CN1353123A - Process for preparing low-molecular polyisobutylene - Google Patents
Process for preparing low-molecular polyisobutylene Download PDFInfo
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- CN1353123A CN1353123A CN 00130282 CN00130282A CN1353123A CN 1353123 A CN1353123 A CN 1353123A CN 00130282 CN00130282 CN 00130282 CN 00130282 A CN00130282 A CN 00130282A CN 1353123 A CN1353123 A CN 1353123A
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Abstract
A process for preparing polybutylene having low molecular weight features that under the existance of AlCl3-arene-acid anhydride catalyst system and in liquid-phase state, the isobutylene or the raw C4 material containing isobutylene takes part in polymerizing reaction at -20-40 deg.C for 10-50 min. The resultant polybutylene has 300-5000 of number average molecular weight, more than 90% of transform rate, and low reducing rate (less than 15%) of the butylene-1 in tail gas.
Description
The present invention relates to carbon four raw materials that utilize iso-butylene or contain iso-butylene, in the presence of liquid phase state and aluminum chloride-aromatic hydrocarbons-anhydride system catalyzer, and the method for the polyisobutene of preparation number-average molecular weight 300～5000.
Utilize lewis acid catalyst, the cationoid polymerisation technology of carrying out iso-butylene or containing carbon four raw materials of iso-butylene as aluminum chloride is well-known.The catalyzer that this technology adopts generally is aluminum halide and metal alkyl halides, have what also adopt is that HCI is as catalyzer.As pointing out among the CN1014693, utilize the catalyzer of aluminum chloride, aromatic hydrocarbons and the 3rd component complexing preparation to can be used for containing the polymerization of carbon four raw materials of iso-butylene, produce polyisobutene.But this catalyzer mainly is the production that is used for carrying out the middle molecule polyisobutene of molecular weight 10000～100000, and such product colour is deep yellow, is unsuitable for producing additive products such as ashless dispersant.In US-A-4558170, point out,, form organic chloride,, can produce the polyisobutene of molecular weight 600～7000 again with aluminum alkyl catalyst catalysis simultaneously if in hydrocarbon feed gases, inject HCI.But this process has individual shortcoming, needs to introduce gasiform HCl exactly, and this will bring great corrosion to conversion unit owing to its strongly-acid.
The invention provides that a kind of security is good, catalytic efficiency is high the aluminum chloride System Catalyst, can cause carbon four polymerizable raw materials that contain iso-butylene, simultaneously can not bring very big corrosive catalyst system again, and synthesize the method for number-average molecular weight at 300～5000 low-molecular-weight polyisobutylene to equipment.
The present invention adopts following technical scheme to realize:
The present invention also adopts following technical scheme:
Carbon four raw materials can come autocatalysis or thermo-cracking, also can be from divinyl raffinate or pure iso-butylene.
Wherein iso-butylene content needs greater than 10%, and butadiene content is less than 1500ppm.
Catalyzer of the present invention:
Adopt AlCl
3Be host, the solution of selecting for use aromatic hydrocarbons and the 3rd component to form is made complexing agent, the preparation complex solution.Wherein aromatic hydrocarbons can use benzene,toluene,xylene, trimethylbenzene, or the mixture of above-mentioned aromatic hydrocarbons, or contains the petroleum fractions of aromatic hydrocarbons; And the 3rd component can be acid, acid anhydrides etc., as formic acid, acetate, oxalic acid, acetic anhydride, phthalic anhydride, maleic anhydride etc.
The acid of catalyzer raw material (or acid anhydrides)/rubbing of aluminum chloride and than being 0.1～0.5, aromatic hydrocarbons/with the mol ratio of aluminum chloride be 1～5.
The catalyzer that polymerization is used can be preserved more than 30 days; The number-average molecular weight of the polyisobutene of polymerization gained is 300～5000; Isobutene conversion reaches more than 90% in carbon four raw materials; Carbon four polymerizable raw material tail gas butene-1 rates of descent are lower than 15%.
The ratio of each raw material of catalyzer and its polymerization effect have very big relation, and the 3rd component can not be given full play to catalytic effect very little, and the 3rd component is too many, can make troubles to polymerization and aftertreatment again, therefore a proper proportion will be arranged.
