CN104263442B - A kind of method utilizing ionic liquid desulfurization from natural gas to take off lighter hydrocarbons - Google Patents
A kind of method utilizing ionic liquid desulfurization from natural gas to take off lighter hydrocarbons Download PDFInfo
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Abstract
The present invention discloses a kind of method utilizing ionic liquid desulfurization from natural gas to take off lighter hydrocarbons, first using the mixed solvent of ionic liquid or ionic liquid and molecular solvent as absorbent, contacting with natural gas, absorb sulfide, lighter hydrocarbons and the carbon dioxide in natural gas, be absorbed liquid and residual exhaust；Described lighter hydrocarbons are for mainly containing C2～C4Alkane or alkene；Described absorbing liquid carrying out two sections of desorptions again, lighter hydrocarbons, sulfide is desorbed successively, the absorbent that desorption obtains recycles.The invention provides a kind of mixed solvent with ionic liquid or ionic liquid and molecular solvent composition as absorbent, the method that desulfurization takes off lighter hydrocarbons from natural gas.The ionic liquid that designed anion contains long alkyl side chain has the selective dissolution ability of the gases such as the highest hydrogen sulfide, lighter hydrocarbons, is better than conventional ionic liquid, it is achieved thereby that sulfide efficient removal and the recovery of lighter hydrocarbons.
Description
Technical field
The present invention relates to natural gas separate and purification art, be specifically related to one and utilize ionic liquid from sky
The method that so in gas, desulfurization takes off lighter hydrocarbons.
Background technology
Natural gas, as a kind of important resource substance, is also particularly important basis in chemical field
Unstripped gas.Need for some downstream processes, and the recycling of resource, need natural gas is entered
Row desulfurization, and the recovery of lighter hydrocarbons.At present, the desulfurization in natural gas of the more use absorption process
De-lighter hydrocarbons.
The Chinese patent literature of Publication No. CN101016492A discloses a kind of for gas material
The low-temp methanol washing process of gas decarbonization desulfurization, technological process is: unstripped gas enters through absorption tower bottom inlet
Entering absorption tower, the low temperature poor methanol entered with top, absorption tower is fully contacted, the hydrogen sulfide in unstripped gas
Absorbed by poor methanol with carbon dioxide, absorb the rich methanol liquid of hydrogen sulfide and carbon dioxide from absorption tower
Bottom is flowed out, and enters flash tank flash distillation after entering poor rich liquid heat exchanger, with poor methanol liquid heat exchange, through dodging
Rich methanol liquid after steaming enter poor rich liquid heat exchanger again with poor methanol liquid heat exchange, enter back on stripping tower
Portion carries out air lift, obtains poor methanol liquid at the bottom of stripping tower tower, and tower top obtains hydrogen sulfide and carbon dioxide.
Use the technique in this patent, make the hydrogen sulfide in absorbent removing natural gas _ raw material gas, tower with methyl alcohol
In top gas body, hydrogen sulfide content is less than 0.1ppm.
The Chinese patent literature of Publication No. CN1414067A discloses the recovery side of light hydrocarbon in natural gas
Method, makes gains carry out gas-liquid separation in entering two grades of three phase separators after the shallow cold technique of natural gas,
Make gas enter bottom absorption tower and carry out gas-liquid exchange generation C with the absorbent in absorption tower3、C4Component
Rear recovery；Enter after lighter hydrocarbons mixing in liquid and two grades of three phase separators in desorption tower abjection methane and
Ethane, makes the desorption liquid of formation enter Analytic Tower and cuts out C3、C4Reclaim after component, in Analytic Tower also
Have gas and heavy hydrocarbon, the heavy hydrocarbon in Analytic Tower be forced into 1.35～1.55Mpa, be cooled to 38 DEG C～
42 DEG C, reclaim after forming lighter hydrocarbons.
In absorption process disclosed above, or removal efficiency is the highest, or cannot realize desulfurization simultaneously
With de-lighter hydrocarbons.
Ionic liquid is in room temperature or being closely in a liquid state at room temperature of being made up of specific positive and negative ion completely
Material, it is tasteless, nonflammable and vapour pressure is extremely low, good to the dissolubility of gas, operable model
Enclose width, be a kind of emerging solvent and reaction medium, should in the field such as extract and separate and catalytic reaction
With having a extensive future, it is possible to use as good adsorption and the release agent of gas.
