CN103103556B - Tubular ceramic membrane reactor and methanol synthesis method implemented by using same - Google Patents
Tubular ceramic membrane reactor and methanol synthesis method implemented by using same Download PDFInfo
- Publication number
- CN103103556B CN103103556B CN201310070960.0A CN201310070960A CN103103556B CN 103103556 B CN103103556 B CN 103103556B CN 201310070960 A CN201310070960 A CN 201310070960A CN 103103556 B CN103103556 B CN 103103556B
- Authority
- CN
- China
- Prior art keywords
- microtubule
- electrolyzer
- tubular
- ceramic membrane
- membrane reactor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Abstract
The invention relates to a tubular ceramic membrane reactor and a methanol synthesis method implemented by using the same. The method is used for synthesizing methanol through the tubular ceramic membrane reactor by taking enormously discharged greenhouse gas CO2 and water vapor as raw material gas, namely, under the action of a high temperature (400-800 DEG C) and an external electric field (1.2-2.5 V), water is subjected to electrolytic reaction at the anode of a proton type microtubular electrolytic cell so as to generate H<+>, the H<+> generated by the anode is transmitted to the cathode of the electrolytic cell through a proton conductor electrolyte membrane, CO2 fed into a cathode chamber is reacted with the high-activity H<+> and e<-> on a gas/solid interface in a Ni-based porous cathode with catalytic activity, so that the methanol is synthesized at normal pressure. The methanol synthesis method has the characteristics of energy conservation, emission reduction, environmental friendliness and capability of mass production, so that the method has the advantage of broad application prospect.
Description
Technical field
The invention belongs to ceramic material technical field, be specifically related to a kind of method of tubular ceramic membrane reactor and synthesizing methanol thereof.
Background technology
Methyl alcohol is the raw material of chemistry and energy industry widespread use, be widely used in and produce plastics, synthon, synthetic rubber, coating, spices, medicine and agricultural chemicals etc., and be a kind of important organic solvent, be that the Chemicals of raw material production can reach hundreds of with methyl alcohol.Methyl alcohol is also a kind of environment-protecting clean fuel, as the substitute of petroleum or product function more and more obviously (methanol fuel and deep processed product dme thereof all can be used as relatively cheap traffic fuel), mate with existing energy structure, have broad application prospects.
Methane synthesizing method conventional at present for raw material, is converted into synthetic gas (H with fossil resource (Sweet natural gas, coal and oil etc.)
2with CO gas mixture), then in synthetic tower under high temperature (350 ~ 400 DEG C) and high pressure (20 ~ 30MPa) and catalyzer acting in conjunction synthesizing methanol.This conventional methanol synthetic method limits by thermodynamics of reactions condition, methanol yield is low, also can cause the huge consumption of non-renewable fossil resource, and there is the shortcoming that investment is large, high to equipment requirements, occupation of land space is large, production process energy consumption is large, environmental pollution serious and production cost is higher.In recent years, CO is passed through
2hydrogenation (H
2) synthesizing methanol just receiving increasing concern, this method is with the CO discharged in industrial production
2the waste gas that content is high or the CO trapped from air
2replacement CO is raw material, in the synthetic tower of certain temperature (220 ~ 300 DEG C), pressure (5 ~ 10MPa), with H under copper-based catalysts effect
2reactive Synthesis methyl alcohol, its raw materials used CO
2gas is the abundantest potential carbon source of nature, is also cause one of Greenhouse effect primary discharge gas.Therefore, CO
2gas hydrogenation (H
2) synthesizing methanol is to CO
2recycling and eliminate CO
2the harm tool of environment is of great significance, but this methane synthesizing method needs elevated pressures with traditional by the method for fossil resource synthesizing methanol is the same and consumes huge energy source and power, and CO
2low conversion rate (< 20%) and synthesizing methanol productive rate little (< 12%), and hydrogen used mainly adopts fossil oil to prepare, and also can consume a large amount of non-renewable fossil resources and produce CO
2deng environmental pollutant.
Summary of the invention
The technical problem to be solved in the present invention is to provide a kind of efficient, clean, economic, the method for tubular ceramic membrane reactor synthesizing methanol that can be mass-produced.
