Continuous production method and system of high isotactic polybutylene-1

Abstract

The invention relates to a high isotactic polybutylene-1 continuous production method and system, and the method comprises the following steps: taking liquid-phase butylene-1 as a polymerization monomer, taking hydrogen as a molecular weight regulator, sequentially adding the polymerization monomer, a reaction solvent, a main catalyst, a cocatalyst and an external electron donor into a polymerization reaction kettle according to a ratio, and fully mixing; introducing a molecular weight regulator, and carrying out polymerization reaction; after a period of time, part of materials are discharged and enter a flash tank, and unpolymerized monomers, the reaction solvent and polybutylene-1 are separated; recovering the gas-phase component from the flash tank to a rectifying tower and separating the unpolymerized monomer and the reaction solvent; recovering crude polybutylene-1 from the bottom of the flash tank, washing with water, and devolatilizing to obtain a high isotactic polybutylene-1 product; and respectively purifying and quenching the recovered unpolymerized monomer and the reaction solvent with the newly supplemented polymerized monomer and the reaction solvent, and then adding into the polymerization reaction kettle to participate in a new round of polymerization reaction. The method has the characteristics of high catalytic efficiency, short reaction time and low reaction energy consumption.

Description

Technical Field

[0001] The invention relates to the technical field of high molecular polymer synthesis, and in particular to a method and system for continuously producing highly isotactic polybutene-1. Background Art

[0002] Polybutene-1 (PB-1 for short) is an isotactic polymer inert homopolymer with the structural formula -(H2C-CH(C2H5))n-, which is polymerized by pure butene-1 monomer and catalyst in a reactor. Polybutene-1 is a good raw material for preparing pipes, films and other blended modified polymer products due to its high modulus, excellent creep resistance, temperature resistance, environmental stress cracking resistance, excellent chemical corrosion resistance, wear resistance and dielectric properties. The broad application prospects of polybutene-1 have attracted widespread attention in the industry.

[0003] At present, the industrial preparation process of polybutene-1 is a homogeneous solution polymerization process. This process uses butene-1 as raw material. First, the raw material is pretreated and refined to remove other impurities. After refining, butene-1 enters the polymerization section. At the same time, the polymerization reaction uses organic alkanes as solvents, uses Ziegler-Natta catalysts, selects specific co-catalysts and initiators, and achieves polymerization in a patented reactor system under specified temperature and pressure conditions. After the polymerization reaction is completed, the polymer solution in the reactor undergoes, polymer-unreacted butene-1 monomer recovery, solvent recovery, glue washing, polymer devolatilization, and drying to obtain a powder product; or, after wet extrusion of the glue, it is washed and dried to obtain a granular product. The traditional polybutene-1 process is a homogeneous solution polymerization process. Due to the low catalyst efficiency and poor selection of reaction solvents, there are low quality and poor yield of polybutene-1, resulting in low single-pass monomer utilization, excessive solvent consumption, and solvent accompanying the process waste gas removal system, resulting in high energy consumption and material consumption of the process technology, and high production costs.

[0004] Therefore, a method and system for continuous production of highly isotactic polybutene-1 are urgently needed to solve the above problems. Summary of the invention

[0005] In order to solve the technical problems existing in the above-mentioned prior art, the purpose of the present invention is to provide a method and system for continuous production of highly isotactic polybutene-1, which has the characteristics of high catalytic efficiency, short reaction time period and low reaction energy consumption.

[0006] To achieve the above-mentioned object of the invention, the present invention provides a method for continuously producing highly isoisobutylene-1, comprising the following steps:

[0007] Using liquid butene-1 as a polymerization monomer and hydrogen as a molecular weight regulator, the polymerization monomer, reaction solvent, main catalyst, co-catalyst and external electron donor are sequentially added into a polymerization reactor in proportion and fully mixed, and then the molecular weight regulator is introduced to cause a polymerization reaction;

[0008] After a period of reaction, part of the materials in the polymerization reactor are discharged into a flash tank to separate the unpolymerized monomers, the reaction solvent and the polybutene-1;

[0009] Recovering the gaseous components containing unpolymerized monomers and reaction solvent from the top of the flash tank to a distillation tower; recovering the unpolymerized monomers from the gaseous components at the top of the distillation tower, and recovering the reaction solvent from the bottom of the distillation tower;

[0010] Recovering crude polybutene-1 from the bottom of the flash tank, and obtaining a highly isotactic polybutene-1 product after washing and devolatilization;

[0011] The recovered unpolymerized monomers and the reaction solvent are added to the polymerization reactor after being purified and rapidly cooled together with the newly added polymerized monomers and the reaction solvent to participate in a new round of polymerization reaction.

