in the mixed gas containing is selectively methanated.

  The hydrogen production apparatus of the present invention is characterized by comprising the carbon monoxide selective methanation catalyst.

  The fuel cell system of the present invention comprises the hydrogen generator.

  According to the present invention, it is possible to provide a long-life carbon monoxide selective methanation catalyst, a hydrogen generator, and a fuel cell system having excellent CO selectivity and CO removal performance.

  As a result of intensive studies by the present inventors, when a methanation catalyst of Patent Document 1 is used when a fuel containing DME is used, problems as described in the following (1) and (2) may occur. It became clear experimentally.

(1) By-product and unreacted DME contained in the reformed gas, the performance of the catalyst is affected, and sufficient selectivity for CO cannot be obtained. For this reason, in particular, under the reaction conditions with a high CO conversion rate, hydrogenation of carbon dioxide (CO ₂ ) present in a large amount in the reformed gas also proceeds partly, and the hydrogen generated at the corner is wasted. End up.

(2) By-products and unreacted DME contained in the reformed gas cause coking on the acid sites of the catalyst carrier, leading to a rapid decrease in catalyst activity.

  In particular, in a portable fuel cell system, the reformer is downsized and the amount of reforming catalyst provided therein is limited, so that the reforming reaction does not proceed sufficiently, and the reformed gas is May increase the amount of by-products and unreacted DME. For this reason, the above problems (1) and (2) become prominent.

  As a result of diligent research to solve the above problems, the present inventors have determined that potassium (K), among alkali metals and alkaline earth metals, is particularly used for the catalyst having Ru as the main active component. It has been found that a long-life carbon monoxide selective methanation catalyst having excellent CO selectivity and CO removal performance can be realized by addition. The present invention is based on these findings.

  The effect of adding potassium is considered to be due to the reason explained below.

Potassium has an electron donating property, and when used as an additive to the metal catalyst, the electron density of the central metal (here, Ru), which is the main active component, is increased. This intensifies the reverse donation of π electrons to the adsorbed CO. As a result, since CO adsorption is relatively stronger than carbon dioxide such as CO ₂ , CO reactivity is considered to be higher than carbon dioxide reactivity. In addition, potassium is less adsorbable for CO itself in the form of metal or oxide, and has a higher affinity for carbon dioxide in the form of oxide. Thereby, it is considered that potassium existing apart from Ru acts as a carbon dioxide trap, thereby contributing to selective reaction of Ru with CO. As a result, it is considered that the addition of potassium increases the CO selectivity of the reaction substrate composed of the Ru-supported carrier.

  Furthermore, the following effects are also produced by adding potassium.

  That is, the carrier converts a very small amount of unreacted DME into an olefinic hydrocarbon at its acid point. The olefin polymerizes and caulks to poison the catalyst. However, when potassium is added to the catalyst, the acid sites of the carrier are neutralized, so that such a reaction is suppressed, and it is considered that the activity is hardly lowered. In addition, since the pore diameter is narrowed due to the presence of the additive, the diffusion of carbon dioxide, which is a larger molecule, can also be suppressed, which is considered to contribute to the selective reaction of CO. These effects are particularly remarkable when zeolite is used as a carrier.

  Patent Document 2 discloses a method of adding an alkali metal compound or an alkaline earth metal compound as a method for improving the reaction selectivity with respect to CO in the reformed gas with respect to the Ru-supported carrier. However, when a metal having a weaker alkali than potassium (lithium, sodium, alkaline earth metal, etc.) is added, neutralization of the acid point of the carrier becomes insufficient. For this reason, as described above, coking due to by-products contained in the reformed gas and unreacted DME proceeds. In particular, since zeolite has a strong acid site, this problem becomes remarkable.

  On the other hand, when a metal (rubidium, cesium, francium, etc.) whose alkali is stronger than potassium is added, the catalytic activity is lowered. The reason for this is not clear, but this problem becomes particularly prominent when a support having pores having no branch such as mordenite-type zeolite is used, and can be estimated as follows. That is, since alkali metals stronger than potassium, especially rubidium and cesium, have a large atomic radius, when they exist in a state where they do not donate electrons away from Ru, the reaction gas in the pores of the zeolite It is thought to inhibit diffusion and reduce the reaction rate.

