CN104208983B - The decarbonization method of coal-based indirect liquefaction Fischer-Tropsch process exhaust - Google Patents
The decarbonization method of coal-based indirect liquefaction Fischer-Tropsch process exhaust Download PDFInfo
- Publication number
- CN104208983B CN104208983B CN201410455603.0A CN201410455603A CN104208983B CN 104208983 B CN104208983 B CN 104208983B CN 201410455603 A CN201410455603 A CN 201410455603A CN 104208983 B CN104208983 B CN 104208983B
- Authority
- CN
- China
- Prior art keywords
- tower
- gas
- methyl alcohol
- fischer
- tropsch process
- 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.)
- Active
Links
Classifications
-
- 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
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of decarbonization method of coal-based indirect liquefaction Fischer-Tropsch process exhaust.Comprise the steps: that Fischer-Tropsch process exhaust cools through preliminary and spray into methyl alcohol, isolate gaseous component and liquid phase component; Gaseous component enters prewashing tower and carries out absorption operation from the rich methanol in middle pressure flash tank, removes the hydro carbons in this stream stock and part CO
2; The gas phase portion removing hydro carbons enters described decarbonizing tower, absorbs the CO in gas phase by poor methanol
2obtain clean gas; The methanol solution that prewashing tower bottom is rich in hydro carbons and the liquid phase component be isolated to, inject extraction tower after heat exchange; Methyl alcohol bottom decarbonizing tower is after heat exchange cools and reduces pressure and discharge effective gas, and a part pumps into prewashing tower, and another part removes CO in nitrogen stripping tower
2realize Mathanol regenerating; The tail gas of nitrogen stripper-overhead gas and Mathanol regenerating top of tower, after heat exchange, is absorbed the methyl alcohol contained in gas recovery, and delivers to Mathanol regenerating tower by water.Hydrocarbon loss of the present invention is few, has some superiority for the overall yield improving F-T synthesis.
Description
Technical field
The present invention relates to a kind of decarbonization method of coal-based indirect liquefaction Fischer-Tropsch process exhaust.
Background technology
Coal liquifaction technique is a kind of technical process coal being converted on a large scale liquid fuel through the process of high effect cleaning.Coal liquifaction technology is divided into coal direct liquefaction and indirect coal liquefaction technology.Indirect coal liquefaction refer to by coal after gasification purification through F-T synthesis, produce the thick product such as gaseous hydrocarbon, liquid hydrocarbon, synthetic wax.The products such as diesel oil, gasoline naphtha and refining wax produced by liquid hydrocarbon and synthetic wax after hydrotreatment.In Ministry of Science and Technology's 863 Program, under the support of the government departments such as the Chinese Academy of Sciences and the many enterprises such as Yi Tai group and Lu An group, the exploitation of the proprietary technology researched and developed for many years is gone through by Zhongke Synthetic Oil Technology Co., Ltd., obtain with F-T synthesis high temperature slurry bed system technique and the high temperature slurry bed system ferrum-based catalyst complete indirect coal liquefaction technology that is technological core (see Chinese invention patent ZL200410012189.2, ZL200410012191.X and the open CN101396647A of patent), this technology is through the checking of pilot scale and 160,000 tons/year of ICL for Indirect Coal Liquefaction synthesis demonstration plants, possess the technical conditions implementing the project construction of megaton large industrialized.And assume responsibility for the design objective of multiple megaton coal liquifaction project.
F-T synthesis (Fischer-TropschSynthesis, FTS) is a kind of method being raw material indirect synthesis oil product containing carbon resource with coal, natural gas, living beings etc.Its product is generally by mink cell focus, light oil, synthetic water (containing organic oxygen-containing compounds such as alcohol, aldehyde, ketone, acid, fat), CO
2, methane, lower carbon number hydrocarbons (C
6following alkane alkene), unreacted synthesis gas (CO, H
2) and the composition such as nitrogen.Wherein Fischer-Tropsch process exhaust mainly contains H
2, CO, lower carbon number hydrocarbons (C
6following alkane alkene), CO
2, N
2deng composition.Lower carbon number hydrocarbons based on methane, its content usually at 20% ~ 60% (mol), also containing part C
2~ C
6alkene, is about 1% ~ 10% (mol).In Fischer-Tropsch process exhaust, the content of sulphur and oxygen is lower than 0.1ppm.Fischer-Tropsch process exhaust composition is obviously different from oil refinery dry gas and coke-stove gas.
