CN102618317A - Method for recovering liquefied gas component in Fischer-Tropsch synthesis tail gas - Google Patents
Method for recovering liquefied gas component in Fischer-Tropsch synthesis tail gas Download PDFInfo
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Abstract
The invention relates to a method for recovering a liquefied gas component in Fischer-Tropsch synthesis tail gas, which is characterized in that absorption and analytic principles are used for recovering the liquefied gas component in the Fischer-Tropsch synthesis tail gas; the employed main technology comprises the steps of oil-gas separation, absorption, analysis, stabilization, regeneration and the like; the concrete technology is characterized in that the Fischer-Tropsch synthesis tail gas, analytic tower top gas and a rich absorbent at the bottom of an absorbing tower are subjected to three phases separation of gas, oil and water in an oil and gas separator, the gas phase enters into the absorbing tower, under the low temperature state of the absorbing tower, C2<->(containing C2 component)component taken as a product dry gas comes out of the absorbing tower, the absorbed rich absorbent of C3<+>(containing C3 component) component in raw material gas is discharged from the bottom of the absorbing tower, the rich absorbent passes through the oil and gas separator to remove partial C2<+> and then enter into the analytic tower after heating, the main effect of the analytic tower enables removal of residual C2<->component in the rich absorbent, analytic tower top gas to the oil and gas separator and the liquid at the bottom of the analytic tower to a stabilization tower, the liquefied gas component can be recovered from the stabilization tower top, the liquid at the bottom of the stabilization tower removes partial C5-C6 component through a regeneration tower, the liquid at the bottom of the stabilization tower can be taken as the absorbent and then cooled to return to the absorbing tower for cycle utilization.
Description
Technical field
The present invention relates to a kind of method that reclaims liquefied gas component in the Fischer-Tropsch process exhaust, specifically, is the method for resolving through low temperature absorption, high temperature, reclaims the low temperature oil wash stripping technique of liquefied gas component in the Fischer-Tropsch process exhaust.
Background technology
China is the country of coal oil starvation more than, if can coal be converted into liquid fuel on a large scale with the process method of high effect cleaning, will alleviate the pressure of oil supply effectively, promotes that economy develops sustainedly and stably.Coal system oil tech can be divided into ICL for Indirect Coal Liquefaction technology and direct coal liquefaction technology.The ICL for Indirect Coal Liquefaction technology is meant that coal contains H through gasification production earlier
2With the coal based synthetic gas of CO, coal based synthetic gas obtains appropriate H through process steps such as conversion and purifications again
2The synthetic gas of/CO ratio; Synthetic gas gets in the Fischer-Tropsch synthesis device and under the effect of catalyzer, carries out Fischer-Tropsch synthesis then; Generate thick product such as hydrocarbon gas, liquid hydrocarbon, synthetic wax, liquid hydrocarbon and synthetic wax can be produced products such as diesel oil, gasoline, petroleum naphtha and refining wax after hydrotreatment; Fischer-Tropsch synthesis described here typically refers to synthetic gas (CO and H
2Gas mixture) under certain temperature and pressure, be converted into the reaction of hydrocarbon compound through catalyzed reaction.Under many enterprises such as Ministry of Science and Technology's 863 Program, Chinese Academy of Sciences's knowledge innovation project project and Yi Tai group and the Lushui River peace group support; Go through proprietary technology exploitation for many years by Zhongke Synthetic Oil Technology Co., Ltd., having obtained to starch attitude bed ferrum-based catalyst with Fischer-Tropsch synthesizing high temperature slurry attitude bed process and high temperature is that the complete indirect coal liquefaction engineering of technological core (is seen Chinese invention patent ZL200410012189.2; ZL200410012191.X; And the open CN101396647A of patent), this technology has possessed the technical qualification that get into the project construction of MT large industrialized through the checking of pilot scale and 160,000 tons of/year ICL for Indirect Coal Liquefaction synthetic oil industriallization demonstrations.