  The addition amount of potassium is preferably in the range of 0.1 to 5% by mass as a metal with respect to 100% by mass of the total amount of ruthenium and the carrier. When there is too little quantity of potassium, the addition effect of potassium will become small. When there is too much quantity of potassium, the improvement effect of CO selectivity will become small compared with the addition amount of potassium. In addition, the additive may cover the surface of Ru to reduce the effective metal surface area, or clog the pores of the support to hinder the diffusion of the reactants, thereby reducing the activity of the catalyst. A more preferable range of the addition amount of potassium is 1 to 2% by mass as a metal with respect to 100% by mass of the total amount of ruthenium and the support. Thereby, both particularly excellent CO selectivity and CO removal performance can be achieved.

  The content of ruthenium is preferably in the range of 0.5 to 4.5 mass% as a metal with respect to 100 mass% of the total amount of ruthenium and the support. If the amount of ruthenium is too small, the effect of removing CO becomes small. If the amount of ruthenium is too large, ruthenium is a noble metal, so its price is high and the cost of the catalyst becomes high. Further, even if the ruthenium content is more than 4.5% by mass, the improvement of the CO removal effect is hardly observed. A more preferable range of the content of ruthenium is 1.0 to 3.0% by mass as a metal with respect to 100% by mass of the total amount of ruthenium and the support. Thereby, both particularly excellent CO selectivity and CO removal performance can be achieved.

  In the catalyst, potassium is preferably in a molar ratio (Ru: K) of 3: 1 to 1: 3 with respect to ruthenium. Thereby, both particularly excellent CO selectivity and CO removal performance can be achieved.

  Examples of the carrier include zeolite and titanosilicate. Among these, zeolite is preferable. As described above, the effect of the present invention becomes particularly remarkable by using zeolite as a carrier. Examples of zeolite include γ-type zeolite, mordenite-type zeolite, and Y-type zeolite. In particular, mordenite-type zeolite is preferable. Thereby, both particularly excellent CO selectivity and CO removal performance can be achieved.

Moreover, it is preferable to use a zeolite having a pore diameter (average pore diameter) of 0.63 nm or more and a pore volume of 0.3 to 1 cm ³ / g as the carrier. By using a zeolite having a pore diameter and a pore volume in this range, a particularly excellent CO removal effect can be obtained. The pore diameter of zeolite is preferably 0.7 nm or less. Thereby, the catalytic reaction with CO ₂ having a larger molecular diameter than CO can be reduced, and CO selectivity can be further improved. A more preferable range of the pore volume of the zeolite is 0.64 to 0.68 cm ³ / g.

  Note that the pore diameter is one of the intrinsic physical properties of zeolite. When the type of zeolite is determined, a certain range of pore diameters (or representative values of a certain range of pore diameters) are uniquely determined. is there. In order to actually measure the pore size, the pore size is measured by TEM observation, and the average value of a plurality of measured values, for example, the arithmetic mean, the center value, and the mode value are the pore diameter (average pore diameter). And

The pore volume can be measured by a gas adsorption measuring device. Specifically, it can be measured using N ₂ gas.

  The form of this catalyst is not particularly limited, and for example, it can be in the form of particles, channels, plates or the like.

  This catalyst can be produced, for example, as described below.

First, Ru is supported on the aforementioned carrier. The supporting method is not particularly limited, but the impregnation method is simple and preferable. Ruthenium raw materials used in the impregnation method include Ru (NO) (NO ₃ ) _x (OH) _y , Ru (NO ₂ ) ₂ (NO ₃ ) ₂ , Ru (NO ₃ ) ₃ , RuCl ₃ , Ru (CH ₃ COO ₃ ), (NH ₄ ) ₂ RuCl ₆ , [Ru (NH ₃ ) ₆ ] Cl ₃ Ru (NO) Cl ₃ , Ru ₃ (CO) _{12 and the} like. The above-mentioned carrier is impregnated with a solution containing these ruthenium raw materials, and then dried and fired. In the drying and firing step, for example, after holding at 120 ° C. for 1 hour, the temperature is raised from 120 ° C. to 500 ° C. at 5 ° C./min, and then held at 500 ° C. for 2 hours.

