CN105477978A - Method for enabling tail gas discharge of reaction circulation gas decarbonization to reach environmental protection index - Google Patents
Method for enabling tail gas discharge of reaction circulation gas decarbonization to reach environmental protection index Download PDFInfo
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- CN105477978A CN105477978A CN201410468469.8A CN201410468469A CN105477978A CN 105477978 A CN105477978 A CN 105477978A CN 201410468469 A CN201410468469 A CN 201410468469A CN 105477978 A CN105477978 A CN 105477978A
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
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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
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- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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Abstract
The invention discloses a method for enabling tail gas discharge of decarbonizing solution regeneration to reach an environmental protection index, after CO2 is removed from synthetic circulation gas containing a large amount of organic matters. After circulation gas decarbonization is performed under the absolute pressure of 1.0-8.0 MPa, a process of desorbing an absorbing pregnant solution comprises medium-pressure flash evaporation, low-pressure flash evaporation and air stripping, and boiling regeneration. Based on the value of the absorption pressure, the medium-pressure flash evaporation can be divided into one-stage or two-stage flash evaporation. A last-stage flash evaporation is performed under the absolute pressure ranging from 0.75-1.6 MPa for separation of H2, CO, and low-carbon hydrocarbons. The low-pressure flash evaporation is carried out under the absolute pressure ranging from 0.1-0.35 MPa, aim at ensuring the relieving rate and concentration of non-methane in the regeneration gas to meet environmental requirements during a process of processing the pregnant solution after flash evaporation into a barren solution through air stripping with a regeneration tower and boiling desorption.
Description
Technical field
The invention belongs to atmospheric environment protection field, be specifically related to a kind ofly removing CO from the synthetic cyclic gas containing large amount of organic
2after, regeneration of waste liquor exhaust emissions reaches the method for environmental protection index.
Background technology
Accessory substance CO can be generated in some courses of reaction
2, in order to prevent CO
2accumulation, need CO in gas after reflecting tower tail gas separation product
2be removed to below index and send reactor back to again, Here it is reaction cycle gas decarbonization.Such as, CO and H
2synthin (oil product) F-T synthesis, has accessory substance CO
2generate.Tail gas after being separated by oil product send decarburization unit to remove CO
2, circulating air returns F-T synthesis.Again such as, O
2and C
2h
4the oxidation reaction of (ethene), also generates accessory substance CO
2.The tail gas being separated oxirane removes CO
2after, circulating air returns oxidative synthesis.Propylene oxidation generates expoxy propane, ethylene process produces vinyl acetate etc., has circulating air to remove CO
2process.
This class circulating air decarburization, because gas composition is complicated, is only suitable for the decarbonization process adopting hot wet chemical, decarbonizing solution desorb release CO
2after, recycle.Owing to there being a small amount of CO in absorption process
2other gas dissolutions in addition more than 99% are CO in the regeneration gas of therefore desorb except water vapour
2, also have the gas of a small amount of environmental protection limiting emission, such as non-methane hydrocarbon, although rate of discharge is less than environmental protection index 100kg/h(aiutage height 40 meters), concentration index 120mg/m
3be difficult to reach.
Emission gases way up to standard can be made at present to have " burning method " and " catalytic oxidation ", and the former is after supplementary a certain amount of air, and in incinerator, temperature is 800 ~ 1100 DEG C and is thoroughly burnouted by combustible; The latter is after supplementary a certain amount of air, at palladium-platinum catalyst temperature is 350 ~ 550 DEG C, is CO by hydrocarbon oxidation
2and water.These methods are more applicable for medium and small device, for discharge tolerance be five ten thousand steres, ten ten thousand steres, the even large-scale and super-huge device of 20 ten thousand steres, in order to removing per hour tens kilograms of non-methane hydrocarbons, not only need to drop into up to ten million unit and build incinerator or Catalytic oxidation furnace; And also need kilostere natural gas on supplementary hundreds of per hour to burn because calorific value is too low.Extremely unreasonable economically, enterprise is also difficult to bear.
