CN103525466A - Method and device for indirectly liquefying coal and separating carbon dioxide - Google Patents
Method and device for indirectly liquefying coal and separating carbon dioxide Download PDFInfo
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- CN103525466A CN103525466A CN201310497294.9A CN201310497294A CN103525466A CN 103525466 A CN103525466 A CN 103525466A CN 201310497294 A CN201310497294 A CN 201310497294A CN 103525466 A CN103525466 A CN 103525466A
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- reactor
- fischer
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- tropsch synthesis
- hydrogen production
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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
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
Abstract
The invention discloses a method and a device indirectly liquefying coal and separating carbon dioxide. The device comprises a gasification furnace, a purification device, a Fischer-Tropsch synthesis reactor, an oil wash tower, a gas scrubbing knockout tower, a chemical chain hydrogen production device and a compressor, wherein the chemical chain hydrogen production device comprises a vapour reactor, a fuel reactor, and an air reactor. Coal, oxygen and vapour are fed into the gasification furnace and react to generate coarse coal gas, dust and acid gases including H2S, COS and CO2 in the coarse coal gas are removed by the purification device, purified coarse coal gas, hydrogen made by the chemical chain hydrogen production device and cycle gas are mixed and taken as the synthesis gas of the Fischer-Tropsch synthesis reactor, the synthesis products of the Fischer-Tropsch synthesis reactor are wax, heavy oil, light oil and purge gas, wax is dissolved out in the Fischer-Tropsch synthesis reactor, the heavy oil is dissolved out in the oil wash tower, the light oil is dissolved out in the gas scrubbing knockout tower, 2/3 of purge gas is recycled as cycle gas of the system by the compressor, and the left purge gas enters the chemical chain hydrogen production device for making hydrogen.
Description
Technical field
The method and the device that the present invention relates to a kind of ICL for Indirect Coal Liquefaction, relate in particular to the expense based on iron-based oxygen carrier
Holder synthetic speed to exit chain type hydrogen manufacturing separation of C O
2method and device.
Background technology
Coal is the abundantest fossil oil that can access on the earth, and the working life of coal, it will be the reliable energy that substitutes continuous decline petroleum resources higher than oil.Gasification produces synthetic gas (CO+H
2), then by the process that synthetic gas is synthetic liquid fuel or chemical products, be called the indirect liquefaction of coal.ICL for Indirect Coal Liquefaction mainly adopts Fischer-Tropsch synthesis device to generate various hydro carbons and oxygenatedchemicals, and Fischer-Tropsch synthesis device requires H in unstripped gas
2/ CO is 1.2～1.5, and in gasification generation raw gas, carbon monoxide content is more much higher than hydrogen, can not directly be applicable to the needs of synthetic gas, the part carbon monoxide in raw gas need be changed into hydrogen, adjusts H
2/ CO ratio.Traditional ICL for Indirect Coal Liquefaction liquefaction adopts conversion and PSA device for producing hydrogen to improve H in synthetic gas
2the ratio of/CO, but these two kinds of devices exist facility investment large, the shortcoming that energy consumption is high, therefore, find a kind of hydrogen production process of less energy-consumption, contribute to reduction and the large-scale promotion of the energy consumption of ICL for Indirect Coal Liquefaction technique, to reducing the dependence of petroleum-based energy, have important realistic meaning and strategic importance.
Summary of the invention
Technical problem: the invention provides a kind of raising fischer-tropsch reaction synthetic gas H
2/ CO ratio, has simplified ICL for Indirect Coal Liquefaction technique, has reduced energy consumption, simultaneously high efficiency separation CO
2, ICL for Indirect Coal Liquefaction the separation of C O of minimizing greenhouse gas emission
2method, a kind of device of realizing aforesaid method is provided simultaneously.
Technical scheme: ICL for Indirect Coal Liquefaction of the present invention separation of C O
2method, comprise following flow process:
Coal, oxygen and water vapour are passed in vapourizing furnace, and under 800～1800 ℃, 0.1～4MPa condition, reaction generates raw gas, and the composition of raw gas comprises H
2, CO, CO
2, H
2s, COS and CH
4, H wherein
2account for raw gas volume percent more than 60% with CO; Raw gas enters in refining plant, by low-temp methanol method, removes dust and the sour gas H in raw gas
2s, COS, CO
2, the raw gas H after purification
2s content is lower than 0.1ppm, CO
2content is lower than 20ppm.
