CN104263442A - Method for removing sulfide and light dydrocarbon from natural gas by utilizing ionic liquid - Google Patents
Method for removing sulfide and light dydrocarbon from natural gas by utilizing ionic liquid Download PDFInfo
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Abstract
The invention discloses a method for removing sulfide and light dydrocarbon from natural gas by utilizing ionic liquid. The method comprises the following steps: taking the ionic liquid or a mixed solvent of the ionic liquid and a molecular solvent as an absorbent to contact with the natural gas and absorb the sulfide, the light dydrocarbon and the carbon dioxide in the natural gas so as to obtain absorption liquid and residual tail gas, wherein the light dydrocarbon is alkane or alkene containing C2-C4; and carrying out two-stage desorption on the absorption liquid so as to desorb the light dydrocarbon and the sulfide in sequence, wherein the absorbent obtained through the desorption is recycled. The method provided by the invention is used for removing the sulfide and the light dydrocarbon from the natural gas by taking the ionic liquid or the mixed solvent of the ionic liquid and the molecular solvent as the absorbent. The designed ionic liquid, the negative ion of which contains a long alkyl side chain, has high selective dissolving capacity for the gas such as hydrogen sulfide and light dydrocarbon and the selective dissolving capacity is superior to that of the conventional ionic liquid, so that the efficient removal of the sulfide and the recovery of the light dydrocarbon are realized.
Description
Technical field
The present invention relates to Sweet natural gas abstraction and purification field, be specifically related to a kind of method utilizing ionic liquid desulfurization from Sweet natural gas to take off lighter hydrocarbons.
Background technology
Sweet natural gas, as a kind of important resource substance, is also particularly important basic material gas in chemical field.Need for some downstream processes, and the recycling of resource, need to carry out desulfurization to Sweet natural gas, and the recovery of lighter hydrocarbons.At present, the desulfurization that more use absorption process is used in Sweet natural gas takes off lighter hydrocarbons.
Publication number is that the Chinese patent literature of CN101016492A discloses a kind of low-temp methanol washing process for natural gas _ raw material gas decarbonization, desulfuration, technical process is: unstripped gas enters absorption tower through absorption tower bottom inlet, the low temperature poor methanol entered with top, absorption tower fully contacts, hydrogen sulfide in unstripped gas and carbonic acid gas are absorbed by poor methanol, the rich methanol liquid absorbing hydrogen sulfide and carbonic acid gas flows out bottom absorption tower, enter poor rich liquid heat exchanger, flash tank flash distillation is entered with after the heat exchange of poor methanol liquid, rich methanol liquid after flash distillation enter poor rich liquid heat exchanger again with the heat exchange of poor methanol liquid, enter gas stripping column top again and carry out air lift, poor methanol liquid is obtained at the bottom of gas stripping column tower, tower top obtains hydrogen sulfide and carbon dioxide.Adopt the technique in this patent, to remove the hydrogen sulfide in natural gas _ raw material gas as absorption agent with methyl alcohol, in overhead gas, hydrogen sulfide content is less than 0.1ppm.
Publication number is the recovery method that the Chinese patent literature of CN1414067A discloses light hydrocarbon in natural gas, after the shallow cold technique of Sweet natural gas, gains are entered in secondary triphase separator and carry out gas-liquid separation, gas is entered to carry out with the absorption agent in absorption tower bottom absorption tower gas-liquid to exchange and generate C
3, C
4reclaim after component; Liquid enters in desorption tower after mixing with the lighter hydrocarbons in secondary triphase separator deviates from methane and ethane, makes the desorption liquid of formation enter Analytic Tower and cuts out C
3, C
4reclaim after component, also have gas and heavy hydrocarbon in Analytic Tower, the heavy hydrocarbon in Analytic Tower is forced into 1.35 ~ 1.55Mpa, is cooled to 38 DEG C ~ 42 DEG C, reclaim after forming lighter hydrocarbons.
In above-mentioned disclosed absorption process, or removal efficiency is not high, or cannot realize desulfurization and de-lighter hydrocarbons simultaneously.
Ionic liquid be completely by specific positive and negative ion form at room temperature or the material that is in a liquid state under being bordering on room temperature, it is tasteless, nonflammable and vapour pressure is extremely low, good to the solvability of gas, can operating restraint wide, a kind of emerging solvent and reaction medium, have a extensive future in the field such as extracting and separating and catalyzed reaction, the favourable absorption as gas and separating agent can be utilized.
