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Method for synthesizing polyethylene

A technology of polyethylene and comonomer, applied in the field of olefin polymerization, can solve the problems of detonation, unstable performance of special materials, equipment shutdown, etc., and achieve the effect of reducing detonation

Pending Publication Date: 2022-03-18
PETROCHINA CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

However, the production process control of high-end brands by major domestic production companies is not yet very mature, especially for the active release technology of emerging high-activity catalyst systems, they still lack experience, and most of them use the traditional pulsed continuous feeding method, which is no longer suitable for new-type catalysts. The high-activity catalyst’s polymerization characteristics require that it is very easy to cause the catalyst’s activity to be released too quickly, causing implosion or local hot spots, causing the device to flake, blocking each operation unit, and causing the device to stop production; at the same time, frequent switching of grades is important for the stability of resin performance. Sexuality also has a certain impact, leading to an increase in the complaint rate of downstream users
Therefore, in the development of high-end new products in China, there are shortcomings such as short device operation period and unstable performance of special materials, resulting in frequent shutdown of devices and excessive transition materials, which greatly affects the benefits of enterprises and restricts the process of domestic new product development.

Method used

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  • Method for synthesizing polyethylene
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  • Method for synthesizing polyethylene

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0029] On the 50kg / h gas-phase fluidized bed process device, a dry powder metallocene catalyst (being a carrier type metallocene catalyst, with silica gel as a carrier, an active center metal zirconium content of 0.35wt%, and a cocatalyst of triisobutylaluminum / boron) is adopted. Acid salt, Al / Zr molar ratio is 142), active 18000gPE / gcat, catalyst initiation temperature 55 ℃, comonomer 1-hexene, its concentration 16% mol, target product is 0.910-0.914g / cm 3 VLDPE products.

[0030] The setting method of catalyst addition is as follows:

[0031] (1) Before the catalyst is injected, set the system temperature to 48°C; (2) The catalyst is transported by nitrogen flow, the catalyst feed rate is 0.8g / h, and the heating rate is 1.0°C / h; (3) When the reactor inlet temperature reaches 60°C , the reactor bed pressure difference reaches the following range: 0.2KPa-0.4KPa for the first stage, 0.4KPa-0.6KPa for the second stage, 0.8KPa-1.8KPa for the third stage, 1.0KPa-1.4KPa for the fo...

Embodiment 2

[0038] On the 50kg / h gas-phase fluidized bed process device, a dry powder metallocene catalyst (being a carrier type metallocene catalyst, with silica gel as a carrier, an active center metal zirconium content of 0.35wt%, and a cocatalyst of triisobutylaluminum, Al / Zr molar ratio is 160), activity 20000gPE / gcat, catalyst initiation temperature 50 ℃, comonomer 1-hexene, concentration 18% mol, target product is 0.890-0.912g / cm 3 VLDPE and POE mixed products.

[0039] The setting method of catalyst addition is as follows:

[0040] (1) Before the catalyst is injected, set the system temperature to 45°C; (2) The catalyst is transported by nitrogen flow, the catalyst feed rate is 0.7g / h, and the heating rate is 0.8°C / h; (3) When the reactor inlet temperature is 58°C, The pressure difference of the reactor bed reaches the range: the first stage is 0.2KPa-0.4KPa, the second stage is 0.4KPa-0.6KPa, the third stage is 0.8KPa-1.8KPa, the fourth stage is 1.0KPa-1.4KPa, and the fifth sta...

Embodiment 3

[0047] On the 50kg / h gas-phase fluidized bed process device, dry powder Z-N catalyst (Al / Ti molar ratio is 180, Mg / Ti molar ratio is 2.2, internal electron donor is diisooctyl phthalate, D50 is 34μm) , activity 8000gPE / gcat, catalyst initiation temperature 70°C, comonomer 1-butene, concentration 12% mol, target product 0.915-0.935g / cm 3 LLDPE products.

[0048] The setting method of catalyst addition is as follows:

[0049] (1) Before the catalyst is injected, set the system temperature to 65°C; (2) The catalyst is transported by nitrogen flow, the catalyst feed rate is 1.2g / h, and the heating rate is 2°C / h; (3) When the reactor inlet temperature is 60°C, The pressure difference of the reactor bed reaches the range: the first stage is 0.2KPa-0.4KPa, the second stage is 0.4KPa-0.6KPa, the third stage is 0.8KPa-1.8KPa, the fourth stage is 1.0KPa-1.4KPa, and the fifth stage is 10.2KPa-12.4KPa. The feed rate of the catalyst is set at 2.0-3.2g / h, and the heating rate is 2.5°C / h; ...

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Abstract

The invention discloses a method for synthesizing polyethylene, which comprises the following steps: (1) before a catalyst is injected, setting the temperature of a system to be 20-30% lower than the reaction temperature; (2) the catalyst is conveyed in a nitrogen flow mode, the feeding rate of the catalyst is 0.5-2.0 g / h, and the heating rate is 0.5-1.5 DEG C / h; (3) when the inlet temperature of the reactor reaches 90%-95% of the reaction temperature and the bed pressure difference of the reactor reaches 0.1 KPa to 0.6 KPa in the first section, 0.4 KPa to 0.7 KPa in the second section, 0.8 KPa to 2.0 KPa in the third section, 1.0 KPa to 1.8 KPa in the fourth section and 8.0 KPa to 12.4 KPa in the fifth section, the feeding rate of the catalyst is set to be 1.0-2.5 g / h, and the heating rate is set to be 1.0-5.0 DEG C / h; and (4) after the activity of the catalyst meets the design requirement and the polymerization system enters steady-state operation, the feeding rate of the catalyst is related to the change of the vicat softening point of a polymerization reaction product.

Description

technical field [0001] The invention belongs to the field of olefin polymerization, in particular to a method for synthesizing polyethylene, which is especially suitable for gas-phase fluidized bed reactors. Background technique [0002] Polyolefin production processes include slurry process, solution process, and gas phase process. With the advancement and development of technology, the advantages and disadvantages of each major production process are gradually emerging. Slurry method polyethylene, dispersed in a solvent to form a slurry, this production method solves the viscosity problem of the polymer solution, there is no limit to the MFR of the product, but there is a strict limit on the lower limit of the product density, generally at 0.935g / cm 3 About; the solution method is restricted by the viscosity of the solution, and has a certain limit on the lower limit of the product MFR, but there is no limit on the density; the gas phase method polymerizes ethylene in a ...

Claims

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Application Information

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IPC IPC(8): C08F210/16C08F2/00C08F2/34C08F2/01
CPCC08F210/16C08F2/00C08F2/34C08F2/01Y02P20/52
Inventor 葛腾杰吴双高宇新张明强王斯晗姜艳峰张瑞安彦杰李瑞杨国兴宋磊王世华国海峰韦德帅张德英赵兴龙郭峰张怀志马丽王玉如牛娜
Owner PETROCHINA CO LTD
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