  Next, K is supported on the carrier supporting Ru. The supporting method is not particularly limited, but the impregnation method is simple and preferable.

  The potassium raw material used in the impregnation method is not particularly limited as long as it can obtain a liquid property that does not dissolve the support such as zeolite when it is made into a solution. Examples of the potassium raw material include inorganic salts such as hydroxides, carbonates, hydrogen carbonates, oxalates, acetates and nitrates, and organic salts such as alkoxides and acetylacetone salts. Examples of the solution used for the impregnation method include an aqueous solution adjusted to pH by adjusting the concentration of the inorganic salt described above, an aqueous solution adjusted to pH by neutralizing a solution containing the inorganic salt described above, or the organic salt described above. A solution dissolved in an organic solvent such as acetone, hexane, tetrahydrofuran (THF), or the like can be used. The solution containing these potassium raw materials is impregnated with a carrier carrying Ru, and the solution is evaporated to dryness, followed by drying and baking. At this time, by evaporating the solution to dryness, almost the entire amount of K in the solution can be supported on the carrier, so that a catalyst having a desired amount of K can be obtained. In the drying and firing step, for example, after holding at 120 ° C. for 1 hour, the temperature is raised from 120 ° C. to 500 ° C. at 10 ° C./min, and then held at 500 ° C. for 2 hours.

  The manufacturing method of the catalyst which concerns on embodiment of this invention is not limited to what was mentioned above. For example, Ru and K may be supported on the carrier at the same time. Also in this case, the supporting method is not particularly limited, but the impregnation method is simple and preferable.

  Next, the hydrogen generator will be described.

  A hydrogen generator according to an embodiment of the present invention includes a fuel supply unit that supplies a fuel containing DME, a reforming unit that reforms the fuel to generate a reformed gas containing hydrogen, and the reforming unit. A CO removing unit that removes at least a part of CO contained in the gas, and the CO removing unit is provided with a catalyst containing the above-mentioned carrier and ruthenium and potassium supported on the carrier. It is characterized by.

  The hydrogen generator and the fuel cell system will be described in more detail with reference to FIG.

  FIG. 1 is a block diagram schematically showing a fuel cell system according to an embodiment of the present invention.

  The fuel cell system 1 of FIG. 1 includes a fuel cell, a hydrogen generator, a vaporizer 3, and a combustion air pump 7. A fuel tank 2 can be detachably connected to the fuel cell system 1. The hydrogen production device includes a reforming unit 4, a CO shift reaction unit 5, a CO selective methanation reaction unit 6, and a catalytic combustion unit 8. A combination of the CO shift reaction unit 5 and the CO selective methanation reaction unit 6 can be referred to as a CO removal unit. The fuel cell includes a fuel electrode 10, an oxidant electrode 12, and a hydrogen permeable membrane 11 disposed between the fuel electrode 10 and the oxidant electrode 12. This fuel cell system is preferably portable.

  The fuel tank 2 contains a mixture of fuel and water. Examples of the fuel include pure DME and a mixture of DME and methanol. The fuel preferably contains DME as a main component. Typically, the amount of DME in the fuel is in the range of 50-100% by volume. Thereby, the effect of this invention becomes more remarkable. A more preferred range of the amount of DME in the fuel is 90-100% by volume. In particular, when DME is used as the fuel, the mixing ratio of DME and water is preferably in the range of 1: 3 to 1: 4.5 in terms of molar ratio (DME: water). In this case, the layer separation of water and DME in the fuel tank 2 is suppressed by adding methanol to the mixture of DME and water in an amount of 10% by volume or less with respect to 100% by volume of the mixture of water and methanol. And good fuel supply can be performed.

  The fuel tank 2 communicates with the vaporizer 3 by piping or the like. The pipe is provided with an on-off valve 2a. The vaporizer 3 is supplied with a mixture of fuel and water from the fuel tank 2 using the pressure of DME. Here, the mixture of fuel and water is vaporized to obtain vaporized gas.

  The fuel and water may be supplied from different containers instead of being mixed in the fuel tank 2 as described above.

