CN101210192A - Process for preparing alkylated oil - Google Patents
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- CN101210192A CN101210192A CN 200610105399 CN200610105399A CN101210192A CN 101210192 A CN101210192 A CN 101210192A CN 200610105399 CN200610105399 CN 200610105399 CN 200610105399 A CN200610105399 A CN 200610105399A CN 101210192 A CN101210192 A CN 101210192A
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Abstract
The invention discloses an alkylate preparation method in petrochemical field, in particular to a method for preparing alkylate by using an ionic liquid as a catalyst. The method can prepare the alkylate with high octane number by selecting the ionic liquid as the catalyst and the mixture of isobutane and C4 olefin as the reactants and by intermittent or continuous operation of a tank reactor or a fiber membrane reactor at 30 to 85 DEG C, in the presence or absence of reaction auxiliary agent and under a pressure that can ensure the reactants are liquid. The catalytic activity and C8 selectivity of the invention reach or exceed the level of industrial production of alkylate, and the ionic liquid catalyst has almost no corrosion and can form a two-phase system with the alkylate, so that the alkylate product can be easily separated from the catalyst. The ionic liquid catalyst can be used for substituting for liquid strong acid, and the method is a green and clean alkylation process at scale and is suitable for large-scale industrial continuous production.
Description
Technical field
The present invention relates to the preparation method of petrochemical industry alkylate oil, particularly adopt the method for ionic liquid as the Preparation of Catalyst alkylate oil.
Background technology
In the various industrial application of alkylated reaction, with the Trimethylmethane is alkylating reagent, low-carbon alkene (mainly being butylene and propylene) is carried out alkylated reaction, and be that the isobutane alkylation of purpose is one of most important alkylation industrial application to generate the high-octane rating gasoline alkylate.Advantages such as isoparaffin and low-carbon alkene alkylation generate a kind of stop bracket gasoline, and this gasoline has that susceptibility is low, steam forces down, combustion heat value height, burning clean fully, free from environmental pollution are the desirable blend components of aviation spirit and motor spirit.Develop rapidly and human pay attention to day by day along with automotive industry to environment protection; more strict regulation has been made to vehicle fuel in countries in the world; indexs such as aromaticity content, olefin(e) centent, vapour pressure in the restriction motor spirit; the demand of unleaded stop bracket gasoline constantly increases, and the ideal composition that alkylate oil becomes reformulated gasoline is subjected to extensive concern.Nowadays, the petroleum resources shortage, refining of petroleum and processing technology are more complete, and the catalytic cracking of heavy oil becomes the main process in the refining of petroleum.Its process is a large amount of with C in producing
3～C
5Be main lower carbon number hydrocarbons, throughput is big, it is numerous to relate to enterprise.Make full use of these cheap raw materials, use alkylation techniques and convert it into market fuel gasoline in short supply, become the most valued course of processing of alkylation process technology.
Hydrofluoric acid HF and sulfuric acid H
2SO
4It is the traditional industry catalyzer of alkane and olefin alkylation.Although HF and H
2SO
4On active, selectivity and catalyst life, all shown superperformance, but HF and H in the production process
2SO
4Problems such as the environmental pollution that is caused, equipment corrosion and personal injury make the industrial application of isobutane alkylation be subjected to considerable restraint.The catalyzer that alkylation industry presses for a kind of " close friend " to be to substitute existing liquid strong acid, seeks new catalytic material, development of new technology then is the basic outlet that solves the isobutane alkylation existing issue.
