CN114133473A - Special resin powder for chlorinated polyethylene and preparation method and application thereof - Google Patents

Special resin powder for chlorinated polyethylene and preparation method and application thereof Download PDF

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CN114133473A
CN114133473A CN202111545906.8A CN202111545906A CN114133473A CN 114133473 A CN114133473 A CN 114133473A CN 202111545906 A CN202111545906 A CN 202111545906A CN 114133473 A CN114133473 A CN 114133473A
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chlorinated polyethylene
antimony
resin powder
slurry
catalyst
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CN114133473B (en
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李允升
徐彦龙
蓝程程
朱文俊
李胜龙
高晴晴
王琪
张建新
张宏科
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Wanhua Chemical Group 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
    • C08F210/00—Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F210/16—Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
    • 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
    • C08F8/00—Chemical modification by after-treatment
    • C08F8/18—Introducing halogen atoms or halogen-containing groups
    • C08F8/20—Halogenation
    • C08F8/22—Halogenation by reaction with free halogens
    • 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

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  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
  • Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)

Abstract

本发明提供一种氯化聚乙烯专用树脂粉末及其制备方法和应用。所述专用树脂粉末具有相对低的蜡含量、相对宽的分子量分布和相对小的平均粒径，基于本发明提供的氯化聚乙烯专用树脂粉末，能有有效克服现有专用料应用于下游生产氯化聚乙烯时存在氯化不均匀、易粘釜、无法兼顾良好的加工性能与力学性能的问题。本发明提供一种氯化聚乙烯专用树脂粉末，所述氯化聚乙烯专用树脂粉末是聚乙烯或乙烯与α‑烯烃的共聚物，所述氯化聚乙烯专用树脂粉末的粉料密度为0.945～0.960g/cm3，MFR5kg为0.1～10g/10min，平均粒径为100‑300μm，S值为17‑31，蜡含量≤0.5wt％。The invention provides a special resin powder for chlorinated polyethylene and a preparation method and application thereof. The special resin powder has relatively low wax content, relatively wide molecular weight distribution and relatively small average particle size. Based on the special resin powder for chlorinated polyethylene provided by the present invention, it can effectively overcome the existing special materials for downstream production. When chlorinated polyethylene, there are problems of uneven chlorination, easy sticking, and inability to take into account good processability and mechanical properties. The invention provides a special resin powder for chlorinated polyethylene. The special resin powder for chlorinated polyethylene is a copolymer of polyethylene or ethylene and α-olefin, and the powder density of the special resin powder for chlorinated polyethylene is 0.945 ～0.960g/cm 3 , MFR 5kg is 0.1～10g/10min, average particle size is 100-300μm, S value is 17-31, wax content≤0.5wt%.

Description

Special resin powder for chlorinated polyethylene and preparation method and application thereof
Technical Field
The invention relates to the technical field of preparation of special resin for chlorinated polyethylene.
Background
Chlorinated polyethylene is a chlorinated random polymer prepared by chlorination substitution reaction of polyethylene resin, can be regarded as a terpolymer of ethylene, vinyl chloride and 1, 2-dichloroethylene, and has the same carbon main chain structure as the polyethylene resin. Its properties are related to the crystallization regularity, molecular weight and distribution, molecular chain and branched chain structure, particle size and distribution, melt flow rate and S value of the resin raw material, and also related to chlorine content and chlorination production mode.
The chlorinated polyethylene can be classified into plastic chlorinated polyethylene (with a chlorine content of 15%), elastic chlorinated polyethylene (with a chlorine content of 16-25%), elastomer chlorinated polyethylene (with a chlorine content of 26-50%), hard chlorinated polyethylene (with a chlorine content of 51-60%) and high-elasticity chlorinated polyethylene (> 60%) according to the difference of the chlorine content. The special structure of the chlorinated polyethylene endows the chlorinated polyethylene with excellent flexibility, weather resistance, ozone resistance, chemical corrosion resistance, cold resistance and flame resistance, so that the chlorinated polyethylene is widely applied to the fields of plastic doors and windows, PVC pipes and plates, waterproof coiled materials, anticorrosive coatings, wires and cables and the like.
The production method of chlorinated polyethylene mainly comprises three methods, namely a solution method, a suspension method and a gas-solid phase method. The solution process was the first developed process for preparing chlorinated polyethylene and has been largely eliminated. The suspension method comprises a water phase suspension method and a solid phase suspension method, and is the most mature and widely applied production method at present. The gas-solid phase method has not been industrialized at present. The powder resin used in the suspension process can be directly produced by polymerization, or can be obtained by grinding and sieving conventional polyethylene resin.
The conventional special resin for chlorinated polyethylene adopts a Ziegler-Natta catalyst system, and obtains the special resin with wide distribution by multi-kettle series polymerization. However, the special resin for chlorinated polyethylene prepared by the method tends to generate excessive low molecular wax in the first reaction kettle, and the average size of resin particles is relatively large. When the content of the oligomer wax in the special resin is too high, the melting is easy to occur in the chlorination process, so that the viscosity of the system is too high, and the mutual adhesion among powder materials is caused, so that the chlorination of the chlorinated polyethylene product is not uniform, and process safety accidents such as kettle adhesion and parking are easy to occur. When the particle size is too large, the chlorination rate is reduced, and the impact strength, production efficiency and processability of the chlorinated product as a downstream blending modifier are low.
Patent CN10451337A discloses a resin powder for chlorinated polyethylene with low mooney viscosity and a preparation method thereof. Under the action of a Ziegler-Natta catalyst, n-hexane is used as a dispersing agent, polymerization is carried out in a mode of connecting two reaction kettles in series, and the chlorinated polyethylene with narrow particle size distribution and low Mooney viscosity is obtained by controlling the process parameters of a reactor and a reactor. However, in the first reaction kettle of the method, excessive low molecular wax is generated under the condition of high hydrogen-ethylene ratio, and the average particle size of the prepared special resin is larger. Meanwhile, the parameter difference of the first and second kettles is very large, and the matching control has certain difficulty, so that the product quality is easy to fluctuate.
Patent CN104284912A discloses a special resin for chlorinated polyethylene with controlled wax content. The special resin powder with low wax content is prepared in a continuous slurry reaction kettle by taking normal hexane as a dispersing agent under the metallocene catalyst system. However, the special resin prepared by the method has small S value (molecular weight distribution) and cannot simultaneously have good processability and mechanical property.
Disclosure of Invention
The invention provides special resin powder for chlorinated polyethylene and a preparation method and application thereof. The special resin powder for chlorinated polyethylene provided by the invention has relatively low wax content, relatively wide molecular weight distribution and relatively small average particle size, and can obtain a product with the characteristics through optimizing a catalyst system used in the preparation process of the special resin powder for chlorinated polyethylene.
