CN114524893B - Ethylene polymer and process for producing the same - Google Patents

Ethylene polymer and process for producing the same Download PDF

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Publication number
CN114524893B
CN114524893B CN202210092295.4A CN202210092295A CN114524893B CN 114524893 B CN114524893 B CN 114524893B CN 202210092295 A CN202210092295 A CN 202210092295A CN 114524893 B CN114524893 B CN 114524893B
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ethylene
polymerization
ethylene polymer
polyethylene
comonomer
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CN114524893A (en
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李传峰
汪文睿
景昆
陈明华
杨柳
邢跃军
郭峰
游忠林
翟建宏
陈韶辉
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China Petroleum and Chemical Corp
Sinopec Yangzi Petrochemical Co Ltd
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China Petroleum and Chemical Corp
Sinopec Yangzi Petrochemical Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F10/02—Ethene
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F110/00—Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F110/02—Ethene
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F210/00—Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F210/02—Ethene
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Abstract

The invention relates to an ethylene polymer and a preparation method thereof, wherein the average grain diameter of the ethylene polymer is 50-3000 mu m, and the bulk density is 0.28-0.55g/cm 3 The true density is 0.930-0.980g/cm 3 Melt index at 190 deg.c of 2.16Kg of 0.01-2500g/10min, crystallinity of 30-90%, melting point of 105-147 deg.c, molar insertion rate of comonomer of 0.01-5mol%, weight average molecular weight of 2-40 g/mol and molecular weight distribution of 1.8-10. In the preparation method, an alkane solvent with a boiling point of 5-55 ℃ or a mixed alkane solvent with a saturated vapor pressure of 20-150KPa at 20 ℃ is used as a polymerization solvent, and the molar ratio of hydrogen to ethylene is 0.01-20 in the presence of a polyethylene catalytic system: 1. preferably 0.015-10:1, the molar ratio of hydrogen to comonomer is 8-30:1, preferably 10-25:1, subjecting a feedstock comprising ethylene, hydrogen and comonomer to tank slurry polymerization under conditions to produce an ethylene polymer.

Description

Ethylene polymer and process for producing the same
Technical Field
The present invention relates to a high density ethylene polymer and a slurry polymerization process for preparing the ethylene polymer. Specifically, the invention relates to a high-density ethylene copolymer, and a preparation method thereof, wherein an alkane solvent with a boiling point of 5-55 ℃ or a mixed alkane solvent with a saturated vapor pressure of 20-150KPa at 20 ℃ is used as a polymerization solvent, and raw materials comprising ethylene, hydrogen and comonomer are subjected to kettle-type slurry polymerization under the condition of ethylene slurry polymerization in the presence of a polyethylene catalyst system, so as to obtain the ethylene copolymer.
Background
The production method of polyethylene mainly includes high-pressure polymerization, gas-phase polymerization, slurry polymerization, solution polymerization and other processes and methods. Among them, the ethylene slurry polymerization method is one of the main methods for producing polyethylene. The method is divided into a loop reactor polymerization process and a stirred tank slurry polymerization process.
Ethylene homopolymerization in the absence of comonomer can result in medium and high density polyethylenes, such as ultra high molecular weight polyethylenes, polyethylene waxes, and the like. Ethylene is copolymerized with a comonomer in the presence of a comonomer such as propylene, 1-butene, 1-hexene, 1-octene, a medium-density and high-density polyethylene (ethylene copolymer) excellent in toughness can be obtained, and as the insertion rate of the comonomer unit in the copolymer increases, the density of the ethylene copolymer gradually decreases, and in the case where the molar insertion rate of the comonomer unit is the same, the longer the chain length of the comonomer carbon becomes, the more significant the density of the ethylene copolymer decreases.
The results of the prior studies have shown that in general, under comparable conditions, such as the same catalytic system, similar polymerization, etc., the longer the chain segment of the comonomer, the more excellent the properties of the ethylene copolymer product, such as the ethylene and 1-octene copolymer having properties superior to those of ethylene and 1-hexene copolymer, ethylene and 1-hexene copolymer having properties superior to those of ethylene and 1-butene copolymer, ethylene and 1-butene copolymer having properties superior to those of ethylene and propylene copolymer.
However, in the existing ethylene stirred tank type slurry polymerization process or polymerization method, such as the triple well chemical ethylene slurry polymerization CX process and the Herst process of Basel company, hexane is used as a polymerization solvent, in this case, when 1-hexene is used as a comonomer, separation is difficult due to the close boiling points (the difference of less than 2 ℃) between hexane and 1-hexene, so that the hexane-used ethylene stirred tank type slurry polymerization process or polymerization method is not suitable for using 1-hexene as a polymerization comonomer, which greatly limits the development of the stirred tank type slurry polymerization process and high performance products using 1-hexene as a comonomer.
On the other hand, when a solvent with a boiling point higher than that of hexane is used in ethylene slurry polymerization, such as n-heptane, isoheptane or isomer solvents thereof, the energy consumption for vaporization and condensation is high due to the high polymerization boiling point, and the method is not suitable for the heat removal mode of gas-phase circulation condensation on the existing industrial production device, and the content of the polymer powder solvent after filtration or centrifugal separation is high, so that the polymerization production and post-treatment drying cost is high.
In addition, the existing ethylene slurry polymerization process has lower polymerization pressure, lower ethylene partial pressure caused by the existence of hydrogen and comonomer partial pressure, and in addition, when producing high melt index and low density ethylene polymer, the polyethylene main catalyst has low activity, larger catalyst consumption and high production cost.
Accordingly, in the prior art, there is still a great room for improvement in a process for producing a high-density ethylene polymer (ethylene copolymer) by a tank-type ethylene slurry polymerization method, and a high-density ethylene polymer produced thereby.
Disclosure of Invention
Based on the prior art, the inventor creatively discovers that the prior polyethylene catalytic system can be applied under the ethylene slurry polymerization condition by adopting an alkane solvent with the boiling point of 5-55 ℃ or a mixed alkane solvent with the saturated vapor pressure of 20-150KPa at 20 ℃ as a polymerization solvent through a great deal of experiments, analysis and intensive researches, and further can apply propylene, 1-butene, 1-hexene, 1-octene and the like which are common in the prior industrial production and application as comonomers, thereby better solving the problems existing in the prior art, and the invention is completed.
Further, in the invention, the ethylene slurry polymerization method which adopts the low boiling point alkane solvent or the high saturated vapor pressure mixed alkane solvent as the polymerization solvent and controls the proportion of certain hydrogen and comonomer has large adjustable space of ethylene polymer performance and flexible production mode, and the high-density ethylene copolymer with excellent performance can be prepared without strict polymerization kettle configuration and polymerization reaction condition.
Specifically, the present invention provides a high-density ethylene polymer having an average particle diameter of 50 to 3000 μm, preferably 100 to 1000 μm, a weight average molecular weight of 2 to 40 g/mol, preferably 5 to 30 g/mol, a molecular weight distribution of 1.8 to 10, preferably 2.0 to 8.0, a comonomer molar insertion ratio of 0.01 to 5mol%, preferably 0.05 to 2.5mol%, preferably a melt index of 0.01 to 2500g/10min, preferably 0.1 to 2000g/10min, more preferably 0.1 to 1000g/10min, a bulk density of 0.28 to 0.55g/cm at 190℃under a load of 2.16Kg 3 Preferably 0.32-0.50g/cm 3 The true density is 0.930-0.980g/cm 3 Preferably 0.940-0.970g/cm 3 More preferably 0.942-0.970g/cm 3 The crystallinity is 30-90%, preferably 40-80%, the melting point is 105-147 ℃, preferably 110-143 ℃, and the processing index in the blown film test is 4.0-6.0, preferably 4.5-5.9, more preferably 5.0-5.8.
The invention also provides a preparation method of the ethylene polymer, wherein an alkane solvent with a boiling point of 5-55 ℃ or a mixed alkane solvent with a saturated vapor pressure of 20-150KPa at 20 ℃ is used as a polymerization solvent, and the molar ratio of hydrogen to ethylene is 0.01-20 in the presence of a polyethylene catalytic system: 1. preferably 0.015-10:1, the molar ratio of hydrogen to comonomer is 8-30:1, preferably 10-25:1, more preferably 12-23:1, subjecting a feedstock comprising ethylene, hydrogen and comonomer to a tank slurry polymerization under conditions, the polyethylene catalyst system comprising a polyethylene main catalyst other than a metallocene catalyst.
Technical effects
The invention provides a high-density ethylene polymer (ethylene copolymer), which has high bulk density, high true density, wide and adjustable and controllable range of melt index, crystallinity, melting point, comonomer molar insertion rate, weight average molecular weight and the like, moderate and adjustable and controllable molecular weight distribution and good subsequent processability, and is very suitable for production and application of a kettle type ethylene slurry polymerization process.
In the method for producing an ethylene polymer according to the present invention, an alkane solvent having a boiling point of 5 to 55 ℃ or a mixed alkane solvent having a saturated vapor pressure of 20 to 150KPa at 20 ℃ is used as a polymerization solvent, and a raw material comprising ethylene, hydrogen and a comonomer is subjected to slurry polymerization to obtain an ethylene polymer (polyethylene, ethylene copolymer). The separation of the solvent and comonomer, such as propylene, 1-butene, 1-hexene, 1-octene, etc. is easier in the separation stage after the polymerization of the polymer mass obtained, whereby the present polymerization process allows to obtain high density ethylene polymers (ethylene copolymers) of different properties more efficiently. Further, the oligomer produced in the polymerization reaction remains in the resulting ethylene polymer due to the use of a specific polymerization solvent, so that the subsequent processability of the resulting ethylene polymer is excellent.
By adopting the ethylene slurry polymerization method, the ethylene polymer powder obtained after the polymerization is very easy to dry, the solvent residual content in the wet polymer is less than 20wt% after the direct filtration after the polymerization is finished, and the solvent residual content is lower than that of the wet polymer which is higher than 25wt% when the prior hexane is used as the polymerization solvent, thereby being very beneficial to shortening the drying time of the polyethylene material and saving the post-treatment cost of the polyethylene and further being beneficial to the subsequent industrial application of the ethylene polymer.
In the method of the present invention, by setting the ratio of hydrogen to ethylene to a specific range, the ratio of hydrogen to comonomer to a specific range, an oligomer having an appropriate content is produced while the ethylene and comonomer are polymerized. Further, the oligomer produced by the polymerization reaction remains in the ethylene polymer due to the use of a specific polymerization solvent, so that the processability of the resulting ethylene polymer is excellent.
In the polymerization method of the present invention, only an alkane solvent having a boiling point of 5 to 55 ℃ or a mixed alkane solvent having a saturated vapor pressure of 20 to 150KPa at 20 ℃ is used as the polymerization solvent, and no other solvents such as a dispersant and a diluent are required, so that the reaction system is single, and the post-treatment is simple and easy.
Detailed Description
The following detailed description of embodiments of the invention is provided, but it should be noted that the scope of the invention is not limited by these embodiments, but is defined by the appended claims.
In the context of this specification, any matters or matters not mentioned are directly applicable to those known in the art without modification except as explicitly stated. Moreover, any embodiment described herein can be freely combined with one or more other embodiments described herein, and the technical solutions or ideas thus formed are all deemed to be part of the original disclosure or original description of the present invention, and should not be deemed to be a new matter which has not been disclosed or contemplated herein, unless such combination is clearly unreasonable by those skilled in the art.
In the context of the present invention, unless otherwise specifically defined or the meaning is beyond the understanding of the skilled artisan, hydrocarbon or hydrocarbon derivative groups of 3 carbon atoms or more (such as propyl, propoxy, butyl, butane, butene, butenyl, hexane, etc.) have the same meaning as when the prefix "positive" is uncrowded. For example, propyl is generally understood to be n-propyl, while butyl is generally understood to be n-butyl.
In the context of the present invention, physical property values of a substance (such as boiling point) are measured at normal temperature (25 ℃) and normal pressure (101325 Pa), unless specified otherwise.
In the present invention, the ethylene polymer is a copolymer of ethylene and other comonomers, sometimes referred to simply as polyethylene.
As a result of intensive studies, the inventors of the present invention have found that, in the polymerization method of the present invention, by using an alkane solvent having a boiling point of 5 to 55℃or a mixed alkane solvent having a saturated vapor pressure of 20 to 150KPa at 20℃as a polymerization solvent, the specific polymerization solvent of the present invention and ethylene and a copolymerized olefin (e.g., propylene, 1-butene, 1-hexene, 1-octene) as reactants have a significant difference in boiling point from the conventional polymerization solvents, and that the post-treatment of the resulting ethylene polymer can be carried out conveniently and efficiently, and that the resulting ethylene polymer powder has a low solvent residue content, which is advantageous in shortening the drying time of the ethylene polymer powder and saving the post-treatment cost of the ethylene polymer powder.
