Continuous solution polymerization method of vinyl polyolefin elastomer
By employing a continuous solution polymerization method using a nickel diimine catalyst and a multi-stage deashing and devolatilization process, the problem of high-cost α-olefin dependence in the production of vinyl polyolefin elastomers has been solved, achieving low-cost, stable, and high-performance polymer production.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2025-12-22
- Publication Date
- 2026-04-07
AI Technical Summary
In the current production of polyolefin elastomers, the reliance on high-cost α-olefin comonomers leads to high production costs and a single source of raw materials, making it difficult to achieve efficient and stable production using ethylene as a raw material.
Vinyl polyolefin elastomers were prepared by continuous solution polymerization in a multi-stage reactor using nickel diimide catalyst and triethylaluminum as a co-catalyst, combined with multi-stage deashing and static devolatilization processes.
It achieves low-cost production using ethylene as the sole raw material, with extremely low ash and volatile matter content, excellent mechanical properties and light transmittance, adaptable to continuous production, and reduces equipment investment and operating energy consumption.
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Abstract
Description
Technical Field
[0001] This invention belongs to the field of olefin polymerization catalyst technology, and relates to a continuous solution polymerization method for vinyl polyolefin elastomers. Background Technology
[0002] Existing polyolefin elastomer (POE) production technologies generally rely on introducing specific α-olefins (such as 1-butene, 1-hexene, and 1-octene) as comonomers during ethylene polymerization to control the polymer chain structure and reduce crystallinity in order to achieve the desired elastomer properties. However, these α-olefin monomers are typically expensive to produce, and their sources are limited by specific production processes. This raw material cost factor directly increases the production cost of traditional POE products, not only limiting their application in fields requiring high cost-effectiveness but also exposing the entire industry chain to a certain degree of reliance on a single source of raw materials and the risk of price fluctuations.
[0003] Although the industry has proposed a technology for preparing polyolefin elastomers using ethylene as a single raw material, aiming to fundamentally reduce dependence on α-olefins, the realization of this route faces core technological challenges. Specifically, how to achieve precise control over the polymer chain structure in an ethylene homopolymerization system through catalyst and process design, thereby stably and efficiently producing polyolefin elastomers with excellent mechanical properties, optical properties, and high purity, remains a key technical problem that urgently needs to be solved. In particular, developing a catalyst system that combines high activity, excellent chain structure control capabilities, and applicability to continuous solution polymerization processes is the core bottleneck for achieving the industrial-scale production of this low-cost route. Summary of the Invention
[0004] In view of the problems and defects existing in the prior art, a continuous solution polymerization method for vinyl polyolefin elastomers is proposed.
[0005] In a first aspect, the present invention provides a continuous solution polymerization method for vinyl polyolefin elastomers, comprising: using ethylene as a polymerization monomer, carrying out a continuous polymerization reaction in a multi-stage polymerization reactor in a reaction system containing a main catalyst, a co-catalyst and a solvent, and after the polymerization reaction, performing multi-stage deashing and static devolatilization treatments in sequence, and extruding and granulating to obtain vinyl polyolefin elastomers.
[0006] Furthermore, in the continuous solution polymerization method for vinyl polyolefin elastomers provided by the present invention, the main catalyst is a nickel diimine catalyst, having the structure shown in Formula I.
[0007] R1 is selected from any one of Li, Na, and K; R2 is selected from any one of methyl, methoxy, trifluoromethyl, nitro, and tert-butyl, and R2 may be the same or different; X is a halogen, and X may be the same or different.