In recent decades, the research work of novel alkylation catalyst never is interrupted.Solid acid, AlCl
3-ether system, heteropolyacid-acetate system and liquid superacid, all the Ceng Zuowei catalyzer is incorporated in the isobutane alkylation reaction and is studied.But all there are problems such as not high, the easy inactivation of activity, complex process in various degree, finally fail in alkylation industry, to realize using.Ionic liquid is as a class novel compounds objects system, caused people's extensive concern in the application of all many-sides such as electrochemistry, liquid-liquid separation, extraction, Industrial Catalysis, biocatalysis and polymerization.The environmental friendliness that some ion liquid systems had, strongly-acid, chemical property can adjust, easily and characteristics such as product separation, cyclic utilization rate height, make it may become the novel catalytic material of a class and substitute HF and H
2SO
4Carrying out Deng liquid strong acid catalytic alkylation reaction.
In recent years, some effects have been obtained with ionic liquid as the trial that catalyzer is applied to the preparation aspect of alkylated reaction and alkylated oil.WO98/50153 provides a kind of R
3N.HCl and AlCl
3The alkylation that original position synthetic ionic-liquid catalyst is used for benzene mainly obtains the alkylbenzene product of straight chain.US2006/0131209, US2006/0135839 provide a kind of pyridine and imidazole type and AlCl
3And Al
2Cl
7The ionic liquid-catalyzed system of forming has been described the alkylated reaction that is used for pentane and ethene and the alkylation of syncatalytic Trimethylmethane of anhydrous HCl gas and butylene.Because catalyzer has used AlCl
3With HCl gas, system poor stability, can't avoid the influence of minor amount of water to catalyzer, catalytic activity obviously descends in conditional request harshness, the working cycle, has increased the problem such as separating difficulty of oil product and can't enter practical application.US2004/01333056 discloses a kind of hydrohalogenation compound and AlCl by amine or pyridine
3And the compound ion liquid catalyst of other metallic compound composition, and catalyst series afterwards with toluene, the modification of acetone equal solvent, be applied to the alkylation of Trimethylmethane and butylene, what described catalyst levels was few surpasses 30%, surpass two times of raw material volume, but all unavoidable above-mentioned AlCl
3The defective that catalyst system brings.Described the triflate catalyst that a kind of polyacrylic acid supports in the US2005/0059848 patent and used at the alkylated reaction of Trimethylmethane iso-butylene, efficient is lower than sulfuric acid process and other ionic liquid catalyst alkylation reaction efficiency, does not relate to C
4In the reaction and the influence of other alkene.
HF and H
2SO
4Two kinds of industrial alkylation catalysts are subjected to many censures of people on the one hand and denounce, and they have still guaranteed lower process cost and the important task of producing high-quality gasoline on the other hand.Therefore, development of new alkylated oil catalysis technique should be able to substitute existing HF and H fully
2SO
4Two kinds of commercial catalystss reduce the harm to environment significantly; Under the prerequisite that keeps identical quality product of present industrial alkylation and productive rate, has identical or lower production cost; Catalyzer should have wide in range suitability and loose relatively process conditions to refinery's raw material; Technical process is applicable to the large-scale production process of refinery.
Summary of the invention
The object of the present invention is to provide a kind of preparation method of alkylate oil.
The present invention realizes by following measure:
Our invention thought is to select a kind of suitable ionic liquid as catalyzer, finds suitable reaction conditions, makes Trimethylmethane and C
4Olefine reaction generates high-octane alkylate oil.
A kind of preparation method of alkylate oil is characterized in that: this method adopts ionic liquid as catalyzer, and wherein the ionic liquid positively charged ion is selected from imidazoles or pyridine, and negatively charged ion is selected from CF
3SO
3-, CH
3COO
-, CF
3COO
-, (CF
3SO
2)
2N
-, (CF
3SO)
3C
-, F
-, Cl
-, Br
-, I
-, CH
3C
6H
6SO
3-, HSO
3-In a kind of; With Trimethylmethane and C
4The mixture of alkene is as reactant, do not use reaction promoter or use reaction promoter, guarantee that at 30～85 ℃ reactant is under the pressure condition of liquid state, adopts tank reactor or tunica fibrosa reactor, intermittence or operate continuously obtain high-octane alkylate oil.