In order to achieve the purpose, the invention provides the following technical scheme:
the invention provides special resin powder for chlorinated polyethylene, which is polyethylene or a copolymer of ethylene and alpha-olefin, and the powder density of the special resin powder for chlorinated polyethylene is 0.945-0.960 g/cm3，MFR5kg0.1-10 g/10min, an average particle size of 100-.
In the art, the wax in the chlorinated polyethylene specialized resin powder is generally an oligomeric wax having a weight average molecular weight of 500-.
Further, the alpha-olefin is propylene, butene-1, hexene-1, octene-1 or 4-methylpentene-1.
The invention also provides a preparation method of the resin powder special for chlorinated polyethylene, wherein ethylene and optional alpha-olefin are subjected to slurry polymerization reaction in a single slurry reaction kettle in the presence of a catalyst to prepare the resin powder special for chlorinated polyethylene, wherein the catalyst comprises an antimony element modified supported chromium-based catalyst, and the average particle size of the antimony element modified supported chromium-based catalyst is preferably 6-20 μm.
By adopting the preparation method, the antimony element modified supported chromium catalyst is adopted to produce the special resin powder for the chlorinated polyethylene, and the advantages of low wax content, wide molecular weight distribution and small average particle size can be obtained. Moreover, the reaction of the invention can be carried out in a single slurry reaction kettle, and the process of generating micromolecules in the first step during step reaction is avoided, thereby reducing the production of oligomer wax; and the reaction is carried out in a single reaction kettle, so that the process parameters are easy to control, and the process control difficulty is greatly reduced. The chlorinated polyethylene produced by the special resin powder provided by the invention has the advantages of high chlorination rate, stable chlorination pressure and uniform chlorine distribution, and the obtained chlorinated polyethylene has excellent processability while maintaining good mechanical properties.
Preferably, the antimony-modified supported chromium-based catalyst is added in an amount of 0.02 to 2mg, preferably 0.03 to 0.2mg, per gram of ethylene.
Further, the catalyst also comprises a cocatalyst which is an aluminum alkyl, preferably the cocatalyst is one or more of triethylaluminum, triisobutylaluminum, ethoxydiethylaluminum, monochlorodiethylaluminum or methylaluminoxane, and more preferably triisobutylaluminum;
preferably, the amount of the cocatalyst is 0.01-10mL, preferably 0.05-1mL, per mg of the antimony-modified supported chromium-based catalyst.
Further, the amount of the antimony element is 0.01 to 5 wt%, preferably 0.02 to 1 wt%, based on the total weight of the antimony element modified supported chromium-based catalyst.
In a preferred embodiment, the preparation of the antimony modified supported chromium-based catalyst comprises:
1) putting a supported chromium catalyst (used as a carrier) into a tubular furnace, loading an antimony element in an antimony compound onto the supported chromium catalyst through vapor deposition, and roasting to obtain a precursor;
2) the precursor obtained in the step 1) is subjected to reduction reaction in the presence of an organic metal reducing agent, a catalyst of low-valence active metal elements is obtained through reduction, and the obtained reduction product is dried to obtain the antimony element modified supported chromium catalyst.
In some embodiments, the vapor deposition in step 1) is performed under an inert atmosphere, and the flow rate of the inert gas is 5-100 mL/min, preferably 40-60 mL/min; the reaction temperature in the step 1) is 100-600 ℃, and preferably 300-550 ℃; the deposition time is 120-480 min, preferably 180-300 min. In the step 1), roasting is carried out in inert gas, the roasting temperature is 300-1000 ℃, preferably 400-800 ℃, the time is 1-10 hours, preferably 4-6 hours, and then cooling is carried out; or the roasting is carried out in two stages, namely a low-temperature stage and a high-temperature stage, wherein the low-temperature stage is carried out at 100-300 ℃ for 1-10 hours, preferably 4-8 hours, and the high-temperature stage is carried out at 300-900 ℃ for 1-10 hours, preferably 4-8 hours.
In some embodiments, in step 2), the reduction reaction is carried out under an inert atmosphere, and the reduction temperature is 20 ℃ to 100 ℃, preferably 20 ℃ to 70 ℃; the reduction time is 0.5 to 20 hours, preferably 0.5 to 10 hours.
The inert gas used is not particularly limited, and nitrogen is preferred.
In step 1), the supported chromium-based catalyst used may be a commercially available product such as the additive C-series catalyst from Basell corporation.
In some embodiments, in step 1), the antimony compound is selected from one or more of antimony trioxide, antimony pentoxide, antimony trichloride, antimony pentachloride, sodium antimonate, sodium hexafluoroantimonate and antimony acetate, and preferably antimony trioxide.
In some embodiments, in step 2), the organometallic reducing agent is one or more of triethylaluminum, triisobutylaluminum, diethylaluminum ethoxide, diethylaluminum monochloride or methylalumoxane, preferably diethylaluminum ethoxide; preferably, the molar ratio of aluminum to chromium is preferably 0.01 to 500, more preferably 0.1 to 50, based on the aluminum element in the organometallic reducing agent and the chromium element in the supported chromium-based catalyst.
In some embodiments, the slurry polymerization is carried out in a single slurry reactor in the presence of the catalyst in an alkane solvent as a medium;
the slurry polymerization reaction is carried out at a reaction temperature of 70 to 85 ℃ preferably 75 to 82 ℃, a reaction pressure of 0.5 to 1.5MPa preferably 0.8 to 1.2MPa, a molar ratio of hydrogen to ethylene of 0.01 to 1, preferably 0.02 to 0.1, and a molar ratio of alpha-olefin to ethylene of 0 to 0.1, preferably 0.01 to 0.04.
In a specific embodiment, the preparation method of the resin powder special for chlorinated polyethylene specifically comprises the following steps:
(1) adding alkane solvent into a slurry reaction kettle, starting continuous stirring, and heating the reaction kettle to 70-85 ℃;
(2) feeding hydrogen and optionally an alpha-olefin to the slurry reactor in a hydrogen to ethylene molar ratio of 0.01 to 1 and an alpha-olefin to ethylene molar ratio of 0 to 0.1;
(3) introducing ethylene into the slurry reaction kettle, and enabling the reaction pressure in the slurry reaction kettle to reach 0.5-1.5 MPa;
(4) adding a catalyst into the slurry reactor to perform a slurry polymerization reaction, for example, for 1 to 5 hours (for example, for 3 hours); in the polymerization reaction process, the pressure in the reaction kettle is kept relatively stable through the introduction of ethylene;
(5) venting the pressure in the slurry reactor and reducing the temperature of the slurry reactor contents, e.g., to 20 ℃, by reactor jacket water;
(6) and (3) discharging the slurry of the polymerization reactant from the bottom of the slurry reaction kettle, and carrying out flash evaporation, centrifugation and drying to obtain the special resin powder for the chlorinated polyethylene.