[0008] Furthermore, in the continuous solution polymerization method for vinyl polyolefin elastomers provided by the present invention, the co-catalyst is selected from at least one of triethylaluminum, triisobutylaluminum, trihexylaluminum, trioctylaluminum, diethylaluminum chloride, dichloroethylaluminum, methylaluminoxane, modified methylaluminoxane, perfluorophenylboron, triphenylcarbazo(pentafluorophenyl)borate, N,N-dimethylanilinetetra(pentafluorophenyl)borate, and N,N-di(hexadecyl)phenylammoniumtetra(pentafluorophenyl)borate; The solvent is selected from at least one of isobutane, n-pentane, isopentane, n-hexane, methylcyclopentane, n-heptane, methylcyclohexane, isooctane, toluene, and C10-C16 isomeric saturated alkanes.
[0009] Furthermore, in the continuous solution polymerization method for vinyl polyolefin elastomers provided by the present invention, the multi-reactor polymerization reactor is a three-reactor series polymerization reactor, and the polymerization operation mode is selected from any one of single-reactor operation, double-reactor series operation, and triple-reactor series operation; The polymerization reaction is carried out at a temperature of 60~200℃, a pressure of 1~10MPa, a residence time of 5~60min, an ethylene flow rate of 1~2kg / h, a main catalyst concentration of 2~50μmol / L, and a ratio of the number of moles of Al in the co-catalyst to the number of moles of Ni in the main catalyst of 50:1~500:1.
[0010] Furthermore, in the continuous solution polymerization method for vinyl polyolefin elastomers provided by the present invention, the multi-stage deashing is either single-stage or two-stage deashing. The deashing process is either washing deashing or adsorption deashing; The detergent used for washing and deashing is an aqueous solution of acid or alkali, with a concentration of 0.1% to 10%. The adsorbent for adsorption and deashing is selected from any one of molecular sieves, alumina, and polyacrylamide.
[0011] Furthermore, in the continuous solution polymerization method for vinyl polyolefin elastomers provided by the present invention, when the deashing process is washing deashing, the washing temperature is 10~150℃ and the pressure is 0.1~1MPa; When the deashing process is adsorption deashing, the adsorption temperature is 120~200℃ and the pressure is 2~8MPa.
[0012] Furthermore, in the continuous solution polymerization method for vinyl polyolefin elastomers provided by the present invention, the static devolatilization is performed by a two-stage flash tank series operation or a three-stage flash tank series operation.
[0013] Furthermore, in the continuous solution polymerization method for vinyl polyolefin elastomers provided by the present invention, the pressure inside the flash tank for static devolatilization is 0.1~5MPa, the temperature is 100~250℃, and the residence time in a single flash tank is 3~30min; The flash tank is equipped with a stirrer, and the stirrer type is selected from any one of single ribbon stirring, double ribbon stirring, and anchor stirring.
[0014] Furthermore, in the continuous solution polymerization method for vinyl polyolefin elastomers provided by the present invention, the extrusion granulation temperature is 100~220℃ and the rotation speed is 100~250rpm.
[0015] A vinyl polyolefin elastomer, characterized in that it is prepared by a continuous solution polymerization method of the above-mentioned vinyl polyolefin elastomer.
[0016] Compared with the prior art, the technical solution provided by the present invention has at least the following beneficial effects or advantages: (1) This invention uses ethylene as the sole polymerization raw material, eliminating the need to use expensive α-olefins as comonomers and avoiding the use of expensive metallocene catalysts. Instead, it adopts highly active nickel-based catalysts, which significantly reduces the overall cost of raw materials and catalytic systems at the source.
[0017] (2) The purification and feeding process of α-olefins in the traditional process is omitted during the production process. At the same time, there is no need to perform deep purification of raw material ethylene. The process flow is simplified, and the equipment investment and operating energy consumption are reduced accordingly, thus improving the economy of the whole process.
[0018] (3) Through optimized multi-stage deashing technology and efficient static devolatilization process, catalyst residues and small molecule volatiles can be effectively removed, resulting in extremely low ash and volatile content in the product (e.g., ash ≤ 40 ppm, volatiles ≤ 90 ppm), achieving continuous production of "ultra-pure" polymers. The product also possesses mechanical properties comparable to traditional POE, high volume resistivity, and good light transmittance, and exhibits high batch stability.