Raw gas is delivered to Fischer-Tropsch synthesis device from refining plant, the venting of speeding that the hydrogen simultaneously making to Fischer-Tropsch synthesis device conveying hydrogen production of chemical chain device and gas scrubbing knockout tower reclaim, the hydrogen that wherein raw gas and hydrogen production of chemical chain device make accounts for 1/3 of Fischer-Tropsch synthesis device inlet mouth gas mixture volume, and the venting of speeding that gas scrubbing knockout tower reclaims accounts for 2/3 of Fischer-Tropsch synthesis device inlet mouth gas mixture volume.Fischer-Tropsch synthesis device adopts ferrum-based catalyst, temperature of reaction is 260～330 ℃, pressure is 2～3MPa, carrying out the synthetic product that Fischer-Tropsch synthesis obtains is wax, heavy oil, lightweight oil and the venting of speeding, and wherein 300～500 ℃ of the boiling points of wax, are in a liquid state, wax precipitation from Fischer-Tropsch synthesis device bottom, the heavy oil of gaseous state, lightweight oil and the venting of speeding enter in oil scrubber and gas scrubbing knockout tower successively, and heavy oil is separated out in oil scrubber, and light oil is at gas scrubbing knockout tower condensation; The inlet mouth that is circulated to Fischer-Tropsch synthesis device is reclaimed in more than 2/3 venting of speeding through compressor from gas scrubbing knockout tower, all the other venting of speeding enter in the fuel reactor of hydrogen production of chemical chain device.
In fuel reactor, under 800～950 ℃ of conditions, venting and preset Fe speed
2o
3reaction, generates CO
2, water vapour and FeO, wherein CO
2discharge from fuel reactor top with water vapour, FeO enters in the water vapour reactor of hydrogen production of chemical chain device, and under 800～950 ℃ of conditions, FeO reacts with water vapour and generates H
2and Fe
3o
4, H wherein
2be delivered to the inlet mouth of Fischer-Tropsch synthesis device, Fe
3o
4enter in the air reactor of hydrogen production of chemical chain device; Fe
3o
4enter after air reactor, under 800～950 ℃ of conditions, generate Fe with air reaction
2o
3with oxygen debt air, oxygen debt air is discharged from air reactor top, Fe
2o
3be delivered in fuel reactor, realize Fe
2o
3recycle.
ICL for Indirect Coal Liquefaction of the present invention separation of C O
2device, comprise the vapourizing furnace, refining plant, Fischer-Tropsch synthesis device, oil scrubber and the gas scrubbing knockout tower that by reaction sequence, connect successively, and be connected, provide reaction required hydrogen production of chemical chain device with the inlet mouth of Fischer-Tropsch synthesis device, be connected, realize the compressor of the deflation cycles reuse of speeding with the inlet mouth of Fischer-Tropsch synthesis device with the venting port of gas scrubbing knockout tower.
Hydrogen production of chemical chain device comprises water vapour reactor, fuel reactor and air reactor, the inlet mouth of fuel reactor is connected with the venting port of gas scrubbing knockout tower, discharge port is connected with the opening for feed of water vapour reactor, the venting port of water vapour reactor is connected with the inlet mouth of Fischer-Tropsch synthesis device, the returning charge mouth of water vapour reactor is connected with the opening for feed of air reactor, and the discharge port of air reactor is connected with the opening for feed of fuel reactor.
The present invention adopts hydrogen production of chemical chain device to substitute conversion and PSA device for producing hydrogen in traditional ICL for Indirect Coal Liquefaction, and the hydrogen making of exitting of speeding that utilizes fischer-tropsch reactor to obtain improves fischer-tropsch reaction synthetic gas H
2/ CO ratio.Compare with original device, simplified ICL for Indirect Coal Liquefaction technique, reduced energy consumption, simultaneously high efficiency separation CO
2, reduce greenhouse gas emission.