Traditionally, Fischer-Tropsch process exhaust can as fuel combustion to be used for heat supply or generating.Along with oil price rise, this kind of way becomes very uneconomical.If lower carbon number hydrocarbons wherein can be separated and obtains CO, H
2recycle as synthesis gas, then greatly can improve the complex energy utilization ratio of whole artificial oil factory, increase economic benefit and the product category of artificial oil factory.
Dry discloses a kind of technological process (MarkEDry of Fischer-Tropsch process exhaust process, TheFischer-Tropschprocess-commercialaspects, CatalysisToday, 1990,6 (3): 183-206) Fischer-Tropsch process exhaust sub-argument is gone out CO by the method, adopting low-temperature deep to be separated
2, methane, ethene, propylene, C
3~ C
5hydrocarbon mixture.The open CN1944358A of Chinese patent proposes C in a kind of recovery Fischer-Tropsch process exhaust
3~ C
5the method of hydrocarbon mixture.The process employs the processing steps such as decarburization, first cold, washing, dehydration, decompression, deep cooling, fractionation, obtain C
3~ C
5hydrocarbon mixture.
Along with the production-scale increase of coal liquifaction indirect liquefaction, the Fischer-Tropsch process exhaust produced also increases sharply thereupon.How more reasonable, effective utilization and conversion Fischer-Tropsch process exhaust, be related to the whole economy of coal liquifaction factory and the feasibility of technique.The present invention bases oneself upon separation and the recovery of Fischer-Tropsch process exhaust useful constituent, proposes to utilize low-temp methanol to be separated each component as absorbent selective absorbing, realizes CO
2remove.
Summary of the invention
The object of this invention is to provide a kind of decarbonization method of coal-based indirect liquefaction Fischer-Tropsch process exhaust, the inventive method adopts low-temp methanol as absorbing medium, and various component in selective absorbing Fischer-Tropsch process exhaust, realizes CO in Fischer-Tropsch process exhaust
2remove and CO, H
2and the recycling of lower carbon number hydrocarbons.
The decarbonization method of coal-based indirect liquefaction Fischer-Tropsch process exhaust provided by the present invention, comprises the steps.
(1) Fischer-Tropsch process exhaust from F-T synthesis device cools through preliminary and spray into methyl alcohol, isolates gaseous component and liquid phase component;
(2) described gaseous component enters prewashing tower, removes CO and H with from middle pressure flash tank
2after rich methanol carry out absorption operation, remove the hydro carbons in this stream stock and part CO
2;
(3) gas phase portion removing hydro carbons enters described decarbonizing tower, absorbs the CO in gas phase by poor methanol
2obtain clean gas;
(4) described prewashing tower bottom is rich in the methanol solution of hydro carbons and is separated the described liquid phase component obtained through step (1), and inject after heat exchange bottom extraction tower, described extraction tower top adds extractant, and described extractant is water;
The oil phase extracted enters downstream oil product processing workshop section; Water methanol goes Mathanol regenerating part mutually, reclaims methyl alcohol;
(5) methyl alcohol bottom described decarbonizing tower is after heat exchange cools and reduces pressure and discharge effective gas, and a part pumps into prewashing tower and absorbs hydrocarbon component, and another part enters nitrogen stripping tower after decompression, in described nitrogen stripping tower, remove CO
2realize Mathanol regenerating;
(6) methyl alcohol regenerated and supplementary new methyl alcohol mix after heat exchange, through pump pressurization and with cooling system heat exchange after enter described decarbonizing tower, absorb CO
2;
(7) tail gas of described nitrogen stripper-overhead gas and Mathanol regenerating top of tower is after heat exchange, is absorbed the methyl alcohol contained in gas recovery, and deliver to Mathanol regenerating tower by water.
In above-mentioned decarbonization method, containing the light hydrocarbon component of 1% ~ 16% in described Fischer-Tropsch process exhaust, be volumn concentration, described light hydrocarbon comprises the linear paraffin of C2 ~ C5 and alkene etc.
In above-mentioned decarbonization method, in step (1), described Fischer-Tropsch process exhaust is tentatively cooled to-15 DEG C ~-40 DEG C.
In above-mentioned decarbonization method, the theoretical cam curve of described prewashing tower is 5 ~ 40, and top of tower temperature is-30 DEG C ~-15 DEG C, and operating pressure is 1MPa ~ 6MPa;
Liquid-gas ratio in described prewashing tower is 0.5 ~ 4, and unit is mg/mg.
In above-mentioned decarbonization method, " poor methanol " that adopt refers in low-temp methanol washing process, refers to the methyl alcohol of methanol content higher state.
In above-mentioned decarbonization method, in step (5), described effective gas bag draws together H
2and CO.
In above-mentioned decarbonization method, the Fischer-Tropsch process exhaust after step (2) process cools through heat exchange or directly enters described decarbonizing tower and carries out decarburization.
In above-mentioned decarbonization method, containing the hydrocarbon component of 0 ~ 3% in the Fischer-Tropsch process exhaust after step (2) process, be volumn concentration.
In above-mentioned decarbonization method, described Mathanol regenerating tower realizes the regeneration of methyl alcohol by rectifying.
The present invention is compared with original scheme (hot potassium carbonate+low temperature oil wash scheme) removing sour gas, and tool has the following advantages:
1, flow process is simple.What adopt 5 rectifying columns and 1 extraction tower just can complete sour gas removes work.
2, simple to operate.The rectifying column of this technique centre halfback routine and extraction tower, simple to operate, be easy to promote.
3, cost-saving.Equipment cost required for this flow process and running cost, have certain advantage relative to existing scheme.
4, hydrocarbon loss is few.Relative to hot potassium carbonate technique, the hydrocarbon loss of this technique is few, has some superiority for the overall yield improving F-T synthesis.
5, environmental protection.Hydro carbons and available gas (H in this technique
2and CO) can better be reclaimed, the gas to environmental emission more can meet the requirement of environmental protection.
Accompanying drawing explanation
Fig. 1 is the flow chart of Fischer-Tropsch process exhaust decarburization of the present invention.
Detailed description of the invention
The experimental technique used in following embodiment if no special instructions, is conventional method.
Material used in following embodiment, reagent etc., if no special instructions, all can obtain from commercial channels.
According to the flow process shown in Fig. 1, realize the decarburization of Fischer-Tropsch process exhaust.
From the Fischer-Tropsch process exhaust 30 (H of F-T synthesis unit
2: 0.57, N
2: 0.082, CO:0.072, H
2o:0.004, CH
4: 0.067, CO
2: 0.15, C
2: 0.012, C
3: 0.007, C
4: 0.01, C
5: 0.004, C
6: 0.002, C
7: 0.0005, C
8: 0.0001, molar fraction) and spray methyl alcohol 52 and circulation compressed gas 44 (H
2: 0.21, N
2: 0.006, CO:0.071, CH
4: 0.12, CO
2: 0.53, C
2: 0.012, molar fraction) be cooled to-10 ~-30 DEG C through ice chest 1 after mixing, then send in gas-liquid separator 2 and carry out gas-liquid separation, isolated vapor phase stream stock 32 is for containing C
3 -the CO of hydro carbons
2/ CO/H
2stream stock, liquid phase stream stock 33 is C
4 +hydrocarbon mixture, stream stock 32 sends into prewashing tower 3 through prewashing process, further removing C wherein
3 -hydro carbons, obtain flowing stock 34, the washing agent of above-mentioned prewashing processing procedure is the cold methanol stream stock 39 from intermediate pressure flash vessel 6, and the gaseous state obtained after prewashing process, mutually stream stock 34 are sent into decarbonizing tower 5 from prewashing tower top and carried out carbonization treatment, containing C
3 -the flow of methanol stock 65 of hydro carbons etc. is sent in intermediate pressure flash vessel 4 at the bottom of prewashing tower.In decarbonizing tower 5, vapor phase stream stock 34 from bottom to top, and through decarburization tower top top-down low temperature liquid phase methyl alcohol counter current contacting, removes the CO in stream stock 34 at the bottom of tower
2component, obtaining Main Ingredients and Appearance is CO/H
2vapor phase stream stock 35 (H
2: 0.71, N
2: 0.1, CO:0.09, CH
4: 0.08, CO
2: 0.01, C
2: 0.004, C
3: 0.00, molar fraction), stream stock 35 36 returns F-T synthesis unit and is used as unstripped gas after ice chest 1 heat exchange.Stream stock 65 is isolated to gaseous flow stock 41 and liquid flow stock 66 in intermediate pressure flash vessel 4, send in extraction tower 11 together with 67 after stream stock 66 mixes with liquid phase stream stock 33 out at the bottom of gas-liquid separator 2 tower, taking water as extractant, flowing stock 55 (H mutually by being extracted after the methanol extraction in stream stock 66
2+ CO:0.038, C
2: 0.27, C
3: 0.32, C
4: 0.22, C
5: 0.08, C
6: 0.04, C
7: 0.01, C