As the Chinese patent literature of Publication No. CN103055676A discloses the purification of a kind of natural gas
Method, step is: a, normal temperature ionic liquid absorption foreign gas；B, water at low temperature compound hydration reaction
Absorb foreign gas, if natural gas purity is up to standard, natural gas is passed through hothouse and exports after drying, no
Then natural gas is reentered ionic liquid absorption room circularly purifying until purity is up to standard；C, ionic liquid
Body and the recycling of water.This patent is with the ethanol solution purifying natural of conventional imidazole type ion liquid
Gas, but the method can only remove the sulfide in natural gas and carbon dioxide, in natural gas
C2～C4Light hydrocarbon component there is no separating effect.
Therefore, it is necessary to exploitation novel absorbent solvent and absorption process, realize natural gas vulcanizes simultaneously
Thing and the efficient removal of lighter hydrocarbons, improve the rate of recovery and economic benefit.
Summary of the invention
The invention provides a kind of mixing with ionic liquid or ionic liquid and molecular solvent composition molten
Agent is absorbent, the method that desulfurization takes off lighter hydrocarbons from natural gas.Designed anion contains long alkyl
The ionic liquid of side chain has the selective dissolution ability of the gases such as the highest hydrogen sulfide, lighter hydrocarbons, is better than
Conventional ionic liquid, it is achieved thereby that sulfide efficient removal and the recovery of lighter hydrocarbons.
The invention discloses a kind of method utilizing ionic liquid desulfurization from natural gas to take off lighter hydrocarbons, step
As follows:
(1) using the mixed solvent of ionic liquid or ionic liquid and molecular solvent as absorbent, with
Natural gas contacts, and absorbs sulfide, lighter hydrocarbons and carbon dioxide in natural gas, and be absorbed liquid and surplus
Remaining tail gas；
Described lighter hydrocarbons are for mainly containing C2～C4Alkane or alkene；
(2) absorbing liquid that step (1) obtains is carried out two sections of desorptions, successively by lighter hydrocarbons, sulfide
Desorbing, the absorbent that desorption obtains recycles.
Described ionic liquid is by cation M+Form with anion N-two parts, it has been investigated that,
The ionic liquid of anion N-above contain long alkyl chain has the highest lighter hydrocarbons solubility, it is possible to selectivity
From natural gas reclaim C2～C4Lighter hydrocarbons；This kind of ionic liquid has the most suitable alkali simultaneously
Property, the selective absorbing of sulfide can be realized, and there is the features such as viscosity liquid journey low, wide, therefore may be used
Lighter hydrocarbons are taken off for selexol process.
As preferably, described anion N-for long-chain fat acid anion that carbon number is 6～22
(CnH2n+1COO-, n=5～21), carbon number be 4～12 chain alkyl sulphonic acid ester anion
(CnH2n+1SO4 -, n=4～12), carbon number be 4～12 chain alkyl phosphate anion
((CnH2n+1)2PO4 -, n=4～12), carbon number be 4～12 chain alkyl phosphite ester anion
(CnH2n+1HPO3 -, n=4～12) in one；
Described cation M+For imidazole type cation, season type cation, quaternary ammonium cation,
One in pyrrolidines type cation.Preferably there is the imidazole type cation of substituent, there is replacement
The season type cation of base, there is the quaternary ammonium cation of substituent, there is the pyrrolidines type of substituent
One in cation.Described imidazole type cation, season type cation, quaternary ammonium cation and
On pyrrolidines type cation with substituent each independent, and its kind is strictly limited
Fixed, can be selected for C4～C16Alkyl, the number of substituent can be monosubstituted or polysubstituted (as two take
Generation or three replacements etc.), time polysubstituted, the substituent in different loci can be the same or different.
For having the ionic liquid of viscosity higher, then can add molecular solvent wherein as dilution
Agent, improves mobility, forms the mixed solvent of ionic liquid and organic solvent.
As preferably, described molecular solvent is C6～C16Hydro carbons, aromatic hydrocarbons, N, N-dimethyl formyl
Amine or 1-METHYLPYRROLIDONE；Described aromatic hydrocarbons can be benzene,toluene,xylene etc..
As preferably, the volume hundred of the mixed solvent Middle molecule solvent of described ionic liquid and molecular solvent
Mark is 0.1～20%.
But in order to more completely reclaim absorbent, reach preferably to deviate from effect, the purest
Ionic liquid makees absorbent.
