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Process for Olefin Polymerization

A technology for polyolefins and olefin monomers, applied in the field of reaction systems, can solve problems such as limiting maximum productivity, and achieve the effect of improving operability and continuity

Active Publication Date: 2020-07-14
SABIC GLOBAL TECH BV
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Therefore, in commercial practice, the use of cooled recycle gas as the sole means of removing the heat of polymerization from the gas fluidized bed polymerization of olefins has the disadvantage of limiting the maximum achievable productivity

Method used

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  • Process for Olefin Polymerization
  • Process for Olefin Polymerization
  • Process for Olefin Polymerization

Examples

Experimental program
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Effect test

example

[0213] The following examples show that controlling catalyst activity in the expansion section (by adding thermal runaway reducing agents) results in a more homogeneous product.

[0214] The inventors believe that the reason for obtaining a more homogeneous product is the control of the temperature in the expansion section due to the control of the catalyst activity.

[0215] The present invention relates to the cooling of the expansion section by taking part of the cooled recycle stream and adding it to the expansion section. It is expected that this will also control the temperature in the expansion section. Accordingly, the inventors believe that by withdrawing a liquid-containing stream from a portion of the cooled recycle stream, introducing said liquid-containing stream into the expansion section during at least part of the polymerization process, and causing said liquid-containing stream to Contact with at least a portion of the inner surface of the expanded section wi...

example 1

[0220] Example 1. TRRA is PEEB

[0221] The polymerization catalyst was prepared as follows:

[0222] Example 1: Preparation of procatalyst on activated butyl-Grignard support.

[0223] Preparation of Grignard reagent (step o)) - stage A

[0224] This step o) constitutes the first part of stage A of the process for preparing the procatalyst.

[0225] A stirred flask equipped with a reflux condenser and funnel was charged with magnesium powder (24.3 g). Place the flask under nitrogen. Magnesium was heated at 80°C for 1 hour, after which dibutyl ether (150ml), iodine (0.03g) and n-chlorobutane (4ml) were added sequentially. After the color of iodine disappeared, the temperature was raised to 80° C. and a mixture of n-chlorobutane (110 ml) and dibutyl ether (750 ml) was added slowly for 2.5 hours. The reaction mixture was stirred for a further 3 hours at 80°C. Stirring and heating were then discontinued and a small amount of solid material was allowed to settle for 24 h...

example 2

[0272] C-donor means: cyclohexylmethyldimethoxysilane.

[0273] N-donor means: n-Propyltrimethoxysilane

[0274] The polymerization catalyst was prepared as described in Example-1. Similar procedures and equipment used in Example-1 were used in this example for molecular weight distribution (MWD) using GPC and crystallinity using ATREF.

[0275] The effect of different TRRA / Si ratios on yield for both TA and DB is shown in Table 4 below:

[0276] Table 4. Yield versus TRRA / Si molar ratio for TA and DB at 67°C and 82°C.

[0277]

[0278]Table 4 shows the yield for TA at different molar ratios of TRRA to electron donor (TRRA / Si). The addition of TA showed almost similar degrees of inactivation at both temperatures, where when benchmarked with zero TA at 67°C, the activity drops were −43% and −67% at 67°C and 82°C, respectively . Therefore, TA is preferably used as one of the components in a mixture with another TRRA. Table 4 also shows the yield for DB at different mola...

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Abstract

The present invention relates to a process for the continuous preparation of polyolefins in a reactor from one or more alpha-olefin monomers, at least one of which is ethylene or propylene, wherein the reaction The reactor comprises a fluidized bed, an expansion section at or near the top of the reactor, a distribution plate in the lower part of the reactor and an inlet for a recycle stream below the distribution plate, wherein the process comprising - feeding a polymerization catalyst into a fluidized bed in a region above said distribution plate - feeding said one or more alpha-olefin monomers into said reactor - from said reactor Withdrawing the polyolefin - recirculating fluid from the top of the reactor to the bottom of the reactor, wherein the recirculating fluid is compressed using a compressor and then cooled using a heat exchanger to form a cooled recirculation comprising liquid stream, and wherein the cooled recycle stream is introduced into the reactor using the recycle stream inlet, wherein a portion of the cooled recycle stream is withdrawn to form a liquid-containing stream, wherein in the The liquid-containing stream is introduced into the expansion section during at least a portion of the polymerization process, and wherein the liquid-containing stream is contacted with at least a portion of the inner surface of the expansion section.

Description

technical field [0001] The present invention relates to a process for preparing polyolefins in a reactor from one or more alpha-olefin monomers, at least one of which is ethylene or propylene. The invention also relates to polyolefins obtained or obtainable by said process and a reaction system for operating said process. Background technique [0002] Processes for the homopolymerization and copolymerization of olefins such as the production of homopolypropylene or propylene-ethylene copolymers in the gas phase are well known in the art. Typically, in a fluidized bed polymerization process, solid particles are projected upwards into the expansion section by the collapse of gas bubbles rising at the surface of the fluidized bed, and most of these particles typically return to the flow under the force of gravity. bed because its velocity is dissipated in the lower gas velocity of the expansion section. Small amounts of fines or fines are elutriated from the projected particl...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C08F2/01B01J8/08C08F110/06C08F210/06C08F2/34C08F10/06C08F10/00C08F110/02C08F210/02C08F10/02
CPCB01J8/08C08F110/02C08F110/06C08F210/02C08F210/06C08F2/01C08F2/34C08F10/00C08F10/02B01J8/1818B01J8/1827B01J8/1836B01J2208/00176B01J2208/00274B01J2208/00991C08F10/06C08F210/16B01J8/1863B01J8/20B01J2208/00017B01J2219/00033
Inventor Y·巴纳特A·A·阿尔谢班O·阿尔胡麦丹
Owner SABIC GLOBAL TECH BV
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