8: 0.0006, molar fraction), extraction phase stream stock 55 is delivered to downstream units and is processed into LPG, naphtha etc. further after heat exchange.Send downstream units to process further to obtain hydrocarbon products that (this partial material contains linear paraffin and the alkene of C2 ~ C5, delivers to oil product machining cell and carries out conventional rectification separation, can obtain LPG and naphtha.)。Mathanol regenerating recovery is carried out at the middle part sending into methyl alcohol hot recycling tower 12 from the raffinate phase stream stock 56 of extraction tower 11, and the flow of methanol stock 57 obtained can be sent into nitrogen stripping tower 8 or directly send into methyl alcohol replenishment system 9.The pure water stream 58 that methyl alcohol hot recycling tower bottom obtains is divided into two strands, and one 59 feeding extraction tower 11 is used as extractant, and another stock 60 is sent into tail gas washing tower 13 and is used as washing tail gas agent.Stream stock 37 bottom decarbonizing tower 5 is sent into intermediate pressure flash vessel 6 and is reclaimed available gas, the cold methanol solution stream stock reclaimed after available gas is two parts, a part 39 is delivered to prewashing tower 3 and is used as washing agent, another part 40 sends into nitrogen stripping tower 8, in nitrogen stripping tower, stream stock 40, with nitrogen stream stock 64 counter-current operation from bottom to top, resolves the CO be rich in methyl alcohol from top to bottom
2and other gas component, obtain high-purity flow of methanol stock 49, major part 50 is sent in methyl alcohol replenishment system 9, a small amount of methyl alcohol 52 is sent in stream stock 30, as spray methyl alcohol, mix with stream stock 30, to prevent a small amount of water contained in Fischer-Tropsch process exhaust icing blocking pipeline in cooling procedure.In order to utilize the cold of methyl alcohol, take out flow of methanol stock 47 from nitrogen stripping tower 8 medium position and send into heat exchanger 7, after convection current stock 53 carries out heat exchange cooling, 48 return nitrogen stripping tower lower entrances again and carry out air lift, the periodic off-gases stream stock 45 of going out from nitrogen stripping tower 8 tower top is via 46 sending into bottom tail gas washing towers 13 after ice chest 1 heat exchange, contain the water solution flow stock 60 of a small amount of methyl alcohol and new supplementary 61 deaerated water countercurrent mass transfers with top-down, obtain tail gas stream stock 63 (H
2: 0, N
2: 0.42, CO:0.001, H
2o:0.002, CH
4: 0.007, CO
2: 0.57, molar fraction) be sent to catalytic combustion unit, the water solution flow stock 62 after fully absorbing methyl alcohol processes by sending at the bottom of tail gas washing tower in the middle part of methyl alcohol hot recycling tower 12, to reclaim contained methyl alcohol.Be separated the methyl alcohol obtained and water in methyl alcohol hot recycling tower 12 to recycle respectively as the washing agent materials of whole technological process.After stream stock 41 from intermediate pressure flash vessel 4 mixes with the stream stock 38 from intermediate pressure flash vessel 6,42 to pressurize through compressor 10 and obtain flowing stock 43, obtain flowing stock 44 again after cooler 14 heat exchange cooling, as the unstripped gas of this PROCESS FOR TREATMENT after stream stock 44 mixes with Fischer-Tropsch process exhaust stream stock 30.
Claims (7)
1. the decarbonization method of coal-based indirect liquefaction Fischer-Tropsch process exhaust, comprises the steps:
(1) Fischer-Tropsch process exhaust from F-T synthesis device cools through preliminary and spray into methyl alcohol, isolates gaseous component and liquid phase component;
(2) described gaseous component enters prewashing tower, removes CO and H with from middle pressure flash tank
2after rich methanol carry out absorption operation, remove the hydro carbons in this stream stock and part CO
2;
(3) gas phase portion removing hydro carbons enters decarbonizing tower, absorbs the CO in gas phase by poor methanol
2obtain clean gas;
(4) described prewashing tower bottom is rich in the methanol solution of hydro carbons and is separated the described liquid phase component obtained through step (1), and inject after heat exchange bottom extraction tower, described extraction tower top adds extractant, and described extractant is water;
The oil phase extracted enters downstream oil product processing workshop section; Water methanol goes Mathanol regenerating part mutually, reclaims methyl alcohol;
(5) methyl alcohol bottom described decarbonizing tower is after heat exchange cools and reduces pressure and discharge effective gas, and a part pumps into prewashing tower and absorbs hydrocarbon component, and another part enters nitrogen stripping tower after decompression, in described nitrogen stripping tower, remove CO
2realize Mathanol regenerating;
(6) methyl alcohol regenerated and supplementary new methyl alcohol mix after heat exchange, through pump pressurization and with cooling system heat exchange after enter described decarbonizing tower, absorb CO
2;
(7) tail gas of described nitrogen stripper-overhead gas and Mathanol regenerating top of tower is after heat exchange, is absorbed the methyl alcohol contained in gas recovery, and deliver to Mathanol regenerating tower by water.
