CN110016092B

CN110016092B - Method for continuously preparing polyolefin and polyolefin prepared by method

Info

Publication number: CN110016092B
Application number: CN201810016257.4A
Authority: CN
Inventors: 李化毅
Original assignee: Institute of Chemistry CAS
Current assignee: Institute of Chemistry CAS
Priority date: 2018-01-08
Filing date: 2018-01-08
Publication date: 2021-01-26
Anticipated expiration: 2038-01-08
Also published as: CN110016092A

Abstract

The invention discloses a method for continuously preparing polyolefin, in particular to a method for continuously preparing polyolefin elastomer or a mixture thereof and the polyolefin prepared by the method. The preparation process adopts a kettle type reactor for prepolymerization, which has the function of improving the viscosity of a reaction system so as to facilitate the subsequent operation of a screw reactor; in the preparation process, a static mixer is adopted for static mixing polymerization, and is used for continuously increasing the viscosity of the system and prolonging the reaction residence time; in the preparation process, a reactive screw extruder is adopted for extrusion polymerization, so that the polymerization reaction under high conversion rate and high viscosity is realized. The preparation process can be suitable for various types of polyolefins, and is particularly suitable for the preparation of polyolefin elastomers or mixtures thereof.

Description

Method for continuously preparing polyolefin and polyolefin prepared by method

Technical Field

The invention belongs to the technical field of polyolefin material preparation, and particularly relates to a method for continuously preparing polyolefin and the polyolefin prepared by the method, in particular to a method for continuously preparing polyolefin elastomer or a mixture of the polyolefin elastomer and a product prepared by the method.

Background

Polyolefin elastomers are widely used mainly as adhesives, hot melt adhesives, ink additives, waterproof rolls, toughening materials and the like, wherein the toughening material is a main use mode of modified polypropylene or polyethylene. Polyolefin elastomers are generally copolymers of two or more olefins with low or no melting point and low glass transition temperature.

Polyolefin plastics, such as typical high density polyethylene, linear low density polyethylene, isotactic polypropylene, etc., can be produced by liquid phase bulk polymerization, gas phase polymerization, slurry polymerization, etc., such as Unipol process, Spheripol process, Novolene process, etc., olefin gas is converted into polymer particles under the catalysis of a coordination catalyst, the polymerization temperature is generally between 60 and 90 ℃, in this temperature range, the polymer particles keep shapes in a reactor and do not stick to the reactor, and the polymer is discharged out of the reactor in the form of particles.

However, in the case of polypropylene elastomers, when the polymerization temperature is between 60 ℃ and 90 ℃, the resulting polymer is sticky, the morphology cannot be maintained, the reactor is severely clogged, and continuous production cannot be achieved. The optimum polymerization temperature of the existing catalyst systems cannot be lowered. Therefore, to meet the characteristics of polyolefin elastomers, new continuous process reactors must be developed.

Reactive extrusion is a new polymerization method, and U.S. Pat. No. 5, 4,058,654 (1977) reports that random polybutene-1 material is prepared by reactive extrusion technology, the catalytic system is metal alkyl or titanium catalyst-aluminum alkyl cocatalyst, the polymerization residence time disclosed in the patent is difficult to reach the requirement of butene-1 catalytic polymerization, and therefore, no subsequent industrial application report about the patent technology is found. The U.S. Pat. No. 5,644,007 discloses a process for polymerizing alpha-olefins by plug flow reaction, but in the examples of the above patents, liquid olefins such as octene or hexene are mainly used as monomers, while gaseous monomers such as ethylene, propylene and butene are avoided, so that it can be seen that the above polymerization process conditions are still very incomplete and need to be improved. CN102190832A discloses a method for preparing polybutene-1 material by an extrusion process, but the method has the defects of unreasonable prepolymerization feeding mode, no stirring, difficult discharging and small process application range.

