CN115260347A - Production system and method of polypropylene with high isotacticity - Google Patents
Production system and method of polypropylene with high isotacticity Download PDFInfo
- Publication number
- CN115260347A CN115260347A CN202211061206.6A CN202211061206A CN115260347A CN 115260347 A CN115260347 A CN 115260347A CN 202211061206 A CN202211061206 A CN 202211061206A CN 115260347 A CN115260347 A CN 115260347A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- unit
- polypropylene
- powder
- prepolymerization
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- 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
- C08F110/04—Monomers containing three or four carbon atoms
- C08F110/06—Propene
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M50/00—Constructional details or processes of manufacture of the non-active parts of electrochemical cells other than fuel cells, e.g. hybrid cells
- H01M50/40—Separators; Membranes; Diaphragms; Spacing elements inside cells
- H01M50/403—Manufacturing processes of separators, membranes or diaphragms
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M50/00—Constructional details or processes of manufacture of the non-active parts of electrochemical cells other than fuel cells, e.g. hybrid cells
- H01M50/40—Separators; Membranes; Diaphragms; Spacing elements inside cells
- H01M50/409—Separators, membranes or diaphragms characterised by the material
- H01M50/411—Organic material
- H01M50/414—Synthetic resins, e.g. thermoplastics or thermosetting resins
- H01M50/417—Polyolefins
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Manufacturing & Machinery (AREA)
- Health & Medical Sciences (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Abstract
The invention provides a production system of polypropylene with high isotacticity, which is sequentially connected with the following process units in series: the device comprises a catalyst prepolymerization unit, a catalyst washing unit, at least one liquid phase body reaction kettle, an active polymer powder treatment unit, at least one gas phase fluidized bed reactor, a degassing bin unit and a drying bin unit. According to the invention, the washing pretreatment of the prepolymerized catalyst and the intermediate treatment of active powder in the polymerization process are added in the traditional Hypol polypropylene process, so that the elimination of low isotactic component and fine powder component is realized, the production of high isotactic low ash polypropylene is realized, and the stability and consistency of product performance can be ensured by industrial continuous production; the film product prepared by the material has relatively high melting point, better film puncture strength, less surface crystal points and gel after film forming.
Description
Technical Field
The invention relates to the technical field of polypropylene preparation, in particular to a production process technology of polypropylene with high isotacticity characteristics.
Background
The lithium ion battery is one of the key components of the current energy storage product, wherein one of the key materials for separating the positive electrode and the negative electrode of the battery and ensuring the stable operation of the battery is a diaphragm, the diaphragm material produced in large scale is a wet-process polyethylene diaphragm, the diaphragm is produced by using a solvent, the dissolving capacity of the solvent can be used, and unnecessary large particles and low molecular components in the product are separated by mechanical force such as filtration or centrifugal separation, but the existence of the solvent causes the production process to be slow, the solvent recovery treatment cost is high, and the lithium ion battery is not more and more suitable for the requirements of safety and environmental protection; meanwhile, compared with a polypropylene product, the melting point of polyethylene is low, and after the polyethylene is made into a battery, the diaphragm can be quickly melted through after the heat release phenomenon occurs, so that the risk of fire is caused. In contrast, the melting point of polypropylene is at least 20 ℃ higher than that of polyethylene, and the reaction treatment time can be left for a user by matching with an efficient temperature control alarm system, so that the safety level is essentially improved.
At present, new polypropylene devices are more and more built in China, but a loop pipe process or a fluidized bed process is mostly selected, the new polypropylene devices are characterized in that a single kettle is large in yield, short in flow, small in occupied space and few in power equipment, the traditional Hypol process devices in China only comprise early introduction devices such as Lanzhou petrochemical, daqing petrochemical, yanshan petrochemical and the like, and particularly after the devices are improved by Japan three-well companies, the original combined process of a reaction kettle and a fluidized bed is evolved into a loop pipe and fluidized bed process, the new devices are not built any more. The process flow is long, the reaction unit and other auxiliary units are arranged in parallel, the occupied area is large, the number of the tank towers is large, the number of the mobile devices is large, the material residence time is long, the polymerization is sufficient, the catalyst pretreatment unit is arranged, the production of high-rigidity products is facilitated, and the production of high-specification products can be realized by matching with a novel external electron donor.