Further preferably, described ionic liquid is tetrabutyl n-caproic acid salt, TBuA caprylic acid
Salt, 1-butyl-2,3-methylimidazole sulfate pentahydrate, N, N-butyl methyl pyrrolidines dibutylphosphoric acid ester,
N, the N-butyl ethyl own ester of pyrrolidines phosphorous acid or three hexyl myristyl ammonium phosphorous acid butyl esters.Above-mentioned excellent
The ionic liquid of choosing is all to sulfide and C2～C4Lighter hydrocarbons have splendid solubility and excellence point
From selectivity, the removal efficiency of sulfide is more than 95%, and the removal efficiency of lighter hydrocarbons is more than 92%.
As preferably, in step (1), with absorbent absorb the sulfide in natural gas, lighter hydrocarbons and
The condition of carbon dioxide is: temperature is 5～30 DEG C, and pressure is 0.1～3.0MPa；More preferably
15℃、1.0MPa.Research shows that temperature is too low, and the mobility of ionic liquid is deteriorated, and temperature is too high then
The solubility of sulfide and lighter hydrocarbons is remarkably decreased, and higher absorption pressure is conducive to desulfurization to take 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.
Concretely comprising the following steps of the described method utilizing ionic liquid desulfurization from natural gas to take off lighter hydrocarbons:
(1) absorbent is cooled to 5～30 DEG C, under pressure is 0.1～3.0MPa, and is cooled to
The natural gas contact of 5～30 DEG C, absorbs sulfide, lighter hydrocarbons and the carbon dioxide in natural gas, is inhaled
Receive liquid and residual exhaust；
(2) absorbing liquid that step (1) obtains is carried out two sections of desorptions, first 35～80 DEG C,
Under 0.1～0.8MPa, lighter hydrocarbons and a part of carbon dioxide are desorbed, then 60～120 DEG C,
Under 0.01～0.2MPa, Desorption separation obtains sulfide and residual carbon dioxide, the absorbent that desorption obtains
Recycle.
As preferably, described absorbent is counter current contacting with the way of contact of natural gas, can be more preferable
Improve mass transfer effect.
Compared with prior art, present invention have the advantage that
1. use ionic liquid as absorbent, the heat endurance having had, extremely low saturated vapor pressure,
The repeatedly recycling of absorbent can be realized by heating under reduced pressure, and will not produce in gas desorption
Give birth to any ionic liquid steam and product is polluted.
2. the ionic liquid that the anion designed by the present invention contains long alkyl side chain has the highest sulphur
Change the selective dissolution ability of the gas such as hydrogen, lighter hydrocarbons, be better than conventional ionic liquid, it is achieved thereby that sulphur
Compound efficient removal and the recovery of lighter hydrocarbons.
3. process route and ionic liquid designed by the present invention achieve sulfide removing and return with lighter hydrocarbons
The coupling received, simplifies process route, improves economic benefit.
4. the inventive method with ionic liquid or the solvent that is made up of ionic liquid and organic solvent is
Absorbent, the method using absorption and desorption, the sulfide in removing natural gas and lighter hydrocarbons, it is possible to
Realize the continuous recycling of ionic liquid, have that separative efficiency is high, solvent consumption is few, safety and environmental protection,
It is suitable for the advantages such as industrialized production.
Detailed description of the invention:
The present invention utilizes ionic liquid desulfurization from natural gas to take off the specifically comprising the following steps that of method of lighter hydrocarbons
1. raw natural gas is forced into 0.1MPa～3.0MPa through compressor, makes temperature by cooling
Being down to 5 DEG C～30 DEG C, be passed through bottom absorbing tower, absorption tower tower top adds pure ionic liquid absorption
The mixed solvent of agent or ionic liquid and molecular solvent, it is ensured that the C of wherein most2～C4Hydro carbons and having
Machine sulfide is absorbed, and obtains rich in C at the bottom of tower2～C4Hydro carbons and the absorbing liquid of organic sulfur compound, tower top
Obtain methane-rich gas.
2. absorbing liquid at the bottom of tower enters lighter hydrocarbons desorber, the method using the desorption that heats up, first will desorption temperature
Degree control at 35～80 DEG C, or use heat up, reduce pressure and with desorb, pressure limit is 0.1～0.8MPa.
Tower top obtains C2～C4Lighter hydrocarbons and partial CO 2, obtain rich in sulfur-containing compounds such as hydrogen sulfide at the bottom of tower
With the absorbing liquid of carbon dioxide, then absorbing liquid is passed through sulfide desorber, heats up, desorption of reducing pressure,
The sulfur-containing compounds and two such as temperature is 60～120 DEG C, and pressure is 0.01～0.2MPa, tower top hydrogen sulfide
Carbonoxide, be absorbed at the bottom of tower agent recycle and reuse.
