CN103103556A - 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
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- CN103103556A CN103103556A CN2013100709600A CN201310070960A CN103103556A CN 103103556 A CN103103556 A CN 103103556A CN 2013100709600 A CN2013100709600 A CN 2013100709600A CN 201310070960 A CN201310070960 A CN 201310070960A CN 103103556 A CN103103556 A CN 103103556A
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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 the 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, the Chemicals take methyl alcohol as raw material production can reach hundreds of.Methyl alcohol is also a kind of environment-protecting clean fuel, as the function of the substitute of petroleum or product more and more obviously (methanol fuel and deep processed product dme thereof all can be used as relatively cheap traffic fuel), with existing energy structure coupling, have broad application prospects.
Methane synthesizing method commonly used is as raw material, to be converted into synthetic gas (H take fossil resource (Sweet natural gas, coal and oil etc.) at present
2With the CO gas mixture), then in synthetic tower in high temperature (350～400 ℃) and high pressure (20～30MPa) and the catalyzer acting in conjunction under synthesizing methanol.This traditional methane synthesizing method is subjected to the thermodynamics of reactions condition restriction, methanol yield is low, also can cause the huge consumption of non-renewable fossil resource, and the existence investment is large, high to equipment requirements, the occupation of land space is large, the production process energy consumption is large, environmental pollution serious and the higher shortcoming of production cost.In recent years, pass through CO
2Hydrogenation (H
2) synthesizing methanol just receiving increasing concern, this method is the CO to discharge in industrial production
2The waste gas that content is high or the CO that captures from atmosphere
2Replacement CO is raw material, certain temperature (220～300 ℃), pressure (in 5～10MPa) synthetic tower, under the copper-based catalysts effect with H
2The reaction synthesizing methanol, its raw materials used CO
2Gas is the abundantest potential carbon source of nature, is also to cause one of main emission gases of Greenhouse effect.Therefore, CO
2Gas hydrogenation (H
2) synthesizing methanol is to CO
2Recycling and eliminate CO
2Harm tool to environment is of great significance, needs elevated pressures and consumes huge energy source and power but this methane synthesizing method is the same with the traditional method of passing through the fossil resource synthesizing methanol, and CO
2Low conversion rate (＜20%) and synthesizing methanol productive rate little (＜12%), and hydrogen used mainly adopts fossil oil preparation, 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 method of efficient, cleaning, economic, the 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, consisted of by 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 consists of the 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 of with layered arrangement cathode support body, electrolytic thin-membrane, anode, described tubular anode chamber is provided with steam entry, and it is catalyst based that described tubular type cathode compartment one side is provided with Cu-Zn.
Described microtubule electrolyzer is that external diameter is the microtubule of 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 μ m.
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 ℃, and the catalyst based work area temperature of Cu-Zn is 200～400 ℃.
The method of above-mentioned a kind of tubular ceramic membrane reactor synthesizing methanol is characterized in that comprising the steps:
The first step: the temperature of microtubule electrolyzer is heated to 400～800 ℃ by tubular type gradient electric furnace;
Second step: the cathode support body of microtubule electrolyzer is connected with the negative pole of direct supply, and the anode of microtubule electrolyzer and the positive pole of direct supply join;
The 3rd step: pass into hydrogen in the tubular type cathode compartment, make the NiO on microtubule cathode of electrolytic tank supporter be reduced to Ni;
The 4th step: after the NiO on microtubule cathode of electrolytic tank supporter reduction was completed, the introducing port by the tubular type cathode compartment passed into CO
2Gas;
The 5th step: the steam entry by the tubular anode chamber is passed into steam-laden Ar gas and carries out decomposition reaction on the anode of microtubule electrolyzer and generate highly active H
+
The 6th step: highly active H
+Transfer on cathode support body and CO by electrolytic thin-membrane
2Gas reacts, synthesizing methanol under normal pressure, and by being derived by the export mouth of tubular type cathode compartment behind Cu-Zn catalyst based zone.
The electrolysis voltage of described microtubule electrolyzer is 1.2～2.5V.
Described methyl alcohol synthesizes required H
+Quantity can by adjust water vapour content in Ar gas, flow rates,
Cell operation temperature, electrolysis voltage are controlled.
