JP2018143941A - Catalyst for hydrogen production and hydrogen production method - Google Patents
Catalyst for hydrogen production and hydrogen production method Download PDFInfo
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- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 46
- 239000003054 catalyst Substances 0.000 title claims abstract description 43
- 239000001257 hydrogen Substances 0.000 title claims abstract description 43
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 43
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 20
- 239000007789 gas Substances 0.000 claims abstract description 40
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 24
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 24
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 24
- 229910052723 transition metal Inorganic materials 0.000 claims abstract description 13
- 150000003624 transition metals Chemical class 0.000 claims abstract description 13
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 44
- 150000001875 compounds Chemical class 0.000 claims description 20
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 14
- 239000010419 fine particle Substances 0.000 claims description 9
- 229910052759 nickel Inorganic materials 0.000 claims description 4
- 150000002431 hydrogen Chemical class 0.000 claims description 3
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 18
- 238000006243 chemical reaction Methods 0.000 description 17
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 10
- 238000010438 heat treatment Methods 0.000 description 8
- 239000000292 calcium oxide Substances 0.000 description 7
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 7
- 230000003197 catalytic effect Effects 0.000 description 7
- 238000000034 method Methods 0.000 description 7
- 239000002994 raw material Substances 0.000 description 7
- 239000000843 powder Substances 0.000 description 6
- 239000001569 carbon dioxide Substances 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 5
- 239000006185 dispersion Substances 0.000 description 5
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 229940043430 calcium compound Drugs 0.000 description 4
- 150000001674 calcium compounds Chemical class 0.000 description 4
- 239000013078 crystal Substances 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000012495 reaction gas Substances 0.000 description 4
- 239000002904 solvent Substances 0.000 description 4
- 238000000629 steam reforming Methods 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 229910052782 aluminium Inorganic materials 0.000 description 3
- -1 aluminum compound Chemical class 0.000 description 3
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 3
- 238000006555 catalytic reaction Methods 0.000 description 3
- 229910001873 dinitrogen Inorganic materials 0.000 description 3
- 238000011156 evaluation Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 238000004817 gas chromatography Methods 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 239000002105 nanoparticle Substances 0.000 description 3
- 239000003960 organic solvent Substances 0.000 description 3
- 239000010453 quartz Substances 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- XFWJKVMFIVXPKK-UHFFFAOYSA-N calcium;oxido(oxo)alumane Chemical compound [Ca+2].[O-][Al]=O.[O-][Al]=O XFWJKVMFIVXPKK-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 239000011812 mixed powder Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 229910052763 palladium Inorganic materials 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 238000000634 powder X-ray diffraction Methods 0.000 description 2
- 238000010298 pulverizing process Methods 0.000 description 2
- 229910052703 rhodium Inorganic materials 0.000 description 2
- 229910052707 ruthenium Inorganic materials 0.000 description 2
- 229930195734 saturated hydrocarbon Natural products 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 229910002056 binary alloy Inorganic materials 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000009837 dry grinding Methods 0.000 description 1
- 238000002296 dynamic light scattering Methods 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 239000002638 heterogeneous catalyst Substances 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000010416 ion conductor Substances 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 238000003801 milling Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 238000001238 wet grinding Methods 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
Abstract
Description
本発明は、炭化水素ガスから水素を製造するための触媒及び水素の製造方法に関する。 The present invention relates to a catalyst for producing hydrogen from hydrocarbon gas and a method for producing hydrogen.
水素は従来、各種水素添加反応の還元剤、あるいはアンモニアやメタノールの製造用原料として大量に使用されている。近年、クリーンエネルギーとして着目され、燃料電池の燃料としても注目されている。燃料電池車の開発も進められており、実用化されれば水素のエネルギーとしての需要は大きく、今後も水素の使用量は増大することが想定される。 Conventionally, hydrogen is used in large quantities as a reducing agent for various hydrogenation reactions or as a raw material for producing ammonia and methanol. In recent years, it has attracted attention as clean energy and has attracted attention as a fuel for fuel cells. Fuel cell vehicles are also being developed, and if they are put to practical use, the demand for hydrogen energy will be large, and it is expected that the amount of hydrogen used will continue to increase.
