CN1291166A - Use of a membrane reactor for hydrogen production via direct cracking of hydrocarbons - Google Patents
Use of a membrane reactor for hydrogen production via direct cracking of hydrocarbons Download PDFInfo
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- CN1291166A CN1291166A CN 99803205 CN99803205A CN1291166A CN 1291166 A CN1291166 A CN 1291166A CN 99803205 CN99803205 CN 99803205 CN 99803205 A CN99803205 A CN 99803205A CN 1291166 A CN1291166 A CN 1291166A
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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
- C01B3/22—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
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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
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/501—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by diffusion
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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
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/501—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by diffusion
- C01B3/503—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by diffusion characterised by the membrane
- C01B3/505—Membranes containing palladium
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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
- 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
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- C01—INORGANIC CHEMISTRY
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- 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
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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
- 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
- C01B2203/0465—Composition of the impurity
- C01B2203/047—Composition of the impurity the impurity being carbon monoxide
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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
- 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
- C01B2203/0465—Composition of the impurity
- C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
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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
- 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
- C01B2203/0465—Composition of the impurity
- C01B2203/048—Composition of the impurity the impurity being an organic compound
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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
- 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
- C01B2203/0465—Composition of the impurity
- C01B2203/0495—Composition of the impurity the impurity being water
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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
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/085—Methods of heating the process for making hydrogen or synthesis gas by electric heating
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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
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1005—Arrangement or shape of catalyst
- C01B2203/1011—Packed bed of catalytic structures, e.g. particles, packing elements
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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
- 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
- C01B2203/1047—Group VIII metal catalysts
- C01B2203/1052—Nickel or cobalt catalysts
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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
- 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
- C01B2203/1082—Composition of support materials
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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
- 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
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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
- 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
- C01B2203/1241—Natural gas or methane
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
A process for producting substantially pure hydrogen by contacting a stream of a hydrocarbon gas with a nickel containing catalyst in a membrane reactor. The membrane reactor combines a hydrogen permeable membrane and a catalyst capable of producing hydrogen via the direct cracking of hydrocarbons. The stream of a hydrocarbon gas is contacted with the catalyst at a temperature in the range of about 400 to 900 DEG C which results in the conversion of the gas to substantially pure hydrogen, which selectively permeates through the membrane wall.
Description
Invention field
The present invention relates generally to the preparation method of hydrogen, more specifically, relate to membrane reactor in the purposes for preparing by direct cracking hydrocarbon in the hydrogen.
Background of invention
Past has used mineral membrane such as palladium (Pd), palladium-Yin (Pd-Ag) and several other alloy films to come separation of hydrogen from other reagents of various reactions (comprising hydrogenation and dehydrogenation) and product.Because the cost height of these films, people made very big effort and developed composite membrane and alloy film decades in the past.The film of the type is made by the thin palladium metal film (selective permeability is provided) that is coated on porous or the non-hole carrier (required physical strength is provided).Buxbaum and colleague thereof have developed a kind of film (membrane science magazine J.Membr.Sci.) of specific type, and 85,29 (1993), and US patent 5,149,420 and 5,215,729).The advantage of this film is that several refractory metals such as niobium (Nb), tantalum (Ta), zirconium (Zr) and vanadium (V) they are the same orders of magnitude to hydrogen permeability, and than the perviousness height of palladium, but also have acceptable physical strength.Use electroless plating technology that palladium membranes (1-2 micron thickness) is deposited on these refractory metal surfaces.With film, particularly Pd-Nb and the Pd-Ta of this method preparation, guarantee to have the purity of high extracting hydrogen, and can be than the more hydrogen of pure palladium membrane permeation.In addition, these films are stronger and more durable, also can at high temperature use.
The applicant has illustrated the possibility for preparing hydrogen by direct cracking methane and other suitable hydrocarbon in advance.This method has been described in detail in exercise question another independent invention for " preparing hydrogen by direct cracking hydrocarbon ".But this methane cracking reaction is subjected to the restriction of thermodynamic(al)equilibrium.In addition, dynamic test illustrates the inhibition of the speed of this reaction by the hydrogen product.For these two purposes, it is useful removing the hydrogen that forms from reaction zone reaction process.