The mol ratio of preparation catalyzer raw material is generally: the ratio of acid (or acid anhydrides)/aluminum chloride is preferably between 0.05 to 1.0, most preferably between 0.1 to 0.5 between 0.02 to 1.5.And the mol ratio of aromatic hydrocarbons and aluminum chloride is between 0.5 to 10, is advisable between being preferably 1 to 5.Under this proportioning, aromatic hydrocarbons and aluminum chloride are pre-mixed, then slowly add acid or acid anhydrides again, control adding speed makes temperature fluctuation range in 15 ℃.The catalyst preparation temperature at 15 ℃ to 80C, preferably at 30 ℃ to 50 ℃.The catalyzer of this process preparation can be used for containing the polymerization of carbon four raw materials of iso-butylene.
Polymerizable raw material:
At AlCl
3The catalyzer that forms with aromatic hydrocarbons and acid anhydrides causes down, iso-butylene or contain carbon four hydro carbons of iso-butylene can be in traditional reactor, as tank reactor, tubular reactor carry out intermittently, semicontinuous or successive polymerization process.Reaction heat is removed by refrigerating unit.
The retention time of polyreaction can be from 5 minutes to 3 hours, preferably from 10～50 minutes, and most preferably 15～30 minutes.
The amount of the catalyzer of introducing be in the raw material iso-butylene content 0.05～1%, preferred 0.2%～0.6%.
Polymerization temperature is regulated according to the desired molecule amount, and general molecular weight is-20 ℃～40 ℃ in 500～5000 polymerization temperature scope, preferred-5 ℃～20 ℃, most preferably is 5 ℃～15 ℃.Polymerization pressure generally carries out under barometric point, and in polymerization process, reaction process can produce certain pressure, but this pressure is usually to not influence of reaction effect.
Form under certain situation at raw material, polymerization is preferably carried out under the condition that waits heat, raw material isobutylene monomer concentration need be greater than 10%, can come the raw material of catalytic cracking, also can be from the divinyl raffinate, perhaps their mixture, preferred isobutylene concentration be greater than 30%, most preferably pure isobutene polymerisation.
After reaching polymerization time, stop with terminator.Terminator be can make catalyst deactivation medium, polymerization is stopped.Have for reaching the operable material of this purpose: water, alcohol, the liquid solution of amine or metal is as hydroxy solution of basic metal and alkaline earth metal or the like.
After termination finishes, need wash several times, generally wash with water or alcohol is washed to remove remaining catalyzer.After washing finishes, distill by normal pressure and pressure reducing mode, to remove unreacted iso-butylene, solvent, oligopolymer etc.
By process of the present invention, it is transparent to prepare colourless or little Huang, and number-average molecular weight is at 500～5000 low-molecular-weight polyisobutylene, this process selectivity height, and the transformation efficiency height, molecular weight ranges is adjustable.
The present invention is further elaborated with the following examples.
The molecular weight of the polyisobutene of the polymerization gained of introducing in example is measured by V.P.O. (vapour pressure osmometry).
Example 1: in container, pack into the toluene of 25ml and the dimethylbenzene of 10ml; be pre-mixed under 20 ℃ of conditions, the acetic anhydride of Dropwise 5 ml carries out complexing in container then, stirs fast in the complexing process always; continuously with the N2 protection, rate of addition is no more than 15 ℃ with ascending temperature and is advisable simultaneously.After all dripping end, continue to stir 1 hour.
The divinyl raffinate can be used as polymer raw, and its isobutylene concentration is 37%, with raw material drying, makes wherein water-content less than 50ppm with molecular sieve.This raw material is joined in traditional tank reactor that has heat exchanger, be cooled to 5 ℃ in advance, polymerization temperature remains on 14 ℃.To wherein dripping the catalyzer of preparation in advance, general one ton of raw material adds 10 liters catalyzer then.Retention time control 20～30 minutes.
After reaction was finished, the NaOH solution with 10% stopped in the polymerization outlet, makes catalyst deactivation, and added alkali lye destruction remainder catalyst in addition, formed thick polymers.Thick polymers water is cleaned so that remove remainder catalyst phase and unnecessary base resistates.At last, thick polymers is distilled so that remove oligopolymer and solvent etc.The product isobutene conversion that obtains.The butene-1 rate of descent sees Table 1 in molecular weight, molecular weight distribution, the polymerization.