As the publication number Chinese patent literature that is CN103055676A discloses a kind of method of purification of Sweet natural gas, step is: a, normal temperature ionic liquid absorption foreign gas; B, water at low temperature compound hydration reaction absorption impurity gas, if Sweet natural gas purity is up to standard, export after Sweet natural gas being passed into kiln drying, otherwise Sweet natural gas reentered ionic liquid absorption room circularly purifying until purity is up to standard; The recycling of c, ionic liquid and water.This patent is with the ethanolic soln purified natural gas of conventional imidazole type ion liquid, but the method can only remove sulfide in Sweet natural gas and carbonic acid gas, for the C in Sweet natural gas
2~ C
4light hydrocarbon component there is no separating effect.
Therefore, be necessary development of new lyosorption and absorption process, realize the efficient removal of Sweet natural gas medium sulphide content and lighter hydrocarbons simultaneously, improve the rate of recovery and economic benefit.
Summary of the invention
The invention provides a kind of with the mixed solvent of ionic liquid or ionic liquid and molecular solvent composition for absorption agent, from Sweet natural gas, desulfurization takes off the method for lighter hydrocarbons.The ionic liquid that designed negatively charged ion contains long alkyl group side chain has the selective dissolution ability of the gases such as very high hydrogen sulfide, lighter hydrocarbons, is better than conventional ionic liquid, thus achieves the recovery of sulfide efficient removal and lighter hydrocarbons.
The invention discloses a kind of method utilizing ionic liquid desulfurization from Sweet natural gas to take off lighter hydrocarbons, step is as follows:
(1) using the mixed solvent of ionic liquid or ionic liquid and molecular solvent as absorption agent, contact with Sweet natural gas, absorb sulfide, lighter hydrocarbons and the carbonic acid gas in Sweet natural gas, be absorbed liquid and residual exhaust;
Described lighter hydrocarbons are main containing C
2~ C
4alkane or alkene;
(2) absorption liquid that step (1) obtains is carried out two sections of desorbs, successively lighter hydrocarbons, sulfide are desorbed, the absorption agent recycle that desorb obtains.
Described ionic liquid is by positively charged ion M
+with anion N-two portions composition, find after deliberation, the ionic liquid of anion N-above containing long alkyl chain has very high lighter hydrocarbons solubleness, optionally can reclaim C from Sweet natural gas
2~ C
4lighter hydrocarbons; This kind of ionic liquid has comparatively suitable alkalescence simultaneously, can realize the selective absorbing of sulfide, and have the features such as low, the wide liquid journey of viscosity, therefore may be used for selexol process and take off lighter hydrocarbons.
As preferably, described anion N-for carbon number be the long-chain fat acid anion (C of 6 ~ 22
nh
2n+1cOO
-, n=5 ~ 21), carbon number be 4 ~ 12 chain alkyl sulphonate negatively charged ion (C
nh
2n+1sO
4 -, n=4 ~ 12), carbon number be 4 ~ 12 chain alkyl phosphoric acid ester negatively charged ion ((C
nh
2n+1)
2pO
4 -, n=4 ~ 12), carbon number be 4 ~ 12 chain alkyl phosphorous acid ester negatively charged ion (C
nh
2n+1hPO
3 -, n=4 ~ 12) in one;
Described positively charged ion M
+for the one in imidazole type positively charged ion, quaternary phosphine type positively charged ion, quaternary ammonium cation, tetramethyleneimine type positively charged ion.Preferably there is substituent imidazole type positively charged ion, there is substituent quaternary phosphine type positively charged ion, there is substituent quaternary ammonium cation, the one had in substituent tetramethyleneimine type positively charged ion.On described imidazole type positively charged ion, quaternary phosphine type positively charged ion, quaternary ammonium cation and tetramethyleneimine type positively charged ion with substituting group independent separately, and its kind strictly not to be limited, can C be selected
4~ C
16alkyl, substituent number can be monosubstituted or polysubstituted (as two replace or three replace etc.), substituting group time polysubstituted in different loci can be the same or different.
For the ionic liquid with viscosity higher, then can add molecular solvent wherein as thinner, improve mobility, form the mixed solvent of ionic liquid and organic solvent.