Brief summary of the invention
In another was invented separately, we had illustrated in conventional fixed-bed reactor, prepare the feasibility of hydrogen by direct cracking methane with nickel-containing catalyst.But the usefulness owing to having hydrogen at reaction zone to this method of design has produced negative impact.The above-mentioned viewpoint explanation of prior art:, use membrane reactor may improve the performance of the steam that is used for catalytic cracking methane by removing hydrogen from reaction zone effectively.
Therefore, an object of the present invention is by catalytic cracking hydrocarbon to prepare effectively High Purity Hydrogen.
Another object of the present invention provides the method for using the direct cracking hydrocarbon of membrane reactor and preparing hydrogen.
Another purpose of the present invention provides the use nickel-containing catalyst, direct cracking hydrocarbon and prepare the method for the pure basically hydrogen that does not contain the carbon monoxide pollution thing in membrane reactor.
A further object of the present invention provides uses silicon dioxide carried nickel-containing catalyst, prepares the method for High Purity Hydrogen in membrane reactor in the direct cracking methane of low temperature.
The invention solves the problems referred to above,, and illustrated by using the direct cracking hydrocarbon of membrane reactor to prepare the feasibility of pure basically hydrogen.Membrane reactor can be removed hydrogen from reaction zone, therefore, has eliminated the negative interaction to molecular balance and speed of reaction.As a result, use membrane reactor can obviously increase the efficient of process for making hydrogen.This film can be the material of any kind of, if selective permeation hydrogen uniquely, and isolate hydrogen in the carbon monoxide from reaction mixture and other compositions (as unreacted hydrocarbon, carbonic acid gas, water vapour etc.) effectively.With Pd-Nb type film explanation the present invention, believe that this film has special advantage, as in background technology, discussing.But, get rid of other films of use or compound or blended ion ceramic mould in no instance.In one embodiment, this film preferably includes Pd-Nb.The present invention also is applicable to any suitable hydrocarbon of cracking such as methane, Sweet natural gas, ethane, ethene, propane, propylene, butane, pentane, hexane and their mixture, and the hydro carbons of molecular weight between gasoline and diesel range.
This membrane reactor uses catalyst bed, and this catalyst bed preferably includes the nickel-containing catalyst that is carried on the silica supports.The hydrogen that produces at reactor zone optionally penetrates membranous wall, and is taken away by sweeping gas.In operation, the temperature of reaction zone typically is about 400-900 ℃ scope.
Brief description of drawings
Essence for a more complete understanding of the present invention and purpose describe enforcement preferred implementation of the present invention in detail below in conjunction with accompanying drawing.
Fig. 1 represents the side cross-sectional view of amplification of the catalytic reaction zone of two-tube catalytic film reactor.
Fig. 2 represents with 0.2 gram 16wt% Ni/SiO
2The comparison curves of catalyzer methane conversion in the reactor of conventional fixed-bed reactor and Fig. 1 under 550 ℃ of conditions.
Fig. 3 represents with 0.2 gram 16wt% Ni/SiO
2Catalyzer is at 7600h
-1The comparison curves of the methane conversion under the condition in the reactor of conventional fixed-bed reactor and Fig. 1.
Fig. 4 represents the side cross-sectional view of amplification of catalytic reaction zone of the fixed bed catalytic reactor with film dividing plate of another kind of design.
The detailed description of invention
The present invention illustrates with two-tube catalytic film reactor (10) shown in Figure 1.The Pd-Nb film pipe that uses has the external diameter of 9.525 millimeters (3/8 inches), 0.25 millimeter of wall thickness, and according to disclosed method manufacturing in relevant patent (US5149420 and 5215729) (comprising its manufacturing and use), it is for reference that described patent is incorporated into this paper.This reactor comprises pipe (12) and stainless steel or quartz outer tube (14) in the film, and they have determined flow passage (16).Catalyst bed (18) is arranged in pipe (12).Electric heater (20) control reaction temperature.The hydrogen that produces in reactor zone optionally permeates by membranous wall and by the sweeping gas that dash-dot arrows is represented to be taken away.Outer tube (SS, 1 inch of external diameter, thick 0.028 inch) directly is connected with sweeping gas source of the gas (not shown).Film occupies the central section of interior pipe and is connected in the entrance and exit of reactor with suitable components.Catalyzer (16wt% Ni/SiO
2Catalyzer) be encapsulated in the film pipe, and the hydrogen that produces is removed at the shell-side face with inert purge gas such as argon gas.Other hydrogen is also discharged reactor from the bottom of catalyst bed, shown in the solid line arrow.