Can produce a large amount of Fischer-Tropsch process exhausts in the Fischer-Tropsch synthesis process of ICL for Indirect Coal Liquefaction, mainly by H
2, CO, lower carbon number hydrocarbons (C
6Following hydrocarbon), CO
2, N
2Deng composition, Fischer-Tropsch process exhaust acts as a fuel usually traditionally, is used for heat supply or generating; But along with the rise of International Crude Oil, it is very uneconomical that this way becomes, and reduced the use value of resource; If can from Fischer-Tropsch process exhaust, isolate products such as hydrogen, liquefied gas, low-carbon alkene; Can improve the economic worth of Fischer-Tropsch process exhaust greatly, improve the complex energy utilising efficiency of whole synthetic oil factory simultaneously, increase the economic benefit and the product category of synthetic oil factory.
Dry discloses technical process (the Mark E Dry that a kind of Fischer-Tropsch process exhaust is handled; The Fischer-Tropsch process-commercial aspects; Catalysis Today; 1990,6 (3): 183-206), adopt the isolating method of low-temperature deep that Fischer-Tropsch process exhaust is isolated CO respectively
2, methane, ethene, propylene, C
3-C
5Hydrocarbon mixture, methane is through O then
2Be converted into synthetic gas with the water vapour partially oxidation and loop back again in the reactor feed gas, ethene is used to make Vilaterm, and propylene is used to make Vestolen PP 7052, C
3-C
5Hydrocarbon is through products such as oligomerisation reaction system gasoline, diesel oil and LPG.This technical process is complicated, and energy consumption is big, but the product category that forms is more.
CN 101173190A has provided a kind of low temperature oil wash of three tower process briefly and has handled the oily of Fischer-Tropsch synthesis oil through obtaining after the unifining; At first oily gets into absorption tower and absorption agent counter current contact; Rich absorbent gets into Analytic Tower at the bottom of the tower, and the rich absorbent after the parsing gets into stabilizer tower, and overhead product is a liquefied gas; Bottom product is a petroleum naphtha, C in the liquefied gas LPG product of this technology by-product
5Above component concentration is higher, and raw material oil gas has only been done rough separation.
In the Fischer-Tropsch process exhaust processing technological flow of Zhongke Synthetic Oil Technology Co., Ltd.'s exploitation; The purified gas that Fischer-Tropsch process exhaust obtains through the decarburization unit; Contain a certain amount of liquefied gas component; This decarburization purification unit gas also can obtain to be rich in the infiltration gas of hydrogen through film separation unit; This infiltration gas that is rich in hydrogen is produced hydrogen to psa unit after boosting, and the non-infiltration gas of membrane sepn also contains a large amount of liquefied gas components, if decarburization purification unit gas or the non-infiltration gas of film separation unit or any Fischer-Tropsch process exhaust that contains the liquefied gas component are separated the liquefied gas product that will obtain high value.The present invention proposes a kind of method that from Fischer-Tropsch process exhaust, reclaims the liquefied gas component; Adopting the lightweight oil of Fischer-Tropsch building-up process production or the petroleum naphtha of oil product machining cell is absorption agent; Reclaim liquefied gas through steps such as low temperature absorption, high temperature parsings; Increase the product category and the added value of product of the coal-based synthetic oil technology of indirect liquefaction, improve the economic benefit of coal system oil process.
Summary of the invention
The objective of the invention is provides a kind of and resolves the method that reclaims liquefied gas through low temperature absorption, high temperature in order to increase the product category and the added value of product of the coal-based synthetic oil technology of indirect liquefaction.