By adopting the slurry polymerization method of the ethylene polymer, the ethylene polymer powder obtained after the polymerization is very easy to dry, the solvent residual content in the wet polymer is less than 20 weight percent after the direct filtration after the polymerization reaction is finished, and the solvent residual content is lower than that of the wet polymer which takes the prior hexane as the polymerization solvent and is higher than 25 weight percent, thereby being very beneficial to shortening the drying time of the polyethylene material, saving the post-treatment cost of the polyethylene and further being beneficial to the subsequent industrial application of the ethylene polymer. In addition, due to the use of a specific polymerization solvent, the oligomer produced along with the polymerization reaction remains in the ethylene polymer, so that the processability of the resulting ethylene polymer is excellent.
In addition, by adopting the slurry polymerization method of the ethylene polymer, under the similar ethylene slurry homopolymerization condition except that no comonomer participates in the polymerization reaction, the copolymerization process of ethylene and the comonomer shows more remarkable polymerization activity effect than the ethylene homopolymerization process, namely, the copolymerization activity is higher than the homopolymerization activity, thereby improving the molar insertion rate of the comonomer.
Therefore, the invention can provide an ethylene polymer which has high bulk density and true density, wide and adjustable and controllable ranges of melt index, crystallinity, melting point, weight average molecular weight and the like, has moderate and adjustable and controllable molecular weight distribution, and is very suitable for preparing the ethylene polymer in a customized way. And the resulting ethylene polymer has excellent processability.
The present inventors have surprisingly found that in an ethylene slurry polymerization process, by using an alkane solvent having a boiling point of 5 to 55 ℃ or a mixed alkane solvent having a saturated vapor pressure of 20 to 150KPa at 20 ℃ as a polymerization solvent, and making the ratio of hydrogen and ethylene be in a specific range and the ratio of hydrogen and comonomer be in a specific range, the resulting ethylene polymer exhibits excellent processability when used for subsequent processing.
Without being bound by any theory, the inventors speculate that, although the copolymerization reaction between ethylene and comonomer is the main reaction in the polymerization method of the present invention, by making the ratio of hydrogen and ethylene in a specific range and the ratio of hydrogen and comonomer in a specific range, a specific copolymerized oligomer can be produced concomitantly in the polymerization reaction, and the solubility of the oligomer in the specific polymerization solvent of the present invention is very low, which allows the oligomer in the resulting ethylene polymer to remain, and the oligomer with a moderate residual content is advantageous for improving the processability of the product, reducing the processing cost, and improving the processing shaping efficiency when the ethylene polymer is used in the subsequent processing of the ethylene polymer (such as extrusion of pipes and profiles, film blowing, casting, blow molding, rotational molding, coating, wire drawing, pressing of plates and profiles).
More specifically, the present invention provides a high-density ethylene polymer having an average particle diameter of 50 to 3000. Mu.m, preferably 100 to 1000. Mu.m. The high density ethylene polymer of the present invention has a weight average molecular weight of from 2 to 40 g/mol, preferably from 5 to 30 g/mol. The high density ethylene polymers of the present invention have a molecular weight distribution of from 1.8 to 10, preferably from 2.0 to 8.0. The comonomer molar insertion of the high density ethylene polymer of the present invention is 0.05 to 5mol%, preferably 0.1 to 2.5mol%. The processing index in the blown film test of the high-density ethylene polymer of the present invention is 4.0 to 6.0, preferably 4.5 to 5.9, and more preferably 5.0 to 5.8.
In one embodiment of the invention, the ethylene polymer has a melt index of 0.01 to 2500g/10min, preferably 0.1 to 2000g/10min, more preferably 0.1 to 1000g/10min at 190℃under a load of 2.16 Kg. The bulk density of the high density ethylene polymers of the present invention is from 0.28 to 0.55g/cm 3 Preferably 0.32-0.50g/cm 3 . The high density ethylene polymers of the present invention have a true density of from 0.930 to 0.980g/cm 3 Preferably 0.940-0.970g/cm 3 More preferably 0.942-0.970g/cm 3 . The crystallinity of the high density ethylene polymers of the present invention is from 30 to 90%, preferably from 40 to 80%. The high density ethylene polymers of the present invention have a melting point of 105 to 147℃and preferably 110 to 143 ℃.
The invention also provides a preparation method of the ethylene polymer, wherein an alkane solvent with a boiling point of 5-55 ℃ or a mixed alkane solvent with a saturated vapor pressure of 20-150KPa at 20 ℃ is used as a polymerization solvent, and the molar ratio of hydrogen to ethylene is 0.01-20 in the presence of a polyethylene catalytic system: 1. preferably 0.015-10:1, the molar ratio of hydrogen to comonomer is 8-30:1, preferably 10-25:1, more preferably 12-23:1, subjecting a feed comprising ethylene and comonomer to tank slurry polymerization,
the polyethylene catalyst system comprises a polyethylene main catalyst other than a metallocene catalyst.
In one embodiment of the present invention, in the method for producing an ethylene polymer, the ratio of the polyethylene main catalyst to the polymerization solvent is 0.001 to 0.500mmol of the polyethylene main catalyst/L of the polymerization solvent, preferably 0.005 to 0.200mmol of the polyethylene main catalyst/L of the polymerization solvent, more preferably 0.005 to 0.05mmol of the polyethylene main catalyst/L of the polymerization solvent.
In the process for the preparation of ethylene polymers according to the invention, the polymerization temperature is from 30 to 110℃and preferably from 50 to 100 ℃; the polymerization pressure is 0.2 to 4.0MPa, preferably 1.0 to 3.8MPa; in the molar ratio of hydrogen to ethylene of 0.01-20: 1. preferably 0.015-10:1, the molar ratio of hydrogen to comonomer is 8-30:1, preferably 10-25:1, and the slurry concentration is 50-500 g polymer/L polymerization solvent, preferably 100-400 g polymer/L polymerization solvent, and ethylene kettle type slurry polymerization is carried out in batch or continuous mode to obtain ethylene polymer.
In the preparation method of the ethylene polymer, the solvent content of the powder material after the slurry subjected to polymerization reaction is subjected to flash evaporation, filtration or centrifugal separation is less than 20 weight percent.
The method for producing the ethylene polymer of the present invention will be specifically described below.
Specifically, the polymerization solvent is described below.
According to the present invention, examples of the alkane solvent having a boiling point of 5 to 55℃include 2, 2-dimethylpropane (also known as neopentane, having a saturated vapor pressure of 146.63KPa at 20℃and a saturated vapor pressure of 76.7KPa at 20℃and a saturated vapor pressure of 27.83℃and a saturated vapor pressure of 56.5KPa at 20℃and a saturated vapor pressure of cyclopentane (having a boiling point of 49.26℃and a saturated vapor pressure of 34.6KPa at 20 ℃) and a normal pentane (having a boiling point of 25 to 50 ℃) and a saturated vapor pressure of cyclopentane (having a boiling point of 49.26 ℃) are given.
As the mixed alkane with the saturated vapor pressure of 20-150KPa at 20 ℃, the mixed alkane with the saturated vapor pressure of 40-110KPa at 20 ℃ is preferable, and the mixed alkane is a mixed solvent formed by mixing different alkane solvents according to proportion, such as a mixed solvent formed by hexane and an isomer solvent thereof, pentane and an isomer solvent thereof, and can also come from a mixture of alkanes which are cut and extracted according to a distillation range by a solvent rectifying device. Preferably a mixed solvent of pentane and its isomer solvents. Specifically, a combination of n-pentane and isopentane, a combination of isopentane and neopentane, a combination of n-pentane and cyclopentane, a combination of n-pentane and neopentane, a combination of isopentane and cyclopentane, a combination of neopentane and cyclopentane, a combination of n-hexane and n-pentane, a combination of n-pentane-isopentane-cyclopentane, a combination of n-pentane-n-hexane-isopentane, and the like can be cited. But is not limited thereto. So long as the alkane mixture is saturated with a vapor pressure of 20 to 150KPa (preferably 40 to 110 KPa) at 20 ℃.
In one embodiment of the present invention, as the mixed alkane having a saturated vapor pressure of 20 to 150KPa (preferably 40 to 110 KPa) at 20 ℃, a mixed alkane having a saturated vapor pressure of 20 to 150KPa (preferably 40 to 110 KPa) at 20 ℃ which is a mixture of two or more alkanes selected from the group consisting of n-pentane, isopentane, neopentane and cyclopentane, more preferably a combination of n-pentane and isopentane, a combination of isopentane and neopentane, a combination of n-pentane and cyclopentane, a combination of isopentane and cyclopentane, a combination of neopentane and cyclopentane, a combination of n-pentane-isopentane-cyclopentane, a combination of neopentane-isopentane-n-pentane, and the like are preferable. For the ratio of the individual alkanes in the mixed alkane, for example, the molar ratio of the two alkane solvents when mixed may be 0.01 to 100:1, preferably 0.1 to 10:1, when the three alkane solvents are mixed, the molar ratio of the alkane solvents can be 0.01 to 100:0.01-100:1, preferably 0.1 to 10:0.1-10:1, provided that the resulting mixed alkane solvent has a saturated vapor pressure of 20 to 150KPa (preferably 40 to 110 KPa) at 20 ℃. In one embodiment of the present invention, only an alkane solvent having a boiling point of 5 to 55℃or a mixed alkane solvent having a saturated vapor pressure of 20 to 150KPa at 20℃is used as the polymerization solvent.
The description of the polyethylene catalyst system is as follows.
In the present invention, the polyethylene catalyst system comprises a polyethylene main catalyst other than a metallocene catalyst.
In one embodiment of the present invention, the polyethylene catalyst system of the present invention may be a catalyst system comprising a polyethylene procatalyst and a cocatalyst.
As the main catalyst for polyethylene, a non-metallocene catalyst commonly used in the art for catalyzing the polymerization of ethylene, or a complex of a non-metallocene catalyst with a metallocene catalyst and/or a Ziegler-Natta catalyst may be used. Specifically, supported Ziegler-Natta and non-metallocene composite catalysts, supported dual or multiple non-metallocene catalysts, supported metallocene and non-metallocene composite catalysts, and the like can be cited.
Specifically, as the polyethylene main catalyst, a supported non-metallocene catalyst may be selected, for example, the invention patent CN200310106156.X, CN, CN200510119401.X, CN 2009101970985. X, CN CN, CN201010285969.X, CN 20110259258. X, CN 20110259258. X CN, CN201010285969.X, CN-CN, CN, CN CN, CN 20110259219. X, CN 20110259258. X.
According to the present invention, the term "non-metallocene complex" is a single-site olefin polymerization catalyst with respect to a metallocene catalyst, which does not contain cyclopentadienyl groups such as a metallocene ring, fluorene ring or indene ring or derivatives thereof in the structure, and which is capable of exhibiting olefin polymerization catalytic activity when combined with a cocatalyst such as those described below (thus the non-metallocene complex is sometimes also referred to as a non-metallocene olefin polymerizable complex). The compound comprises a central metal atom and at least one multidentate ligand (preferably a tridentate ligand or more) bound to the central metal atom in a coordination bond, and the term "non-metallocene ligand" is the aforementioned multidentate ligand.
According to the invention, the non-metallocene complex is selected from compounds having the following chemical formula:
。
according to the chemical formula, the ligands forming a coordination bond with the central metal atom M include n groups X and M multidentate ligands (structural formulas in brackets). Depending on the chemical structure of the polydentate ligand, groups A, D and E (coordinating groups) form a coordination bond with the central metal atom M through the coordinating atoms (e.g., N, O, S, se and P heteroatoms) contained in these groups.
According to the invention, the total number of negative charges carried by all ligands (including the group X and the multidentate ligand) is the same absolute value as the positive charge carried by the central metal atom M.
In a more specific embodiment, the non-metallocene complex is selected from the group consisting of compounds (a) and (B) having the following chemical structural formula.
And->
（A） （B）。
In a more specific embodiment, the non-metallocene complex is selected from the group consisting of compounds (A-1) to (A-4) and compounds (B-1) to (B-4) having the following chemical structural formula.