Disclosure of Invention

In order to solve the disadvantages of the prior art, it is an object of the present invention to provide a process for the continuous preparation of polyolefins, in particular of polyolefin elastomers or mixtures thereof.

It is another object of the present invention to provide a polyolefin, in particular a polyolefin elastomer or a mixture thereof, obtainable by the above process.

It is a further object of the present invention to provide a system for the above preparation method.

The purpose of the invention is realized by the following technical scheme:

the first aspect of the present invention provides a process for continuously preparing a polyolefin, in particular a polyolefin elastomer or a mixture thereof, comprising a prepolymerization, a static mixing polymerization and a screw extrusion polymerization, which comprises the steps of:

s1, prepolymerization: continuously adding reaction materials from the bottom of the kettle type reactor, and continuously increasing the material level of the materials under the conditions of temperature control and stirring to reach the material discharging level; the reaction materials comprise a polymerization monomer, a catalyst system, a molecular weight regulator, a polymerization regulator and a solvent;

s2, static mixing polymerization: after the reaction material in the step S1 is discharged, sending the reaction material into a static mixer for continuous reaction, and continuously increasing the material level of the material to reach the discharge material level under the condition of controlling the temperature; optionally, supplementing at least one of a polymerization monomer, a molecular weight regulator, a polymerization regulator and a solvent as required;

s3, screw extrusion polymerization: after the reaction material obtained in the step S2 is discharged, feeding the reaction material into a reactive screw extruder to continue reacting; optionally, at least one of the polymerization monomer, the molecular weight regulator, the polymerization regulator and the solvent is additionally added as necessary.

According to the invention, the method further comprises the steps of:

s4, devolatilizing: after the reaction material in the step S3 is discharged, feeding the reaction material into a devolatilization device for devolatilization treatment;

s5, extruding and granulating: and (S4) discharging the reaction material, conveying the discharged reaction material into a granulating screw extruder, and extruding and granulating to obtain polyolefin, particularly a polyolefin elastomer or a mixture thereof.

According to the invention, in step S1, the tank reactor is a stirred tank reactor, and the stirred tank reactor is a single-layer stirred tank reactor or a multilayer stirred tank reactor. The heat in the kettle type reactor is fed in or taken out through a jacket or a built-in coil, and the transmission medium of the heat is water or heat conducting oil.

According to the present invention, in step S1, it is understood by those skilled in the art that parameters such as the capacity and the stirring power of the tank reactor are not particularly limited and may be adjusted according to the polymerization process and the polymerization conditions.

According to the present invention, in step S1, the pre-polymerization is performed in 1 or more stages depending on the viscosity of the material, the monomer conversion rate, the residence time and/or the polymer structure, and in case of multiple stages, the material is transferred between each stage using a transfer pump.

According to the invention, in step S2, the static mixer is preferably a tubular static mixer; it will be understood by those skilled in the art that the length and diameter of the static mixer are not particularly limited and may be adjusted according to the polymerization process and polymerization conditions.

According to the present invention, at least one of the polymerization monomer, the molecular weight modifier, the polymerization modifier and the solvent is additionally added in step S2 depending on the polymerization process and the polymerization conditions, and the additional addition position may be set to one or more depending on the length of the static mixer.

According to the present invention, in step S2, the static mixer is 1 stage or more depending on the viscosity of the material, the monomer conversion rate, the residence time and/or the polymer structure, and if it is a plurality of stages, the material is transferred between the stages using a transfer pump.

According to the invention, in step S2, the reaction mass output of step S1 is preferably fed to a static mixer via a transfer pump.