Embodiment 1
Absorbent forms: [P4444][C5H11COO] the pure ionic liquid absorption of tetrabutyl n-caproic acid salt
Agent.Raw natural gas composition (mol ratio): methane 79.8%, ethane 1.9%, propane 7.6%, fourth
Alkane 5.6%, hydrogen sulfide 1.1%, thioether 305mg/m3, mercaptan 421mg/m3And other components.
Raw natural gas is forced into 1.0MPa through compressor, makes temperature be down to 15 DEG C by cooling,
Being passed through bottom absorbing tower, absorption tower tower top adds absorbent, it is ensured that the C of wherein most2～C4
Hydro carbons and organic sulfur compound are absorbed, obtain at the bottom of tower rich in C2～C4Hydro carbons and the suction of organic sulfur compound
Receiving liquid, tower top obtains methane-rich gas and is practically insoluble in the H in absorbent on a small quantity2、CO、N2
Deng gas.
Absorbing liquid at the bottom of tower enters lighter hydrocarbons desorber, and the method using the desorption that heats up, desorption temperature controls
65℃.Tower top obtains C2～C4Lighter hydrocarbons, obtain the absorbing liquid rich in sulfur-containing compounds such as hydrogen sulfide at the bottom of tower,
Then absorbing liquid being passed through sulfide desorber, heats up, desorption of reducing pressure, temperature is 100 DEG C, pressure
For 0.1MPa, tower top obtains the sulfur-containing compounds such as hydrogen sulfide, obtains [P at the bottom of tower4444][C5COO] ion
Liquid-absorbant, recycle and reuse.Hydrogen sulfide stripping rate: 98.5%, thioether removal efficiency: 93.3%,
Mercaptan removal rate: 94.5%, ethane removal efficiency: 91.5%, propane removal efficiency: 94.8%, butane takes off
Except rate 96.5%.
Embodiment 2
Absorbent forms: [N4444][C7H15COO] the pure ionic liquid absorption of TBuA caprylic acid salt
Agent.Raw natural gas composition (mol ratio): methane 81.5%, ethane 8.5%, propane 8.5%, fourth
Alkane 5.1%, hydrogen sulfide 1.0% and other components.
Such as embodiment 1, raw natural gas and absorbent 5 DEG C, counter current contacting absorbs under 2.5MPa,
Absorbing liquid desorbs light hydrocarbon component 50 DEG C of intensifications, and absorbing liquid heats up to reduce pressure through alkane desorber again and solves
Inhale, 90 DEG C, desorb hydrogen sulfide under 0.1MPa, be absorbed at the bottom of tower agent recycle and reuse.
Hydrogen sulfide stripping rate: 97.6%, ethane removal efficiency: 91.4%, propane removal efficiency: 95.2%, butane
Removal efficiency 97.7%.
Embodiment 3
Absorbent forms: [bmpyrr] [Bu2PO4] N, N-butyl methyl pyrrolidines dibutylphosphoric acid ester salt from
Sub-liquid, 1-METHYLPYRROLIDONE composite absorber, ionic liquid accounts for 95% (volume fraction).Former
Material natural gas composition (mol ratio): methane 88.2%, ethane 5.9%, propane 2.0%, butane 0.9%,
Hydrogen sulfide 1.2% and other components.
Such as embodiment 1, raw natural gas and absorbent 10 DEG C, counter current contacting absorbs under 1.8MPa,
55 DEG C of intensifications of absorbing liquid desorb light hydrocarbon component, and absorbing liquid heats up to reduce pressure through sulfide desorber again and solves
Inhale, 85 DEG C, desorb hydrogen sulfide under 0.05MPa, be absorbed at the bottom of tower agent recycle and reuse.
Hydrogen sulfide stripping rate: 97.5%, ethane removal efficiency: 92.1%, propane removal efficiency: 96.7%, butane
Removal efficiency 97.1%.
Embodiment 4
Absorbent forms: [bepyrr] [HexHPO3] N, N-butyl ethyl pyrrolidines phosphorous acid own ester ion
Liquid.Raw natural gas composition (mol ratio): methane 76.3%, ethane 11.0%, propane 6.0%,
Butane 2.9%, hydrogen sulfide 0.9%, carbon dioxide 0.4% and other components.