、 />、
（A－1） （A－2）
、 />、
（A－3） （A－4）
、/>、
（B－1） （B－2）
And->
（B－3） （B－4）。
In all of the above chemical structural formulas,
q is 0 or 1;
d is 0 or 1;
m is 1, 2 or 3;
m is a central metal atom selected from the group consisting of metal atoms of groups III to XI of the periodic Table of elements, preferably a metal atom of group IVB, for example, ti (IV), zr (IV), hf (IV), cr (III), fe (III), ni (II), pd (II) or Co (II);
n is 1, 2, 3 or 4, depending on the valence of the central metal atom M;
x is selected from halogen, hydrogen atom, C 1 －C 30 Hydrocarbyl, substituted C 1 －C 30 A hydrocarbon group, an oxygen-containing group, a nitrogen-containing group, a sulfur-containing group, a boron-containing group, an aluminum-containing group, a phosphorus-containing group, a silicon-containing group, a germanium-containing group, or a tin-containing group, and a plurality of X's may be the same or different, or may be bonded or looped to each other;
A is selected from oxygen atom, sulfur atom, selenium atom,、-NR 23 R 24 、-N(O）R 25 R 26 、/>、-PR 28 R 29 、-P(O）R 30 OR 31 Of sulfone, sulfoxide or-Se (O) R 39 Wherein N, O, S, se and P are each an atom for coordination;
b is selected from nitrogen atom, nitrogen-containing group, phosphorus-containing group or C 1 －C 30 A hydrocarbon group;
d is selected from nitrogen atom, oxygen atom, sulfur atom, selenium atom, phosphorus atom, nitrogen-containing group, phosphorus-containing group, C 1 －C 30 A hydrocarbyl, sulfone, or sulfoxide group, wherein N, O, S, se and P are each a coordinating atom;
e is selected from a nitrogen-containing group, an oxygen-containing group, a sulfur-containing group, a selenium-containing group, a phosphorus-containing group, or a cyano group (-CN), wherein N, O, S, se and P are each a coordinating atom;
f is selected from nitrogen atom, nitrogen-containing group, oxygen atom, sulfur atom, selenium atom, phosphorus atom or phosphorus-containing group, wherein N, O, S, se and P are each an atom for coordination;
g is selected from C 1 －C 30 Hydrocarbyl, substituted C 1 －C 30 Hydrocarbon or inert functional groups;
y is selected from an oxygen atom, a nitrogen-containing group, an oxygen-containing group, a sulfur-containing group, a selenium-containing group, or a phosphorus-containing group, wherein N, O, S, se and P are each an atom for coordination;
z is selected from nitrogen-containing groups, oxygen-containing groups, sulfur-containing groups, selenium-containing groups, phosphorus-containing groups or cyano groups (-CN), for example, -NR 23 R 24 、-N(O）R 25 R 26 、-PR 28 R 29 、-P(O）R 30 R 31 、-OR 34 、-SR 35 、-S(O）R 36 、-SeR 38 or-Se (O) R 39 Wherein N, O, S, se and P are each an atom for coordination;
Represents a single bond or a double bond;
-represents a covalent bond or an ionic bond;
representing a coordinate bond, a covalent bond or an ionic bond.
R 1 To R 4 、R 6 To R 21 Each independently selected from hydrogen, C 1 －C 30 Hydrocarbyl, substituted C 1 －C 30 Hydrocarbyl (of which halogenated hydrocarbyl groups such as-CH are preferred 2 Cl and-CH 2 CH 2 Cl) or inert functional groups. R is R 22 To R 36 、R 38 And R is 39 Each independently selected from hydrogen, C 1 －C 30 Hydrocarbyl or substituted C 1 －C 30 Hydrocarbon groups (of which halogenated hydrocarbon groups are preferred, ratioSuch as-CH 2 Cl and-CH 2 CH 2 Cl). The above groups may be the same or different from each other, wherein adjacent groups such as R 1 And R is R 2 ，R 6 And R is R 7 ，R 7 And R is R 8 ，R 8 And R is R 9 ，R 13 And R is R 14 ，R 14 And R is R 15 ，R 15 And R is R 16 ，R 18 And R is R 19 ，R 19 And R is R 20 ，R 20 And R is R 21 ，R 23 And R is R 24 Or R 25 And R is R 26 Etc. may be bonded to each other to form a bond or a ring, preferably an aromatic ring, such as an unsubstituted benzene ring or a ring having 1 to 4C 1 －C 30 Hydrocarbyl or substituted C 1 －C 30 Hydrocarbyl (of which halogenated hydrocarbyl groups such as-CH are preferred 2 Cl and-CH 2 CH 2 Cl) substituted benzene ring, and
R 5 selected from lone pair electrons on nitrogen, hydrogen, C 1 －C 30 Hydrocarbyl, substituted C 1 －C 30 Hydrocarbon groups, oxygen-containing groups, sulfur-containing groups, nitrogen-containing groups, selenium-containing groups, or phosphorus-containing groups. When R is 5 R in the case of an oxygen-containing group, a sulfur-containing group, a nitrogen-containing group, a selenium-containing group or a phosphorus-containing group 5 The N, O, S, P and Se of (a) may be used as the coordinating atom (coordinating with the central metal atom M).
In the context of the present invention, the R 22 To R 36 、R 38 And R is 39 Each independently selected from hydrogen, C 1 -C 30 Hydrocarbyl or substituted C 1 -C 30 Hydrocarbyl groups, which may be the same or different from each other, wherein adjacent groups may be bonded to each other to form a bond or a ring, preferably an aromatic ring.
In the context of the present invention, examples of inert functional groups include groups selected from the group consisting of halogen, oxygen-containing groups, nitrogen-containing groups, silicon-containing groups, germanium-containing groups, sulfur-containing groups, tin-containing groups, C 1 －C 10 Ester or nitro (-NO) 2 ) At least one of (C) and the like, but generally does not include C 1 －C 30 Hydrocarbyl radicalsSubstituted C 1 －C 30 A hydrocarbon group.
In the context of the present invention, the inert functional group has the following characteristics, limited by the chemical structure of the multidentate ligand of the present invention:
(1) Does not interfere with the coordination process of the group A, D, E, F, Y or Z with the central metal atom M, and
(2) The ability to coordinate to the central metal atom M is lower than the A, D, E, F, Y and Z groups and does not displace the existing coordination of these groups to the central metal atom M.
In accordance with the invention, in all of the formulae described above, any adjacent two or more groups, such as R, as the case may be 21 With a group Z, or R 13 With a group Y, which may be bound to each other to form a ring, preferably C comprising heteroatoms from said group Z or Y 6 －C 30 Aromatic heterocyclic ring such as pyridine ring and the like, wherein the aromatic heterocyclic ring is optionally substituted with 1 or more groups selected from C 1 －C 30 Hydrocarbyl and substituted C 1 －C 30 The substituent of the hydrocarbon group is substituted.
In the context of the present invention, the halogen is selected from F, cl, br or I. The nitrogen-containing group is selected from、-NR 23 R 24 、-T-NR 23 R 24 or-N (O) R 25 R 26 . The phosphorus-containing group is selected from->、-PR 28 R 29 、-P(O）R 30 R 31 or-P (O) R 32 (OR 33 ). The oxygen-containing group is selected from the group consisting of hydroxy, -OR 34 and-T-OR 34 . The sulfur-containing group is selected from the group consisting of-SR 35 、-T-SR 35 、-S(O）R 36 or-T-SO 2 R 37 . The selenium-containing group is selected from the group consisting of-Ser 38 、-T-SeR 38 、-Se(O）R 39 or-T-Se (O) R 39 . The radicals T being selected from C 1 －C 30 Hydrocarbyl or substituted C 1 －C 30 A hydrocarbon group. The R is 37 Selected from hydrogen, C 1 －C 30 Hydrocarbyl or substituted C 1 －C 30 A hydrocarbon group.
In the context of the present invention, the C 1 －C 30 The hydrocarbon radical being selected from C 1 －C 30 Alkyl (preferably C 1 －C 6 Alkyl, such as isobutyl), C 7 －C 50 Alkylaryl groups (such as tolyl, xylyl, diisobutylphenyl, and the like), C 7 －C 50 Aralkyl (e.g. benzyl), C 3 －C 30 Cyclic alkyl, C 2 －C 30 Alkenyl, C 2 －C 30 Alkynyl, C 6 －C 30 Aryl (e.g., phenyl, naphthyl, anthracenyl, etc.), C 8 －C 30 Condensed ring groups or C 4 －C 30 A heterocyclic group, wherein the heterocyclic group contains 1 to 3 hetero atoms selected from nitrogen atoms, oxygen atoms, or sulfur atoms, such as pyridyl, pyrrolyl, furyl, thienyl, or the like.
According to the invention, in the context of the present invention, the said C, depending on the specific case of the relevant group to which it is bound 1 －C 30 Hydrocarbyl is sometimes referred to as C 1 －C 30 Hydrocarbadiyl (divalent radicals, otherwise known as C 1 －C 30 Hydrocarbylene) or C 1 －C 30 Hydrocarbon tri (trivalent groups), as will be apparent to those skilled in the art.
In the context of the present invention, the substituted C 1 －C 30 Hydrocarbyl refers to C bearing one or more inert substituents 1 －C 30 A hydrocarbon group. By inert substituents is meant that these substituents are substituted for the aforementioned coordinating groups (meaning the aforementioned groups A, D, E, F, Y and Z, or optionally also including the group R 5 ) No substantial interference with the coordination process of the central metal atom M; in other words, these substituents are not capable or have no chance (e.g., affected by steric hindrance, etc.) to be bound by the chemical structure of the multidentate ligands of the present inventionThe central metal atom M undergoes a coordination reaction to form a coordination bond. In general, the inert substituents are selected, for example, from halogen or C 1 －C 30 Alkyl (preferably C 1 －C 6 Alkyl groups such as isobutyl).
In the context of the present invention, the boron-containing group is selected from BF 4 - 、(C 6 F 5 ） 4 B - Or (R) 40 BAr 3 ） - The method comprises the steps of carrying out a first treatment on the surface of the The aluminum-containing group is selected from aluminum alkyls, alPh 4 - 、AlF 4 - 、AlCl 4 - 、AlBr 4 - 、AlI 4 - Or R is 41 AlAr 3 - The method comprises the steps of carrying out a first treatment on the surface of the The silicon-containing group is selected from-SiR 42 R 43 R 44 or-T-SiR 45 The method comprises the steps of carrying out a first treatment on the surface of the The germanium-containing group is selected from-GeR 46 R 47 R 48 or-T-GeR 49 The method comprises the steps of carrying out a first treatment on the surface of the The tin-containing group is selected from-SnR 50 R 51 R 52 、-T-SnR 53 or-T-Sn (O) R 54 Wherein Ar represents C 6 －C 30 Aryl groups. R is R 40 To R 54 Each independently selected from hydrogen, C as described above 1 －C 30 Hydrocarbyl or substituted C as previously described 1 －C 30 Hydrocarbyl groups, which may be the same or different from each other, wherein adjacent groups may be bonded to each other to form a bond or a ring. Wherein the radicals T are as defined above.
Examples of the non-metallocene complex include the following compounds:
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and->。
The non-metallocene complex is preferably selected from the following compounds:
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The non-metallocene complex is further preferably selected from the following compounds:
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More preferably, the non-metallocene complex is selected from the following compounds:
and->。
These non-metallocene complexes may be used singly or in combination of plural kinds in any ratio.
According to the present invention, the polydentate ligand in the non-metallocene complex is not a diether compound commonly used in the art as an electron donor compound.
The non-metallocene complex or the polydentate ligand may be manufactured according to any method known to those skilled in the art. For details of the manufacturing method, see, for example, WO03/010207 and Chinese patents ZL01126323.7 and ZL02110844.7, etc., the entire contents of which are incorporated herein by reference.
Among them, supported non-metallocene catalysts are preferred, and supported one-component non-metallocene catalysts are more preferred.
The active metal in the polyethylene main catalyst can be active metal commonly used in the field, for example, can be selected from IVB group, such as titanium, zirconium or hafnium element; group VB, such as vanadium, group VIII, such as iron, cobalt, nickel, palladium, etc., preferably group IVB metal, most preferably titanium metal.
The polyethylene procatalysts, including but not limited to non-metallocene catalysts, are typically admixed with an active metal which may be a commonly used active metal in the art, and may be selected from group IVB, such as titanium, zirconium or hafnium; group VB, such as vanadium, group VIIB, such as chromium; group VIII elements such as iron, cobalt, nickel, palladium, etc., preferably group IVB metal elements, most preferably titanium metal elements.
According to the present invention, the polyethylene main catalyst may be a supported catalyst, and the support may be selected from a porous silica gel support, a layered porous support, an organic polymer support, a magnesium compound support, an oxide support, and the like.
The magnesium compound carrier may be selected from magnesium compounds such as magnesium halides, alkoxymagnesium, alkylmagnesium halides and alkylalkoxymagnesium.