水素の製造方法としては様々な方法があるが、メタン等の炭化水素と水蒸気を反応させて、水素を製造する水蒸気改質法が一般的に用いられている。この水蒸気改質法に用いられる触媒としては、Ｎｉを担持したアルミナ触媒が工業的に利用されている。 Although there are various methods for producing hydrogen, a steam reforming method is generally used in which hydrogen is produced by reacting a hydrocarbon such as methane with steam. As a catalyst used in this steam reforming method, an alumina catalyst supporting Ni is industrially used.
一方、特異な結晶構造を有する１２ＣａＯ・７Ａｌ2Ｏ3化合物は、その結晶構造内に酸素イオンラジカルを高濃度に含むことが知られており、酸化触媒、イオン伝導体などの用途に有用であることが提案されている（特許文献１、２、３）。さらに、アンモニアを合成するための安定で高性能な触媒として利用できることが提案されている（特許文献４）。 On the other hand, a 12CaO · 7Al 2 O 3 compound having a unique crystal structure is known to contain oxygen ion radicals in a high concentration in the crystal structure, and is useful for applications such as oxidation catalysts and ion conductors. (Patent Documents 1, 2, and 3). Furthermore, it has been proposed that it can be used as a stable and high-performance catalyst for synthesizing ammonia (Patent Document 4).
しかしながら、前記の水蒸気改質法によれば、メタンガスから水素が得られるとともに二酸化炭素が生成するという問題がある。従って、二酸化炭素が生成しない水素の製造方法が望まれる。
また、１２ＣａＯ・７Ａｌ2Ｏ3化合物が水素製造用触媒の担体として利用できることは報告されていない。
本発明の課題は、炭化水素ガスを直接分解して水素を製造できる触媒及び水素の製造方法を提供することにある。
However, the steam reforming method has a problem that hydrogen is obtained from methane gas and carbon dioxide is generated. Therefore, a method for producing hydrogen that does not produce carbon dioxide is desired.
Further, it has not been reported that 12CaO · 7Al 2 O 3 compound can be used as a carrier for a catalyst for hydrogen production.
An object of the present invention is to provide a catalyst capable of producing hydrogen by directly decomposing hydrocarbon gas and a method for producing hydrogen.
そこで本発明者は、種々の担体に遷移金属を担持した触媒を用いて炭化水素ガスから水素を生産する方法を検討してきたところ、１２ＣａＯ・７Ａｌ2Ｏ3化合物微粒子含有担体に遷移金属を担持した触媒に炭化水素ガスを接触させれば、炭化水素ガスが直接分解して水素ガスが効率良く製造できることを見出し、本発明を完成した。 Therefore, the present inventor has studied a method for producing hydrogen from hydrocarbon gas using a catalyst in which a transition metal is supported on various supports. As a result, the transition metal is supported on a support containing 12CaO · 7Al 2 O 3 compound fine particles. It has been found that if hydrocarbon gas is brought into contact with the catalyst, the hydrocarbon gas is directly decomposed to produce hydrogen gas efficiently, and the present invention has been completed.
すなわち、本発明は、次の〔１〕〜〔４〕を提供するものである。 That is, the present invention provides the following [1] to [4].
〔１〕炭化水素ガスを直接分解して水素を製造するための触媒であって、１２ＣａＯ・７Ａｌ2Ｏ3化合物微粒子含有担体に遷移金属が担持した水素製造用触媒。
〔２〕前記遷移金属がニッケルである〔１〕記載の水素製造用触媒。
〔３〕〔１〕又は〔２〕に記載の触媒に、炭化水素ガスを接触させることを特徴とする水素の製造方法。
〔４〕前記炭化水素ガスがメタンガスである〔１〕記載の水素の製造方法。
[1] A catalyst for producing hydrogen by directly decomposing hydrocarbon gas, wherein a transition metal is supported on a carrier containing 12CaO · 7Al 2 O 3 fine particles.
[2] The hydrogen production catalyst according to [1], wherein the transition metal is nickel.
[3] A method for producing hydrogen, comprising bringing a hydrocarbon gas into contact with the catalyst according to [1] or [2].
[4] The method for producing hydrogen according to [1], wherein the hydrocarbon gas is methane gas.
本発明の触媒を用いれば、炭化水素ガスを直接分解して水素ガスが効率良く製造できる。本発明による水素の製造方法は、水蒸気改質ではないので二酸化炭素が生成しない。 If the catalyst of this invention is used, hydrocarbon gas can be decomposed | disassembled directly and hydrogen gas can be manufactured efficiently. Since the method for producing hydrogen according to the present invention is not steam reforming, carbon dioxide is not generated.
