JP4738024B2 - Method and system for reforming methane with carbon dioxide and steam, catalyst for reforming, and method for producing the catalyst - Google Patents
Method and system for reforming methane with carbon dioxide and steam, catalyst for reforming, and method for producing the catalyst Download PDFInfo
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims description 116
- 239000003054 catalyst Substances 0.000 title claims description 87
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims description 84
- 239000001569 carbon dioxide Substances 0.000 title claims description 42
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims description 42
- 238000000034 method Methods 0.000 title claims description 29
- 238000002407 reforming Methods 0.000 title claims description 28
- 238000004519 manufacturing process Methods 0.000 title claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 32
- 239000010948 rhodium Substances 0.000 claims description 24
- 229910052707 ruthenium Inorganic materials 0.000 claims description 21
- 229910052703 rhodium Inorganic materials 0.000 claims description 20
- 239000000395 magnesium oxide Substances 0.000 claims description 14
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 14
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 14
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 claims description 12
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 claims description 11
- 239000002002 slurry Substances 0.000 claims description 11
- 239000003513 alkali Substances 0.000 claims description 9
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 9
- 239000002245 particle Substances 0.000 claims description 9
- 239000002244 precipitate Substances 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 claims description 7
- 238000001556 precipitation Methods 0.000 claims description 7
- 229910000420 cerium oxide Inorganic materials 0.000 claims description 6
- 238000001704 evaporation Methods 0.000 claims description 6
- BMMGVYCKOGBVEV-UHFFFAOYSA-N oxo(oxoceriooxy)cerium Chemical compound [Ce]=O.O=[Ce]=O BMMGVYCKOGBVEV-UHFFFAOYSA-N 0.000 claims description 6
- IATRAKWUXMZMIY-UHFFFAOYSA-N strontium oxide Chemical compound [O-2].[Sr+2] IATRAKWUXMZMIY-UHFFFAOYSA-N 0.000 claims description 6
- 230000008020 evaporation Effects 0.000 claims description 5
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 claims description 5
- 229910001928 zirconium oxide Inorganic materials 0.000 claims description 5
- 239000013078 crystal Substances 0.000 claims description 4
- 239000000047 product Substances 0.000 claims description 4
- 238000001354 calcination Methods 0.000 claims 1
- 238000006057 reforming reaction Methods 0.000 description 21
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 18
- 238000006243 chemical reaction Methods 0.000 description 15
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 14
- 229910052799 carbon Inorganic materials 0.000 description 12
- 230000000694 effects Effects 0.000 description 12
- 238000010304 firing Methods 0.000 description 11
- 239000004480 active ingredient Substances 0.000 description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 238000002360 preparation method Methods 0.000 description 9
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 8
- 230000000052 comparative effect Effects 0.000 description 8
- 230000008021 deposition Effects 0.000 description 7
- 238000000629 steam reforming Methods 0.000 description 7
- 229910052782 aluminium Inorganic materials 0.000 description 6
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 6
- 239000002131 composite material Substances 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 239000000843 powder Substances 0.000 description 6
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 5
- 239000007864 aqueous solution Substances 0.000 description 5
- 229910052712 strontium Inorganic materials 0.000 description 5
- 229910052726 zirconium Inorganic materials 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 4
- 239000008187 granular material Substances 0.000 description 4
- VDRDGQXTSLSKKY-UHFFFAOYSA-K ruthenium(3+);trihydroxide Chemical compound [OH-].[OH-].[OH-].[Ru+3] VDRDGQXTSLSKKY-UHFFFAOYSA-K 0.000 description 4
- 238000007086 side reaction Methods 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 3
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 230000003247 decreasing effect Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 238000000465 moulding Methods 0.000 description 3
- GTCKPGDAPXUISX-UHFFFAOYSA-N ruthenium(3+);trinitrate Chemical compound [Ru+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O GTCKPGDAPXUISX-UHFFFAOYSA-N 0.000 description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- HSJPMRKMPBAUAU-UHFFFAOYSA-N cerium(3+);trinitrate Chemical compound [Ce+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O HSJPMRKMPBAUAU-UHFFFAOYSA-N 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 229910052746 lanthanum Inorganic materials 0.000 description 2
- 229940050906 magnesium chloride hexahydrate Drugs 0.000 description 2
- DHRRIBDTHFBPNG-UHFFFAOYSA-L magnesium dichloride hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[Cl-].[Cl-] DHRRIBDTHFBPNG-UHFFFAOYSA-L 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 150000002823 nitrates Chemical class 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- DHEQXMRUPNDRPG-UHFFFAOYSA-N strontium nitrate Chemical compound [Sr+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O DHEQXMRUPNDRPG-UHFFFAOYSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 229910004631 Ce(NO3)3.6H2O Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-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
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 229910052788 barium Inorganic materials 0.000 description 1
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- -1 hydroxide compound Chemical class 0.000 description 1
- FZLIPJUXYLNCLC-UHFFFAOYSA-N lanthanum atom Chemical compound [La] FZLIPJUXYLNCLC-UHFFFAOYSA-N 0.000 description 1
- 229960002337 magnesium chloride Drugs 0.000 description 1
- 229910001629 magnesium chloride Inorganic materials 0.000 description 1
- AOPCKOPZYFFEDA-UHFFFAOYSA-N nickel(2+);dinitrate;hexahydrate Chemical compound O.O.O.O.O.O.[Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O AOPCKOPZYFFEDA-UHFFFAOYSA-N 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- UFQXGXDIJMBKTC-UHFFFAOYSA-N oxostrontium Chemical compound [Sr]=O UFQXGXDIJMBKTC-UHFFFAOYSA-N 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- KTEDZFORYFITAF-UHFFFAOYSA-K rhodium(3+);trihydroxide Chemical compound [OH-].[OH-].[OH-].[Rh+3] KTEDZFORYFITAF-UHFFFAOYSA-K 0.000 description 1
- VXNYVYJABGOSBX-UHFFFAOYSA-N rhodium(3+);trinitrate Chemical compound [Rh+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O VXNYVYJABGOSBX-UHFFFAOYSA-N 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
Classifications
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Hydrogen, Water And Hydrids (AREA)
- Catalysts (AREA)
Description
本発明は、二酸化炭素及び水蒸気によるメタンの改質方法及びシステム、この改質用の触媒、並びにこの触媒の製造方法に関する。 The present invention relates to a method and system for reforming methane with carbon dioxide and steam, a catalyst for the reforming, and a method for producing the catalyst.