Disclosure of Invention
The invention aims to provide a production method and a system of high isotacticity polypropylene, so as to realize the production of high isotacticity polypropylene products with low ash content, high rigidity, narrow particle size distribution and high relative molecular mass.
The invention is realized by adopting the following technical scheme:
the invention provides a production system of polypropylene with high isotacticity, which is sequentially connected in series with the following process units: the device comprises a catalyst prepolymerization unit, a catalyst washing unit, at least one liquid phase body reaction kettle, an active polymer powder treatment unit, at least one gas phase fluidized bed reactor, a degassing bin unit and a drying bin unit.
The catalyst prepolymerization unit is used for prepolymerization reaction of propylene and a catalyst.
And the catalyst washing unit is used for removing fine powder, a low isotactic part and a small amount of catalyst shedding carriers formed after prepolymerization, and pressurizing and injecting a washed catalytic system into the first liquid-phase bulk reaction kettle.
The liquid phase body reaction kettle is used for realizing the liquid phase body polymerization reaction of propylene, and preferably two liquid phase body reaction kettles are connected in series.
The active polymer powder treatment unit aims to remove a small amount of low isotacticity polymer and propylene liquid phase bulk in the liquid phase bulk polymerization reaction product. The active polymer powder treatment unit consists of a filtering mechanism and/or a cyclone separating mechanism.
The gas-phase fluidized bed reactor is mainly used for further realizing the synthesis of polypropylene with required molecular weight, and certainly can also realize the copolymerization of propylene, ethylene and the like, thereby realizing the switching of different polypropylene grades. The addition of ethylene is optional and is not an essential component of the target product of the present invention. Preferably two gas phase fluidized bed reactors are connected in series.
The degassing bin unit and the drying bin unit are respectively used for removing unreacted monomers and drying powder; the powder inactivation storage unit is treated by nitrogen containing a small amount of water vapor to sufficiently remove the activity of the unconsumed cocatalyst.
The inventor unexpectedly finds that the elimination of low isotactic component and fine powder component is realized by adding a pretreatment unit of prepolymerized catalyst and an intermediate treatment unit of active powder in the polymerization process in the traditional Hypol polypropylene process, and a high-activity catalytic system is matched, so that compared with the original process, the production of high-isotacticity low-ash polypropylene can be realized, and the stable and consistent product performance can be ensured by industrial continuous production. The present inventors have completed the present invention based on the above findings.
Preferably, hydrogen is used to adjust the relative molecular mass of the product in the liquid phase bulk reactor and/or the gas phase fluidized bed reactor.
And a processing aid metering and feeding unit and a granulating unit can be sequentially connected in series after the powder inactivation storage unit.
The invention also provides a production method of the polypropylene with high isotacticity, which comprises the following steps:
s1, injecting a catalyst, a cocatalyst and an external electron donor into a catalyst prepolymerization reaction kettle (namely a catalyst prepolymerization unit), wherein the temperature of the catalyst prepolymerization reaction kettle is 5-15 ℃, polymer-grade propylene is injected into the catalyst prepolymerization reaction kettle in a liquid-phase bulk form to perform prepolymerization reaction, and the pressure is controlled to be 3.0-3.6Mpa;
s2, after prepolymerization, enabling the catalytic system to enter a catalyst washing unit, removing fine powder, a low isotactic part and a small amount of catalyst shedding carriers formed after prepolymerization, and pressurizing and injecting the washed catalytic system into a first liquid-phase body reaction kettle;
s3, controlling the total pressure of the first liquid phase body reaction kettle to be 2.9-3.3Mpa, controlling the average retention time of materials to be 40-80min, and controlling the material level to be 35-75%;
s4, sequentially feeding the polymerization materials into a second liquid-phase body reaction kettle for continuous polymerization, controlling the total pressure of the second liquid-phase body reaction kettle to be 2.5-2.8Mpa, controlling the average retention time of the materials to be 40-80min, and controlling the material level to be 35-75%;
s5, the polymer material enters an active polymer powder treatment unit, a small amount of low-isotacticity polymer is dissolved or swelled in liquid-phase propylene, and the liquid-phase propylene containing the low-isotacticity polymer is removed and separated through filtration and cyclone separation;
s6, sequentially feeding the treated polymerization powder into a first gas-phase fluidized bed reactor and a second gas-phase fluidized bed reactor for continuous reaction, controlling the total pressure to be 1.9-2.4MPa and 1.4-1.8MPa respectively, and controlling the average residence time of the materials to be 45-90min;
and S7, feeding the powder discharged from the second gas-phase fluidized bed reactor into a degassing tower (namely a degassing bin unit) and a drying tower (namely a drying bin unit), removing unreacted monomers, then feeding the powder into an inactivation treatment unit, and treating the powder by using nitrogen containing a small amount of water vapor so as to fully remove the activity of the unconsumed cocatalyst and finally obtain the high isotacticity polypropylene powder.