Beneficial effect: compared with prior art, tool of the present invention has the following advantages:
Traditional ICL for Indirect Coal Liquefaction liquefaction adopts conversion and PSA device for producing hydrogen to improve H in synthetic gas
2the ratio of/CO, wherein, changing device principal reaction is:
COS+H
2O→CO
2+H
2S
CO+H
2O→CO
2+H
2
Owing to there being strongly-acid product H in changing device
2s, shift-converter need to adopt acid-resistant stainless steel, and acid-resistant stainless steel fancy price has increased the cost of changing device equipment.The ICL for Indirect Coal Liquefaction factory of industrial scale 480,000 t/a, changing device need to consume recirculated cooling water 500～600m
3/ h, consumes electricity 400～500KW, consumes de-salted water 250～300t/h, transformation catalyst 8～10t/a.
PSA device for producing hydrogen can be realized the hydrogen extraction yield of 85% left and right, device is comprised of a plurality of adsorption towers, gas is at high pressure 2～3MPa, under the condition of temperature≤40 ℃, from tower bottom, enter adsorption tower, impurity is partly adsorbed agent absorption, hydrogen is difficult to absorption discharges from the top of tower, and adsorbent impurity part is regenerated, and at the bottom of tower, discharges.The ICL for Indirect Coal Liquefaction factory PSA device for producing hydrogen of industrial scale 480,000 t/a needs power consumption 500～600KW.
In the present invention, hydrogen production of chemical chain device adopts iron-based oxygen carrier, and the reduction reaction that iron-based oxygen carrier occurs in fuel reactor is as follows:
From fuel reactor gaseous product out, be only carbonic acid gas and water vapour, by the cooling separable pure carbonic acid gas that goes out, the ferriferous oxide being reduced enters in water vapour reactor oxidizing reaction occurs, and reacts as follows:
The gaseous product that water vapour reactor generates is only hydrogen and water vapour, by the cooling separable pure hydrogen that goes out, higher than the hydrogen extraction yield of PSA device, in order to improve the oxygen carrier rate of ferriferous oxide, Fe in water vapour reactor
3o
4with air reaction, be further oxidized to Fe
2o
3, there is reaction as follows:
The oxidation and the reduction reaction formula that from hydrogen production of chemical chain device ferriferous oxide, occur, the heat that the heat that hydrogen production of chemical chain process discharges and fuel and oxygen direct fuel discharge is thought same, angle from energy balance, hydrogen production of chemical chain device does not need external energy in operation, the angle of utilizing from energy, hydrogen production of chemical chain process heat transfer temperature difference is little, burning
lose little.In actually operating, hydrogen production of chemical chain device is normal pressure equipment, equipment cost is low, compare with PSA device for producing hydrogen with changing device, the ICL for Indirect Coal Liquefaction factory of industrial scale 480,000 t/a, oxygen carrier consumption≤0.5t/a, power consumption derives from utility appliance (blower fan, water pump and instrument etc.).Therefore, the energy expenditure of hydrogen production of chemical chain device and equipment cost are less than changing device and PSA device for producing hydrogen.
Accompanying drawing explanation
Fig. 1 is a kind of ICL for Indirect Coal Liquefaction of the present invention separation of C O
2the principle schematic of device.
Embodiment
Below in conjunction with embodiment and Figure of description, the present invention is further described in detail.
ICL for Indirect Coal Liquefaction of the present invention separation of C O
2method, comprise following flow process:
Coal, oxygen and water vapour are passed in vapourizing furnace 1, and under 800～1800 ℃, 0.1～4MPa condition, reaction generates raw gas, and the main component of raw gas comprises H
2, CO, CO
2, H
2s, COS and CH
4, H wherein
2account for raw gas volume percent more than 60% with CO, but in raw gas, also there is the impurity such as dust particle, tar steam, water vapour, sulfide and carbonic acid gas, these impurity cause Fischer-Tropsch synthesis catalyst deactivation, therefore raw gas enters in refining plant 2, by low-temp methanol method, removes dust and sour gas H in raw gas
2s, COS, CO
2the sour gas that low-temp methanol washing removes in raw gas is a physical absorption and desorption process, under 2～7MPa ,-30～-70 ℃ of conditions, the impurity such as the sulfide in raw gas and carbonic acid gas are dissolved in polar solvent methyl alcohol, and after step-down, they easily desorb again from solution, adopt low-temp methanol washing to remove raw gas H
2s content is lower than 0.1ppm, CO
2content is lower than 20ppm.