[0019] (4) This method has good process tolerance for changes in catalyst concentration, type and amount of co-catalyst, can use more cost-effective co-catalysts (such as triethylaluminum to replace methylaluminoxane), and can control the molecular weight of the product under multi-stage tandem polymerization conditions, adapting to the requirements of continuous and large-scale production, and has good engineering scale-up potential. Detailed Implementation
[0020] The technical solution of the present invention will be described below with reference to embodiments. However, the present invention is not limited to the following embodiments. Unless otherwise specified, the experimental methods and detection methods described in each embodiment are conventional methods; unless otherwise specified, the reagents and materials can be purchased commercially.
[0021] The main catalyst used in the following preparation examples is a nickel diimine catalyst, whose general structural formula is shown in Formula I:
[0022] R1 is selected from any one of Li, Na, and K; R2 is selected from any one of methyl, methoxy, trifluoromethyl, nitro, and tert-butyl, and R2 may be the same or different; X is a halogen, and X may be the same or different.
[0023] The cocatalyst is selected from at least one of triethylaluminum, triisobutylaluminum, trihexylaluminum, trioctylaluminum, diethylaluminum chloride, dichloroethylaluminum, methylaluminoxane, modified methylaluminoxane, perfluorophenylboron, triphenylcarbazo(pentafluorophenyl)borate, N,N-dimethylanilinetetra(pentafluorophenyl)borate, and N,N-di(hexadecyl)phenylammoniumtetra(pentafluorophenyl)borate.
[0024] The solvents used in the following examples are selected from at least one of isobutane, n-pentane, isopentane, n-hexane, methylcyclopentane, n-heptane, methylcyclohexane, isooctane, toluene, and C10-C16 isomeric saturated alkanes (such as isodecane, isododecane, isotridecane, and isohexadecane), preferably n-hexane, methylcyclopentane, n-heptane, and isomeric saturated alkanes, and more preferably n-hexane and n-heptane.
[0025] The continuous solution polymerization method for vinyl polyolefin elastomers involved in the following examples is shown below: S1. Raw material storage and preparation: Ethylene recovered from the continuous solution polymerization system of ethylene and vinyl polyolefin elastomer is stored in an ethylene storage tank for later use; solvent recovered from the continuous solution polymerization system of solvent and vinyl polyolefin elastomer is stored in a solvent storage tank for later use; the main catalyst and co-catalyst are placed in the main catalyst tank and co-catalyst tank respectively for later use.
[0026] S2. Polymerization reaction: Ethylene and the main catalyst are directly introduced into the reactor. The co-catalyst and solvent are mixed in the pipeline and then introduced into the reactor. The reaction temperature is 60~200℃, the pressure is 1~10MPa, and the residence time in a single reactor is 5~60min.
[0027] S3. Deashing: After the adhesive liquid comes out of the reactor, it flows through the buffer tank and then through a primary or multi-stage deashing system to deeply remove the residual catalyst and co-catalyst in the adhesive liquid.
[0028] S4. Static Deviation: The deashed adhesive solution passes through a multi-stage static deviation system, with the pressure inside the flash tank controlled at 0.1~5MPa and the temperature at 100~250℃. The residence time of the adhesive solution in a single flash tank is 3~30min. The flash tank is equipped with a stirrer, which can be one of the following: single ribbon stirring, double ribbon stirring, or anchor stirring. The volatile content in the final devolatilized polymer is ≤100ppm.
[0029] S5. Extrusion Granulation: The devolatilized material is processed through a single-screw extruder. The extruder temperature is controlled at 100~220℃ and the speed is controlled at 100~250rpm. After extrusion, the material is granulated underwater to obtain vinyl polyolefin elastomer particles.
