WO2005085127A1 - 水素の製造方法およびそのためのシステム - Google Patents
水素の製造方法およびそのためのシステム Download PDFInfo
- Publication number
- WO2005085127A1 WO2005085127A1 PCT/JP2005/004397 JP2005004397W WO2005085127A1 WO 2005085127 A1 WO2005085127 A1 WO 2005085127A1 JP 2005004397 W JP2005004397 W JP 2005004397W WO 2005085127 A1 WO2005085127 A1 WO 2005085127A1
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- WO
- WIPO (PCT)
- Prior art keywords
- hydrogen
- membrane
- reaction
- catalyst
- separation membrane
- Prior art date
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- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 403
- 239000001257 hydrogen Substances 0.000 title claims abstract description 403
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 317
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 66
- 239000012528 membrane Substances 0.000 claims abstract description 209
- 238000000926 separation method Methods 0.000 claims abstract description 116
- 238000006243 chemical reaction Methods 0.000 claims abstract description 114
- 239000003054 catalyst Substances 0.000 claims abstract description 94
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 91
- 238000006356 dehydrogenation reaction Methods 0.000 claims abstract description 67
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 57
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 57
- 229910052751 metal Inorganic materials 0.000 claims abstract description 47
- 239000002184 metal Substances 0.000 claims abstract description 47
- 238000000034 method Methods 0.000 claims abstract description 42
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 37
- 125000000113 cyclohexyl group Chemical group [H]C1([H])C([H])([H])C([H])([H])C([H])(*)C([H])([H])C1([H])[H] 0.000 claims abstract description 23
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 19
- 229910044991 metal oxide Inorganic materials 0.000 claims abstract description 16
- 150000004706 metal oxides Chemical class 0.000 claims abstract description 16
- 229910045601 alloy Inorganic materials 0.000 claims description 75
- 239000000956 alloy Substances 0.000 claims description 75
- 238000003860 storage Methods 0.000 claims description 58
- 239000012466 permeate Substances 0.000 claims description 35
- UAEPNZWRGJTJPN-UHFFFAOYSA-N methylcyclohexane Chemical compound CC1CCCCC1 UAEPNZWRGJTJPN-UHFFFAOYSA-N 0.000 claims description 22
- 239000000919 ceramic Substances 0.000 claims description 16
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 15
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 14
- GYNNXHKOJHMOHS-UHFFFAOYSA-N methyl-cycloheptane Natural products CC1CCCCCC1 GYNNXHKOJHMOHS-UHFFFAOYSA-N 0.000 claims description 11
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical group CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims description 5
- 125000004122 cyclic group Chemical group 0.000 claims 1
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- 238000011084 recovery Methods 0.000 description 26
- 239000007789 gas Substances 0.000 description 25
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 23
- 239000000758 substrate Substances 0.000 description 17
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 14
- 238000010438 heat treatment Methods 0.000 description 14
- 239000007795 chemical reaction product Substances 0.000 description 13
- 239000000126 substance Substances 0.000 description 13
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 10
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- 229910052763 palladium Inorganic materials 0.000 description 9
- 230000000052 comparative effect Effects 0.000 description 8
- 230000000694 effects Effects 0.000 description 8
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- 239000000047 product Substances 0.000 description 7
- 239000000377 silicon dioxide Substances 0.000 description 7
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 7
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 6
- 101001012040 Pseudomonas aeruginosa (strain ATCC 15692 / DSM 22644 / CIP 104116 / JCM 14847 / LMG 12228 / 1C / PRS 101 / PAO1) Immunomodulating metalloprotease Proteins 0.000 description 6
- 230000005540 biological transmission Effects 0.000 description 6
- CXWXQJXEFPUFDZ-UHFFFAOYSA-N tetralin Chemical group C1=CC=C2CCCCC2=C1 CXWXQJXEFPUFDZ-UHFFFAOYSA-N 0.000 description 6
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- 239000010949 copper Substances 0.000 description 5
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- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 3
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- 125000000217 alkyl group Chemical group 0.000 description 3
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- NNBZCPXTIHJBJL-UHFFFAOYSA-N decalin Chemical group C1CCCC2CCCCC21 NNBZCPXTIHJBJL-UHFFFAOYSA-N 0.000 description 3
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- 229910052736 halogen Inorganic materials 0.000 description 2
- 150000002367 halogens Chemical class 0.000 description 2
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- 229910052758 niobium Inorganic materials 0.000 description 2
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- 238000002360 preparation method Methods 0.000 description 2
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- 229910052761 rare earth metal Inorganic materials 0.000 description 2
- 229910052702 rhenium Inorganic materials 0.000 description 2
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- 238000007086 side reaction Methods 0.000 description 2
- 238000000629 steam reforming Methods 0.000 description 2
- 229910052719 titanium Inorganic materials 0.000 description 2
- 229910052720 vanadium Inorganic materials 0.000 description 2
- PXXNTAGJWPJAGM-UHFFFAOYSA-N vertaline Chemical group C1C2C=3C=C(OC)C(OC)=CC=3OC(C=C3)=CC=C3CCC(=O)OC1CC1N2CCCC1 PXXNTAGJWPJAGM-UHFFFAOYSA-N 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- NHCREQREVZBOCH-UHFFFAOYSA-N 1-methyl-1,2,3,4,4a,5,6,7,8,8a-decahydronaphthalene Chemical class C1CCCC2C(C)CCCC21 NHCREQREVZBOCH-UHFFFAOYSA-N 0.000 description 1
- -1 B e 2 T i Inorganic materials 0.000 description 1
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- 229910000861 Mg alloy Inorganic materials 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
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Classifications
-
- 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
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
- C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
- C01B3/26—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons using catalysts
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
- B01D53/228—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion characterised by specific membranes
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- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01D—SEPARATION
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
- B01D63/06—Tubular membrane modules
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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
- C01B3/0005—Reversible uptake of hydrogen by an appropriate medium, i.e. based on physical or chemical sorption phenomena or on reversible chemical reactions, e.g. for hydrogen storage purposes ; Reversible gettering of hydrogen; Reversible uptake of hydrogen by electrodes
- C01B3/001—Reversible uptake of hydrogen by an appropriate medium, i.e. based on physical or chemical sorption phenomena or on reversible chemical reactions, e.g. for hydrogen storage purposes ; Reversible gettering of hydrogen; Reversible uptake of hydrogen by electrodes characterised by the uptaking medium; Treatment thereof
- C01B3/0031—Intermetallic compounds; Metal alloys; Treatment thereof
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/367—Formation of an aromatic six-membered ring from an existing six-membered ring, e.g. dehydrogenation of ethylcyclohexane to ethylbenzene
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/144—Purification; Separation; Use of additives using membranes, e.g. selective permeation
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- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/42—Platinum
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- 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
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/48—Silver or gold
- B01J23/50—Silver
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- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0215—Coating
- B01J37/0225—Coating of metal substrates
- B01J37/0226—Oxidation of the substrate, e.g. anodisation
-
- 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
- C01B2203/0266—Processes for making hydrogen or synthesis gas containing a decomposition step
- C01B2203/0277—Processes for making hydrogen or synthesis gas containing a decomposition step containing a catalytic decomposition step
-
- 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
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0405—Purification by membrane separation
- C01B2203/041—In-situ membrane purification during hydrogen production
-
- 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
- C01B2203/1235—Hydrocarbons
- C01B2203/1252—Cyclic or aromatic hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
- C07C2521/02—Boron or aluminium; Oxides or hydroxides thereof
- C07C2521/04—Alumina
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
- C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
- C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
- C07C2523/42—Platinum
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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
- Y02E60/32—Hydrogen storage
Definitions
- the present invention relates to a method and a system for producing hydrogen in a field of hydrogen production, in which hydrogen is generated by a dehydrogenation reaction of a feedstock composed of a hydrocarbon, for example, a feedstock composed mainly of a hydrocarbon having a cyclohexane ring. is there.