Such as embodiment 1, raw natural gas and absorbent 20 DEG C, counter current contacting absorbs under 2.8MPa,
Absorbing liquid 80 DEG C heats up and desorbs, and tower top obtains C2～C4Lighter hydrocarbons and partial CO 2, remain at the bottom of tower
Absorbing liquid heats up decompression desorption through sulfide desorber again, 110 DEG C, desorb sulphur under 0.12MPa
Changing hydrogen, be absorbed at the bottom of tower agent recycle and reuse.Hydrogen sulfide stripping rate: 96.7%, ethane removes
Rate: 92.4%, propane removal efficiency: 94.4%, butane removal efficiency 95.1%.
Embodiment 5
Absorbent forms: [bmmim] [BuSO4] 1-butyl-2,3-methylimidazole sulfate pentahydrate from
Sub-liquid and DMF composite absorber, ionic liquid volume fraction is 80%.Former
Material natural gas composition (mol ratio): methane 52.3%, ethane 20.3%, propane 11.6%, butane 5.6%,
Hydrogen sulfide 1.1%, carbon dioxide 0.6%, mercaptan 421mg/m3And other components.
Such as embodiment 1, raw natural gas and absorbent 10 DEG C, counter current contacting absorbs under 1.5MPa,
Absorbing liquid 55 DEG C, 0.3MPa heat up to reduce pressure and desorb, and tower top obtains C2～C4Lighter hydrocarbons and part titanium dioxide
Carbon, residual absorption liquid at the bottom of tower heats up to reduce pressure through sulfide desorber again and desorbs, at 95 DEG C, 0.08MPa
Under desorb hydrogen sulfide sulfides, be absorbed at the bottom of tower agent recycle and reuse.Hydrogen sulfide stripping rate:
98.2%, Mercaptan removal rate: 98.9%, ethane removal efficiency: 92.2%, propane removal efficiency: 93.1%,
Butane removal efficiency 94.2%.
Embodiment 6
Absorbent forms: [N666(14)][BuHPO3] three hexyl myristyl ammonium phosphorous acid butyl ester ionic liquid
Body absorbent, 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.
Such as embodiment 1, raw natural gas and absorbent 30 DEG C, counter current contacting absorbs under 0.8MPa,
Absorbing liquid 70 DEG C heats up and desorbs, and tower top obtains C2～C4Lighter hydrocarbons, residual absorption liquid at the bottom of tower is again through sulfuration
Thing desorber heats up decompression desorption, 100 DEG C, desorb hydrogen sulfide under 0.15MPa, obtain at the bottom of tower
Absorbent recycle and reuse.Hydrogen sulfide stripping rate: 97.7%, ethane removal efficiency: 92.7%, third
Alkane removal efficiency: 93.2%, butane removal efficiency 94.1%.
Comparative example 1
Absorbent forms: [bmim] [OAc] 1-butyl-3-methylimidazole acetate ionic liquid.Raw material
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.
Such as embodiment 1, raw natural gas and absorbent 15 DEG C, counter current contacting absorbs under 1.0MPa,
Absorbing liquid 65 DEG C heats up and desorbs, and tower top obtains C2～C4Lighter hydrocarbons, residual absorption liquid at the bottom of tower is again through sulfuration
Thing desorber heats up decompression desorption, 100 DEG C, desorb hydrogen sulfide under 0.1MPa, inhaled at the bottom of tower
Receive agent recycle and reuse.Hydrogen sulfide stripping rate: 90.3%, ethane removal efficiency: 75.3%, propane
Removal efficiency: 80.3%, butane removal efficiency 82.1%.
Comparative example 2
Absorbent forms: [bmpyrr] [Me2PO4] N, N-butyl methyl pyrrolidines dimethyl phosphate ion
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.
Such as embodiment 1, raw natural gas and absorbent 10 DEG C, counter current contacting absorbs under 1.9MPa,
60 DEG C of intensifications of absorbing liquid desorb light hydrocarbon component, and absorbing liquid heats up to reduce pressure through sulfide desorber again and solves
Inhale, 85 DEG C, desorb hydrogen sulfide under 0.05MPa, be absorbed at the bottom of tower agent recycle and reuse.
Hydrogen sulfide stripping rate: 92.3%, ethane removal efficiency: 80.1%, propane removal efficiency: 82.2%, butane
Removal efficiency: 84.7%.