Therefore, the new regeneration of waste liquor exhaust emissions that can make of exploitation is needed to reach the method for environmental protection index.
Summary of the invention
The object of the invention is reach environmental protection index for reaction cycle gas decarbonization exhaust emissions and the technology proposed.
Main technical schemes of the present invention: reaction cycle gas decarbonization exhaust emissions reaches the method for environmental protection index, it is characterized in that under 1.0 ~ 8.0MPa (absolute pressure) after circulating air decarburization, press flash distillation, low pressure flash and air lift in the desorption process employing of absorption rich solution, boil regeneration; Middle pressure flash distillation is divided into one-level or double flash evaporation to be separated H
2, CO and low-carbon (LC) hydro carbons, low pressure flash pressure is 0.1 ~ 0.35MPa (absolute pressure), ensures that the rich solution after flash distillation meets environmental requirement through regenerator air lift, the regeneration gas of boiling desorb and becoming the release of lean solution process.
The inventive method has following characteristics:
(1) absorption of gas: circulating air pressure of decarburization can in 1.0 ~ 8.0MPa (absolute pressure) according to differential responses design, and this gas is except CO
2outside carbonate solution reactive absorption, other gas flows various dissolved under different absorption pressure are different, therefore, absorb rich solution and are made up of different.
(2) the middle pressure flash distillation of rich solution: absorption pressure is under the condition of more than 4.0MPa (absolute pressure), and middle pressure flash distillation can point two-stage be carried out, and first order flashing pressure is 2.0 ~ 3.5MPa (absolute pressure), is separated H
2, CO and low-carbon (LC) hydro carbons reclaim; Second level flashing pressure determines decarburization rich solution flash tank pressure according to desorber height (being generally 40 ~ 100 meters) and low voltage operated pressure, this pressure is generally 0.75 ~ 1.6MPa (absolute pressure), rich solution after this pressure must ensure flash distillation oneself can be pressed onto regeneration overhead low-pressure flashing tank, does not need to use pump supercharging.CO in the gas that middle pressure rich solution flashes off
2lower with water vapor concentration, H
2, CO, the gas such as various hydro carbons and other aldehyde, ketone, acid, alcohol is many, flashed vapour, after washing section cooling in flash tank top is separated, directly can send gas ductwork; Also can determine whether to be worth by compressor retrieval system according to gas composition.
(3) low pressure flash of rich solution: therefrom press flash tank rich solution to be out sent to the low pressure flash section at regenerator top, flashing pressure needs analog computation to determine, this pressure is 0.1 ~ 0.35MPa (absolute pressure), and target ensures that the rich solution after flash distillation meets environmental requirement through regenerator air lift, the regeneration gas of boiling desorb and becoming the release of lean solution process.That is, low pressure flash is sufficiently abundant, and harmful components remaining in solution after flash distillation are enough low.In order to flash distillation is thorough, a certain amount of technique inert gas with pressure can be passed into from flash drum bottom if desired.Simultaneously under the prerequisite meeting standard, low pressure flash pressure is higher as far as possible, to reduce CO
2with the concentration of water vapour, improve low pressure flash gases value.
(4) process of low pressure flash gas: the whereabouts of low pressure flash gas, mainly according to its composition, can be recycled; Also gas ductwork or relevant boiler can be sent according to calorific value is high; Calorific value is lower, can be sent to torch in the lump with other gas; Calorific value is low again will send incinerator or Catalytic oxidation furnace to, and it is seldom a part of that flash distillation tolerance only accounts for whole regeneration gas.
(5) gas discharged: directly discharge air or the use of supply lower procedure after the gas cooling that regenerator desorb discharges, separation.If discharge, except CO in regeneration gas
2environmental protection (discharge standard of air pollutants) speed and concentration index must be met with other compositions outside water vapour simultaneously.
(6) regeneration of waste liquor quality: solution stripping must thoroughly, and harmful substance residual in the lean solution after regeneration can not be too much, otherwise after long term accumulation, harmful components in regeneration gas can be made to exceed environmental protection standard.Concrete measure: one is to provide the enough heats of regenerator, makes harmful composition in solution reach a low concentration balance; Two is adopt the high boiling point organic compound in activated carbon or resin adsorption solution, reduces their concentration in decarbonizing solution.