2. decarbonization method as claimed in claim 1, is characterized in that: containing the light hydrocarbon component of 1% ~ 16% in described Fischer-Tropsch process exhaust, be volumn concentration.
3. decarbonization method as claimed in claim 1 or 2, is characterized in that: in step (1), described Fischer-Tropsch process exhaust is tentatively cooled to-15 DEG C ~-40 DEG C.
4. decarbonization method as claimed in claim 3, is characterized in that: the theoretical cam curve of described prewashing tower is 5 ~ 40, and top of tower temperature is-30 DEG C ~-15 DEG C, and operating pressure is 1MPa ~ 6MPa;
Liquid-gas ratio in described prewashing tower is 0.5 ~ 4, and unit is mg/mg.
5. decarbonization method as claimed in claim 4, is characterized in that: the Fischer-Tropsch process exhaust after step (2) process cools through heat exchange or directly enters described decarbonizing tower and carries out decarburization.
6. decarbonization method as claimed in claim 5, is characterized in that: containing the hydrocarbon component of 0 ~ 3% in the Fischer-Tropsch process exhaust after step (2) process, be volumn concentration.
7. decarbonization method as claimed in claim 6, is characterized in that: described Mathanol regenerating tower realizes the regeneration of methyl alcohol by rectifying.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410455603.0A CN104208983B (en) | 2014-09-09 | 2014-09-09 | The decarbonization method of coal-based indirect liquefaction Fischer-Tropsch process exhaust |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410455603.0A CN104208983B (en) | 2014-09-09 | 2014-09-09 | The decarbonization method of coal-based indirect liquefaction Fischer-Tropsch process exhaust |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104208983A CN104208983A (en) | 2014-12-17 |
| CN104208983B true CN104208983B (en) | 2016-03-16 |
Family
ID=52091128
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410455603.0A Active CN104208983B (en) | 2014-09-09 | 2014-09-09 | The decarbonization method of coal-based indirect liquefaction Fischer-Tropsch process exhaust |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104208983B (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105344211A (en) * | 2015-12-02 | 2016-02-24 | 天津渤化永利化工股份有限公司 | Method for efficiently removing impurities in methanol washed in low-temperature methanol washing system |
| CN107684932A (en) * | 2017-10-11 | 2018-02-13 | 武汉凯迪工程技术研究总院有限公司 | Slurry bed system Co based Fischer-Tropsch synthesis catalyst regenerated offline method and its device |
| CN113577812B (en) * | 2017-12-04 | 2023-03-17 | 碳回收国际公司 | System and method for separating dissolved gases by distillation and stripping |
| CN112387072A (en) * | 2019-08-16 | 2021-02-23 | 国家能源投资集团有限责任公司 | CO capture by absorption2Method and system of |
| EP4029926A1 (en) * | 2021-01-15 | 2022-07-20 | Evonik Operations GmbH | Two-stage exhaust gas scrubbing |
| CN113368663B (en) * | 2021-05-18 | 2022-09-02 | 中科合成油技术股份有限公司 | Treatment method of Fischer-Tropsch synthesis decarbonized tail gas and equipment system for implementing method |
| CN114437841A (en) * | 2022-02-14 | 2022-05-06 | 中科合成油技术股份有限公司 | Method and device for co-producing natural gas, LPG and naphtha by using Fischer-Tropsch synthesis tail gas |
| CN114904364B (en) * | 2022-05-30 | 2024-04-09 | 万华化学集团股份有限公司 | Tail gas treatment method for polyacrylic acid device |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6667347B2 (en) * | 2001-09-14 | 2003-12-23 | Chevron U.S.A. Inc. | Scrubbing CO2 from methane-containing gases using an aqueous stream |
| US8419829B2 (en) * | 2010-10-27 | 2013-04-16 | General Electric Company | Method and system for treating Fishcher-Tropsch reactor tail gas |
| CN102614763B (en) * | 2011-01-27 | 2014-08-06 | 中科合成油工程有限公司 | Method for processing Fischer-Tropsch synthesis tail gas |
