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A method, an arrangement and use of an arrangement for olefin polymerisation

A technology of olefin polymerization and olefin, which is applied in the field of olefin polymerization, can solve problems not related to the use of improving the heat transfer rate of polymer particles, and achieve the effect of improving fluid dynamic conditions and being easy to handle

Active Publication Date: 2020-01-21
BOREALIS AG
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

However, none of the above patents relates to a method, a device and an application of the device for increasing the heat transfer rate of polymer particles to the gas medium, that is, the fluidization gas

Method used

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  • A method, an arrangement and use of an arrangement for olefin polymerisation
  • A method, an arrangement and use of an arrangement for olefin polymerisation
  • A method, an arrangement and use of an arrangement for olefin polymerisation

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0127] In a continuous polyethylene prepolymerization reactor, at a temperature of 70°C and a pressure of 65 bar, propane is used as a solvent (2300kg / h), an ethylene feed rate of 350Kg / h, 0.1KgH2 / tnC3, 40KgC4 / tnC3, Polymerized Ziegler-Natta catalyst particles with a particle size distribution of d 10 Equal to 10μm, d 50 Equal to 25μm, d 90 Equal to 40μm (that is, the span is 1.0), the average residence time is 30 minutes, and the average measured catalyst activity is 2Kg / gcat / h. Subsequently, the polymer material was transferred to a slurry loop reactor where the polymerization was carried out at a temperature of 85°C and a pressure of 63 bar, where the ratio of hydrogen to ethylene (expressed as mol / kmol) was 300 ( H2 / C2=300), the ratio of 1-butene to ethylene (expressed as mol / kmol) is 600 (C4 / C2=600), the solid concentration in the slurry phase loop reactor is 37% by weight, and the average residence time For 60 minutes, the average measured catalyst activity is 18Kg / gcat / h...

Embodiment 2

[0131] Example 1 was repeated, except for the operating conditions in the traditional bubbled fluidized gas phase reactor (GPR). Therefore, the polymerization was carried out at a temperature of 85°C and a total pressure of 19 bar. An ethylene partial pressure of 4.5 bar was used and 1-butene was added (copolymerization conditions). The ratio of hydrogen to ethylene (expressed as mol / kmol) is 8 (H2 / C2=8), and the ratio of 1-butene to ethylene (expressed as mol / kmol) is 650 (C4 / C2=650). The polymer particles were polymerized in GPR, the average residence time was 2 hours, and the average measured catalyst activity was 18Kg / gcat / h. Measure the d of the polymer particles prepared in the gas phase reactor 90 Equal to 2350μm. During the dynamic operation of the reactor, part of the temperature measurement value increased by 15°C beyond the temperature set value (ie 85°C), facing serious operation problems and detecting a large number of agglomerates.

[0132] Table 2. Aggregate hea...

Embodiment 3

[0134] Example 3 (invention):

[0135] Example 2 is repeated, except that: after the flashing step, the polymer particles are fed into a gas phase reactor, which has a conical bottom and top area and no distribution plate, its inner diameter is 3.6m, and it is round The height of the cylindrical part is 16m. The apparent gas velocity is equal to 0.7m / s, the polymer particles are polymerized, the average residence time is 1.5 hours, and the average measured catalyst activity is 18Kg / gcat / h. Measure the d of the polymer particles produced in the gas phase reactor 90 It is 1850μm. During the dynamic operation of the reactor, no temperature measurement value in the reactor rises above the temperature set value (ie 85°C) by more than 6°C. No operational problems were observed and no large agglomerates were detected.

[0136] Table 3. Aggregate health status summary

[0137]

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Abstract

An olefin polymerisation method and arrangement comprising polymerising at least one olefin in gas phase in a fluidised bed in the presence of an olefin polymerisation catalyst in a polymerisation reactor having a vertical body; a generally conical downwards tapering bottom zone; a generally cylindrical middle zone, above and connected to said bottom zone; and a generally conical upwards taperingtop zone above and connected to said middle zone wherein (i) fluidisation gas is introduced to the bottom zone of the reactor from where it passes upwards through the reactor; (ii) the fluidisation gas is withdrawn from the top zone of the reactor; (iii) a fluidised bed is formed within the reactor where the growing polymer particles are suspended in the upwards rising gas stream; and wherein thepolymerisation reactor has an operating temperature set point and which reactor comprises at least one temperature measurement sensor, wherein a temperature difference (DT) between the temperature measurement sensor (Tm), and the operating temperature set point (Ts) of the reactor is equal to or less than 10 DEG C.

Description

Technical field [0001] The invention relates to a method, a device for olefin polymerization, and the use of the device. Background technique [0002] Traditional fluidized bed reactors, namely bubbling gas phase olefin polymerization reactors, are known in the art. The reactor is usually operated at a moderate superficial gas velocity value, especially for polyethylene production, to ensure sufficient gas-solid mixing efficiency and to suppress solid residue / entrainment. The apparent gas velocity value used is generally 0.35-0.5m / s for polyethylene, and 0.40-0.70m / s for polypropylene. However, depending on the grade of the polymer to be produced, many operational problems related to fluidization quality, solid segregation, and fluidized bed uniformity may be encountered. In addition, it may be particularly necessary to process large-sized agglomerates in traditional gas phase reactors. One of the biggest challenges in traditional gas phase olefin polymerization reactors is th...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C08F2/01B01J8/08C08F2/34C08F10/00
CPCB01J8/24B01J2208/0053C08F2410/06C08F210/16C08F2/34C08F2/001C08F2/002C08F2/01C08F210/08C08F2500/24C08F210/14B01J8/1809B01J8/1827B01J8/1845C08F10/02
Inventor A.克拉利斯V.卡内洛波洛斯
Owner BOREALIS AG
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