- the present invention provides a membrane-type reactor having a hydrogen separation membrane therein, and when performing a dehydration reaction of a raw material oil composed of hydrocarbons, for example, a hydrocarbon having mainly a cyclohexane ring, a hydrogen storage alloy is used.
- the present invention relates to a method for producing hydrogen, characterized in that the pressure on the permeate side is made lower than that on the non-permeate side of the membrane, thereby improving the hydrogen recovery rate, and to a hydrogen production system used for this method.
- Hydrogen is widely used in all industrial fields, including petroleum refining and the chemical industry.
- hydrogen energy has been attracting attention as a future energy, and research has been progressing mainly on fuel cells.
- hydrogen gas has a large volume per calorific value, and the energy required for liquefaction is large.
- Storage and transportation systems are an important issue.
- new infrastructure needs to be provided for hydrogen supply (see Non-Patent Document 1).
- liquid hydrocarbons have a higher energy density than hydrogen gas, are easier to handle, and have the advantage that existing infrastructure can be used. It is important to produce hydrogen from hydrocarbons as needed.
- aromatic hydrocarbons can be liquefied and separated from hydrogen by lowering the temperature of the generated hydrogen and aromatic hydrocarbons to room temperature under atmospheric pressure, but the amount of aromatics depends on the vapor pressure at room temperature.
- Group hydrocarbons are mixed into hydrogen gas. For example, in the case of toluene, it is 15 and under atmospheric pressure, about 2.1% is mixed. Therefore, when it is necessary to increase the purity of hydrogen, such as in fuel cell applications, a problem arises in the separation of hydrogen and aromatic hydrocarbons.
- a method of separation there is a method of separation by cooling, but in order to achieve a hydrogen concentration of 99.9% or more, a low temperature of about 130 at normal pressure is required. Cooling to 130 ° C using a refrigerator is not a preferable removal method because it causes a decrease in energy efficiency and increases equipment in hydrogen production.
- adsorption separation method in which an adsorbent adsorbs and separates.
- the PSA method pressure swing adsorption method
- the recovery rate of hydrogen gas and the overall efficiency are low, and the pressure and pressure are reduced. Operation required and system There is a drawback that the system becomes large.
- Separation methods other than the above include a membrane separation method.
- the membrane separation method is characterized by high energy efficiency, and the main types of separation membranes are palladium membranes, polymer membranes, ceramic membranes, and carbon membranes.
- palladium membranes have been put to practical use for the purpose of high-purity hydrogen purification (see Non-Patent Document 3).
- the dehydrogenation reaction of a hydrocarbon having a cyclohexane ring mainly needs to be performed at a lower temperature in order to suppress a decomposition reaction which is a side reaction.
- a decomposition reaction which is a side reaction.
- a membrane reactor incorporating a hydrogen separation membrane is used to selectively remove hydrogen generated in the dehydrogenation process from the reaction field, thereby achieving an improvement in hydrogen yield and a lower reaction temperature.
- Patent Document 1 discloses a technique of incorporating a porous ceramic membrane that selectively permeates hydrogen and performing a dehydrogenation reaction of cyclohexane.
- Patent Documents 2 and 3 disclose hydrogen production technology by reaction separation using a palladium membrane.
- Dehydrogenation of the cyclohexane ring is a large endothermic reaction.
- the reaction enthalpy for dehydrogenation of cyclohexane is 50 kca 1 / mo 1, and even for a hydrocarbon having a substituent, the reaction enthalpy per cyclohexane ring is almost the same.
- Ordinary solid catalyst with active metal supported on oxide granules, pellets, extruded products, etc.
- Patent Document 4 discloses a method for steam reforming methanol characterized by using a thermally conductive catalyst in which an ultrafine catalyst material is supported on the surface of a continuous metal substrate. It discloses that hydrogen and carbon monoxide can be obtained in high yield.
- the methanol reforming reaction has a drawback that it involves many steps as a small-scale hydrogen production method.
- Non-Patent Document 1 Nori Kobayashi, Quarterly Energy Engineering, Vol. 25, No. 4, pp. 73-87 (2003)
- Non-Patent Document 2 Masaru Takakawa, Industrial Materials, Vol. 51, No. 4, pp. 62-69 (2003)
- Non-Patent Document 3 Supervised by Masayuki Nakagaki, Membrane Processing Technology System (1st volume), Fuji, Techno System, pp. 61-662 and pp. 922-925 (11991)
- Patent Document 1 Japanese Patent Application Laid-Open No. 7-171638
- Patent Literature 2 Japanese Patent Application Laid-Open No. 3-212172
- Patent Document 3 Japanese Patent Application Laid-Open No. Hei 5-3-171708
- Patent Document 4 Japanese Patent Application Laid-Open No. 5-116901 discloses the invention
- An object of the present invention in the first embodiment is to separate, lower the temperature, supply heat, etc. in a method for producing hydrogen by a dehydrogenation reaction of a feedstock made of a hydrocarbon, for example, a feedstock mainly made of a hydrocarbon having a cyclohexane ring. It is an object of the present invention to provide a hydrogen production method and a hydrogen production system for efficiently producing hydrogen by solving the above problems.