(7) technological process of regeneration of waste liquor: in order to reduce the steam consumption of regeneration of waste liquor, can adopt the various energy saving technique flow process succeeded in developing, comprise: jet regeneration, double-cable suspension bridge etc.
(8) press flash zone and the washing section thereof of rich solution flash tank in, and low-pressure flashing tank can install one deck or two-layer filler (structured packing or random packing) increases flash distillation area, improves flash evaporation effect.
Accompanying drawing explanation
Fig. 1 is embodiment of the present invention process flow diagram.
In accompanying drawing, 1-purge gas separator; 2-purified gas cooler; 3-semi-leanpump; 4-CO
2absorption tower; Flash tank is pressed in 5-; 6-lean pump; 7-activated carbon (resin) filter; 8-low-pressure flashing tank; 9-regenerator; 10-steam boiling device; 11-regeneration gas cooler; 12-regeneration gas separator.
Detailed description of the invention
Below in conjunction with drawings and Examples, the present invention is described in detail.
As accompanying drawing, the circulating air from reactor outlet enters decarburization unit absorption tower 4 through separation of products, removes CO at Ta Nei and lean solution, semi lean solution counter current contacting
2, after decarburization, reach CO
2the purified gas of content's index is through subcooler 2, separator 1 Returning reactor.
First rich solution out at the bottom of absorption tower enters middle pressure flash tank 5, complete middle pressure flash distillation wherein, its afterbody flashing pressure is generally 0.75 ~ 1.6MPa (absolute pressure), and the rich solution after this pressure must ensure flash distillation oneself can be pressed onto regenerator top, does not need to carry out supercharging with pump.Press flash tank afterbody pressure according to regenerator height and low pressure flash pressure in decarburization, add pipeline valve resistance to determine.The gas flashed off, after washing section cooling in flash tank top is separated, directly can send gas ductwork; Also can determine whether to be worth returning gas handling system by compressor according to gas composition.The flash zone of middle pressure flash tank 5 and washing section can install one section or two sections of fillers (structured packing or random packing) increase flash distillation area, improve flash evaporation effect; Strengthen clean result.
Enter regeneration overhead low-pressure flashing tank 8 from rich solution flash tank rich solution out, carry out the low pressure flash of rich solution.Low pressure flash pressure needs to be determined by analog computation, this pressure model is 0.1 ~ 0.35MPa (absolute pressure), target be ensure the rich solution after flash distillation through regenerator air lift, boil desorb and become non-methane hydrocarbon speed and concentration in the regeneration gas discharged in lean solution process and all meet environmental requirement.The whereabouts of low pressure flash gas, mainly according to its composition, can be recycled; Also gas ductwork or relevant boiler can be sent according to calorific value is high; Calorific value is lower, can be sent to torch in the lump with other gas; Calorific value is low again will send incinerator or Catalytic oxidation furnace to, differently by clean for pernicious gas process.It is seldom a part of that flash distillation tolerance only accounts for whole regeneration gas.Low-pressure flashing tank 8 can install one section or two sections of fillers (structured packing or random packing) increase flash distillation area, improve flash evaporation effect.
Rich solution after low pressure flash enters regenerator 9, and in tower, air lift regeneration forms semi lean solution, goes out tower through semi-leanpump 3, pump into absorption tower in the middle part of tower.Semi lean solution continues desorb in regenerator, and by steam boiling device 10, finally forms lean solution, by lean pump 6, pumps into absorption tower and realizes circulation; Lean pump outlet manifold part lean solution is high boiling point organic compound (boiling point is more than 125 DEG C) in activated carbon (resin) filter 7 adsorbent solution, reduces their concentration in decarbonizing solution.
From regenerator gas out through subcooler 11, separator 12, air directly can be discharged or supply lower procedure uses, except CO in regeneration gas
2all environmental requirement must be met with other component velocities outside water vapour and concentration.
embodiment 1
Certain scale is the coal liquifaction device of 1,000,000 tons/year, and its Fischer-Tropsch synthesis circulating air removes side reaction product CO
2decarburization unit adopt potash decarbonization process.Pressure 1.8MPa (absolute pressure) circulating air enters decarbonization system, and circulating flow rate is 375650.00Nm
3/ h, wherein CO
2concentration 15.795mol%, hydro carbons concentration 22.966mol%, alcohol, acid, ketone concentration 1.033mol%.Absorb CO
2after rich solution in non-methane hydrocarbon content 74.93kg/h, alcohol, acid, ketone content 1236.81kg/h.In 1.2MPa (absolute pressure) rich solution, press flash tank, in the rich solution after flash distillation, non-methane hydrocarbon content is reduced to 37.5kg/h, and alcohol, acid, ketone content are reduced to 234.59kg/h.Flash gas, after washing section cooling in flash tank top is separated, directly will send gas ductwork.
Low pressure flash carries out at regenerator top low-pressure flashing tank, and pressure is 0.26MPa (absolute pressure), and containing non-methane hydrocarbon content 30.79kg/h in flashed vapour, alcohol, acid, ketone content are kept to 222.63kg/h, and all the other are CO
2and water vapour, and a small amount of inert gas N2 and Ar.Gas heating value is greater than the requirement entering gas ductwork, can send gas ductwork, also can send torch.Non-methane hydrocarbon content 6.71kg/h in liquid after low pressure flash, alcohol, acid, ketone content 11.96kg/h.
After low pressure flash liquid in regenerator air lift, boil form lean solution, non-methane hydrocarbon content is reduced to 4.05kg/h in the regeneration gas that discharges in semi lean solution process, alcohol (not containing methyl alcohol), acid, ketone content are kept to 3.2kg/h.Non-methane hydrocarbon concentration 101mg/Nm
3lower than 120mg/Nm
3(discharge standard of air pollutants GB16297-1996).Last remnants non-methane hydrocarbon in the solution (being mainly heavy hydrocarbon) content 2.66kg/h, alcohol, acid, ketone content are kept to 8.76kg/h, meet the normal requirement run.
embodiment 2
Certain scale is the ethene epoxy ethane device of 200,000 tons/year, and its oxidative synthesis reaction cycle qi exhaustion is except side reaction product CO
2decarburization unit adopts potash decarbonization process.Pressure 2.38MPa (absolute pressure) circulating air enters decarbonization system, and circulating flow rate is 668822.04kg/h, wherein CO
2concentration 1.44mol%, ethylene concentration 28.61mol%, O
2concentration 5.68mol%, all the other are CH
4, C
2h
6, N
2, Ar and a small amount of steam and MEG.Absorb CO
2after rich solution in non-methane hydrocarbon content 322.11kg/h, in 1.2MPa (absolute pressure) rich solution, press flash tank, in the rich solution after middle pressure flash distillation, non-methane hydrocarbon content is reduced to 87.5kg/h.Flash gas, after washing section cooling in flash tank top is separated, can compress retrieval system; Also gas ductwork can be sent.
Low pressure flash carries out at regenerator top low-pressure flashing tank, and pressure is 0.13MPa (absolute pressure), and in order to promote flash distillation, introduce 285kg/h methane gas from trench bottom, non-methane hydrocarbon content 86.82kg/h in flashed vapour, all the other are CO
2and water vapour, and inert gas CH
4, N2 and Ar.After refrigerated separation, gas is through tail-gas compressor supercharging retrieval system; Also gas ductwork can be sent.
Remaining non-methane hydrocarbon content 0.68kg/h in liquid after low pressure flash.After low pressure flash liquid in regenerator air lift, boil non-methane hydrocarbon content in the regeneration gas that formed and discharge in lean solution process and be reduced to 0.68kg/h, non-methane hydrocarbon concentration 98mg/Nm
3, lower than the 120mg/Nm that discharge standard of air pollutants GB16297-1996 specifies
3.