[0030] In the above method, the reactor in S2 is a three-reactor series, each reactor has a solvent, a main catalyst, a co-catalyst and an ethylene feed inlet, which can realize single-reactor operation, two-reactor series operation and three-reactor series operation; the ethylene flow rate is 1~2 kg / h, the single-reactor concentration of the main catalyst is 2~50 μmol / L, and the number of moles of aluminum in the co-catalyst is 50~500 times the number of moles of Ni in the catalyst.
[0031] S3. The deashing system can be a primary or secondary deashing system, with each stage being either washing deashing or adsorption deashing. A secondary deashing system is preferred, with the primary stage being washing deashing and the secondary stage being adsorption deashing. The washing deashing process uses aqueous solutions of acid and alkali, with concentrations of both solutions ranging from 0.1% to 10%. The acid can be any commercially available strong or weak acid, and the alkali can be any commercially available strong or weak alkali. The washing temperature is 10–150°C, and the pressure is 0.1–1 MPa. The adsorption deashing process can use any commercially available molecular sieve, alumina, or polyacrylamide as the adsorbent, with a pressure of 2–8 MPa and a temperature of 120–200°C. Each deashing unit is configured with one unit in operation and one on standby.
[0032] S4. The static devolatilization process can be either two-stage or three-stage. Three-stage static devolatilization, i.e., three flash tanks operating in series, is preferred, achieving ultra-low volatile matter residue (≤50ppm) in the polymer. Two-stage static devolatilization, i.e., two flash tanks operating in series, results in volatile matter residue (≤100ppm) in the polymer.
[0033] The ethylene and solvent recovered during the static devolatilization process are recycled into ethylene storage tanks and solvent storage tanks, respectively.
[0034] Example 1 This embodiment provides a continuous solution polymerization method for vinyl polyolefin elastomers.
[0035] S1. Raw Material Storage and Preparation: Ethylene recovered from the continuous solution polymerization system of ethylene and vinyl polyolefin elastomers is stored in an ethylene storage tank for later use; solvent recovered from the continuous solution polymerization system of solvent and vinyl polyolefin elastomers is stored in a solvent storage tank for later use; the main catalyst and co-catalyst are stored in a main catalyst tank and a co-catalyst tank, respectively, for later use. The main catalyst is Catalyst 1 (R1 is Li, R2 is methyl, X is Br), the solvent is n-heptane, ethylene polymerization grade ethylene, and the co-catalyst is triethylaluminum.
[0036] S2. Polymerization reaction: Ethylene and the main catalyst are directly introduced into the reactor. The co-catalyst and solvent are mixed in a pipeline and then introduced into the reactor. The reaction process is a single-reactor operation, with a reaction temperature of 70℃, a pressure of 3MPa, an ethylene flow rate of 2kg / h, a residence time of 30min, a single-reactor concentration of the main catalyst of 2μmol / L, and the number of moles of aluminum in triethylaluminum being 50 times the number of moles of Ni in the catalyst.
[0037] S3. Deashing: After the liquid from the reactor flows through the buffer tank, it passes through the primary deashing system and is deashed using adsorption deashing technology. The adsorbent is 3A molecular sieve, the pressure is 4MPa, and the temperature is 180℃.
[0038] S4. Static devolatilization: The deashed adhesive enters the secondary devolatilization system and passes through two flash evaporators connected in series. The flash temperature of both flash evaporators is 180℃, and the pressure inside the flash evaporator is 0.2MPa. The stirring method inside the flash evaporator is single spiral ribbon stirring. The residence time of the adhesive in the first and second flash evaporators is 15min and 30min, respectively.
[0039] S5. Extrusion granulation: The devolatilized material is processed through a single-screw extruder. The extruder temperature is controlled at 180℃ and the speed is controlled at 100rpm. After extrusion, the material is granulated underwater to obtain vinyl polyolefin elastomer particles.
[0040] Example 2 Example 2 is the same as Example 1, except that the main catalyst in Example 2 is catalyst 2 (R1 is Na, R2 is methyl, and X is Br).