- the present inventors have conducted intensive studies to solve the above-mentioned problems, and as a result, when generating hydrogen by the dehydrogenation reaction of hydrocarbon, the metal on the surface of the heat conductive support was Using a membrane reactor that can selectively remove hydrogen with a catalyst supporting an active metal on the oxide layer, and further optimizing the reaction conditions, we found a method for efficiently producing hydrogen. Things.
- a membrane-type reactor capable of selectively removing hydrogen is used when generating hydrogen by a hydrocarbon dehydration reaction, and furthermore, hydrogen is provided on the permeate side thereof.
- the first aspect of the present invention in the first aspect is that a metal oxide layer is unevenly distributed on a surface of a carrier made of a heat conductive support made of metal, and a catalyst supported on a carrier is present in a flow-type reaction tube.
- a dehydrogenation reaction system for producing a hydrogen and an aromatic hydrocarbon by dehydrogenating a hydrocarbon having a cyclohexane ring In a dehydrogenation reaction system for producing a hydrogen and an aromatic hydrocarbon by dehydrogenating a hydrocarbon having a cyclohexane ring,
- a hydrogen production method characterized in that hydrogen is mainly removed on the permeation side by the hydrogen separation membrane while the dehydrogenation reaction is proceeding, and aromatic hydrocarbon is mainly obtained on the non-permeation side.
- the catalyst uses a metal support, it is easy to control the heat of dehydrogenation, and it is a simple device because it simultaneously performs dehydrogenation and hydrogen separation.
- a second aspect of the present invention in the first aspect is the first aspect of the present invention, wherein the hydrocarbon having a cyclohexane ring contains methylcyclohexane, and toluene generated by dehydrogenation is separated. This is a method for producing hydrogen.
- a third aspect of the present invention in the first aspect is the method for producing hydrogen according to the first or second aspect of the present invention, wherein the hydrogen separation membrane is a ceramic membrane.
- the hydrogen separation membrane is a ceramic membrane.
- hydrocarbon separation is easy with ceramic membrane separation.
- a fourth aspect of the present invention in the first aspect is the first to third aspects of the present invention, wherein the hydrogen separation membrane is a metal membrane containing 100 to 100 mass% of Pd. It is a manufacturing method. Hydrocarbons can be easily separated by such metal film separation.
- a fifth aspect of the present invention according to the first aspect is the method for producing hydrogen according to any one of the first to fourth aspects of the present invention, wherein the carrier in the catalyst is a carrier containing alumina.
- the carrier is advantageous for heat conduction.
- a sixth aspect of the present invention according to the first aspect is the first to fifth aspects of the present invention, wherein the reaction tube has a double-tube structure, an outer tube is a metal heat conductive support, and The inner tubes are each composed of a hydrogen separation membrane,
- the gap between the double tubes is provided with a plurality of metal and heat conductive fin-shaped protrusions which are long in the flow direction and extend from the outer tube toward the inside,
- the above-mentioned double tube with internal fins is convenient because it has excellent thermal efficiency of dehydrogenation and can simultaneously perform dehydration and membrane separation.
- the seventh aspect of the present invention in the first aspect is a double-tube flow-type reaction tube, in which the outer tube is a heat conductive support made of metal, and the inner tube is formed of a hydrogen separation membrane.
- the gap between the double pipes is provided with a plurality of metal- and heat-conductive fin-shaped protrusions which are long in the flow direction and extend from the outer pipe toward the inside of the pipe.
- At least the metal oxide layer is unevenly distributed on the surface of the fin-like projections to support the catalyst
- An eighth aspect of the present invention in the first aspect is that, in a reaction system for producing hydrogen and a reaction product by reacting hydrocarbons in a flow-type reaction tube, a hydrogen removing means by a hydrogen separation membrane is provided inside the reaction system,
- a method for producing hydrogen in which hydrogen is mainly removed on the permeation side of the membrane by the hydrogen separation membrane, and the reaction product is mainly obtained on the non-permeation side of the membrane A method for producing hydrogen, characterized by lowering the partial pressure of hydrogen on the permeate side by flowing steam on the permeate side of the membrane.
- a ninth aspect of the present invention according to the first aspect is that, in a reaction system for producing hydrogen and a reaction product by reacting hydrocarbons in a catalyst layer in a flow-type reaction tube, hydrogen removal means by a hydrogen separation membrane is provided inside the reaction system,
- a method for producing hydrogen in which hydrogen is mainly removed on the permeation side of the membrane by the hydrogen separation membrane, and the reaction product is mainly obtained on the non-permeation side of the membrane,
- reaction pressure is 0.4 MPa or more in absolute pressure
- permeation pressure of the hydrogen separation membrane is 0.12 MPa or less in absolute pressure
- catalyst layer outlet temperature is in the range of 300 ° C or more and 360 ° C or less.
- the hydrogen recovery can be made 80% or more.
- a tenth aspect of the present invention in the first aspect is that a hydrogen removing means using a hydrogen separation membrane is provided in a reaction system for producing hydrogen and a reaction product by reacting hydrocarbons in a catalyst layer in a flow-type reaction tube. Indwelling,
- a method for producing hydrogen in which hydrogen is mainly removed on the permeation side of the membrane by the hydrogen separation membrane, and the reaction product is mainly obtained on the non-permeation side of the membrane,
- the reaction pressure is 0.4 MPa or more in absolute pressure
- the pressure on the permeate side of the hydrogen separation membrane is 0.12 MPa or less in absolute pressure
- the flow of water vapor on the permeate side of the hydrogen separation membrane makes the hydrogen partial pressure on the permeate outlet absolute.
- the hydrogen recovery can be made 80% or more.
- the eleventh aspect of the present invention according to the first aspect is that the catalyst layer in the flow-type reaction tube contains hydrocarbons.
- the hydrogen separation membrane mainly removes hydrogen on the permeation side of the membrane, and mainly obtains a reaction product on the non-permeation side of the membrane.
- the reaction pressure is 0.2 MPa or more in absolute pressure
- the permeate pressure of the hydrogen separation membrane is 0.12 MPa or less in absolute pressure
- the flow of steam to the permeate side of the hydrogen separation membrane reduces the partial pressure of hydrogen at the permeate outlet.
- the hydrogen recovery can be made 80% or more.
