WO2012105355A1 - Production method for hydrogen gas - Google Patents
Production method for hydrogen gas Download PDFInfo
- Publication number
- WO2012105355A1 WO2012105355A1 PCT/JP2012/051351 JP2012051351W WO2012105355A1 WO 2012105355 A1 WO2012105355 A1 WO 2012105355A1 JP 2012051351 W JP2012051351 W JP 2012051351W WO 2012105355 A1 WO2012105355 A1 WO 2012105355A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- gas
- oxygen
- catalyst
- hydrogen gas
- containing gas
- Prior art date
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/323—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents
- C01B3/326—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents characterised by the catalyst
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/40—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts characterised by the catalyst
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/72—Copper
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/90—Regeneration or reactivation
- B01J23/94—Regeneration or reactivation of catalysts comprising metals, oxides or hydroxides of the iron group metals or copper
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/16—Reducing
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0244—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being an autothermal reforming step, e.g. secondary reforming processes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1041—Composition of the catalyst
- C01B2203/1076—Copper or zinc-based catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1217—Alcohols
- C01B2203/1223—Methanol
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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
- 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
Abstract
Description
CH3OH + 0.5O2 → CO2 + 2H2 (1)
で表されるように、メタノールが酸化し、水素ガスと二酸化炭素ガスが生成する。このメタノールの酸化反応は、発熱反応であるため、系内の温度が上昇する。 When methanol and water are brought into contact with an oxygen-containing gas, the formula (1):
CH 3 OH + 0.5O 2 → CO 2 + 2H 2 (1)
As shown, the methanol is oxidized to produce hydrogen gas and carbon dioxide gas. Since the methanol oxidation reaction is an exothermic reaction, the temperature in the system rises.
CH3OH → CO + 2H2 (2)
で表されるように、一酸化炭素ガスと水素ガスに分解したり、式(3):
CH3OH + H2O → CO2 + 3H2 (3)
で表されるように、二酸化炭素ガスと水素ガスに分解したりする。これらの分解反応は、いずれも吸熱反応であることから、前記酸化反応で発生した熱の一部が打ち消される。その結果、系内の温度は、前記酸化反応のみが起こる場合の温度と対比して、幾分かは低い温度となる。また、これらの反応以外にも、式(4):
CO + H2O → CO2 + H2 (4)
で表されるシフト反応が起こると考えられている。 Further, in parallel with the methanol oxidation reaction, a part of the methanol is represented by the formula (2) without involving oxygen gas:
CH 3 OH → CO + 2H 2 (2)
As expressed by carbon monoxide gas and hydrogen gas, or the formula (3):
CH 3 OH + H 2 O → CO 2 + 3H 2 (3)
As shown, it decomposes into carbon dioxide gas and hydrogen gas. Since these decomposition reactions are endothermic reactions, part of the heat generated by the oxidation reaction is canceled out. As a result, the temperature in the system is somewhat lower than the temperature when only the oxidation reaction occurs. In addition to these reactions, the formula (4):
CO + H 2 O → CO 2 + H 2 (4)
It is believed that a shift reaction represented by
〔酸素ガス停止時間の比率〕
=〔(酸素ガスの供給を停止する時間)÷(1周期に要する時間)〕×100 (I)
で表される酸素ガス停止時間の比率は、酸化銅/酸化アルミニウム触媒の触媒活性を充分に回復させるとともに水素ガスを効率よく製造する観点から、30%以下であることが好ましい。例えば、前記1周期に要する時間を10秒間としたとき、酸素含有ガスを供給する時間が7秒間以上であり、酸素含有ガスの供給を停止する時間が3秒間以下であることが好ましい。 The time for stopping the supply of the oxygen-containing gas with respect to the time required for one cycle from the start of the supply of the oxygen-containing gas to the start of the supply of the next oxygen-containing gas after the supply of the oxygen-containing gas is stopped The ratio of formula (I):
[Ratio of oxygen gas stop time]
= [(Time for stopping supply of oxygen gas) ÷ (Time required for one cycle)] × 100 (I)
Is preferably 30% or less from the viewpoint of sufficiently recovering the catalytic activity of the copper oxide / aluminum oxide catalyst and efficiently producing hydrogen gas. For example, when the time required for one cycle is 10 seconds, the time for supplying the oxygen-containing gas is preferably 7 seconds or more, and the time for stopping the supply of the oxygen-containing gas is preferably 3 seconds or less.