[0012] According to a technical solution of the present invention, the catalyst is a Ziegler-Natta type catalyst, including a main catalyst, a co-catalyst and an external electron donor; the reaction solvent is isopentane;

[0013] After releasing part of the materials, the reaction solvent was circulated back to the polymerization reactor to maintain the polymer concentration in the polymerization reactor at 30%wt.

[0014] According to a technical solution of the present invention, the temperature of the quenching air is 30-50°C.

[0015] According to a technical solution of the present invention, the polymerization reaction temperature of the polymerization reactor is 45-90° C., the pressure is 1.5-5.0 MPaG, and the reaction time is 1.5-6 hours.

[0016] According to a technical solution of the present invention, the mass ratio of the liquid phase butene-1 to the main catalyst is 40000-150000:1; the mass ratio of the liquid phase butene-1 to the co-catalyst is 900-15000:1; the mass ratio of the liquid phase butene-1 to the external electron donor is 30000-300000:1; the amount of the liquid phase butene-1 to the hydrogen is 1200-400000:1.

[0017] According to one aspect of the present invention, a high isopolybutene-1 continuous production system is provided, which is used to implement the above-mentioned high isopolybutene-1 continuous production method, comprising a polymerization reactor, and further comprising:

[0018] A pretreatment unit, used for purifying the materials entering the polymerization reactor;

[0019] A flash tank, the inlet of which is connected to the outlet of the polymerization reactor, and is used for preliminarily separating unreacted polymerization monomers, reaction solvent and polybutene-1;

[0020] A distillation tower, whose inlet is connected to the top outlet of the flash tank, whose top outlet is connected to the inlet of the pretreatment unit through a monomer recovery pipeline; and whose bottom outlet is connected to the inlet of the pretreatment unit through a solvent recovery pipeline;

[0021] The devolatilization and post-treatment unit has an inlet connected to the bottom outlet of the flash tank and is used for devolatilization and post-treatment of the crude polybutene-1 rubber solution to obtain a highly isotactic polybutene-1 product.

[0022] According to a technical solution of the present invention, the devolatilization and post-treatment unit comprises:

[0023] A water washer connected to the bottom of the flash tank and used to wash the crude polybutene-1 glue solution with water to recover the catalyst;

[0024] The devolatilizer is connected to the water scrubber and uses hot nitrogen as the devolatilization medium to devolatilize and purify the crude polybutene-1 rubber solution after washing.

[0025] According to a technical solution of the present invention, the devolatilization and post-processing unit further comprises a washing and drying unit for washing and drying the devolatilized 1-butene rubber solution to obtain a pellet product;

[0026] Alternatively, the devolatilization and post-processing unit further comprises a dryer for extruding the devolatilized 1-butene rubber solution to obtain a powder product.

[0027] According to a technical solution of the present invention, the cleanliness requirement of the polymerization reactor is that the impurity content is less than 3 ppm;

[0028] The operating temperature of the flash tank is 80-120°C and the operating pressure is 0-0.05MPaG;

[0029] The operating temperature of the distillation tower is 100-200°C and the operating pressure is 0.05-0.5MPaG;

[0030] The operating temperature of the devolatilizer is 100-200°C, and the operating pressure is 0-1.0 MPaG.

[0031] According to a technical solution of the present invention, the preprocessing unit includes:

[0032] The first quenching unit and the second quenching unit are used to quench the materials in the monomer recovery pipeline and the solvent recovery pipeline respectively;

[0033] A raw material pretreatment unit connected to the first quenching unit, used to remove impurities in fresh liquid phase butene-1 and recovered liquid phase butene-1;

[0034] The solvent pretreatment unit is connected to the second quenching unit and is used to remove impurities in the fresh reaction solvent and the recovered reaction solvent.

[0035] Compared with the prior art, the present invention has the following beneficial effects:

[0036] Seeking to adopt a highly selective and high-yield catalyst system in order to reduce the material and energy consumption of the process technology; adopting efficient solvent and monomer recovery technology to minimize the solvent circulation volume; adopting efficient and low-energy devolatilization technology to ensure high-quality product performance and reduce raw material consumption; reducing waste gas emissions has become a hot topic of research at home and abroad.