The invention provides a kind of method through liquefied gas in low temperature absorption, the synthetic membrane sepn tail gas of high temperature parsing recovery Fischer-Tropsch, this method is selected absorption, parsing, stable, regeneration four-column process flow for use, has ensured the output of dry gas product gas purity and liquefied gas.This method may further comprise the steps:
(1) oil-gas separator: the rich absorbent that comes at the bottom of Fischer-Tropsch process exhaust, parsing overhead gas and the self-absorption tower carries out the three phase separation of oil, gas, water in oil-gas separator, oil phase removes Analytic Tower after heating up, and gas phase is gone to the absorption tower after cooling;
(2) absorb: the absorption agent through being cooled to certain temperature that comes from regenerator column heads into from the absorption tower; The gas that comes from oil-gas separator gets into the bottom, absorption tower through being cooled to certain temperature; Carry out low temperature absorption on the absorption tower; The gas that is not absorbed the agent absorption goes out from cat head as the product dry gas, and rich absorbent returns oil-gas separator at the bottom of tower, release portion C
2 -After the component, remove Analytic Tower;
(3) resolve: the rich absorbent that comes from the absorption tower carries out oil, gas, water sepn oil-gas separator; Oil phase gets into Analytic Tower after heating up; Carry out high temperature at Analytic Tower and resolve, separate gassing and after cooling, return oil-gas separator, liquid removes stabilizer tower at the bottom of the Analytic Tower after decompression;
(4) stable: liquid under lower pressure, is resolved and is obtained the liquefied gas product in stabilizer tower at the bottom of the Analytic Tower, and liquid removes regenerator column at the bottom of the tower after decompression;
(5) regeneration: liquid is gone into regenerator column at the bottom of the tower from stabilizer tower, extracts a part of C out
5～C
6Component is gone to other unit, and liquid can partly go to other unit at the bottom of the regenerator column, and part goes to the absorption tower to recycle as absorption agent, also can all recycle as absorption agent.
Particularly, in above-mentioned technical process of the present invention:
Said Fischer-Tropsch process exhaust is non-infiltration gas or other any Fischer-Tropsch synthesis unit tail gas that contains the liquefied gas component of the unitary purified gas of decarburization, film separation unit.
Oil-gas separator can be provided with a separator or the different a plurality of separators of separation temperature in the step (1); Before or after this oil-gas separator, be provided with heat-exchange equipment, with so that the isolated gas of oil-gas separator before getting into the absorption tower with temperature be reduced to absorb temperature required.
The service temperature of said oil-gas separator is-40～60 ℃, preferred-25～40 ℃; Pressure is 1.0～6.0MPa, preferred 2.5～4.5MPa; This oil-gas separator oil phase goes the temperature of Analytic Tower after heat exchange be 20～120 ℃, preferred; 65～85 ℃.
Said oil-gas separator low temperature part can add frostproofer, prevents that the low temperature part from causing obstruction that system can't be operated by LP because of the icing of water, and said frostproofer can be the aqueous solution of ethanol, terepthaloyl moietie, USP Kosher etc.
Said absorption tower number of theoretical plate is 5～40, preferred 10～20; Tower top temperature is-40～20 ℃, preferred-10～0 ℃; Column bottom temperature is-40～30 ℃, preferred-10～10 ℃; Working pressure is 1.0～6.0MPa; Preferred 2.5～4.5MPa.The temperature that absorption agent gets into the absorption tower is-40～20 ℃, preferred-30～-10 ℃.Said absorption agent is synthetic lightweight oil of Fischer-Tropsch or petroleum naphtha, and concrete, this lightweight oil or petroleum naphtha component are C
5～C
10Hydrocarbon comprises alkane and the alkene of arbitrary proportion, positive structure hydrocarbon and isomeric hydrocarbon.
Said Analytic Tower number of theoretical plate is 5～40, preferred 10～20; Tower top temperature is 40～200 ℃, preferred 80～120 ℃; Column bottom temperature is 70～300 ℃, preferred 180～220 ℃; Working pressure is 1.0～6.0MPa, preferred 2.5～4.5MPa.
Said stabilizer tower number of theoretical plate is 5～40, preferred 20～30; Tower top temperature is 20～180 ℃, preferred 60～90 ℃; Column bottom temperature is 80～300 ℃, preferred 180～230 ℃; Working pressure is 0.5～3.0MPa, preferred 1.0～2.0MPa; Reflux ratio is 2～20, preferred 2～5.