Raw gas is delivered to Fischer-Tropsch synthesis device 3 from refining plant 2, the venting of speeding that the hydrogen simultaneously being made by raw gas and hydrogen production of chemical chain device 6 to 3 conveyings of Fischer-Tropsch synthesis device and gas scrubbing knockout tower 5 reclaim, the hydrogen that wherein raw gas and hydrogen production of chemical chain device 6 make accounts for 1/3 of Fischer-Tropsch synthesis device 3 inlet mouth gas mixture volumes, the venting of speeding that gas scrubbing knockout tower 5 reclaims, accounts for 2/3 of Fischer-Tropsch synthesis device 3 inlet mouth gas mixture volumes.
Select fixed bed as Fischer-Tropsch synthesis device 3, fixed-bed reactor are shell-and-tubes, and catalyzer is housed in pipe, pass into the water coolant of boiling between pipe, remove reaction heat.Fischer-Tropsch synthesis device 3 is selected activation precipitated iron catalyst, temperature of reaction is 260～330 ℃, pressure is 2～3MPa, carries out Fischer-Tropsch synthesis, and the synthetic product obtaining is wax, heavy oil, lightweight oil and the venting of speeding, 300～500 ℃ of the boiling points of wax wherein, be in a liquid state, wax precipitation from Fischer-Tropsch synthesis device 3 bottoms, the heavy oil of gaseous state, lightweight oil and the venting of speeding enter in oil scrubber 4 and gas scrubbing knockout tower 5 successively, heavy oil is separated out in oil scrubber 4, and light oil is at gas scrubbing knockout tower 5 condensations; More than 2/3 venting of speeding reclaims through compressor 7 inlet mouth that is circulated to Fischer-Tropsch synthesis device 3 from gas scrubbing knockout tower 5, and all the other venting of speeding enter in the fuel reactor 6-2 of hydrogen production of chemical chain device 6.
Hydrogen production of chemical chain device 6 adopts Fe
2o
3as oxygen carrier, fuel reactor 6-2 selects fixed bed form, adopts gas-solid adverse current form, and in fuel reactor 6-2, under 800～950 ℃ of conditions, the venting of speeding enters and preset Fe from fixed bed bottom
2o
3reaction, generates gaseous product CO
2, water vapour, solid product FeO and Fe
3o
4, CO
2from fuel reactor 6-2 top, discharge FeO and Fe with water vapour
3o
4enter in the water vapour reactor 6-1 of hydrogen production of chemical chain device 6; Water vapour reactor 6-1 selects bubbling fluidized bed form, and water vapour enters from water vapour reactor 6-1 bottom, and under 800～950 ℃ of conditions, FeO reacts with water vapour and generates H
2and Fe
3o
4, H wherein
2from water vapour reactor 6-1 bottom, discharge, be delivered to the inlet mouth of Fischer-Tropsch synthesis device 3, Fe
3o
4enter in the air reactor 6-3 of hydrogen production of chemical chain device 6; Air reactor 6-3 selects circulating fluidized bed form, and air enters from air reactor 6-3 bottom, under 800～950 ℃ of conditions, and Fe
3o
4generate Fe with air reaction
2o
3with oxygen debt air, oxygen debt air is discharged from air reactor 6-2 top, Fe
2o
3be delivered in fuel reactor 6-2, realize Fe
2o
3recycle.
Above-mentioned ICL for Indirect Coal Liquefaction the separation of C O of realizing of the present invention
2the device of method, comprises the vapourizing furnace 1, refining plant 2, Fischer-Tropsch synthesis device 3, oil scrubber 4 and the gas scrubbing knockout tower 5 that by reaction sequence, connect successively, and is connected, provides reaction required H with the inlet mouth of Fischer-Tropsch synthesis device 3
2hydrogen production of chemical chain device 6, be connected, realize the compressor 7 of the deflation cycles reuse of speeding with the inlet mouth of Fischer-Tropsch synthesis device 3 with the venting port of gas scrubbing knockout tower 5.Hydrogen production of chemical chain device 6 comprises water vapour reactor 6-1, fuel reactor 6-2 and air reactor 6-3, the inlet mouth of fuel reactor 6-2 is connected with the venting port of gas scrubbing knockout tower 5, discharge port is connected with the opening for feed of water vapour reactor 6-1, the venting port of water vapour reactor 6-1 is connected with the inlet mouth of Fischer-Tropsch synthesis device 3, the returning charge mouth of water vapour reactor 6-1 is connected with the opening for feed of air reactor 6-3, and the discharge port of air reactor 6-3 is connected with the opening for feed of fuel reactor 6-2.