メタンを改質して水素を生成する方法は、メタンと水蒸気とを反応させる水蒸気改質反応（式１）が主体となっている。
ＣＨ4＋Ｈ2Ｏ→３Ｈ2＋ＣＯ・・・（式１）
A method of reforming methane to generate hydrogen mainly consists of a steam reforming reaction (Equation 1) in which methane reacts with steam.
CH 4 + H 2 O → 3H 2 + CO (Formula 1)
水蒸気改質反応は、反応の段階で、原料の水を水蒸気にする必要があるが、メタンに対する水蒸気の比（以下、「Ｓ／Ｃ比」と略す）が低い場合、メタンの水蒸気改質が十分に行われずに、副反応として、メタンの分解反応（式２）が起こる。
ＣＨ4→２Ｈ2＋Ｃ・・・（式２）
In the steam reforming reaction, the raw material water needs to be steam at the reaction stage, but when the ratio of steam to methane (hereinafter referred to as “S / C ratio”) is low, steam reforming of methane is not possible. If it is not performed sufficiently, a methane decomposition reaction (formula 2) occurs as a side reaction.
CH 4 → 2H 2 + C (Formula 2)
この副反応によって触媒上に炭素が析出すると、触媒の活性が阻害され、反応効率が低下するという問題がある。したがって、炭素析出を防止するために、Ｓ／Ｃ比を高くする必要がある。しかしながら、Ｓ／Ｃ比を高くすると熱効率の低下などが生じ、経済的な面での損失が大きくなるという問題がある。 When carbon is deposited on the catalyst by this side reaction, there is a problem that the activity of the catalyst is inhibited and the reaction efficiency is lowered. Therefore, it is necessary to increase the S / C ratio in order to prevent carbon deposition. However, when the S / C ratio is increased, there is a problem that the thermal efficiency is reduced and the loss in terms of economy is increased.
一方、温室効果ガスである二酸化炭素を固定化する方法の１つとして、二酸化炭素をメタンと反応させて水素を生成する方法が提案されている。この反応を式３に示す。
ＣＨ4＋ＣＯ2→２Ｈ2＋２ＣＯ・・・（式３）
On the other hand, as one method of fixing carbon dioxide, which is a greenhouse gas, a method of generating hydrogen by reacting carbon dioxide with methane has been proposed. This reaction is shown in Equation 3.
CH 4 + CO 2 → 2H 2 + 2CO (Formula 3)
この式３の反応に有効な触媒としては、酸化アルミニウム担持ニッケル触媒がある。しかしながら、このＮｉ／Ａｌ2Ｏ3触媒は、副反応（式２）の炭素析出により活性低下が甚だしいという問題がある。そこで、炭素の析出防止を図るために、上記の触媒にランタン（Ｌａ）又はバリウム（Ｂａ）を添加することが提案されている（非特許文献１）。
本発明は、メタンに対する水蒸気の比（Ｓ／Ｃ比）を相対的に減少させるために、水蒸気とともに二酸化炭素によってメタンを改質することを図るものである。すなわち、本発明は、水蒸気改質反応（式１）と二酸化炭素改質反応（式３）とを同時に進行させることを図るものである。しかしながら、水蒸気改質反応に用いられる従来の触媒は、二酸化炭素改質反応に対して活性が非常に低いという問題がある。一方、上記文献に記載されたＬａ又はＢａ添加のＮｉ触媒は、二酸化炭素改質反応に対して活性が高いものの、依然として副反応（式２）により炭素が析出して触媒活性が低下すること、及び触媒成分であるＮｉが水蒸気により酸化され触媒性能が低下することから長期間にわたって安定してメタンを改質することができないという問題がある。 The present invention aims to reform methane with carbon dioxide together with water vapor in order to relatively reduce the ratio of water vapor to methane (S / C ratio). That is, the present invention intends to allow the steam reforming reaction (Formula 1) and the carbon dioxide reforming reaction (Formula 3) to proceed simultaneously. However, the conventional catalyst used for the steam reforming reaction has a problem that its activity is very low for the carbon dioxide reforming reaction. On the other hand, the La or Ba-added Ni catalyst described in the above document has high activity with respect to the carbon dioxide reforming reaction, but carbon is still precipitated by the side reaction (formula 2) and the catalytic activity is reduced. In addition, since Ni which is a catalyst component is oxidized by water vapor and the catalytic performance is lowered, there is a problem that methane cannot be stably reformed over a long period of time.
そこで本発明は、上記の問題点に鑑み、メタンに対する水蒸気の比（Ｓ／Ｃ比）を低くできるとともに、メタンを長期間にわたって安定して改質することができる二酸化炭素及び水蒸気によるメタンの改質方法及びシステム、この改質用の触媒、並びにこの触媒の製造方法を提供することを目的とする。 Therefore, in view of the above problems, the present invention can reduce the ratio of water vapor to methane (S / C ratio) and can improve the stability of methane over a long period of time. It is an object of the present invention to provide a quality method and system, a catalyst for the reforming, and a method for producing the catalyst.
上記の目的を達成するために、本発明に係る二酸化炭素及び水蒸気によりメタンを改質するための触媒は、ルテニウム及びロジウムからなる群から選択される少なくとも１つの活性成分が、酸化セリウムの第１の酸化物と、酸化アルミニウム及び酸化ジルコニウムからなる群から選択される少なくとも１つの第２の酸化物とを含む担体に担持されていることを特徴とする。 In order to achieve the above object, in the catalyst for reforming methane with carbon dioxide and steam according to the present invention, at least one active component selected from the group consisting of ruthenium and rhodium is the first cerium oxide . And a support containing at least one second oxide selected from the group consisting of aluminum oxide and zirconium oxide.