[0037] In view of the technical deficiencies of the current traditional polybutene-1 preparation process, such as low single-pass conversion rate and selectivity, large consumption of reaction solvents, complex post-treatment process, and poor product quality, there is no report on the continuous production process of polybutene-1 that uses high-selectivity and high-yield catalysts, high-efficiency solvents and monomer recovery technology to minimize solvent recovery, integrate high-efficiency and low-energy devolatilization technology to ensure high-quality product performance, reduce raw material consumption and reduce waste gas emissions.

[0038] The invention proposes a method and system for continuous production of highly isotactic polybutene-1. The invention adopts a high-efficiency solution polymerization process, uses liquid phase butene-1 as a polymerization monomer, isopentane as a reaction solvent, hydrogen as a molecular weight regulator, Ziegler-Natta as a polymerization catalyst, and the polymerization reaction temperature is 50-80°C. The catalyst used in the process has high catalytic efficiency, high single-pass conversion rate, high monomer utilization rate, and very small monomer circulation volume. An efficient solvent is used to minimize the use of the solvent. An efficient monomer recovery technology is used to fully recover and utilize 1-butene monomers. An efficient and low-energy consumption devolatilization technology is used to ensure the excellent performance of the product polybutene-1, while reducing the emission of waste gas. The device process is simple, easy to operate, and stable in operation. It has the advantages of small investment and low energy consumption. BRIEF DESCRIPTION OF THE DRAWINGS

[0039] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments are briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention, and for ordinary technicians in this field, other drawings can be obtained based on these drawings without creative work.

[0040] Figure 1 The schematic diagram shows the structure of a continuous production system of highly isotactic polybutene-1 according to one embodiment of the present invention.

[0041] The corresponding relationship between the component names and the reference numerals is as follows:

[0042] 1. Polymerization reactor; 2. Flash tank; 3. Distillation tower; 4. Water scrubber; 5. Devolatilizer; 6. Dryer; 7. First quenching unit; 8. Raw material pretreatment unit. DETAILED DESCRIPTION

[0043] The description of the embodiments of this specification should be combined with the corresponding drawings, which should be considered as part of the complete specification. In the drawings, the shape or thickness of the embodiments may be enlarged and indicated for simplification or convenience. Furthermore, the parts of each structure in the drawings will be described separately. It is worth noting that the elements not shown in the drawings or not described in words are in a form known to ordinary technicians in the relevant technical field.

[0044] The description of the embodiments herein and any reference to directions and orientations are only for the convenience of description and are not to be construed as any limitation on the scope of protection of the present invention. The following description of the preferred embodiments may involve combinations of features, which may exist independently or in combination, and the present invention is not particularly limited to the preferred embodiments. The scope of the present invention is defined by the claims.

[0045] like Figure 1 As shown, the present invention provides a continuous production system of highly isotactic polybutene-1, comprising a polymerization reactor 1, a pretreatment unit, a flash tank, a distillation tower, and a devolatilization and post-treatment unit.

[0046] A pretreatment unit is used to purify the materials entering the polymerization reactor;

[0047] The inlet of the flash tank 2 is connected to the outlet of the polymerization reactor 1, and is used for preliminary separation of unreacted polymerization monomers, reaction solvent and polybutene-1;

[0048] The inlet of the distillation tower 3 is connected to the top outlet of the flash tank 2, and the top outlet of the distillation tower 3 is connected to the inlet of the pretreatment unit through a monomer recovery pipeline; the bottom outlet of the distillation tower 3 is connected to the inlet of the pretreatment unit through a solvent recovery pipeline;

[0049] The inlet of the devolatilization and post-treatment unit is connected to the bottom outlet of the flash tank 2, and is used for devolatilization and post-treatment of the crude polybutene-1 rubber solution to obtain a highly isotactic polybutene-1 product.

[0050] Furthermore, the devolatilization and post-treatment unit includes a water scrubber 4 and a devolatilizer 5. The water scrubber 4 is connected to the bottom of the flash tank 2 and is used to wash the crude polybutene-1 rubber solution with water and recover the catalyst. The devolatilizer 5 is connected to the water scrubber 4 and uses hot nitrogen as the devolatilization medium to devolatilize and purify the crude polybutene-1 rubber solution after washing.