Claims (2)
1. a method for ICL for Indirect Coal Liquefaction separating carbon dioxide, is characterized in that, the method comprises following flow process:
Coal, oxygen and water vapour are passed in vapourizing furnace (1), and under 800～1800 ℃, 0.1～4MPa condition, reaction generates raw gas, and the composition of described raw gas comprises H
2, CO, CO
2, H
2s, COS and CH
4, H wherein
2account for raw gas volume percent more than 60% with CO; Raw gas enters in refining plant (2), by low-temp methanol method, removes dust and the sour gas H in raw gas
2s, COS, CO
2, the raw gas H after purification
2s content is lower than 0.1ppm, CO
2content is lower than 20ppm;
Raw gas is delivered to Fischer-Tropsch synthesis device (3) from refining plant (2), the venting of speeding that the hydrogen simultaneously making to Fischer-Tropsch synthesis device (3) conveying hydrogen production of chemical chain device (6) and gas scrubbing knockout tower (5) reclaim, the hydrogen that wherein raw gas and hydrogen production of chemical chain device (6) make accounts for 1/3 of Fischer-Tropsch synthesis device (3) inlet mouth gas mixture volume, the venting of speeding that gas scrubbing knockout tower (5) reclaims, accounts for 2/3 of Fischer-Tropsch synthesis device (3) inlet mouth gas mixture volume; Fischer-Tropsch synthesis device (3) adopts ferrum-based catalyst, temperature of reaction is 260～330 ℃, pressure is 2～3MPa, carry out Fischer-Tropsch synthesis, the synthetic product obtaining is wax, heavy oil, lightweight oil and the venting of speeding, 300～500 ℃ of the boiling points of wax wherein, be in a liquid state, wax precipitation from Fischer-Tropsch synthesis device (3) bottom, the heavy oil of gaseous state, lightweight oil and the venting of speeding enter in oil scrubber (4) and gas scrubbing knockout tower (5) successively, heavy oil is separated out in oil scrubber (4), and light oil is at gas scrubbing knockout tower (5) condensation; The inlet mouth that is circulated to Fischer-Tropsch synthesis device (3) is reclaimed in more than 2/3 venting of speeding through compressor (7) from gas scrubbing knockout tower (5), all the other venting of speeding enter in the fuel reactor (6-2) of hydrogen production of chemical chain device (6);
In fuel reactor (6-2), under 800～950 ℃ of conditions, venting and preset Fe speed
2o
3reaction, generates CO
2, water vapour and FeO, wherein CO
2discharge from fuel reactor (6-2) top with water vapour, FeO enters in the water vapour reactor (6-1) of hydrogen production of chemical chain device (6), and under 800～950 ℃ of conditions, FeO reacts with water vapour and generates H
2and Fe
3o
4, H wherein
2be delivered to the inlet mouth of Fischer-Tropsch synthesis device (3), Fe
3o
4enter in the air reactor (6-3) of hydrogen production of chemical chain device (6); Fe
3o
4enter after air reactor (6-3), under 800～950 ℃ of conditions, generate Fe with air reaction
2o
3with oxygen debt air, described oxygen debt air is discharged from air reactor (6-2) top, Fe
2o
3be delivered in fuel reactor (6-2), realize Fe
2o
3recycle.