Technical scheme of the present invention is: a kind of tubular ceramic membrane reactor, be made up of tubular type gradient electric furnace, microtubule electrolyzer, sealing-in sleeve pipe, described microtubule electrolyzer internal passages is cathode compartment, described microtubule electrolyzer sealing-in sleeve pipe outside with it forms anolyte compartment, it is inner that described sealing-in sleeve pipe is arranged on tubular type gradient electric furnace, it is characterized in that: described microtubule electrolyzer is made up of with layered arrangement cathode support body, electrolytic thin-membrane, anode, described tubular anode room is provided with steam entry, and it is catalyst based that described tubular type cathode compartment side is provided with Cu-Zn.
The microtubule of described microtubule electrolyzer to be external diameter be 2 ~ 3mm.
Described microtubule material is the mixture of NiO and proton conductor material, and its mass percent is 60%:40%.
Described proton conductor material is BaZr
0.3ce
0.5y
0.16zn
0.04o
3-δ.
The thickness of described microtubule electrolytic cell anode is 20 ~ 40 μm.
The material of described microtubule electrolytic cell anode is La
0.6sr
0.4co
0.2fe
0.8o
3-δwith
BaZr
0.3ce
0.5y
0.16zn
0.04o
3-δmixture, its mass percent is 70%:30%.
The material of described microtubule cell electrolyte film is BaZr
0.3ce
0.5y
0.16zn
0.04o
3-δ.
The work area temperature of described microtubule electrolyzer is 400 ~ 800 DEG C, and the catalyst based work area temperature of Cu-Zn is 200 ~ 400 DEG C.
The method of above-mentioned a kind of tubular ceramic membrane reactor synthesizing methanol, is characterized in that comprising the steps:
The first step: by tubular type gradient electric furnace by the heating temperatures of microtubule electrolyzer to 400 ~ 800 DEG C;
Second step: the cathode support body of microtubule electrolyzer is connected with the negative pole of direct supply, the anode of microtubule electrolyzer connects with the positive pole of direct supply;
3rd step: pass into hydrogen in tubular type cathode compartment, makes the NiO on microtubule cathode of electrolytic tank supporter be reduced to Ni;
4th step: after the NiO on microtubule cathode of electrolytic tank supporter has reduced, pass into CO by the introducing port of tubular type cathode compartment
2gas;
5th step: the anode by the steam entry of tubular anode room steam-laden Ar gas being passed into microtubule electrolyzer carries out decomposition reaction and generates highly active H
+;
6th step: highly active H
+by electrolytic thin-membrane transfer on cathode support body with CO
2gas reacts, at ambient pressure synthesizing methanol, and is derived by the export mouth of tubular type cathode compartment by behind the catalyst based region of Cu-Zn.
The electrolysis voltage of described microtubule electrolyzer is 1.2 ~ 2.5V.
H needed for described methanol-fueled CLC
+quantity by water vapour content in adjustment Ar gas, flow rates,
Cell operating temperature, electrolysis voltage control.
The electrolytic reaction that described electrolytic cell anode occurs is: 3H
2o (g) → 6H
++ 3/2O
2(g)+6e
-.
The electrolytic reaction that described cathode of electrolytic tank supporter occurs is: CO
2(g)+6H
++ 6e
-→ CH
3oH (g)+H
2o (g).
The building-up reactions of the catalyst based generation of described Cu-Zn is: CO
2(g)+3H
2→ CH
3oH (g)+H
2o (g).
Technical scheme of the present invention compared with prior art has following innovation:
(1) adopt the technology of the present invention can under normal pressure (~ 0.1MPa) synthesizing methanol, and CO
2transformation efficiency and methanol yield significantly improve than prior art, can simplify methanol synthesizing process and reduce costs;
(2) CO can be transformed on a large scale
2for fuel and industrial chemicals, save non-renewable fossil fuel resource, greatly reduce greenhouse gases CO
2discharge and realize neutral carbon circulation, to environment protection important in inhibiting;
(3) be convenient to, in the electric energy that renewable energy source (sun power, wind energy etc.) or advanced nuclear reactor provided and the reaction of heat energy efficient for high-temperature vapour electrolytic hydrogen production ion, finally carry out the synthesis of methyl alcohol, to reduce the consumption to fossil resource in methanol-fueled CLC;
(4) anolyte compartment can obtain pure oxygen and H
2the gas mixture of O, this high-temperature oxygen-enriched steam can directly apply to the gasification reaction etc. of coal or biomass;
(5) methanol yield can reach 25.4%, far above the productive rate of prior art methyl alcohol.
Accompanying drawing explanation
Accompanying drawing 1 is the structural representation of tubular ceramic membrane reactor cross-section of the present invention.
Embodiment
Below in conjunction with the drawings and specific embodiments, the present invention will be described in detail:
embodiment 1
The preparation of electrolytic cell:
(1) NiO and BaZr is adopted
0.3ce
0.5y
0.16zn
0.04o
3-δ(BZCYZ) mixture (mass percent is 60%:40%) prepares by phase inversion process is shaping the cathode support body 4 that external diameter is 2mm, burns till after drying at 1250 DEG C of insulation 4h;
(2) on cathode support body 4, prepare by vacuum aided dip-coating method the BaZr that thickness is 20 μm
0.3ce
0.5y
0.16zn
0.04o
3-δ(BZCYZ) electrolytic thin-membrane 5, burns till at 1400 DEG C of insulation 4h after drying;
(3) adopt spin-coating method at electrolytic thin-membrane 5 surface preparation La
0.6sr
0.4co
0.2fe
0.8o
3 δ(LSCF)-BaZr
0.3ce
0.5y
0.16zn
0.04o
3-δ(BZCYZ) anode, and burn till at 1000 DEG C of insulation 2h, finally making structure is: the proton type microtubule electrolytic cell of NiO-BZCYZ/ BZCYZ/LSCF-BZCYZ type.
The structure of tubular ceramic membrane reactor:
The cathode compartment 3 of structure to be proton type microtubule electrolyzer 11 internal passages of NiO-BZCYZ/ BZCYZ/LSCF-BZCYZ be reactor, sealing-in sleeve pipe 12 outside with it forms the anolyte compartment 2 of reactor, it is inner that sealing-in sleeve pipe 12 is fixed on tubular type gradient electric furnace 1 together with internal micro-tubes electrolyzer 11, finally makes tubular ceramic membrane reactor.
Methane synthesizing method:
The tubular ceramic membrane reactor of structure shown in Fig. 1 is adopted to carry out methanol-fueled CLC, CO in building-up process
2transformation efficiency is 36.2%, and methanol yield is 22.8%, and concrete steps are as follows:
The first step: by tubular type gradient electric furnace 1 by the heating temperatures of microtubule electrolyzer 11 to 650 DEG C;
Second step: the cathode support body 4 of microtubule electrolyzer 11 is connected with the negative pole of direct supply, the anode 6 of microtubule electrolyzer 11 connects with the positive pole of direct supply, and the voltage of direct supply is 1.6V;
3rd step: pass into hydrogen in tubular type cathode compartment 3, makes the NiO on microtubule electrolyzer 11 cathode support body 4 be reduced to Ni;
4th step: after the NiO on microtubule electrolyzer 11 cathode support body 4 has reduced, passes into CO by the introducing port 8 of tubular type cathode compartment 3 with the speed of 40ml/min
2gas;
5th step: the anode 6 by the steam entry 10 of tubular anode room 2 the Ar gas of containing water vapor 20% being passed into microtubule electrolyzer 11 with the speed of 200ml/min carries out decomposition reaction and generates highly active H
+;
6th step: highly active H
+by electrolytic thin-membrane 5 transfer on cathode support body 4 with CO
2gas reacts, at ambient pressure synthesizing methanol gas, and by being derived by the export mouth 9 of tubular type cathode compartment 3 behind catalyst based 7 regions of Cu-Zn.
embodiment 2:
The preparation of electrolytic cell and the structure of tubular ceramic membrane reactor are with embodiment 1.
Methane synthesizing method:
The tubular ceramic membrane reactor of structure shown in Fig. 1 is adopted to carry out methanol-fueled CLC, CO in building-up process
2transformation efficiency is 43.7%, and methanol yield is 25.4%, and concrete steps are as follows:
The first step: by tubular type gradient electric furnace 1 by the heating temperatures of microtubule electrolyzer 11 to 650 DEG C;
Second step: the cathode support body 4 of microtubule electrolyzer 11 is connected with the negative pole of direct supply, the anode 6 of microtubule electrolyzer 11 connects with the positive pole of direct supply, and the voltage of direct supply is 2V;
3rd step: pass into hydrogen in tubular type cathode compartment 3, makes the NiO on microtubule electrolyzer 11 cathode support body 4 be reduced to Ni;
4th step: after the NiO on microtubule electrolyzer 11 cathode support body 4 has reduced, passes into CO by the introducing port 8 of tubular type cathode compartment 3 with the speed of 40ml/min
2gas;
5th step: the anode 6 by the steam entry 10 of tubular anode room 2 the Ar gas of containing water vapor 30% being passed into microtubule electrolyzer 11 with the speed of 200ml/min carries out decomposition reaction and generates highly active H
+;
6th step: highly active H
+by electrolytic thin-membrane 5 transfer on cathode support body 4 with CO
2gas reacts, at ambient pressure synthesizing methanol gas, and by being derived by the export mouth 9 of tubular type cathode compartment 3 behind catalyst based 7 regions of Cu-Zn.
The above, be only the present invention's preferably embodiment, but scope is not limited thereto, and is equal to and replaces or change, all should be encompassed within protection scope of the present invention according to technical scheme of the present invention and inventive concept thereof.
Claims (9)
1. a tubular ceramic membrane reactor, by tubular type gradient electric furnace (1), microtubule electrolyzer (11), sealing-in sleeve pipe (12) is formed, described microtubule electrolyzer (11) internal passages is cathode compartment (3), described microtubule electrolyzer (11) sealing-in sleeve pipe (12) outside with it forms anolyte compartment (2), it is inner that described sealing-in sleeve pipe (12) is arranged on tubular type gradient electric furnace (1), it is characterized in that: described microtubule electrolyzer (11) is by cathode support body (4), electrolytic thin-membrane (5), anode (6) is formed with layered arrangement, described tubular anode room is provided with steam entry (10), described tubular type cathode compartment (3) side is provided with Cu-Zn catalyst based (7),
The material of described microtubule electrolyzer (11) anode (6) is La
0.6sr
0.4co
0.2fe
0.8o
3-δwith BaZr
0.3ce
0.5y
0.16zn
0.04o
3-δmixture, its mass percent is 70%:30%.
2. a kind of tubular ceramic membrane reactor according to claim 1, is characterized in that: described microtubule electrolyzer (11) for external diameter be the microtubule of 2 ~ 3mm.
3. a kind of tubular ceramic membrane reactor according to claim 2, it is characterized in that: described microtubule material is the mixture of NiO and proton conductor material, its mass percent is 60%:40%.
4. a kind of tubular ceramic membrane reactor according to claim 3, is characterized in that: described proton conductor material is BaZr
0.3ce
0.5y
0.16zn
0.04o
3-δ.
5. a kind of tubular ceramic membrane reactor according to claim 1, is characterized in that: the thickness of described microtubule electrolyzer (11) anode (6) is 20 ~ 40 μm.
6. a kind of tubular ceramic membrane reactor according to claim 1, is characterized in that: the material of described microtubule electrolyzer (11) electrolytic thin-membrane (5) is BaZr
0.3ce
0.5y
0.16zn
0.04o
3-δ.
7. a kind of tubular ceramic membrane reactor according to claim 1, is characterized in that: the work area temperature of described microtubule electrolyzer (11) is 400 ~ 800 DEG C, and the work area temperature of Cu-Zn catalyst based (7) is 200 ~ 400 DEG C.
8., according to the method for the arbitrary described a kind of tubular ceramic membrane reactor synthesizing methanol of claim 1-7, it is characterized in that comprising the steps:
The first step: by tubular type gradient electric furnace (1) by the heating temperatures of microtubule electrolyzer (11) to 400 ~ 800 DEG C;
Second step: the cathode support body (4) of microtubule electrolyzer (11) is connected with the negative pole of direct supply, the anode (6) of microtubule electrolyzer (11) connects with the positive pole of direct supply;
3rd step: pass into hydrogen in tubular type cathode compartment (3), makes the NiO on microtubule electrolyzer (11) cathode support body (4) be reduced to Ni;
4th step: after the NiO on microtubule electrolyzer (11) cathode support body (4) has reduced, passes into CO by the introducing port (8) of tubular type cathode compartment (3)
2gas;
5th step: the anode (6) by the steam entry (10) of tubular anode room (2) steam-laden Ar gas being passed into microtubule electrolyzer (11) carries out decomposition reaction and generates highly active H
+;
6th step: highly active H
+transfer on cathode support body (4) and CO by electrolytic thin-membrane (5)
2gas reacts, at ambient pressure synthesizing methanol, and is derived by the export mouth (9) of tubular type cathode compartment (3) by behind Cu-Zn catalyst based (7) region.
9. the method for a kind of tubular ceramic membrane reactor synthesizing methanol according to claim 8, is characterized in that: the electrolysis voltage of described microtubule electrolyzer (11) is 1.2 ~ 2.5V.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310070960.0A CN103103556B (en) | 2013-03-06 | 2013-03-06 | Tubular ceramic membrane reactor and methanol synthesis method implemented by using same |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310070960.0A CN103103556B (en) | 2013-03-06 | 2013-03-06 | Tubular ceramic membrane reactor and methanol synthesis method implemented by using same |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103103556A CN103103556A (en) | 2013-05-15 |
| CN103103556B true CN103103556B (en) | 2015-05-20 |
Family
ID=48311738
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310070960.0A Expired - Fee Related CN103103556B (en) | 2013-03-06 | 2013-03-06 | Tubular ceramic membrane reactor and methanol synthesis method implemented by using same |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103103556B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3106542A1 (en) * | 2015-06-19 | 2016-12-21 | Technische Universität Dresden | Device for the synthesis of hydrogenated compounds |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103613067B (en) * | 2013-11-22 | 2015-10-28 | 山东理工大学 | The method of synthetic gas is prepared in humidify carbon dioxide electrocatalysis |
| CN105200448B (en) * | 2015-09-30 | 2017-08-22 | 大连理工大学 | A kind of organic matter dehydrogenation and hydrogenation coupled electrochemistry hydrogen pump double-reactor |
| CN105220172B (en) * | 2015-10-27 | 2017-06-16 | 中国科学技术大学 | It is a kind of that carbon dioxide and vapor gaseous mixture are converted into tubular structure of gas rich in methane and its preparation method and application |
| CN109529851B (en) * | 2018-12-26 | 2021-10-01 | 大连海事大学 | Nickel-based supported catalyst and method for catalyzing CO by using plasma of nickel-based supported catalyst2Method for preparing methanol by hydrogenation |
| CN111359543A (en) * | 2020-05-11 | 2020-07-03 | 信阳学院 | Metal ceramic membrane reactor for natural gas conversion |
| CN112760671B (en) * | 2020-12-22 | 2022-08-09 | 广东工业大学 | Methanol synthesis method based on mixed ion conductor membrane reactor and application thereof |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102004015878A1 (en) * | 2004-03-31 | 2005-10-20 | Siemens Ag | Production of functional layers on defined regions of a substrate comprises using a hydraulically binding high temperature resistant ceramic material as masking material |
| CN1701455A (en) * | 2002-09-27 | 2005-11-23 | 荷兰能源建设基金中心 | Electrode-supported fuel cell |
| CN101034753A (en) * | 2006-03-12 | 2007-09-12 | 中国科学技术大学 | Flat pole supporting solid oxide fuel battery |
| CN101252199A (en) * | 2008-04-01 | 2008-08-27 | 南京工业大学 | Method for preparing hollow fiber-type solid-oxide fuel battery |
| CN101577340A (en) * | 2009-03-04 | 2009-11-11 | 中国科学院上海硅酸盐研究所 | Method for preparing cathode-supported tubular solid oxide fuel cells |
| CN102290589A (en) * | 2011-07-19 | 2011-12-21 | 中国科学院上海硅酸盐研究所 | Cathode-supported direct carbon fuel cell |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101119396B1 (en) * | 2009-08-31 | 2012-03-06 | 삼성전기주식회사 | Solid oxide fuel cell structure |
-
2013
- 2013-03-06 CN CN201310070960.0A patent/CN103103556B/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1701455A (en) * | 2002-09-27 | 2005-11-23 | 荷兰能源建设基金中心 | Electrode-supported fuel cell |
| DE102004015878A1 (en) * | 2004-03-31 | 2005-10-20 | Siemens Ag | Production of functional layers on defined regions of a substrate comprises using a hydraulically binding high temperature resistant ceramic material as masking material |
| CN101034753A (en) * | 2006-03-12 | 2007-09-12 | 中国科学技术大学 | Flat pole supporting solid oxide fuel battery |
| CN101252199A (en) * | 2008-04-01 | 2008-08-27 | 南京工业大学 | Method for preparing hollow fiber-type solid-oxide fuel battery |
| CN101577340A (en) * | 2009-03-04 | 2009-11-11 | 中国科学院上海硅酸盐研究所 | Method for preparing cathode-supported tubular solid oxide fuel cells |
| CN102290589A (en) * | 2011-07-19 | 2011-12-21 | 中国科学院上海硅酸盐研究所 | Cathode-supported direct carbon fuel cell |
Non-Patent Citations (3)
| Title |
|---|
| Bin Lin et al..Stable, easily sintered BaCe0.5Zr0.3Y0.16Zn0.04O3−ıelectrolyte-based proton-conducting solid oxide fuel cells by gel-casting and suspension spray.《Journal of alloys and compound》.2008,第478卷 * |
| Fabrication and characterization of micro-tubular cathode-supported SOFC for intermediate temperature operation;Yu Liu et al.;《Journal of power sources》;20070906;第174卷;第95-102页 * |
| 中空纤维陶瓷透氧膜反应器;谭小耀 等;《山东理工大学学报》;20060131;第20卷(第1期);第1-4页 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3106542A1 (en) * | 2015-06-19 | 2016-12-21 | Technische Universität Dresden | Device for the synthesis of hydrogenated compounds |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103103556A (en) | 2013-05-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103103556B (en) | Tubular ceramic membrane reactor and methanol synthesis method implemented by using same | |
| Zhao et al. | Integrated design for electrocatalytic carbon dioxide reduction | |
| Zhang et al. | Progress and prospects of hydrogen production: Opportunities and challenges | |
| Dalena et al. | Methanol production and applications: an overview | |
| Ortiz et al. | Hydrogen production research in Mexico: A review | |
| CN106977369B (en) | Device and method for combined preparation of methanol and ammonia by comprehensively utilizing electric energy | |
| CN106242946B (en) | A kind of equipment and technique of solar hydrogen making synthesizing methanol | |
| CN111378980A (en) | Energy storage system and method for coproducing hydrogen and urea | |
| WO2011029283A1 (en) | Method for composite utilizing coal and system thereof | |
| CN104478656B (en) | A kind of method of carbon dioxide reduction | |
| CN104362355A (en) | Methanol water hydrogen-making machine and hydrogen-making method thereof | |
| CN104328046A (en) | Apparatus and method for producing acetic acid by reducing carbon dioxide through microbial-electrochemical system | |
| Meshksar et al. | Solar reformers coupled with PEMFCs for residential cogeneration and trigeneration applications | |
| CN104649227B (en) | Comprehensive solar energy utilization system based on oxygen permeating membrane | |
| CN107699915A (en) | A kind of temperature maintains carbon dioxide and water vapour electrolysis unit and its application process altogether certainly | |
| Kalinci et al. | Performance assessment of hydrogen production from a solar-assisted biomass gasification system | |
| CN206219468U (en) | A kind of equipment of solar hydrogen making synthesizing methanol | |
| CN101172574A (en) | Method for producing hydrogen gas and synthesis gas with solar molten salt chemical circulation | |
| Braga et al. | Hydrogen production processes | |
| CN210237792U (en) | Energy router using water and carbon dioxide as raw materials | |
| Nong et al. | Simulation of energy conversion in a plant of photocatalysts water splitting for hydrogen fuel | |
| CN109650331A (en) | Hydrogen production process and hydrogen generating system based on silicon powder and silicon material | |
| CN208627261U (en) | Photovoltaic water decomposition system couples the device for preparing organic-fuel with photo-thermal catalysis system | |
| CN204281300U (en) | A kind of methanol-water hydrogen making machine | |
| CN207199753U (en) | A kind of hydrogen fuel cell system based on hydrogen from ethanol reforming |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C53 | Correction of patent of invention or patent application | ||
| CB03 | Change of inventor or designer information |
Inventor after: Zhang Xiaozhen Inventor after: Hu Jianping Inventor after: Zhou Jianer Inventor after: Wang Yongqing Inventor after: Jiang Yuhua Inventor after: Wu Chunrong Inventor after: Zhang Jing Inventor before: Zhang Xiaozhen Inventor before: Wu Chunrong Inventor before: Zhou Jianer Inventor before: Wang Yongqing Inventor before: Zhang Jing Inventor before: Jiang Yuhua |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: INVENTOR; FROM: ZHANG XIAOZHEN WU CHUNRONG ZHOU JIANER WANG YONGQING ZHANG JING JIANG YUHUA TO: ZHANG XIAOZHEN HU JIANPING ZHOU JIANER WANG YONGQING JIANG YUHUA WU CHUNRONG ZHANG JING |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150520 Termination date: 20170306 |