Claims (6)
1. reaction cycle gas decarbonization exhaust emissions reaches a method for environmental protection index, it is characterized in that under 1.0 ~ 8.0MPa (absolute pressure) after circulating air decarburization, presses flash distillation, low pressure flash and air lift, boils regeneration in the desorption process employing of absorption rich solution; Middle pressure flash distillation is divided into one-level or double flash evaporation to be separated H
2, CO and low-carbon (LC) hydro carbons, low pressure flash pressure is 0.1 ~ 0.35MPa (absolute pressure), ensures that the rich solution after flash distillation meets environmental requirement through regenerator air lift, the regeneration gas of boiling desorb and becoming the release of lean solution process.
2. the method for claim 1, it is characterized in that absorption pressure is under the condition of more than 4.0MPa (absolute pressure), middle pressure flash distillation point two-stage is carried out, and first order flashing pressure is 2.0 ~ 3.5MPa (absolute pressure), is separated H
2, CO and low-carbon (LC) hydro carbons reclaim; Afterbody flashing pressure according to regenerator height and low pressure flash pressure, add pipeline valve resistance and be defined as 0.75 ~ 1.6MPa (absolute pressure), the rich solution after this pressure ensures flash distillation oneself can be pressed onto regeneration overhead, does not need to use pump supercharging; CO in the gas that rich solution flashes off under 0.75 ~ 1.6MPa (absolute pressure)
2smaller with water vapor concentration, H
2, CO, various hydro carbons and other aldehyde, ketone, acid, alcohol gas is many, after washing section cooling in flash tank top is separated, directly send gas ductwork or determine whether to be worth returning gas handling system by compressor according to gas composition.
3. the method for claim 1, it is characterized in that low pressure flash pressure is 0.1 ~ 0.35MPa (absolute pressure), ensure the rich solution after flash distillation through regenerator air lift, boil desorb and become non-methane hydrocarbon speed and concentration in the regeneration gas of lean solution process release and all meet environmental requirement; For flash distillation is thorough, bottom flash zone, pass into technique inert gas with pressure, simultaneously under the prerequisite meeting standard, improve low pressure flash pressure, to reduce CO
2with the concentration of water vapour, improve low pressure flash gases value.
4. the method for claim 1, is characterized in that the necessary thoroughly desorb of solution, reduces harmful substance residual in the lean solution after regeneration: one is to provide the enough heats of regenerator, makes to be harmful to composition maintenance low concentration balance in solution; Two is adopt high boiling point organic compound in activated carbon or resin adsorption solution, reduces their concentration in decarbonizing solution.
5. the method for claim 1, is characterized in that the flash zone of middle pressure rich solution flash tank and washing section installs one section or two sections of fillers (structured packing or random packing) increase flash distillation area raising flash evaporation effect; Strengthen clean result.
6. the method for claim 1, is characterized in that rich solution low-pressure flashing tank installs one section or two sections of fillers (structured packing or random packing) increase flash distillation area raising flash evaporation effect.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111039479A (en) * | 2018-10-12 | 2020-04-21 | 中国石油化工股份有限公司 | Treatment method of Fischer-Tropsch synthesis recycle gas decarburization wastewater |
| CN112742174A (en) * | 2019-10-29 | 2021-05-04 | 中国石油化工股份有限公司 | Method for removing alcohol from decarbonization unit of ethylene oxide/ethylene glycol device |