Specifically, examples of magnesium halide include magnesium chloride (MgCl) 2 ) Magnesium bromide (MgBr) 2 ) Magnesium iodide (MgI) 2 ) And magnesium fluoride (MgF) 2 ) Among them, magnesium chloride is preferable.
Examples of the alkoxymagnesium halide include methoxymagnesium chloride (Mg (OCH) 3 ) Cl), ethoxymagnesium chloride (Mg (OC) 2 H 5 ) Cl), magnesium chloride propoxy (Mg (OC) 3 H 7 ) Cl), magnesium n-butoxide (Mg (OC) 4 H 9 ) Cl), magnesium isobutoxy chloride (Mg (i-OC) 4 H 9 ) Cl), methoxy magnesium bromide (Mg (OCH) 3 ) Br), ethoxymagnesium bromide (Mg (OC) 2 H 5 ) Br), magnesium propoxybromide (Mg (OC) 3 H 7 ) Br), n-butoxymagnesium bromide (Mg (OC) 4 H 9 ) Br), magnesium isobutoxy bromide (Mg (i-OC) 4 H 9 ) Br), magnesium methoxyiodide (Mg (OCH) 3 ) I), magnesium ethoxyiodide (Mg (OC) 2 H 5 ) I), magnesium propoxyiodide (Mg (OC) 3 H 7 ) I), magnesium n-butoxide iodide (Mg (OC) 4 H 9 ) I) and magnesium isobutoxy iodide (Mg (I-OC) 4 H 9 ) I), etc., of which methoxy magnesium chloride, ethoxy magnesium chloride and isobutoxy magnesium chloride are preferred.
Examples of the magnesium alkoxide include magnesium methoxide (Mg (OCH) 3 ) 2 ) Magnesium ethoxide (Mg (OC) 2 H 5 ) 2 ) Magnesium propoxy (Mg (OC) 3 H 7 ) 2 ) Magnesium butoxide (Mg (OC) 4 H 9 ) 2 ) Magnesium isobutoxide (Mg (i-OC) 4 H 9 ) 2 ) And 2-ethylhexyloxy magnesium (Mg (OCH) 2 CH(C 2 H 5 )C 4 H 8 ) 2 ) And the like, of which ethoxymagnesium and isobutoxymagnesium are preferable.
Examples of the alkyl magnesium include methyl magnesium (Mg (CH) 3 ) 2 ) Ethyl magnesium (Mg (C) 2 H 5 ) 2 ) Propyl magnesium (Mg (C) 3 H 7 ) 2 ) N-butylmagnesium (Mg (C) 4 H 9 ) 2 ) And isobutyl magnesium (Mg (i-C) 4 H 9 ) 2 ) And the like, of which ethyl magnesium and n-butyl magnesium are preferable.
Examples of the alkyl magnesium halide include methyl magnesium chloride (Mg (CH) 3 ) Cl), ethyl magnesium chloride (Mg (C) 2 H 5 ) Cl), propyl magnesium chloride (Mg (C) 3 H 7 ) Cl), n-butyl magnesium chloride (Mg (C) 4 H 9 ) Cl), isobutyl magnesium chloride (Mg (i-C) 4 H 9 ) Cl), methyl magnesium bromide (Mg (CH) 3 ) Br), ethyl magnesium bromide (Mg (C) 2 H 5 ) Br), propyl magnesium bromide (Mg (C) 3 H 7 ) Br), n-butylmagnesium bromide (Mg (C) 4 H 9 ) Br), isobutyl magnesium bromide (Mg (i-C) 4 H 9 ) Br), methyl magnesium iodide (Mg (CH) 3 ) I), ethyl magnesium iodide (Mg (C) 2 H 5 ) I), propyl magnesium iodide (Mg (C) 3 H 7 ) I), n-butyl magnesium iodide (Mg (C) 4 H 9 ) I) and magnesium isobutyl iodide (Mg (I-C) 4 H 9 ) I), etc., among which methyl magnesium chloride, ethyl magnesium chloride and isobutyl magnesium chloride are preferred.
Examples of the alkylalkoxymagnesium include methylmagnesium (Mg (OCH) 3 )(CH 3 ) Magnesium methylethoxy (Mg (OC) 2 H 5 )(CH 3 ) Magnesium methylpropionate (Mg (OC) 3 H 7 )(CH 3 ) Methyl n-butoxymagnesium (Mg (OC) 4 H 9 )(CH 3 ) Magnesium methyl isobutoxide (Mg (i-OC) 4 H 9 )(CH 3 ) Ethyl methoxymagnesium (Mg (OCH) 3 )(C 2 H 5 ) Magnesium ethyl ethoxide (Mg (OC) 2 H 5 )(C 2 H 5 ) Magnesium ethylpropoxide (Mg (OC) 3 H 7 )(C 2 H 5 ) Magnesium ethyl n-butoxide (Mg (OC) 4 H 9 )(C 2 H 5 ) Magnesium ethyl isobutoxide (Mg (i-OC) 4 H 9 )(C 2 H 5 ) Propyl methoxy magnesium (Mg (OCH) 3 )(C 3 H 7 ) Magnesium propyl ethoxy (Mg (OC) 2 H 5 )(C 3 H 7 ) Magnesium propylpropoxide (Mg (OC) 3 H 7 )(C 3 H 7 ) Propyl magnesium n-butoxide (Mg (OC) 4 H 9 )(C 3 H 7 ) Magnesium propyl isobutoxide (Mg (i-OC) 4 H 9 )(C 3 H 7 ) N-butyl methoxy magnesium (Mg (OCH) 3 )(C 4 H 9 ) N-butyl ethoxymagnesium (Mg (OC) 2 H 5 )(C 4 H 9 ) N-butyl-propoxy magnesium (Mg (OC) 3 H 7 )(C 4 H 9 ) N-butyl n-butoxymagnesium (Mg (OC) 4 H 9 )(C 4 H 9 ) N-butyl magnesium isobutoxide (Mg (i-OC) 4 H 9 )(C 4 H 9 ) Isobutyl methoxymagnesium (Mg (OCH) 3 )(i-C 4 H 9 ) Isobutyl ethoxymagnesium (Mg (OC) 2 H 5 )(i-C 4 H 9 ) Magnesium isopropoxide (Mg (OC) 3 H 7 )(i-C 4 H 9 ) Isobutyl n-butoxymagnesium (Mg (OC) 4 H 9 )(i-C 4 H 9 ) And isobutylmagnesium isobutoxide (Mg (i-OC) 4 H 9 )(i-C 4 H 9 ) Butyl ethoxy magnesium is preferred among others.
These magnesium compounds may be used singly or in combination of two or more.
Examples of the porous carrier include organic or inorganic porous solids conventionally used as carriers in the art for producing supported olefin polymerization catalysts.
Specifically, examples of the organic porous solid include olefin homo-or copolymer, polyvinyl alcohol or its copolymer, cyclodextrin, (co) polyester, (co) polyamide, vinyl chloride homo-or copolymer, acrylate homo-or copolymer, methacrylate homo-or copolymer, and styrene homo-or copolymer, and partially crosslinked forms of these homo-or copolymers, and among these, a partially crosslinked (for example, a degree of crosslinking of at least 2% but less than 100%) styrene polymer is preferable.
According to the present invention, when an organic porous solid is used as the carrier, the organic porous solid may also be subjected to a heat activation treatment before use. The heat-activation treatment may be carried out in a usual manner, such as heat-treating the organic porous solid under reduced pressure or an inert atmosphere. The inert atmosphere as used herein means that the gas contains only very small amounts or no components that can react with the organic porous solid. Examples of the inert atmosphere include a nitrogen gas atmosphere and a rare gas atmosphere, and a nitrogen gas atmosphere is preferable. Since the organic porous solid is poor in heat resistance, the heat activation process is premised on not damaging the structure and basic composition of the organic porous solid itself. Typically, the temperature of the thermal activation is 50-400 ℃, preferably 100-250 ℃, and the thermal activation time is 1-24 hours, preferably 2-12 hours. After the heat activation treatment, the organic porous solid needs to be preserved for standby under positive pressure in an inert atmosphere.
As the inorganic porous solid, for example, there may be mentioned refractory oxides of metals of group IIA, III A, IVA or IVB of the periodic Table (such as silica (also referred to as silica or silica gel), alumina, magnesia, titania, zirconia or thoria, etc.), or any refractory composite oxides of these metals (such as silica alumina, magnesia alumina, titania silica, titania magnesia and titania alumina, etc.), and clays, molecular sieves (such as ZSM-5 and MCM-41), mica, montmorillonite, bentonite and diatomaceous earth, etc. The inorganic porous solid may be an oxide formed by high-temperature hydrolysis of a gaseous metal halide or a gaseous silicon compound, such as silica gel obtained by high-temperature hydrolysis of silicon tetrachloride, alumina obtained by high-temperature hydrolysis of aluminum trichloride, or the like. Silica, alumina, magnesia, silica alumina, magnesia alumina, titania silica, titania, molecular sieves, montmorillonite and the like are preferred, with silica being particularly preferred. Suitable silicas can be prepared by conventional methods or can be any commercially available product, such as Grace 955, grace 948, grace SP9-351, grace SP9-485, grace SP9-10046, davision Syloid 245 and Aerosil812, ES70X, ES70Y, ES70W, ES757, EP10X and EP11 from Ineos, and CS-2133 and MS-3040 from PQ.
Specifically, the amount of the polyethylene main catalyst is described below.
According to the present invention, the amount of the polyethylene main catalyst may be the amount of the catalyst commonly used in the art, and the main amount thereof is determined according to the ethylene slurry polymerization activity of the catalyst, wherein the low amount of the polyethylene main catalyst is used under the high ethylene slurry polymerization activity, and the higher amount of the polyethylene main catalyst is used under the low ethylene slurry polymerization activity, thereby realizing the concentration of the slurry to meet the requirements of the present invention. For example, the ratio of the polyethylene main catalyst to the polymerization solvent is 0.001 to 0.500mmol of the polyethylene main catalyst per liter of the polymerization solvent, preferably 0.005 to 0.200mmol of the polyethylene main catalyst per liter of the polymerization solvent, more preferably 0.005 to 0.05mmol of the polyethylene main catalyst per liter of the polymerization solvent, based on the active metal element in the polyethylene main catalyst. In general, for the production of polyethylene at high polymerization activities, such as at lower hydrogen to ethylene molar ratios, higher comonomer to ethylene molar ratios, or higher polymerization pressures, or higher polymerization temperatures, lower polyethylene procatalyst concentrations may be employed; conversely, higher concentrations of the polyethylene procatalyst may be employed, such as at higher hydrogen to ethylene molar ratios, lower comonomer to ethylene molar ratios, or lower polymerization pressures, or lower polymerization temperatures. In addition, the ratio of the polyethylene main catalyst to the polymerization solvent can be 0.005-0.05mmol of the polyethylene main catalyst/L of the polymerization solvent.
In the present invention, unless otherwise specified, the molar amount of the polyethylene main catalyst is calculated as the active metal element in the polyethylene main catalyst.
In the present invention, the cocatalyst is described below.
According to the invention, the cocatalyst is selected from aluminoxanes, alkylaluminum, haloalkylaluminum, borohalothane, alkylboron or alkylboron ammonium salts or mixtures thereof.
Among them, as the aluminoxane, for example, a linear aluminoxane represented by the following general formula (I) can be cited: (R) (R) Al- (Al (R) -O) n -O-Al (R), and a cyclic aluminoxane represented by the following general formula (II): - (Al (R) -O-) n+2 -。
In the formulae (I) and (II) described above, the radicals R are identical or different (preferably identical) from one another and are each independently selected from C 1 -C 8 Alkyl groups, preferably methyl, ethyl, propyl, butyl and isobutyl, most preferably methyl, isobutyl; n is any integer in the range of 1-50, preferably any integer in the range of 10-30.
As the aluminoxane, methylaluminoxane, ethylaluminoxane, isobutylaluminoxane and n-butylaluminoxane are preferred, and methylaluminoxane and isobutylaluminoxane are further preferred.
These aluminoxanes may be used singly or in combination of plural kinds in any ratio.
Examples of the aluminum alkyl include compounds represented by the following general formula:
Al(R) 3
wherein the radicals R are identical or different (preferably identical) from one another and are each independently selected from C 1 -C 8 Alkyl groups, preferably methyl, ethyl, propyl, butyl and isobutyl groups, most preferably methyl, isobutyl groups.