このように、活性成分としてルテニウム又はロジウムを採用することで、水蒸気改質反応及び二酸化炭素改質反応の両方に対して優れた活性を得ることができる。また、上記第１の酸化物と上記第２の酸化物との両方を含む担体を採用することで、第１の酸化物である酸化セリウムにより担体全体が電子供与性（δ-）となり、水蒸気及び二酸化炭素が担体に活性化吸着するので、相対的に触媒表面でのメタンの分解反応を防止することができる。したがって、本触媒によれば、Ｓ／Ｃ比を低くすることができるとともに、触媒上への炭素析出が防止され、メタンを長期間にわたって安定して改質することができる。 As described above, by using ruthenium or rhodium as an active component, it is possible to obtain excellent activity for both the steam reforming reaction and the carbon dioxide reforming reaction. Further, by employing a carrier containing both the first oxide and the second oxide, the entire carrier becomes electron donating (δ − ) by cerium oxide, which is the first oxide, and water vapor Since carbon dioxide and activated carbon are activated and adsorbed on the carrier, the decomposition reaction of methane on the catalyst surface can be relatively prevented. Therefore, according to the present catalyst, the S / C ratio can be lowered, carbon deposition on the catalyst can be prevented, and methane can be stably reformed over a long period of time.
前記活性成分であるルテニウム又はロジウムの粒径は、５ｎｍ以下であることが好ましい。活性成分の粒径を５ｎｍ以下にすることで、活性成分も電子供与性（δ-）にすることができる。したがって、水蒸気及び二酸化炭素が活性成分に活性化吸着するので、活性成分表面への炭素析出をより確実に防止することができるので、触媒の活性低下をさらに顕著に防止することができる。 The particle size of ruthenium or rhodium as the active ingredient is preferably 5 nm or less. By making the particle size of the active ingredient 5 nm or less, the active ingredient can also be electron donating (δ − ). Therefore, since water vapor and carbon dioxide are activated and adsorbed on the active component, carbon deposition on the surface of the active component can be more reliably prevented, so that a decrease in the activity of the catalyst can be more remarkably prevented.
前記活性成分であるルテニウム又はロジウムの結晶形態は、アモルファス状であることが好ましい。活性成分の結晶形態をアモルファス状にすることで、特に二酸化炭素改質反応の活性を顕著に向上させることができる。 The crystalline form of ruthenium or rhodium, which is the active ingredient, is preferably amorphous. By making the crystal form of the active component amorphous, the activity of the carbon dioxide reforming reaction can be significantly improved.
前記活性成分の量は、触媒全体を１００重量％とすると、０．０１〜５重量％であることが好ましい。また、前記第１の酸化物の量は、前記第１の酸化物と前記第２の酸化物の合計を１００重量％とすると、２０〜６０重量％であることが好ましい。 The amount of the active component is preferably 0.01 to 5% by weight when the total catalyst is 100% by weight. The amount of the first oxide is preferably 20 to 60% by weight when the total of the first oxide and the second oxide is 100% by weight.
このように、ルテニウム又はロジウムの水酸化物を含有するスラリーを、担体である粒状の酸化物に添加して焼成することで、活性成分となるルテニウム又はロジウムを担体上に５ｎｍ以下の粒径でアモルファス状に高分散化させることができる。 Thus, the slurry containing ruthenium or rhodium hydroxide is added to the granular oxide as the carrier and baked, so that the ruthenium or rhodium as the active ingredient is deposited on the carrier with a particle size of 5 nm or less. Highly dispersed in an amorphous state.
なお、前記粒状の担体は、アルカリ沈殿法又は蒸発乾固法によって生成する沈殿物又は乾固物を焼成することによって得られるものが好ましい。 The granular carrier is preferably obtained by firing a precipitate or a dried product produced by an alkali precipitation method or an evaporation to dryness method.
本発明は、別の態様として、二酸化炭素及び水蒸気によりメタンを改質するための触媒を製造する方法であって、ルテニウム及びロジウムからなる群から選択される少なくとも１つの元素の水酸化物を含有するスラリーを、酸化セリウムの第１の酸化物と、酸化アルミニウム及び酸化ジルコニウムからなる群から選択される少なくとも１つの第２の酸化物とを含む粒状の担体に添加して焼成する工程と含んでなることを特徴とする。 Another aspect of the present invention is a method for producing a catalyst for reforming methane with carbon dioxide and steam, which contains a hydroxide of at least one element selected from the group consisting of ruthenium and rhodium. Adding the slurry to be granulated to a granular support containing a first oxide of cerium oxide and at least one second oxide selected from the group consisting of aluminum oxide and zirconium oxide, and firing. It is characterized by becoming.
本発明に係る製造方法は、アルカリ沈殿法又は蒸発乾固法によって生成する沈殿物又は乾固物を焼成して前記粒状の担体を得る工程をさらに含むことが好ましい。 The production method according to the present invention preferably further includes a step of obtaining a granular carrier by baking a precipitate or a dried product produced by an alkali precipitation method or an evaporation to dry method.
本発明は、さらに別の態様として、二酸化炭素及び水蒸気によりメタンを改質する方法であって、上記に記載した触媒を用いることを特徴とする。 As another aspect of the present invention, there is provided a method for reforming methane with carbon dioxide and water vapor, wherein the catalyst described above is used.
本発明は、またさらに別の態様として、二酸化炭素及び水蒸気によりメタンを改質するシステムであって、上記に記載した触媒を備えていることを特徴とする。 As still another aspect of the present invention, there is provided a system for reforming methane with carbon dioxide and steam, which is characterized by comprising the catalyst described above.
上記したように、本発明によれば、Ｓ／Ｃ比を低くできるとともに、メタンを長期間にわたって安定して改質することができる二酸化炭素及び水蒸気によるメタンの改質方法及びシステム、この改質用の触媒、並びにこの触媒の製造方法が提供される。 As described above, according to the present invention, a method and system for reforming methane with carbon dioxide and steam, which can lower the S / C ratio and can stably reform methane over a long period of time, and this reforming And a process for producing the catalyst.
以下、本発明の一実施の形態について説明する。先ず、本発明に係る触媒の一実施の形態について説明する。触媒の活性成分は、ルテニウム（Ｒｕ）又はロジウム（Ｒｈ）である。Ｒｕ又はＲｈを活性成分として用いることで、水蒸気改質反応及び二酸化炭素改質反応の両方に対して優れた活性を得ることができる。また、Ｒｕ又はＲｈの粒径は直径５ｎｍ以下であることが好ましい。粒径を５ｎｍ以下にすることで、活性成分を電子供与性（δ-）にすることができる。 Hereinafter, an embodiment of the present invention will be described. First, an embodiment of the catalyst according to the present invention will be described. The active component of the catalyst is ruthenium (Ru) or rhodium (Rh). By using Ru or Rh as an active ingredient, excellent activity can be obtained for both the steam reforming reaction and the carbon dioxide reforming reaction. The particle size of Ru or Rh is preferably 5 nm or less in diameter. By making the particle size 5 nm or less, the active component can be made electron donating (δ − ).