The vaporizer 3 communicates with the hydrogen generator through piping or the like. The vaporized gas is supplied to the reforming unit 4 of the hydrogen generator. The reforming unit 4 is provided with a reforming catalyst. Here, the vaporized gas is steam reformed to obtain a reformed gas. In the case of a portable fuel cell system, the contact amount of the vaporized gas per unit weight of the reforming catalyst in the reforming unit 4 can be set in the range of 30 to 150 mL / min, for example. This reformed gas is mainly composed of hydrogen (H ₂ ), and typically contains 1 to 2% by volume of CO, by-products (eg, ethylene, propylene, etc.), and unreacted DME. It is a mixed gas.

  This reformed gas is supplied to the CO shift reaction unit 5. The CO shift reaction unit 5 is provided with a shift catalyst that promotes the shift reaction of CO present in the reformed gas. Typically, here, the amount of CO in the reformed gas is reduced to 2000-10000 ppm by volume.

  Thereafter, the reformed gas is supplied to the CO selective methanation reaction unit 6. The CO selective methanation reaction unit 6 includes the carbon monoxide selective methanation catalyst according to the above-described embodiment of the present invention. Typically, here, the amount of CO in the reformed gas is reduced to 100 ppm or less by volume. Here, the reformed gas with reduced CO is referred to as purified gas. The methanation reaction in the CO selective methanation reaction section 6 is preferably performed in a temperature range of 225 ° C. or more and less than 250 ° C. By setting this temperature range, the CO removal efficiency can be made particularly good, and the effect of improving the CO selectivity by the addition of potassium is particularly remarkable.

  The purified gas reduced in CO in the CO selective methanation reaction unit 6 is supplied to the fuel electrode 10 of the fuel cell. On the other hand, oxygen-containing air is supplied to the oxidant electrode 11 of the fuel cell. Thereby, power generation is performed in the fuel cell.

  The exhaust gas from the fuel cell is supplied to the catalytic combustion section 8 of the hydrogen generator. The catalyst combustion unit 8 is provided with a combustion catalyst. The exhaust gas supplied to the catalyst combustion section is mixed with the air supplied from the combustion air pump 7, burned, and discharged out of the system.

  Typically, the hydrogen generator and the vaporizer 3 are housed in a single insulated container 9. As a result, the heat generated in the catalytic combustion unit 8 can be efficiently transferred to the vaporizer 3, the reforming unit 4, the CO shift reaction unit 5 and the CO selective methanation reaction unit 6 of the hydrogen generator. The reaction efficiency in the system can be improved. Further, since an auxiliary device such as a heater can be omitted or the necessary capacity of the auxiliary device can be reduced, the fuel cell system can be reduced in size. The vaporizer 3 and the hydrogen generator can be collectively referred to as a reformer.

  As described above in detail, according to the present invention, it is possible to provide a long-life carbon monoxide selective methanation catalyst, a hydrogen generator, and a fuel cell system having excellent CO selectivity and CO removal performance. In addition, by using the catalyst according to the embodiment of the present invention for CO selective methanation, it is possible to suppress waste of hydrogen due to the reaction of excess carbon dioxide gas, so that the efficiency of hydrogen generation from fuel is high. A hydrogen generator can be realized. Furthermore, in a portable fuel cell system, even when reformed gas containing a large amount of by-products and unreacted DME is generated, CO can be sufficiently reduced over a long period of time and supplied to the fuel cell. Therefore, deterioration of the power generation performance of the power generation stack can be suppressed.

[Example]
Hereinafter, the present invention will be described with reference to examples.

<Manufacture of catalyst>
(Example)
As a carrier, H-MOR-20 (mordenite type zeolite) having a pore volume of 0.5 cm ³ / g and an average pore diameter of 0.65 nm was prepared. On the other hand, an aqueous solution prepared by adding ion-exchanged water to an aqueous solution of Ru (NO) (NO ₃ ) _x (OH) _y having a Ru content of 10% by mass as the impregnation solution was adjusted to pH 0.8. The impregnating solution thus obtained was impregnated with the above-mentioned carrier, dried at 110 ° C. for 15 hours, heated to 450 ° C. at 10 ° C./min, and baked at 450 ° C. for 2 hours as it was. A pre-catalyst having an Ru loading of 2% by mass with respect to 100% by mass was obtained.