In typical test, 0.2 catalyzer (25-35 order) that restrains is dispersed in the 0.3 gram inertia silicon-dioxide (25-35 order), be encapsulated in subsequently in the intermediate zone of film pipe.Reactor is washed with rare gas element, and be heated to temperature of reaction.The flow rate control of the argon gas that purges is in the constant rate of speed of 150 cc/min.With raw material introduce begin in the reactor reaction, raw material is 20% methane that is contained in the helium, shown in the solid arrow at top.By gc analysis from sweeping gas and the discharge air-flow that obtains in reactor-side.
It should be understood that and the invention is not restricted to concrete structure shown in Figure 1.In fact, other structures of any combined catalyst effectively (can produce hydrogen by direct cracking hydrocarbon) and film (can only selective permeation hydrogen) can be used for the present invention.Select the structure of Fig. 1 to illustrate that the present invention is because it is simple.Another example that is suitable for membrane reactor structure of the present invention is shown in Fig. 4, and fixed bed catalytic reactor wherein or fuel processor are equipped with the film dividing plate.Utilize direct cracked fuel processor that hydrocarbon feed is changed into hydrogen and carbon product, and by using the film dividing plate, optionally extracting hydrogen and prepare pure basically hydrogen product.The film dividing plate reactor 30 that is shown in Fig. 4 comprises one group of metal or metal alloy film pipe 32, up to 50 or 34 sealings at one end of more little open tube, and at the other end 36 openings.This pipe is surrounded by the bed of catalystic material 38, and all is encapsulated in together in the shell 40 of reactor.In operating process, 42 appropriate hydrocarbon gas infeeded by entering the mouth, and in inner room 44 cracking.The hydrogen permeate that cracking produces is gone into selectivity porous membrane tube 32 and is moved on to outlet 48 (seeing small arrow), and simultaneously, carbon monoxide, other reaction product and unreacted hydrocarbon through port 46 are discharged.
Can find out that from above-mentioned explanation the end that hydrocarbon gas feed enters reactor passes catalyst bed, reaction product and unreacted hydrocarbon are discharged from the other end.In the film dividing plate, the mobile outer side inflow inboard of hydrogen from the film pipe.Effusive pure basically hydrogen merging enters in the shared well heater 50 from all film pipes, and collects at outlet 48 places.Other alternative structure of reactor that are used as this class reactor in industrial operation can comprise fluidized-bed or moving-burden bed reactor.
Be used for catalyzer of the present invention because carbon laydown and final inactivation.The carbon that is deposited on the catalyzer can restore and be used for electrochemical applications (superconductor, electrode and fuel cell) or fuel storage application.In addition, the catalyzer of inactivation can be by sedimentary the carbon vaporization of oxidation or steam and holomorphosis in air.
Fig. 2 has compared the methane turnover ratio, described turnover ratio by conventional fixed-bed reactor and Fig. 1 reactor 550 ℃ with different air speed conditions under obtain.Methane turnover ratio in conventional fixed-bed reactor is from air speed 60000h
-131.7% be changed at 7500h
-142.2%.In membrane reactor, the methane turnover ratio is from 60000h
-137.2% be changed at 7500h
-170.8%.Under the low-speed condition, its difference more remarkable (therefore, embodying the advantage of using membrane reactor), this is because more embodied the negative interaction of hydrogen under these conditions.
Under differing temps, measured the hydrogen permeate rate of the Pd-Nb film that in this example, uses, found that rate of permeation increases with temperature.Can suppose by under higher temperature, using membrane reactor more favourable observed methane turnover ratio.This has obtained checking by the test of temperature up to 550 ℃, as shown in Figure 3.In addition higher temperature under, the difference of two class reactor performances reduces, this is because the film cause of degenerating under these conditions.
Although understand the present invention specifically with reference to preferred mode shown in the drawings, what it should be appreciated by those skilled in the art is can carry out various variations under the prerequisite of the spirit and scope that do not break away from claim of the present invention.