The alkane solvent is used as a polymerization dispersant, and preferably, the alkane solvent is one or more of butane, pentane, n-hexane or heptane; n-hexane is preferred.
The invention also provides application of the special resin powder for chlorinated polyethylene in a preparation process of chlorinated polyethylene.
The invention adopts the antimony modified supported chromium catalyst which has multiple active centers, each active center has different chain transfer rate and chain growth constant, the obtained product has the characteristics of large melt strength, wide processability and the like, and no obvious by-products such as low molecular wax and the like are generated during polymerization. By optimizing the catalyst system, the invention can overcome the problems of high wax content, narrow molecular weight distribution, large product particle size and the like of the special resin prepared by the existing slurry polymerization process of the special resin for chlorinated polyethylene; the special resin for chlorinated polyethylene provided by the invention is beneficial to solving the problems that the existing special resin is uneven in chlorination, easy to stick to a kettle and incapable of considering good processability and mechanical properties when used for downstream production of chlorinated polyethylene.
According to the special resin powder for chlorinated polyethylene, the chlorinated polyethylene is prepared through downstream chlorination, so that the problems of overhigh chlorination pressure, easy kettle adhesion, low chlorination rate and the like in the chlorination process can be solved.
Detailed Description
In order to better understand the technical solution of the present invention, the following examples are further provided to illustrate the present invention, but the present invention is not limited to the following examples.
Description of the Performance test method of the resin powder specially used for chlorinated polyethylene:
density: reference GB/T1033.2-2010
MFR21.6kgAnd MFR5kg: reference GB/T3682-
Bulk density: reference GB/T1636-
Wax content: weighing about 10g of special resin powder sample for chlorinated polyethylene, putting the special resin powder sample into an extraction paper cylinder with known weight, and putting the paper cylinder and the sample (m)1) The mixture was put into an extractor containing n-heptane, and the extractor was put into a constant temperature oil bath and extracted at 80 ℃ for 6 hours. After extraction, the extraction paper tube containing residual polymer is placed in a vacuum oven, dried to constant weight at 90 ℃, then moved into a silica gel drying oven, cooled for 30 minutes, weighed and recorded as m2(to the nearest 0.1mg), wax content ═ m1-m2)*100％/m1。
S value: s value of the polymer is MFR21.6kgAnd MFR5kgRatio of
Average particle size: the method is carried out on a Beckman Coulter LS230 type laser particle size analyzer, and the particle size measuring range is 0.04-2000 microns.
Description of the chlorinated polyethylene performance detection method:
chlorine content/%: refer to the B method in GB/T7139-.
Mooney viscosity: reference is made to GB/T1232.1-2000.
Shore hardness: reference is made to GB/T531.1-2008.
Tensile strength: the method is carried out according to GB/T528-.
Elongation at break: reference is made to GB/T1340.1-2006.
Example 1
Example 1 a resin powder for chlorinated polyethylene was prepared according to the following process steps:
(1) adding alkane solvent into a slurry reaction kettle, starting continuous stirring, and heating the reaction kettle to 80 ℃; wherein the alkane solvent is n-hexane, and the stirring speed is 500 rpm.
(2) Adding hydrogen and alpha-olefin into the slurry reactor, wherein the molar ratio of the hydrogen to the ethylene is 0.04, and the molar ratio of the alpha-olefin to the ethylene is 0.02; wherein the alpha-olefin is hexene-1.
(3) Introducing ethylene into the slurry reaction kettle, and enabling the reaction pressure in the slurry reaction kettle to reach 0.80 MPa;
(4) adding an antimony modified supported chromium catalyst and a cocatalyst into a slurry reaction kettle to perform slurry polymerization reaction (wherein the dosage of the antimony modified supported chromium catalyst is 20mg, the dosage of the cocatalyst is 3mL, and the cocatalyst is triisobutylaluminum), and reacting for 3 hours; in the polymerization reaction process, introducing ethylene to maintain the relative stability of the pressure in the reaction kettle, and reacting 423g of ethylene;
(5) venting the pressure in the slurry reactor and reducing the temperature of the materials in the slurry reactor to 20 ℃ by reactor jacket water;
(6) and (3) discharging the slurry of the polymerization reactant from the bottom of the slurry reaction kettle, and carrying out flash evaporation, centrifugation and drying to obtain the special resin powder for the chlorinated polyethylene.
The properties of the resin powder for chlorinated polyethylene obtained in example 1 were as follows: the density is 0.949g/cm3，MFR5kg2.1g/10min, and a bulk density of 0.41g/cm3The wax content was 0.38%, the S value was 25, and the average particle diameter was 259. mu.m.
Example 2
Example 2a resin powder for chlorinated polyethylene was prepared according to the following process steps:
(1) adding alkane solvent into a slurry reaction kettle, starting continuous stirring, and heating the reaction kettle to 80 ℃; wherein the alkane solvent is n-hexane, and the stirring speed is 500 rpm.
(2) Adding hydrogen and alpha-olefin into the slurry reactor, wherein the molar ratio of the hydrogen to the ethylene is 0.02, and the molar ratio of the alpha-olefin to the ethylene is 0.01; wherein the alpha-olefin is butene-1.
(3) Introducing ethylene into the slurry reaction kettle, and enabling the reaction pressure in the slurry reaction kettle to reach 0.85 MPa;
(4) adding an antimony modified supported chromium catalyst and a cocatalyst into a slurry reaction kettle to perform slurry polymerization reaction (wherein the dosage of the antimony modified supported chromium catalyst is 20mg, the dosage of the cocatalyst is 3mL, and the cocatalyst is triisobutylaluminum), and reacting for 3 hours; 486g of ethylene is reacted in total by introducing the ethylene to maintain the relative stability of the pressure in the reaction kettle in the polymerization reaction process;
(5) venting the pressure in the slurry reactor and reducing the temperature of the materials in the slurry reactor to 20 ℃ by reactor jacket water;
(6) and (3) discharging the slurry of the polymerization reactant from the bottom of the slurry reaction kettle, and carrying out flash evaporation, centrifugation and drying to obtain the special resin powder for the chlorinated polyethylene.
The properties of the resin powder special for chlorinated polyethylene obtained in example 2 are as follows: the density was 0.956g/cm3，MFR5kg1.1g/10min, and a bulk density of 0.40g/cm3The wax content was 0.23%, the S value was 29, and the average particle diameter was 241 μm.