Said regenerator column number of theoretical plate is 3～35, preferred 10～20; Tower top temperature is 40～200 ℃, preferred 100～140 ℃; Column bottom temperature is 80～300 ℃, preferred 140～180 ℃; Working pressure is 0.2～1.5MPa, preferred 0.5～1.0MPa.
In order to guarantee the assimilation effect of absorption agent, the present invention also is provided with the absorption agent additional project, and additional absorption agent can be for from the unitary petroleum naphtha of unifining, also can be for the lightweight oil of Fischer-Tropsch synthesis unit, and concrete, this lightweight oil or petroleum naphtha component are C
5～C
10Hydrocarbon comprises alkane and the alkene of arbitrary proportion, positive structure hydrocarbon and isomeric hydrocarbon.The absorption agent that replenishes can remove absorption tower or regenerator column, also can remove other device.Additional absorption agent can be identical with former absorption agent, also can or different.
The mol ratio of absorption agent and Fischer-Tropsch process exhaust can be in 0.05～5 scope, preferred 0.1-1.
If desired, can control gas-oil separation and absorption portion and under higher pressure, carry out, preferred 4.0～6.0MPa can further improve the output of liquefied gas like this.
In sum, the present invention has following characteristics:
(1) this unit adopts the low temperature oil wash technology of Zhongke Synthetic Oil Technology Co., Ltd.'s exploitation; This technological borrowing plant catalytic cracking and hydrocracking absorb stable experience; Based on the concrete condition of Fischer-Tropsch process exhaust, propose under cryogenic conditions, to utilize the absorption stability principle to make Fischer-Tropsch process exhaust, the synthetic light oil of Fischer-Tropsch be separated into dry gas, liquefied gas, oil wash naphtha;
(2) absorption tower and Analytic Tower are provided with respectively, thereby have realized low temperature absorption and high temperature parsing;
(3) adopt low temperature partly to add the method for frostproofer, prevent the low temperature part because of water icing causes system can't the LP operation;
(4) be provided with the absorbent regeneration tower, main purpose is to remove portion C in the absorption agent
5～C
6Component;
(5) absorption agent selects for use the synthetic lightweight oil of Fischer-Tropsch or petroleum naphtha (concrete to be C
5～C
10Hydrocarbon comprises alkane and the alkene of arbitrary proportion, positive structure hydrocarbon and isomeric hydrocarbon), the measure of considering to replenish absorption agent simultaneously;
(6) with liquefied ammonia or the charging of propylene cooling and absorbing tower, operate at low temperature on the realization absorption tower, has guaranteed the higher liquefied gas recovery.
Description of drawings
Accompanying drawing 1 reclaims the schematic flow sheet of liquefied gas component in the Fischer-Tropsch process exhaust for the present invention, and accompanying drawing 2 is the schematic flow sheet of embodiment 1,2, wherein
The 1-oil-gas separator; 1-1-oil-gas separator one; 1-2-oil-gas separator two; 1-3-oil-gas separator three; The 2-absorption tower; The 3-Analytic Tower; The 4-stabilizer tower; The 5-regenerator column; 101-membrane sepn tail gas; The 102-absorption agent; 103-replenishes absorption agent; The 104-dry gas; The 105-liquefied gas; 106-discharges absorption agent; 107-circulation absorption agent; 108-waste water a; The 109-frostproofer; 110-waste water b; 111-discharges frostproofer
Embodiment
Further explain method of the present invention below in conjunction with accompanying drawing 1.
A) raw material pretreatment portion
Low temperature oil wash unit utilizes the liquefied gas component that absorbs in the Analytic principle recovery Fischer-Tropsch process exhaust at a lower temperature.Fischer-Tropsch synthesis unit tail gas is with getting into oil-gas separator from the synthesis unit lightweight oil, resolve overhead gas through cooling off after and the rich absorbent at the bottom of the absorption tower also get into oil-gas separator.In oil-gas separator, carry out gas, water, oily three phase separation, as the Analytic Tower charging, gas goes to the absorption tower to oil phase after cooling after heating up.In order to prevent freezing of water, gas is injected into antifreeze glycol solution before cooling.