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) employing the technology of the present invention can be at normal pressure (～0.1MPa) lower synthesizing methanol, and CO
2Transformation efficiency and methanol yield can be simplified methanol synthesizing process and reduce costs than the obvious raising of prior art;
(2) can transform on a large scale CO
2Be fuel and industrial chemicals, save non-renewable fossil fuel resource, greatly reduce greenhouse gases CO
2Discharge and realize the neutral carbon circulation, to the environment protection important in inhibiting;
(3) in the electric energy and the reaction of heat energy efficient for high-temperature vapour electrolytic hydrogen production ion of being convenient to renewable energy source (sun power, wind energy etc.) or advanced nuclear reactor are provided, finally carry out the synthetic of methyl alcohol, with reduce methyl alcohol synthetic in to the consumption of fossil resource;
(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 of coal or biomass etc.;
(5) methanol yield can reach 25.4%, far above the productive rate of prior art methyl alcohol.
Description of drawings
Accompanying drawing 1 is the structural representation of tubular ceramic membrane reactor cross-section of the present invention.
Embodiment
The present invention will be described in detail below in conjunction with the drawings and specific embodiments:
Embodiment 1
The preparation of electrolytic cell:
(1) adopt NiO and BaZr
0.3Ce
0.5Y
0.16Zn
0.04O
3-δ(BZCYZ) mixture (mass percent is 60%:40%) prepares by the phase inversion process moulding cathode support body 4 that external diameter is 2mm, burns till at 1250 ℃ of insulation 4h after drying;
(2) preparing thickness by vacuum aided immersion coating method on cathode support body 4 is the BaZr of 20 μ m
0.3Ce
0.5Y
0.16Zn
0.04O
3-δ(BZCYZ) electrolytic thin-membrane 5, burn till at 1400 ℃ 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 ℃ of insulation 2h, finally make structure and be: the proton type microtubule electrolytic cell of NiO-BZCYZ/ BZCYZ/LSCF-BZCYZ type.
The structure of tubular ceramic membrane reactor:
Structure is that proton type microtubule electrolyzer 11 internal passagess of NiO-BZCYZ/ BZCYZ/LSCF-BZCYZ are the cathode compartment 3 of reactor, sealing-in sleeve pipe 12 outside with it consists of the anolyte compartment 2 of reactor, sealing-in sleeve pipe 12 is fixed on tubular type gradient electric furnace 1 inside together with internal micro-tubes electrolyzer 11, finally make the tubular ceramic membrane reactor.
Methane synthesizing method:
Adopt the tubular ceramic membrane reactor of structure shown in Figure 1 to carry out methyl alcohol synthetic, 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: be heated to 650 ℃ by tubular type gradient electric furnace 1 temperature with microtubule electrolyzer 11;
Second step: the cathode support body 4 of microtubule electrolyzer 11 is connected with the negative pole of direct supply, and the anode 6 of microtubule electrolyzer 11 joins with the positive pole of direct supply, and the voltage of direct supply is 1.6V;
The 3rd step: pass into hydrogen in tubular type cathode compartment 3, make the NiO on microtubule electrolyzer 11 cathode support bodies 4 be reduced to Ni;
The 4th step: after the NiO on microtubule electrolyzer 11 cathode support bodies 4 reduction was completed, the introducing port 8 by tubular type cathode compartment 3 passed into CO with the speed of 40ml/min
2Gas;
The 5th step: the steam entry 10 by tubular anode chamber 2 is passed into the Ar gas of containing water vapor 20% and carries out decomposition reaction on the anode 6 of microtubule electrolyzer 11 and generate highly active H with the speed of 200ml/min
+
The 6th step: highly active H
+Transfer on cathode support body 4 and CO by electrolytic thin-membrane 5
2Gas reacts, synthesizing methanol gas under normal pressure, and derive by the rear export mouth 9 by tubular type cathode compartment 3 in catalyst based 7 zones of Cu-Zn.
Embodiment 2:
The structure of the preparation of electrolytic cell and tubular ceramic membrane reactor is with embodiment 1.
Methane synthesizing method:
Adopt the tubular ceramic membrane reactor of structure shown in Figure 1 to carry out methyl alcohol synthetic, 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: be heated to 650 ℃ by tubular type gradient electric furnace 1 temperature with microtubule electrolyzer 11;
Second step: the cathode support body 4 of microtubule electrolyzer 11 is connected with the negative pole of direct supply, and the anode 6 of microtubule electrolyzer 11 joins with the positive pole of direct supply, and the voltage of direct supply is 2V;
The 3rd step: pass into hydrogen in tubular type cathode compartment 3, make the NiO on microtubule electrolyzer 11 cathode support bodies 4 be reduced to Ni;
The 4th step: after the NiO on microtubule electrolyzer 11 cathode support bodies 4 reduction was completed, the introducing port 8 by tubular type cathode compartment 3 passed into CO with the speed of 40ml/min
2Gas;
The 5th step: the steam entry 10 by tubular anode chamber 2 is passed into the Ar gas of containing water vapor 30% and carries out decomposition reaction on the anode 6 of microtubule electrolyzer 11 and generate highly active H with the speed of 200ml/min
+
The 6th step: highly active H
+Transfer on cathode support body 4 and CO by electrolytic thin-membrane 5
2Gas reacts, synthesizing methanol gas under normal pressure, and derive by the rear export mouth 9 by tubular type cathode compartment 3 in catalyst based 7 zones of Cu-Zn.
The above only be the better embodiment of the present invention, but protection domain of the present invention is not limited to this, is equal to replacement or changes according to technical scheme of the present invention and inventive concept thereof, within all should being encompassed in protection scope of the present invention.
Claims (10)
1. tubular ceramic membrane reactor, by tubular type gradient electric furnace (1), microtubule electrolyzer (11), sealing-in sleeve pipe (12) consists of, described microtubule electrolyzer (11) internal passages is cathode compartment (3), described microtubule electrolyzer (11) sealing-in sleeve pipe outside with it (12) consists of anolyte compartment (2), described sealing-in sleeve pipe (12) is arranged on tubular type gradient electric furnace (1) inside, it is characterized in that: described microtubule electrolyzer (11) is by cathode support body (4), electrolytic thin-membrane (5), anode (6) consists of with layered arrangement, described tubular anode chamber is provided with steam entry (10), described tubular type cathode compartment (3) one sides are provided with Cu-Zn catalyst based (7).
2. a kind of tubular ceramic membrane reactor according to claim 1, it is characterized in that: described microtubule electrolyzer (11) is the microtubule of 2～3mm for external diameter.
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, it 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, it is characterized in that: the thickness of described microtubule electrolyzer (11) anode (6) is 20～40 μ m.
6. a kind of tubular ceramic membrane reactor according to claim 5, it is characterized in that: 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%.
7. a kind of tubular ceramic membrane reactor according to claim 1, it 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
8. a kind of tubular ceramic membrane reactor according to claim 1, it is characterized in that: the work area temperature of described microtubule electrolyzer (11) is 400～800 ℃, the work area temperature of Cu-Zn catalyst based (7) is 200～400 ℃.
9. the method for according to claim 1-8 arbitrary described a kind of tubular ceramic membrane reactor synthesizing methanols, is characterized in that comprising the steps:
The first step: the temperature of microtubule electrolyzer (11) is heated to 400～800 ℃ by tubular type gradient electric furnace (1);
Second step: the cathode support body (4) of microtubule electrolyzer (11) is connected with the negative pole of direct supply, and the anode (6) of microtubule electrolyzer (11) joins with the positive pole of direct supply;
The 3rd step: pass into hydrogen in tubular type cathode compartment (3), make the NiO on microtubule electrolyzer (11) cathode support body (4) be reduced to Ni;
The 4th step: after the NiO on microtubule electrolyzer (11) cathode support body (4) reduction was completed, the introducing port (8) by tubular type cathode compartment (3) passed into CO
2Gas;
The 5th step: the steam entry (10) by tubular anode chamber (2) is passed into steam-laden Ar gas and carries out decomposition reaction on the anode (6) of microtubule electrolyzer (11) and generate highly active H
+
The 6th step: highly active H
+Transfer to cathode support body (4) upward and CO by electrolytic thin-membrane (5)
2Gas reacts, synthesizing methanol under normal pressure, and derive by the rear export mouth (9) by tubular type cathode compartment (3) in Cu-Zn catalyst based (7) zone.