Comparative example 3
Absorbent forms: [bmmim] [MeSO4] 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%, carbon dioxide 0.7%, mercaptan 381mg/m3, remaining is nitrogen.
Such as embodiment 1, raw natural gas and absorbent are at 10 DEG C, and under 2.0MPa, counter current contacting absorbs,
Absorbing liquid 55 DEG C, 0.1MPa heat up to reduce pressure and desorb, and tower top obtains C2～C4Lighter hydrocarbons and part titanium dioxide
Carbon, residual absorption liquid at the bottom of tower heats up to reduce pressure through sulfide desorber again and desorbs, at 95 DEG C, 0.05MPa
Under desorb hydrogen sulfide sulfides, be absorbed at the bottom of tower agent recycle and reuse.Hydrogen sulfide stripping rate:
88.6%, Mercaptan removal rate: 89.3%, carbon dioxide eliminating rate: 80.3%, ethane removal efficiency: 70.3%,
Propane removal efficiency: 73.4%, butane removal efficiency 76.1%.
Claims (7)
1. one kind utilizes the method that ionic liquid desulfurization from natural gas takes off lighter hydrocarbons, it is characterised in that
Comprise the steps:
(1) using the mixed solvent of ionic liquid or ionic liquid and molecular solvent as absorbent, with
Natural gas contacts, and absorbs sulfide, lighter hydrocarbons and carbon dioxide in natural gas, and be absorbed liquid and surplus
Remaining tail gas；
Described lighter hydrocarbons are for mainly containing C2～C4Alkane or alkene；
Described ionic liquid is by cation M+And anion N-Two parts form, anion N-For carbon
Chain alkyl sulphonic acid ester anion that long-chain fat acid anion that number is 6～22, carbon number are 4～12,
The chain alkyl phosphorous acid that chain alkyl phosphate anion that carbon number is 4～12, carbon number are 4～12
One in ester anion；Cation M+For imidazole type cation, season type cation, quaternary ammonium type
One in cation, pyrrolidines type cation；
(2) absorbing liquid that step (1) obtains is carried out two sections of desorptions, successively by lighter hydrocarbons, sulfide
Desorbing, the absorbent that desorption obtains recycles.
Method the most according to claim 1, it is characterised in that described molecular solvent is C6~
C16Hydro carbons, aromatic hydrocarbons, N,N-dimethylformamide or 1-METHYLPYRROLIDONE；
The percentage by volume of the mixed solvent Middle molecule solvent of described ionic liquid and molecular solvent is
0.1～20%.
3. according to the method described in claim 1～2 any claim, it is characterised in that described
Absorbent be ionic liquid.
Method the most according to claim 3, it is characterised in that described ionic liquid is four
Butyl n-caproic acid salt, TBuA caprylic acid salt, 1-butyl-2,3-methylimidazole sulfate pentahydrate,
N, N-butyl methyl pyrrolidines dibutylphosphoric acid ester, N, the N-butyl ethyl own ester of pyrrolidines phosphorous acid or three are own
Base myristyl ammonium phosphorous acid butyl ester.
5., according to the method described in claim 1 or 4, it is characterised in that in step (1), use
Absorbent absorbs the condition of sulfide, lighter hydrocarbons and carbon dioxide in natural gas: temperature is 5～30 DEG C,
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.
Method the most according to claim 5, it is characterised in that the concrete steps of described method
For:
(1) absorbent is cooled to 5～30 DEG C, under pressure is 0.1～3.0MPa, and is cooled to
The natural gas contact of 5～30 DEG C, absorbs sulfide, lighter hydrocarbons and the carbon dioxide in natural gas, is inhaled
Receive liquid and residual exhaust；
(2) absorbing liquid that step (1) obtains is carried out two sections of desorptions, first 35～80 DEG C,
Under 0.1～0.8MPa, lighter hydrocarbons and a part of carbon dioxide are desorbed, then 60～120 DEG C,
Under 0.01～0.2MPa, Desorption separation obtains sulfide and residual carbon dioxide, the absorbent that desorption obtains
Recycle.
Method the most according to claim 6, it is characterised in that described absorbent is with natural
The way of contact of gas is counter current contacting.
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| 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 |
| CN114835573B (en) * | 2021-02-01 | 2023-04-18 | 中国科学院化学研究所 | Method for synthesizing carboxylate compound |
| CN113101782B (en) * | 2021-04-08 | 2023-03-24 | 浙江工业大学 | Functionalized ionic liquid absorption liquid and preparation method and application thereof |
| 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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