B) absorb the stable regeneration part
The C that extract out at a poor absorption agent part and the regenerator column top of regenerator column bottom
5～C
6Component comes along other unit, remainingly gets into the top, absorption tower through cooling back as the circulation absorption agent, and the gas that oil-gas separator comes out gets into bottom the absorption tower.It is the C that absorbs in the low temperature oil wash unit feed that the absorption tower mainly acts on
3 +Component (contain C
3Component), overhead gas is the oil wash dry gas, the gas separating device that deoils of the rich absorbent oil at the bottom of the tower.
Remove Analytic Tower from the isolated liquid phase of oil-gas separator.It is the C that removes in the rich absorbent oil that Analytic Tower mainly acts on
2 -Component (contains C
2Component), the overhead gas gas separating device that deoils is deethanizing oil at the bottom of the tower, and deethanizing oil is delivered to stabilizer tower, and stabilizer tower is also referred to as debutanizing tower.
The stabilizer tower overhead product is the liquefied gas product, and oil removes regenerator column at the bottom of the stabilizer tower, and regenerator column is also referred to as depentanizer, extracts C out from the regenerator column top
5～C
6Cut, the poor absorption agent of regeneration at the bottom of the Tata can part after overcooling as absorption agent, part also can all recycle after cooling as absorption agent as other device raw material.
As the case may be, can replenish absorption agent in case of necessity, additional absorption agent is synthetic lightweight oil of Fischer-Tropsch or the unitary petroleum naphtha of unifining, and concrete, this lightweight oil or petroleum naphtha component are C
5～C
10Hydrocarbon comprises alkane and the alkene of arbitrary proportion, positive structure hydrocarbon and isomeric hydrocarbon.
Further explain the present invention with the mode of embodiment below, but the present invention is not limited to these embodiment.
According to flow process shown in Figure 2; (the concrete non-infiltration stream thigh 101 for film separation unit gets into oil-gas separator one with flowing thigh 102 from the synthesis unit lightweight oil to Fischer-Tropsch process exhaust in the present embodiment; Resolve overhead gas through cooling off after and the rich absorbent at the bottom of the absorption tower also get into oil-gas separator one; Under 35 ℃, the operational condition of 2.8MPa, carry out gas, oil, water three phase separation, oil phase after heating up as the Analytic Tower charging, the gas gas separating device two that after the heat exchange cooling, deoils; Under 15 ℃, the operational condition of 2.75MPa, carry out further gas, oil, water three phase separation; The oil phase that obtains returns oil-gas separator one, and the gas cooling gas separating device three that deoils after-30 ℃ carries out gas, oil, the water three phase separation under the low temperature under-20 ℃, the operational condition of 2.7MPa; The oil phase that obtains returns oil-gas separator two, and gas goes to the absorption tower.In order to prevent freezing of water, gas is injected into antifreeze glycol solution 109 before cooling.
(stream strand 107) got into absorption tower after the poor absorption agent that comes from regenerator column bottom was cooled to-30 ℃, and the working pressure on absorption tower is 2.65MPa, and the gas streams 104 that cat head obtains from the absorption tower is the oil wash dry gas, the gas separating device one that deoils of the rich absorbent at the bottom of the tower; After heating up, get into Analytic Tower from the liquid of oil-gas separator one, it is the C that removes in the rich absorbent oil that Analytic Tower mainly acts on
2 -Component (contains C
2Component), the Analytic Tower working pressure is that 2.85MPa, tower top temperature are that 99 ℃, column bottom temperature are 207 ℃, resolves the overhead gas gas separating device one that deoils, and liquid is deethanizing oil at the bottom of the Analytic Tower, and deethanizing oil is delivered to stabilizer tower; The stabilizer tower working pressure is that 1.5MPa, tower top temperature are that 60 ℃, column bottom temperature are 213 ℃, and stable overhead product is a liquefied gas product 105, and oil removes regenerator column at the bottom of the stabilizer tower; The regenerator column working pressure is that 0.5MPa, tower top temperature are that 100 ℃, column bottom temperature are 160 ℃, extracts portion C out from the regenerator column top
5～C
6Cut, the poor absorption agent part at the bottom of the regeneration Tata still is gone to the absorption tower as absorption agent, all the other and regenerator column cat head C after overcooling
5～C
6Cut comes along the unifining unit after mixing.
Absorption agent and virgin gas mol ratio are 0.6 in the present embodiment, do not have the absorption agent of replenishing.
Raw material and product data see Table 1:
Table 1 embodiment 1 logistics data unit: kg/h
| The thing stream number | Media name | Mass rate Kg/ |
| 101 | Membrane sepn tail gas | 73575 |
| 102 | Lightweight oil | 18356 |
| 104 | Dry gas | 51934 |
| 105 | Liquefied gas | 18196 |
| 106 | Discharge absorption agent | 21383 |
| 107 | The circulation absorption agent | 94000 |
| 108 | Waste water | 418 |
With the identical situation of embodiment 1 technology under, only the working pressure with absorption system becomes 4.5MPa by 2.65MPa, all the other parameters are all constant, this moment, raw material and product data were seen table 2:
Table 2 embodiment 2 logistics data units: kg/h
| The thing stream number | Media name | Mass rate Kg/ |
| 101 | Membrane sepn tail gas | 73575 |
| 102 | Lightweight oil | 18356 |
| 104 | Dry gas | 51811 |
| 105 | Liquefied gas | 18657 |
| 106 | Discharge absorption agent | 21031 |
| 107 | The circulation absorption agent | 94000 |
| 108 | Waste water | 432 |
Claims (10)
1. method that reclaims liquefied gas component in the Fischer-Tropsch process exhaust is characterized in that this method may further comprise the steps:
(1) gas-oil separation: the rich absorbent that comes at the bottom of Fischer-Tropsch process exhaust, Analytic Tower overhead gas and the self-absorption Tata carries out the three phase separation of oil, gas, water in oil-gas separator, and oil phase removes Analytic Tower after heating up, and gas phase is gone to the absorption tower after cooling;
(2) absorb: from the next absorption agent cat head entering of regenerator column from the absorption tower through being cooled to certain temperature; Gas from oil-gas separator gets into the bottom, absorption tower after being cooled to certain temperature; Low temperature absorption is carried out in the gas-liquid counter current contact on the absorption tower; Unabsorbed gas goes out from cat head as the product dry gas, and rich absorbent returns oil-gas separator at the bottom of tower, release portion C
2 -Remove Analytic Tower after the component;
(3) resolve: the rich absorbent that comes from the absorption tower carries out oil, gas, water sepn oil-gas separator; Oil phase gets into Analytic Tower after heating up; Carry out high temperature at Analytic Tower and resolve, separate gassing and after cooling, return oil-gas separator, liquid removes stabilizer tower at the bottom of the Analytic Tower after decompression;
(4) stable: liquid under lower pressure, is resolved and is obtained the liquefied gas product in stabilizer tower at the bottom of the Analytic Tower, and liquid removes regenerator column at the bottom of the tower after decompression;
(5) regeneration: liquid is gone into regenerator column at the bottom of the tower from stabilizer tower, extracts a part of C out
5～C
6Component is gone to other unit, and liquid can partly go to other unit at the bottom of the regenerator column, and part goes to the absorption tower to recycle as absorption agent, also can all recycle as absorption agent.
2. the method for claim 1, it is characterized in that: said Fischer-Tropsch process exhaust is non-infiltration gas or other any Fischer-Tropsch synthesis unit tail gas that contains the liquefied gas component of the unitary purified gas of decarburization, film separation unit.