As preferably, described molecular solvent is C
6~ C
16hydro carbons, aromatic hydrocarbons, DMF or N-Methyl pyrrolidone; Described aromatic hydrocarbons can be benzene,toluene,xylene etc.
As preferably, the percent by volume of the mixed solvent Middle molecule solvent of described ionic liquid and molecular solvent is 0.1 ~ 20%.
But in order to more completely reclaim absorption agent, reaching and better deviating from effect, preferred pure ionic liquid makes absorption agent as much as possible.
Further preferably, described ionic liquid is 4-butyl-phosphonium n-caproic acid salt, TBuA n-caprylic acid salt, 1-butyl-2,3-methylimidazole sulfate pentahydrate, N, N-butyl methyl tetramethyleneimine dibutyl phosphate, the own ester of N, N-butyl ethyl tetramethyleneimine phosphorous acid or three hexyl tetradecyl ammonium phosphorous acid butyl esters.Above-mentioned preferred ionic liquid is all to sulfide and C
2~ C
4lighter hydrocarbons there is splendid solubleness and the separation selectivity of excellence, the decreasing ratio of sulfide is greater than 95%, and the decreasing ratio of lighter hydrocarbons is greater than 92%.
As preferably, in step (1), by the condition of sulfide, lighter hydrocarbons and carbonic acid gas in absorption agent absorption Sweet natural gas be: temperature is 5 ~ 30 DEG C, and pressure is 0.1 ~ 3.0MPa; More preferably 15 DEG C, 1.0MPa.Research shows that temperature is too low, and the mobility of ionic liquid is deteriorated, and temperature is too high, and the solubleness of sulfide and lighter hydrocarbons significantly declines, and higher absorption pressure is conducive to desulfurization and takes off lighter hydrocarbons.
In step (2), the Desorption separation condition of lighter hydrocarbons is: temperature is 35 ~ 80 DEG C, and pressure is 0.1 ~ 0.8MPa; More preferably 65 DEG C, 0.2MPa.
The Desorption separation condition of sulfide is: temperature is 60 ~ 120 DEG C, and pressure is 0.01 ~ 0.2MPa; More preferably 100 DEG C, 0.1MPa.
The described concrete steps utilizing ionic liquid desulfurization from Sweet natural gas to take off the method for lighter hydrocarbons are:
(1) absorption agent is cooled to 5 ~ 30 DEG C, under pressure is 0.1 ~ 3.0MPa, contacts with the Sweet natural gas being cooled to 5 ~ 30 DEG C, absorb sulfide, lighter hydrocarbons and the carbonic acid gas in Sweet natural gas, be absorbed liquid and residual exhaust;
(2) absorption liquid that step (1) obtains is carried out two sections of desorbs, first 35 ~ 80 DEG C, lighter hydrocarbons and a part of carbonic acid gas are desorbed under 0.1 ~ 0.8MPa, again 60 ~ 120 DEG C, Desorption separation obtains sulfide and residual carbon dioxide, the absorption agent recycle that desorb obtains under 0.01 ~ 0.2MPa.
As preferably, the way of contact of described absorption agent and Sweet natural gas is counter current contact, better can improve mass transfer effect.
Compared with prior art, tool of the present invention has the following advantages:
1. adopt ionic liquid as absorption agent, the thermostability had, extremely low saturated vapor pressure, the repeatedly recycling of absorption agent can be realized by heating under reduced pressure, and any ionic liquid steam can not be produced and product is polluted in desorption of gases.
2. the ionic liquid that the negatively charged ion designed by the present invention contains long alkyl group side chain has the selective dissolution ability of the gases such as very high hydrogen sulfide, lighter hydrocarbons, is better than conventional ionic liquid, thus achieves the recovery of sulfide efficient removal and lighter hydrocarbons.
3. the operational path designed by the present invention and ionic liquid achieve sulfide and remove the coupling with lighter hydrocarbons recovery, simplify operational path, improve economic benefit.
4. the inventive method with ionic liquid or the solvent that is made up of ionic liquid and organic solvent for absorption agent, adopt the method for absorption-desorb, remove the sulfide in Sweet natural gas and lighter hydrocarbons, and the continuous circulation that can realize ionic liquid uses, there is the advantages such as separation efficiency is high, solvent consumption is few, safety and environmental protection, applicable suitability for industrialized production.