  20 g of the obtained preliminary catalyst was impregnated in an aqueous solution in which 0.72 g of potassium carbonate was dissolved. This solution was evaporated to dryness while stirring with a rotary evaporator on a 60 ° C. water bath, dried at 120 ° C. for 16 hours, heated to 500 ° C. at 10 ° C./min, and baked at 500 ° C. for 2 hours. Thus, a CO selective methanation catalyst having a K loading of 2% by mass with respect to 100% by mass of the total amount of Ru and the support was obtained.

(Comparative Example 1)
The pre-catalyst of the example was used as the catalyst of Comparative Example 1.

(Comparative Example 2)
A catalyst was obtained in the same manner as in Example except that 0.55 g of sodium carbonate was used instead of 0.72 g of potassium carbonate.

(Comparative Example 3)
A catalyst was obtained in the same manner as in Example except that 1.7 g of cesium carbonate was used instead of 0.72 g of potassium carbonate.

<Evaluation of catalyst characteristics 1>
1 g of each of the catalysts of Examples and Comparative Examples 1 to 3 was charged into a fixed bed flow tubular reactor. In this reactor, a mixed gas of 25 mL of water vapor and 150 mL of model gas was circulated per standard condition. The composition of the model gas is 1% by volume of carbon monoxide (CO), 23% by volume of carbon dioxide (CO ₂ ), 5% by volume of methane (CH ₄ ), 47% by volume of hydrogen (H ₂ ), and the balance is nitrogen (N ₂ ). The total flow rate Fr and CO concentration Cc of all the substances per unit time of the outlet gas of this reactor were measured. From this result, the CO flow rate Cf per unit time represented by the following formula (1) was calculated.

Cf = Fr × Cc (1)
Here, the CO flow rate Cf of the outlet gas is indicated by Cf ₁ . Similarly, the CO flow rate Cf per unit time was calculated for the model gas (inlet gas). Here, the CO flow Cf inlet gas Cf _2. The ratio of the CO flow rate Cf ₁ of the outlet gas to the CO flow rate Cf ₂ of the inlet gas was defined as the CO conversion rate (%). Similarly, CO ₂ conversion (%) was measured. This evaluation is performed at each reaction temperature from 100 ° C. to 300 ° C., and the results are shown in FIG. In FIG. 2, the vertical axis indicates the CO conversion rate (%) and the CO ₂ conversion rate (%), and the horizontal axis indicates the reaction temperature (° C.).

  Further, FIG. 3 shows the result of the CO concentration of the outlet gas. In FIG. 3, the vertical axis indicates the CO concentration (volume%, ppm) of the outlet gas, and the horizontal axis indicates the reaction temperature (° C.). Here, the CO concentration at 225 ° C. was 17 ppm in the Example, 9 ppm in Comparative Example 1, and 12 ppm in Comparative Example 2. In Comparative Example 3, the CO concentration at 250 ° C. was 103 ppm.

Further, except that the reaction temperature was fixed at 225 ° C. and the inlet gas was switched from the above mixed gas to the reformed gas obtained using pure DME as fuel, the CO conversion rate was the same as described above, The CO ₂ conversion rate and the CO concentration of the outlet gas were measured.

As is apparent from FIGS. 2 and 3, the catalyst of the example including the carrier and ruthenium and potassium supported on the carrier has a high CO conversion rate and a low CO ₂ conversion in the temperature range from 225 ° C. to 300 ° C. The rate was obtained and CO selective methanation advanced. Further, the CO concentration of the outlet gas was 100 ppm or less in the temperature range from 225 ° C. to 250 ° C., and excellent CO removal performance was also obtained. Further, even in such a temperature range where the CO conversion rate is high, a low CO ₂ conversion rate of 2% or less was obtained, and very excellent CO selectivity was exhibited. Further, even after 1 hour from the start of the flow of the reformed gas, neither CO conversion rate nor CO ₂ conversion rate is observed, which is caused by a small amount of by-products in the reformed gas and unreacted DME. There was no poisoning. That is, it was confirmed that the catalysts of the examples had both good CO selectivity and anti-poisoning properties against unreacted DME and by-products.