According to the present invention, in step S3, the reactive screw extruder is preferably a single screw extruder or a twin screw extruder or a hybrid configuration of a single screw and a twin screw extruder; it will be understood by those skilled in the art that the length and diameter of the reactive screw extruder are not particularly limited and may be adjusted according to the polymerization process and polymerization conditions; illustratively, the single-screw extruder or the twin-screw extruder is selected to have an aspect ratio (ratio of the length L of the screw extruder to the diameter D) as large as possible under the conditions allowed by the mechanical manufacturing and process, for example, the aspect ratio (L/D) > 35 of the single-screw extruder and the aspect ratio (L/D) > 50 of the twin-screw extruder are selected to increase the residence time in the screw extruder during polymerization of the polymerization monomers; the screw extruder is exemplarily selected from a screw extruder with cooling water and an electric heating jacket, and the screw rotating speed of the screw extruder can be adjusted according to different polymerization reaction conditions, output and residence time required by polymerization reaction; the screw in the screw extruder can be used in a multi-stage mixing manner, such as a mixing stage, a propelling stage and a powerful extruding stage.

According to the present invention, in step S3, at least one of a polymerization monomer, a molecular weight modifier, a polymerization modifier, a solvent, and the like is additionally added according to a polymerization process and polymerization conditions; the addition position may be set to one or more depending on the length of the reactive screw extruder.

According to the present invention, the reactive screw extruder is in 1 stage or more depending on the viscosity of the material, the monomer conversion rate, the residence time and/or the polymer structure, and if it is in more than one stage, the material is transferred between each stage using a transfer pump at step S3.

According to the invention, in step S3, the reaction mass output of step S2 is fed to the reactive screw extruder, preferably via a transfer pump.

According to the invention, in the steps S1-S3, the temperature of the polymerization reaction is-40 ℃ to 150 ℃, the conversion rate of the polymerization reaction is more than 15%, the retention time is 10-240min, and the pressure of the polymerization reaction is not more than 10 MPa.

According to the invention, in steps S1-S3, the polymerized monomers are selected from C_2-30Such as terminal or internal olefins, for example selected from ethylene, propylene, butylene, and the like.

According to the present invention, in step S1, the catalyst system is selected from any homogeneous or heterogeneous catalyst system capable of catalyzing the polymerization or oligomerization of olefins, as will be understood by those skilled in the art; illustratively, the catalyst system comprises a procatalyst and a cocatalyst, the procatalyst may for example be selected from the group consisting of a homogeneous or supported Ziegler-Natta catalyst, a homogeneous or supported metallocene catalyst, a homogeneous or supported non-metallocene catalyst, a homogeneous or supported rare earth metal catalyst; the cocatalyst may be, for example, a compound selected from aluminum alkyls, methylaluminoxanes or boranes.

According to the present invention, in steps S1-S3, it will be understood by those skilled in the art that the molecular weight regulator is selected from hydrogen and other compounds that can directly chain transfer to olefin polymerization.

According to the invention, in steps S1-S3, the polymerization regulator is an alkylsiloxane compound.

According to the invention, in steps S1-S3, the solvent is selected from C_3-20Straight chain alkane of (1), C_3-20Branched alkane or C_3-20At least one of cycloalkanes of (a), or is selected from C_6-10The aromatic hydrocarbon of (1).

According to the present invention, the polymer prepared in steps S1-S3 may be dissolved or swollen in the polymerized monomer and/or the solvent.

According to the present invention, in step S4, the devolatilization process is to remove unreacted polymerized monomers, solvents, and the like under flash evaporation and low pressure conditions; preferably, unreacted polymerization monomers, solvent and the like are flashed and then enter a condenser for condensation and collection; also preferably, the unreacted polymerization monomer, solvent and the like may be recycled.

According to the present invention, it will be understood by those skilled in the art that the devolatilization apparatus is not particularly limited and may be adjusted according to the polymerization process and polymerization conditions, for example, selected from a kettle devolatilizer, a screw devolatilizer, or a combination of both.

According to the invention, in step S4, the temperature of the devolatilization device, i.e. the heating temperature for removing the unreacted polymerization monomer and the solvent, is required to ensure that the polymer has certain fluidity, so as to facilitate the material transportation; illustratively, the temperature of the devolatilization device is 100-.

According to the invention, in step S5, the reaction mass of step S4 is discharged and then fed to a pelletizing screw extruder via a conveying pump.

According to the present invention, in step S5, an aluminum alkyl-based deactivator is further added during the extrusion granulation.

According to the invention, the aluminum alkyl inactivator is selected from water, alcohol (such as methanol and ethanol), ammonia (such as ammonia) and other compounds with active hydrogen or their mixture.

According to the present invention, in step S5, other additives may be added during the extrusion granulation.

According to the invention, the other auxiliary agents are selected from antioxidants, acid scavengers, fillers and the like.

It will be understood by those skilled in the art that the antioxidant, acid scavenger and filler are not particularly limited and may be suitably used in the polymerization system of the present invention; illustratively, the antioxidant is selected from the group consisting of antioxidant 1010, antioxidant 1076, and the like; the acid scavenger is selected from hydrotalcite; the filler is selected from silicon dioxide, silicon nitride, silicon carbide, silicate, calcium carbonate, carbon black, clay, glass fiber, magnesium sulfate, sodium sulfate, kaolin, zinc oxide, aluminum oxide, mica, titanium dioxide and the like.

In a second aspect, the present invention provides a polyolefin prepared by the above process, in particular a polyolefin elastomer or a mixture thereof.

According to the invention, the polyolefin may be polybutene-1, butene-based butene/ethylene copolymers, random polypropylene, ethylene/higher alpha-olefin copolymers, ethylene/propylene random copolymers, ethylene/propylene/diene terpolymers, ethylene/styrene copolymers, hyperbranched polyethylene, norbornene homopolymers and copolymers thereof, or polyolefin multi-block copolymers, etc.

Preferably, the polyolefin is a polyolefin elastomer or a mixture thereof.

Preferably, the polyolefin elastomer is a polyolefin thermoplastic elastomer.

A third aspect of the present invention provides a system for the above process, comprising a prepolymerization reactor, a static mixer and a reactive screw extruder arranged in this order; wherein, the prepolymerization reactor is a kettle-type reactor.

According to the invention, the system also comprises a devolatilization device and a granulation device arranged in sequence after the reactive screw extruder.

According to the invention, the materials are fed between the devices by a conveying pump.

According to the invention, the tank reactor is a stirred tank reactor, and the stirred tank reactor is a single-layer stirred tank reactor or a multilayer stirred tank reactor. The heat in the kettle type reactor is fed in or taken out through a jacket or a built-in coil, and the transmission medium of the heat is water or heat conducting oil.

According to the present invention, it will be understood by those skilled in the art that parameters such as the capacity and the stirring power of the tank reactor are not particularly limited and may be adjusted according to the polymerization process and the polymerization conditions.

According to the invention, the static mixer is preferably a tubular static mixer; it will be understood by those skilled in the art that the length and diameter of the static mixer are not particularly limited and may be adjusted according to the polymerization process and polymerization conditions.

According to the invention, the reactive screw extruder is preferably a single screw extruder or a twin screw extruder or a mixed configuration of single and twin screw extruders; it will be understood by those skilled in the art that the length and diameter of the reactive screw extruder are not particularly limited and may be adjusted according to the polymerization process and polymerization conditions;

illustratively, the single-screw extruder or the twin-screw extruder is selected to have an aspect ratio (ratio of the length L of the screw extruder to the diameter D) as large as possible under the conditions allowed by the mechanical manufacturing and process, for example, the aspect ratio (L/D) > 35 of the single-screw extruder and the aspect ratio (L/D) > 50 of the twin-screw extruder are selected to increase the residence time in the screw extruder during polymerization of the polymerization monomers; the screw extruder is exemplarily selected from a screw extruder with cooling water and an electric heating jacket, and the screw rotating speed of the screw extruder can be adjusted according to different polymerization reaction conditions, output and residence time required by polymerization reaction; the screw in the screw extruder can be used in a multi-stage mixing manner, such as a mixing stage, a propelling stage, a powerful extruding stage and the like.

The invention has the beneficial effects that:

the present invention provides a process for the continuous preparation of polyolefins, in particular of polyolefin elastomers or mixtures thereof. The preparation process adopts a kettle type reactor for prepolymerization, which has the function of improving the viscosity of a reaction system so as to facilitate the subsequent operation of a screw reactor; in the preparation process, a static mixer is adopted for static mixing polymerization, and is used for continuously increasing the viscosity of the system and prolonging the reaction residence time; in the preparation process, a reactive screw extruder is adopted for extrusion polymerization, so that the polymerization reaction under high conversion rate and high viscosity is realized. The preparation method can be suitable for the preparation of various types of polyolefin, and is particularly suitable for the preparation of polyolefin elastomer or mixture thereof.

Further, the preparation process also comprises the step of devolatilization treatment by using a devolatilization device, wherein the devolatilization device is used for removing unreacted polymerization monomers and solvents, and the unreacted polymerization monomers and the solvents can be recycled after being condensed by a condenser.

Drawings

FIG. 1 is a flow chart of a process for continuously preparing polyolefin according to a preferred embodiment of the present invention.

Detailed Description

The invention will be further illustrated with reference to the following specific examples. It should be understood that these examples are only for illustrating the present invention and are not intended to limit the scope of the present invention. Furthermore, it should be understood that various changes or modifications can be made by those skilled in the art after reading the description of the present invention, and equivalents may fall within the scope of the present invention.

Example 1 high isotacticity polybutene-1

In the S1 stage, a single multi-blade stirring kettle is adopted, heat conducting oil is adopted for heating, a heating coil and a heat removal coil are arranged in the stirring kettle, and the reaction temperature is controlled to be 70 ℃. Continuously adding butene-1 monomer, cyclohexane, high isotacticity Ziegler-Natta catalyst, triethyl aluminum, external electron donor (such as dicyclopentyl dimethoxy silane) and hydrogen into a reactor, wherein the rotating speed of the reactor is 10-30 r/min, the polymerization residence time is 40min, the conversion rate of the butene-1 monomer is 30-35%, the isotacticity of polybutene is more than 98%, and the melt index is controlled between 0.2-0.25g/10 min.

After the material enters the S2 stage, monomers and hydrogen are added, the residence time is controlled to be 40min, the reaction temperature is controlled to be 70 ℃, the monomer conversion rate is controlled to be 20-25%, the isotacticity of the polybutene is more than 98%, and the melt index is controlled to be 0.3-0.35g/10 min.

After the material enters the S3 section, a double-screw extruder with a two-stage length-diameter ratio (L/D) of 50 is adopted, monomers and hydrogen are added into a feed inlet of each stage of screw, the retention time of each stage of screw is controlled to be 20min, the monomer conversion rate is 15-20%, the isotacticity of polybutene is more than 98%, the final melt index is controlled to be 0.5-0.55g/10min, and the solid content is 60-80%.

The material enters a devolatilization kettle at the S4 stage, the temperature is 180 ℃, the pressure is 5KPa, and butylene and cyclohexane are removed. And (3) connecting a twin-screw into the devolatilization kettle, wherein the temperature of the twin-screw is 180 ℃, adding assistants such as alkyl aluminum inactivator water, antioxidant, acid scavenger and the like into the inlet of the screw, extruding and granulating, and then feeding into a bin and a packaging line.

EXAMPLE 2 preparation of ethylene/octene copolymer elastomer

In the S1 stage, a single multi-blade stirring kettle is adopted, heat conducting oil is adopted for heating, a heating coil and a heat removal coil are arranged in the stirring kettle, and the reaction temperature is controlled to be 90 ℃. Continuously adding ethylene, octene-1, cyclohexane, a catalyst with a limited geometric configuration, a methyl aluminoxane toluene solution and hydrogen into a reactor, wherein the rotating speed of the reactor is 10-30 r/min, the polymerization residence time is 40min, the conversion rate of an octene-1 monomer is 30-35%, controlling the ethylene/octene ratio to ensure that the melting point of the polymer is 110-115 ℃ and the melt index is controlled between 8-10g/10 min.

After the material enters the S2 section, ethylene, octene-1 and hydrogen are supplemented, the residence time is controlled to be 40min, the reaction temperature is controlled to be 90 ℃, the conversion rate of octene-1 monomer is controlled to be 20-25%, the melting point of the polymer is 110-115 ℃, and the melt index is controlled to be 10-12g/10 min.

After the material enters the S3 section, a double-screw extruder with a two-stage length-diameter ratio of 50 is adopted, each stage of screw is supplemented with octene, ethylene and hydrogen at the feed inlet, the residence time of each stage of screw is controlled to be 20min, the conversion rate of octene-1 is 15-20%, the melting point of the polymer is 110-115 ℃, the melt index is controlled to be 12-14g/10min, and the final solid content is 60-80%.

The material enters a devolatilization kettle at the S4 stage, the temperature is 180 ℃, the pressure is 5KPa, and ethylene, octene-1 and cyclohexane are removed. And (3) connecting a twin-screw into the devolatilization kettle, wherein the temperature of the twin-screw is 180 ℃, adding assistants such as alkyl aluminum inactivator water, antioxidant, acid scavenger and the like into the inlet of the screw, extruding and granulating, and then feeding into a bin and a packaging line.

EXAMPLE 3 preparation of ethylene/propylene random copolymer elastomer

In the S1 stage, two multi-blade stirring kettles are adopted, heat conducting oil is adopted for heating, a heating coil and a heat-removing coil are arranged in the stirring kettles, and the reaction temperature is controlled to be 80 ℃.

In the S1-1 stage, ethylene, propylene, cyclohexane, catalyst with limited geometrical configuration, methyl aluminoxane toluene solution and hydrogen are continuously added into a reactor, the rotating speed of the reactor is 20-40 r/min, the polymerization residence time is 20min, the conversion rate of ethylene monomer is 60-70%, the ethylene/propylene ratio is controlled, propylene is taken as the main component, the melting point of the polymer is 95-100 ℃, and the melt index is controlled between 6-7g/10 min.

In the S1-2 stage, ethylene and propylene are continuously added into a reactor, the rotating speed of the reactor is 20-40 r/min, the polymerization residence time is 20min, the conversion rate of ethylene monomers is 60-70%, the ethylene/propylene ratio is controlled, propylene is taken as the main component, the melting point of the polymer is 95-100 ℃, and the melt index is controlled between 6-7g/10 min.

After the material enters the section S2, the material consists of a two-stage static mixer, wherein:

in the S2-1 stage, the polymerization residence time is 20min, the conversion rate of ethylene monomer is 60-70%, the ethylene/propylene ratio is controlled, the propylene is taken as the main component, the melting point of the polymer is 95-100 ℃, and the melt index is controlled between 6-7g/10 min.

In the S2-2 stage, the polymerization residence time is 20min, the conversion rate of ethylene monomer is 60-70%, the ethylene/propylene ratio is controlled, the propylene is taken as the main component, the melting point of the polymer is 95-100 ℃, and the melt index is controlled between 6-7g/10 min.

After the material enters the S3 section, a double-screw extruder with a two-stage length-diameter ratio (L/D) of 50 is adopted, ethylene, propylene and hydrogen are supplemented at a feed inlet of each stage of screw, the retention time of each stage of screw is controlled to be 20min, the conversion rate of ethylene monomers is controlled to be 60-70%, the ethylene/propylene ratio is controlled, propylene is taken as a main component, the melting point of the polymer is 95-100 ℃, the melt index is controlled to be 6-7g/10min, and the final solid content is 60-80%.