Ion liquid positively charged ion of the present invention adopts imidazoles, and structural formula is:
Wherein R represents H, CH
3Perhaps C
2～C
16Alkyl group, they can be identical or different groups, n represents 2～4 carbon alkyl.
Ion liquid positively charged ion of the present invention adopts pyridine, and structural formula is:
R wherein
1, R
2, R
3Represent H, CH
3Perhaps C
2～C
16Alkyl group, they can be identical or different groups, n represents 2～4 carbon alkyl.
Reactant of the present invention is carbon four raw materials of oil-refining chemical industry indication: comprise Trimethylmethane, 2-butylene, 1-butylene, iso-butylene or their two or more mixtures, and the mixed C of ordinary meaning
4Raw material, the mol ratio of alkane and alkene are 1: 1～1: 20.
The present invention adopts ionic liquid as catalyzer, and consumption is 0.3～6.0wt% of reactant.
The present invention can suitably improve the selectivity of the yield and the trimethylpentane of alkylate oil by adding some auxiliary agents, described reaction promoter comprises quaternary ammonium salt, metallic compound, sulfocompound, can be selected from the mixture on two kinds of a kind of, two kinds or they in them, the addition of auxiliary agent is no more than 3000ppm.
Quaternary ammonium salt can be selected from tetrabutylammonium chloride, Tetrabutyl amonium bromide, tetrabutylammonium iodide, etamon chloride, 4 bromide, tetraethylammonium bromide, tetraethyl ammonium iodide, tri-n-octyl methyl ammonium chloride, benzyl trimethyl ammonium chloride.
Metallic compound is selected from the halogenide or the vitriol of copper, iron, zinc, nickel, lithium, potassium.
Sulfocompound is selected from dithiocarbonic anhydride, C
2～C
6Mercaptan compound.
Reaction times of the present invention was controlled at 8～60 minutes because of temperature of reaction is different with reactive mode.
Alkylate oil yield of the present invention can reach 202% of alkene feed volume, C in the alkylate oil
8Content reaches 84%, trimethylpentane: dimethylhexane (TMP: DMH) can reach more than 10: 1.
Ionic-liquid catalyst of the present invention can directly use, and also is suitable for using in solvent.Employed solvent can be single also mixed solvent, only otherwise influence directly separating of ionic-liquid catalyst and alkylate oil, comprises that water can be as the solvent use of the inventive method.
Reactor used in the present invention is the autoclave of band whipping appts, the employed continuous production device of industrial sulfuric acid or hydrofluoric acid method alkylated reaction.Two-phase system is specially adapted to the continuous production device of tunica fibrosa type of reactor, reaches high-level efficiency, high yield, saving cost.
Ionic liquid is owing to have that steam forces down, toxicity is little, Heat stability is good, do not burn and separate characteristics such as simple with blast, solubility property uniqueness, reaction product.In the research of organic chemical reactionses such as Friedel-Crafts reaction, alkylation, isomerization, dimerizing olefins, epoxidation, epoxy compounds cycloaddition, be used to replace traditional organic solvent or inorganic acid catalyst.Between forming ion liquid yin, yang ion chemistry diversity structure and designability, the design of novel ion liquid, synthetic, character and be subjected to the concern of various countries' catalysis circle and petroleum chemical enterprise circle and progressively acceptance as eco-friendly " cleaning " solvent and new catalyst system.Isoparaffin and olefin alkylation synthesis of alkyl carburetion are crucial technological processs in the petroleum refining industry among the present invention, are most important alkylation industrial application.
The environmental friendliness that ionic-liquid catalyst used in the present invention has, strongly-acid, chemical property can adjust, easily and characteristics such as product separation, cyclic utilization rate height, make it may become the novel catalytic material of a class and substitute HF and H
2SO
4Deng liquid strong acid, the carrying out of catalytic alkylation reaction.This ionic-liquid catalyst has guaranteed lower process cost and the important task of producing high-quality gasoline on the one hand, reduces the harm to environment simultaneously significantly; On the other hand, catalyzer has wide in range suitability and loose relatively process conditions to refinery's raw material, and technical process is applicable to the large-scale production process of refinery, under the prerequisite that keeps alkylate oil quality and productive rate, has lower production cost.