- the first aspect of the present invention in the second aspect is that, while a hydrocarbon is subjected to a dehydrogenation reaction in a flow-type reaction system provided with a dehydrogenation catalyst and a hydrogen separation membrane, the produced hydrogen is continuously fed through the hydrogen separation membrane. Hydrogen permeating and separating at least a part of the obtained hydrogen flow into a hydrogen storage alloy so that the pressure of the hydrogen permeation side of the hydrogen separation membrane is lower than the pressure of the non-permeation side. Is a manufacturing method.
- a second aspect of the present invention according to the second aspect relates to the method for producing hydrogen according to the first aspect of the present invention, wherein the hydrocarbon comprises a hydrocarbon having a cyclohexane ring. It is.
- a third aspect of the present invention in the second aspect relates to the method for producing hydrogen according to the second aspect of the present invention in the second aspect, wherein the hydrocarbon having a cyclohexane ring is methylcyclohexane. Things.
- a fourth aspect of the present invention in the second aspect relates to the method for producing hydrogen according to any one of the first to third aspects of the present invention in the second aspect, wherein the hydrogen separation membrane is a ceramic membrane.
- a fifth aspect of the present invention in the second aspect is the first to fourth aspects of the present invention in the second aspect, wherein the hydrogen separation membrane is a metal membrane containing 100 to 10 mass% of Pd.
- the present invention relates to a method for producing hydrogen.
- a sixth aspect of the present invention in the second aspect is that the sixth aspect has two or more flow-type membrane reactors, two or more hydrogen storage alloy units, a cooler, a flow path connecting these, and a flow path switching means.
- the present invention relates to a hydrogen production system for carrying out the hydrogen production methods according to the first to fifth aspects of the present invention, characterized in that hydrogen is absorbed and released in a hydrogen storage alloy unit by selectively switching channels. It is.
- a seventh aspect of the present invention in the second aspect is the sixth aspect of the present invention in the second aspect, wherein two or more flow-type membrane reactors, two or more hydrogen storage alloy units, and a cooler are connected.
- a flow path and a flow path switching means wherein the flow path switching means cools a permeated hydrogen flow from one flow-type membrane reactor by a cooler and stores the permeated hydrogen flow in one hydrogen storage alloy unit.
- the present invention relates to a hydrogen production system characterized by obtaining hydrogen from a membrane reactor and hydrogen released from the hydrogen storage alloy.
- the effects of the invention in the first embodiment are as follows. That is, when generating hydrogen from a hydrocarbon having a cyclohexane ring mainly by a dehydrogenation reaction, a catalyst supporting an active metal is placed on a metal oxide layer on the surface of the heat conductive support, and the hydrogen is generated. According to the method of the present invention, which uses a membrane reactor capable of selectively removing hydrogen, hydrogen can be efficiently produced within a range of optimized reaction conditions.
- FIG. 1 is a perspective view of the internal fin type membrane reactor in the first embodiment, and a cross-sectional view thereof is shown on the left side.
- the inner pipe is not shown in any case.
- FIG. 2 shows a conceptual diagram of the hydrogen production system of the present invention in the first embodiment.
- FIG. 3 is a schematic diagram of a membrane reactor used in Experimental Example 1 of the first embodiment and having a structure in which catalyst particles are filled in gaps of a double tube structure in which an inner tube is formed of a hydrogen separation membrane.
- This figure is also a schematic cross-sectional view of the membrane reactor used in Examples 1 and 2 and Comparative Example in the second embodiment.
- FIG. 4 is a conceptual diagram of one embodiment of the hydrogen production system of the present invention in the second embodiment.
- FIG. 5 is a conceptual diagram of another embodiment of the hydrogen production system of the present invention in the second embodiment.
- FIG. 6 is a conceptual diagram of the operation in the first and second embodiments according to the second embodiment.
- membrane reactor In the present invention, a so-called membrane reactor is used.
- the membrane reactor referred to in the present invention more precisely,
- the hydrogen separation membrane constitutes the inner tube of the reaction tube, and the entire structure often has a double tube structure.
- the substrate is circulated from one side of the flow-type reaction tube, and the substrate present in the gap is dehydrogenated to generate hydrogen and a reaction product.
- the generated hydrogen is separated in-situ by the hydrogen separation membrane that constitutes the inner tube, and hydrogen is selectively permeated into the inner tube of the double tube.
- hydrogen is discharged out of the system, thereby obtaining high-purity hydrogen.
- a known method such as heating with a heating medium can be appropriately employed for the appropriate heating from the outside of the tube.
- a metal membrane or a porous inorganic membrane capable of selectively separating hydrogen from a mixed gas of hydrocarbon and hydrogen is preferable.
- a metal membrane it is a hydrogen separation membrane in which a metal thin film is formed on the inner surface or outer surface of a tubular porous metal support having pores or a tubular ceramic support having pores.
- any method can be selected for forming the metal thin film, specific examples include an electroless plating method, a vapor deposition method, and a rolling method.
- a porous inorganic membrane it is a hydrogen separation membrane in which a ceramic thin film having a controlled pore diameter is formed on the inner surface or the outer surface of a porous ceramic support having tubular pores. Since the porous inorganic membrane selectively separates by a molecular sieve action, the pore diameter of the thin film portion is preferably 0.3 nm or more and 0.7 nm or less, more preferably 0.3 nm or more and 0.5 nm or less.
- known ceramic materials can be used, but silica, alumina, titania, glass, silicon carbide, and silicon nitride are preferable.
- the main component of the catalytic activity in the dehydrogenation catalyst of the present invention is a component having dehydrogenation activity and can be arbitrarily selected, but is preferably a group VII, VIII or IB element in the periodic table.
- IB element in the periodic table.
- the preparation method for incorporating these catalytically active main components into the molded catalyst is optional, but an impregnation method is preferred. Specific examples include the incipient wetness method and the evaporation to dryness method.
- the compound of the element used is preferably a water-soluble salt, and may be impregnated as an aqueous solution. preferable. Preferred examples of the water-soluble compound include chlorides, nitrate
- additives may be added to the catalyst.
- Preferred additives include basic substances.
- the coexistence of the basic substance suppresses side reactions such as decomposition due to acidity, and also suppresses catalyst deterioration due to carbonaceous deposition.
- the type of the basic substance is arbitrary, but a compound of a group IA element and a group III element is preferable. Is preferred. As these compounds, water-soluble substances are preferred. Chloride, sulfate, nitrate and carbonate are more preferred.
- the content of the basic substance is preferably in the range of 0.1 to 100 in terms of weight ratio to the catalytically active main component.