Example 2: preparation catalyzer condition and polymerizing condition are identical with above-mentioned example 1, and the aromatic hydrocarbons that only is to use is ethylbenzene.This catalyzer carries out the polymerization of divinyl raffinate, and the butene-1 rate of descent sees Table 1 in the product isobutene conversion that obtains, molecular weight, molecular weight distribution, the polymerization.
Example 3: preparation catalyzer condition is identical with above-mentioned example 1, be polymer raw be catalyzed carbon four raw materials, iso-butylene content is 18.9%, butadiene content 1400ppm, polymerization temperature are 5 ℃, other condition is identical with example 1.The butene-1 rate of descent sees Table 1 in the product isobutene conversion that obtains, molecular weight, molecular weight distribution, the polymerization.
Example 2: preparation catalyzer condition and polymerizing condition are identical with above-mentioned example 1, and the aromatic hydrocarbons that only is to use is ethylbenzene.This catalyzer carries out the polymerization of divinyl raffinate, and the butene-1 rate of descent sees Table 1 in the product isobutene conversion that obtains, molecular weight, molecular weight distribution, the polymerization.
Example 3: preparation catalyzer condition is identical with above-mentioned example 1, be polymer raw be catalyzed carbon four raw materials, iso-butylene content is 18.9%, butadiene content 1400ppm, polymerization temperature are 5 ℃, other condition is identical with example 1.The butene-1 rate of descent sees Table 1 in the product isobutene conversion that obtains, molecular weight, molecular weight distribution, the polymerization.
Example 4: other is identical with example 3, and just catalyzer is 35 days a catalyzer of room temperature preservation.The butene-1 rate of descent sees Table 1 in the product isobutene conversion that obtains, molecular weight, molecular weight distribution, the polymerization.
Example 5: except that polymerization temperature is 9 ℃, preparation catalyzer condition and other polymerizing condition are identical with above-mentioned example 1, and the butene-1 rate of descent sees Table 1 in the product isobutene conversion that obtains, molecular weight, molecular weight distribution, the polymerization.
Comparative example:
According to CN1014693 preparation catalyzer, polymer raw is catalyzed carbon four raw materials, and iso-butylene content is 18.9%, butadiene content 1400ppm, polymerization temperature is 8 ℃, and the butene-1 rate of descent sees Table 1 in the product isobutene conversion that obtains, molecular weight, molecular weight distribution, the polymerization.Table 1
| Embodiment | Isobutene conversion % | Number-average molecular weight | Molecular weight distribution | Butene-1 rate of descent in the polymerization | Color |
| ????1 | ????92 | ????919 | ????2.1 | ????9 | Colourless |
| ????2 | ????94 | ????1100 | ????2.03 | ????7 | Colourless |
| ????3 | ????96 | ????1020 | ????2.37 | ????8 | Colourless |
| ????4 | ????93 | ????986 | ????2.46 | ????10 | Little Huang |
| ????5 | ????91 | ????2150 | ????2.27 | ????12 | Colourless |
| Comparative example | ????82 | ????775 | ????3.83 | ????22 | Yellow |
Claims (5)
1. the preparation method of a low-molecular-weight polyisobutylene, it is characterized in that: utilize carbon four hydrocarbon feeds that contain iso-butylene, in the presence of aluminum chloride, aromatic hydrocarbons and the 3rd component complex catalyst system, carry out polyreaction, the amount of the catalyzer of introducing be in the raw material iso-butylene content 0.05～1%, temperature of reaction-20～40 ℃, the retention time of polyreaction 10～50 minutes.The number-average molecular weight of polyisobutene is 300～5000; Isobutene conversion reaches more than 90% in carbon four raw materials; Carbon four polymerizable raw material tail gas butene-1 rates of descent are lower than 15%.
2. the preparation method of a kind of low-molecular-weight polyisobutylene according to claim 1, it is characterized in that: carbon four raw materials can come autocatalysis or thermo-cracking, also can be from divinyl raffinate or pure iso-butylene.Wherein iso-butylene content needs greater than 10%, and butadiene content is less than 1500ppm.