Embodiment:
It is as follows that the present invention utilizes ionic liquid desulfurization from Sweet natural gas to take off the concrete steps of the method for lighter hydrocarbons:
1. raw natural gas is forced into 0.1MPa ~ 3.0MPa through compressor, temperature is made to be down to 5 DEG C ~ 30 DEG C by cooling, pass into bottom absorbing tower, absorption tower tower top adds the mixed solvent of pure ionic liquid absorption agent or ionic liquid and molecular solvent, guarantees wherein most C
2~ C
4hydro carbons and organic sulfide are absorbed, and obtain being rich in C at the bottom of tower
2~ C
4the absorption liquid of hydro carbons and organic sulfide, tower top obtains methane-rich gas.
2. absorption liquid at the bottom of tower enters lighter hydrocarbons desorption tower, adopts the method for intensification desorb, first controls desorption temperature at 35 ~ 80 DEG C, or employing heats up, reduces pressure and use desorb, and pressure range is 0.1 ~ 0.8MPa.Tower top obtains C
2~ C
4lighter hydrocarbons and partial CO 2, the absorption liquid being rich in the sulfocompounds such as hydrogen sulfide and carbonic acid gas is obtained at the bottom of tower, then absorption liquid is passed into sulfide desorption tower, intensification, decompression desorb, temperature is 60 ~ 120 DEG C, pressure is sulfocompound and the carbonic acid gas such as 0.01 ~ 0.2MPa, tower top hydrogen sulfide, and be absorbed at the bottom of tower agent recycle and reuse.
Embodiment 1
Absorption agent forms: [P
4444] [C
5h
11cOO] the pure ionic liquid absorption agent of 4-butyl-phosphonium n-caproic acid salt.Raw natural gas composition (mol ratio): methane 79.8%, ethane 1.9%, propane 7.6%, butane 5.6%, hydrogen sulfide 1.1%, thioether 305mg/m
3, mercaptan 421mg/m
3and other components.
Raw natural gas is forced into 1.0MPa through compressor, and make temperature be down to 15 DEG C by cooling, pass into bottom absorbing tower, absorption tower tower top adds absorption agent, guarantees wherein most C
2~ C
4hydro carbons and organic sulfide are absorbed, and what obtain at the bottom of tower is rich in C
2~ C
4the absorption liquid of hydro carbons and organic sulfide, the H that tower top obtains methane-rich gas and is dissolved in hardly on a small quantity in absorption agent
2, CO, N
2deng gas.
Absorption liquid at the bottom of tower enters lighter hydrocarbons desorption tower, and adopt the method for intensification desorb, desorption temperature controls at 65 DEG C.Tower top obtains C
2~ C
4lighter hydrocarbons, obtain the absorption liquid being rich in the sulfocompounds such as hydrogen sulfide, then absorption liquid are passed into sulfide desorption tower at the bottom of tower, intensification, decompression desorb, temperature is 100 DEG C, and pressure is 0.1MPa, and tower top obtains the sulfocompounds such as hydrogen sulfide, obtains [P at the bottom of tower
4444] [C
5cOO] ionic liquid absorption agent, recycle and reuse.Hydrogen sulfide stripping rate: 98.5%, thioether decreasing ratio: 93.3%, Mercaptan removal rate: 94.5%, ethane decreasing ratio: 91.5%, propane decreasing ratio: 94.8%, butane decreasing ratio 96.5%.
Embodiment 2
Absorption agent forms: [N
4444] [C
7h
15cOO] the pure ionic liquid absorption agent of TBuA n-caprylic acid salt.Raw natural gas composition (mol ratio): methane 81.5%, ethane 8.5%, propane 8.5%, butane 5.1%, hydrogen sulfide 1.0% and other components.
As embodiment 1, raw natural gas and absorption agent 5 DEG C, counter current contact absorbs under 2.5MPa, absorption liquid heats up at 50 DEG C and separates sucking-off light hydrocarbon components, and absorption liquid to heat up decompression desorb through alkane desorption tower again, 90 DEG C, separate sucking-off hydrogen sulfide under 0.1MPa, be absorbed at the bottom of tower agent recycle and reuse.Hydrogen sulfide stripping rate: 97.6%, ethane decreasing ratio: 91.4%, propane decreasing ratio: 95.2%, butane decreasing ratio 97.7%.