- the preparation method for incorporating these basic substances into the catalyst body is optional, but an impregnation method is preferably used. Specific examples include the incipient wetness method and the evaporation to dryness method.
- a catalyst is used for dehydrogenation.
- the reaction of the catalyst of the present invention is preferably carried out using a solid catalyst having dehydrogenation activity.
- a solid catalyst having dehydrogenation activity.
- a catalyst in which a catalyst active main component is supported on a carrier can be suitably used.
- a catalyst supported on a conventionally known granular or pellet-shaped carrier can also be used.
- These conventional granular and pelletized catalysts can be used, for example, in such a form that they are simply filled in the gap between the double tubes.
- a stable metal oxide as the carrier because it has high mechanical strength, is thermally stable and has a large surface area. More preferably, a support in which a metal oxide is formed on the surface of a support having good thermal conductivity (a heat conductive support) is preferable.
- the metal oxide as the carrier include alumina, silica, titania, zirconia, and silica-alumina. More preferably, it is alumina, silica or a mixture thereof.
- the thermally conductive support is defined as a catalyst having a substrate having a thermal conductivity at 300 K of 10 W / m * K or more as a base.
- the substrate of the heat conductive catalyst is preferably a metal, and has a coating such as an oxide on its surface. Including those that do.
- the metal of the base any commonly used metal and alloy can be used, and particularly, aluminum and a metal and alloy having aluminum on the surface are preferable.
- the use of a metal as a base has the effect of increasing the thermal conductivity of the catalyst body, increasing the heat supply, and improving the reaction efficiency. That is, since the dehydrogenation reaction is an endothermic reaction, as described above, a double tube itself is used as a metal base and a metal tube is used, and heat is supplied from the outside of the double tube by an appropriate heating means. By applying heat to the dehydrogenation reaction in the pipe gap, it becomes easy to apply heat to the dehydrogenation reaction.
- reaction tube for example, and to significantly shorten the start-up time of the reaction apparatus by applying a current directly by utilizing the conductivity of the catalyst body as a metal.
- the surface of the metal substrate is preferably treated to have a high surface area so as to have a function as a carrier of the catalytically active main component.
- Known methods can be used for this treatment. For example, as described in Japanese Patent Application Laid-Open Publication No. 2002-119856, the surface area is increased based on the anodic oxidation treatment. Is preferred.
- an alumina hydrate sol can be applied to the surface of a substrate having a high surface, dried, and then fired to form a metal oxide layer.
- the shape of the catalyst carrier including the metal substrate is arbitrary, and may be plate-like, tubular, mesh-like, honeycomb-like, or fin-like protrusions directly installed inside the reaction tube.
- a catalyst is present in the gap between the double pipes, and the reaction in the gap is a dehydrogenation reaction and an endothermic reaction.
- the catalyst support are preferably in direct contact.
- the shape of the catalyst carrier be a plate-like, tubular, or internal fin directly in contact with the outer tube of the double tube, such as a heat exchanger having a large area in contact with the substrate. It is possible to increase the area in direct contact with the heating source and the substrate. Any shape can be used if desired.
- the inner fin type a structure in which the outer tube of the double tube structure is part of the metal substrate, and is provided with a plurality of fin-like protrusions that are long in the direction of substrate flow and extend from the outer tube toward the inner tube.
- a catalyst can be supported by forming a metal oxide layer on the fin surface.
- this metal substrate is made of a metal such as aluminum, and can have a high surface by the above-described method.
- the catalyst can be appropriately supported on a portion other than the fin, such as the inner surface of the outer tube, by the above-described method. Since the inner tube can be supported separately, a plurality of fins extending from the outer tube toward the inner tube may or may not contact the hydrogen separation membrane constituting the inner tube.
- FIG. 1 shows the outer tube of the double tube.
- an inner tube made of a hydrogen separation membrane is inserted inside and used for dehydrogenation.
- the plurality of fins may or may not contact the hydrogen separation membrane of the inner tube.
- the number of fins, their height, thickness, and the like can be appropriately selected as long as they are not limited by strength or the like.
- the fin shape is a plate shape that extends directly perpendicularly from the outer tube surface in FIG. 1, but it can have an opening or an appropriate shape to increase the surface area.
- Such an internal fin type is preferable because it can directly contact a heating source disposed outside the tube and has a large contact area with a substrate flowing through the gap, so that heating becomes easy.
- the catalyst does not necessarily need to be placed in contact with the hydrogen separation membrane. The point is that the hydrogen generated by the operation of the catalyst is immediately and simultaneously subjected to a hydrogen membrane separation operation in situ to transfer hydrogen to the outside of the dehydrogenation reaction system. It is important to selectively discharge.
- the raw material for dehydrogenation in the present invention is preferably a hydrocarbon, and more preferably a hydrocarbon having a cyclohexane ring.
- a hydrocarbon having a cyclohexane ring include cyclohexane and alkyl substituted cycline, decalin and alkyl substituted decalin, and tetralin and alkyl substituted tetralin.
- These hydrocarbons having a cyclohexane ring may be a mixture of a plurality of hydrocarbons. As long as the reaction is not hindered And may optionally contain other compounds such as hydrocarbons having no cyclohexane ring.
- the products of dehydrogenation are hydrogen and unsaturated hydrocarbons, and the unsaturated hydrocarbons are mainly aromatic hydrocarbons. These can be recovered and hydrogenated to convert them back into raw hydrocarbons. Alternatively, it can be used as a fuel of a heat source necessary for the dehydrogenation reaction, if necessary.
- aromatic hydrocarbons generally have a high octane number, substances having a suitable boiling point can be used as a gasoline base material. Alternatively, it can be used as a chemical product.
- Reaction conditions are appropriately selected according to the type of raw materials and the type of reaction.
- the reaction pressure is preferably not less than 0. IMPa and not more than 2.0 MPa, more preferably not less than 0. IMPa and not more than 1. OMPa.
- a pressure is shown by an absolute pressure unless there is particular notice.
- the reaction temperature is preferably high in terms of chemical equilibrium, but is preferably low in terms of energy efficiency.
- the preferred reaction temperature is from 200 ° C to 400 ° C, more preferably from 270 ° C to 360 ° C, most preferably from 220 ° C to 360 ° C.
- hydrogen may be added to the raw material for the purpose of preventing deactivation of the catalyst or for the operation of the apparatus. When hydrogen is added to the raw material, the molar ratio of hydrogen to the raw material is preferably 0.01 or more and 1 or less.
