SIBS cyclone agglomeration method and device

Abstract

The present disclosure relates to a SIBS cyclone coagulation method and apparatus, providing a SIBS cyclone coagulation method comprising the following steps: (A) monomer refining using a microchannel separator and a shaped coalescer; (B) polymerization in a microchannel reactor; (C) cyclone dynamic mixing and blending; (D) cyclone separation and coagulation; (E) solution refining; and (F) post-processing. Also provided is a SIBS cyclone coagulation apparatus. The present disclosure utilizes cyclone coagulation technology to not only optimize the production process and reduce production energy consumption, but also improve product quality, achieving the goal of high-efficiency and low-consumption production.

Description

Technical Field

[0001] The present disclosure belongs to the field of polymer material technology, relates to a method for preparing SIBS, and more particularly to a method and apparatus for preparing SIBS by using cyclone coagulation technology. Specifically, the present disclosure provides a method and apparatus for preparing SIBS by using cyclone coagulation technology. Background Art

[0002] The new thermoplastic rubber, SIBS (integrated elastomer), is composed of a tetrablock copolymer of styrene, isoprene, butadiene, and cyclohexane. The middle block is polyisoprene with a methyl side chain. Its unique triblock molecular structure imparts excellent cohesion, adhesion, and compatibility. As a polymer material, SIBS combines the high elasticity of vulcanized rubber with the plasticity of plastic. In recent years, my country has strongly supported the polymer materials and emerging adhesives industries, and SIBS hot-melt pressure-sensitive adhesives have become one of the fastest-growing products in the hot-melt adhesive market.

[0003] SIBS possesses excellent adhesion, and related products have been widely used in adhesives, coatings, and plastic modification. Demand for SIBS materials is rapidly increasing in production and daily life. However, the current SIBS production process is plagued by complex production processes, high energy consumption, high equipment construction and management costs, and low equipment utilization efficiency. Mass production results in significant waste of resources and energy.

[0004] In the traditional SIBS preparation process, a three-reactor coagulation process with hydrolysis is usually used to coagulate the glue. However, since this process is a three-stage reaction and requires multiple reactors, the process continuity is poor, the production cycle is long, and the equipment utilization rate is low.

[0005] The SIBS preparation process is generally plagued by high energy consumption, low efficiency, high processing costs, and poor production continuity. The existing three-reactor coagulation process based on hydrolysis cannot meet the requirements for high efficiency and low consumption. Therefore, there is an urgent need to develop a highly efficient, environmentally friendly, energy-saving, and continuous SIBS preparation process. Summary of the Invention

[0006] The present disclosure provides a novel SIBS cyclone coagulation method and apparatus, thereby solving the problems of poor process continuity, low equipment utilization and high energy consumption in the prior art.

[0007] In one aspect, the present disclosure provides a SIBS cyclone agglomeration method, the method comprising the following steps:

[0008] (A) Monomer Refining Based on a Microchannel Separator and Shape Coalescer: Crude styrene, crude isoprene, crude butadiene, and crude cyclohexane raw materials are added to a monomer refining unit composed of a microchannel separator and a shape coalescer to remove impurities therein and obtain refined raw materials;

[0009] (B) Microchannel reactor polymerization: the refined raw material obtained in step (A) is added to a microchannel reactor. After the reaction is completed, the generated glue is added to a glue buffer tank, and then extracted by a micro-droplet extraction tank containing an antioxidant;

[0010] (C) Cyclone dynamic mixing and blending: adding the extracted rubber solution obtained in step (B) into a dynamic blending tank and stirring and blending uniformly;

[0011] (D) Cyclone separation and coagulation: The uniformly mixed adhesive obtained in step (C) is added to a cyclone classifier, and the adhesive is coagulated by cyclone separation, and the adhesive particles are separated from the adhesive through the coagulation process; wherein the accuracy of the cyclone classifier is 0.1 mm;

[0012] (E) Solution purification: recovering the solvent used in the cyclone fractionator in step (D) and recycling it after treatment; and

[0013] (F) Post-processing: The condensed particles obtained in step (D) are added to a non-phase change drying system. The particles enter a cyclone separator for rotation to achieve drying. The particles in the product packaging silo enter the packaging system to obtain the final product SIBS.