Embodiment 3
Absorption agent forms: [bmpyrr] [Bu
2pO
4] N, N-butyl methyl tetramethyleneimine dibutyl phosphate ionic liquid, N-Methyl pyrrolidone composite absorber, ionic liquid accounts for 95% (volume fraction).Raw natural gas composition (mol ratio): methane 88.2%, ethane 5.9%, propane 2.0%, butane 0.9%, hydrogen sulfide 1.2% and other components.
As embodiment 1, raw natural gas and absorption agent 10 DEG C, counter current contact absorbs under 1.8MPa, absorption liquid 55 DEG C heats up and separates sucking-off light hydrocarbon component, and absorption liquid to heat up decompression desorb through sulfide desorption tower again, 85 DEG C, separate sucking-off hydrogen sulfide under 0.05MPa, be absorbed at the bottom of tower agent recycle and reuse.Hydrogen sulfide stripping rate: 97.5%, ethane decreasing ratio: 92.1%, propane decreasing ratio: 96.7%, butane decreasing ratio 97.1%.
Embodiment 4
Absorption agent forms: [bepyrr] [HexHPO
3] the own ester ionic liquid of N, N-butyl ethyl tetramethyleneimine phosphorous acid.Raw natural gas composition (mol ratio): methane 76.3%, ethane 11.0%, propane 6.0%, butane 2.9%, hydrogen sulfide 0.9%, carbonic acid gas 0.4% and other components.
As embodiment 1, raw natural gas and absorption agent 20 DEG C, counter current contact absorbs under 2.8MPa, absorption liquid 80 DEG C of intensification desorbs, tower top obtains C
2~ C
4lighter hydrocarbons and partial CO 2, residual absorption liquid at the bottom of tower to heat up decompression desorb through sulfide desorption tower again, 110 DEG C, separate sucking-off hydrogen sulfide under 0.12MPa, be absorbed at the bottom of tower agent recycle and reuse.Hydrogen sulfide stripping rate: 96.7%, ethane decreasing ratio: 92.4%, propane decreasing ratio: 94.4%, butane decreasing ratio 95.1%.
Embodiment 5
Absorption agent forms: [bmmim] [BuSO
4] 1-butyl-2,3-methylimidazole sulfate pentahydrate ionic liquid and DMF composite absorber, ionic liquid volume fraction is 80%.Raw natural gas composition (mol ratio): methane 52.3%, ethane 20.3%, propane 11.6%, butane 5.6%, hydrogen sulfide 1.1%, carbonic acid gas 0.6%, mercaptan 421mg/m
3and other components.
As embodiment 1, raw natural gas and absorption agent 10 DEG C, counter current contact absorbs under 1.5MPa, absorption liquid 55 DEG C, 0.3MPa heat up decompression desorb, and tower top obtains C
2~ C
4lighter hydrocarbons and partial CO 2, residual absorption liquid at the bottom of tower to heat up decompression desorb through sulfide desorption tower again, 95 DEG C, separate sucking-off hydrogen sulfide sulfides under 0.08MPa, be absorbed at the bottom of tower agent recycle and reuse.Hydrogen sulfide stripping rate: 98.2%, Mercaptan removal rate: 98.9%, ethane decreasing ratio: 92.2%, propane decreasing ratio: 93.1%, butane decreasing ratio 94.2%.
Embodiment 6
Absorption agent forms: [N
666 (14)] [BuHPO
3] three hexyl tetradecyl ammonium phosphorous acid butyl ester ionic liquid absorption agent, raw natural gas composition (mol ratio): methane 96.4%, ethane 0.7%, propane 0.2%, butane 0.1%, hydrogen sulfide 0.7% and other components.
As embodiment 1, raw natural gas and absorption agent 30 DEG C, counter current contact absorbs under 0.8MPa, absorption liquid 70 DEG C of intensification desorbs, tower top obtains C
2~ C
4lighter hydrocarbons, residual absorption liquid at the bottom of tower to heat up decompression desorb through sulfide desorption tower again, 100 DEG C, separate sucking-off hydrogen sulfide under 0.15MPa, be absorbed at the bottom of tower agent recycle and reuse.Hydrogen sulfide stripping rate: 97.7%, ethane decreasing ratio: 92.7%, propane decreasing ratio: 93.2%, butane decreasing ratio 94.1%.