[0051] Furthermore, the devolatilization and post-processing unit also includes a washing and drying unit for washing and drying the devolatilized 1-butene rubber solution to obtain a pellet product;

[0052] Alternatively, the devolatilization and post-processing unit further comprises a dryer 6 for extruding the devolatilized 1-butene rubber solution to obtain a powder product.

[0053] Furthermore, the cleanliness requirement of the polymerization reactor is that the impurity content (such as water, oxygen, etc.) is less than 3 ppm; the operating temperature of the flash tank 2 is 80-120°C, preferably 90-100°C; the operating pressure of the flash tank 2 is 0-0.05MPaG, preferably 0-0.025MPaG; the operating temperature of the distillation tower 3 is 100-200°C, preferably 150°C; the operating pressure of the distillation tower 3 is 0.05-0.5MPaG, preferably 0-0.1MPaG; the operating temperature of the devolatilizer 5 is 100-200°C, and the operating pressure is 0-1.0MPaG, preferably 0-0.1MPaG.

[0054] Further, the pretreatment unit includes a first quenching unit 7 and a second quenching unit (not shown in the figure), a raw material pretreatment unit 8 and a solvent pretreatment unit (not shown in the figure). The first quenching unit 7 and the second quenching unit are used to quench the materials in the monomer recovery pipeline and the solvent recovery pipeline, respectively. The raw material pretreatment unit 8 is connected to the first quenching unit to remove impurities in the fresh liquid phase butene-1 and the recovered liquid phase butene-1. The solvent pretreatment unit is connected to the second quenching unit to remove impurities in the fresh reaction solvent and the recovered reaction solvent.

[0055] The present invention also provides a method for continuously producing highly isotactic polybutene-1, comprising the following steps:

[0056] With liquid butene-1 as polymerization monomer and hydrogen as molecular weight regulator, the polymerization monomer, reaction solvent, main catalyst, co-catalyst and external electron donor are sequentially added into a polymerization reaction kettle 1 in proportion and fully mixed, and then the molecular weight regulator is introduced to cause polymerization reaction;

[0057] After a period of reaction, part of the material in the polymerization reactor 1 is discharged and enters the flash tank 2 to separate the unpolymerized monomer, reaction solvent and polybutene-1;

[0058] Recovering the gaseous components containing unpolymerized monomers and reaction solvent from the top of the flash tank 2 to the distillation tower 3; recovering the unpolymerized monomers from the gaseous components at the top of the distillation tower 3, and recovering the reaction solvent from the bottom of the distillation tower 3;

[0059] Recovering crude polybutene-1 from the bottom of the flash tank 2, washing and devolatilizing to obtain a highly isotactic polybutene-1 product;

[0060] The recovered unpolymerized monomers and reaction solvent are purified and rapidly cooled together with the newly added polymerized monomers and reaction solvent, and then added into the polymerization reactor to participate in a new round of polymerization reaction.

[0061] Furthermore, the catalyst is a Ziegler-Natta catalyst system, including a main catalyst, a co-catalyst and an external electron donor; the reaction solvent is isopentane;

[0062] After releasing part of the materials, the reaction solvent was circulated back to the polymerization reactor 1 to maintain the polymer concentration in the polymerization reactor 1 at 30%wt.

[0063] Furthermore, the quenching gas temperature of the first quenching unit 7 and the second quenching unit is 30-50° C., preferably 35-45° C. The introduction of quenching gas helps to provide a relatively stable initial reaction temperature for the subsequent polymerization reaction, avoids the reaction runaway due to excessive temperature, and ensures the safety and controllability of the reaction.

[0064] Furthermore, the polymerization reaction temperature of the polymerization reactor 1 is 45-90°C, the pressure is 1.5-5.0MPaG, and the reaction time is 1.5-6 hours. Preferably, the reaction temperature is 60-70°C, the pressure is 2.0-3.0MPaG, and the average residence time (or average reaction time) is about 1-5h, preferably 2.0-3.0h.

[0065] Furthermore, the mass ratio of liquid phase butene-1 to the main catalyst is 40000-150000:1; the mass ratio of liquid phase butene-1 to the co-catalyst is 900-15000:1; the mass ratio of liquid phase butene-1 to the external electron donor is 30000-300000:1; the amount of liquid phase butene-1 to hydrogen is 1200-400000:1.