3. the method for claim 1 is characterized in that: oil-gas separator can be provided with a separator or the different a plurality of separators of separation temperature in the said step (1); Before or after this oil-gas separator, be provided with heat-exchange equipment, with so that the isolated gas of oil-gas separator before getting into the absorption tower with temperature be reduced to absorb temperature required; The gas-oil separation process of said step (1) can adopt frostproofer to avoid the icing latch up phenomenon that when service temperature is low, possibly cause.
4. the method for claim 1 is characterized in that: separation temperature be-40～60 ℃ in the said step (1), and pressure is 1.0～6.0MPa, and the middle separation temperature of preferred said step (1) is-25～40 ℃; Pressure is 2.5～4.5MPa; It is 20～120 ℃ that the middle oil phase of said step (1) goes the temperature of Analytic Tower, and it is 65～85 ℃ that the middle oil phase of preferred said step (1) goes the temperature of Analytic Tower; The temperature on absorption agent entering absorption tower is-40～20 ℃ in the said step (2), and the temperature on absorption agent entering absorption tower is-30～-10 ℃ in the preferred said step (2); The number of theoretical plate on absorption tower is 5～40 in the said step (2); Tower top temperature is-40～20 ℃, and column bottom temperature is-40～30 ℃, and working pressure is 1.0～6.0MPa; The number of theoretical plate on absorption tower is 10～20 in the preferred said step (2); Tower top temperature is-10～0 ℃, and column bottom temperature is-10～10 ℃, and working pressure is 2.5～4.5MPa; The number of theoretical plate of Analytic Tower is 5～40 in the said step (3); Tower top temperature is 40～200 ℃, and column bottom temperature is 70～300 ℃, and working pressure is 1.0～6.0MPa; The number of theoretical plate of Analytic Tower is 10-20 in the preferred said step (3); Tower top temperature is 80～120 ℃, and column bottom temperature is 180～220 ℃, and working pressure is 2.5～4.5MPa; The number of theoretical plate of stabilizer tower is 5～40 in the said step (4), and tower top temperature is 20～180 ℃, and column bottom temperature is 80～300 ℃; Working pressure is 0.5～3.0MPa, and reflux ratio is 2～20, and the number of theoretical plate of stabilizer tower is 20～30 in the preferred said step (4); Tower top temperature is 60～90 ℃; Column bottom temperature is 180～230 ℃, and working pressure is 1.0～2.0MPa, and reflux ratio is 2～5; The number of theoretical plate of regenerator column is 3～35 in the said step (5); Tower top temperature is 40～200 ℃, and column bottom temperature is 80～300 ℃, and working pressure is 0.2～1.5MPa; The number of theoretical plate of regenerator column is preferred 10～20 in the preferred said step (5); Tower top temperature is 100～140 ℃, and column bottom temperature is 140～180 ℃, and working pressure is 0.5～1.0MPa;
5. the method for claim 1, it is characterized in that: the molar ratio of said absorption agent and Fischer-Tropsch process exhaust is 0.05～5.
6. method as claimed in claim 5 is characterized in that: the molar ratio of said absorption agent and Fischer-Tropsch process exhaust is 0.1～1.
7. the method for claim 1 is characterized in that: said absorption agent is synthetic lightweight oil of Fischer-Tropsch or petroleum naphtha, and this lightweight oil or petroleum naphtha component are C
5～C
10Hydrocarbon comprises alkane and the alkene of arbitrary proportion, positive structure hydrocarbon and isomeric hydrocarbon.
8. like the described method of arbitrary claim among the claim 1-7, it is characterized in that: inject to absorption tower, regenerator column or other devices and replenish absorption agent.
9. method as claimed in claim 8 is characterized in that: the absorption agent and the former absorption agent that replenish are identical or different.