In step S1, the degree of prepolymerization is controlled to be 5 to 50, preferably 15 to 35. The ratio (molar ratio) of the total amount of propylene added to the catalyst prepolymerization reactor to the total amount of the catalyst was defined as the degree of prepolymerization.
In step S1, the catalyst, cocatalyst and external electron donor are used in the following amounts: the molar ratio of cocatalyst to catalyst is 10-200, preferably 30-80:1; the molar ratio of external electron donor to catalyst is 5-30, preferably 8-20.
Preferably, the catalyst uses active Ti as a catalytic center, and uses ether or ester compounds as an internal electron donor, including but not limited to cyclobutyl-1, 1-dimethanol dimethyl ether, 1, 3-diethers, 1, 3-propylene glycol dimethyl ether, 2-diisobutyl-1, 3-propylene glycol dimethyl ether, cyclopentyl-1, 1-dimethanol dimethyl ether, 1, 3-diol ester compounds, di-n-butyl phthalate, diisobutyl phthalate, ethyl benzoate, dibutyl phthalate, etc., preferably, the internal electron donor is a catalyst of ether compounds, and a mixture of ether and ester compounds can also be used.
The cocatalyst includes but is not limited to aluminum organyls such as triethylaluminum, triisobutylaluminum, diisoylaluminum monochloride, etc., preferably triethylaluminum.
The external electron donor includes, but is not limited to, phenyltriethoxysilane, diphenyldimethoxysilane, diisobutyldimethoxysilane, dicyclopentyldimethoxysilane, diisopropyldimethoxysilane, isopropylisobutyldimethoxysilane, cyclopentylisobutyldimethoxysilane, cyclohexylmethyldimethoxysilane, etc., preferably diisobutyldimethoxysilane, dicyclopentyldimethoxysilane.
In step S3, according to the characteristics of the final product, ethylene can be used for regulating the melting point and the crystallization temperature, hydrogen can be used for regulating MFR, the relative molecular mass and the distribution thereof, and the blanking program is controlled by the polymerization material level, wherein the material level is preferably controlled to be 50-55%.
In step S4, the second liquid-phase bulk reaction kettle can be supplemented or not supplemented with ethylene and/or hydrogen, and the blanking program is controlled through the polymerization material level, wherein the material level is preferably controlled to be 50-55%.
In step S6, the first gas-phase fluidized-bed reactor and the second gas-phase fluidized-bed reactor may or may not be supplemented with ethylene and/or hydrogen, and further adjust the physical properties of the product, such as melting point, crystallization temperature, MFR, relative molecular mass and distribution thereof.
Preferably, the polypropylene powder with high isotacticity can be further added with an auxiliary agent and then enters a granulator for granulation.
The invention also provides application of the high isotacticity polypropylene prepared by the method in preparation of a lithium battery diaphragm.