The present invention has the following advantages:
1) ionic-liquid catalyst thermostability height, stable to empty G﹠W, non-volatile is very low to conversion unit corrodibility.
2) catalyzer and alkylate oil form two-phase system, and oil product and catalyzer are easily separated, and catalyst recirculation is used easy and simple to handle.
3) fully improved C in the finish
8Component and isoparaffin in the content of trimethylpentane (TMP), alkylation products has higher octane value.
4) catalyst levels is little, the reactive behavior height, and the transformation efficiency of 1-butylene can reach 100%.
5) reaction times weak point, the production efficiency height, tunica fibrosa reactor production capacity is bigger.
6) reaction can be used polar solvent or the solvent-free and available water as solvent immiscible with alkylate oil, all can reach reaction effect.
7) the alkylate oil yield can reach 150～202% of alkene charging feed volume, C during alkylate oil is formed
8Add up to 70～84%, trimethylpentane: dimethylhexane (TMP: DMH) reach more than 10: 1.
8) the ratio industrial sulphuric acid of alkane and alkene and hydrofluoric acid method reduce greatly, have reduced the internal circulating load of alkane in the reaction system, and energy efficient effectively reduces running cost.
9) catalyzer is wide to the scope of application of raw material olefin, the mixed olefins that is applicable to different C 4 olefins and contains few butadiene, methyl alcohol and ethers impurity.
10) catalytic activity and C
8Selectivity has has met or exceeded the level of industrial production alkylate oil, but is the alkylation process of the green cleaning of a kind of alternative liquid strong acid mass-producing, demonstrates the wide application prospect of alkylation catalyst systems of new generation.
Embodiment
With concrete case study on implementation the present invention is further specified below, but application of the present invention not only is confined to the listed scope of embodiment.
Embodiment 1:
The toluene sulfonic acide ionic-liquid catalyst of 6.0 gram pyridine butyl sulfonic acids is added in the autoclave of band stirring, use N
2Stamping press advances Trimethylmethane and butene-1 mixing raw material 80g to 0.5MPa, and the alkane alkene ratio in the raw material is 6: 1.Start stirring, in 30min, temperature is risen to 70 ℃, use N
2Guarantee pressure 1.6MPa, reaction 0.5h.After reaction finishes, cooling, release.Pour reaction solution in separating funnel standing demix, lower floor is the catalyzer phase, and the upper strata is the alkylation oil phase.
Embodiment 2:
The trifluoromethanesulfonic acid ionic-liquid catalyst of the 2-butyl-pyridinium propyl sulfonic acid ester with 2.0% adds in the autoclave of band stirring, uses N
2Stamping press advances Trimethylmethane and butene-1 mixing raw material 80g to 0.5MPa, and the alkane alkene ratio in the raw material is 6: 1.Start stirring, in 30min, temperature is risen to 70 ℃, use N
2Guarantee pressure 1.6MPa, reaction 0.5h.After reaction finishes, cooling, release.Pour reaction solution in separating funnel standing demix, lower floor is the catalyzer phase, and the upper strata is the alkylation oil phase.
Embodiment 3:
The toluene sulfonic acide ionic-liquid catalyst of 6.0 gram 1-butyl imidazole sulfonic acid butyl esters is added in the autoclave of band stirring, use N
2Stamping press advances Trimethylmethane and butene-1 mixing raw material 80g to 0.5MPa, and the alkane alkene ratio in the raw material is 10: 1.Start stirring, in 30min, temperature is risen to 70 ℃, use N
2Guarantee pressure 1.6MPa, reaction 0.5h.After reaction finishes, cooling, release.Pour reaction solution in separating funnel standing demix, lower floor is the catalyzer phase, and the upper strata is the alkylation oil phase.