Specifically, examples of the aluminum alkyl include trimethylaluminum (Al (CH) 3 ) 3 ) Triethylaluminum (Al (CH) 3 CH 2 ) 3 ) Tri-n-propylaluminum (Al (C) 3 H 7 ) 3 ) Triisopropylaluminum (Al (i-C) 3 H 7 ) 3 ) Triisobutylaluminum (Al (i-C) 4 H 9 ) 3 ) Tri-n-butyl aluminum (Al (C) 4 H 9 ) 3 ) Triisopentylaluminum (Al (i-C) 5 H 11 ) 3 ) Tri-n-pentylaluminum (Al (C) 5 H 11 ) 3 ) Tri-n-hexylaluminum (Al (C) 6 H 13 ) 3 ) Triisohexylaluminum (Al (i-C) 6 H 13 ) 3 ) Diethyl methylaluminum (Al (CH) 3 )（CH 3 CH 2 ) 2 ) And dimethyl ethyl aluminum ((Al (CH) 3 CH 2 )(CH 3 ) 2 ) And the like,among them, trimethylaluminum, triethylaluminum, tripropylaluminum and triisobutylaluminum are preferable, and triethylaluminum and triisobutylaluminum are most preferable.
These aluminum alkyls may be used alone or in combination of plural kinds in any ratio.
Examples of the haloalkylaluminum include a compound represented by the following general formula:
Al(R) n X 3-n
wherein the radicals R are identical or different (preferably identical) from one another and are each independently selected from C 1 -C 8 Alkyl groups, preferably methyl, ethyl, propyl, butyl and isobutyl, most preferably methyl, isobutyl; x represents fluorine, chlorine, bromine or iodine; n represents 1 or 2.
Specifically, examples of the haloalkylaluminum include dimethylaluminum chloride (Al (CH) 3 ) 2 Cl), aluminum dichloromethyl (Al (CH) 3 )Cl 2 ) Diethyl aluminum chloride (Al (CH) 3 CH 2 ) 2 Cl), ethylaluminum dichloride (Al (CH) 3 CH 2 )Cl 2 ) Dipropylaluminum chloride (Al (C) 3 H 7 ) 2 Cl), aluminum dichloropropylate (Al (C) 3 H 7 )Cl 2 ) Di-n-butylaluminum monochloride (Al (C) 4 H 9 ) 2 Cl), n-butylaluminum dichloride (Al (C) 4 H 9 )Cl 2 ) Diisobutylaluminum chloride (Al (i-C) 4 H 9 ) 2 Cl), isobutyl aluminum dichloride (Al (i-C) 4 H 9 )Cl 2 ) Di-n-pentylaluminum monochloride (Al (C) 5 H 11 ) 2 Cl), n-pentylaluminum dichloride (Al (C) 5 H 11 )Cl 2 ) Diisoamyl aluminum monochloride (Al (i-C) 5 H 11 ) 2 Cl), isoamyl aluminum dichloride (Al (i-C) 5 H 11 )Cl 2 ) Di-n-hexylaluminum monochloride (Al (C) 6 H 13 ) 2 Cl), n-hexylaluminum dichloride (Al (C) 6 H 13 )Cl 2 ) Diisohexylaluminum monochloride (Al (i-C) 6 H 13 ) 2 Cl), isocohexylaluminum dichlorideAl(i-C 6 H 13 )Cl 2 ) Chloromethylethylaluminum (Al (CH) 3 )(CH 3 CH 2 ) Cl), chloromethyl propyl aluminum (Al (CH) 3 )(C 3 H 7 ) Cl), chloromethyl n-butylaluminum (Al (CH) 3 )(C 4 H 9 ) Cl), chloromethyl isobutyl aluminum (Al (CH) 3 )(i-C 4 H 9 ) Cl), ethyl propyl aluminum monochloride (Al (CH) 2 CH 3 )(C 3 H 7 ) Cl), ethyl-n-butyl-aluminum monochloride (AlCH) 2 CH 3 )(C 4 H 9 ) Cl), chloromethyl isobutyl aluminum (Al (CH) 2 CH 3 )(i-C 4 H 9 ) Cl), and the like, among which diethylaluminum chloride, ethylaluminum dichloride, di-n-butylaluminum chloride, n-butylaluminum dichloride, diisobutylaluminum chloride, isobutylaluminum dichloride, di-n-hexylaluminum monochloride, n-hexylaluminum dichloride are preferable, diethylaluminum chloride, ethylaluminum dichloride, and di-n-hexylaluminum monochloride are further preferable, and diethylaluminum monochloride is most preferable.
These haloalkylaluminum may be used alone or in combination of plural kinds in an arbitrary ratio.
As the borane, alkylboron and alkylboron ammonium salt, those conventionally used in the art can be directly used, and are not particularly limited, such as trimethylboron, triethylboron, triphenylboron, tris (pentafluorophenyl) boron, tris [3, 5-bis (trifluoromethyl) phenyl ] boron, hexafluorophenylboron, trityltetra (pentafluorophenyl) borate, N-dimethylanilinium tetrakis (pentafluorophenyl) borate, 1-butyl-3-methylimidazolium tetrafluoroborate, ferrocenetetrafluoroborate, trimethylammonium tetraphenylborate, triethylammonium tetraphenylborate, tripropylammonium tetraphenylborate, tributylammonium tetraphenylborate, trimethylammonium tetrakis (p-tolyl) borate, tripropylammonium tetrakis (p-tolyl) boron, trimethylammonium tetrakis (o, para-dimethylphenyl) borate, triethylammonium tetrakis (ortho, para-dimethylphenyl) borate, trimethylammonium tetrakis (para-trifluoromethylphenyl) borate, tributylammonium tetrakis (pentafluorophenyl) borate, N-diethylanilinium tetraphenyl borate, N-diethylanilinium tetrapentafluorophenyl borate, diethylammonium tetrapentafluorophenyl borate, and the like.
In addition, according to the present invention, one kind of the above-mentioned cocatalysts may be used alone, or a plurality of kinds of the above-mentioned cocatalysts may be used in combination in an arbitrary ratio as required, and the ratio of each component in the mixture is not particularly limited and may be arbitrarily selected as required.
According to the invention, the cocatalysts are generally used in solution. In preparing the solution of the cocatalyst, the solvent used at this time is not particularly limited as long as it can dissolve the cocatalyst, and is generally selected from alkane solvents such as n-pentane, isopentane, cyclopentane, neopentane, etc., or aromatic hydrocarbon solvents such as toluene, ethylbenzene, xylene, etc., and the same solvent as the polymerization solvent is preferable for facilitating the subsequent separation according to the present invention; or the same solvent as one of the mixed solvents for polymerization.
In the present invention, when the cocatalyst is aluminoxane, alkylaluminum or haloalkylaluminum, the molar amount of the cocatalyst is calculated on the molar amount of Al element unless otherwise specified; when the cocatalyst is boron fluorine, alkyl boron or alkyl boron ammonium salt, the molar quantity of the cocatalyst is calculated by the molar quantity of B element.
Specifically, the ratio and the addition mode of the cocatalyst to the polyethylene main catalyst are described below.
According to the invention, for the ratio of the cocatalyst to the polyethylene main catalyst, the molar ratio of aluminum to active metal is 10-500, calculated by the total aluminum element in aluminoxane, alkyl aluminum and halogenated alkyl aluminum in the cocatalyst and the active metal element in the polyethylene main catalyst: 1, preferably the molar ratio of aluminium to active metal is from 20 to 100:1.
the molar ratio of boron to active metal is 1-50 based on boron element in the boron halothane, alkyl boron or alkyl boron ammonium salt in the cocatalyst and active metal element in the polyethylene main catalyst: 1, preferably the molar ratio of boron to active metal is from 1 to 20:1.
the molar ratio of aluminum, boron and active metal is 10-100 based on the total aluminum element in the cocatalyst aluminoxane, alkyl aluminum and halogenated alkyl aluminum, boron element in the boron-fluorine, alkyl boron or alkyl boron ammonium salt and active metal element in the polyethylene main catalyst: 1-20:1, preferably aluminum, boron, in a molar ratio to active metal of 20 to 50:1-10:1.
the manner of adding the polyethylene main catalyst and the cocatalyst to the polymerization reaction system is not particularly limited, and the polyethylene main catalyst may be added first, then the cocatalyst may be added, or the cocatalyst may be added first, then the polyethylene main catalyst may be added, or both may be added together after contact and mixing, or may be added simultaneously, or a part of the cocatalyst may be added first, then the polyethylene main catalyst and the remaining cocatalyst may be added simultaneously, or a part of the polyethylene main catalyst may be added first, and then the remaining polyethylene main catalyst and the cocatalyst may be added simultaneously. When the main catalyst and the cocatalyst of the polyethylene are added respectively, the main catalyst and the cocatalyst of the polyethylene can be added in the same feeding pipeline in sequence or in multiple feeding pipelines in sequence, wherein the main catalyst and the cocatalyst of the polyethylene are added respectively at the same time, and multiple feeding pipelines are selected.
Specifically, the ethylene slurry polymerization conditions for producing an ethylene polymer are described below.
According to one embodiment of the invention, the polymerization temperature of the slurry polymerization is 30-110 ℃, preferably 50-100 ℃. According to one embodiment of the invention, the polymerization pressure is from 0.2 to 4.0MPa, preferably from 1.0 to 3.8MPa. According to one embodiment of the invention, the molar ratio of hydrogen to ethylene is between 0.01 and 20:1, preferably 0.015-10:1. according to one embodiment of the invention, the molar ratio of hydrogen to comonomer is from 8 to 30:1, preferably 10-25:1, more preferably 12-23:1. according to one embodiment of the invention, the molar ratio of comonomer to ethylene is between 0.01 and 0.500: 1. preferably 0.015-0.350:1.
according to one embodiment of the present invention, the ratio of the polyethylene main catalyst to the polymerization solvent is 0.001 to 0.500mmol of the polyethylene main catalyst per liter of the polymerization solvent, preferably 0.005 to 0.200mmol of the polyethylene main catalyst per liter of the polymerization solvent, more preferably 0.005 to 0.05mmol of the polyethylene main catalyst per liter of the polymerization solvent, in terms of the amount of the active metal. According to one embodiment of the invention, the slurry concentration is 50-500 g polymer/L polymerization solvent, preferably 100-400 g polymer/L polymerization solvent.
Among them, an ethylene slurry polymerization reactor for preparing an ethylene polymer is described as follows.
For the preparation method of the ethylene polymer, in the presence of hydrogen and gaseous or liquid comonomer, the ethylene slurry polymerization is carried out in a single or a plurality of ethylene slurry reactors by continuously feeding gaseous ethylene or liquid ethylene slurry, wherein the ethylene slurry polymerization reactor can be a single kettle reactor with stirring, a series multistage kettle reactor with stirring, a parallel multistage kettle reactor with stirring, a series multistage kettle reactor with stirring, a parallel kettle reactor with stirring, a series kettle reactor with stirring, a parallel kettle reactor with stirring, a series kettle reactor with stirring, a parallel kettle reactor with stirring, and a parallel kettle reactor with stirring; preferably a single stirred tank reactor, a series multistage tank reactor, a parallel multistage tank reactor, a series-first parallel tank reactor, more preferably a single stirred tank reactor, a series-type two-stage or three-stage tank reactor, a parallel-type two-stage tank reactor, a series-first parallel three-stage tank reactor. Among them, the embodiment of the ethylene tank type slurry polymerization for preparing an ethylene polymer is explained as follows.
When intermittent copolymerization is adopted, the polyethylene main catalyst, the cocatalyst, the polymerization solvent, the comonomer and the hydrogen are firstly added into an ethylene slurry polymerization reactor according to the proportion at one time, then ethylene is continuously introduced, the polymerization pressure and the polymerization temperature are constant, after the reaction is finished, the ethylene is stopped being introduced, the gas in the kettle is discharged, the slurry material in the kettle is discharged after being cooled to the room temperature, and the slurry material is filtered and dried.
When batch copolymerization is adopted, the respective proportions of hydrogen and comonomer and ethylene are obtained by dividing the respective molar amounts of hydrogen and comonomer which are added in advance by the total cumulative molar amount of ethylene added in the whole process from the beginning to the end of the reaction.
When continuous copolymerization is adopted, the polyethylene main catalyst, the cocatalyst, the polymerization solvent, the comonomer, the hydrogen and the ethylene are simultaneously and continuously added into an ethylene slurry polymerization reactor according to the proportion, the reaction is carried out under constant polymerization pressure and polymerization temperature, the materials generated by the polymerization reaction also continuously leave an ethylene slurry stirring kettle and enter post-treatment processes such as degassing, desolventizing (such as flash evaporation, centrifugation or filtration), drying, granulating (or not granulating) and the like.