[0041] Example 3 Example 3 is the same as Example 1, except that the main catalyst in Example 2 is catalyst 3 (R1 is K, R2 is methyl, and X is Br).
[0042] Example 4 Example 4 is the same as Example 1, except that the main catalyst in Example 2 is catalyst 2 (R1 is Li, R2 is methoxy, and X is Br).
[0043] Example 5 Example 5 is the same as Example 1, except that the main catalyst in Example 2 is catalyst 2 (R1 is Li, R2 is tert-butyl, and X is Br).
[0044] Example 6 Example 6 is the same as Example 1, except that the main catalyst in Example 2 is catalyst 2 (R1 is Li, R2 is methyl, and X is Cl).
[0045] Example 7 Example 7 is the same as Example 1, except that the concentration of the main catalyst is 10 μmol / L.
[0046] Example 8 Example 8 is the same as Example 1, except that the concentration of the main catalyst is 50 μmol / L.
[0047] Example 9 Example 9 is the same as Example 1, except that the co-catalyst is methylaluminoxane.
[0048] Example 10 Example 10 is the same as Example 1, except that the co-catalyst is methylaluminoxane, and the number of moles of aluminum in the co-catalyst is 200 times the number of moles of Ni in the main catalyst.
[0049] Example 11 Example 11 is the same as Example 1, except that the polymerization reaction is carried out in three reactors connected in series. The reaction temperature of all three reactors is 70°C and the pressure is 3MPa. In the first reactor, the ethylene flow rate is 1.5 kg / h, the residence time is 15 min, the concentration of the main catalyst in a single reactor is 1.5 μmol / L, and the molar number of aluminum in the co-catalyst (triethylaluminum) is 50 times the molar number of Ni in the main catalyst. In the second reactor, the ethylene flow rate is 0.5 kg / h, the residence time is 5 min, the concentration of the main catalyst in a single reactor is 0.5 μmol / L, and the molar number of aluminum in the co-catalyst (triethylaluminum) is 50 times the molar number of Ni in the main catalyst. No ethylene, main catalyst, or co-catalyst is added to the third reactor.
[0050] Example 12 Example 12 is the same as Example 1, except that the adsorbent in the deashing process is alumina.
[0051] Example 13 Example 13 is the same as Example 1, except that a two-stage deashing system is used for deashing. The first stage of deashing is washing deashing, with a 0.1 wt% hydrochloric acid aqueous solution as the washing agent, a temperature of 80°C, and a pressure of 0.1 MPa. The second stage of deashing is adsorption deashing, with alumina as the adsorbent, a pressure of 4 MPa, and a temperature of 180°C.
[0052] Example 14 Example 14 is the same as Example 13, except that the static devolatilization is a three-stage devolatilization system, passing through three flash evaporators connected in series. The flash temperature of the first and second flash evaporators is 180°C, the pressure inside the flash evaporators is 0.2 MPa, and the stirring method inside the flash evaporators is single ribbon stirring. The residence time of the adhesive in the first and second flash evaporators is 5 min and 10 min, respectively. The flash temperature of the third flash evaporator is 220°C, the pressure is 0.1 MPa, the stirring method inside the flash evaporator is anchor stirring, and the flash residence time is 10 min.
[0053] Example 15 Example 15 is the same as Example 14, except that the extruder temperature is 150°C and the rotation speed is 180 rpm during the extrusion granulation process.