- LHSV liquid hourly space velocity
- Hydrogen generated by the dehydrogenation reaction is in a state of being mixed with reaction products such as aromatic hydrocarbons, but in the present invention, it is immediately subjected to a membrane separation operation using a hydrogen separation membrane in situ.
- the inner tube of the double tube is composed of a hydrogen separation membrane, operate the innermost part of the double tube as the hydrogen permeation side and the gap between the double tubes as the non-permeation side.
- the pressure on the permeation side of the hydrogen separation membrane in the membrane separation reactor is preferably 0.2 MPa or less, more preferably 0.12 MPa or less.
- an inert gas may be supplied for permeation of the hydrogen separation membrane in order to reduce the partial pressure of hydrogen on the permeation side.
- the hydrogen partial pressure on the permeation side is preferably 0.1 MPa or less, more preferably 0.05 MPa or less.
- the inert gas steam that can be easily separated by condensation is preferable.
- steam is more preferable for such a purpose because steam can be introduced without being removed. By adding steam to the permeate side, high-purity hydrogen can be produced even if the hydrogen partial pressure on the permeate side is 0.05 MPa or less.
- reaction conditions of the present invention using a membrane reactor are adopted, not only the inner fin type shown in FIG. 1 but also a simple catalyst-filled reaction tube shown in FIG. That is, a reaction tube in which a simple double-pipe gap is filled with a catalyst supported on a conventionally known granular or pellet-shaped carrier is used, and the hydrogen recovery rate in the membrane separation process is 80% or more. It is possible to achieve
- FIG. 2 shows a conceptual diagram of the hydrogen production system of the present invention as a first embodiment according to the above.
- a feedstock of a reaction substrate preferably a hydrocarbon containing a cyclohexane ring
- a membrane reactor preferably a hydrocarbon containing a cyclohexane ring
- the generated hydrogen is membrane-separated by a hydrogen separation membrane, and most of it is separated outside the system as a permeated gas, and becomes high-purity hydrogen, which is product hydrogen.
- Part of the remaining hydrogen and unsaturated hydrocarbons such as aromatic hydrocarbons are recovered as non-permeate gas.
- a so-called membrane reactor is used as the reactor used in the flow reaction system.
- the membrane reactor according to the present invention as the second embodiment is more precisely a flow-type reaction tube, comprising a dehydrogenation catalyst and a hydrogen separation membrane. Is provided in the reaction tube.
- the hydrogen separation membrane constitutes the inner tube of the reaction tube, and the catalyst often has a double tube structure in which the catalyst exists between the outer tube and the inner tube.
- the raw hydrocarbon is supplied and circulated from one of the flow-type reaction tubes, and the raw hydrocarbon is dehydrogenated by the catalyst present in the gap.
- Hydrogen and reaction products including dehydrogenated hydrocarbons, by-products, and unreacted hydrocarbons
- the generated hydrogen is simultaneously and in situ converted into a hydrogen separation membrane that constitutes the inner tube.
- hydrogen is selectively passed through the inner pipe of the double pipe to discharge hydrogen out of the system, thereby obtaining high-purity hydrogen.
- the generated hydrogen is quickly separated, and the gap between the double tubes where the endothermic dehydrogenation reaction is performed can be easily heated by providing an appropriate heating means from outside the tube. Is easily supplied and the dehydrogenation reaction proceeds easily.
- a known method such as heating with a heating medium can be appropriately employed for appropriate heating from the outside of the tube.
- a known hydrogen separation membrane having a function of selectively separating hydrogen from a mixed gas of hydrocarbon and hydrogen can be used, such as a metal membrane or a porous inorganic membrane. Is preferred.
- the hydrogen separation membrane or the like in the first embodiment can be used.
- the dehydrogenation reaction is performed using a catalyst.
- the catalyst is preferably a solid catalyst having dehydrogenation activity.
- a catalyst having a catalytically active main component supported on a carrier can be suitably used.
- the carrier Since the carrier has high mechanical strength, is thermally stable and has a large surface area, it is necessary to use a stable metal acid or metal oxide on the surface of a support with good thermal conductivity (heat conductive support). It is preferable to form a sword.
- the dehydrogenation catalyst does not necessarily need to be disposed in contact with the hydrogen separation membrane.
- the hydrogen generated by the action of the catalyst is immediately and simultaneously subjected to a hydrogen membrane separation operation in situ, It is important to selectively discharge hydrogen out of the dehydrogenation reaction system.
- the raw material for dehydrogenation in the present invention is preferably a hydrocarbon, and more preferably a hydrocarbon having a cyclohexane ring. Specifically, those exemplified in the first embodiment can be used.
- reaction conditions for dehydrogenation are appropriately selected according to the type of the raw material. Specifically, the reaction conditions described in the first embodiment can be exemplified.
- the hydrogen generated by the dehydrogenation reaction is in a state of being mixed with a reaction product such as an aromatic hydrocarbon.
- the hydrogen is immediately subjected to a membrane separation operation using a hydrogen separation membrane in situ.
- the membrane reactor which is a flow-type reactor to be used the side where hydrogen of the hydrogen separation membrane is separated and exits is the permeate side, and the opposite side is the It is called the non-transmission side.
- the flow-type reaction tube is a double tube and the inner tube is composed of a hydrogen separation membrane, operate the innermost part of the double tube as the hydrogen permeation side and the gap between the double tubes as the non-permeation side.
- FIG. 3 shown in the first embodiment, which is shown in FIG. Used in examples and comparative examples.
- the reaction tube 1 is a membrane reactor having a double tube structure
- the outer tube 3 is made of a material having good thermal conductivity, for example, metal, etc.
- the tube wall of the inner tube 4 has a hydrogen content. It consists of a release membrane (hydrogen permeable membrane 4).
- appropriate heating means such as heating with a heat medium are provided on the outside of the double tube.
- the gap between the double pipes, that is, the gap between the inner pipe and the outer pipe is filled with the catalyst 5 supported on, for example, an appropriate granular carrier.
- the raw material gas is introduced from the raw material supply pipe 2 located at one end of the double pipe into the above-mentioned gap, and a part of the reaction product as a non-permeable gas from the non-permeable component discharge pipe 7 located at the other end of the gap. Of hydrogen is discharged.
- the temperature of dehydrogenation is measured and adjusted by inserting a thermocouple 8 in the gap.
- Hydrogen selectively membrane-separated flows inside the inner pipe 4 as a permeated gas. From the permeated gas discharge pipe 6 at the other end of the inner pipe 4, High-purity hydrogen is taken out as a permeated gas.