When continuous copolymerization is used, the ratio of the respective amounts of hydrogen and comonomer to ethylene refers to the ratio of the respective molar amounts of hydrogen and comonomer to the molar amount of ethylene in the gas phase component in the reaction vessel when the polymerization process is stable.
Among them, the stirring method and stirring speed of ethylene slurry polymerization for producing an ethylene polymer are described below.
The stirring system and stirring speed are not particularly limited as long as sufficient stirring and dispersion of the polyethylene main catalyst, the cocatalyst, ethylene, hydrogen, the comonomer and the slurry in the ethylene slurry reactor can be ensured. Generally, the stirring method may be anchor type stirring paddles, ribbon type stirring paddles, paddle type stirring paddles, turbine type stirring paddles, propelling type stirring paddles (propeller type stirring paddles), or frame type stirring paddles. When the height of the paddle is relatively large (for example, greater than 2), the paddle may be a multi-layer paddle, and the manner of stirring and sealing is not particularly limited. In general, a mechanical seal type or a magnetic seal type can be used, and the volume of the ethylene slurry polymerization reactor is 10m or more 3 In this case, a mechanical seal is preferably used. In ethylene slurry polymerization reactor volume of less than 10m 3 When in use, magnetic sealing is preferably adopted; the stirring speed is related to the ethylene slurry reactor volume and the stirring mode, and generally, the smaller the reactor volume (e.g., 5m or less 3 ) Or an anchor type stirring paddle, a paddle type stirring paddle, a turbine type stirring paddle, a propelling type stirring paddle (propeller type) and the like are adopted, and the stirring rotating speed is 200-1000rpm as the required stirring rotating speed is larger. The larger the reactor volume (e.g. greater than 10m 3 ) Or by helical ribbon type stirring paddles, frame type stirring paddles, etcThe smaller the stirring speed required, the stirring speed is between 10 and 200rpm. In the reactor volume of more than 5m 3 And less than 10 is equal to m 3 When stirring, the stirring speed is 100-500rpm.
The ethylene slurry polymerization temperature for preparing ethylene polymers is described below.
According to the present invention, the ethylene slurry polymerization temperature for preparing the ethylene polymer is a polymerization slurry temperature of 30 to 110℃and preferably 50 to 100 ℃.
The polymerization temperature has influence on polymerization activity of a main catalyst of polyethylene, polymerization service life, stability of instant consumption of ethylene and the like, and on properties of ethylene polymers prepared by ethylene slurry polymerization, such as bulk density, true density, molecular weight and distribution thereof, copolymerization sequence content, composition, distribution and the like, stability of quality and the like. Generally, at higher polymerization temperatures (e.g., 65-110 ℃), the ethylene slurry polymerization activity of the polyethylene procatalyst is higher and the polymerization lifetime is shorter, thus resulting in a lower molecular weight and higher melt index of the ethylene polymer; and at lower polymerization temperatures (e.g., 30-65 ℃), the ethylene slurry polymerization activity of the polyethylene main catalyst is lower, the polymerization life is longer, and the molecular weight of the resulting ethylene polymer is higher and the melt index is lower.
The polymerization temperature is mainly the combined result of chain polymerization of ethylene and comonomer in polymerization solvent in the presence of polyethylene main catalyst and cocatalyst, and the heat released by combination, and the heat or heat-removing mode of external jacket heating or heat-removing, internal coil heating or heat-removing, slurry external circulation heating or heat-removing, gas phase evaporation heat-removing or phase change latent heat-removing released from gas phase to liquid phase, etc. of ethylene slurry reactor is adopted. In addition, when the ethylene slurry is used for preparing the ethylene polymer, the modes of reducing the input amount of the main catalyst of the polyethylene or stopping the input, reducing the polymerization pressure, increasing the molar ratio of hydrogen to ethylene and the like can be adopted to assist in reducing and controlling the polymerization temperature when one temperature is difficult to control, so that the polymerization phenomena of agglomeration, plasticization and the like of the ethylene polymer caused by the fact that the polymerization temperature is out of control (for example, the temperature is increased by 0.5-2 ℃ per minute when the temperature is 20 ℃ above and below the preset polymerization temperature) can be prevented and avoided. In the most extreme case, the polymerization pressure can be suddenly vented, or a small amount of inactivating agent such as carbon monoxide, carbon dioxide, ethanol, water vapor, or a mixture thereof or a terminator can be introduced to quench the ethylene slurry polymerization activity of the polyethylene main catalyst, so that the polymerization temperature is prevented from flying to a temperature (such as 20 ℃ above and below the preset polymerization temperature, and the temperature is increased by more than 2 ℃ per minute) to cause the polymerization phenomena such as ethylene polymer plasticization and the like.
Among them, the polymerization pressure of ethylene slurry for preparing ethylene polymer is described as follows.
According to the present invention, the ethylene slurry polymerization pressure for preparing the ethylene polymer is the total pressure of the ethylene slurry polymerization reactor, which is determined by the partial pressure and vapor pressure of ethylene, cocatalyst and dissolved solvent, hydrogen, comonomer, polymerization solvent, etc. in the ethylene slurry polymerization reactor at the polymerization temperature and optionally added inert gas, and is 0.2 to 4.0MPa, preferably 1.0 to 3.8MPa. The polymerization pressure may also be 1.2 to 3.6MPa.
Similar to the ethylene slurry polymerization temperature, the ethylene slurry polymerization pressure has an influence on the polymerization activity of the main catalyst of polyethylene, the polymerization life, the stability of the instant consumption of ethylene, and the like, and on the properties of the ethylene polymer prepared by the ethylene slurry polymerization, such as bulk density, true density, molecular weight and the stability of the distribution thereof, copolymerization sequence content, composition, distribution, and the like. Generally, at higher polymerization pressures (e.g., 1.5-4.0 MPa), the ethylene slurry polymerization activity of the polyethylene main catalyst is higher; while at lower polymerization pressures (e.g., 0.2-1.5 MPa), the ethylene slurry polymerization activity of the polyethylene main catalyst is lower.
The choice of ethylene slurry polymerization pressure requires a combination of factors and conditions for the ethylene polymer, and generally, when the polymerization solvent is selected from the lower boiling alkane solvents or the higher vapor pressure mixed alkane solvents at 20 ℃, the higher polymerization pressure can be implemented to exert the ethylene slurry polymerization activity of the polyethylene main catalyst and reduce the polymerization cost. According to the research of the invention, it is found that the alkane solvent such as n-pentane, neopentane, cyclopentane or isopentane at 5-55 ℃ or the mixed alkane solvent with saturated vapor pressure of 20-150KPa at 20 ℃ is adopted as a polymerization solvent, the polymerization pressure higher than 1.5MPa can be implemented, the high polymerization pressure can provide a wide polymerization condition selection space for adopting a larger molar ratio of hydrogen to ethylene and a larger molar ratio of comonomer to ethylene under the ethylene slurry polymerization activity condition of fully releasing the polyethylene main catalyst, and further ethylene polymers with different molecular weights, different melt indexes, different comonomer insertion rates, different true densities and the like can be regulated and obtained within a larger polymerization process condition range. Meanwhile, the present inventors have unexpectedly found that an excessively high polymerization pressure does not result in a high ethylene slurry polymerization activity of the polyethylene main catalyst, and that in one polymerization example, for example, above 4.0MPa, the polymerization activity of the polyethylene main catalyst is drastically reduced, and that there is little significant polymerization activity (polymerization activity below 1KgPE/g of the polyethylene main catalyst) in the initial time (0 to 1 h) for starting the ethylene slurry polymerization.
Among them, the ethylene slurry polymerized comonomer for preparing an ethylene polymer is described as follows.
According to the invention, the comonomer is selected from the group consisting of alpha-olefins, diolefins, cyclic olefins and other ethylenically unsaturated compounds.
Specifically, the alpha-olefin may be C 3 -C 10 Examples of the α -olefin include propylene, 1-butene, 1-hexene, 1-heptene, 4-methyl-1-pentene, 1-octene, 1-decene, 1-undecene, 1-dodecene, and styrene. Examples of the cyclic olefin include 1-cyclopentene, ethylidene norbornene, and the like. Examples of the diolefin include 1, 4-butadiene, 2, 5-pentadiene, 1, 6-heptadiene, vinyl norbornene, norbornadiene, and 1, 7-octadiene. Examples of the other ethylenically unsaturated compound include vinyl acetate and (meth) acrylate. Wherein the comonomer is preferably C 3 -C 10 The alpha-mono-olefin is more preferably at least one of propylene, 1-butene, 1-hexene and 1-octene.
In carrying out the polymerization, ethylene and comonomer are fed into the polymerization vessel to carry out the polymerization. In the present invention, "ethylene and comonomer are fed together into a polymerization vessel" means that ethylene and comonomer are fed together into a reaction vessel to perform polymerization reaction together, and there is no step of stage polymerization, i.e., there is no stage step of polymerizing ethylene before adding comonomer for polymerization, and there is no stage step of homopolymerizing comonomer before adding ethylene for polymerization. The polyethylene obtained is a random copolymer structure.
The copolymerization of ethylene and the comonomer can reduce the true density and crystallinity of the ethylene polymer, improve and enhance the mechanical properties, such as mechanical strength and toughness, and increase the environmental stress cracking resistance.
According to the invention, the molar ratio of comonomer to ethylene is between 0.01 and 0.500: 1. preferably 0.015-0.350:1. the invention can regulate and control the performances of the ethylene polymer such as melt index, true density, comonomer insertion rate, weight average molecular weight, molecular weight distribution, crystallinity, melting point and the like under the load of 2.16Kg and 190 ℃ under the polymerization conditions such as proper polyethylene main catalyst and the like.
Next, the molar ratio of hydrogen to ethylene in the ethylene slurry polymerization for producing an ethylene polymer is described below.
Hydrogen acts as a chain transfer agent and a terminator for the ethylene slurry polymerization, the main function of which is to reduce the melt index and molecular weight of the ethylene polymer thus obtained, and to obtain the oligomer in copolymerized form thereby. In general, ethylene polymers obtained under ethylene slurry polymerization conditions of high hydrogen to ethylene molar ratio have lower molecular weights and higher melt indices, whereas ethylene polymers obtained under ethylene slurry polymerization conditions of low hydrogen to ethylene molar ratio have higher molecular weights and lower melt indices. The presence of hydrogen at certain polymerization pressure conditions reduces the ethylene partial pressure and thus reduces the ethylene slurry polymerization activity of the polyethylene procatalyst.
The inventor researches and discovers that when a partially supported non-metallocene catalyst is used as a main catalyst of polyethylene, the sensitivity of an ethylene slurry polymerization reaction to hydrogen is higher.
According to the invention, the molar ratio of hydrogen to ethylene under ethylene slurry polymerization conditions is between 0.01 and 20: 1. preferably 0.015-10:1, further preferably 0.02 to 5:1.
next, the molar ratio of hydrogen to comonomer in the ethylene slurry polymerization for producing an ethylene polymer is described below.
The present inventors have found that by setting the molar ratio of hydrogen to the comonomer to a specific range under the specific reaction conditions of the present invention under comparable conditions, a specific copolymerization-type oligomer can be produced concomitantly in the polymerization reaction, and further, by blending the specific polymerization solvent of the present invention, the oligomer can be retained in the resulting ethylene polymer, thereby improving the processability of the ethylene polymer.
According to the invention, the molar ratio of hydrogen to comonomer under ethylene slurry polymerization conditions is between 8 and 30:1, preferably 10-25:1, more preferably 12-23:1.
in addition, the residence time of ethylene slurry polymerization for the preparation of ethylene polymers is described below.
The polymerization residence time is not particularly limited, and may be selected according to the polymerization pressure, polymerization temperature, molar ratio of hydrogen to ethylene, molar ratio of comonomer to ethylene, polymerization activity of the polyethylene main catalyst, polymerization activity life, amount of the polyethylene main catalyst and slurry concentration. In general, a high polymerization activity may be chosen for a short polymerization time, such as an ethylene slurry polymerization activity of less than 1 million grams of polyethylene per gram of polyethylene procatalyst per hour, and a polymerization residence time of from 1 to 12 hours, preferably from 2 to 8 hours; when the ethylene slurry polymerization activity is higher than or equal to 1 g of polyethylene/g of polyethylene main catalyst but less than 3 g of polyethylene/g of polyethylene main catalyst per hour, the polymerization residence time can be selected to be 0.5 to 6 hours, preferably 1 to 4 hours; when the ethylene slurry polymerization activity per hour is higher than or equal to 3 g of polyethylene per g of polyethylene main catalyst, the polymerization residence time may be selected to be 0.2 to 4 hours, preferably 0.5 to 2 hours. But is not limited thereto.
In addition, the concentration of ethylene slurry for preparing ethylene polymer is described below.