The material enters a devolatilization kettle at the S4 stage, the temperature is 180 ℃, the pressure is 5KPa, and ethylene, propylene and cyclohexane are removed. And (3) connecting a twin-screw into the devolatilization kettle, wherein the temperature of the twin-screw is 180 ℃, adding assistants such as alkyl aluminum inactivator water, antioxidant, acid scavenger and the like into the inlet of the screw, extruding and granulating, and then feeding into a bin and a packaging line.

The embodiments of the present invention have been described above. However, the present invention is not limited to the above embodiment. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A process for the continuous preparation of a polyolefin elastomer or a mixture of polyolefin elastomers, characterized in that it comprises the following steps:

s1 prepolymerization: continuously adding reaction materials from the bottom of the kettle type reactor, and continuously increasing the material level of the materials under the conditions of temperature control and stirring to reach the material discharging level; the reaction materials comprise a polymerization monomer, a catalyst system, a molecular weight regulator, a polymerization regulator and a solvent;

s2 static mixing polymerization: after the reaction material in the step S1 is discharged, sending the reaction material into a static mixer for continuous reaction, and continuously increasing the material level of the material to reach the discharge material level under the condition of controlling the temperature; optionally, supplementing at least one of a polymerization monomer, a molecular weight regulator, a polymerization regulator and a solvent as required;

s3 screw extrusion polymerization: after the reaction material obtained in the step S2 is discharged, feeding the reaction material into a reactive screw extruder to continue reacting; optionally, supplementing at least one of a polymerization monomer, a molecular weight regulator, a polymerization regulator and a solvent as required;

in the steps S1-S3, the temperature of the polymerization reaction is-40 ℃ to 150 ℃, the conversion rate of the polymerization reaction is more than 15%, the retention time is 10-240min, and the pressure of the polymerization reaction is not more than 10 MPa.

2. The method of claim 1, further comprising the steps of:

s4, devolatilization: after the reaction material in the step S3 is discharged, feeding the reaction material into a devolatilization device for devolatilization treatment;

s5, extruding and granulating: and (5) discharging the reaction material obtained in the step (S4), feeding the reaction material into a granulation screw extruder, and extruding and granulating to obtain the polyolefin elastomer or the mixture thereof.

3. The method according to claim 1, wherein in step S1, the tank reactor is a stirred tank reactor, and the stirred tank reactor is a single-layer stirred tank reactor or a multi-layer stirred tank reactor; the heat in the kettle type reactor is sent in or taken out through a jacket or a built-in coil, and the transmission medium of the heat is water or heat conducting oil.

4. The method of claim 1, wherein in step S1, the pre-polymerization is performed in 1 or more stages, and in the case of multiple stages, a transfer pump is used to transfer the materials between each stage.

5. The method of claim 1, wherein in step S2, the static mixer is a tubular static mixer.

6. The method of claim 1, wherein at least one of the polymerization monomer, the molecular weight modifier, the polymerization modifier and the solvent is additionally added in step S2 according to the polymerization process and the polymerization conditions, and the additional addition position is set to one or more according to the length of the static mixer.

7. The method of claim 1, wherein the static mixer is provided with 1 or more stages in step S2, and a transfer pump is used to transfer the materials between each stage in the case of multiple stages.

8. The method of claim 1, wherein in step S2, the reaction mass output of step S1 is fed to a static mixer via a transfer pump.

9. The method of claim 1, wherein in step S3, the reactive screw extruder is a single screw extruder or a twin screw extruder or a hybrid configuration of a single screw and a twin screw extruder.

10. The method according to claim 9, wherein the single screw extruder has a length to diameter ratio > 35 and the twin screw extruder has a length to diameter ratio > 50.

11. The process according to claim 1 or 9, wherein the reactive screw extruder is a screw extruder with cooling water and an electrically heated jacket, the screw speed of which is adjusted according to the different polymerization conditions, the throughput and the residence time required for the polymerization.