Claims (12)
1, the method for the pure basically hydrogen of a kind of preparation comprises:
(a) provide the membrane reactor that comprises hydrogen permeable film and catalyst bed; And
(b) air-flow with hydrocarbon contacts in about 400-900 ℃ temperature range with described catalyzer, and the result makes described gas reforming become pure basically hydrogen, and described hydrogen optionally permeates by this membranous wall.
2, the method for claim 1, wherein described film can only selective permeation hydrogen, and isolate hydrogen effectively in the carbon monoxide from reaction mixture and other compositions.
3, the method for claim 1, wherein described film comprises metal or metal alloy.
4, the method for claim 1, wherein described film comprises Pd or Pd alloy.
5, the method for claim 1, wherein described film comprises Pd-Nb.
6, the method for claim 1, wherein described film comprises matrix material or ceramic mould film.
7, the method for claim 1, wherein this catalyzer contains nickel and is carried on the silica supports.
8, the method for claim 1, wherein this catalyzer contains the nickel of 5wt% at least.
9, the method for claim 1, wherein, this appropriate hydrocarbon gas is selected from a kind of by in the following group of forming: methane, Sweet natural gas, ethane, ethene, propane, propylene, butane, pentane, hexane and their mixture, and the hydro carbons of molecular weight between gasoline and diesel range.
10, the method for claim 1, wherein this appropriate hydrocarbon gas is mixed with inert carrier gas.
11, the method for claim 1, wherein this catalyzer is regenerated by the aerial oxidation of deposit carbon.
12, the method for claim 1, wherein this catalyzer is regenerated by the steam vaporization of deposit carbon.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US7581498P | 1998-02-24 | 1998-02-24 | |
| US60/075,814 | 1998-02-24 | ||
| US23186299A | 1999-01-14 | 1999-01-14 | |
| US09/231,862 | 1999-01-14 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1291166A true CN1291166A (en) | 2001-04-11 |
Family
ID=26757305
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 99803205 Pending CN1291166A (en) | 1998-02-24 | 1999-02-19 | Use of a membrane reactor for hydrogen production via direct cracking of hydrocarbons |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP1066216A1 (en) |
| CN (1) | CN1291166A (en) |
| AU (1) | AU2773899A (en) |
| CA (1) | CA2317396A1 (en) |
| WO (1) | WO1999043610A1 (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100342576C (en) * | 2002-08-30 | 2007-10-10 | 荷兰能源建设基金中心 | Shift membrane burner/fuel cell combination |
| CN100410167C (en) * | 2004-01-21 | 2008-08-13 | 雷敏宏 | Process and reactor module for quick start hydrogen production |
| CN100562485C (en) * | 2002-04-12 | 2009-11-25 | 益达科技责任有限公司 | Steam reforming fuel processor |
| CN107469628A (en) * | 2017-09-21 | 2017-12-15 | 中国科学院上海应用物理研究所 | The device and method of gaseous state tritium and its isotope in a kind of removal fused salt |
| CN108745262A (en) * | 2018-07-05 | 2018-11-06 | 山东理工大学 | The preparation method and its test system of the saturating hydrogen-flat membrane reactor of methane portion oxidation dehydrogenation triple effect of oxygen flow- |
| CN108745263A (en) * | 2018-07-05 | 2018-11-06 | 山东理工大学 | The preparation method of the saturating hydrogen-reaction triple effect tubulose membrane reactor of the oxygen flow-of partial oxidation of methane hydrogen |
| CN109824627A (en) * | 2019-03-01 | 2019-05-31 | 山东理工大学 | A kind of method of the saturating hydrogen coupled film microreactor synthesizing epoxypropane of oxygen flow |
| CN110483228A (en) * | 2018-11-06 | 2019-11-22 | 中国科学院青岛生物能源与过程研究所 | A kind of method and apparatus reacted in proton-conductive films reactor while obtaining high-purity hydrogen and chemicals |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE10040539A1 (en) * | 2000-08-18 | 2002-03-07 | Aral Ag & Co Kg | Membrane reactor for producing highly pure hydrogen, used in vehicle driven by fuel cell or in domestic heating, involves steam reforming hydrocarbon stream, and is heated by hot conductor in center of reactor |