- a hydrogen storage alloy is connected to the permeation side, and at least a part of the hydrogen obtained in the alloy is occluded. Reduce the pressure inside (reaction field) to improve the hydrogen recovery rate.
- hydrogen gas obtained from the permeation side is cooled by a heat exchanger and then introduced into the hydrogen storage alloy.
- the pressure in the transmission side system is made lower than the pressure in the non-transmission side system (corresponding to the above reaction pressure) by using the hydrogen storage capacity of the hydrogen storage alloy at low temperature.
- the pressure on the permeation side may be lower than the pressure in the non-permeation side system (corresponding to the above reaction pressure). It is preferably IMPa or less, more preferably 0.05 MPa or less.
- the hydrogen storage alloy is a composite comprising at least one metal component and another metal or a nonmetal component such as halogen, and capable of storing hydrogen in the form of a metal hydride or the like. It has the reversible property of releasing hydrogen when heated and absorbing hydrogen when cooled.
- the type of the hydrogen storage alloy used in the present invention is not particularly limited as long as it is an alloy having the ability to store hydrogen, including conventionally known hydrogen storage alloys.
- hydrogen storage alloys are (1) Mg or Ca alloys (Ni, Cu, Ti, etc. are the other components in this case, and specific examples of alloys are Mg 2 Ni, Mg 2 Cu , Ti Cu, LaMg, CaNi, etc.), (2) an alloy of Ti, Zr, V or Nb (Fe, etc.
- an alloy that can contain (occlude) hydrogen by lmass% or more is particularly preferable.
- the alloy has the reversibility to release the occluded hydrogen due to a temperature change or the like, and a particularly preferable alloy is the alloy (2) described above.
- the shape of these hydrogen storage alloys is not particularly limited, but is preferably in the form of particles.
- the particle size is preferably about 0.1 to 10 mm in diameter.
- Hydrogen-absorbing alloy [Well, it releases hydrogen when heated and absorbs (occludes) hydrogen when cooled.]
- the hydrogen-absorbing alloy is filled in a container whose temperature can be controlled. Is more preferable.
- FIGS. 4 and 5 are conceptual diagrams of a hydrogen production system used in the hydrogen production method of the present invention.
- Fig. 4 (a) As shown in Fig. 4 (a), two membrane reactors A and B, two hydrogen storage alloy units A and B containing hydrogen storage alloy in containers (storage alloys A and B in the figure), and a cooling machine And a pipe connecting them.
- a raw hydrocarbon preferably a hydrocarbon containing a cyclohexane ring
- a membrane reactor is introduced into a membrane reactor and converted into hydrogen and unsaturated hydrocarbons such as aromatic hydrocarbons on a dehydrogenation catalyst.
- Most of the generated hydrogen is separated as a permeated gas by a hydrogen separation membrane in situ, and a part of the remaining hydrogen and unsaturated hydrocarbons such as aromatic hydrocarbons are recovered as non-permeated gas.
- the hydrogen on the permeation side is cooled by the cooler and stored in the hydrogen storage alloy, or it becomes generated hydrogen together with the hydrogen released from the hydrogen storage alloy by bypassing the cooler, and this is repeated periodically.
- the permeated gas of the membrane reactor A is cooled by the cooler and stored in the storage alloy A whose outlet is closed.
- the pressure in the permeation side system is reduced compared to that in the non-permeation side system, and hydrogen recovery The rate is improved.
- the permeated gas of the membrane reactor B is introduced into the storage alloy B while maintaining the high temperature after the reaction.
- the storage alloy B is heated, releases the hydrogen stored in the previous cycle, and generates hydrogen together with the hydrogen generated in the membrane reactor B.
- cycle 2 of FIG. 4 (c) the permeated gas of the membrane reactor B is cooled by the cooler and stored in the storage alloy B whose outlet is closed.
- the pressure in the permeation side system is reduced as compared with the pressure in the non-permeation side system, and the hydrogen recovery rate S is improved.
- the permeated gas of the membrane reactor A is introduced into the storage alloy A while maintaining the high temperature after the reaction. As a result, the storage alloy A is heated and releases the stored hydrogen in the cycle 1, and generates hydrogen together with the hydrogen generated in the membrane reactor A.
- FIG. 5 Another example of the system of the present invention is shown in FIG. As shown in Fig. 5 (a), two membrane reactors (A, B), two hydrogen storage alloy units containing hydrogen storage alloy in containers (in the figure, two storage alloys A and B), a cooler and It is composed of piping connecting these.
- the configuration of the piping is different from that of Fig. 4, and the permeated hydrogen of the membrane reactor B is always stored in the hydrogen storage alloy A or B, and the permeated hydrogen of the membrane reactor A is It is always generated hydrogen together with the hydrogen released from the hydrogen storage alloy A or B.
- the permeated gas of the membrane reactor B is cooled by the cooler and stored in the storage alloy B whose outlet is closed.
- the pressure in the permeation-side system is reduced compared to that in the non-permeation-side system, and the hydrogen recovery rate is improved.
- the permeated gas of the membrane reactor A is introduced into the storage alloy A while maintaining the high temperature after the reaction.
- the storage alloy A is heated, releases the hydrogen stored in the previous cycle, and generates hydrogen together with the hydrogen generated in the membrane reactor A.
- cycle 2 of FIG. 5 (c) the permeated gas of the membrane reactor B is cooled by the cooler and stored in the storage alloy A whose outlet is closed.
- the pressure in the permeation side system is reduced as compared with the pressure in the non-permeation side system, and the hydrogen recovery rate S is improved.
- the permeated gas in membrane reactor A was maintained at a high temperature after the reaction. It is also introduced into the storage alloy B. As a result, the storage alloy B is heated, releases the stored hydrogen in the cycle 1, and generates hydrogen together with the hydrogen generated in the membrane reactor A.
- the switching of the cycles occurs before the hydrogen storage alloy saturates.
- the illustrated reactor has two units for both the membrane reactor and the hydrogen storage alloy unit, it is preferable to use two or more units for the purpose of making hydrogen generation more continuous.
- alumina layer 1 layer After forming one layer of alumina on the surface of a porous ceramic tube with an outer diameter of 1 O mm, an inner diameter of 8.4 mm, and a length of 30 O mm, three a-alumina layers Let it form. Further to form a silica layer 1 layer, then, obtained by forming a silica thin film on the final surface, the hydrogen permeability coefficient 4. 2 X 1 0 7 mol / m 2 / sec / Pa, toluene permeability coefficient 2. 8 X 1 A separation membrane A is a ceramic membrane having a density of 0 1 ( ⁇ mol / m 2 / sec / Pa).