In contrast, the catalyst of Comparative Example 1 that supports ruthenium but does not support potassium already has a CO ₂ conversion rate exceeding 5% at 225 ° C., and the CO selectivity of the catalyst is lower than that of the Example. It was. Further, one hour after the start of the flow of the reformed gas, the CO conversion rate decreased to 10% or less, and the life was shorter than in the examples. This is probably because the catalyst was poisoned by a small amount of by-products in the reformed gas and unreacted DME.

In the catalyst of Comparative Example 2 supporting sodium instead of potassium, in the temperature range from 225 ° C. to 250 ° C., the same CO, CO ₂ conversion rate and CO concentration in the outlet gas as in the examples were obtained. One hour after starting the flow of the quality gas, the CO conversion decreased to 10% or less.

In the catalyst of Comparative Example 3 supporting cesium instead of potassium, the CO ₂ conversion rate was low, but the reaction temperature required to obtain the CO conversion rate equivalent to that of the Example was high, so the outlet was restricted due to equilibrium restrictions. The CO concentration of the gas could not be reduced to 100 ppm or less, and the CO removal performance was inferior compared to the examples. In addition, 1 hour after starting the flow of the reformed gas, neither CO nor CO ₂ conversion was changed.

<Evaluation of catalyst characteristics 2>
A portable fuel cell system having the same structure as the system of FIG. 1 was prepared.

  The reforming unit 4 is a catalyst in which a commercially available Pt-based reforming catalyst and a commercially available shift catalyst are mixed at a weight ratio of 1: 1, the CO shift reaction unit 5 is a commercially available shift catalyst, and the CO selective methanation reaction unit 6 is Were filled with 1 g each of the catalyst of the example. The temperature of the vaporizer 3 was controlled to 120 ° C., the reforming unit 4 to 350 ° C., the CO shift reaction unit 5 to 275 ° C., and the CO selective methanation reaction unit 6 to 250 ° C. From the fuel tank 2, a mixture in which pure DME as fuel and water were mixed at a molar ratio (DME: water) of 1: 4 was supplied. The amount of gas contact per unit weight of the reforming catalyst in the reforming unit 4 was 65 mL / min.

  As a result, it was confirmed that a purified gas containing an almost stoichiometrically predicted amount of hydrogen was obtained, and the concentration of CO remaining in the purified gas was 100 ppm or less.

  Further, the purified gas containing hydrogen thus obtained was supplied to the fuel electrode 10, and air containing oxygen was supplied to the oxidant electrode 11, thereby generating power in the fuel cell. The exhaust gas from the fuel cell was burned in the catalytic combustion section 8 filled with a commercially available Pd catalyst, and then discharged out of the system.

As a result, there was no decrease in the generated power over time that occurs when the fuel electrode 10 is poisoned by CO. Further, the final exhaust gas from the catalytic combustion section 8 does not contain CO, H ₂ , and CH ₄ and is safe.

In addition, except that the carrier has a pore volume of 0.5 to 0.8 cm ³ / g, H-MOR-20 of the same type as in the examples is used, and a catalyst is produced in the same manner as in the examples. When the characteristics were evaluated, the same results as in the example were obtained.

  Further, when 10% by volume of methanol was added to 100% by volume of the mixture of water and methanol to the mixture of fuel and water used above, the layer separation of water and DME in the fuel tank was suppressed, which was good. The fuel could be supplied.

  As described in detail above, the catalysts of the examples can selectively react with carbon monoxide in the reformed gas obtained from DME or a mixture of DME and methanol, and also suppress catalyst deterioration. I was able to.

<Evaluation of catalyst characteristics 3>
Further, the catalyst of the example was pulverized to 100 mesh under, and mixed with silica similarly pulverized to 100 mesh under so that the weight ratio (catalyst of the example: silica) was 7: 3. To 300 g of this mixed powder, 700 mL of hexane was added to prepare a slurry.