The antimony-modified supported chromium-based catalyst used in example 1-2 was prepared as follows:
a) fully mixing a supported chromium catalyst and an antimony compound, and then placing the mixture in a tubular furnace, wherein the supported chromium catalyst is Advent C, and the antimony compound is antimony trioxide. The temperature was raised to 500 ℃ at 10 ℃/min under a nitrogen atmosphere (flow rate 50mL/min) and maintained for 3 hours. Then roasting in nitrogen atmosphere at 600 ℃ for 5h, and then naturally cooling to obtain the precursor.
b) And c) carrying out reduction reaction on the precursor obtained in the step a) in the presence of an organic metal reducing agent under the nitrogen atmosphere, and drying the obtained reduction product to obtain the antimony element modified supported chromium catalyst. Wherein the organic metal reducing agent is ethoxy diethyl aluminum, the reduction temperature of the reduction reaction is 20 ℃, the reduction time is 1 hour, and the molar ratio of aluminum to chromium is 40 based on the aluminum element in the organic metal reducing agent and the chromium element in the supported chromium catalyst.
In the obtained antimony element-modified supported chromium-based catalyst, the amount of antimony element supported was 0.3% by weight based on the total weight of the antimony element-modified supported chromium-based catalyst, and the average particle diameter was 14 μm.
Example 3
Example 3 a resin powder for chlorinated polyethylene was prepared according to the following process steps:
(1) adding alkane solvent into a slurry reaction kettle, starting continuous stirring, and heating the reaction kettle to 80 ℃; wherein the alkane solvent is n-hexane, and the stirring speed is 500 rpm.
(2) Adding hydrogen and alpha-olefin into the slurry reactor, wherein the molar ratio of the hydrogen to the ethylene is 0.08, and the molar ratio of the alpha-olefin to the ethylene is 0.02; wherein the alpha-olefin is butene-1.
(3) Introducing ethylene into the slurry reaction kettle, and enabling the reaction pressure in the slurry reaction kettle to reach 0.85 MPa;
(4) adding an antimony modified supported chromium catalyst and a cocatalyst into a slurry reaction kettle to perform slurry polymerization reaction (wherein the dosage of the antimony modified supported chromium catalyst is 20mg, the dosage of the cocatalyst is 3mL, and the cocatalyst is triethylaluminum), and reacting for 3 hours; 376g of ethylene is reacted in total by introducing the ethylene to maintain the relative stability of the pressure in the reaction kettle in the polymerization reaction process;
(5) venting the pressure in the slurry reactor and reducing the temperature of the materials in the slurry reactor to 20 ℃ by reactor jacket water;
(6) and (3) discharging the slurry of the polymerization reactant from the bottom of the slurry reaction kettle, and carrying out flash evaporation, centrifugation and drying to obtain the special resin powder for the chlorinated polyethylene.
The properties of the resin special for chlorinated polyethylene obtained in example 3 are as follows: the density was 0.952g/cm3，MFR5kg2.7g/10min, and a bulk density of 0.41g/cm3The wax content was 0.46%, the S value was 24, and the average particle diameter was 255 μm.
Example 4 (without alpha-olefin)
Example 4 a resin powder for chlorinated polyethylene was prepared according to the following process steps:
(1) adding alkane solvent into a slurry reaction kettle, starting continuous stirring, and heating the reaction kettle to 80 ℃; wherein the alkane solvent is normal hexane, and the stirring speed is 500 rpm;
(2) adding hydrogen into the slurry reactor, wherein the molar ratio of the hydrogen to the ethylene is 0.02;
(3) introducing ethylene into the slurry reaction kettle, and enabling the reaction pressure in the slurry reaction kettle to reach 0.85 MPa;
(4) adding an antimony modified supported chromium catalyst and a cocatalyst into a slurry reaction kettle to perform slurry polymerization reaction (wherein the dosage of the antimony modified supported chromium catalyst is 20mg, the dosage of the cocatalyst is 3mL, and the cocatalyst is triisobutylaluminum), and reacting for 3 hours; 486g of ethylene is reacted in total by introducing the ethylene to maintain the relative stability of the pressure in the reaction kettle in the polymerization reaction process;
(5) venting the pressure in the slurry reactor and reducing the temperature of the materials in the slurry reactor to room temperature of 20 ℃ by reactor jacket water;
(6) and (3) discharging the slurry of the polymerization reactant from the bottom of the slurry reaction kettle, and carrying out flash evaporation, centrifugation and drying to obtain the special resin powder for the chlorinated polyethylene.
Example 4 preparation ofThe properties of the obtained special resin powder for chlorinated polyethylene are as follows: density 0.964g/cm3 MFR5kg0.96g/10min, and a bulk density of 0.39g/cm3The wax content was 0.28%, the S value was 26, and the average particle diameter was 244 μm.
The preparation of the antimony modified supported chromium catalysts used in examples 3-4 was as follows:
a) fully mixing a supported chromium catalyst and an antimony compound, and then placing the mixture in a tubular furnace, wherein the supported chromium catalyst is Advent C, and the antimony compound is antimony pentoxide. The temperature was raised to 500 ℃ at 10 ℃/min under a nitrogen atmosphere (flow rate 50mL/min) and maintained for 3 hours. Then roasting in nitrogen atmosphere at 600 ℃ for 5h, and then naturally cooling to obtain the precursor.
b) And c) carrying out reduction reaction on the precursor obtained in the step a) in the presence of an organic metal reducing agent under the nitrogen atmosphere, and drying the obtained reduction product to obtain the antimony element modified supported chromium catalyst. Wherein the organic metal reducing agent is methylaluminoxane, the reduction temperature of the reduction reaction is 20 ℃, the reduction time is 1 hour, and the molar ratio of aluminum to chromium is 40 based on the aluminum element in the organic metal reducing agent and the chromium element in the supported chromium catalyst.
In the obtained antimony element-modified supported chromium-based catalyst, the amount of antimony element supported was 0.3% by weight based on the total weight of the antimony element-modified supported chromium-based catalyst, and the average particle diameter was 14 μm.
Example 5
Example 5 a resin powder for chlorinated polyethylene was prepared according to the following process steps:
(1) adding alkane solvent into a slurry reaction kettle, starting continuous stirring, and heating the reaction kettle to 80 ℃; wherein the alkane solvent is n-hexane, and the stirring speed is 500 rpm.