Ｒｕ又はＲｈの結晶形態は、アモルファス状であることが好ましい。アモルファス状にすることで、特に二酸化炭素改質反応の活性を顕著に向上させることができる。活性成分の量は、触媒全体を１００重量％とすると、０．０１〜５重量％が好ましく、０．１〜２重量％がより好ましい。０．０１重量％以上にすることで、反応活性サイトが多くなり十分な反応速度を得ることができる。また、５重量％以下にすることで、担体からの電子供与効果が十分に得られ、メタンの直接分解反応をより確実に防止することができる。 The crystal form of Ru or Rh is preferably amorphous. By making it amorphous, particularly the activity of the carbon dioxide reforming reaction can be remarkably improved. The amount of the active component is preferably 0.01 to 5% by weight, more preferably 0.1 to 2% by weight, based on 100% by weight of the entire catalyst. By setting the content to 0.01% by weight or more, the reaction active sites increase and a sufficient reaction rate can be obtained. Further, when the content is 5% by weight or less, the effect of donating electrons from the carrier can be sufficiently obtained, and the direct decomposition reaction of methane can be more reliably prevented.
また、触媒の担体は、酸化マグネシウム（ＭｇＯ）、酸化セリウム（ＣｅＯ2）及び酸化ストロンチウム（ＳｒＯ）のうちの少なくとも１種の第１の酸化物と、酸化アルミニウム（Ａｌ2Ｏ3）及び酸化ジルコニウム（ＺｒＯ2）のうちの少なくとも１種の第２の酸化物とを含む担体である。第１の酸化物としてＭｇＯ、ＣｅＯ2又はＳｒＯを用いることで、担体を電子供与性（δ-）にすることができる。そして、第１の酸化物と第２の酸化物との両方を含む担体とすることで、担体全体が電子供与性（δ-）となり、水蒸気及び二酸化炭素が担体に活性化吸着されるので、相対的に触媒表面でのメタンの分解反応を防止することができる。 The catalyst carrier includes at least one first oxide of magnesium oxide (MgO), cerium oxide (CeO 2 ), and strontium oxide (SrO), aluminum oxide (Al 2 O 3 ), and zirconium oxide. A support containing at least one second oxide of (ZrO 2 ). By using MgO, CeO 2 or SrO as the first oxide, the carrier can be made electron donating (δ − ). And, by using a carrier containing both the first oxide and the second oxide, the entire carrier becomes electron donating (δ − ), and water vapor and carbon dioxide are activated and adsorbed on the carrier. The decomposition reaction of methane on the catalyst surface can be relatively prevented.
なお、第２の酸化物としてＡｌ2Ｏ3又はＺｒＯ2を用いることで、８００℃以上の高温状態に晒されてもその多孔質性を維持することができ、改質反応時における触媒のメタンに対する高い接触効率が維持される。第１の酸化物の量は、第１の酸化物と第２の酸化物との合計を１００重量％とすると、２０〜６０重量％であることが好ましい。２０重量％以上にすることで、これらは容易に複合酸化物となり電子供与効果を十分に発揮することができる。また、６０重量％以下にすることで、８００℃以上の高温使用によっても担体の比表面積を確実に維持することができる。 By using Al 2 O 3 or ZrO 2 as the second oxide, the porosity can be maintained even when exposed to a high temperature state of 800 ° C. or higher, and the catalyst methane during the reforming reaction. High contact efficiency is maintained. The amount of the first oxide is preferably 20 to 60% by weight when the total of the first oxide and the second oxide is 100% by weight. By setting it to 20% by weight or more, these easily become complex oxides and can sufficiently exhibit the electron donating effect. Moreover, the specific surface area of a support | carrier can be reliably maintained by using 60 weight% or less by high temperature use of 800 degreeC or more.
次に、本発明に係る触媒の製造方法の一実施の形態について説明する。触媒の担体は、アルカリ沈殿法や蒸発乾固法等により調製することが好ましい。以下に先ず、アルカリ沈殿法による手順について詳細に説明する。先ず、Ｍｇ、Ｃｅ又はＳｒの塩化物や硝酸塩等の塩と、Ａｌ又はＺｒの塩化物や硝酸塩等の塩とに、炭酸ナトリウム（Ｎａ2ＣＯ3）、水酸化ナトリウム（ＮａＯＨ）、アンモニア（ＮＨ4ＯＨ）等のアルカリを加える。これにより、Ｍｇ、Ｃｅ又はＳｒと、Ａｌ又はＺｒとの水酸化化合物又は塩基性炭酸塩を含む沈殿物を得ることができる。 Next, an embodiment of a method for producing a catalyst according to the present invention will be described. The catalyst carrier is preferably prepared by alkali precipitation, evaporation to dryness, or the like. First, the procedure by the alkali precipitation method will be described in detail. First, Mg, Ce or Sr chloride or nitrate salt, Al or Zr chloride or nitrate salt, sodium carbonate (Na 2 CO 3 ), sodium hydroxide (NaOH), ammonia (NH 4 Add an alkali such as OH). Thereby, the deposit containing the hydroxide compound or basic carbonate of Mg, Ce, or Sr and Al or Zr can be obtained.
この得られた沈殿物を焼成することで、Ｍｇ、Ｃｅ又はＳｒと、Ａｌ又はＺｒとの複合酸化物が得られる。なお、焼成温度は５００〜１１００℃が好ましく、焼成時間は１〜２４時間が好ましい。また、焼成前に沈殿物を乾燥させておくことが好ましい。得られた複合酸化物は直径１０〜３０μｍの粉末状であるので、反応ガスの通気性向上のため、直径１〜７ｍｍの粒状に成型することが好ましい。 By firing the obtained precipitate, a composite oxide of Mg, Ce or Sr and Al or Zr is obtained. The firing temperature is preferably 500 to 1100 ° C., and the firing time is preferably 1 to 24 hours. Moreover, it is preferable to dry the precipitate before firing. Since the obtained composite oxide is in the form of a powder having a diameter of 10 to 30 μm, it is preferably molded into a particle having a diameter of 1 to 7 mm in order to improve the gas permeability of the reaction gas.