| CN102618317A (en) * | 2011-01-27 | 2012-08-01 | 中科合成油工程有限公司 | Method for recovering liquefied gas component in Fischer-Tropsch synthesis tail gas |
| US9783738B2 (en) * | 2012-07-20 | 2017-10-10 | Shell Oil Company | Hydrocarbon recovery from Fischer-Tropsch off-gas |
| CN102806000B (en) * | 2012-09-05 | 2015-05-20 | 大连佳纯气体净化技术开发有限公司 | Energy-saving one-step rectisol method |
| CN103666518B (en) * | 2013-12-04 | 2015-10-28 | 中国科学院山西煤炭化学研究所 | A kind of method of Fischer-Tropsch process exhaust higher value application |
-
2014
- 2014-09-09 CN CN201410455603.0A patent/CN104208983B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN104208983A (en) | 2014-12-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104208983B (en) | The decarbonization method of coal-based indirect liquefaction Fischer-Tropsch process exhaust | |
| CN103588604B (en) | A kind of system and method combining carbon two in absorption process recovery oil refinery dry gas | |
| CN104892340A (en) | Three-tower device and method for recycling ethylene and ethane from dry gas through oil absorption | |
| JP7546555B2 (en) | Method and system for separating light hydrocarbons | |
| CN102614763A (en) | Method for processing Fischer-Tropsch synthesis tail gas | |
| CN102304009B (en) | Method and system for separating MTP (Methanol to Propylene) reaction mixed gas | |
| CN104557384A (en) | Refinery mixed dry gas recovery system and recovery method | |
| CN102267850A (en) | Method for separating light olefins gas | |
| CN202081036U (en) | Mixed gas separating system in MTP reaction | |
| CN101456537B (en) | Method for reducing carbon dioxide in GTL synthesis cycle gas | |
| CN104557386B (en) | A kind of refinery's mixing dry gas recovery system and recovery method | |
| CN103965009B (en) | The method of the hydrocarbonylation tail gas ethylbenzene after a kind of catalysis drying gas preparation of styrene | |
| CN100384510C (en) | Method for removing sulfides and carbon dioxide by high pressure | |
| CN103695043B (en) | Method for drying, purifying and cooling conversion rough synthesized gas and SNG product gas through low-temperature methanol washing and device thereof | |
| CN107089644A (en) | A kind of carbon dioxide discharge-reduction and the apparatus and method of comprehensive utilization | |
| CN102618317A (en) | Method for recovering liquefied gas component in Fischer-Tropsch synthesis tail gas | |
| CN103030494B (en) | Absorption and hydration coupling device and method for separating ethylene and ethane in catalytic cracking dry gas or ethylene pyrolysis gas | |
| CN105733647A (en) | Method for recovering liquefied petroleum gas from Fischer-Tropsch synthesis tail gas | |
| CN110631326A (en) | Fischer-Tropsch synthesis tail gas recycling system process | |
| CN103073378B (en) | Low-temperature methanol washing and alkane dehydrogenation combination system and coupling system of low-temperature methanol washing and alkane dehydrogenation combination system and alkene separation system | |
| CN109456139A (en) | The oily method for absorbing and separating of methane product of ethylene reaction | |
| CN111004079B (en) | Separation method and device for reaction gas for preparing ethylene by oxidative coupling of methane | |
| CN113368663B (en) | Treatment method of Fischer-Tropsch synthesis decarbonized tail gas and equipment system for implementing method | |
| CN104276916B (en) | A kind of system and separation method preparing Trimethylmethane | |
| CN203295451U (en) | Ethane-rich dry gas purifying and refining device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 101407 No.1, south 2nd Yueyuan street, C District, Yanqi Development Zone, Huairou District, Beijing Patentee after: Zhongke synthetic oil Technology Co.,Ltd. Address before: 101407 No.1, south 2nd Yueyuan street, C District, Yanqi Development Zone, Huairou District, Beijing Patentee before: SYNFUELS CHINA TECHNOLOGY Co.,Ltd. |
|
| CP01 | Change in the name or title of a patent holder |