| CN114075445A (en) * | 2020-08-14 | 2022-02-22 | 国家能源投资集团有限责任公司 | Method for obtaining catalyst carbon dioxide selectivity under Fischer-Tropsch synthesis recycle gas decarburization condition |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4814104A (en) * | 1987-02-05 | 1989-03-21 | Uop | Tertiary alkanolamine absorbent containing an ethyleneamine promoter and its method of use |
| CN1088472A (en) * | 1992-12-24 | 1994-06-29 | 四川化工总厂 | From mist, remove the method for carbon dioxide |
| CN1377825A (en) * | 2001-12-10 | 2002-11-06 | 大连理工大学 | Energy saving raw material gas purifying methanol washing method |
| CN201419074Y (en) * | 2009-06-03 | 2010-03-10 | 上海国际化建工程咨询公司 | Shunting type energy-saving scrubbing unit using low temperature methanol |
| CN101816878A (en) * | 2010-04-30 | 2010-09-01 | 四川省精细化工研究设计院 | Novel high-efficient compound decarbonization solvent |
| CN102423620A (en) * | 2011-10-26 | 2012-04-25 | 东莞市康达机电工程有限公司 | Compound decarbonizing solvent for removing carbon dioxide from biogas |
| CN102806000A (en) * | 2012-09-05 | 2012-12-05 | 大连佳纯气体净化技术开发有限公司 | Energy-saving one-step rectisol method |
| CN103214009A (en) * | 2013-03-22 | 2013-07-24 | 中石化宁波工程有限公司 | Synthesis ammonia decarburization technology |
-
2014
- 2014-09-16 CN CN201410468469.8A patent/CN105477978B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4814104A (en) * | 1987-02-05 | 1989-03-21 | Uop | Tertiary alkanolamine absorbent containing an ethyleneamine promoter and its method of use |
| CN1088472A (en) * | 1992-12-24 | 1994-06-29 | 四川化工总厂 | From mist, remove the method for carbon dioxide |
| CN1377825A (en) * | 2001-12-10 | 2002-11-06 | 大连理工大学 | Energy saving raw material gas purifying methanol washing method |
| CN201419074Y (en) * | 2009-06-03 | 2010-03-10 | 上海国际化建工程咨询公司 | Shunting type energy-saving scrubbing unit using low temperature methanol |
| CN101816878A (en) * | 2010-04-30 | 2010-09-01 | 四川省精细化工研究设计院 | Novel high-efficient compound decarbonization solvent |
| CN102423620A (en) * | 2011-10-26 | 2012-04-25 | 东莞市康达机电工程有限公司 | Compound decarbonizing solvent for removing carbon dioxide from biogas |
| CN102806000A (en) * | 2012-09-05 | 2012-12-05 | 大连佳纯气体净化技术开发有限公司 | Energy-saving one-step rectisol method |
| CN103214009A (en) * | 2013-03-22 | 2013-07-24 | 中石化宁波工程有限公司 | Synthesis ammonia decarburization technology |
Non-Patent Citations (2)
| Title |
|---|
| 何杰等: "高效规整填料及新型塔内件在低压闪蒸槽中的应用", 《化肥工业》 * |
| 符德学: "《无机化工工艺学》", 31 August 2005 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111039479A (en) * | 2018-10-12 | 2020-04-21 | 中国石油化工股份有限公司 | Treatment method of Fischer-Tropsch synthesis recycle gas decarburization wastewater |
| CN112742174A (en) * | 2019-10-29 | 2021-05-04 | 中国石油化工股份有限公司 | Method for removing alcohol from decarbonization unit of ethylene oxide/ethylene glycol device |
| CN112742174B (en) * | 2019-10-29 | 2022-09-09 | 中国石油化工股份有限公司 | Method for removing alcohol from decarbonization unit of ethylene oxide/ethylene glycol device |
| CN114075445A (en) * | 2020-08-14 | 2022-02-22 | 国家能源投资集团有限责任公司 | Method for obtaining catalyst carbon dioxide selectivity under Fischer-Tropsch synthesis recycle gas decarburization condition |
| CN114075445B (en) * | 2020-08-14 | 2024-02-13 | 国家能源投资集团有限责任公司 | Method for obtaining catalyst carbon dioxide selectivity under Fischer-Tropsch synthesis recycle gas decarburization condition |
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Address after: Liuhe District of Nanjing City, Jiangsu province 210048 geguan Road No. 699 Patentee after: China Petroleum & Chemical Corp. Patentee after: SINOPEC NANJING CHEMICAL RESEARCH INSTITUTE Co.,Ltd. Address before: Liuhe District of Nanjing City, Jiangsu province 210048 geguan Road No. 699 Patentee before: China Petroleum & Chemical Corp. Patentee before: Nanhua Group Research Institute |