次に、蒸発乾固法による担体の調製手順について詳細に説明する。先ず、Ｍｇ、Ｃｅ又はＳｒの塩化物や硝酸塩等の塩を溶解させた水溶液にＡｌ2Ｏ3又はＺｒＯ2の粉末又は粒子を浸漬する。この水溶液を加熱して水分を蒸発させることで、乾固物を得ることができる。また、Ａｌ2Ｏ3又はＺｒＯ2は、Ａｌ又はＺｒの塩化物や硝酸塩等の塩にアルカリを加えることで得られる。そして、この乾固物を焼成して酸化物化することで、Ｍｇ、Ｃｅ又はＳｒと、Ａｌ又はＺｒとの複合酸化物を得ることができる。なお、焼成の条件は上記と同様である。 Next, the procedure for preparing the carrier by the evaporation to dryness method will be described in detail. First, Al 2 O 3 or ZrO 2 powder or particles are immersed in an aqueous solution in which a salt such as chloride, nitrate or the like of Mg, Ce or Sr is dissolved. A dried product can be obtained by heating the aqueous solution to evaporate the water. Al 2 O 3 or ZrO 2 can be obtained by adding an alkali to a salt such as a chloride or nitrate of Al or Zr. And by baking this dried solid substance and oxidizing it, the complex oxide of Mg, Ce, or Sr, and Al or Zr can be obtained. The firing conditions are the same as above.
そして、上記により得られた粒状の複合酸化物に活性成分を担持させる。活性成分の担持方法は、活性成分の水酸化物を含有するスラリーを担体に分散させて焼成する方法が好ましい。以下、本方法の手順について詳細に説明する。先ず、アルカリ沈殿法や、Ｒｕ又はＲｈの水酸化物を湿式粉砕する等の方法によって、Ｒｕ又はＲｈの水酸化物スラリーを調製する。アルカリ沈殿法では、Ｒｕ又はＲｈの硝酸塩又は炭酸塩を、アンモニウム水や水酸化ナトリウム等のアルカリで中和して、Ｒｕ又はＲｈの水酸化物を含有するスラリーを生成する。 And an active ingredient is carry | supported by the granular complex oxide obtained by the above. As a method for supporting the active ingredient, a method in which a slurry containing a hydroxide of the active ingredient is dispersed in a carrier and calcined is preferable. Hereinafter, the procedure of this method will be described in detail. First, a hydroxide slurry of Ru or Rh is prepared by an alkali precipitation method or a method of wet pulverizing a hydroxide of Ru or Rh. In the alkaline precipitation method, Ru or Rh nitrate or carbonate is neutralized with an alkali such as ammonium water or sodium hydroxide to produce a slurry containing Ru or Rh hydroxide.
このスラリーを、上記により得られた粒状の複合酸化物に混合添加した後、この混合添加したものを焼成する。これにより、Ｒｕ又はＲｈの水酸化物は、結晶形態がアモルファス状で、粒径が直径５ｎｍ以下であるＲｕ又はＲｈとなり、粒状の複合酸化物の表面上に分散担持される。なお、焼成温度は５００〜１１００℃が好ましく、焼成時間は１〜２４時間が好ましい。また、焼成前に乾燥させておくことが好ましい。以上により、本発明に係る触媒を製造することができる。 The slurry is mixed and added to the granular composite oxide obtained as described above, and then the mixture and added are fired. Thereby, the hydroxide of Ru or Rh becomes Ru or Rh whose crystal form is amorphous and whose particle diameter is 5 nm or less, and is dispersed and supported on the surface of the granular composite oxide. The firing temperature is preferably 500 to 1100 ° C., and the firing time is preferably 1 to 24 hours. Moreover, it is preferable to dry before baking. As described above, the catalyst according to the present invention can be produced.
さらに次に、本発明に係る二酸化炭素及び水蒸気によりメタンを改質するシステムの一実施の形態について説明する。本システムは、本発明に係る触媒が内部に充填された改質部と、この改質部に原料であるメタンを供給するメタン供給部と、この改質部に二酸化炭素を供給する二酸化炭素供給部と、この改質部に水蒸気を供給する水蒸気供給部と、この改質部を加熱する加熱部とから主に構成されている。 Next, an embodiment of a system for reforming methane with carbon dioxide and steam according to the present invention will be described. The system includes a reforming unit filled with a catalyst according to the present invention, a methane supply unit that supplies methane as a raw material to the reforming unit, and a carbon dioxide supply that supplies carbon dioxide to the reforming unit. Part, a steam supply part for supplying steam to the reforming part, and a heating part for heating the reforming part.
このような構成によれば、先ず、加熱部によって改質部の内部を５００〜１０００℃、好ましくは６５０〜８５０℃の温度に加熱する。そして、この改質部の内部にメタン、二酸化炭素及び水蒸気を各供給部から供給する。ここで、メタンに対する水蒸気の比（Ｓ／Ｃ比）は、０．１〜３ｍｏｌ／ｍｏｌが好ましく、１．０〜２．０ｍｏｌ／ｍｏｌがより好ましい。Ｓ／Ｃ比を０．１ｍｏｌ／ｍｏｌ以上にすることで、二酸化炭素とメタンの改質反応を安定に行うことができる。また、Ｓ／Ｃ比を３ｍｏｌ／ｍｏｌ以下にすることで、水蒸気添加によるプロセス効率の低下を防止することができる。 According to such a configuration, first, the inside of the reforming section is heated to a temperature of 500 to 1000 ° C., preferably 650 to 850 ° C., by the heating section. And methane, a carbon dioxide, and water vapor | steam are supplied from this supply part inside this reforming part. Here, the ratio of water vapor to methane (S / C ratio) is preferably 0.1 to 3 mol / mol, and more preferably 1.0 to 2.0 mol / mol. By setting the S / C ratio to 0.1 mol / mol or more, the reforming reaction of carbon dioxide and methane can be performed stably. Moreover, the process efficiency fall by water vapor | steam addition can be prevented because S / C ratio shall be 3 mol / mol or less.