[0066] The components in the Ziegler-Natta catalyst system can be selected conventionally in the art. The Ziegler-Natta catalyst is TiCl4 supported on magnesium chloride, the co-catalyst is an aluminum compound, and the external electron donor is selected from one or more of silicon compounds, ethers and esters.

[0067] The Ziegler-Natta catalyst also contains a certain amount of internal electron donor to improve the stereoregularity of its product. The internal electron donor can be selected from at least one of 1,3-diketone, 1,3-diether, alkoxy ketone, succinate, 1,3-diol ester, 1,4-diol ester, 1,5-diol ester, hydroxy acid ester and higher phthalate ester.

[0068] The organic aluminum compound may be selected from an alkyl aluminum compound or an aluminum compound of an aluminoxane, and is preferably a trialkyl aluminum, and more preferably at least one of triethyl aluminum, triisobutyl aluminum and tri-n-butyl aluminum.

[0069] The external electron donor may be selected from at least one of alkoxysilanes, aminosilanes, organic amine compounds and ether compounds.

[0070] The technical solution of the present invention is described in detail below in conjunction with the accompanying drawings and embodiments.

[0071] Example 1

[0072] The high isoisobutene-1 continuous production system used is as follows Figure 1 shown.

[0073] The production process is as follows: the feed amount of liquid butene-1 is 5000 kg, the total feed amount of the subsequently supplemented liquid butene-1 and the liquid butene-1 entering the cycle after recovery is maintained at 5000 kg, the liquid butene-1 is quenched to 45°C by the first quenching heat exchanger 7, and then mixed with the main catalyst, co-catalyst, external electron donor and hydrogen in proportion and sent to the polymerization reactor 1, wherein the mass ratio of the main catalyst to butene-1 is 1:50000, the mass ratio of the co-catalyst to butene-1 is 1:1000, the mass ratio of the external electron donor to butene-1 is 1:100000, and the mass ratio of hydrogen to butene-1 is 1:3000. The polymerization operation temperature is 75°C, the operation pressure is 1.8MPaG, and the operation time is 3h. After the polymerization operation is completed, part of the polymerized glue in the polymerization reactor 1 is sent to the flash tank 2, the operating temperature of the flash tank 2 is 90°C and the operating pressure is 0.02MPaG, and the unreacted polymerization monomer butene-1 and the reaction solvent isopentane are removed to obtain high-purity polybutene-1 glue. The unreacted polymerization monomer butene-1 and the reaction solvent isopentane are separated in the distillation tower 3, the operating temperature of the distillation tower 3 is 150°C, and the operating pressure is 0.1MPaG, so as to achieve the separation of butene-1 and isopentane. The high-purity polybutene-1 glue is removed from the solid impurities by the water scrubber 4, and the light components are removed by the devolatilizer 5 at an operating temperature of 150°C and an operating pressure of 0.1MPaG to obtain the polybutene-1 product-grade glue, and then the dried polybutene-1 product.

[0074] The monomer polymerization degree of the polybutene-1 product prepared in this embodiment is 5000, the monomer utilization rate is 97%, and the recovery rate of the reaction solvent is 99%. At the same time, the discharge of waste is reduced, the device process is simple, easy to operate, and runs smoothly. The process equipment investment is small and the energy consumption is low.

[0075] Example 2

[0076] The high isoisobutene-1 continuous production system used is as follows Figure 1 shown.

[0077] The production process is as follows: the feed amount of liquid butene-1 is 5000kg, the total feed amount of the subsequently supplemented liquid butene-1 and the liquid butene-1 entering the cycle after recovery is maintained at 5000kg, the liquid butene-1 is quenched to 50°C by the first quenching heat exchanger 7, and then mixed with the main catalyst, co-catalyst, external electron donor and hydrogen in proportion and sent to the polymerization reactor 1, wherein the mass ratio of the main catalyst to butene-1 is 1:70000, the mass ratio of the co-catalyst to butene-1 is 1:1500, the mass ratio of the external electron donor to butene-1 is 1:150000, and the mass ratio of hydrogen to butene-1 is 1:3000. The polymerization operation temperature is 75°C, the operation pressure is 1.8MPaG, and the operation time is 3.5h. After the polymerization operation is completed, part of the polymerized glue in the polymerization reactor 1 is sent to the flash tank 2. The operating temperature of the flash tank 2 is 100°C and the operating pressure is 0.02MPaG. The unreacted polymerization monomer butene-1 and the reaction solvent isopentane are removed to obtain a high-purity polybutene-1 glue. The unreacted polymerization monomer butene-1 and the reaction solvent isopentane are separated in the distillation tower 3. The operating temperature of the distillation tower 3 is 150°C and the operating pressure is 0.1MPaG to achieve the separation of butene-1 and isopentane. The high-purity polybutene-1 glue is removed from the solid impurities by the water scrubber 4, and the light components are removed by the devolatilizer 5 at an operating temperature of 150°C and an operating pressure of 0.1MPaG to obtain a polybutene-1 product-grade glue, and then the dried polybutene-1 product.

[0078] The monomer polymerization degree of the polybutene-1 product prepared in this embodiment is 7000, the monomer utilization rate is 98%, and the recovery rate of the reaction solvent is 99%. At the same time, the discharge of waste is reduced, the device process is simple, easy to operate, and runs smoothly. The process equipment investment is small and the energy consumption is low.

[0079] Example 3

[0080] The high isoisobutene-1 continuous production system used is as follows Figure 1 shown.

[0081] The production process is as follows: the feed amount of liquid butene-1 is 5000 kg, the total feed amount of the subsequently supplemented liquid butene-1 and the liquid butene-1 entering the cycle after recovery is maintained at 5000 kg, the liquid butene-1 is quenched to 55° C. by the first quenching heat exchanger 7, and then mixed with the main catalyst, co-catalyst, external electron donor and hydrogen in proportion and sent to the polymerization reactor 1, wherein the mass ratio of the main catalyst to butene-1 is 1:80000, the mass ratio of the co-catalyst to butene-1 is 1:2000, the mass ratio of the external electron donor to butene-1 is 1:200000, and the mass ratio of hydrogen to butene-1 is 1:3000. The polymerization operation temperature is 75°C, the operation pressure is 1.8MPaG, and the operation time is 4h. After the polymerization operation is completed, part of the polymerized glue in the polymerization reactor 1 is sent to the flash tank 2. The operating temperature of the flash tank 2 is 100°C and the operating pressure is 0.02MPaG. The unreacted polymerization monomer butene-1 and the reaction solvent isopentane are removed to obtain a high-purity polybutene-1 glue. The unreacted polymerization monomer butene-1 and the reaction solvent isopentane are separated in the distillation tower 3. The operating temperature of the distillation tower 3 is 150°C and the operating pressure is 0.1MPaG to achieve the separation of butene-1 and isopentane. The high-purity polybutene-1 glue is removed from the solid impurities by the water scrubber 4, and the light components are removed by the devolatilizer 5 at an operating temperature of 150°C and an operating pressure of 0.1MPaG to obtain a polybutene-1 product-grade glue, and then the dried polybutene-1 product.

[0082] The monomer polymerization degree of the polybutene-1 product prepared in this embodiment is 8000, the monomer utilization rate is 98%, and the recovery rate of the reaction solvent is 99%. At the same time, the discharge of waste is reduced, the device process is simple, easy to operate, and runs smoothly. The process equipment investment is small and the energy consumption is low.

[0083] Finally, it should be noted that the above is a preferred embodiment of the present invention. It should be pointed out that although the preferred embodiment of the present invention has been described, for those skilled in the art, once the basic creative concept of the present invention is known, several improvements and modifications can be made without departing from the principles of the present invention, and these improvements and modifications should also be regarded as the protection scope of the present invention. Therefore, the attached claims are intended to be interpreted as including the preferred embodiment and all changes and modifications that fall within the scope of the embodiments of the present invention.

Claims

1. A method for continuous production of highly isoisobutene-1, characterized in that: The following steps are involved: Using liquid butene-1 as a polymerization monomer and hydrogen as a molecular weight regulator, the polymerization monomer, reaction solvent, main catalyst, co-catalyst and external electron donor are sequentially added into a polymerization reactor in proportion and fully mixed, and then the molecular weight regulator is introduced to cause a polymerization reaction; After a period of reaction, part of the materials in the polymerization reactor are discharged into a flash tank to separate the unpolymerized monomers, the reaction solvent and the polybutene-1; Recovering the gaseous components containing unpolymerized monomers and reaction solvent from the top of the flash tank to a distillation tower; recovering the unpolymerized monomers from the gaseous components at the top of the distillation tower, and recovering the reaction solvent from the bottom of the distillation tower; Recovering crude polybutene-1 from the bottom of the flash tank, and obtaining a highly isotactic polybutene-1 product after washing and devolatilization; The recovered unpolymerized monomers and the reaction solvent are added to the polymerization reactor after being purified and rapidly cooled together with the newly added polymerized monomers and the reaction solvent to participate in a new round of polymerization reaction.

2. The method for continuous production of highly isoisobutylene-1 according to claim 1, characterized in that: The catalyst is a Ziegler-Natta type catalyst, including a main catalyst, a co-catalyst and an external electron donor; the reaction solvent is isopentane; After releasing part of the materials, the reaction solvent was circulated back to the polymerization reactor to maintain the polymer concentration in the polymerization reactor at 30%wt.

3. The method for continuous production of highly isotactic polybutene-1 according to claim 1, characterized in that: The temperature of the quenching air for the quenching is 30-50°C.

4. The method for continuous production of highly isoisobutylene-1 according to claim 1, characterized in that: The polymerization reaction kettle has a polymerization reaction temperature of 45-90° C., a pressure of 1.5-5.0 MPaG, and a reaction time of 1.5-6 hours.

5. The method for continuous production of highly isoisobutylene-1 according to claim 1, characterized in that: The mass ratio of the liquid phase butene-1 to the main catalyst is 40000-150000:1; the mass ratio of the liquid phase butene-1 to the co-catalyst is 900-15000:1; the mass ratio of the liquid phase butene-1 to the external electron donor is 30000-300000:1; the amount of the liquid phase butene-1 to the hydrogen is 1200-400000:

1.

6. A continuous production system of highly isoisobutene-1, characterized in that: The method for continuously producing highly isoisobutylene-1 according to any one of claims 1 to 5 comprises a polymerization reactor, and further comprises: A pretreatment unit, used for purifying the materials entering the polymerization reactor; A flash tank, the inlet of which is connected to the outlet of the polymerization reactor, and is used for preliminarily separating unreacted polymerization monomers, reaction solvent and polybutene-1; A distillation tower, whose inlet is connected to the top outlet of the flash tank, whose top outlet is connected to the inlet of the pretreatment unit through a monomer recovery pipeline; and whose bottom outlet is connected to the inlet of the pretreatment unit through a solvent recovery pipeline; The devolatilization and post-treatment unit has an inlet connected to the bottom outlet of the flash tank and is used for devolatilization and post-treatment of the crude polybutene-1 rubber solution to obtain a highly isotactic polybutene-1 product.

7. The system according to claim 6, characterized in that The devolatilization and post-treatment unit comprises: A water washer connected to the bottom of the flash tank and used to wash the crude polybutene-1 glue solution with water to recover the catalyst; The devolatilizer is connected to the water scrubber and uses hot nitrogen as the devolatilization medium to devolatilize and purify the crude polybutene-1 rubber solution after washing.

8. The system according to claim 7, characterized in that The devolatilization and post-processing unit also includes a washing and drying unit for washing and drying the devolatilized 1-butene rubber solution to obtain a pellet product; Alternatively, the devolatilization and post-processing unit further comprises a dryer for extruding the devolatilized 1-butene rubber solution to obtain a powder product.

9. The system according to claim 7, characterized in that The cleanliness requirement of the polymerization reactor is that the impurity content is less than 3 ppm; The operating temperature of the flash tank is 80-120°C and the operating pressure is 0-0.05MpaG; The operating temperature of the distillation tower is 100-200°C and the operating pressure is 0.05-0.5MpaG; The operating temperature of the devolatilizer is 100-200°C, and the operating pressure is 0-1.0MpaG.

10. The system according to claim 6, characterized in that The pre-processing unit comprises: The first quenching unit and the second quenching unit are used to quench the materials in the monomer recovery pipeline and the solvent recovery pipeline respectively; A raw material pretreatment unit connected to the first quenching unit, used to remove impurities in fresh liquid phase butene-1 and recovered liquid phase butene-1; The solvent pretreatment unit is connected to the second quenching unit and is used to remove impurities in the fresh reaction solvent and the recovered reaction solvent.

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