Embodiment 4:
The ionic-liquid catalyst of the hydrosulfate of the 1-hexyl imidazoles butyl sulfonic acid esters of 1.0 grams is added in the autoclave that band stirs, add the small amount of toluene solvent, be convenient to separate.Use N
2Stamping press advances Trimethylmethane and butene-1 mixing raw material 80g to 0.5MPa, and the alkane alkene ratio in the raw material is 6: 1.Start stirring, in 30min, temperature is risen to 70 ℃, use N
2Guarantee pressure 1.6MPa, reaction 0.5h.After reaction finishes, cooling, release.Pour reaction solution in separating funnel standing demix, lower floor is the catalyzer phase, and the upper strata is the alkylation oil phase.
Embodiment 5:
The tertiary butyl trifluoro azochlorosulfonate acid ion liquid of the 1.0 1-octyl group imidazoles butyl sulfonic acid esters that restrain is added in the autoclave of band stirring, add a little amount of heptane, use N
2Stamping press advances Trimethylmethane and butene-1 mixing raw material 100g to 0.5MPa, and the alkane alkene ratio in the raw material is 4: 1.Start stirring, in 30min, temperature is risen to 75 ℃, use N
2Guarantee pressure 1.6MPa, reaction 0.5h.After reaction finishes, cooling, release.Pour reaction solution in separating funnel standing demix, lower floor is the catalyzer phase, and the upper strata is the alkylation oil phase.
Embodiment 6:
The ionic-liquid catalyst of embodiment 1 is added in the autoclave of band stirring, advance the mixing raw material 100g of Trimethylmethane and C 4 olefin, the alkane alkene ratio in the raw material is 6: 1.Start stirring, temperature is risen to 60 ℃, keep reaction 0.5h.After reaction finishes, cooling, release.Pour reaction solution in separating funnel standing demix, lower floor is the catalyzer phase, and the upper strata is the alkylation oil phase.C
8Add up to 79.6%, wherein TMP accounts for 71.3%, C
9+Add up to 4.5%.
Embodiment 7:
With the amount of the ionic-liquid catalyst of adding among the embodiment 6 is 3.0 grams, and reaction is poured reaction solution in separating funnel standing demix after finishing, and lower floor is the catalyzer phase, and the upper strata is the alkylation oil phase.C
8Add up to 80.8%, wherein TMP accounts for 74.6%, C
9+Add up to 3.2%.
Embodiment 8:
With the alkane alkene ratio in the raw material among the embodiment 7 is 3.5: 1, adds auxiliary agent tetraethylammonium bromide 1000ppm, and reaction is poured reaction solution in separating funnel standing demix after finishing, and lower floor is the catalyzer phase, and the upper strata is the alkylation oil phase.C
8Add up to 85%, wherein TMP accounts for 77%, C
9+Add up to 3.5%.
Embodiment 9:
The trifluoromethanesulfonic acid ionic-liquid catalyst of the 3.0 1-butyl imidazole butyl sulfonic acids that restrain is added in the autoclave of band stirring, add a spot of water, advance the mixing raw material 100g of Trimethylmethane and C 4 olefin, the alkane alkene ratio in the raw material is 6: 1.Start stirring, temperature is risen to 70 ℃, keep reaction 0.5h.After reaction finishes, cooling, release.Pour reaction solution in separating funnel standing demix, lower floor is the catalyzer phase, and the upper strata is the alkylation oil phase.C
8Add up to 89%, wherein TMP accounts for 80.8%, C
9+Add up to 6.2%, alkylate oil yield 200%.
Embodiment 10:
The ionic-liquid catalyst of embodiment 5 is added in the autoclave of band stirring, advance the mixing raw material 100g of Trimethylmethane and C 4 olefin, the alkane alkene ratio in the raw material is 6: 1.Start stirring, temperature is risen to 60 ℃, keep reaction 0.5h.After reaction finishes, cooling, release.Pour reaction solution in separating funnel standing demix, lower floor is the catalyzer phase, and the upper strata is the alkylation oil phase.C
8Add up to 88%, wherein TMP accounts for 77%, C
9+Add up to 7.7%, alkylate oil yield 203%.
Embodiment 11:
The ionic-liquid catalyst of embodiment 2 is added in the autoclave of band stirring, and the LiCl that adds 500ppm is an auxiliary agent, the mixing raw material 100g of Trimethylmethane and C 4 olefin, and the alkane alkene ratio in the raw material is 6: 1.Start stirring, temperature is risen to 60 ℃, keep reaction 0.5h.After reaction finishes, cooling, release.Pour reaction solution in separating funnel standing demix, lower floor is the catalyzer phase, and the upper strata is the alkylation oil phase.C
8Add up to 81.5%, wherein TMP accounts for 74%, C
9+Add up to 2.5%.
Embodiment 12:
Ionic-liquid catalyst 3.0 grams with embodiment 4 add in the autoclave of band stirring, and the butyl sulfhydryl that adds 800ppm is an auxiliary agent, the mixing raw material 100g of Trimethylmethane and C 4 olefin, and the alkane alkene ratio in the raw material is 6: 1.Start stirring, temperature is risen to 60 ℃, keep reaction 20 minutes.After reaction finishes, cooling, release.Pour reaction solution in separating funnel standing demix, lower floor is the catalyzer phase, and the upper strata is the alkylation oil phase.C
8Add up to 84%, wherein TMP accounts for 76%, C
9+Add up to 3%.
Embodiment 13:
Reaction times among the embodiment 12 is shortened to 10 minutes, and temperature remains on 70 ℃, after reaction finishes, and cooling, release.Pour reaction solution in separating funnel standing demix, lower floor is the catalyzer phase, and the upper strata is the alkylation oil phase.C
8Add up to 80.5%, wherein TMP accounts for 73.2%, C
9+Add up to 3.3%.
Embodiment 14:
In embodiment 11, the iso-butylene content in the C 4 olefin mixing raw material brings up to 45%, and alkane alkene ratio remained on 3.5: 1.Start stirring, temperature is risen to 60 ℃, keep reaction 0.5h.After reaction finishes, cooling, release.Pour reaction solution in separating funnel standing demix, lower floor is the catalyzer phase, and the upper strata is the alkylation oil phase.C
8Add up to 86.2%, wherein TMP accounts for 77%, C
9+Add up to 2.4%.
Embodiment 15:
With 2.0 grams of the ionic-liquid catalyst among the embodiment 9, add in the autoclave of band stirring, add the LiCl of 500ppm and two kinds of auxiliary agents of butyl sulfhydryl of 800ppm, the mixing raw material 100g of Trimethylmethane and C 4 olefin, the alkane alkene ratio in the raw material is 3: 1.Start stirring, temperature is risen to 70 ℃, keep reaction 20 minutes.After reaction finishes, cooling, release.Pour reaction solution in separating funnel standing demix, lower floor is the catalyzer phase, and the upper strata is the alkylation oil phase.C
8Add up to 79%, wherein TMP accounts for 70%, C
9+Add up to 4.9%.