An aluminum channel 13 having a shape as shown in FIG. 4 was prepared. The channel 13 has a structure in which a plurality of channel forming plates 15 are suspended from a flat plate 14. Here, the flat plate 14 and the channel forming plate 15 are integrated. The thickness of the channel forming plate 15 and the interval between the channel forming plates 15 are both 0.5 mm wide. The number of grooves formed between the channel forming plate 15 and the adjacent channel forming plate 15 is 45. The height of the channel forming plate 15 (length in the orthogonal direction of the flat plate 14) is 6.5 mm, and the length of the channel forming plate 15 (length in the parallel direction of the flat plate 14) is 4 cm. The total geometric surface area of the channel portion (the side of the channel 13 having the channel forming plate 15) is 243 cm ² . An operation in which the surface of the channel 13 was roughened was dipped in the slurry, dried at room temperature for 12 hours, and then fired at 500 ° C. for 2 hours. Thus, a catalyst layer 16 having a thickness of about 40 μm was formed on the surfaces of the Al bases 14 and 15 as shown in FIG. As a result, 2.9 g of the catalyst layer 16 was formed on the channel 13, and the catalyst powder of the example was about 2 g in the catalyst layer 16.

  The channel 13 packed in a stainless steel casing was used in the CO selective methanation reaction section 6 of the fuel cell system having the same structure as that shown in FIG. The reforming unit 4 was filled with 2 g of a commercially available Pt-based reforming catalyst and a commercially available shift catalyst mixed at a weight ratio of 1: 1, and the CO shift reaction unit 5 was filled with 2 g of a commercially available shift catalyst. The temperature was controlled so that the reforming unit 4 was 350 ° C., the CO shift reaction unit 5 was 275 ° C., and the CO selective methanation reaction unit 6 was 250 ° C. From the fuel tank 2, a mixture in which pure DME and water were mixed at a molar ratio (pure DME: water) at a ratio of 1: 4 was supplied. The amount of gas contact per weight of the reforming catalyst in the reforming unit 4 was 65 mL per minute in terms of standard conditions.

  As a result, the CO concentration at the outlet of the CO selective methanation catalyst 6 could be reduced to 100 ppm or less.

  Note that the present invention is not limited to the above-described embodiment as it is, and can be embodied by modifying the constituent elements without departing from the scope of the invention in the implementation stage. Further, various inventions can be formed by appropriately combining a plurality of constituent elements disclosed in the embodiment. For example, some components may be deleted from all the components shown in the embodiment. Furthermore, you may combine suitably the component covering different embodiment.

1 is a block diagram schematically showing a fuel cell system according to an embodiment of the present invention. Characteristic diagram showing the relationship between the CO conversion and CO ₂ conversion and reaction temperature. The characteristic diagram which shows the relationship between CO density | concentration of outlet gas, and reaction temperature. The perspective view which shows the channel used in the Example typically. The cross-sectional schematic diagram which shows the channel which has a catalyst layer.

Explanation of symbols

  DESCRIPTION OF SYMBOLS 1 ... Fuel cell system, 2 ... Fuel tank, 2a ... On-off valve, 3 ... Vaporizer, 4 ... Reforming part, 5 ... CO shift reaction part, 6 ... CO selective methanation reaction part, 7 ... Combustion air pump, DESCRIPTION OF SYMBOLS 8 ... Catalytic combustion part, 9 ... Thermal insulation container, 10 ... Fuel electrode, 11 ... Hydrogen permeable film, 12 ... Oxidant electrode, 13 ... Channel, 14 ... Flat plate, 15 ... Channel formation board, 16 ... Catalyst layer.

Claims (4)

A carrier, and ruthenium and potassium supported on the carrier,
The ruthenium is in a ratio of 0.5 to 4.5% by mass as a metal with respect to 100% by mass of the total amount of the ruthenium and the support,
The carrier includes a zeolite having a pore diameter of 0.63 nm or more and a pore volume of 0.3 to 1 cm ³ / g,
Carbon monoxide selective methane characterized by selectively methanating carbon monoxide in a mixed gas containing hydrogen, carbon monoxide and carbon dioxide produced by steam reforming a fuel containing dimethyl ether Catalyst. The fuel dimethyl ether containing 50 to 100 vol%, the carbon monoxide selective methanation catalyst according to claim 1, wherein the remainder is methanol. A hydrogen generator comprising the carbon monoxide selective methanation catalyst according to claim 1 or 2 . A fuel cell system comprising the hydrogen generator according to claim 3 .

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