The slurry concentration of the ethylene polymer in the ethylene slurry polymerization is an important index for reflecting the degree of the ethylene slurry polymerization process, if the concentration is too low, the preparation cost is high due to the separation of the solvent and the materials, if the concentration is too high, the stirring is difficult to fully disperse, the heat transfer effect is poor, the materials in the kettle are uneven, and the ethylene polymer is not beneficial to being obtained. According to the invention, the slurry concentration of the ethylene polymer in the ethylene slurry polymerization reactor is 50-500 g polyethylene/liter polymerization solvent, preferably 100-400 g polyethylene/liter polymerization solvent.
In one embodiment of the present invention, there is provided an ethylene polymer having an average particle diameter of 50 to 3000 μm and a bulk density of 0.28 to 0.55g/cm 3 The true density is 0.920-0.980g/cm 3 Melt index at 190 deg.c of 2.16 kg, crystallinity of 30-90%, melting point of 105-147 deg.c, comonomer molar insertion rate of 0-5mol%, weight average molecular weight of 1-150 g/mol and molecular weight distribution of 1.9-20.0.
In one embodiment of the present invention, there is provided an ethylene polymer having an average particle diameter of 100 to 1000 μm and a bulk density of 0.33 to 0.50g/cm 3 The true density is 0.930-0.960g/cm 3 The melt index at 190 ℃ under 2.16 kg load is 0-1000g/10min, the crystallinity is 40-80%, the melting point is 110-143 ℃, the molar insertion rate of the comonomer is 0-3.5mol%, the weight average molecular weight is 2-150 g/mol, and the molecular weight distribution is 2.2-10.0.
In one embodiment of the present invention, there is provided a process for producing an ethylene polymer, wherein an alkane solvent having a boiling point of 5 to 55℃or a mixed alkane solvent having a saturated vapor pressure of 20 to 150KPa (preferably 30 to 80 KPa) at 20℃is used as a polymerization solvent, and a polymerization pressure of 0.2 to 4.0MPa and a molar ratio of hydrogen to ethylene of 0 to 40 is carried out at a polymerization temperature of 30 to 110℃in the presence of a polyethylene catalyst system having a non-metallocene catalyst as a main catalyst: 1, the molar ratio of comonomer to ethylene is 0-1:1, the mixture ratio of the polyethylene main catalyst and the polymerization solvent is 0.001-0.500mmol of the polyethylene main catalyst/L of the polymerization solvent, and the slurry concentration of the slurry is 50-500 g of the polymer/L of the polymerization solvent, and the batch-type or continuous ethylene slurry polymerization is carried out.
In one embodiment of the present invention, there is provided a process for producing an ethylene polymer, wherein the polymerization pressure is 0.5 to 3.0MPa and the molar ratio of hydrogen to ethylene is 0.01 to 20 at a polymerization temperature of 50 to 95 ℃): 1, the molar ratio of comonomer to ethylene is 0.01-0.50:1, the ratio of the polyethylene main catalyst to the polymerization solvent is 0.005-0.200mmol of the polyethylene main catalyst/L of the polymerization solvent, and the slurry concentration is 100-400 g of the polymer/L of the polymerization solvent. The ethylene polymer provided by the invention has excellent physical properties and processability, and can be applied to the fields of textile, papermaking, food, chemical industry, packaging, agriculture, construction, medical treatment, filter cores of filter equipment, sports, entertainment, military and the like.
Examples
The present invention will be described in further detail with reference to examples, but the present invention is not limited to these examples.
Bulk Density of ethylene Polymer (in g/cm 3 ) Is carried out with reference to standard GB 1636-79, the true density of ethylene polymers (in g/cm 3 ) Tests were performed in density tubes according to standard GB/T1033-86.
The content of active metal elements in the polyethylene main catalyst is measured by an ICP-AES method.
The polymerization activity of the polyethylene main catalyst was calculated as follows: when using the ethylene slurry batch process, after the polymerization reaction is finished, the polymerization product in the reaction vessel is filtered and dried, and then the mass of the polymerization product is weighed, and the polymerization activity of the catalyst (kg ethylene polymer/g catalyst or kgPE/gCat) is expressed as a ratio of the mass of the polymerization product divided by the mass of the polyethylene main catalyst used, and when using the ethylene slurry continuous process, the polymerization activity of the catalyst (kg ethylene polymer/g catalyst or kgPE/gCat) is expressed as a value obtained by dividing the instantaneous consumption rate (also called absorption) of ethylene by the continuous addition rate of the polyethylene main catalyst at steady state (polymerization pressure, polymerization temperature and gas phase composition are maintained).
The slurry concentration was calculated as follows, and the weight meter was m after uniform sampling from the ethylene slurry polymerization reactor 1 (in g) and then sufficiently dried to give a dried ethylene polymer m 2 (in g) and the polymerization solvent density was ρ (in g/ml), and the slurry concentration was calculated according to the following formula.
Slurry concentration =。
The melt index of the ethylene polymer (190 ℃ C.; load of 2.16Kg, or, stated otherwise, 5Kg or 21.6 Kg) is determined: reference standard GB T3682-2000 (in g/10 min).
The polymer average particle size is measured on a Microtrac S3500 type laser particle size analyzer, and the particle size measurement range is 0.01-10000 microns.
The weight average molecular weight Mw (in terms of vang/mol), the number average molecular weight Mn (in terms of vang/mol) and the Molecular Weight Distribution (MWD) of the ethylene polymer were measured by using a GPC PL220 high temperature gel chromatograph from Agilent corporation of America, using 4 columns of type Agilent PLgel Olexis, and using 1,2, 4-trichlorobenzene as the mobile phase, the temperature at the measurement was 150℃and calculated as MWD=Mw/Mn, wherein Mw is the weight average molecular weight and Mn is the number average molecular weight.
The determination of the comonomer content in the ethylene polymer was calibrated with a 600M NMR spectrometer from Bruck company and was determined outside a 66/S Fourier transform infrared spectrometer from Bruck company, germany, using a copolymer of known content.
Determination of the crystallinity and melting point of ethylene polymers was determined by differential scanning calorimetry, the apparatus was a Q1000 DSC differential scanning calorimeter from TA company of America, reference standard YYT 0815-2010.
The determination of the residual solvent content in the wet material after the polymerization reaction is that, for the ethylene polymer powder obtained after the polymerization reaction in the polymerization reactor is completed, a 100-mesh filter screen is adopted for direct filtration, the mass m1 of the wet polymer is weighed, the mass m2 of the dry polymer powder is weighed after the wet polymer is completely dried under the vacuum of 20mBar at 80 ℃, and then the residual solvent content is calculated.
Solvent residual content =。
The processing index in the blown film test was determined as follows:
for ethylene polymers, film blowing tests were performed on a Gao Tefu Xtrude 1400 film blowing machine with a host screw diameter of 45mm, an aspect ratio of 25, a die diameter of 80mm, a die gap of 0.8mm, and cooling with annular air at a cooling air temperature of 20 ℃. Extruder screw speed 20rpm, blow ratio 2.3, draw speed: 8 m/min.+ -. 0.5m/min, cooling line height: 230mm-250mm, film thickness: 0.03mm + -0.003 mm.
In the film blowing test, the magnitude of the host current (unit: A) represents the processing index in the film blowing test of the polymer.
The processing index in this blown film test reflects the processability of the polymer, i.e., the smaller the host current, the more excellent the polymer processability, but on the other hand, if too small, extrusion pressure cannot be formed, failing to cause molding processing.
When the processing index in the film blowing test is lower than 4.0, the polymer is very easy to extrude during extrusion, and effective extrusion pressure is difficult to form, so that film blowing molding cannot be performed;
when the processing index in the film blowing test exceeds 6.0, the polymer is very difficult to extrude when extruding, the extruding pressure is too high, and film blowing processing is not easy to carry out;
When the processing index in the film blowing test is between 4.0 and 6.0, the extrusion pressure of the polymer is proper during extrusion processing, and the film blowing processing is easy to carry out;
when the processing index in the film blowing test is between 4.0 and 6.0, the lower the processing index is, the more excellent the processing property is.
In order to more clearly illustrate the ethylene polymer and the process for its preparation of the present invention, in a specific example, the polyethylene slurry polymerization catalyst used is as follows:
a supported non-metallocene catalyst (CAT-1) was prepared as described in example 1 of Chinese patent ZL200710162677.5, wherein the active metallic titanium content was 4.25wt%.
However, according to the present invention, the polyethylene main catalyst includes, but is not limited to, the specific catalysts described above, and the claims are in control.
Example 1
The main catalyst of polyethylene adopts a supported non-metallocene catalyst CAT-1 (concentration is 0.024 mmol/L), the cocatalyst is a pentane solution of Triethylaluminum (TEAL) (concentration is 1.0 mol/L), the polymerization pressure is 1.8MPa, the polymerization temperature is 85 ℃, the polymerization solvent adopts n-pentane (boiling point is 36.1 ℃), the dosage is 2.5L, and the comonomer is 1-hexene.
In a 5L anchored ethylene slurry polymerization kettle with stirring, firstly adding 2.5L polymerization solvent into the polymerization autoclave at normal temperature, starting stirring at the speed of 300rpm, then adding a mixture of a polyethylene catalyst and a cocatalyst at one time, adding a comonomer at one time, adding hydrogen, finally continuously introducing ethylene to ensure that the polymerization pressure and the polymerization temperature are constant, continuously reacting for 2 hours, venting the gas in the kettle, discharging the polymer in the kettle, drying, weighing the mass, marking the ethylene polymer as PE-1, wherein the preparation process and the conditions of the ethylene polymer are shown in the table 1-1, and the properties of the ethylene polymer are shown in the table 1-2.
Example 1-1
Substantially the same as in example 1, but with the following modifications:
the concentration of the main catalyst of the polyethylene is changed to 0.021mmol/L, the cocatalyst is a cyclopentane solution of triethylaluminum (the concentration is 1.0 mol/L), the polymerization pressure is 1.2MPa, the polymerization temperature is 95 ℃, the polymerization solvent adopts cyclopentane (boiling point is 49.26 ℃), the dosage is 2.5L, the comonomer is 1-octene, the rotating speed is 240rpm, the polymerization time is 1.5h, the ethylene polymer is PE-1-1, the preparation process and the conditions of the ethylene polymer are shown in the table 1-1, and the properties of the ethylene polymer are shown in the table 1-2.
Examples 1 to 2
Substantially the same as in example 1, but with the following modifications:
the concentration of the main catalyst of the polyethylene is changed to 0.028mmol/L, the cocatalyst is 2-methyl butane (also called isopentane) solution of triethylaluminum (the concentration is 1 mol/L), the polymerization pressure is 2.4MPa, the polymerization temperature is 78 ℃, isopentane (boiling point 27.83 ℃) is adopted as the polymerization solvent, and the dosage is 2.5L. The rotational speed was 200rpm, and after 3 hours of polymerization time, the gas in the vessel was vented, the polymer in the vessel was discharged, and after drying, the mass was weighed and the ethylene polymer was designated PE-1-2. The preparation process and conditions of the ethylene polymer are shown in Table 1-1, and the properties of the ethylene polymer are shown in Table 1-2.
Examples 1 to 3
Substantially the same as in example 1, but with the following modifications:
the cocatalyst was a neopentane solution (concentration 2.0 mol/L) of Triisobutylaluminum (TIBA), the polymerization pressure was 3.6MPa, the polymerization temperature was 62 ℃, the polymerization solvent was neopentane (boiling point 9.5 ℃ C.), the amount was 2.5L, the comonomer was 1-butene, the rotational speed was 40rpm, the polymerization time was 1h, and the ethylene polymer was designated PE-1-3. The preparation process and conditions of the ethylene polymer are shown in Table 1-1, and the properties of the ethylene polymer are shown in Table 1-2.
Examples 1 to 4
Substantially the same as in example 1, but with the following modifications:
n-pentane and isopentane with saturated vapor pressures of 66.6KPa at 20 ℃ in the polymerization solvent were prepared according to 1:1 mol ratio of the mixed alkane solvent. The co-catalyst solvent also uses the mixed alkane solvent.
The ethylene polymer was designated PE-1-4. The preparation process and conditions of the ethylene polymer are shown in Table 1-1, and the properties of the ethylene polymer are shown in Table 1-2.
Examples 1 to 5
Substantially the same as in example 1, but with the following modifications:
neopentane and isopentane with saturated vapor pressure of 100.01KPa at 20℃as polymerization solvents were prepared according to 0.5:1 mol ratio of the mixed alkane solvent. The co-catalyst solvent also uses the mixed alkane solvent.