(2) Adding hydrogen and alpha-olefin into the slurry reactor, wherein the molar ratio of the hydrogen to the ethylene is 0.02, and the molar ratio of the alpha-olefin to the ethylene is 0.01; wherein the alpha-olefin is butene-1
(3) Introducing ethylene into the slurry reaction kettle, and enabling the reaction pressure in the slurry reaction kettle to reach 0.80 MPa;
(4) adding an antimony modified supported chromium catalyst and a cocatalyst into a slurry reaction kettle to perform slurry polymerization reaction (wherein the dosage of the antimony modified supported chromium catalyst is 20mg, the dosage of the cocatalyst is 3mL, and the cocatalyst is triisobutylaluminum), and reacting for 3 hours; in the polymerization reaction process, 516g of ethylene is reacted together by introducing ethylene to maintain the relative stability of the pressure in the reaction kettle;
(5) venting the pressure in the slurry reactor and reducing the temperature of the materials in the slurry reactor to room temperature of 20 ℃ by reactor jacket water;
(6) and (3) discharging the slurry of the polymerization reactant from the bottom of the slurry reaction kettle, and carrying out flash evaporation, centrifugation and drying to obtain the special resin powder for the chlorinated polyethylene.
The properties of the resin powder special for chlorinated polyethylene obtained in example 5 are as follows: the density was 0.955g/cm3，MFR5kg1.3g/10min, and a bulk density of 0.4g/cm3The wax content was 0.23%, the S value was 17, and the average particle diameter was 252 μm.
Example 6
Example 6 a resin powder for chlorinated polyethylene was prepared according to the following process steps:
(1) adding alkane solvent into a slurry reaction kettle, starting continuous stirring, and heating the reaction kettle to 80 ℃; wherein the alkane solvent is n-hexane, and the stirring speed is 500 rpm.
(2) Adding hydrogen and alpha-olefin into the slurry reactor, wherein the molar ratio of the hydrogen to the ethylene is 0.02, and the molar ratio of the alpha-olefin to the ethylene is 0.01; wherein the alpha-olefin is butene-1
(3) Introducing ethylene into the slurry reaction kettle, and enabling the reaction pressure in the slurry reaction kettle to reach 0.80 MPa;
(4) adding an antimony modified supported chromium catalyst and a cocatalyst into a slurry reaction kettle to perform slurry polymerization reaction (wherein the dosage of the antimony modified supported chromium catalyst is 20mg, the dosage of the cocatalyst is 3mL, and the cocatalyst is triisobutylaluminum), and reacting for 3 hours; in the polymerization reaction process, introducing ethylene to maintain the relative stability of the pressure in the reaction kettle, and reacting ethylene in total 492 g;
(5) venting the pressure in the slurry reactor and reducing the temperature of the materials in the slurry reactor to room temperature of 20 ℃ by reactor jacket water;
(6) and (3) discharging the slurry of the polymerization reactant from the bottom of the slurry reaction kettle, and carrying out flash evaporation, centrifugation and drying to obtain the special resin powder for the chlorinated polyethylene.
The properties of the resin powder for chlorinated polyethylene obtained in example 6 were as follows: the density was 0.956g/cm3，MFR5kg1.3g/10min, and a bulk density of 0.39g/cm3The wax content was 0.25%, the S value was 18, and the average particle diameter was 253. mu.m.
Example 7
Example 7a resin powder for chlorinated polyethylene was prepared according to the following process steps:
(1) adding alkane solvent into a slurry reaction kettle, starting continuous stirring, and heating the reaction kettle to 80 ℃; wherein the alkane solvent is n-hexane, and the stirring speed is 500 rpm.
(2) Adding hydrogen and alpha-olefin into the slurry reactor, wherein the molar ratio of the hydrogen to the ethylene is 0.02, and the molar ratio of the alpha-olefin to the ethylene is 0.01; wherein the alpha-olefin is butene-1
(3) Introducing ethylene into the slurry reaction kettle, and enabling the reaction pressure in the slurry reaction kettle to reach 0.80 MPa;
(4) adding an antimony modified supported chromium catalyst and a cocatalyst into a slurry reaction kettle to perform slurry polymerization reaction (wherein the dosage of the antimony modified supported chromium catalyst is 20mg, the dosage of the cocatalyst is 3mL, and the cocatalyst is triisobutylaluminum), and reacting for 3 hours; in the polymerization reaction process, 266g of ethylene is reacted together by introducing the ethylene to maintain the relative stability of the pressure in the reaction kettle;
(5) venting the pressure in the slurry reactor and reducing the temperature of the materials in the slurry reactor to room temperature of 20 ℃ by reactor jacket water;
(6) and (3) discharging the slurry of the polymerization reactant from the bottom of the slurry reaction kettle, and carrying out flash evaporation, centrifugation and drying to obtain the special resin powder for the chlorinated polyethylene.
Examples7 the properties of the special resin powder for chlorinated polyethylene obtained are as follows: the density is 0.954g/cm3，MFR5kg2g/10min, and a bulk density of 0.39g/cm3The wax content was 0.32%, the S value was 28, and the average particle diameter was 251 μm.
Example 8
Example 8 a resin powder for chlorinated polyethylene was prepared according to the following process steps:
(1) adding alkane solvent into a slurry reaction kettle, starting continuous stirring, and heating the reaction kettle to 80 ℃; wherein the alkane solvent is n-hexane, and the stirring speed is 500 rpm.
(2) Adding hydrogen and alpha-olefin into the slurry reactor, wherein the molar ratio of the hydrogen to the ethylene is 0.02, and the molar ratio of the alpha-olefin to the ethylene is 0.01; wherein the alpha-olefin is butene-1
(3) Introducing ethylene into the slurry reaction kettle, and enabling the reaction pressure in the slurry reaction kettle to reach 0.80 MPa;
(4) adding an antimony modified supported chromium catalyst and a cocatalyst into a slurry reaction kettle to perform slurry polymerization reaction (wherein the dosage of the antimony modified supported chromium catalyst is 20mg, the dosage of the cocatalyst is 3mL, and the cocatalyst is triisobutylaluminum), and reacting for 3 hours; in the polymerization reaction process, introducing ethylene to maintain the relative stability of the pressure in the reaction kettle, and reacting 107g of ethylene;
(5) venting the pressure in the slurry reactor and reducing the temperature of the materials in the slurry reactor to room temperature of 20 ℃ by reactor jacket water;
(6) and (3) discharging the slurry of the polymerization reactant from the bottom of the slurry reaction kettle, and carrying out flash evaporation, centrifugation and drying to obtain the special resin powder for the chlorinated polyethylene.
The properties of the resin powder for chlorinated polyethylene obtained in example 8 were as follows: the density is 0.954g/cm3，MFR5kg3.1g/10min, and a bulk density of 0.4g/cm3The wax content was 0.51%, the S value was 31, and the average particle diameter was 247 μm.