また、メタンに対する二酸化炭素の比（ＣＯ2／ＣＨ4比）は、０．１〜３．０ｍｏｌ／ｍｏｌが好ましく、１．０〜２．０ｍｏｌ／ｍｏｌがより好ましい。ＣＯ2／ＣＨ4比を０．１ｍｏｌ／ｍｏｌ以上にすることで、水蒸気とメタンの改質反応を安定に行うことができる。また、ＣＯ2／ＣＨ4比を３．０ｍｏｌ／ｍｏｌ以下にすることで、水及び二酸化炭素を効率よくメタンの改質反応に利用することができる。さらに、メタンに対する二酸化炭素と水蒸気の比（（ＣＯ2＋Ｈ2Ｏ）／ＣＨ4比）は、２．５ｍｏｌ／ｍｏｌ以上が好ましい。（ＣＯ2＋Ｈ2Ｏ）／ＣＨ4比を２．５ｍｏｌ／ｍｏｌ以上にすることで、二酸化炭素と水蒸気とメタンの改質反応を安定に行うことができる。 The ratio of carbon dioxide for methane (CO 2 / CH 4 ratio) is preferably from 0.1~3.0mol / mol, 1.0~2.0mol / mol is more preferable. By setting the CO 2 / CH 4 ratio to 0.1 mol / mol or more, the reforming reaction of water vapor and methane can be performed stably. Moreover, water and carbon dioxide can be efficiently utilized for the reforming reaction of methane by setting the CO 2 / CH 4 ratio to 3.0 mol / mol or less. Furthermore, the ratio of carbon dioxide and water vapor to methane (ratio of (CO 2 + H 2 O) / CH 4 ) is preferably 2.5 mol / mol or more . By setting the (CO 2 + H 2 O) / CH 4 ratio to 2.5 mol / mol or more, the reforming reaction of carbon dioxide, water vapor, and methane can be performed stably.
これにより、改質部において、メタンが水蒸気改質及び二酸化炭素改質され、水素と一酸化炭素を含有する合成ガスが得られる。改質部の内部には、本発明に係る触媒が充填されているので、二酸化炭素を供給しても、二酸化炭素によるメタンの改質反応が十分に進む。また、二酸化炭素の供給により相対的にＳ／Ｃ比が減少しても、本発明に係る触媒によって炭素の析出は防止されるので、長期間にわたってメタンを安定して改質することができる。 Thereby, in the reforming section, methane is steam reformed and carbon dioxide reformed, and a synthesis gas containing hydrogen and carbon monoxide is obtained. Since the inside of the reforming section is filled with the catalyst according to the present invention, the reforming reaction of methane by carbon dioxide proceeds sufficiently even if carbon dioxide is supplied. Further, even if the S / C ratio is relatively decreased by the supply of carbon dioxide, the catalyst according to the present invention prevents carbon deposition, so that methane can be stably reformed over a long period of time.
（触媒番号１の調製）
無水炭酸ナトリウム（Ｎａ2ＣＯ3、ＭＷ＝１０６）１８５０ｇをイオン交換水１００Ｌに溶かし、これに塩化マグネシウム６水和物（ＭｇＣｌ2・６Ｈ2Ｏ、ＭＷ＝２０３．３）１７３０ｇと無水塩化アルミニウム（ＡｌＣｌ3、ＭＷ＝１３３．３）１１６０ｇを加えた。これより得られた沈殿物を十分に水洗し、１２０℃で乾燥した後、１１００℃で５ｈ焼成した。これより得られた粉末は、酸化マグネシウムと酸化アルミニウムの重量比が５０：５０の酸化マグネシウムと酸化アルミニウムの複合酸化物（ＭｇＯ・Ａｌ2Ｏ3）であった。この粉末１ｋｇを直径約３ｍｍの粒状に成型して担体を調製した。
(Preparation of catalyst number 1)
1850 g of anhydrous sodium carbonate (Na 2 CO 3 , MW = 106) is dissolved in 100 L of ion-exchanged water, and then 1730 g of magnesium chloride hexahydrate (MgCl 2 .6H 2 O, MW = 203.3) and anhydrous aluminum chloride ( 1160 g of AlCl 3 , MW = 133.3) was added. The precipitate obtained from this was sufficiently washed with water, dried at 120 ° C., and calcined at 1100 ° C. for 5 hours. The powder thus obtained was a composite oxide (MgO.Al 2 O 3 ) of magnesium oxide and aluminum oxide having a weight ratio of magnesium oxide to aluminum oxide of 50:50. A carrier was prepared by molding 1 kg of the powder into granules having a diameter of about 3 mm.
続いて、５ｗｔ％の硝酸ルテニウム（Ｒｕ（ＮＯ3）4、ＭＷ＝３４９）水溶液１０Ｌに１Ｎのアンモニア水をｐＨ７．５になるまで添加し、黒色の水酸化ルテニウム（Ｒｕ（ＯＨ）4）を含むスラリーを調製した。そして、先に調製したＭｇＯ・Ａｌ2Ｏ3粒状担体１００ｇに、この水酸化ルテニウムスラリーをＲｕ量換算で触媒全重量に対し２ｗｔ％量添加し、１２０℃で１２ｈ十分に乾燥させた後、さらに７００℃で２４ｈ焼成させた。これにより、Ｒｕを２ｗｔ％担持したＲｕ／ＭｇＯ・Ａｌ2Ｏ3触媒（触媒番号１）を得た。 Subsequently, 1N ammonia water is added to 10 L of 5 wt% ruthenium nitrate (Ru (NO 3 ) 4 , MW = 349) aqueous solution until pH 7.5 is reached, and black ruthenium hydroxide (Ru (OH) 4 ) is added. A slurry containing was prepared. And after adding 2 wt% of this ruthenium hydroxide slurry to 100 g of the previously prepared MgO · Al 2 O 3 granular carrier in terms of Ru amount with respect to the total weight of the catalyst and sufficiently drying at 120 ° C. for 12 hours, Firing was performed at 700 ° C. for 24 hours. As a result, a Ru / MgO.Al 2 O 3 catalyst (catalyst number 1) carrying 2 wt% of Ru was obtained.