[0014] In a preferred embodiment, in step (A), the separation accuracy of the microchannel separator reaches 100 nm, and the volumetric accuracy of the raw material is improved by two orders of magnitude year-on-year; the water reuse rate during the treatment process of the microchannel separator reaches 99%; and the accuracy of the crude raw material after treatment by the microchannel separator exceeds 98.5%, and the water content is reduced to less than 20 ppm, based on the weight of the crude raw material.

[0015] In another preferred embodiment, in step (A), the weight ratio of the crude styrene, crude isoprene, crude butadiene and crude cyclohexane is: 1: 1-10: 1-10: 20-30.

[0016] In another preferred embodiment, in step (B), the refined raw material obtained in step (A) is added to a microchannel reactor in a weight ratio of styrene: isoprene: butadiene: cyclohexane = 1: 2-5: 2-5: 24-26; the reaction pressure of the microchannel reactor is 0.05-0.5 MPa, the reaction temperature is 50-130°C, and the reaction time is 20-110 min.

[0017] In another preferred embodiment, in step (B), the styrene conversion rate reaches 99.1%, the isoprene conversion rate reaches 99.75%, and the concentration of the gum obtained by the reaction is 15%-20%.

[0018] In another preferred embodiment, in step (C), the dynamic blending tanks are connected in series.

[0019] In another preferred embodiment, in step (D), the cyclone separator is provided with a liquid inlet, a gas outlet, and a product outlet; the rubber liquid is carried into the cyclone separator by a conveying medium, and the rubber particles with a particle size of less than 0.1 mm enter the conveying medium and are discharged from the overflow port of the cyclone separator. The rubber particles are then separated from the conveying medium by a filtering separation device, and the rubber particles with a particle size greater than 1 mm are discharged from the bottom of the cyclone separator for treatment and recycling; the operating temperature of the cyclone separation and coagulation process is 90-115° C., and the solid content of the rubber particles after cyclone separation and coagulation is 30%-50%.

[0020] In another preferred embodiment, the separation accuracy of the filtering and separating device is 0.01 mm, and the colloidal particles separated in step (D) are separated from the conveying medium, thereby realizing the recycling of the conveying medium.

[0021] In another preferred embodiment, in step (E), the condensed colloid particles are added to the cyclone separator of the non-phase change drying system for rotation, and the rotation speed of the particles in the cyclone separator is 15,000-60,000 rpm; the granules in the product packaging silo are fed into the packaging system and subjected to metering, sewing, sealing, metal inspection, re-inspection, palletizing, and finished product storage to obtain the final product SIBS elastomer, which has a molecular weight of 80,000-150,000 and a melt index of 0.1-30.0; the non-phase change drying system uses hydrogen, nitrogen or steam as a carrier gas, and utilizes the rotation of the colloid particles in the cyclone rotator to remove the transport medium and moisture in the colloid particles, thereby achieving drying of the colloid particles; when the carrier gas temperature is 40°C-70°C, the moisture content of the colloid particles after drying is less than 10%; the operating pressure of the non-phase change drying process is 0.1MPa-0.3MPa.

[0022] In another aspect, the present disclosure provides a SIBS cyclone coagulation device, comprising:

[0023] A monomer refining unit consisting of a microchannel reactor and a shape coalescer connected thereto is used to carry out the monomer refining based on the microchannel separator and the shape coalescer in step (A): crude styrene, crude isoprene, crude butadiene and crude cyclohexane raw materials are added to the monomer refining unit consisting of the microchannel separator and the shape coalescer to remove impurities therein to obtain refined raw materials;

[0024] A microchannel reactor connected to the shape coalescer, a glue buffer tank connected to the microchannel reactor, and a micro-droplet extraction tank connected to the glue buffer tank are used to carry out step (B) microchannel reactor polymerization: the refined raw material obtained in step (A) is added to the microchannel reactor, and after the reaction is completed, the generated glue is added to the glue buffer tank, and then extracted by a micro-droplet extraction tank containing an antioxidant;

[0025] The dynamic blending tank connected to the micro-droplet extraction tank is used to perform the cyclone dynamic mixing and blending in step (C): adding the extracted rubber solution obtained in step (B) into the dynamic blending tank and stirring and blending uniformly;

[0026] The cyclone classification separator connected to the dynamic blending tank is used to perform step (D) cyclone separation and coagulation: adding the uniformly blended glue obtained in step (C) to the cyclone classification separator, adopting cyclone separation to coagulate the glue, and separating the glue particles from the glue through the coagulation process; wherein the accuracy of the cyclone classification separator is 0.1mm; and step (E) solution refining: recovering the solvent used in the cyclone classification separator in step (D), and recycling it after treatment; and

[0027] The non-phase-change drying system connected to the cyclone classifier and the packaging system connected to the non-phase-change drying system are used to perform post-processing in step (F): the agglomerated colloid particles obtained in step (D) are added to the non-phase-change drying system, the colloid particles enter the cyclone separator for rotation to achieve colloid particle drying, and the granules in the product packaging silo enter the packaging system to obtain the final product SIBS. Beneficial effects

[0028] The main advantages of the method and apparatus disclosed herein are:

[0029] (1) The disclosed method uses cyclone separation and coagulation, utilizing the density difference between substances and centrifugal force to separate. In the cyclone fractionator, the contact area of the reactants is large and they are easier to mix evenly, so the reaction efficiency is high. At the same time, its processing energy consumption is only 1 / 5 of the three-pot coagulation process of the water separation method.

[0030] (2) The three-reactor condensation process used in the prior art is a three-stage reaction. Because multiple reactors are required, the process continuity is poor, the production cycle is long, and the equipment utilization rate is low. Since the cyclone separation and condensation used in the method disclosed herein is a continuous reaction process, the production efficiency is high, thus shortening the production cycle and improving the equipment utilization rate.

[0031] (3) The disclosed method can effectively reduce the operating cost of the process, save resources and protect the environment. BRIEF DESCRIPTION OF THE DRAWINGS

[0032] The accompanying drawings are used to provide further understanding of the present disclosure. They only constitute a part of this specification and are used to further explain the present disclosure, but do not constitute a limitation of the present disclosure.

[0033] Figure 1 It is a schematic diagram of the overall process flow of the SIBS cyclone agglomeration method according to a preferred embodiment of the present disclosure.

[0034] Figure 2 It is a structural schematic diagram of a cyclone fractionating separator according to a preferred embodiment of the present disclosure.

[0035] Reference numerals:

[0036] 1: Microchannel separator

[0037] 2: Shape Coalescer

[0038] 3: Microchannel reactor (3-1, 3-2, 3-3, 3-4)

[0039] 4: Glue buffer tank

[0040] 5: Micro-droplet extraction tank

[0041] 6: Dynamic mixing tank

[0042] 7: Cyclone Classification Separator

[0043] 8: Non-phase change drying system

[0044] 9: Packaging system

[0045] 10: Refining Tower (10-1, 10-2)

[0046] 11: Condenser

[0047] 12: Tundish

[0048] 13: Reflux tank

[0049] 14: Heavy component storage tank

[0050] 15: Butadiene product tank

[0051] 16: Deweighting Tower

[0052] 17: Isoprene product tank

[0053] 18: Refined solvent tank

[0054] 19: Separation tank

[0055] 20: Exhaust gas condenser

[0056] 21: Stripping unit mixer

[0057] 22: Dehydration extruder

[0058] 23: Hot water tank

[0059] 24: Dewatering screen

[0060] 101: Product Pipeline

[0061] 102: Bottom flow mouth

[0062] 103: Fixed plate

[0063] 104: Cone segment

[0064] 105: Column segment

[0065] 106: Overflow pipe

[0066] 107: Sewage pipe DETAILED DESCRIPTION

[0067] The endpoints of the ranges and any values disclosed herein are not limited to the precise ranges or values, and these ranges or values should be understood to include values close to these ranges or values. For numerical ranges, the endpoints of each range, the endpoints of each range and individual point values, and the individual point values can be combined with each other to obtain one or more new numerical ranges, which should be considered to be specifically disclosed herein.