The antimony modified supported chromium catalysts used in examples 5-8 were prepared as follows:
a) fully mixing a supported chromium catalyst and an antimony compound, and then placing the mixture in a tubular furnace, wherein the supported chromium catalyst is Advent C, and the antimony compound is antimony trioxide. The temperature was raised to 500 ℃ at 10 ℃/min under a nitrogen atmosphere (flow rate 50mL/min) and maintained for 3 hours. Then roasting in nitrogen atmosphere at 600 ℃ for 5h, and then naturally cooling to obtain the precursor.
b) And c) carrying out reduction reaction on the precursor obtained in the step a) in the presence of an organic metal reducing agent under the nitrogen atmosphere, and drying the obtained reduction product to obtain the antimony element modified supported chromium catalyst. Wherein the organic metal reducing agent is ethoxy diethyl aluminum, the reduction temperature of the reduction reaction is 20 ℃, the reduction time is 1 hour, and the molar ratio of aluminum to chromium is 40 based on the aluminum element in the organic metal reducing agent and the chromium element in the supported chromium catalyst.
In the obtained antimony element-modified supported chromium-based catalyst, the amounts of antimony element supported in examples 5 to 8 were 0.01 wt%, 0.02 wt%, 1 wt%, and 5 wt%, in that order, based on the total weight of the antimony element-modified supported chromium-based catalyst, and the average particle diameter was 14 μm.
Comparative example 1
Comparative example 1 a resin powder for chlorinated polyethylene was prepared according to the following process steps:
(1) adding alkane solvent into a slurry reaction kettle, starting continuous stirring, and heating the reaction kettle to 80 ℃; wherein the alkane solvent is normal hexane, and the stirring speed is 500 rpm;
(2) adding hydrogen into the slurry reactor, wherein the molar ratio of the hydrogen to the ethylene is 0.04;
(3) introducing ethylene into the slurry reaction kettle, and enabling the reaction pressure in the slurry reaction kettle to reach 0.75 MPa;
(4) 20mg of Ziegler-Natta catalyst (Avant Z501) is added into the slurry reactor, and the gas phase components are discharged after 1.5 hours of reaction; in the polymerization reaction process, 517g of ethylene is reacted together by introducing the ethylene to maintain the relative stability of the pressure in the reaction kettle;
(5) hydrogen and alpha-olefin were fed back to the slurry reactor at a hydrogen to ethylene molar ratio of 2.5 and an alpha-olefin to ethylene molar ratio of 0.04. Wherein the alpha-olefin is butene-1;
(6) introducing ethylene into the slurry reaction kettle, and enabling the reaction pressure in the slurry reaction kettle to reach 0.25MPa for 1.5 hours; in the polymerization reaction process, the pressure in the reaction kettle is kept relatively stable through the introduction of ethylene;
(7) venting the pressure in the slurry reactor and reducing the temperature of the materials in the slurry reactor to 20 ℃ by reactor jacket water;
(8) and (3) discharging the slurry of the polymerization reactant from the bottom of the slurry reaction kettle, and carrying out flash evaporation, centrifugation and drying to obtain the special resin powder for the chlorinated polyethylene.
The properties of the resin powder special for chlorinated polyethylene obtained in comparative example 1 were as follows: the density is 0.954g/cm3，MFR5kg2.6g/10min, and a bulk density of 0.39g/cm3The wax content was 2.73%, the S value was 27, and the average particle diameter was 367 μm.
COMPARATIVE EXAMPLE 2 (COMPARATIVE WITH EXAMPLE 2)
Comparative example 2 the resin powder special for chlorinated polyethylene was prepared according to the following process steps:
(1) adding alkane solvent into a slurry reaction kettle, starting continuous stirring, and heating the reaction kettle to 80 ℃; wherein the alkane solvent is n-hexane, and the stirring speed is 500 rpm.
(2) Adding hydrogen and alpha-olefin into the slurry reactor, wherein the molar ratio of the hydrogen to the ethylene is 0.02, and the molar ratio of the alpha-olefin to the ethylene is 0.01; wherein the alpha-olefin is butene-1.
(3) Introducing ethylene into the slurry reaction kettle, and enabling the reaction pressure in the slurry reaction kettle to reach 0.85 MPa;
(4) adding a Metallocene catalyst XCAT Metallocene cocatalyst (manufacturer Univation) into a slurry reaction kettle to perform slurry polymerization reaction (wherein the dosage of the Metallocene catalyst is 20mg, the dosage of the cocatalyst is 3mL, and the cocatalyst is triisobutylaluminum), and reacting for 3 hours; in the polymerization reaction process, the pressure in the reaction kettle is kept relatively stable by introducing ethylene, and 590g of ethylene is reacted;
(5) venting the pressure in the slurry reactor and reducing the temperature of the materials in the slurry reactor to 20 ℃ by reactor jacket water;
(6) and (3) discharging the slurry of the polymerization reactant from the bottom of the slurry reaction kettle, and carrying out flash evaporation, centrifugation and drying to obtain the special resin powder for the chlorinated polyethylene.
The properties of the resin powder special for chlorinated polyethylene obtained in comparative example 2 were as follows: the density was 0.956g/cm3，MFR5kg1.7g/10min, and a bulk density of 0.41g/cm3The wax content was 1.06%, the S value was 8, and the average particle diameter was 220 μm.
COMPARATIVE EXAMPLE 3 (COMPARATIVE WITH EXAMPLE 2)
Comparative example 3 the resin powder special for chlorinated polyethylene was prepared according to the following process steps:
(1) adding alkane solvent into a slurry reaction kettle, starting continuous stirring, and heating the reaction kettle to 80 ℃; wherein the alkane solvent is n-hexane, and the stirring speed is 500 rpm.
(2) Adding hydrogen and alpha-olefin into the slurry reactor, wherein the molar ratio of the hydrogen to the ethylene is 0.02, and the molar ratio of the alpha-olefin to the ethylene is 0.01; wherein the alpha-olefin is butene-1.
(3) Introducing ethylene into the slurry reaction kettle, and enabling the reaction pressure in the slurry reaction kettle to reach 0.85 MPa;
(4) adding a chromium-based catalyst Advent C and a cocatalyst into a slurry reaction kettle to perform a slurry polymerization reaction (wherein the dosage of the chromium-based catalyst is 20mg, the dosage of the cocatalyst is 3mL, and the cocatalyst is triisobutylaluminum), and reacting for 3 hours; in the polymerization reaction process, introducing ethylene to maintain the relative stability of the pressure in the reaction kettle, and reacting 503g of ethylene;
(5) venting the pressure in the slurry reactor and reducing the temperature of the materials in the slurry reactor to 20 ℃ by reactor jacket water;
(6) and (3) discharging the slurry of the polymerization reactant from the bottom of the slurry reaction kettle, and carrying out flash evaporation, centrifugation and drying to obtain the special resin powder for the chlorinated polyethylene.