（触媒番号２の調製）
触媒番号１の調製方法に対し、硝酸ルテニウムを硝酸ロジウム（Ｒｈ（ＮＯ3）3、ＭＷ＝２８９)に変え、Ｒｈ量を触媒全重量に対し０．１ｗｔ％にしたこと以外は全て同様の調製方法により、Ｒｈ／ＭｇＯ・Ａｌ2Ｏ3触媒（触媒番号２）を調製した。
(Preparation of catalyst number 2)
All preparations are the same as the preparation method of catalyst number 1 except that ruthenium nitrate is changed to rhodium nitrate (Rh (NO 3 ) 3 , MW = 289) and the amount of Rh is 0.1 wt% with respect to the total weight of the catalyst. By the method, a Rh / MgO.Al 2 O 3 catalyst (catalyst number 2) was prepared.
（触媒番号３及び４の調製）
触媒番号１の調製方法に対し、塩化マグネシウムを硝酸第一セリウム（Ｃｅ（ＮＯ3）3・６Ｈ2Ｏ、ＭＷ＝４３４．２）１８９０ｇ又は無水硝酸ストロンチウム（Ｓｒ（ＮＯ3）2、ＭＷ＝２１１．６）６１５ｇに変えたこと以外は全て同様の調製方法により、Ｒｕ／ＣｅＯ2・Ａｌ2Ｏ3触媒（触媒番号３）及びＲｕ／ＳｒＯ・Ａｌ2Ｏ3触媒（触媒番号４）を調製した。
(Preparation of catalyst numbers 3 and 4)
For the preparation method of Catalyst No. 1, magnesium chloride is replaced with 1890 g of cerium nitrate (Ce (NO 3 ) 3 .6H 2 O, MW = 434.2) or anhydrous strontium nitrate (Sr (NO 3 ) 2 , MW = 211). .6) Ru / CeO 2 · Al 2 O 3 catalyst (Catalyst No. 3) and Ru / SrO · Al 2 O 3 catalyst (Catalyst No. 4) were prepared in the same manner except that the amount was changed to 615 g. .
（触媒番号比較１の調製）
無水炭酸ナトリウム（Ｎａ2ＣＯ3、ＭＷ＝１０６）１８５０ｇをイオン交換水１００Ｌに溶かし、これに無水塩化アルミニウム（ＡｌＣｌ3、ＭＷ＝１３３．３）１１６０ｇを加えた。これにより得られた沈殿物を十分に水洗し、１２０℃で乾燥した後、１１００℃で５ｈ焼成した。これにより得られたα−Ａｌ2Ｏ3粉末１ｋｇを直径約３ｍｍの粒状に成型した。さらにこれを、塩化マグネシウム６水和物（ＭｇＣｌ2・６Ｈ2Ｏ、ＭＷ＝２０３．３）２２０ｇをイオン交換水１．５Ｌに溶解させた水溶液に浸漬させ、加熱により水分を蒸発させた後、１１００℃で５ｈ焼成した。これにより得られた酸化アルミニウムと酸化マグネシウムの複合酸化物（ＭｇＯ／α−Ａｌ2Ｏ3）を直径約３ｍｍの粒状に成型して担体を調製した。
(Preparation of catalyst number comparison 1)
1850 g of anhydrous sodium carbonate (Na 2 CO 3 , MW = 106) was dissolved in 100 L of ion-exchanged water, and 1160 g of anhydrous aluminum chloride (AlCl 3 , MW = 133.3) was added thereto. The precipitate thus obtained was sufficiently washed with water, dried at 120 ° C., and calcined at 1100 ° C. for 5 hours. 1 kg of the α-Al 2 O 3 powder obtained in this way was molded into granules having a diameter of about 3 mm. Further, after immersing 220 g of magnesium chloride hexahydrate (MgCl 2 .6H 2 O, MW = 203.3) in 1.5 L of ion-exchanged water and evaporating the water by heating, Firing was performed at 1100 ° C. for 5 hours. The carrier was prepared by molding the composite oxide (MgO / α-Al 2 O 3 ) of aluminum oxide and magnesium oxide obtained in this manner into granules having a diameter of about 3 mm.
続いて、硝酸ニッケル６水和物（Ｎｉ（ＮＯ3）2・６Ｈ2Ｏ、ＭＷ＝２９０．８）５０ｇをイオン交換水０．５Ｌに溶解させた水溶液に、先に調製したＭｇＯ／α−Ａｌ2Ｏ3担体９０ｇを浸漬させ、加熱により水分を蒸発させた後、５００℃で５ｈ焼成した。これにより、Ｎｉを触媒全重量に対し１０ｗｔ％担持したＮｉ／ＭｇＯ／α−Ａｌ2Ｏ3触媒（触媒番号比較１）を得た。 Subsequently, the MgO / α- prepared above in an aqueous solution in which 50 g of nickel nitrate hexahydrate (Ni (NO 3 ) 2 .6H 2 O, MW = 290.8) was dissolved in 0.5 L of ion-exchanged water. After 90 g of Al 2 O 3 carrier was immersed and water was evaporated by heating, it was calcined at 500 ° C. for 5 hours. As a result, a Ni / MgO / α-Al 2 O 3 catalyst (catalyst number comparison 1) carrying 10 wt% of Ni with respect to the total weight of the catalyst was obtained.
（触媒番号比較２の調製）
無水炭酸ナトリウム（Ｎａ2ＣＯ3、ＭＷ＝１０６）１８５０ｇをイオン交換水１００Ｌに溶かし、これに無水塩化アルミニウム（ＡｌＣｌ3、ＭＷ＝１３３．３）１１６０ｇを加えた。これにより得られた沈殿物を十分に水洗し、１２０℃で乾燥した後、１１００℃で５ｈ焼成した。これにより得られたα−Ａｌ2Ｏ3粉末１ｋｇを直径約３ｍｍの粒状に成型して担体を調製した。
(Preparation of catalyst number comparison 2)
1850 g of anhydrous sodium carbonate (Na 2 CO 3 , MW = 106) was dissolved in 100 L of ion-exchanged water, and 1160 g of anhydrous aluminum chloride (AlCl 3 , MW = 133.3) was added thereto. The precipitate thus obtained was sufficiently washed with water, dried at 120 ° C., and calcined at 1100 ° C. for 5 hours. A carrier was prepared by molding 1 kg of the α-Al 2 O 3 powder thus obtained into granules having a diameter of about 3 mm.