The high isotacticity polypropylene prepared by the method has good crystallization property, and products prepared from the raw materials generally have good rigidity and high glass transition temperature, so that the good dimensional stability of the products can be realized when the products are heated and sterilized in boiling water; meanwhile, the polypropylene with high isotacticity also has the characteristic of low ash content, and a film product prepared by adopting the material has relatively high melting point, better film puncture strength and fewer surface crystal points and gels after film formation.
The invention is further explained by the following combined with the drawings and the embodiments.
Drawings
FIG. 1 is a schematic view of the process of the present invention.
Detailed Description
The following description is presented to disclose the invention so as to enable any person skilled in the art to practice the invention. The preferred embodiments described below are intended as examples only and are not intended to limit the scope of the invention, as other obvious modifications will occur to those skilled in the art. The basic principles of the invention, as defined in the following description, may be applied to other embodiments, variations, modifications, equivalents, and other technical solutions without departing from the spirit and scope of the invention.
The instruments, industrial equipment or reagents in the examples of the present invention are not specified by manufacturers, and are all conventional commercial instruments, industrial equipment or reagents. Wherein the propylene adopts polymer grade propylene.
As shown in FIG. 1, the production system of high isotacticity polypropylene of the present invention is serially connected with the following process units in sequence: the device comprises a catalyst prepolymerization unit, a catalyst washing unit, a first liquid-phase body reaction kettle, a second liquid-phase body reaction kettle, an active polymer powder treatment unit, a first gas-phase fluidized bed reactor, a second gas-phase fluidized bed reactor, a degassing bin unit, a drying bin unit, a powder inactivation storage unit, a processing aid metering and feeding unit and a granulation unit. Wherein the processing agent metering and feeding unit and the granulating unit are optional units, and can also be directly packaged in a powder form.
Of course, it is known in the art that a catalyst configuration unit, a propylene refining unit, and optionally a hydrogen production system, a material transfer system, etc. during the polymerization process are required before the catalyst prepolymerization unit. The combination of the process units can be performed by those skilled in the art according to the actual needs, and the process units themselves, the connection mode between them and the process units provided by the present invention, the process parameters, etc. can all adopt the conventional means in the art, and the present invention is not described in detail.
The production method of the polypropylene with high isotacticity comprises the following steps:
s1, injecting a catalyst, a cocatalyst and an external electron donor into a catalyst prepolymerization reaction kettle (namely a catalyst prepolymerization unit), wherein the temperature of the catalyst prepolymerization reaction kettle is 5-15 ℃, polymer-grade propylene is injected into the catalyst prepolymerization reaction kettle in a liquid-phase bulk form to perform prepolymerization reaction, and the pressure is controlled to be 3.0-3.6Mpa;
s2, after prepolymerization, enabling the catalytic system to enter a catalyst washing unit, removing fine powder, a low isotactic part and a small amount of catalyst shedding carriers formed after prepolymerization, and pressurizing and injecting the washed catalytic system into a first liquid-phase body reaction kettle;
s3, the average residence time of the materials in the first liquid phase bulk reaction kettle is 40-80min;
s4, sequentially feeding the polymerization materials into a second liquid-phase body reaction kettle for continuous polymerization, wherein the average retention time of the materials in the second liquid-phase body reaction kettle is 40-80min;
s5, the polymer material enters an active polymer powder treatment unit, a small amount of low-isotacticity polymer is dissolved or swelled in liquid-phase propylene, and the liquid-phase propylene containing the low-isotacticity polymer is removed and separated through filtration and cyclone separation;
s6, sequentially feeding the treated polymerized powder into a first gas-phase fluidized bed reactor and a second gas-phase fluidized bed reactor for continuous reaction, wherein the average material retention time is 45-90min;
and S7, feeding the powder discharged from the second gas-phase fluidized bed reactor into a degassing tower (namely a degassing bin unit) and a drying tower (namely a drying bin unit), removing unreacted monomers, then feeding the powder into an inactivation treatment unit, and treating the powder by using nitrogen containing a small amount of water vapor so as to fully remove the activity of the unconsumed cocatalyst and finally obtain the high isotacticity polypropylene powder.