[0068] After extensive and in-depth research, the applicants discovered that the existing SIBS production process suffers from poor process continuity, low equipment utilization, and high energy consumption. However, the use of cyclone coagulation technology not only optimizes the production process and reduces energy consumption, but also improves product quality, achieving the goal of high-efficiency and low-energy production. Based on these findings, the present invention was completed.

[0069] In a first aspect of the present disclosure, a SIBS cyclone agglomeration method is provided, the method comprising the following steps:

[0070] (A) Monomer Refining Based on a Microchannel Separator and Shape Coalescer: Crude styrene, crude isoprene, crude butadiene, and crude cyclohexane raw materials are added to a monomer refining unit composed of a microchannel separator and a shape coalescer to remove impurities therein and obtain refined raw materials;

[0071] (B) Microchannel reactor polymerization: the refined raw material obtained in step (A) is added to a microchannel reactor. After the reaction is completed, the generated glue is added to a glue buffer tank, and then extracted by a micro-droplet extraction tank containing an antioxidant;

[0072] (C) Cyclone dynamic mixing and blending: adding the extracted rubber solution obtained in step (B) into a dynamic blending tank and stirring and blending uniformly;

[0073] (D) Cyclone separation and coagulation: The uniformly mixed adhesive obtained in step (C) is added to a cyclone classifier, and the adhesive is coagulated by cyclone separation, and the adhesive particles are separated from the adhesive through the coagulation process;

[0074] (E) Solution purification: recovering the solvent used in the cyclone fractionator in step (D) and recycling it after treatment; and

[0075] (F) Post-processing: The condensed particles obtained in step (D) are added to a non-phase change drying system. The particles enter a cyclone separator for rotation to achieve drying. The particles in the product packaging silo enter the packaging system to obtain the final product SIBS.

[0076] In the present disclosure, in step (A), the separation accuracy of the microchannel separator reaches 100 nm, and the volume accuracy of the raw material is improved by two orders of magnitude year-on-year.

[0077] In the present disclosure, in step (A), the water reuse rate during the microchannel separator treatment process reaches 99%; the accuracy of the crude raw material after treatment by the microchannel separator exceeds 98.5%, and the water content is reduced to below 20 ppm, based on the weight of the crude raw material.

[0078] In the present disclosure, in step (A), the weight ratio of crude styrene, crude isoprene, crude butadiene and crude cyclohexane is: 1: 1-10: 1-10: 20-30, preferably 1: 8: 1.5: 25.

[0079] In the present disclosure, in step (B), the refined raw material obtained in step (A) is added to the microchannel reactor in a weight ratio of styrene: isoprene: butadiene: cyclohexane = 1: 2-5: 2-5: 24-26.

[0080] In the present disclosure, in step (B), the microchannel reactor is a multi-channel small reactor with a heat transfer characteristic that is 1-3 orders of magnitude better than that of traditional equipment.

[0081] In the present disclosure, in step (B), the reaction pressure of the microchannel reactor is 0.05-0.5 MPa, the reaction temperature is 50-130° C., and the reaction time is 20-110 min.

[0082] In the present disclosure, in step (B), the styrene conversion rate reaches 99.1%, the isoprene conversion rate reaches 99.75%, and the concentration of the gum obtained by the reaction is 15%-20%.

[0083] In the present disclosure, in step (C), the dynamic blending tanks are connected in series, which increases the blending capacity and can maximize the blending efficiency.

[0084] In the present disclosure, in step (D), the cyclone separation and coagulation is a low-energy separation technology, and the processing energy consumption is 1 / 5 of the three-kettle coagulation process of the water analysis method; the cyclone classification separator has a simple structure, and the initial investment cost is 1 / 3 of the original process, which reduces the initial investment and operation and management costs.

[0085] In the present disclosure, in step (D), the cyclone classifier is a device that uses density differences between substances and centrifugal force to perform separation, and is provided with a liquid inlet, a gas outlet, and a product outlet.

[0086] In the present disclosure, in step (D), the accuracy of the cyclone separator is 0.1 mm, the rubber liquid is carried into the cyclone separator by the conveying medium, and the rubber particles with a particle size of less than 0.1 mm enter the conveying medium and are discharged from the overflow port of the cyclone separator. The rubber particles are then separated from the conveying medium by a filtering separation device, and the rubber particles with a particle size greater than 1 mm are discharged from the bottom of the cyclone separator for processing and recycling.

[0087] In the present disclosure, in step (D), the separation accuracy of the filtering and separating device is 0.01 mm, and the colloidal particles separated in step (D) are separated from the conveying medium, thereby realizing the recycling of the conveying medium.

[0088] In the present disclosure, in step (D), the operating temperature of the cyclone separation and coagulation process is 80-120°C, such as 80°C, 90°C, 100°C, 110°C, 120°C, preferably 90-115°C.

[0089] In the present disclosure, in step (D), the solid content of the colloidal particles after cyclone separation and coagulation is 30%-50%, for example, 30%, 33%, 35%, 40%, 44%, 46%, 48%, 50%.

[0090] In the present disclosure, in step (E), the agglomerated colloidal particles are added to a cyclone separator of a non-phase change drying system for rotation, and the rotation speed of the particles in the cyclone separator is 15,000-60,000 rpm.

[0091] In the present disclosure, in step (E), the pellets in the product packaging silo enter the packaging system and are then metered, sewn, sealed, metal inspected, re-inspected, palletized, and the finished products are put into storage to obtain the final product SIBS elastomer, which has a molecular weight of 80,000-150,000 and a melt index of 0.1-30.0.

[0092] In the present disclosure, in step (E), the non-phase change drying system uses hydrogen, nitrogen or steam as a carrier gas, and utilizes the rotation of the colloid particles in a cyclone to remove the transport medium and moisture in the colloid particles, thereby achieving drying of the colloid particles; when the carrier gas temperature is 40°C-70°C, the moisture content of the colloid particles after drying is less than 10%.

[0093] In the present disclosure, in step (E), the operating pressure of the non-phase change drying process is 0.1 MPa-0.7 MPa, such as 0.1 MPa, 0.16 MPa, 0.20 MPa, 0.25 MPa, 0.30 MPa, 0.35 MPa, preferably 0.1 MPa-0.3 MPa.

[0094] In a second aspect of the present disclosure, a SIBS cyclone coagulation device is provided, the device comprising:

[0095] A monomer refining unit consisting of a microchannel reactor and a shaped coalescer connected thereto, for carrying out the above step (A);

[0096] A microchannel reactor connected to the shape coalescer, a glue buffer tank connected to the microchannel reactor, and a micro-droplet extraction tank connected to the glue buffer tank are used to perform the above step (B);

[0097] A dynamic blending tank connected to the micro-droplet extraction tank, used to perform the above step (C);

[0098] A cyclone classifier connected to the dynamic blending tank, used to perform the above steps (D) and (E); and

[0099] The non-phase-change drying system connected to the cyclone fractionator and the packaging system connected to the non-phase-change drying system are used to perform the above step (F).

[0100] Please refer to the accompanying drawings below.

[0101] Figure 1 FIG. 1 is a schematic diagram of the overall process flow of the SIBS cyclone agglomeration method according to a preferred embodiment of the present disclosure. Figure 1As shown, crude styrene, crude butadiene, crude isoprene, and crude cyclohexane raw materials are respectively added to a styrene refining unit, a butadiene refining unit, an isoprene refining unit, and a cyclohexane refining unit consisting of a microchannel separator 1 and a shape coalescer 2 connected thereto; wherein, the styrene produced in the styrene refining unit is directly pumped from its shape coalescer 2 to the microchannel reactor 3; the butadiene produced in the butadiene refining unit is pumped from its shape coalescer 2 to the refining tower 10, the refined light component is discharged from the top of the refining tower 10 and sent to the condenser 11 for condensation and then sent to the intermediate tank 12, the refined heavy component is discharged from the bottom of the refining tower 10 and sent to the heavy component storage tank 14, the refined butadiene is sent to the reflux tank 13, the reflux is refluxed to the refining tower 10, the butadiene is sent to the butadiene product tank 15, and then pumped to the microchannel reactor 3; the isoprene produced in the isoprene refining unit is pumped from its shape coalescer 2 to the refining tower 10, and the isoprene produced in the isoprene refining unit is pumped from its shape coalescer 2 to the refining tower 10. The cyclohexane produced by the cyclohexane refining unit is sent to the refining tower 10-1 from its shape coalescer 2, and the light component obtained by the refinement is discharged from the top of the refining tower 10-1 and sent to the condenser 11 for condensation and then sent to the reflux tank 13. Part of the components are refluxed to the cyclohexane refining unit 16, and the isoprene is sent to the isoprene product tank 17, and then pumped to the microchannel reactor 3. The cyclohexane produced by the cyclohexane refining unit is sent to the refining tower 10-1 from its shape coalescer 2, and the light component obtained by the refinement is discharged from the top of the refining tower 10-1 and sent to the condenser 11 for condensation and then sent to the reflux tank 13. Enter the reflux tank 13, the light component is discharged from the top of the reflux tank 13 and sent to the condenser 11 for condensation and then sent to the fine solvent tank 18, part of the components are refluxed to the refining tower 10-1, and the cyclohexane is sent to the refining tower 10-2 to remove the heavy components at the bottom of the tower, and the light component is discharged from the top of the refining tower 10-2 and sent to the condenser 11 for condensation and then sent to the reflux tank 13, part of the components are refluxed to the refining tower 10-2, and the cyclohexane is sent to the fine solvent tank 18, and then pumped to the microchannel reactor 3;

[0102] The glue produced by the microchannel reactor groups 3-1, 3-2, 3-3, and 3-4 is sent to the glue buffer tank 4, and then extracted by the micro-droplet extraction tank 5 containing an antioxidant. The gas phase is discharged from the top of the glue buffer tank 4 and sent to the separation tank 19. The separated gas phase is sent to the tail gas condenser 20. The condensed liquid phase is sent to the shape coalescer 2 and then refined and sent to the cyclone classifier 7 for separation. The obtained product is sent to the reflux tank 13, and then screened by the dehydration screen 24 and sent to the dehydration extruder 22 for extrusion and then sent to the non-phase change drying system 8 to achieve the removal of moisture on the surface and in the pores of the glue particles, and the residual water is removed by RTO treatment. The pellets in the product packaging silo are The final SIBS product is obtained by entering the packaging system 9 for metering, sewing, sealing, metal inspection, re-inspection, palletizing, and storage of finished products; the slag liquid discharged from the separation tank 19 is sent to the shape coalescer 2; the glue liquid extracted by the micro-droplet extraction tank 5 enters the dynamic blending tank 6, and after stirring and blending, the gas phase is discharged from the top and sent to the tail gas condenser 20. The liquid phase is mixed by the stripping unit mixer 29 and then enters the cyclone classification separator 7 for cyclone separation of glue particles; the water removed by the dewatering screen 24 and the dewatering extruder 22 is sent to the hot water tank 23 and then to the shape coalescer 2; the hot water in the hot water tank 23 is added with dispersant and returned to the stripping unit mixer 29.

[0103] Figure 2 Schematic diagram of the structure of a cyclone fractionating separator according to a preferred embodiment of the present disclosure. Figure 2 As shown, the cyclone classifying separator includes: a product pipeline 101, an underflow port 102, a fixed plate 103, a cone section 104, a column section 105, an overflow pipe 106, and a sewage pipe 107. Example

[0104] The present invention will be further described below with reference to specific examples. However, it should be understood that these examples are intended to illustrate the present invention only and are not intended to limit the scope of the invention. The test methods in the following examples, where specific conditions are not specified, were generally performed under conventional conditions or as recommended by the manufacturer. Unless otherwise indicated, all percentages and parts are by weight. Example

[0105] 1. Device Name

[0106] 40kg / h elastomer pilot production unit

[0107] 2. Process

[0108] like Figure 1 shown.

[0109] The material addition control ratio is shown in Table 1 below.

[0110] Table 1: Material addition control ratio

[0111]

[0112] Implementation Effect

[0113] The process analysis data are shown in Table 2 below.

[0114] Table 2: Process analysis data

[0115]

[0116]

[0117] The above analysis data demonstrates that the method of the present invention achieves all process parameters within control requirements, and the resulting rubber product meets the physical and chemical specifications required by the market. The yield of the finished rubber product exceeds 99%, with an isoprene conversion rate of 99.5%, a styrene conversion rate of 99.5%, and a butadiene conversion rate of 99.3%.

[0118] The above-listed embodiments are merely preferred embodiments of the present disclosure and are not intended to limit the scope of implementation of the present disclosure. That is, any equivalent changes and modifications made based on the content of the patent application should fall within the technical scope of the present disclosure.

[0119] All documents mentioned in this disclosure are incorporated herein by reference, just as if each document were incorporated herein by reference individually. It should also be understood that after reading the above teachings of this disclosure, those skilled in the art may make various changes or modifications to this disclosure, and that such equivalents also fall within the scope of the claims appended hereto.

Claims

1. A SIBS cyclone coagulation method, the method comprising the following steps: (A) Monomer Refining Based on a Microchannel Separator and Shape Coalescer: Crude styrene, crude isoprene, crude butadiene, and crude cyclohexane raw materials are added to a monomer refining unit composed of a microchannel separator and a shape coalescer to remove impurities therein and obtain refined raw materials; (B) Microchannel reactor polymerization: the refined raw material obtained in step (A) is added to a microchannel reactor. After the reaction is completed, the generated glue is added to a glue buffer tank, and then extracted by a micro-droplet extraction tank containing an antioxidant; (C) Cyclone dynamic mixing and blending: adding the extracted rubber solution obtained in step (B) into a dynamic blending tank and stirring and blending uniformly; (D) Cyclone separation and coagulation: The uniformly mixed adhesive obtained in step (C) is added to a cyclone classifier, and the adhesive is coagulated by cyclone separation, and the adhesive particles are separated from the adhesive through the coagulation process; wherein the accuracy of the cyclone classifier is 0.1 mm; (E) Solution purification: recovering the solvent used in the cyclone fractionator in step (D) and recycling it after treatment; and (F) Post-processing: The condensed particles obtained in step (D) are added to a non-phase change drying system. The particles enter a cyclone separator for rotation to achieve drying. The particles in the product packaging silo enter the packaging system to obtain the final product SIBS.

2. The method according to claim 1, wherein In step (A), the separation accuracy of the microchannel separator reaches 100 nm; the water reuse rate during the treatment process of the microchannel separator reaches 99%; the accuracy of the crude raw material after treatment by the microchannel separator exceeds 98.5%, and the water content is reduced to below 20 ppm, based on the weight of the crude raw material.

3. The method according to claim 1, wherein In step (A), the weight ratio of the crude styrene, crude isoprene, crude butadiene and crude cyclohexane is: 1: 1-10: 1-10: 20-30.

4. The method according to claim 1, wherein In step (B), the refined raw material obtained in step (A) is added to a microchannel reactor in a weight ratio of styrene: isoprene: butadiene: cyclohexane = 1: 2-5: 2-5: 24-26; the reaction pressure of the microchannel reactor is 0.05-0.5 MPa, the reaction temperature is 50-130°C, and the reaction time is 20-110 min.