10. method as claimed in claim 8 is characterized in that: additional absorption agent is synthetic lightweight oil of Fischer-Tropsch or petroleum naphtha, and this lightweight oil or petroleum naphtha component are C
5～C
10Hydrocarbon comprises alkane and the alkene of arbitrary proportion, positive structure hydrocarbon and isomeric hydrocarbon.
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| CN104208983A (en) * | 2014-09-09 | 2014-12-17 | 中科合成油技术有限公司 | Decarburization method of coal-based indirect liquefaction Fischer-Tropsch synthesis tail gas |
| CN105435598A (en) * | 2015-12-11 | 2016-03-30 | 凯天环保科技股份有限公司 | Purifying system for volatile organic exhaust gas |
| CN105441111A (en) * | 2014-08-29 | 2016-03-30 | 亚申科技研发中心（上海）有限公司 | Method for recovering low-carbon hydrocarbons from Fischer-Tropsch synthesis exhausted gas |
| CN105733647A (en) * | 2014-12-09 | 2016-07-06 | 中科合成油工程股份有限公司 | Method for recovering liquefied petroleum gas from Fischer-Tropsch synthesis tail gas |
| CN105779046A (en) * | 2014-12-16 | 2016-07-20 | 中科合成油工程股份有限公司 | Method for preparing LNG (Liquefied Natural Gas) by using Fischer-Tropsch synthesis tail gas as raw material |
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| CN103173239A (en) * | 2013-04-17 | 2013-06-26 | 中国石油化工股份有限公司 | Light hydrocarbon recycling device and process |
| CN103173239B (en) * | 2013-04-17 | 2014-10-01 | 中国石油化工股份有限公司 | Light hydrocarbon recycling device and process |
| CN105441111A (en) * | 2014-08-29 | 2016-03-30 | 亚申科技研发中心（上海）有限公司 | Method for recovering low-carbon hydrocarbons from Fischer-Tropsch synthesis exhausted gas |
| CN105441111B (en) * | 2014-08-29 | 2017-12-15 | 亚申科技研发中心（上海）有限公司 | A kind of method for reclaiming lower carbon number hydrocarbons in F- T synthesis periodic off-gases |
| CN104208983A (en) * | 2014-09-09 | 2014-12-17 | 中科合成油技术有限公司 | Decarburization method of coal-based indirect liquefaction Fischer-Tropsch synthesis tail gas |
| CN105733647A (en) * | 2014-12-09 | 2016-07-06 | 中科合成油工程股份有限公司 | Method for recovering liquefied petroleum gas from Fischer-Tropsch synthesis tail gas |
| CN105733647B (en) * | 2014-12-09 | 2018-05-01 | 中科合成油工程股份有限公司 | The method that liquefied petroleum gas is recycled from Fischer-Tropsch process exhaust |
| CN105779046A (en) * | 2014-12-16 | 2016-07-20 | 中科合成油工程股份有限公司 | Method for preparing LNG (Liquefied Natural Gas) by using Fischer-Tropsch synthesis tail gas as raw material |
| CN105779046B (en) * | 2014-12-16 | 2018-07-10 | 中科合成油工程股份有限公司 | The method that LNG is prepared using Fischer-Tropsch process exhaust as raw material |
| CN105435598A (en) * | 2015-12-11 | 2016-03-30 | 凯天环保科技股份有限公司 | Purifying system for volatile organic exhaust gas |
| CN105435598B (en) * | 2015-12-11 | 2018-02-23 | 凯天环保科技股份有限公司 | Purification of volatile organic waste gas system |
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Address after: 101407 Beijing city Huairou District Yanqi Economic Development Zone C District No. 1 south two Street Park Applicant after: Synefuels China Inc. Applicant after: Zhongke Synthetic Oil Technology Co., Ltd. Address before: 100195 Haidian District, Beijing, North Village, a road, a static core Park, block N Applicant before: Synefuels China Inc. Applicant before: Zhongke Synthetic Oil Technology Co., Ltd. |
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Application publication date: 20120801 |