長さ20cm、内径2.3cmの反応器内に、酸化銅/酸化アルミニウム触媒[アルドリッチ社製、酸化銅(CuO)と酸化アルミニウム(Al2O3)との質量比〔酸化銅(CuO)/酸化アルミニウム(Al2O3)〕:12/88]を充填した後、水素ガスを含む窒素ガスを約10時間反応器内に導入することにより、酸化銅/酸化アルミニウム触媒を賦活させた。 Example 1
In a reactor having a length of 20 cm and an inner diameter of 2.3 cm, a copper oxide / aluminum oxide catalyst [manufactured by Aldrich, mass ratio of copper oxide (CuO) and aluminum oxide (Al 2 O 3 ) [copper oxide (CuO) / After filling with aluminum oxide (Al 2 O 3 )]: 12/88], a nitrogen gas containing hydrogen gas was introduced into the reactor for about 10 hours to activate the copper oxide / aluminum oxide catalyst.
実施例1において、空気を標準状態で2.2L/分の流量で10分間通気した後、当該空気の通気を60秒間停止する操作を1周期として周期的に繰り返したこと以外は、実施例1と同様の操作を行なった。そのとき、式(I)で表される酸素ガス停止時間の比率は、約9%であった。
その結果を表2に示す。 Example 2
In Example 1, except that air was aerated at a flow rate of 2.2 L / min for 10 minutes in a standard state, and then the operation of stopping the ventilation of the air for 60 seconds was periodically repeated as one cycle. The same operation was performed. At that time, the ratio of the oxygen gas stop time represented by the formula (I) was about 9%.
The results are shown in Table 2.
実施例1において、空気を標準状態で2.0L/分の一定流量で供給したこと以外は、実施例1と同様にして反応を行なった。その結果を表3に示す。 Comparative Example 1
In Example 1, the reaction was performed in the same manner as in Example 1 except that air was supplied at a constant flow rate of 2.0 L / min in the standard state. The results are shown in Table 3.
Claims (5)
- 酸素含有ガスを供給しながら触媒の存在下でメタノールと水を接触させることによって反応ガスを製造し、当該反応ガスから水素ガスを分離することによって水素ガスを製造する方法であって、前記触媒として酸化銅/酸化アルミニウム触媒を用い、酸素含有ガスの供給を一時的に停止することを特徴とする水素ガスの製造方法。 A method of producing hydrogen gas by contacting methanol and water in the presence of a catalyst while supplying an oxygen-containing gas, and producing hydrogen gas by separating the hydrogen gas from the reaction gas, A method for producing hydrogen gas, characterized in that the supply of oxygen-containing gas is temporarily stopped using a copper oxide / aluminum oxide catalyst.
- 酸化銅/酸化アルミニウム触媒をあらかじめ還元させた後に使用する請求項1に記載の水素ガスの製造方法。 The method for producing hydrogen gas according to claim 1, wherein the copper oxide / aluminum oxide catalyst is used after being reduced in advance.
- 酸素含有ガスの供給の開始から当該酸素含有ガスの供給の停止に至るまでの時間を10秒~10分間に制御する請求項1または2に記載の水素ガスの製造方法。 3. The method for producing hydrogen gas according to claim 1, wherein the time from the start of the supply of the oxygen-containing gas to the stop of the supply of the oxygen-containing gas is controlled to 10 seconds to 10 minutes.
- 酸素含有ガスの供給を停止させる時間が3~60秒間である請求項1~3のいずれかに記載の水素ガスの製造方法。 4. The method for producing hydrogen gas according to claim 1, wherein the supply of the oxygen-containing gas is stopped for 3 to 60 seconds.