The process parameters of the polymerization section are shown in table 1:
TABLE 1 Process parameters of the reactor section
| Polymerized units | Temperature of | Pressure Mpa | The material level% |
| First liquid phase body reaction kettle | 70±1.0 | 2.9-3.2 | 45-65 |
| A second liquid phaseBody reaction kettle | 68±1.0 | 2.5-2.8 | 45-65 |
| First gas phase fluidized bed reactor | 84±1.0 | 2.1-2.4 | 45-75 |
| Second gas-phase fluidized-bed reactor | 80±1.0 | 1.6-2.0 | 45-75 |
Example 1
The catalyst is a Z-N catalyst containing a lipid internal electron donor, triethyl aluminum is used as a cocatalyst, diisobutyldimethoxysilane is used as an external electron donor, the Al/Si/Ti molar ratio is 75/9/1, the prepolymerization temperature is 8 ℃, and the prepolymerization degree is 10.
Example 2
The catalyst is a Z-N catalyst containing an ether internal electron donor, aluminum triethyl is matched as a cocatalyst, diisobutyldimethoxysilane is used as an external electron donor, the molar ratio of Al/Si/Ti is 70/8/1, the prepolymerization temperature is 10 ℃, and the degree of prepolymerization is 10 ℃.
Example 3
The catalyst is a Z-N catalyst containing an ether internal electron donor, aluminum triethyl is matched as a cocatalyst, dicyclopentyldimethoxysilane silane is used as an external electron donor, the molar ratio of Al/Si/Ti is 70/9/1, the prepolymerization temperature is 12 ℃, and the degree of polymerization in advance is 15.
Comparative example 1
The same procedure as in example 1 was repeated except that the catalyst washing unit and the corresponding catalyst washing step S2 were not employed.
Comparative example 2
The same procedure as in example 1 was repeated except that the catalyst washing unit and the corresponding catalyst washing step S2 were not used, and the living polymer powder treating unit and the corresponding living powder treating step S5 were not used.
The powder products obtained in the respective examples and comparative examples were granulated by adding antioxidants 1010, 168 and zinc stearate (addition amount is 2500ppm, ratio is 1:
table 2 sample test results 1
Table 3 sample test results 2
Wherein, MFR is tested according to GB/T3682.1-2018, tensile strength is tested according to GB/T1040.2-2006, flexural modulus and flexural strength are tested according to GB/T9341-2008, normal temperature impact strength is tested according to GB/T1043.1-2008, ash is tested according to GB/T9345.1-2008, melting point and crystallization temperature are tested according to GB/T19466.3-2004, and isotacticity is tested according to GB/T2412-2008.
Gel Permeation Chromatography (GPC) analysis: the measurement was carried out by means of a gel permeation chromatograph model PL-220 (1, 2, 4-trichlorobenzene as a solvent, at a leaching temperature of 150 ℃ and a flow rate of 1.0 mL/min) from Polymer Laboratories, inc., U.S.A.
As can be seen from the detection data in tables 1 and 2, the polypropylene material prepared by the method and the production system of the invention has the advantages that the isotacticity is improved by 12.8-14.1% compared with the comparative example, the ash content is reduced by 44.4-83.3% compared with the comparative example, the molecular weight distribution is narrow, the mechanical strength is improved in different degrees, unexpected technical effects are generated, a catalyst washing unit and a corresponding catalyst washing step, an active polymer powder treatment unit and a corresponding active powder treatment step are shown, and the polypropylene material has the effects of unexpectedly and remarkably improving the isotacticity and reducing the ash content. Therefore, the invention is suitable for preparing lithium battery diaphragm products, and has relatively high melting point, better membrane puncture strength, less surface crystal points and gel after membrane formation.
It will be appreciated by persons skilled in the art that the embodiments of the invention described above and shown in the drawings are given by way of example only and are not limiting of the invention. The objects of the present invention have been fully and effectively accomplished. The functional and structural principles of the present invention have been shown and described in the examples, and any variations or modifications of the embodiments of the present invention may be made without departing from the principles.