12. The method according to claim 1 or 9, wherein the screw in the reactive screw extruder is used for multi-stage mixing of a mixing section, a pushing section and an intensive extrusion section.

13. The method of claim 1 or 9, wherein in step S3, at least one of the polymerization monomer, the molecular weight regulator, the polymerization regulator and the solvent is additionally added according to the polymerization process and the polymerization conditions; the addition position is set to one or more according to the length of the reactive screw extruder.

14. The method of claim 1 or 9, wherein the reactive screw extruder is provided in 1 or more stages in step S3, and a transfer pump is used to transfer the materials between each stage in the case of multiple stages.

15. The method according to claim 1 or 9, wherein in step S3, the reaction mass of step S2 is discharged as a feed to a reactive screw extruder via a transfer pump.

16. The method of claim 1, wherein in steps S1-S3, the polymerized monomer is selected from C_2-30One or more of (a) an olefin(s).

17. The method of claim 16, wherein the polymerized monomer is selected from the group consisting of ethylene, propylene, butylene.

18. The method of claim 1, wherein in step S1, the catalyst system comprises a procatalyst and a cocatalyst, the procatalyst is selected from the group consisting of a homogeneous or supported Ziegler-Natta catalyst, a homogeneous or supported metallocene catalyst, a homogeneous or supported non-metallocene catalyst, a homogeneous or supported rare earth metal catalyst; the cocatalyst is selected from aluminum alkyl, methylaluminoxane or borane compounds.

19. The method according to claim 1, wherein in steps S1-S3, the molecular weight regulator is selected from hydrogen.

20. The method of claim 1, wherein in steps S1-S3, the polymerization regulator is an alkyl siloxane compound.

21. The method of claim 1, wherein the solvent is selected from the group consisting of C in steps S1-S3_3-20Straight chain alkane of (1), C_3-20Branched alkane or C_3-20At least one of cycloalkanes of (a), or is selected from C_6-10The aromatic hydrocarbon of (1).

22. The method of claim 1, wherein the polymer prepared in steps S1-S3 is soluble or swellable in the polymerized monomer and/or solvent.

23. The method of claim 2, wherein in step S4, the devolatilization process is to remove unreacted polymerized monomers and solvent under flash evaporation and low pressure conditions.

24. The method of claim 23 wherein unreacted polymerized monomer and solvent are flashed and condensed in a condenser.

25. The method of claim 23, wherein the unreacted polymerized monomer and solvent are recycled.

26. The method of claim 2, wherein said devolatilization apparatus is selected from a kettle devolatilizer, a screw devolatilizer, or a combination of both.

27. The method as claimed in claim 2, wherein the temperature of the devolatilization device is 100 ℃ and 280 ℃, and the pressure of the devolatilization device is less than a standard atmospheric pressure in step S4.

28. The method as claimed in claim 27, wherein in step S4, the temperature of the devolatilization device is 150 ℃ and 260 ℃, and the pressure of the devolatilization device is less than 10 KPa.

29. The method of claim 2, wherein in step S5, the reaction mass of step S4 is discharged and then fed to the pelletizing screw extruder via a conveying pump.

30. The method according to claim 2, wherein in step S5, an aluminum alkyl deactivator is further added during the extrusion granulation, wherein the aluminum alkyl deactivator is selected from water, alcohol, ammonia gas or a mixture thereof.

31. The method of claim 2 or 30, wherein in step S5, other additives selected from an antioxidant, an acid scavenger and a filler are further added during the extrusion granulation.

32. The method of claim 31, wherein the antioxidant is selected from the group consisting of antioxidant 1010, antioxidant 1076; the acid scavenger is selected from hydrotalcite; the filler is selected from silicon dioxide, silicon nitride, silicon carbide, silicate, calcium carbonate, carbon black, clay, glass fiber, magnesium sulfate, sodium sulfate, kaolin, zinc oxide, aluminum oxide, mica and titanium dioxide.