- 酸素含有ガスの供給を開始する時点から、当該酸素含有ガスの供給を停止させた後、次の酸素含有ガスの供給を開始するまでの1周期に要する時間に対する酸素含有ガスの供給を停止させる時間の比率が30%以下である請求項1~4のいずれかに記載の水素ガスの製造方法。 The time for stopping the supply of the oxygen-containing gas with respect to the time required for one cycle from the start of the supply of the oxygen-containing gas to the start of the supply of the next oxygen-containing gas after the supply of the oxygen-containing gas is stopped The method for producing hydrogen gas according to any one of claims 1 to 4, wherein the ratio of is not more than 30%.
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
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KR1020137022961A KR101869580B1 (en) | 2011-01-31 | 2012-01-23 | Production method for hydrogen gas |
JP2012555801A JP6168775B2 (en) | 2011-01-31 | 2012-01-23 | Method for producing hydrogen gas |
Applications Claiming Priority (2)
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JP2011-017867 | 2011-01-31 | ||
JP2011017867 | 2011-01-31 |
Publications (1)
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WO2012105355A1 true WO2012105355A1 (en) | 2012-08-09 |
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PCT/JP2012/051351 WO2012105355A1 (en) | 2011-01-31 | 2012-01-23 | Production method for hydrogen gas |
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JP (2) | JP6168775B2 (en) |
KR (1) | KR101869580B1 (en) |
TW (1) | TWI511920B (en) |
WO (1) | WO2012105355A1 (en) |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6236001A (en) * | 1985-08-07 | 1987-02-17 | Mitsubishi Heavy Ind Ltd | Reforming method for methanol |
JPH04200640A (en) * | 1990-05-25 | 1992-07-21 | Agency Of Ind Science & Technol | Reproduction of methanol reforming catalyst |
JP2001226103A (en) * | 2000-02-18 | 2001-08-21 | Nissan Motor Co Ltd | Fuel reforming device |
JP2005342543A (en) * | 2003-05-20 | 2005-12-15 | Idemitsu Kosan Co Ltd | Oxygen-containing hydrocarbon reforming catalyst, process for producing hydrogen or synthesis gas by using the same and fuel cell system |
WO2009107592A1 (en) * | 2008-02-25 | 2009-09-03 | 住友精化株式会社 | Process and apparatus for production of hydrogen |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE60017611T2 (en) * | 2000-06-22 | 2005-12-22 | Consejo Superior de Investigaciónes Científicas | METHOD FOR PRODUCING HYDROGEN BY PARTIAL METHANOLOXYDATION |
TW200836836A (en) * | 2007-03-12 | 2008-09-16 | Univ Nat Central | Hydrogen production via partial oxidation of methanol over Au/Al2O3-CuO catalysts |
-
2012
- 2012-01-23 WO PCT/JP2012/051351 patent/WO2012105355A1/en active Application Filing
- 2012-01-23 KR KR1020137022961A patent/KR101869580B1/en active IP Right Grant
- 2012-01-23 JP JP2012555801A patent/JP6168775B2/en active Active
- 2012-01-31 TW TW101103090A patent/TWI511920B/en active
-
2016
- 2016-08-31 JP JP2016169920A patent/JP2016196410A/en not_active Withdrawn
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6236001A (en) * | 1985-08-07 | 1987-02-17 | Mitsubishi Heavy Ind Ltd | Reforming method for methanol |
JPH04200640A (en) * | 1990-05-25 | 1992-07-21 | Agency Of Ind Science & Technol | Reproduction of methanol reforming catalyst |
JP2001226103A (en) * | 2000-02-18 | 2001-08-21 | Nissan Motor Co Ltd | Fuel reforming device |
JP2005342543A (en) * | 2003-05-20 | 2005-12-15 | Idemitsu Kosan Co Ltd | Oxygen-containing hydrocarbon reforming catalyst, process for producing hydrogen or synthesis gas by using the same and fuel cell system |
WO2009107592A1 (en) * | 2008-02-25 | 2009-09-03 | 住友精化株式会社 | Process and apparatus for production of hydrogen |
Also Published As
Publication number | Publication date |
---|---|
JP6168775B2 (en) | 2017-07-26 |
TW201245037A (en) | 2012-11-16 |
JPWO2012105355A1 (en) | 2014-07-03 |
KR20140023895A (en) | 2014-02-27 |
TWI511920B (en) | 2015-12-11 |
JP2016196410A (en) | 2016-11-24 |
KR101869580B1 (en) | 2018-06-20 |
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