[0054] The performance testing method for the vinyl polyolefin elastomer prepared by this invention is as follows: The degree of branching was measured using high-temperature NMR with deuterated tetrachloroethane as the reagent, and the value represents the number of branches per 1000 carbon atoms. Refer to GB / T 24131.2-2017 for testing volatile matter; Ash content was tested according to GB / T 9345.1-2008; Hardness was tested according to GB / T 2411-2008; Melt flow index was tested according to GB / T 3682.1-2018 at a temperature of 190℃ and a load of 2.16 kg. Refer to SN / T 4183-2015 to test the weight-average molecular weight (Mw) and molecular weight distribution (PDI). Density should be tested according to GB / T 1033.1-2008; Refer to GB / T 31838.2-2019 for testing volume resistivity; Refer to GB / T 2410-2008 for light transmittance testing; Tensile strength was tested according to GB / T 1040.3-2006.
[0055] Table 1. Test results of the effect of the main catalyst on the properties of vinyl polyolefin elastomers
[0056] Table 1 shows that the vinyl polyolefin elastomers (Examples 1-6) prepared by nickel diimine catalysts with different structures exhibit certain differences in performance, but the ash content of the products is ≤30ppm and the volatile matter is ≤90ppm. This result fully demonstrates that the nickel diimine catalyst used in this invention not only possesses excellent catalytic activity and structure regulation ability in the process of catalyzing the polymerization of ethylene to produce elastomers, but also exhibits good low-residue characteristics.
[0057] Further comparison of Example 1, Example 7 and Example 8 shows that even when the catalyst concentration is significantly increased, the ash content of the vinyl polyolefin elastomer only slightly increases by 5 - 8 ppm, and the volatile content remains basically unchanged. The ash removal and devolatilization processes配套 with the present invention have outstanding adaptability and high efficiency, and can operate stably within a relatively wide range of catalyst concentrations, ensuring that the vinyl polyolefin elastomer has extremely low ash and volatile residues.
[0058] Table 2 Test results of the influence of different reaction conditions on the properties of vinyl polyolefin elastomer
[0059] As shown in Table 2, according to the comparison results of Example 1 and Example 9, it can be seen that when methylaluminoxane and triethylaluminum are used as cocatalysts respectively, the key performance indicators of the obtained vinyl polyolefin elastomer basically remain the same. This indicates that the technology of the present invention can replace expensive methylaluminoxane with significantly lower-cost triethylaluminum without affecting the comprehensive performance of the vinyl polyolefin elastomer.
[0060] Further discovery through the comparison of Example 9 and Example 10 shows that even when the dosage of triethylaluminum is increased to 4 times the original amount, the ash and volatile contents in the vinyl polyolefin elastomer do not increase significantly. This proves that the ash removal and devolatilization processes adopted in the present invention have excellent impurity removal ability and process tolerance, and can effectively cope with the fluctuations in the dosage of the cocatalyst, thus ensuring the ultra-pure quality of the product under continuous production conditions.
[0061] From the comparison of Example 1 and Example 11, it can be seen that the polymerization process with three reactors in series can significantly increase the molecular weight of the vinyl polyolefin elastomer while maintaining the ash and volatile contents of the product at the original low levels, and keeping key indicators such as its mechanical properties, volume resistivity and light transmittance stable. This shows that the multi-stage polymerization process described in the present invention can achieve high performance of the product without introducing additional impurity burden.
[0062] By comparing the experimental results of Example 1 with those of Example 12, 13 and 14, it is found that upgrading the ash removal process from the first stage to the second stage can significantly reduce the ash content in the vinyl polyolefin elastomer; at the same time, upgrading the devolatilization process from the second stage to the third stage can effectively reduce the volatile content. With the further reduction of the ash and volatile contents, both the volume resistivity and light transmittance of the vinyl polyolefin elastomer are significantly improved.
[0063] The embodiments described above are some, but not all, of the embodiments of the present invention. The detailed description of the embodiments of the present invention is not intended to limit the scope of the claimed invention, but merely to illustrate selected embodiments of the invention. All other embodiments obtained by those skilled in the art through related deductions and substitutions based on the inventive concept, without inventive effort, are within the scope of protection of the present invention.
Claims
1. A continuous solution polymerization method for vinyl polyolefin elastomers, characterized in that, include: Using ethylene as the monomer, a continuous polymerization reaction is carried out in a multi-stage polymerization reactor in a reaction system containing a main catalyst, a co-catalyst and a solvent. After the polymerization reaction, multi-stage deashing and static devolatilization treatments are carried out in sequence, followed by extrusion granulation to obtain vinyl polyolefin elastomer.
2. The continuous solution polymerization method for vinyl polyolefin elastomers according to claim 1, characterized in that, The main catalyst is a nickel diimine catalyst, having the structure shown in Formula I. R1 is selected from any one of Li, Na, and K; R2 is selected from any one of methyl, methoxy, trifluoromethyl, nitro, and tert-butyl, and R2 may be the same or different; X is a halogen, and X may be the same or different.
3. The continuous solution polymerization method for vinyl polyolefin elastomers according to claim 1, characterized in that, The cocatalyst is selected from at least one of triethylaluminum, triisobutylaluminum, trihexylaluminum, trioctylaluminum, diethylaluminum chloride, dichloroethylaluminum, methylaluminoxane, modified methylaluminoxane, perfluorophenylboron, triphenylcarbazo(pentafluorophenyl)borate, N,N-dimethylanilinetetra(pentafluorophenyl)borate, and N,N-di(hexadecyl)phenylammoniumtetra(pentafluorophenyl)borate. The solvent is selected from at least one of isobutane, n-pentane, isopentane, n-hexane, methylcyclopentane, n-heptane, methylcyclohexane, isooctane, toluene, and C10-C16 isomeric saturated alkanes.
4. The continuous solution polymerization method for vinyl polyolefin elastomers according to claim 1, characterized in that, The multi-tank polymerization reactor is a three-tank series polymerization reactor, and the polymerization operation mode is selected from any one of single-tank operation, two-tank series operation, and three-tank series operation. The polymerization reaction is carried out at a temperature of 60~200℃, a pressure of 1~10MPa, a residence time of 5~60min, an ethylene flow rate of 1~2kg / h, a main catalyst concentration of 2~50μmol / L, and a ratio of the number of moles of Al in the co-catalyst to the number of moles of Ni in the main catalyst of 50:1~500:
1.
5. The continuous solution polymerization method for vinyl polyolefin elastomers according to claim 1, characterized in that, The multi-stage deashing can be either single-stage or two-stage deashing. The deashing process is either washing deashing or adsorption deashing; The detergent used for washing and deashing is an aqueous solution of acid or alkali, with a concentration of 0.1% to 10%. The adsorbent for adsorption and deashing is selected from any one of molecular sieves, alumina, and polyacrylamide.
6. The continuous solution polymerization method for vinyl polyolefin elastomers according to claim 5, characterized in that, When the deashing process is washing deashing, the washing temperature is 10~150℃ and the pressure is 0.1~1MPa; When the deashing process is adsorption deashing, the adsorption temperature is 120~200℃ and the pressure is 2~8MPa.
7. The continuous solution polymerization method for vinyl polyolefin elastomers according to claim 1, characterized in that, The static devolatilization is either a two-stage flash tank series operation or a three-stage flash tank series operation.
8. The continuous solution polymerization method for vinyl polyolefin elastomers according to claim 7, characterized in that, The pressure inside the flash tank for static devolatilization is 0.1~5MPa, the temperature is 100~250℃, and the residence time in a single flash tank is 3~30min; The flash tank is equipped with a stirrer, and the stirrer type is selected from any one of single ribbon stirring, double ribbon stirring, and anchor stirring.
9. The continuous solution polymerization method for vinyl polyolefin elastomers according to claim 1, characterized in that, The extrusion granulation temperature is 100~220℃ and the rotation speed is 100~250rpm.
10. A vinyl polyolefin elastomer, characterized in that, It is prepared by continuous solution polymerization of the vinyl polyolefin elastomer according to any one of claims 1 to 9.