Comparative example 1
Absorption agent forms: [bmim] [OAc] 1-butyl-3-Methylimidazole acetate ionic liquid.Raw natural gas composition (mol ratio): methane 76.1%, ethane 8.7%, propane 7.8%, butane 5.0%, other components 1.4% such as hydrogen sulfide 1.0% and nitrogen.
As embodiment 1, raw natural gas and absorption agent 15 DEG C, counter current contact absorbs under 1.0MPa, absorption liquid 65 DEG C of intensification desorbs, tower top obtains C
2~ C
4lighter hydrocarbons, residual absorption liquid at the bottom of tower to heat up decompression desorb through sulfide desorption tower again, 100 DEG C, separate sucking-off hydrogen sulfide under 0.1MPa, be absorbed at the bottom of tower agent recycle and reuse.Hydrogen sulfide stripping rate: 90.3%, ethane decreasing ratio: 75.3%, propane decreasing ratio: 80.3%, butane decreasing ratio 82.1%.
Comparative example 2
Absorption agent forms: [bmpyrr] [Me
2pO
4] N, N-butyl methyl tetramethyleneimine dimethyl phosphate ionic liquid.Raw natural gas composition (mol ratio): methane 77.7%, ethane 7.5%, propane 7.1%, butane 4.9%, other components 1.6% such as hydrogen sulfide 1.2% and nitrogen.
As embodiment 1, raw natural gas and absorption agent 10 DEG C, counter current contact absorbs under 1.9MPa, absorption liquid 60 DEG C heats up and separates sucking-off light hydrocarbon component, and absorption liquid to heat up decompression desorb through sulfide desorption tower again, 85 DEG C, separate sucking-off hydrogen sulfide under 0.05MPa, be absorbed at the bottom of tower agent recycle and reuse.Hydrogen sulfide stripping rate: 92.3%, ethane decreasing ratio: 80.1%, propane decreasing ratio: 82.2%, butane decreasing ratio: 84.7%.
Comparative example 3
Absorption agent forms: [bmmim] [MeSO
4] 1-butyl-2,3-methylimidazole methyl sulfate ion liquid.Raw natural gas composition (mol ratio): methane 60.1%, ethane 15.3%, propane 10.8%, butane 5.1%, hydrogen sulfide 1.4%, carbonic acid gas 0.7%, mercaptan 381mg/m
3, all the other are nitrogen.
As embodiment 1, raw natural gas and absorption agent are at 10 DEG C, and under 2.0MPa, counter current contact absorbs, and absorption liquid 55 DEG C, 0.1MPa intensification decompression desorb, tower top obtains C
2~ C
4lighter hydrocarbons and partial CO 2, residual absorption liquid at the bottom of tower to heat up decompression desorb through sulfide desorption tower again, 95 DEG C, separate sucking-off hydrogen sulfide sulfides under 0.05MPa, be absorbed at the bottom of tower agent recycle and reuse.Hydrogen sulfide stripping rate: 88.6%, Mercaptan removal rate: 89.3%, CO2 removal rate: 80.3%, ethane decreasing ratio: 70.3%, propane decreasing ratio: 73.4%, butane decreasing ratio 76.1%.
Claims (8)
1. utilize ionic liquid desulfurization from Sweet natural gas to take off a method for lighter hydrocarbons, it is characterized in that, comprise the steps:
(1) using the mixed solvent of ionic liquid or ionic liquid and molecular solvent as absorption agent, contact with Sweet natural gas, absorb sulfide, lighter hydrocarbons and the carbonic acid gas in Sweet natural gas, be absorbed liquid and residual exhaust;
Described lighter hydrocarbons are main containing C
2~ C
4alkane or alkene;
(2) absorption liquid that step (1) obtains is carried out two sections of desorbs, successively lighter hydrocarbons, sulfide are desorbed, the absorption agent recycle that desorb obtains.
2. method according to claim 1, is characterized in that, described ionic liquid is by positively charged ion M
+with anion N-two portions composition, anion N-for carbon number be 6 ~ 22 long-chain fat acid anion, the carbon number chain alkyl sulphonate negatively charged ion that is 4 ~ 12, the carbon number chain alkyl phosphoric acid ester negatively charged ion that is 4 ~ 12, carbon number be the one in the chain alkyl phosphorous acid ester negatively charged ion of 4 ~ 12; Positively charged ion M
+for the one in imidazole type positively charged ion, quaternary phosphine type positively charged ion, quaternary ammonium cation, tetramethyleneimine type positively charged ion.