5. The method according to claim 1, wherein In step (B), the styrene conversion rate reaches 99.1%, the isoprene conversion rate reaches 99.75%, and the concentration of the rubber solution obtained by the reaction is 15%-20%.

6. The method according to claim 1, wherein In step (C), the dynamic blending tanks are connected in series.

7. The method according to claim 1, wherein In step (D), the cyclone separator is provided with a liquid inlet, a gas outlet, and a product outlet; the rubber liquid is carried into the cyclone separator by a conveying medium, and the rubber particles with a particle size of less than 0.1 mm enter the conveying medium and are discharged from the overflow port of the cyclone separator. The rubber particles are then separated from the conveying medium by a filtering separation device, and the rubber particles with a particle size greater than 1 mm are discharged from the bottom of the cyclone separator for treatment and recycling; the operating temperature of the cyclone separation and coagulation process is 90-115° C., and the solid content of the rubber particles after cyclone separation and coagulation is 30%-50%.

8. The method according to claim 7, wherein The separation accuracy of the filtering and separating device is 0.01 mm, and the colloidal particles separated in step (D) are separated from the conveying medium, thereby realizing the recycling of the conveying medium.

9. The method according to claim 1, wherein In step (E), the condensed colloid particles are added to the cyclone separator of the non-phase change drying system for rotation, and the rotation speed of the particles in the cyclone separator is 15,000-60,000 rpm; the granules in the product packaging silo are fed into the packaging system and subjected to metering, sewing, sealing, metal inspection, re-inspection, palletizing, and finished product storage to obtain the final product SIBS elastomer, which has a molecular weight of 80,000-150,000 and a melt index of 0.1-30.0; the non-phase change drying system uses hydrogen, nitrogen or steam as a carrier gas, and utilizes the rotation of the colloid particles in the cyclone rotator to remove the transport medium and moisture in the colloid particles, thereby achieving drying of the colloid particles; when the carrier gas temperature is 40°C-70°C, the moisture content of the colloid particles after drying is less than 10%; the operating pressure of the non-phase change drying process is 0.1MPa-0.3MPa.

10. A SIBS cyclone coagulation device, comprising: A monomer refining unit consisting of a microchannel separator (1) and a shape coalescer (2) connected thereto is used to carry out step (A) of monomer refining based on the microchannel separator and the shape coalescer: crude styrene, crude isoprene, crude butadiene and crude cyclohexane raw materials are added to the monomer refining unit consisting of the microchannel separator and the shape coalescer to remove impurities therein and obtain refined raw materials; The microchannel reactor (3) connected to the shape coalescer (2), the glue buffer tank (4) connected to the microchannel reactor (3), and the micro-droplet extraction tank (5) connected to the glue buffer tank (4) are used to carry out step (B) microchannel reactor polymerization: the refined raw material obtained in step (A) is added to the microchannel reactor, and after the reaction is completed, the generated glue is added to the glue buffer tank, and then extracted by a micro-droplet extraction tank containing an antioxidant; The dynamic blending tank (6) connected to the micro-droplet extraction tank (5) is used to perform the cyclone dynamic mixing and blending in step (C): adding the extracted glue obtained in step (B) into the dynamic blending tank, stirring and blending uniformly; The cyclone classification separator (7) connected to the dynamic blending tank (6) is used to perform step (D) cyclone separation and coagulation: adding the uniformly mixed glue obtained in step (C) to the cyclone classification separator, adopting the cyclone separation method to coagulate the glue, and separating the glue particles from the glue through the coagulation process; wherein the accuracy of the cyclone classification separator is 0.1mm; and step (E) solution refining: recovering the solvent used in the cyclone classification separator in step (D), and recycling it after treatment; and The non-phase-change drying system (8) connected to the cyclone classifier (7) and the packaging system (9) connected to the non-phase-change drying system (8) are used to perform post-processing in step (F): the condensed colloid particles obtained in step (D) are added to the non-phase-change drying system, the colloid particles enter the cyclone separator for rotation to achieve colloid particle drying, and the granules in the product packaging silo enter the packaging system to obtain the final product SIBS.

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