The properties of the resin powder special for chlorinated polyethylene obtained in comparative example 3 were as follows: the density was 0.957g/cm3，MFR5kg1.4g/10min, and a bulk density of 0.40g/cm3The wax content was 0.27%, the S value was 8, and the average particle diameter was 249 μm.
Example 9
The chlorinated polyethylene special resin obtained in the above examples and comparative examples is prepared by the following steps:
5L of water and 500g of the special resin for the chlorinated polyethylene prepared in the above example or comparative example are added into a reactor, a dispersant, an emulsifier and an initiator are added into the reactor, and chlorination is carried out for 3 hours at 130 ℃ in gaseous chlorine (excess chlorine), so as to obtain chlorinated polyethylene samples 1-11 respectively, and the performances are as shown in the following table. In the table, samples 1 to 11 correspond to chlorinated polyethylene samples prepared by carrying out reactions using the chlorinated polyethylene exclusive resins of example 1, example 2, example 3, example 4, example 5, example 6, example 7, example 8, comparative example 1, comparative example 2, and comparative example 3 in this order.
Wherein, the used dispersant is sodium polymethacrylate, the emulsifier is polyvinylpyrrolidone, and the initiator is dibenzoyl peroxide; the dosage of the three components is 14g, 1g and 4g respectively.
Table: chlorinated polyethylene Performance test results
Figure BDA0003415780620000191
Figure BDA0003415780620000201
From the results in table 6, it can be seen that the chlorinated polyethylene prepared based on the resins special for chlorinated polyethylene of examples 1 to 8 of the present invention has higher chlorine content and better tensile strength in the same chlorination conditions, which indicates that the chlorinated polyethylene produced has fast chlorination rate, uniform chlorine distribution and excellent production efficiency and stability.
From the results in table 6, it can be seen that the chlorinated polyethylene obtained by chlorinating the resin special for chlorinated polyethylene of the present invention shows good mooney viscosity and excellent tensile strength, and the obtained product can well give consideration to both processability and mechanical properties of chlorinated polyethylene, and has good application prospects.
It will be appreciated by those skilled in the art that modifications or adaptations to the invention may be made in light of the teachings of the present specification. Such modifications or adaptations are intended to be within the scope of the present invention as defined in the claims.

Claims (10)

1.一种氯化聚乙烯专用树脂粉末，其特征在于，所述氯化聚乙烯专用树脂粉末是聚乙烯或乙烯与α-烯烃的共聚物，所述氯化聚乙烯专用树脂粉末的粉料密度为0.945～0.960g/cm3，MFR5kg为0.1～10g/10min，平均粒径为100-300μm，S值为17-31，蜡含量≤0.5wt％。1. a special resin powder for chlorinated polyethylene, is characterized in that, the special resin powder for chlorinated polyethylene is the copolymer of polyethylene or ethylene and α-olefin, and the powder for the special resin powder for chlorinated polyethylene is The density is 0.945～0.960g/cm 3 , the MFR 5kg is 0.1～10g/10min, the average particle size is 100-300μm, the S value is 17-31, and the wax content is less than or equal to 0.5wt%. 2.根据权利要求1所述的氯化聚乙烯专用树脂粉末，其特征在于，所述α-烯烃为丙烯、丁烯-1、己烯-1、辛烯-1或4-甲基戊烯-1。2. The special resin powder for chlorinated polyethylene according to claim 1, wherein the α-olefin is propylene, butene-1, hexene-1, octene-1 or 4-methylpentene -1. 3.权利要求1或2所述的氯化聚乙烯专用树脂粉末的制备方法，其特征在于，乙烯和任选的α-烯烃在催化剂存在下在单一的淤浆聚合反应釜中通过淤浆聚合反应制得所述氯化聚乙烯专用树脂粉末，其中所述催化剂包括锑元素改性的负载型铬系催化剂，所述锑元素改性的负载型铬系催化剂的平均粒径优选为6-20μm；3. The preparation method of the special resin powder for chlorinated polyethylene according to claim 1 or 2, characterized in that, ethylene and optional α-olefin are polymerized by slurry in a single slurry polymerization reactor in the presence of a catalyst The special resin powder for chlorinated polyethylene is obtained by reaction, wherein the catalyst comprises a supported chromium-based catalyst modified with antimony element, and the average particle size of the supported chromium-based catalyst modified with antimony element is preferably 6-20 μm ; 优选的，相对于每克乙烯，所述锑元素改性的负载型铬系催化剂的加入量为0.02-2mg，优选0.03-0.2mg。Preferably, per gram of ethylene, the added amount of the antimony element-modified supported chromium-based catalyst is 0.02-2 mg, preferably 0.03-0.2 mg. 4.根据权利要求3所述的制备方法，其特征在于，所述催化剂还包括助催化剂，所述助催化剂为烷基铝，优选所述助催化剂为三乙基铝、三异丁基铝、乙氧基二乙基铝、一氯二乙基铝或甲基铝氧烷中的一种或多种，更优选三异丁基铝；4. preparation method according to claim 3 is characterized in that, described catalyst also comprises cocatalyst, described cocatalyst is alkyl aluminum, preferably described cocatalyst is triethylaluminum, triisobutylaluminum, One or more of ethoxydiethylaluminum, monochlorodiethylaluminum or methylaluminoxane, more preferably triisobutylaluminum; 优选的，相对于每毫克所述锑元素改性的负载型铬系催化剂，所述助催化剂的用量为0.01-10mL，优选0.05-1mL。Preferably, per milligram of the antimony element-modified supported chromium-based catalyst, the amount of the co-catalyst is 0.01-10 mL, preferably 0.05-1 mL. 5.根据权利要求3所述的制备方法，其特征在于，基于所述锑元素改性的负载型铬系催化剂的总重量，所述锑元素的负载量为0.01～5wt％，优选0.02～1wt％。5 . The preparation method according to claim 3 , wherein, based on the total weight of the antimony element-modified supported chromium-based catalyst, the loading amount of the antimony element is 0.01-5 wt %, preferably 0.02-1 wt %. 6 . %. 6.根据权利要求5所述的制备方法，其特征在于，所述锑元素改性的负载型铬系催化剂的制备步骤包括：6. The preparation method according to claim 5, wherein the preparation step of the antimony element-modified supported chromium-based catalyst comprises: 1)将负载型铬系催化剂置于管式炉中，通过气相沉积将锑化合物中的锑元素负载至所述负载型铬系催化剂上，经焙烧得到前驱体；1) placing the supported chromium-based catalyst in a tube furnace, loading the antimony element in the antimony compound onto the supported chromium-based catalyst by vapor deposition, and calcining to obtain a precursor; 2)步骤1)得到的所述前驱体在有机金属还原剂存在下进行还原反应，所得还原产物经干燥得到所述锑元素改性的负载型铬系催化剂。2) The precursor obtained in step 1) is subjected to a reduction reaction in the presence of an organometallic reducing agent, and the obtained reduction product is dried to obtain the antimony element-modified supported chromium-based catalyst. 7.根据权利要求6所述的制备方法，其特征在于，步骤1)在惰性气氛下进行所述气相沉积，惰性气体的流量为5～100mL/min，优选40～60mL/min；步骤1)中的反应温度为100～600℃，优选300～550℃；沉积时间为120～480min，优选180～300min；7. The preparation method according to claim 6, characterized in that, in step 1), the vapor deposition is carried out under an inert atmosphere, and the flow rate of the inert gas is 5-100 mL/min, preferably 40-60 mL/min; step 1) The reaction temperature is 100～600℃, preferably 300～550℃; the deposition time is 120～480min, preferably 180～300min; 步骤1)中，所述焙烧在惰性气体中进行，焙烧温度为300～1000℃，优选400～800℃，时间为1～10h，优选4～6h；或者，所述焙烧以低温阶段和高温阶段两个阶段进行，低温阶段在100～300℃进行，持续1～10小时，优选4～8小时，高温阶段在300～900℃进行，持续1～10小时，优选4～8小时；In step 1), the roasting is carried out in an inert gas, the roasting temperature is 300-1000°C, preferably 400-800°C, and the time is 1-10h, preferably 4-6h; or, the roasting is performed at a low temperature stage and a high temperature stage. Two stages are carried out, the low temperature stage is carried out at 100-300 ° C for 1 to 10 hours, preferably 4 to 8 hours, and the high temperature stage is carried out at 300 to 900 ° C for 1 to 10 hours, preferably 4 to 8 hours; 步骤2)中，在惰性气氛下进行所述还原反应，还原温度为20℃～100℃，优选20℃～70℃；还原时间为0.5～20小时，优选0.5～10小时。In step 2), the reduction reaction is carried out in an inert atmosphere, and the reduction temperature is 20°C to 100°C, preferably 20°C to 70°C; the reduction time is 0.5 to 20 hours, preferably 0.5 to 10 hours. 8.根据权利要求7所述的制备方法，其特征在于，步骤1)中，所述负载型铬系催化剂为Basell公司的Advent C催化剂；8. preparation method according to claim 7, is characterized in that, in step 1), described supported chromium series catalyst is the Advent C catalyst of Basell company; 和/或，步骤1)中，所述锑化合物选自三氧化二锑、五氧化二锑、三氯化锑、五氯化锑、锑酸钠、六氟锑酸钠、醋酸锑中的一种或多种，优选三氧化二锑；And/or, in step 1), the antimony compound is selected from one of antimony trioxide, antimony pentoxide, antimony trichloride, antimony pentachloride, sodium antimonate, sodium hexafluoroantimonate, and antimony acetate. One or more, preferably antimony trioxide; 和/或，步骤2)中，所述有机金属还原剂为三乙基铝、三异丁基铝、乙氧基二乙基铝、一氯二乙基铝或甲基铝氧烷中的一种或多种，优选乙氧基二乙基铝；优选的，以所述有机金属还原剂中的铝元素和所述负载型铬系催化剂中的铬元素计，铝/铬摩尔比优选为0.01～500，更优选0.1～50。And/or, in step 2), the organometallic reducing agent is one of triethylaluminum, triisobutylaluminum, ethoxydiethylaluminum, diethylaluminum monochloride or methylaluminoxane. one or more, preferably ethoxydiethylaluminum; preferably, based on the aluminum element in the organometallic reducing agent and the chromium element in the supported chromium-based catalyst, the aluminum/chromium molar ratio is preferably 0.01 ~500, more preferably 0.1 to 50. 9.根据权利要求3所述的制备方法，其特征在于，以烷烃溶剂为介质，在所述催化剂存在下于单一的淤浆反应釜中进行所述淤浆聚合反应；9. The preparation method according to claim 3, characterized in that, using an alkane solvent as a medium, in the presence of the catalyst, the slurry polymerization reaction is carried out in a single slurry reactor; 所述淤浆聚合反应的反应温度为70-85℃，反应压力为0.5-1.5MPa之间，氢气和乙烯的摩尔比为0.01-1，α-烯烃和乙烯的摩尔比为0-0.1；The reaction temperature of the slurry polymerization reaction is 70-85 DEG C, the reaction pressure is between 0.5-1.5MPa, the molar ratio of hydrogen and ethylene is 0.01-1, and the molar ratio of α-olefin and ethylene is 0-0.1; 优选的，所述烷烃溶剂为丁烷、戊烷、正己烷或庚烷中的一种或多种。Preferably, the alkane solvent is one or more of butane, pentane, n-hexane or heptane. 10.权利要求1-9任一项所述的氯化聚乙烯专用树脂粉末在氯化聚乙烯制备工艺中应用。10. The application of the special resin powder for chlorinated polyethylene according to any one of claims 1 to 9 in the preparation process of chlorinated polyethylene.
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CN104284912A (en) * 2013-04-19 2015-01-14 Lg化学株式会社 Polyethylene with controlled wax content, chlorinated polyethylene thereof, and molded product prepared therefrom
CN104513333A (en) * 2013-09-27 2015-04-15 中国石油化工股份有限公司 Easily processable high-density polyethylene resin used for chlorinated polyethylene and preparing method thereof
CN106699946A (en) * 2015-07-23 2017-05-24 中国石化扬子石油化工有限公司 High-density polyethylene resin, and preparation method and application thereof

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1359396A (en) * 1999-07-15 2002-07-17 陶氏化学公司 High density ethylene homopolymers and blend compositions
CN104284912A (en) * 2013-04-19 2015-01-14 Lg化学株式会社 Polyethylene with controlled wax content, chlorinated polyethylene thereof, and molded product prepared therefrom
CN104513333A (en) * 2013-09-27 2015-04-15 中国石油化工股份有限公司 Easily processable high-density polyethylene resin used for chlorinated polyethylene and preparing method thereof
CN106699946A (en) * 2015-07-23 2017-05-24 中国石化扬子石油化工有限公司 High-density polyethylene resin, and preparation method and application thereof

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