Claims (10)
1. The production system of the polypropylene with high isotacticity is characterized in that the following process units are sequentially connected in series: the device comprises a catalyst prepolymerization unit, a catalyst washing unit, at least one liquid phase body reaction kettle, an active polymer powder treatment unit, at least one gas phase fluidized bed reactor, a degassing bin unit and a drying bin unit.
2. The production system of higher isotacticity polypropylene according to claim 1, wherein the active polymer powder treatment unit is comprised of a filtration mechanism and/or a cyclone separation mechanism.
3. The system for producing higher isotacticity polypropylene according to claim 1 or 2, wherein a powder inactivation storage unit, a processing agent metering and feeding unit and a granulation unit are further connected in series after the drying bin unit.
4. The production method of the polypropylene with high isotacticity is characterized by comprising the following steps:
s1, injecting a catalyst, a cocatalyst and an external electron donor into a catalyst prepolymerization reaction kettle, wherein the temperature of the catalyst prepolymerization reaction kettle is 5-15 ℃, and polymer-grade propylene is injected into the catalyst prepolymerization reaction kettle in a liquid-phase bulk form to carry out prepolymerization reaction, and the pressure is controlled at 3.0-3.6Mpa;
s2, after prepolymerization, enabling the catalytic system to enter a catalyst washing unit, removing fine powder, a low isotactic part and a small amount of catalyst shedding carriers formed after prepolymerization, and pressurizing and injecting the washed catalytic system into a first liquid-phase body reaction kettle;
s3, controlling the first liquid phase body reaction kettle to be under the total pressure of 2.9-3.3Mpa, controlling the average material retention time to be 40-80min, and controlling the material level to be 35-75%;
s4, enabling the polymerization materials to sequentially enter a second liquid-phase body reaction kettle for continuous polymerization, controlling the second liquid-phase body reaction kettle to be under the total pressure of 2.5-2.8Mpa, controlling the average retention time of the materials to be 40-80min, and controlling the material level to be 35-75%;
s5, the polymer material enters an active polymer powder treatment unit, a small amount of low-isotacticity polymer is dissolved or swelled in liquid-phase propylene, and the liquid-phase propylene containing the low-isotacticity polymer is removed and separated through filtration and cyclone separation;
s6, sequentially feeding the treated polymerization powder into a first gas-phase fluidized bed reactor and a second gas-phase fluidized bed reactor for continuous reaction, controlling the total pressure to be 1.9-2.4MPa and 1.4-1.8MPa respectively, and controlling the average residence time of the materials to be 45-90min;
and S7, feeding the powder discharged from the second gas-phase fluidized bed reactor into a degassing tower and a drying tower to remove unreacted monomers, then feeding the powder into an inactivation treatment unit, and treating the powder by using nitrogen containing a small amount of water vapor so as to fully remove the activity of the unconsumed cocatalyst and finally obtain the high isotacticity polypropylene powder.
5. The method according to claim 4, wherein in step S1, the degree of prepolymerization is controlled to be in the range of 5 to 50; the molar ratio of the cocatalyst to the catalyst is 10-200:1; the molar ratio of the external electron donor to the catalyst is 5-30.
6. The method according to claim 4, wherein in step S1, the degree of prepolymerization is controlled to be in the range of 35 to 45; the molar ratio of the cocatalyst to the catalyst is 50-125:1; the molar ratio of the external electron donor to the catalyst is 8-15.
7. The method of claim 4, wherein the catalyst is characterized in that active Ti is used as a catalytic center, and an ether or ester compound is used as an internal electron donor; the cocatalyst is selected from at least one of triethyl aluminum, triisobutyl aluminum and chlorodiisopropyl aluminum; the external electron donor is at least one selected from the group consisting of phenyltriethoxysilane, diphenyldimethoxysilane, diisobutyldimethoxysilane, dicyclopentyldimethoxysilane, diisopropyldimethoxysilane, isopropylisobutyldimethoxysilane, cyclopentylisobutyldimethoxysilane, and cyclohexylmethyldimethoxysilane.