本発明の水素製造用触媒は、１２ＣａＯ・７Ａｌ2Ｏ3化合物微粒子含有担体に遷移金属が担持した触媒である。 The catalyst for producing hydrogen of the present invention is a catalyst in which a transition metal is supported on a support containing fine particles of 12CaO · 7Al 2 O 3 compound.
１２ＣａＯ・７Ａｌ2Ｏ3化合物微粒子含有担体は、カルシウム化合物及びアルミニウム化合物の混合物を、加熱することにより製造することができる。 The 12CaO · 7Al 2 O 3 compound fine particle-containing carrier can be produced by heating a mixture of a calcium compound and an aluminum compound.
原料として用いるカルシウム化合物としては、酸化カルシウム、炭酸カルシウム等が挙げられる。また、アルミニウム化合物としては、酸化アルミニウムが挙げられるが、酸化アルミニウムの結晶構造はα型、γ型のいずれでもよい。また、これらのカルシウム化合物及びアルミニウム化合物は、粉末、固体焼結物、固体単結晶など形状を問わない。原料の混合比率は、酸化物換算のモル比〔（ＣａＯ）／（Ａｌ2Ｏ3）〕で、１．５以上１．９以下が好ましく、１．６以上１．８以下がより好ましい。 Examples of calcium compounds used as raw materials include calcium oxide and calcium carbonate. Examples of the aluminum compound include aluminum oxide. The crystal structure of aluminum oxide may be either α-type or γ-type. Moreover, these calcium compounds and aluminum compounds do not ask | require shapes, such as a powder, a solid sintered compact, and a solid single crystal. The mixing ratio of the raw materials is a molar ratio in terms of oxide [(CaO) / (Al 2 O 3 )], preferably 1.5 or more and 1.9 or less, and more preferably 1.6 or more and 1.8 or less.
カルシウム化合物及びアルミニウム化合物の混合物の加熱は、真空中、不活性ガス雰囲気中、水素雰囲気中、酸素雰囲気中等で行なうことができる。但し、水蒸気を含む雰囲気は好ましくない。酸素濃度２１％程度の乾燥空気中でも行うことができる。なお、酸素雰囲気中で加熱製造する場合は、原料の混合比率をモル比〔（ＣａＯ）／（Ａｌ2Ｏ3）〕で１．５以上１．７以下の範囲にすることが、高純度の１２ＣａＯ・７Ａｌ2Ｏ3化合物を得る観点から好ましい。
加熱条件は、最高温度を原料化合物が反応してカルシウムアルミネートが生成する温度以上とすることが好ましく、１２５０℃以上２５００℃以下とするのがより好ましく、１３００℃以上１８００℃以下とするのがさらに好ましい。原料化合物を溶融させて１２ＣａＯ・７Ａｌ2Ｏ3化合物を製造する場合は、１４００℃以上とすることが好ましい。加熱は、最高温度で１時間以上維持するのが１２ＣａＯ・７Ａｌ2Ｏ3化合物を高純度で得る点で好ましく、２時間以上２４時間以下維持するのがより好ましい。
The mixture of calcium compound and aluminum compound can be heated in a vacuum, in an inert gas atmosphere, in a hydrogen atmosphere, in an oxygen atmosphere, or the like. However, an atmosphere containing water vapor is not preferable. It can be performed even in dry air having an oxygen concentration of about 21%. In addition, when manufacturing by heating in an oxygen atmosphere, the mixing ratio of the raw materials is set to a range of 1.5 to 1.7 in terms of molar ratio [(CaO) / (Al 2 O 3 )]. From the viewpoint of obtaining a 12CaO · 7Al 2 O 3 compound, it is preferable.
As for the heating conditions, the maximum temperature is preferably not less than the temperature at which the raw material compound reacts to form calcium aluminate, more preferably not less than 1250 ° C and not more than 2500 ° C, and more preferably not less than 1300 ° C and not more than 1800 ° C. Further preferred. When the 12CaO · 7Al 2 O 3 compound is produced by melting the raw material compound, the temperature is preferably 1400 ° C. or higher. The heating is preferably maintained at the maximum temperature for 1 hour or more from the viewpoint of obtaining the 12CaO · 7Al 2 O 3 compound with high purity, and more preferably 2 hours or more and 24 hours or less.
前記温度に加熱することにより、原料化合物が反応して１２ＣａＯ・７Ａｌ2Ｏ3化合物が生成するので、必要に応じて粉砕し１２ＣａＯ・７Ａｌ2Ｏ3化合物微粒子を得る。溶融した場合は冷却して固化物とし、得られた固化物を粉砕すれば１２ＣａＯ・７Ａｌ2Ｏ3化合物微粒子が得られる。
冷却条件は、特に制限されないが、溶融した場合は溶融後の温度が１２００℃以下となるまでは降温速度５０℃／時間以上６００℃／時間以下が好ましい。
生成した１２ＣａＯ・７Ａｌ2Ｏ3化合物は、結晶質およびガラス質のいずれでもよい。１２ＣａＯ・７Ａｌ2Ｏ3化合物の純度は５０％以上でその他のカルシウムアルミネート化合物を含んでもよいが、触媒担体として効果的に性能を発揮するためには、１２ＣａＯ・７Ａｌ2Ｏ3化合物の純度が８０％以上であることが好ましく、９０％以上がより好ましい。
１２ＣａＯ・７Ａｌ2Ｏ3化合物の固化物の粉砕工程は、乾式粉砕ならびに１２ＣａＯ・７Ａｌ2Ｏ3化合物の水和を防ぐため有機溶媒を用いた湿式粉砕のいずれかの微粉砕方法を用いることができる。得られる微粒子は、ＢＥＴ比表面積が２ｍ2／ｇ以上の微粉末であることが触媒活性の点で好ましい。
By heating to the above temperature, the raw material compound reacts to produce a 12CaO · 7Al 2 O 3 compound, so that it is pulverized as necessary to obtain 12CaO · 7Al 2 O 3 compound fine particles. When melted, it is cooled to obtain a solidified product, and the obtained solidified product is pulverized to obtain 12CaO · 7Al 2 O 3 compound fine particles.
The cooling conditions are not particularly limited, but when melted, the temperature lowering rate is preferably 50 ° C./hour or more and 600 ° C./hour or less until the temperature after melting becomes 1200 ° C. or less.
The produced 12CaO · 7Al 2 O 3 compound may be either crystalline or glassy. The purity of the 12CaO · 7Al 2 O 3 compound is 50% or more and may contain other calcium aluminate compounds. However, in order to effectively perform as a catalyst carrier, the purity of the 12CaO · 7Al 2 O 3 compound is It is preferably 80% or more, more preferably 90% or more.
Grinding step of solid of 12CaO · 7Al 2 O 3 compound can be any of milling methods wet milling using an organic solvent to prevent hydration of dry grinding and 12CaO · 7Al 2 O 3 compound . The fine particles obtained are preferably fine powders having a BET specific surface area of 2 m 2 / g or more from the viewpoint of catalytic activity.
触媒種としては、遷移金属であればよいが、Ｎｉ、Ｐｔ、Ｐｄ、Ｒｕ、Ｒｈ、Ｃｏ等の８族、９族及び１０族から選ばれる元素の１種又は２種以上が挙げられる。例えば、二元系、三元系等の不均一触媒でもよい。水素製造活性の点から、Ｎｉ、Ｐｔ、Ｐｄ、Ｒｕ、Ｒｈがより好ましく、Ｎｉが特に好ましい。
遷移金属の粒子径は、水素製造活性の点、担体表面への高い分散度を確保する点から、小さいことが好ましく、メジアン径として０．００１μｍ以上１μｍ以下が好ましく、０．００１μｍ以上０．１μｍ以下がより好ましく、０．００１μｍ以上０．０１μｍ以下がさらに好ましい。ここで、メジアン径は、動的光散乱法による累積頻度が５０％となる粒径値である。
The catalyst species may be any transition metal, and examples thereof include one or more elements selected from Group 8, Group 9, and Group 10, such as Ni, Pt, Pd, Ru, Rh, and Co. For example, a heterogeneous catalyst such as a binary system or a ternary system may be used. From the viewpoint of hydrogen production activity, Ni, Pt, Pd, Ru, and Rh are more preferable, and Ni is particularly preferable.
The particle diameter of the transition metal is preferably small from the viewpoint of hydrogen production activity and the high degree of dispersion on the support surface. The median diameter is preferably 0.001 μm to 1 μm, preferably 0.001 μm to 0.1 μm. The following is more preferable, and 0.001 μm or more and 0.01 μm or less is more preferable. Here, the median diameter is a particle diameter value at which the cumulative frequency by the dynamic light scattering method is 50%.
１２ＣａＯ・７Ａｌ2Ｏ3微粒子担体への遷移金属の担持は、例えば有機溶媒を用いた含浸法で行うことができる。具体的には、遷移金属のヘキサン等の有機溶媒分散液中に担体を投入後、撹拌し、溶媒を蒸発させればよい。ここで、遷移金属の担持量は、担体に対して、０．１〜４０質量％が好ましく、１〜２０質量％がより好ましい。 The transition metal can be supported on the 12CaO.7Al 2 O 3 fine particle support by, for example, an impregnation method using an organic solvent. Specifically, the support may be put into an organic solvent dispersion such as hexane of a transition metal and then stirred to evaporate the solvent. Here, the supported amount of the transition metal is preferably 0.1 to 40% by mass, and more preferably 1 to 20% by mass with respect to the carrier.
本発明の触媒を用いれば、炭化水素ガスを直接分解して水素を製造することができる。すなわち、本発明の触媒に炭化水素ガスを接触させれば、炭化水素が直接分解して水素ガスが得られる。反応は、メタンガスの場合を例にとれば、ＣＨ4→Ｃ＋２Ｈ2となる。従って、二酸化炭素や一酸化炭素が副生しない。
炭化水素ガスとしては、飽和炭化水素ガスが好ましく、炭素数１〜４の飽和炭化水素ガスがより好ましく、メタンガスがさらに好ましい。
炭化水素ガスの反応温度は、４００℃以上が好ましく、高転化率を維持するためには６００℃以上がより好ましい。また反応温度の上限は１０００℃で十分である。
炭化水素ガスは、副反応を防止するため二酸化炭素や水素含有量は少ないのが好ましい。
If the catalyst of this invention is used, hydrocarbon gas can be decomposed | disassembled directly and hydrogen can be manufactured. That is, when hydrocarbon gas is brought into contact with the catalyst of the present invention, hydrocarbon is directly decomposed to obtain hydrogen gas. Taking the case of methane gas as an example, the reaction is CH 4 → C + 2H 2 . Therefore, carbon dioxide and carbon monoxide are not by-produced.
As the hydrocarbon gas, a saturated hydrocarbon gas is preferable, a saturated hydrocarbon gas having 1 to 4 carbon atoms is more preferable, and methane gas is more preferable.
The reaction temperature of the hydrocarbon gas is preferably 400 ° C. or higher, and more preferably 600 ° C. or higher in order to maintain a high conversion rate. The upper limit of the reaction temperature is sufficient to be 1000 ° C.
The hydrocarbon gas preferably has a low carbon dioxide or hydrogen content in order to prevent side reactions.
より具体的には、図１に示すようなガス流通触媒反応管を用いて炭化水素ガスから水素を製造するのが好ましい。すなわち、触媒を設置した反応管中で炭化水素ガス（メタンガス等）を流通させて反応ガスを回収すればよい。反応管は加熱炉により４００℃以上に加熱する。 More specifically, it is preferable to produce hydrogen from hydrocarbon gas using a gas flow catalyst reaction tube as shown in FIG. That is, the reaction gas may be recovered by circulating hydrocarbon gas (methane gas or the like) in a reaction tube provided with a catalyst. The reaction tube is heated to 400 ° C. or higher by a heating furnace.
本発明方法によれば、炭化水素ガスから直接分解により水素を効率よく製造することができる。 According to the method of the present invention, hydrogen can be efficiently produced from hydrocarbon gas by direct decomposition.
次に実施例を挙げて本発明を更に詳細に説明する。 EXAMPLES Next, an Example is given and this invention is demonstrated still in detail.
実施例１
（担体作製）
酸化カルシウムとα型酸化アルミニウムがモル比［ＣａＯ］／［Ａｌ2Ｏ3］＝１．６３となる混合粉末を酸化マグネシウム坩堝に入れ、酸素濃度２１％の乾燥空気中で昇温速度４００℃／時間で１４４０℃まで昇温し、溶融させた状態で３時間保持した後降温速度１５０℃／時間で室温まで徐冷し固化物を作製した。得られた固化物は、黄色がかった白色の固体であって粉末Ｘ線回折より１２ＣａＯ・７Ａｌ2Ｏ3を主相とする回折パターンが確認された。得られた凝固物は、ジェットミルにて粉砕し、粉砕後のＢＥＴ比表面積が３．５ｍ2／ｇであった。
Example 1
(Carrier production)
A mixed powder in which the molar ratio of calcium oxide and α-type aluminum oxide is [CaO] / [Al 2 O 3 ] = 1.63 is placed in a magnesium oxide crucible and heated in a dry air with an oxygen concentration of 21% at a heating rate of 400 ° C. / The temperature was raised to 1440 ° C. over time, held in the molten state for 3 hours, and then gradually cooled to room temperature at a temperature drop rate of 150 ° C./hour to produce a solidified product. The obtained solidified product was a yellowish white solid, and a diffraction pattern having 12CaO · 7Al 2 O 3 as a main phase was confirmed by powder X-ray diffraction. The obtained solidified product was pulverized by a jet mill, and the BET specific surface area after pulverization was 3.5 m 2 / g.
（触媒担持）
上記で作製した触媒用担体に活性金属を担持するため、担持量が５質量％となるようＮｉナノ粒子（メジアン径５ｎｍ）のヘキサン分散液中に担体粉末を投入後、スターラーで２４時間撹拌しヘキサン溶媒を蒸発させＮｉ触媒を作製した。
(Catalyst support)
In order to support the active metal on the catalyst support prepared above, the support powder was put into a hexane dispersion of Ni nanoparticles (median diameter 5 nm) so that the supported amount was 5% by mass, and then stirred with a stirrer for 24 hours. The hexane solvent was evaporated to prepare a Ni catalyst.
（触媒性能評価）
図１の模式構成図に示すガス流通触媒反応管を用いて、メタンの直接分解による水素生成に対する触媒活性を調べた。
石英反応管内に触媒試料を設置し、窒素ガス流通雰囲気にて７００℃まで昇温した後５０００ｍＬ／ｈｒの流速でメタンガスを流し１時間保持した。その後、反応ガスを回収してガスクロマトグラフィーにてメタンガス濃度及び水素ガス濃度を測定し、メタン転化率ならびに水素収率を算出して触媒活性を評価した。
その結果、メタン転化率が２５．７％、水素収率が２３．１％であった。
(Catalyst performance evaluation)
Using the gas flow catalytic reaction tube shown in the schematic configuration diagram of FIG. 1, the catalytic activity for hydrogen generation by direct decomposition of methane was examined.
A catalyst sample was placed in a quartz reaction tube, heated to 700 ° C. in a nitrogen gas flow atmosphere, and then methane gas was flowed at a flow rate of 5000 mL / hr and held for 1 hour. Thereafter, the reaction gas was recovered, the methane gas concentration and the hydrogen gas concentration were measured by gas chromatography, the methane conversion rate and the hydrogen yield were calculated, and the catalytic activity was evaluated.
As a result, the methane conversion was 25.7% and the hydrogen yield was 23.1%.
実施例２
（担体作製）
酸化カルシウムとα型酸化アルミニウムがモル比［ＣａＯ］／［Ａｌ2Ｏ3］＝１．７１となる混合粉末を炭素坩堝に入れ、５０Ｐａ以下の真空条件下で昇温速度４００℃／時間で１４４０℃まで昇温し、溶融させた状態で３時間保持した後降温速度１５０℃／時間で室温まで徐冷し固化物を作製した。得られた固化物は、黒色の固体であって粉砕時には緑色の粉末であった。粉末Ｘ線回折より１２ＣａＯ・７Ａｌ2Ｏ3を主相とする回折パターンが確認された。
得られた凝固物は、ジェットミルにて粉砕し、粉砕後のＢＥＴ比表面積が２．５ｍ2／ｇであった。
Example 2
(Carrier production)
A mixed powder in which the molar ratio of calcium oxide and α-type aluminum oxide is [CaO] / [Al 2 O 3 ] = 1.71 is placed in a carbon crucible and 1440 at a heating rate of 400 ° C./hour under a vacuum condition of 50 Pa or less. The temperature was raised to 0 ° C., held in the melted state for 3 hours, and then gradually cooled to room temperature at a temperature drop rate of 150 ° C./hour to produce a solidified product. The obtained solidified product was a black solid and was a green powder when pulverized. From the powder X-ray diffraction, a diffraction pattern having 12CaO · 7Al 2 O 3 as a main phase was confirmed.
The obtained solidified product was pulverized by a jet mill, and the BET specific surface area after pulverization was 2.5 m 2 / g.
（触媒担持）
上記で作製した触媒用担体に活性金属を担持するため、担持量が５ｗｔ％となるようＮｉナノ粒子（メジアン径５ｎｍ）のヘキサン分散液中に担体粉末を投入後、スターラーで２４時間撹拌しヘキサン溶媒を蒸発させＮｉ触媒を作製した。
(Catalyst support)
In order to support the active metal on the catalyst support prepared above, the support powder was put into a hexane dispersion of Ni nanoparticles (median diameter 5 nm) so that the supported amount would be 5 wt%, and then stirred for 24 hours with a stirrer. The solvent was evaporated to prepare a Ni catalyst.
（触媒性能評価）
図１の模式構成図に示すガス流通触媒反応管を用いて、メタンの直接分解による水素生成に対する触媒活性を調べた。
石英反応管内に触媒試料を設置し、窒素ガス流通雰囲気にて７００℃まで昇温した後５０００ｍＬ／ｈｒの流速でメタンガスを流し１時間保持した。その後、反応ガスを回収してガスクロマトグラフィーにてメタン濃度及び水素ガス濃度を測定し、メタン転化率ならびに水素収率を算出して触媒活性を評価した。
その結果、メタン転化率が３０．６％、水素収率が３２．５％であった。
(Catalyst performance evaluation)
Using the gas flow catalytic reaction tube shown in the schematic configuration diagram of FIG. 1, the catalytic activity for hydrogen generation by direct decomposition of methane was examined.
A catalyst sample was placed in a quartz reaction tube, heated to 700 ° C. in a nitrogen gas flow atmosphere, and then methane gas was flowed at a flow rate of 5000 mL / hr and held for 1 hour. Thereafter, the reaction gas was recovered, the methane concentration and the hydrogen gas concentration were measured by gas chromatography, the methane conversion rate and the hydrogen yield were calculated, and the catalytic activity was evaluated.
As a result, the methane conversion was 30.6% and the hydrogen yield was 32.5%.
比較例
（担体作製）
一般に広く用いられるγ型酸化アルミニウムを用いた（ＢＥＴ比表面積３００ｍ2／ｇ）。
（触媒担持）
上記担体に活性金属を担持するため、担持量が５ｗｔ％となるようＮｉナノ粒子（メジアン径５ｎｍ）のヘキサン分散液中に担体粉末を投入後、スターラーで２４時間撹拌しヘキサン溶媒を蒸発させＮｉ触媒を作製した。
Comparative example (carrier preparation)
Generally used γ-type aluminum oxide (BET specific surface area 300 m 2 / g) was used.
(Catalyst support)
In order to support the active metal on the carrier, the carrier powder was put into a hexane dispersion of Ni nanoparticles (median diameter 5 nm) so that the amount supported was 5 wt%, and then stirred for 24 hours with a stirrer to evaporate the hexane solvent to remove Ni. A catalyst was prepared.
（触媒性能評価）
図１の模式構成図に示すガス流通触媒反応管を用いて、メタンの直接分解による水素生成に対する触媒活性を調べた。
石英反応管内に触媒試料を設置し、窒素ガス流通雰囲気にて７００℃まで昇温した後５０００ｍＬ／ｈｒの流速でメタンガスを流し１時間保持した。その後、反応ガスを回収してガスクロマトグラフィーにてメタンガス濃度及び水素ガス濃度を測定し、メタン転化率ならびに水素収率を算出して触媒活性を評価した。
その結果、メタン転化率が０．３％であった。
(Catalyst performance evaluation)
Using the gas flow catalytic reaction tube shown in the schematic configuration diagram of FIG. 1, the catalytic activity for hydrogen generation by direct decomposition of methane was examined.
A catalyst sample was placed in a quartz reaction tube, heated to 700 ° C. in a nitrogen gas flow atmosphere, and then methane gas was flowed at a flow rate of 5000 mL / hr and held for 1 hour. Thereafter, the reaction gas was recovered, the methane gas concentration and the hydrogen gas concentration were measured by gas chromatography, the methane conversion rate and the hydrogen yield were calculated, and the catalytic activity was evaluated.
As a result, the methane conversion was 0.3%.
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| WO2014045780A1 (en) * | 2012-09-20 | 2014-03-27 | 国立大学法人東京工業大学 | Hydrogen generation catalyst and method for producing hydrogen |
| JP2015209344A (en) * | 2014-04-24 | 2015-11-24 | Ｊｆｅエンジニアリング株式会社 | Hydrogen-carbon material production method and production apparatus |
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