- a palladium membrane having a hydrogen permeability coefficient of 200 cc / cm 2 / min / atm 1/2 and a thickness of 2.5 an is referred to as a separation membrane B.
- Catalyst A A spherical commercial catalyst having an average diameter of 1.5 mm and having 0.3 mass% of platinum supported on an alumina carrier is referred to as Catalyst A.
- the inner fin type reaction tube made of aluminum shown in Fig. 1 having an inner diameter of 24 mm, a length of 300 mm, and a fin length of 6 mm was washed with dilute nitric acid, washed with water, dried, and then placed in a chromic acid aqueous solution. Perform anodic oxidation.
- the operation of applying and drying a commercially available pseudo-benzite sol on the fin portion was repeated four times, and then calcined at 450 at room temperature for 2 hours. 0.2504 g of platinum is supported on the fin portion by an impregnation method using an aqueous solution of platinized acid. Then, what was calcined at 30 for 2 hours is referred to as catalyst B.
- Reaction temperature (catalyst layer outlet temperature) Steam was introduced into the permeate side of the hydrogen separation membrane under the conditions of 300, 270, 240, and 220 ° C, and the reaction was performed with the permeate side hydrogen partial pressure set to 0.0 IMPa. Produced hydrogen in the same manner as in Experimental Example 4. Table 5 shows the results.
- a porous ceramic tube with an outer diameter of 10 mm, an inner diameter of 8.4 mm and a length of 300 mm coated with palladium and silver (Pd: Ag 85:15) on the outer surface by electroless plating.
- Hydrogen permeability coefficient A separation membrane B is a palladium membrane having a capacity of 200 cc / cm 2 / min / atm 1/2 and a thickness of 2.5 On.
- a spherical commercial hornworm medium with an average diameter of 1.5 mm and 0.3 mass% of platinum supported on an alumina carrier is used.
- a membrane reactor having the structure shown in Fig. 3 was used.
- the reaction tube has an inner diameter of 24 mm and a length of 300 mm.
- Separation membrane A (Example 1 of the second embodiment) or separation membrane B (Example 2 of the second embodiment and a comparative example) was provided therein.
- the catalyst was filled into the gap between the reaction tube and the hydrogen separation membrane by 11 Occ.
- Separation membrane B was used in the membrane reactor. No cooler, no hydrogen storage alloy and no switching valve were used. Methylcyclohexane is introduced as a raw material into the catalyst layer, and the reaction pressure is 0.2, 0.4, 0.6, 0.8 MPa (absolute pressure), the permeate pressure is 0.1 MPa (absolute pressure), the reaction temperature (catalyst) (Layer outlet temperature) 300, 280, 260 ° C, The dehydrogenation reaction was performed under the condition of LHSV 0.5 hi. Table 6 shows the results.
- LHSV Liquid hourly space velocity
- cc Metalcyclohexane liquid volume
- cc catalyst
- Z time (h) The hydrogen recovery rate is expressed by (hydrogen recovered from the permeate side of the membrane reactor (mol) / theoretical hydrogen generation from the introduced methylcyclohexane (mol) x lOO).
- the apparatus shown in FIG. 6 was used. The reaction is performed for 5 minutes in the same manner as in the comparative example, with the hydrogen generated in the membrane reactor being absorbed by the hydrogen storage alloy as shown in Fig. 6 (a). However, during hydrogen storage, the permeate gas is cooled so that the permeate hydrogen pressure is ⁇ 0.07 MPa.
- Example 6 shows the results.
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Abstract
Description
Claims
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US10/592,285 US20080234527A1 (en) | 2004-03-09 | 2005-03-08 | Method for Producing Hydrogen and System Therefor |
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JP2004-065894 | 2004-03-09 | ||
JP2004065894 | 2004-03-09 | ||
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JP2004100678A JP2005289652A (ja) | 2004-03-09 | 2004-03-30 | 水素の製造方法および反応管 |
JP2004100688A JP2005281103A (ja) | 2004-03-30 | 2004-03-30 | 水素の製造法および水素製造システム |
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US20120078024A1 (en) * | 2010-09-24 | 2012-03-29 | Fina Technology Inc. | Removal of Hydrogen From Dehydrogenation Processes |
CN103998578B (zh) * | 2012-02-01 | 2016-08-17 | 沙特阿拉伯石油公司 | 用于生产降苯汽油的催化重整方法和系统 |
EP2813286A1 (de) * | 2013-06-11 | 2014-12-17 | Evonik Industries AG | Reaktionsrohr und Verfahren zur Herstellung von Cyanwasserstoff |
RU2666446C2 (ru) | 2013-10-11 | 2018-09-07 | Эвоник Дегусса Гмбх | Реакционная труба и способ получения цианистого водорода |
US20160214858A1 (en) * | 2013-10-21 | 2016-07-28 | Air Products And Chemicals, Inc. | Multi-zone dehydrogenation reactor and ballasting system for storage and delivery of hydrogen |
JP6400410B2 (ja) | 2014-09-25 | 2018-10-03 | 国立大学法人横浜国立大学 | 有機ケミカルハイドライド製造用電解セル |
KR102411448B1 (ko) | 2014-11-10 | 2022-06-20 | 고쿠리츠다이가쿠호진 요코하마 고쿠리츠다이가쿠 | 산소 발생용 애노드 |
JP6501141B2 (ja) | 2014-11-21 | 2019-04-17 | 国立大学法人横浜国立大学 | 有機ハイドライド製造装置およびこれを用いた有機ハイドライドの製造方法 |
US20180044264A1 (en) * | 2015-03-05 | 2018-02-15 | Stamicarbon B.V. Acting Under The Name Of Mt Innovation Center | System and method for the production of alkenes by the dehydrogenation of alkanes |
EP3301075A1 (en) | 2016-09-28 | 2018-04-04 | Evonik Degussa GmbH | Method for producing hydrogen cyanide |
CN111893360B (zh) * | 2019-05-06 | 2022-10-21 | 中国石油化工股份有限公司 | Ab5型储氢合金及其制备方法和应用以及含有机物氢气提纯方法 |
JP7472770B2 (ja) * | 2020-12-15 | 2024-04-23 | トヨタ自動車株式会社 | 金属めっき皮膜の成膜装置及び成膜方法 |
CN115043376B (zh) * | 2022-06-01 | 2024-05-07 | 苏州道顺电子有限公司 | 一种甲烷催化裂解制氢副产碳材料的方法 |
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