| DE10118248A1 (en) * | 2000-08-18 | 2002-10-17 | Aral Ag & Co Kg | Process for the production of high-purity hydrogen gas with a membrane reactor and a pretreatment step |
| ATE506322T1 (en) * | 2004-02-03 | 2011-05-15 | Min-Hoi Rei | METHOD AND REACTOR MODULE FOR FAST-START HYDROGEN PRODUCTION |
| WO2007031713A1 (en) * | 2005-09-14 | 2007-03-22 | Bp P.L.C. | Process for hydrogen production |
| ITRM20060102A1 (en) * | 2006-03-01 | 2007-09-02 | Cnr Consiglio Naz Delle Ricerche | MEMBRANE PROCEDURE FOR THE PRODUCTION OF REFORMING HYDROGEN OF ORGANIC COMPOUNDS IN PARTICULAR HYDROCARBONS OR ALCOHOLS |
| DE102010053290A1 (en) * | 2010-12-02 | 2012-06-06 | Linde Ag | Method and apparatus for producing hydrogen from glycerin |
| US9745191B2 (en) | 2011-04-11 | 2017-08-29 | Saudi Arabian Oil Company | Auto thermal reforming (ATR) catalytic structures |
| US8597383B2 (en) | 2011-04-11 | 2013-12-03 | Saudi Arabian Oil Company | Metal supported silica based catalytic membrane reactor assembly |
| SG11201404972QA (en) | 2012-03-08 | 2014-09-26 | Univ Singapore | Catalytic hollow fibers |
| CN103007697B (en) * | 2012-12-21 | 2015-03-18 | 上海合既得动氢机器有限公司 | Membrane separator for methyl alcohol water hydrogen production equipment and fabrication method of membrane separator |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3962411A (en) * | 1973-12-13 | 1976-06-08 | United Technologies Corporation | Method for catalytically cracking a hydrocarbon fuel |
| US4244811A (en) * | 1978-07-25 | 1981-01-13 | Exxon Research & Engineering Co. | Catalytic cracking process with simultaneous production of a low BTU fuel gas and catalyst regeneration |
| US4981676A (en) * | 1989-11-13 | 1991-01-01 | Minet Ronald G | Catalytic ceramic membrane steam/hydrocarbon reformer |
| US5215729A (en) * | 1990-06-22 | 1993-06-01 | Buxbaum Robert E | Composite metal membrane for hydrogen extraction |
| CA2081170C (en) * | 1992-10-22 | 2002-12-24 | Alaa-Eldin Moustafa Adris | Fluidized bed reaction system for steam/hydrocarbon gas reforming to produce hydrogen |
| DE69420604T2 (en) * | 1993-03-16 | 2000-05-25 | Tokyo Gas Co Ltd | Device for producing hydrogen |
| US5525322A (en) * | 1994-10-12 | 1996-06-11 | The Regents Of The University Of California | Method for simultaneous recovery of hydrogen from water and from hydrocarbons |
-
1999
- 1999-02-19 AU AU27738/99A patent/AU2773899A/en not_active Abandoned
- 1999-02-19 WO PCT/US1999/003574 patent/WO1999043610A1/en not_active Application Discontinuation
- 1999-02-19 CN CN 99803205 patent/CN1291166A/en active Pending
- 1999-02-19 CA CA002317396A patent/CA2317396A1/en not_active Abandoned
- 1999-02-19 EP EP99908260A patent/EP1066216A1/en not_active Withdrawn
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100562485C (en) * | 2002-04-12 | 2009-11-25 | 益达科技责任有限公司 | Steam reforming fuel processor |
| CN100342576C (en) * | 2002-08-30 | 2007-10-10 | 荷兰能源建设基金中心 | Shift membrane burner/fuel cell combination |
| CN100410167C (en) * | 2004-01-21 | 2008-08-13 | 雷敏宏 | Process and reactor module for quick start hydrogen production |
| CN107469628B (en) * | 2017-09-21 | 2019-10-01 | 中国科学院上海应用物理研究所 | The device and method of gaseous state tritium and its isotope in a kind of removal fused salt |
| CN107469628A (en) * | 2017-09-21 | 2017-12-15 | 中国科学院上海应用物理研究所 | The device and method of gaseous state tritium and its isotope in a kind of removal fused salt |
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Also Published As
| Publication number | Publication date |
|---|---|
| CA2317396A1 (en) | 1999-09-02 |
| EP1066216A1 (en) | 2001-01-10 |
| AU2773899A (en) | 1999-09-15 |
| WO1999043610A1 (en) | 1999-09-02 |
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