3. according to the preparation method of the described a kind of low-molecular-weight polyisobutylene of claim 1, it is characterized in that: used aluminum chloride, aromatic hydrocarbons and the 3rd component complex catalyst adopt following method preparation, aluminum chloride mixes earlier with aromatic hydrocarbons, aromatic hydrocarbons can use the mixture of benzene,toluene,xylene, ethylbenzene or above-mentioned aromatic hydrocarbons, or contains the petroleum fractions of aromatic hydrocarbons; Add the 3rd acid of component complexing agent or acid anhydrides then, acid or acid anhydrides can be formic acid, acetate, oxalic acid, acetic anhydride, dried, the maleic anhydride of benzene.
4. according to the preparation method of claim 1,3 described a kind of low-molecular-weight polyisobutylenes, it is characterized in that: the acid of catalyzer raw material (or acid anhydrides)/rubbing of aluminum chloride and than being 0.1～0.5, aromatic hydrocarbons/with the mol ratio of aluminum chloride be 1～5.
5. according to the preparation method of the described a kind of low-molecular-weight polyisobutylene of claim 1, it is characterized in that: the catalyzer that polymerization is used can be in room temperature preservation time more than 30 days.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101921352A (en) * | 2010-09-28 | 2010-12-22 | 潍坊滨海石油化工有限公司 | Method for producing low-molecular-weight high-activity polyisobutene |
| CN105149005A (en) * | 2015-10-08 | 2015-12-16 | 山东鸿瑞新材料科技有限公司 | Aluminum trichloride catalyst system and method for producing low-molecular-weight polyisobutene with same |
| CN105439789A (en) * | 2015-10-27 | 2016-03-30 | 天门市德远化工科技有限公司 | HMT continuous synthesis apparatus and method |
| CN112079959A (en) * | 2019-06-12 | 2020-12-15 | 中国石化扬子石油化工有限公司 | Aluminum trichloride complex catalyst, preparation method and application |
| CN115181200A (en) * | 2022-07-06 | 2022-10-14 | 中国石油天然气股份有限公司 | Preparation method of C4-C8 alpha-monoolefin-maleic anhydride copolymer |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100430353C (en) * | 2006-12-26 | 2008-11-05 | 南京石油化工股份有限公司 | Method of separating butane-1 from C4 fraction |
-
2000
- 2000-11-03 CN CNB001302825A patent/CN1170858C/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101921352A (en) * | 2010-09-28 | 2010-12-22 | 潍坊滨海石油化工有限公司 | Method for producing low-molecular-weight high-activity polyisobutene |
| CN101921352B (en) * | 2010-09-28 | 2011-10-26 | 潍坊滨海石油化工有限公司 | Method for producing low-molecular-weight high-activity polyisobutene |
| CN105149005A (en) * | 2015-10-08 | 2015-12-16 | 山东鸿瑞新材料科技有限公司 | Aluminum trichloride catalyst system and method for producing low-molecular-weight polyisobutene with same |
| CN105439789A (en) * | 2015-10-27 | 2016-03-30 | 天门市德远化工科技有限公司 | HMT continuous synthesis apparatus and method |
| CN105439789B (en) * | 2015-10-27 | 2019-04-19 | 天门市德远化工科技有限公司 | A kind of 1,1,3,4,4,6- vegolysen, 2,3,4- tetrahydronaphthalene are continuously synthesizing to device and method |
| CN112079959A (en) * | 2019-06-12 | 2020-12-15 | 中国石化扬子石油化工有限公司 | Aluminum trichloride complex catalyst, preparation method and application |
| CN115181200A (en) * | 2022-07-06 | 2022-10-14 | 中国石油天然气股份有限公司 | Preparation method of C4-C8 alpha-monoolefin-maleic anhydride copolymer |
| CN115181200B (en) * | 2022-07-06 | 2023-11-07 | 中国石油天然气股份有限公司 | Preparation method of C4-C8 alpha-mono-olefin-maleic anhydride copolymer |
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| CN1170858C (en) | 2004-10-13 |
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