Embodiment 16:
Continuous service test on the tunica fibrosa reactor, catalyzer is embodiment 9 and embodiment 15, the ratio of Trimethylmethane and mixed c 4 olefin feedstock is 3: 1, input speed is respectively 210 Grams Per Hours and 140 Grams Per Hours, product overflows from separating tank continuously, detects the content and the product alkylation oil composition of alkene in the tail gas constantly.70 ℃ of temperature, during 20～30 minutes residence time, detect the alkene that contains trace in the tail gas, illustrate that mixed c 4 alkene transforms substantially fully, the alkylate oil composition is respectively: C
5Add up to: 2.2%, 7.1%; C
6Add up to: 5.1%, 5.2%; C
7Add up to: 4.6%, 3.8%; C
8Add up to: 83.7%, 80.8%; Trimethylpentane TMP:74.7% wherein, 73.7%; C
9+Add up to: 4.3%, 3.1%.The ratio of trimethylpentane TMP and dimethylhexane DMH reaches respectively: 8.2 and 10.4.Present embodiment proof functionalized ion liquid catalyzer is used the fiber membrane reactor and is carried out continuous alkylated reaction synthesis of alkyl carburetion, and catalyzer is stable, has easy and simple to handlely, and alkylation output ability increases substantially, and is fit to large-scale industrial production and uses.
It should be noted that at last, above-described examples of implementation only are used to illustrate technical scheme of the present invention and are unrestricted, although content of the present invention has been carried out comparatively detailed explanation with reference to embodiment, one of ordinary skill in the art is to be understood that, can make amendment or be equal to replacement technical scheme of the present invention, and not breaking away from the spirit and scope of technical solution of the present invention, it all should be encompassed in the middle of the claim scope of the present invention.
Claims (10)
1. the preparation method of an alkylate oil is characterized in that: this method adopts ionic liquid as catalyzer, and wherein the ionic liquid positively charged ion is selected from imidazoles or pyridine, and negatively charged ion is selected from CF
3SO
3-, CH
3COO
-, CF
3COO
-, (CF
3SO
2)
2N
-, (CF
3SO)
3C
-, F
-, Cl
-, Br
-, I
-, CH
3C
6H
6SO
3+, HSO
3-In a kind of; With Trimethylmethane and C
4The mixture of alkene is as reactant, do not use reaction promoter or use reaction promoter, guarantee that at 30～85 ℃ reactant is under the pressure condition of liquid state, adopts tank reactor or tunica fibrosa reactor, intermittence or operate continuously obtain high-octane alkylate oil.
2. the method for claim 1 is characterized in that the structural formula of imidazoles is:
Wherein R represents H, CH
3Perhaps C
2～C
16Alkyl group, they can be identical or different groups, n represents 2～4 carbon alkyl.
3. the method for claim 1 is characterized in that the structural formula of pyridine is:
R wherein
1, R
2, R
3Represent H, CH
3Perhaps C
2～C
16Alkyl group, they can be identical or different groups, n represents 2～4 carbon alkyl.
4. the method for claim 1 is characterized in that: with Trimethylmethane and C
4The mixture of alkene is as reactant, and the mol ratio of alkane and alkene is 1: 1～1: 20.
5. the method for claim 1, it is characterized in that: the ionic liquid consumption is 0.3～6.0wt% of reactant.
6. the method for claim 1, it is characterized in that: reaction promoter comprises quaternary ammonium salt, metallic compound, sulfocompound, can be selected from the mixture on two kinds of a kind of, two kinds or they in them, the addition of auxiliary agent is no more than 3000ppm.
7. method as claimed in claim 6, it is characterized in that: quaternary ammonium salt is selected from tetrabutylammonium chloride, Tetrabutyl amonium bromide, tetrabutylammonium iodide, etamon chloride, 4 bromide, tetraethylammonium bromide, tetraethyl ammonium iodide, tri-n-octyl methyl ammonium chloride, benzyl trimethyl ammonium chloride.
8. method as claimed in claim 6 is characterized in that: metallic compound is selected from the halogenide or the vitriol of copper, iron, zinc, nickel, lithium, potassium.
9. method as claimed in claim 6 is characterized in that: sulfocompound is selected from dithiocarbonic anhydride and C
2～C
6Mercaptan compound.
10. the method for claim 1, it is characterized in that: temperature of reaction was controlled at 8～60 minutes.
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