10. the method for a kind of tubular ceramic membrane reactor synthesizing methanol according to claim 9, it is characterized in that: the electrolysis voltage of described microtubule electrolyzer (11) is 1.2～2.5V.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103613067A (en) * | 2013-11-22 | 2014-03-05 | 山东理工大学 | Method for preparing synthetic gas from wet carbon dioxide by electrocatalysis |
| CN105200448A (en) * | 2015-09-30 | 2015-12-30 | 大连理工大学 | Electrochemistry hydrogen pump dual reactor for organic matter dehydrogenation and hydrogenation coupling |
| CN105220172A (en) * | 2015-10-27 | 2016-01-06 | 中国科学技术大学 | A kind of carbonic acid gas and water vapour gas mixture are converted into tubular structure of the gas being rich in methane and its preparation method and application |
| DE102015211391A1 (en) * | 2015-06-19 | 2016-12-22 | Technische Universität Dresden | DEVICE FOR SYNTHESIS OF HYDROGEN-CONTAINING COMPOUNDS |
| CN109529851A (en) * | 2018-12-26 | 2019-03-29 | 大连海事大学 | A kind of Supported Nickel Catalyst and utilize its plasma-catalytic CO2Preparing methanol by hydrogenation method |
| CN111359543A (en) * | 2020-05-11 | 2020-07-03 | 信阳学院 | Metal ceramic membrane reactor for natural gas conversion |
| CN112760671A (en) * | 2020-12-22 | 2021-05-07 | 广东工业大学 | Methanol synthesis method based on mixed ion conductor membrane reactor and application thereof |
Citations (7)
| 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 |
| US20110053046A1 (en) * | 2009-08-31 | 2011-03-03 | Jae Hyoung Gil | Structure of solid oxide fuel cell |
| 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 |
-
2013
- 2013-03-06 CN CN201310070960.0A patent/CN103103556B/en not_active Expired - Fee Related
Patent Citations (7)
| 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 |
| US20110053046A1 (en) * | 2009-08-31 | 2011-03-03 | Jae Hyoung Gil | Structure of solid oxide fuel cell |
| 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−ı electrolyte-based proton-conducting solid oxide fuel cells by gel-casting and suspension spray", 《JOURNAL OF ALLOYS AND COMPOUND》, vol. 478, 13 December 2008 (2008-12-13) * |
| YU LIU ET AL.: "Fabrication and characterization of micro-tubular cathode-supported SOFC for intermediate temperature operation", 《JOURNAL OF POWER SOURCES》, vol. 174, 6 September 2007 (2007-09-06) * |
| 谭小耀 等: "中空纤维陶瓷透氧膜反应器", 《山东理工大学学报》, vol. 20, no. 1, 31 January 2006 (2006-01-31) * |
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|---|---|---|---|---|
| CN103613067A (en) * | 2013-11-22 | 2014-03-05 | 山东理工大学 | Method for preparing synthetic gas from wet carbon dioxide by electrocatalysis |
| 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 |
| DE102015211391A1 (en) * | 2015-06-19 | 2016-12-22 | Technische Universität Dresden | DEVICE FOR SYNTHESIS OF HYDROGEN-CONTAINING COMPOUNDS |
| CN105200448A (en) * | 2015-09-30 | 2015-12-30 | 大连理工大学 | Electrochemistry hydrogen pump dual reactor for organic matter dehydrogenation and hydrogenation coupling |
| 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 |
| CN105220172A (en) * | 2015-10-27 | 2016-01-06 | 中国科学技术大学 | A kind of carbonic acid gas and water vapour gas mixture are converted into tubular structure of the gas being rich in methane and its preparation method and application |
| 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 |
| CN109529851A (en) * | 2018-12-26 | 2019-03-29 | 大连海事大学 | A kind of Supported Nickel Catalyst and utilize its plasma-catalytic CO2Preparing methanol by hydrogenation method |
| 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 |
| CN112760671A (en) * | 2020-12-22 | 2021-05-07 | 广东工业大学 | Methanol synthesis method based on mixed ion conductor membrane reactor and application thereof |
| 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 |
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