The ethylene polymer is designated PE-1-5. The preparation process and conditions of the ethylene polymer are shown in Table 1-1, and the properties of the ethylene polymer are shown in Table 1-2.
Examples 1 to 6
Substantially the same as in example 1, but with the following modifications:
isopentane and cyclopentane with saturated vapor pressure of 72.02KPa at 20 ℃ as polymerization solvents were prepared according to 8:1 mol ratio of the mixed alkane solvent. The co-catalyst solvent also uses the mixed alkane solvent.
The ethylene polymer was designated PE-1-6. The preparation process and conditions of the ethylene polymer are shown in Table 1-1, and the properties of the ethylene polymer are shown in Table 1-2.
Comparative example 1-1
Substantially the same as in example 1, but with the following modifications: the polymerization solvent was changed to hexane solvent, the solvent of the cocatalyst was changed to hexane solution, the ethylene polymer was designated CPE-1-1, the preparation process and conditions of the ethylene polymer were as shown in Table 1-1, and the properties of the ethylene polymer were as shown in Table 1-2.
Comparative examples 1 to 2
Substantially the same as in examples 1-3, but with the following modifications: the polymerization solvent was changed to hexane solvent, the solvent of the cocatalyst was changed to hexane solution, the ethylene polymer was designated CPE-1-2, the preparation process and conditions of the ethylene polymer were as shown in Table 1-1, and the properties of the ethylene polymer were as shown in Table 1-2.
Comparative examples 1 to 3
Substantially the same as in example 1, but with the following modifications:
the molar ratio of comonomer 1-hexene to ethylene was 1 without the addition of hydrogen and the catalyst concentration was changed to 0.007mmol/L.
The ethylene polymer was designated CPE-1-3. The preparation process and conditions of the ethylene polymer are shown in Table 1-1, and the properties of the ethylene polymer are shown in Table 1-2. The polymer is not molded, and the phenomenon of sticking to the kettle is serious.
Comparative examples 1 to 4
Substantially the same as in example 1, but with the following modifications:
no hydrogen and comonomer were added, i.e. the molar ratio of hydrogen to ethylene was 0, the molar ratio of comonomer to ethylene was 0, the polymerization time was 8h and the catalyst concentration was changed to 0.007mmol/L.
The ethylene polymer was designated CPE-1-4. The preparation process and conditions of the ethylene polymer are shown in Table 1-1, and the properties of the ethylene polymer are shown in Table 1-2. The polymer molecular weight is high, GPC cannot measure Mw and Mn, and extrusion processing is impossible.
Comparative examples 1 to 5
Substantially the same as in example 1, but with the following modifications:
the molar ratio of hydrogen to ethylene was 30, and no comonomer was added, i.e., the molar ratio of comonomer to ethylene was 0, and the catalyst concentration was changed to 0.180mmol/L.
The ethylene polymer was designated CPE-1-5. The preparation process and conditions of the ethylene polymer are shown in Table 1-1, and the properties of the ethylene polymer are shown in Table 1-2. The polymer has high melt index and extremely low molecular weight, and the polymer cannot be molded and extruded in processing.
Comparative examples 1 to 6
Substantially the same as in example 1, but with the following modifications:
the molar ratio of hydrogen to comonomer was 0.05 and the catalyst concentration was changed to 0.180mmol/L.
The ethylene polymer was designated CPE-1-6. The preparation process and conditions of the ethylene polymer are shown in Table 1-1, and the properties of the ethylene polymer are shown in Table 1-2. The polymer is not molded, and the phenomenon of sticking to the kettle is serious.
Comparative examples 1 to 7
Substantially the same as in example 1, but with the following modifications:
the molar ratio of hydrogen to comonomer was 40.
The ethylene polymer was designated CPE-1-7. The preparation process and conditions of the ethylene polymer are shown in Table 1-1, and the properties of the ethylene polymer are shown in Table 1-2.
Experimental example
For the ethylene polymers obtained in each example and comparative example, film blowing test was carried out on a Gao Tefu Xtrude 1400 film blowing machine with a host screw diameter of 45mm, an aspect ratio of 25, a die diameter of 80mm, a die gap of 0.8mm, and cooling with annular air with controllable cooling air temperature (cold air temperature of 20 ℃). Extruder screw speed 20rpm, blow ratio 2.3, draw speed: 8 m/min.+ -. 0.5m/min, cooling line height: 230mm-250mm, film thickness: 0.03mm + -0.003 mm. The respective host currents (unit: A) were measured as processing indexes in the film blowing test.
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As is apparent from the comparison of the effects obtained in example 1 and comparative examples 1 to 5 in the above tables, the copolymerization effect of the catalyst is remarkable, i.e., the copolymerization activity of the catalyst is higher than that of the homopolymerization, and the copolymerization can increase the bulk density of the polymer, i.e., improve the particle morphology of the polymer, decrease the true density, melting point and crystallinity of the polymer, and the processability of the high-density polyethylene obtained by the present invention is excellent.
Based on the comparison of the effects obtained in examples 1, 1-3 and comparative examples 1-1 and 1-2 in the above tables, it is apparent that the ethylene polymer powder obtained after completion of the polymerization is very easy to dry by the ethylene slurry polymerization method of the present invention, and the solvent residue content in the wet polymer after completion of the polymerization is less than 20wt% and less than the solvent residue content of more than 25wt% in the wet polymer when hexane is used as the polymerization solvent, which is very advantageous for shortening the drying time of the polyethylene material and saving the post-treatment cost of the polyethylene.
As is clear from a comparison of the examples and comparative examples in the above table, the polyethylene obtained by the ethylene slurry polymerization method of the present invention has a moderate processing index in the blown film test and exhibits excellent processability. This shows that the ethylene polymer obtained by the method of the invention has excellent processability, is very beneficial to post-processing application, can further reduce processing cost under the same conditions, or can further improve the processing efficiency of polyethylene under the same host current.
As can be seen from the data and effects obtained in the table, the ethylene polymer provided by the invention has the advantages of high bulk density, wide and adjustable and controllable range of true density, melt index, crystallinity, melting point, comonomer mole insertion rate, weight average molecular weight and the like, moderate and adjustable and controllable molecular weight distribution, and can realize the regulation and control of the ethylene polymer performance by simply and flexibly changing the polymerization process parameters such as the polyethylene main catalyst, the ratio of the polyethylene main catalyst to the cocatalyst, the molar ratio of hydrogen to ethylene, the molar ratio of the comonomer to the ethylene, the polymerization pressure, the polymerization temperature, the polymerization time and the like, and the obtained high-density polyethylene has excellent processability and is very suitable for the production and application of an ethylene slurry polymerization process.
While the embodiments of the present invention have been described in detail with reference to the examples, it should be noted that the scope of the present invention is not limited by the embodiments, but is defined by the appended claims. Those skilled in the art can make appropriate modifications to these embodiments without departing from the technical spirit and scope of the present invention, and it is apparent that these modified embodiments are also included in the scope of the present invention.

Claims (10)

1. A process for the preparation of a high density ethylene polymer having a true density of from 0.930 to 0.980g/cm 3 Wherein one selected from the group consisting of a combination of n-pentane and isopentane, a combination of neopentane and isopentane, and a combination of isopentane and cyclopentane is used as a polymerization solvent in the presence of a polyethylene catalyst system at a molar ratio of hydrogen to ethylene of 0.01 to 20:1, the molar ratio of hydrogen to comonomer is 8-30:1, subjecting a feedstock comprising ethylene, hydrogen and comonomer to tank slurry polymerization, the polyethylene catalyst system comprising a polyethylene main catalyst which is a non-metallocene catalyst, the polyethylene main catalyst being a supported non-metallocene catalyst, the active metal element of which is selected from group IVB metal elements, the polyethylene catalyst system comprising a cocatalyst which is selected from aluminoxanes, alkylaluminums, haloalkylaluminums, boroalkanes, alkylboranes or alkylsBoron ammonium salt or a mixture of two or more thereof,
the polymerization temperature is 30-110 ℃, the polymerization pressure is 1.0-3.8MPa, kettle type slurry polymerization is carried out in batch type or continuous type, the solvent content in the powder material after flash evaporation, filtration or centrifugal separation of the slurry is less than 20wt%,
the comonomer is more than one selected from propylene, 1-butene, 1-hexene and 1-octene.
2. The process for producing an ethylene polymer according to claim 1, wherein the polymerization temperature is 50 to 100 ℃, the polymerization pressure is 1.0 to 3.8MPa, and the molar ratio of the comonomer to ethylene is 0.01 to 0.500:1.
3. the process for producing an ethylene polymer according to claim 1 or 2, wherein the ratio of the polyethylene main catalyst to the polymerization solvent is 0.001 to 0.500mmol of the polyethylene main catalyst/L of the polymerization solvent, and the slurry concentration is 50 to 500 g of the polymer/L of the polymerization solvent.
4. The process for preparing an ethylene polymer according to claim 1, wherein the molar ratio of aluminum to active metal is from 10 to 500, based on the total aluminum element in the aluminoxane, alkyl aluminum, haloalkyl aluminum in the cocatalyst and the active metal element in the polyethylene main catalyst: 1, the molar ratio of boron to active metal is 1-50 based on boron element in the boron halothane, alkyl boron or alkyl boron ammonium salt in the cocatalyst and active metal element in the polyethylene main catalyst: 1, the mole ratio of aluminum, boron and active metal is 10-100 based on the total aluminum element in cocatalyst aluminoxane, alkyl aluminum and halogenated alkyl aluminum, boron element in boron alkane, alkyl boron or alkyl boron ammonium salt and active metal element in the main catalyst of polyethylene: 1-20:1.
5. The process for preparing an ethylene polymer according to claim 1, wherein the molar ratio of aluminum to active metal is 20 to 100, based on the total aluminum element in the aluminoxane, the alkyl aluminum, the haloalkyl aluminum in the cocatalyst and the active metal element in the polyethylene main catalyst: 1, the mole ratio of boron to active metal is 1-20 based on boron element in the cocatalyst of boron-fluorine, alkyl boron or alkyl boron ammonium salt and active metal element in the main catalyst of polyethylene: 1, the mole ratio of aluminum, boron and active metal is 20-50 based on the total aluminum element in cocatalyst aluminoxane, alkyl aluminum and halogenated alkyl aluminum, boron element in boron alkane, alkyl boron or alkyl boron ammonium salt and active metal element in the main catalyst of polyethylene: 1-10:1.
6. the process for producing an ethylene polymer according to claim 1, wherein the ethylene polymer has a true density of 0.942 to 0.970g/cm 3 The mole ratio of hydrogen to ethylene is 0.015-10:1, the molar ratio of hydrogen to comonomer is 10-25:1.
7. the process for producing an ethylene polymer according to claim 1, wherein the ratio of the polyethylene main catalyst to the polymerization solvent is 0.005 to 0.200mmol of the polyethylene main catalyst/L of the polymerization solvent, and the slurry concentration is 100 to 400 g of the polymer/L of the polymerization solvent.
8. The process for producing an ethylene polymer according to claim 1, wherein the cocatalyst is a catalyst selected from the group consisting of methylaluminoxane, ethylaluminoxane and modified methylaluminoxane, trimethylaluminum, triethylaluminum, triisobutylaluminum, tri-n-hexylaluminum, diethylaluminum chloride, ethylaluminum dichloride or a mixture of two or more thereof,
wherein the molar ratio of hydrogen to comonomer is 12-23:1, the mole ratio of hydrogen to ethylene is 0.02-5:1.
9. the high-density ethylene polymer produced by the process for producing an ethylene polymer as claimed in any one of claims 1 to 8, wherein the ethylene polymer has a true density of 0.930 to 0.980g/cm 3 The weight average molecular weight is 2-40 g/mol, the molecular weight distribution is 1.8-10, the mole insertion rate of comonomer is 0.01-5mol%, the processing index in the blown film test is 4.0-6.0, and the comonomer is more than one selected from propylene, 1-butene, 1-hexene and 1-octene.
10. The ethylene polymer according to claim 9, wherein the ethylene polymer has a melt index of 0.01-2500g/10min at 190 ℃ under a load of 2.16Kg and a bulk density of 0.28-0.55g/cm 3 The average grain diameter of the ethylene polymer is 50-3000 mu m, the crystallinity is 30-90%, and the melting point is 105-147 ℃.
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CN1789292A (en) * 2004-12-17 2006-06-21 扬子石油化工股份有限公司 Application of supported non-metallocene catalyst in ethene polymerization process by slurry method
CN101412765A (en) * 2007-10-16 2009-04-22 中国石化扬子石油化工有限公司 Load type catalyst, load type non-metallocene catalyst and preparations thereof
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