3. method according to claim 1, is characterized in that, described molecular solvent is C
6~ C
16hydro carbons, aromatic hydrocarbons, DMF or N-Methyl pyrrolidone;
The percent by volume of the mixed solvent Middle molecule solvent of described ionic liquid and molecular solvent is 0.1 ~ 20%.
4. the method according to the arbitrary claim of claims 1 to 3, is characterized in that, described absorption agent is ionic liquid.
5. method according to claim 4, it is characterized in that, described ionic liquid is 4-butyl-phosphonium n-caproic acid salt, TBuA n-caprylic acid salt, 1-butyl-2,3-methylimidazole sulfate pentahydrate, N, N-butyl methyl tetramethyleneimine dibutyl phosphate, the own ester of N, N-butyl ethyl tetramethyleneimine phosphorous acid or three hexyl tetradecyl ammonium phosphorous acid butyl esters.
6. the method according to claim 1 or 2 or 5, is characterized in that, in step (1), the condition of the sulfide, lighter hydrocarbons and the carbonic acid gas that absorb in Sweet natural gas with absorption agent is: temperature is 5 ~ 30 DEG C, and pressure is 0.1 ~ 3.0MPa;
In step (2), the Desorption separation condition of lighter hydrocarbons is: temperature is 35 ~ 80 DEG C, and pressure is 0.1 ~ 0.8MPa;
The Desorption separation condition of sulfide is: temperature is 60 ~ 120 DEG C, and pressure is 0.01 ~ 0.2MPa.
7. method according to claim 6, is characterized in that, the concrete steps of described method are:
(1) absorption agent is cooled to 5 ~ 30 DEG C, under pressure is 0.1 ~ 3.0MPa, contacts with the Sweet natural gas being cooled to 5 ~ 30 DEG C, absorb sulfide, lighter hydrocarbons and the carbonic acid gas in Sweet natural gas, be absorbed liquid and residual exhaust;
(2) absorption liquid that step (1) obtains is carried out two sections of desorbs, first 35 ~ 80 DEG C, lighter hydrocarbons and a part of carbonic acid gas are desorbed under 0.1 ~ 0.8MPa, again 60 ~ 120 DEG C, Desorption separation obtains sulfide and residual carbon dioxide, the absorption agent recycle that desorb obtains under 0.01 ~ 0.2MPa.
8. method according to claim 7, is characterized in that, described absorption agent and the way of contact of Sweet natural gas are counter current contact.
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| CN106474869A (en) * | 2016-10-14 | 2017-03-08 | 浙江大学 | A kind of method of absorption and separation lighter hydrocarbons from dry gas or industrial tail gas |
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| CN108479309A (en) * | 2018-04-13 | 2018-09-04 | 南昌大学 | A kind of novel H based on strong basicity proton type ionic liquid2S formulation absorption agent |
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| CN111826212A (en) * | 2020-07-01 | 2020-10-27 | 中煤玮坤(北京)节能环保科技有限公司 | Carbon dioxide capture system and method for blast furnace gas fine desulfurization |
| CN114558549A (en) * | 2020-11-27 | 2022-05-31 | 北京驭碳科技有限公司 | Use of carboxylate compounds as absorbents for capturing carbon dioxide |
| CN112604457A (en) * | 2020-12-09 | 2021-04-06 | 北京化工大学 | Process for dehydrating natural gas by using mixed solvent of ionic liquid and triethylene glycol |
| CN114835573A (en) * | 2021-02-01 | 2022-08-02 | 中国科学院化学研究所 | Method for synthesizing carboxylate compound |
| CN114835573B (en) * | 2021-02-01 | 2023-04-18 | 中国科学院化学研究所 | Method for synthesizing carboxylate compound |
| CN113101782A (en) * | 2021-04-08 | 2021-07-13 | 浙江工业大学 | Functionalized ionic liquid absorption liquid and preparation method and application thereof |
| CN114950079A (en) * | 2022-06-16 | 2022-08-30 | 中国科学院过程工程研究所 | Physical-chemical coupling selective absorption of CO 2 Functional ionic solvent of (2) |
| CN114950079B (en) * | 2022-06-16 | 2024-01-30 | 中国科学院过程工程研究所 | Physical-chemical coupling selective absorption CO 2 Functional ionic solvents of (2) |
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