続いて、５ｗｔ％の硝酸ルテニウム（Ｒｕ（ＮＯ3）4、ＭＷ＝３４９）水溶液１０Ｌに１Ｎのアンモニア水をｐＨ７．５になるまで添加し、黒色の水酸化ルテニウムを含むスラリーを調製した。先に調製したα−Ａｌ2Ｏ3粒状担体１００ｇにこの水酸化ルテニウムスラリーをＲｕ量換算で触媒全重量に対し２ｗｔ％量添加し、１２０℃で１２ｈ十分に乾燥させた後、さらに７００℃で２４ｈ焼成させた。これにより、Ｒｕを２ｗｔ％担持したＲｕ／α−Ａｌ2Ｏ3触媒（触媒番号比較２）を得た。 Subsequently, 1N ammonia water was added to 10 L of a 5 wt% aqueous solution of ruthenium nitrate (Ru (NO 3 ) 4 , MW = 349) until pH 7.5, thereby preparing a slurry containing black ruthenium hydroxide. The ruthenium hydroxide slurry was added to 100 g of the previously prepared α-Al 2 O 3 granular carrier in an amount of 2 wt% based on the total weight of the catalyst in terms of Ru amount, and after sufficiently drying at 120 ° C. for 12 hours, further at 700 ° C. Baked for 24 hours. As a result, a Ru / α-Al 2 O 3 catalyst (catalyst number comparison 2) carrying 2 wt% of Ru was obtained.
以上の触媒番号１〜４及び比較１〜２の触媒の組成及び調製方法を表１にまとめる。
（メタンの改質の性能評価）
触媒番号１〜４及び比較１〜２の各触媒を用いて、固定床流通式リアクタでメタンの改質反応を行った。反応条件を表２に示す。なお、試験番号１は、水蒸気と二酸化炭素によるメタンの改質反応であり、試験番号２及び３は、水蒸気のみによるメタンの改質反応である。
(Performance evaluation of methane reforming)
Using each of the catalysts Nos. 1 to 4 and Comparative Examples 1 and 2, the reforming reaction of methane was performed in a fixed bed flow type reactor. The reaction conditions are shown in Table 2. Test number 1 is a reforming reaction of methane with steam and carbon dioxide, and test numbers 2 and 3 are a reforming reaction of methane with only steam.
改質反応により生成したガスを分析し、以下の式４からメタン反応率（％）を算出した。改質反応の初期のメタン反応率と、５００時間経過後のメタン反応率を表３にまとめた。 The gas produced by the reforming reaction was analyzed, and the methane reaction rate (%) was calculated from the following formula 4. Table 3 shows the initial methane reaction rate of the reforming reaction and the methane reaction rate after 500 hours.
表３に示すように、水蒸気と二酸化炭素によるメタンの改質反応（試験番号１）では、触媒番号１〜４のいずれの触媒においてもメタン反応率は５００時間経過後でもほとんど低下せず、優れた耐久性を示した。一方、活性成分がＮｉである比較１と、担体が酸化アルミニウムのみの比較２では、メタン反応率が５００時間経過後で約３分の１程度まで低下した。また、比較１は、初期のメタン反応率も触媒番号１〜４の触媒の約８０％と低かった。 As shown in Table 3, in the reforming reaction of methane with water vapor and carbon dioxide (test number 1), the methane reaction rate hardly deteriorates even after 500 hours in any of the catalysts of catalyst numbers 1 to 4, and is excellent. Showed high durability. On the other hand, in Comparative 1 where the active ingredient is Ni and Comparative 2 where the support is only aluminum oxide, the methane reaction rate decreased to about one third after 500 hours. In comparison 1, the initial methane reaction rate was also as low as about 80% of the catalysts of catalyst numbers 1 to 4.
また、二酸化炭素を供給せず、水蒸気を上記と同じＳ／Ｃ比で供給した場合のメタンの改質反応（試験番号２）でも、触媒番号１〜４の各触媒は優れた耐久性を示したが、比較１及び２の各触媒はメタン反応率が約３分の１程度まで低下した。なお、二酸化炭素を供給せず、水蒸気を上記の２倍のＳ／Ｃ比で供給した場合のメタンの改質反応（試験番号３）では、比較１及び２の各触媒のメタン反応率は約３分の２程度までの低下となり、耐久性は向上した。 Also, in the methane reforming reaction (test number 2) when water vapor is supplied at the same S / C ratio as above without supplying carbon dioxide, each catalyst of catalyst numbers 1 to 4 exhibits excellent durability. However, each catalyst of Comparative 1 and 2 had a methane reaction rate reduced to about one third. In the methane reforming reaction (test number 3) when carbon dioxide is not supplied and water vapor is supplied at twice the above S / C ratio, the methane reaction rate of each catalyst of Comparative 1 and 2 is about The durability decreased to about two-thirds and the durability was improved.
上記の各試験において、５００時間経過後の触媒番号１〜４及び比較１及び２の各触媒に付着した炭素（Ｃ）の量を測定した。その結果を表４に示す。触媒番号１〜４のいずれの触媒においても炭素析出量は、触媒全体の重量に対して僅かであったが、比較１及び２の各触媒ではこの数倍以上の炭素が付着していた。 In each of the above tests, the amount of carbon (C) adhering to each of the catalyst numbers 1 to 4 and Comparative 1 and 2 after 500 hours was measured. The results are shown in Table 4. In any of the catalysts Nos. 1 to 4, the carbon deposition amount was a little with respect to the weight of the whole catalyst, but in each of the catalysts of Comparative Examples 1 and 2, carbon several times or more adhered.
以上により、触媒番号１〜４の各触媒は、Ｓ／Ｃ比が低くても、触媒上への炭素析出量が非常に少なく、触媒活性の低下が起こらないので、メタンの改質反応を長期にわたって安定して維持できることが確認できた。 As described above, each catalyst of catalyst Nos. 1 to 4 has a very small amount of carbon deposited on the catalyst even when the S / C ratio is low, and the catalytic activity does not decrease. It was confirmed that it could be maintained stably over the entire period.
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