8. The method of claim 7, wherein the internal electron donor is an ether compound.
9. An isotactic polypropylene produced by the process of any one of claims 1 to 8.
10. Use of the highly isotactic polypropylene produced by the process defined in any one of claims 1 to 8 in the production of lithium battery separators.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211061206.6A CN115260347B (en) | 2022-08-31 | 2022-08-31 | Production system and method of high-isotacticity polypropylene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211061206.6A CN115260347B (en) | 2022-08-31 | 2022-08-31 | Production system and method of high-isotacticity polypropylene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115260347A true CN115260347A (en) | 2022-11-01 |
| CN115260347B CN115260347B (en) | 2023-07-21 |
Family
ID=83754921
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211061206.6A Active CN115260347B (en) | 2022-08-31 | 2022-08-31 | Production system and method of high-isotacticity polypropylene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115260347B (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07157525A (en) * | 1993-12-10 | 1995-06-20 | Ube Ind Ltd | Production of propylene block copolymer |
| US20090149610A1 (en) * | 2007-12-11 | 2009-06-11 | Sumitomo Chemocal Company, Limited | Olefin polymerization reactor, polyolefin production system, and polyolefin production process |
| CN113621096A (en) * | 2021-07-06 | 2021-11-09 | 雷剑兰 | Ultra-low ash polyolefin, preparation method and application |
-
2022
- 2022-08-31 CN CN202211061206.6A patent/CN115260347B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07157525A (en) * | 1993-12-10 | 1995-06-20 | Ube Ind Ltd | Production of propylene block copolymer |
| US20090149610A1 (en) * | 2007-12-11 | 2009-06-11 | Sumitomo Chemocal Company, Limited | Olefin polymerization reactor, polyolefin production system, and polyolefin production process |
| CN113621096A (en) * | 2021-07-06 | 2021-11-09 | 雷剑兰 | Ultra-low ash polyolefin, preparation method and application |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115260347B (en) | 2023-07-21 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA1265646A (en) | PROCESS FOR THE START UP OF POLYMERISATION OR COPOLYMERISATION IN THE GAS PHASE OF .alpha.-OLEFINS IN THE PRESENCE OF A ZIEGLER-NATTA CATALYST SYSTEM | |
| CN102030841B (en) | Gas-phase polymerization of propylene | |
| CN109563191B (en) | Process for the manufacture of heterophasic propylene polymer materials | |
| WO2019090884A1 (en) | Polymerization process of impact polypropylene | |
| WO2019090883A1 (en) | Method for preparing polypropylene or propylene-ethylene copolymer | |
| CN108192005B (en) | Polyolefin and preparation method thereof | |
| CA1115683A (en) | Preparation of solid titanium trichloride and propylene polymers using same | |
| CN113845613B (en) | High-purity ultrahigh molecular weight polyethylene resin and production process thereof | |
| KR101590998B1 (en) | Process and apparatus for continuous solution polymerization of olefins | |
| US20220220233A1 (en) | Suspension process for preparing ethylene polymers comprising work-up of the suspension medium | |
| CN115260347B (en) | Production system and method of high-isotacticity polypropylene | |
| CN114478888B (en) | Polyolefin elastomer and preparation method thereof | |
| CN109666092B (en) | Production process of special material for polypropylene lithium battery membrane | |
| JPS5830887B2 (en) | Method for purifying highly crystalline polyolefin | |
| JPH07286004A (en) | Continuous production of polyolefin | |
| US20220227903A1 (en) | Suspension process for preparing ethylene polymers comprising drying of the polymer particles | |
| CN112457436A (en) | High-melt index polypropylene and preparation method thereof | |
| JP3973248B2 (en) | Capacitor insulation film | |
| CN112876591A (en) | Industrial production method of polypropylene resin for battery diaphragm | |
| CN113817083B (en) | Temperature-sensitive ultrahigh molecular weight polyethylene catalyst, preparation method and application thereof | |
| JPS6369809A (en) | Polymerization of propylene | |
| CN114316110B (en) | Propylene-butene random copolymer production system and preparation method | |
| CN111465624A (en) | Polypropylene and preparation method thereof | |
| JPH0432085B2 (en) | ||
| CN112625156B (en) | Polypropylene preparation method suitable for gas phase polymerization process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |