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Method for producing low-molecular-weight high-activity polyisobutene

A technology of polyisobutylene and production methods, applied in the direction of chemical instruments and methods, hydrocarbons, hydrocarbons, etc., can solve the problems of separate catalyst complexation, high cost, and short storage time, so as to save energy consumption and save Energy, the effect of ensuring product quality

Inactive Publication Date: 2011-10-26
潍坊滨海石油化工有限公司
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The present invention provides a low-molecular-weight, high-activity polyisobutene production method aiming at the deficiencies in the existing polyisobutene preparation process that the catalyst needs to be complexed separately, the storage time is short, the product performance is affected, and the cost is high.

Method used

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Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0026]Isobutene is continuously polymerized in a 200L reactor. According to the requirement that the concentration of isobutene monomer is 30-40%, 98Kg / h of n-hexane and 53Kg / h of pure isobutene from catalytic cracking of MTBE are fed respectively, and the stirring is started. And pre-cool to -20°C, keep the pressure of the boron trifluoride gas phase buffer tank at 0.20Mpa, and at the same time feed boron trifluoride gas at a rate of 42g / h, adjust the addition of complexing agent reagent grade according to the heat release in the polymerization kettle The amount of isopropanol is 32-35g / h, and the complexation, initiation and polymerization of the catalyst are realized in the polymerization tank. It takes at least 1-2 hours to reach the steady state equilibrium reaction state. After the reaction steady state equilibrium, the isobutylene monomer is The concentration in the kettle is kept at 6-8%.

[0027] The mixed material coming out of the polymerization reactor is immediate...

Embodiment 2

[0029] Use the same equipment, raw materials and polymerization conditions as in Example 1, except that after the polymerization reaction is completed, the mixed material liquid comes out of the reactor and the terminator is added, and 0.05-0.1‰ of tetrakis [β-(3.5-di-tert-butyl Base-4-hydroxyphenyl) propionate] pentaerythritol ester antioxidant, when it is distilled under reduced pressure in a falling film evaporator, the temperature rises to 140-160 ° C, and after removing water and isobutylene oligomers, a colorless polymer is obtained. Isobutylene products. In this example, the conversion rate of isobutene is 88%, the number average molecular weight of the product polyisobutene is 1353, the molecular weight distribution is 2.0, and the α-terminal double bond content is 84%.

Embodiment 3

[0031] Use the same equipment as in Example 1, just change the kind of raw material, be 32-36% requirement according to isobutene monomer concentration, pass into cyclohexane and 66Kg / h respectively with 85Kg / h and pass into isobutene containing 80% Catalytic cracking of mixed C4 raw materials, start stirring and pre-cooling to -10°C, keep the pressure of the boron trifluoride gas phase buffer tank at 0.15Mpa, and at the same time feed boron trifluoride gas at a rate of 42g / h, according to the temperature in the polymerization tank The amount of isobutanol added is adjusted at 39-43g / h by exothermic heat, and the catalyst synthesis, initiation and polymerization balance are realized in the polymerization kettle. It takes 1-2 hours to establish a steady state equilibrium. After the balance, the isobutene monomer is in the kettle The inner concentration is kept at 6-8%. Add methanol terminator with 0.2‰ of isobutylene in the reaction system material at the outlet of the polymeri...

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Abstract

The invention discloses a method for producing low-molecular-weight high-activity polyisobutene. The method comprises the following steps of: adding an organic solvent and an isobutene-containing raw material into a reaction kettle respectively; introducing gaseous-phase boron trifluoride and a liquid-phase complexing agent into the reaction kettle respectively; performing polymerization reactionat the temperature of between -30 and 15 DEG C under the pressure of between 0.05 and 0.3MPa for 0.5 to 6 hours, wherein the concentration of the isobutene monomer in the reaction process is 5 to 10 weight percent; and after the reaction is finished, processing the obtained mixture material to obtain the low-molecular-weight high-activity polyisobutene. The method overcomes the technical disadvantage that a catalyst needs to be complexed in advance, and saves the complex process for preparing the catalyst, saves the energy consumption and reduces the cost by directly adding the boron trifluoride and the complexing agent into the reaction kettle. The end-group olefin content of the prepared polyisobutene is over 70 percent and even over 80 percent; and the conversion rate of the isobutene reaches over 85 percent.

Description

technical field [0001] The invention relates to a production method of polyisobutene, in particular to a production method of low molecular weight and high activity polyisobutene. Background technique [0002] Cationic polymerization of isobutene or C4 containing isobutene using Lewis acid catalysts is well known. [0003] In the invention patent CN1197807A, the inventor provided a method for controlling the molecular weight distribution of polyisobutylene in the liquid phase polymerization of isobutylene by using a boron trifluoride complex catalyst. The method involves an improved boron trifluoride catalytic system and a boiling liquid reactor. This method introduces electron donors above the liquid level in the reactor, which minimizes the chance of isobutene in the condenser reacting with free boron trifluoride, thereby limiting the formation of impurity polymers and achieving control of poly Isobutylene Molecular Weight Purpose. This method can effectively suppress t...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C08F110/10C08F4/14C08F2/38C08F6/00C08L23/20C08K5/13C08K5/06C07C2/32
Inventor 孙振民李茂春鲁效刚王波李晓明
Owner 潍坊滨海石油化工有限公司
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