2. a device of realizing ICL for Indirect Coal Liquefaction described in claim 1 separating carbon dioxide method, it is characterized in that, this device comprises vapourizing furnace (1), refining plant (2), Fischer-Tropsch synthesis device (3), oil scrubber (4) and the gas scrubbing knockout tower (5) connecting successively by reaction sequence, and is connected, provides reaction required H with the inlet mouth of described Fischer-Tropsch synthesis device (3)
2hydrogen production of chemical chain device (6), be connected, realize the compressor (7) of the deflation cycles reuse of speeding with the inlet mouth of Fischer-Tropsch synthesis device (3) with the venting port of gas scrubbing knockout tower (5);
Hydrogen production of chemical chain device (6) comprises water vapour reactor (6-1), fuel reactor (6-2) and air reactor (6-3), the inlet mouth of described fuel reactor (6-2) is connected with the venting port of gas scrubbing knockout tower (5), discharge port is connected with the opening for feed of water vapour reactor (6-1), the venting port of water vapour reactor (6-1) is connected with the inlet mouth of Fischer-Tropsch synthesis device (3), the returning charge mouth of water vapour reactor (6-1) is connected with the opening for feed of air reactor (6-3), the discharge port of air reactor (6-3) is connected with the opening for feed of fuel reactor (6-2).
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|---|---|---|---|
| CN201310497294.9A CN103525466A (en) | 2013-10-22 | 2013-10-22 | Method and device for indirectly liquefying coal and separating carbon dioxide |
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|---|---|---|---|
| CN201310497294.9A CN103525466A (en) | 2013-10-22 | 2013-10-22 | Method and device for indirectly liquefying coal and separating carbon dioxide |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104194834A (en) * | 2014-07-11 | 2014-12-10 | 中国科学院广州能源研究所 | Device for biomass pyrolysis and chemical-looping hydrogen production by utilizing biomass pyrolysis gas |
| CN104974780A (en) * | 2015-06-09 | 2015-10-14 | 武汉凯迪工程技术研究总院有限公司 | Chloralkali and Fischer-Tropsch synthesis integrated utilization adjustment process and equipment |
| CN105540539A (en) * | 2014-11-03 | 2016-05-04 | 中国石油化工股份有限公司 | Method and apparatus for simultaneously preparing hydrogen and liquid-state fuel |
| TWI572562B (en) * | 2016-05-26 | 2017-03-01 | 行政院原子能委員會核能研究所 | Reactor of Hydrocarbon Fuel Having Space Efficiency for Separating and Purifying Carbon Dioxide |
| CN112919408A (en) * | 2019-12-05 | 2021-06-08 | 中国石油化工股份有限公司 | Hydrogen production system and method, gas supply system, and hydrogen station |
-
2013
- 2013-10-22 CN CN201310497294.9A patent/CN103525466A/en active Pending
Non-Patent Citations (1)
| Title |
|---|
| LIANGSHIH FAN ET AL.: "Utilization of chemical looping strategy in coal gasification processes", 《PARTICUOLOGY》 * |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104194834A (en) * | 2014-07-11 | 2014-12-10 | 中国科学院广州能源研究所 | Device for biomass pyrolysis and chemical-looping hydrogen production by utilizing biomass pyrolysis gas |
| CN104194834B (en) * | 2014-07-11 | 2016-05-25 | 中国科学院广州能源研究所 | A kind of biomass pyrolytic and biomass pyrogenation gasification are learned the device of chain hydrogen manufacturing |
| CN105540539A (en) * | 2014-11-03 | 2016-05-04 | 中国石油化工股份有限公司 | Method and apparatus for simultaneously preparing hydrogen and liquid-state fuel |
| CN105540539B (en) * | 2014-11-03 | 2018-04-10 | 中国石油化工股份有限公司 | A kind of while hydrogen manufacturing and the method and apparatus of liquid fuel |
| CN104974780A (en) * | 2015-06-09 | 2015-10-14 | 武汉凯迪工程技术研究总院有限公司 | Chloralkali and Fischer-Tropsch synthesis integrated utilization adjustment process and equipment |
| CN104974780B (en) * | 2015-06-09 | 2017-03-08 | 武汉凯迪工程技术研究总院有限公司 | Chlor-alkali adjusts technique and its equipment with F- T synthesis comprehensive utilization |
| TWI572562B (en) * | 2016-05-26 | 2017-03-01 | 行政院原子能委員會核能研究所 | Reactor of Hydrocarbon Fuel Having Space Efficiency for Separating and Purifying Carbon Dioxide |
| CN112919408A (en) * | 2019-12-05 | 2021-06-08 | 中国石油化工股份有限公司 | Hydrogen production system and method, gas supply system, and hydrogen station |
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Application publication date: 20140122 |