SIBS swirl strengthening method and device

Abstract

The present disclosure relates to a method and apparatus for SIBS cyclone enhancement, including a method for SIBS cyclone enhancement, 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; and (E) post-processing. A SIBS cyclone enhancement apparatus is also provided. The method provided herein has a short process flow, requires minimal equipment, is highly efficient and low-cost, reduces pollutant emissions, and produces a high-quality product suitable for industrial 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 swirl strengthening of SIBS. Specifically, the present disclosure provides a method and apparatus for preparing SIBS using swirl strengthening technology. Background Art

[0002] The new thermoplastic rubber SIBS (i.e., integrated elastomer) is the third generation of rubber after natural rubber and synthetic rubber. SIBS is composed of styrene, isoprene, butadiene, and cyclohexane. As a polymer material, it combines the high elasticity of vulcanized rubber with the plasticity of plastic. Its special four-block molecular structure gives it excellent cohesion, excellent adhesion, and good compatibility.

[0003] SIBS possesses excellent adhesion, and related products are primarily used in adhesives, coatings, and plastic modification. Pressure-sensitive adhesives and hot-melt adhesives based on SIBS are widely used in medical applications, electrical insulation, packaging, protection, masking, marking, bonding, and interlayer adhesion in composite bags. Demand for SIBS materials is rapidly increasing in production and daily life, but the current SIBS production process is plagued by complex 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] Currently, many companies use distillation to improve the accuracy of raw materials during the production process. However, due to the complexity of the entire process equipment, large space occupation, and high energy consumption, it is unable to solve the current problems of high production costs and low refining efficiency.

[0005] In industrial production, in order to further dry the colloid particles, heating evaporation is often used. By providing sufficient heat to overcome the latent heat of vaporization of water in the colloid particles, the water phase is completely vaporized into water vapor, thereby achieving the drying of the colloid particles. However, due to poor process continuity, a large amount of energy is wasted.

[0006] The SIBS production process is generally plagued by high energy consumption, low efficiency, high processing costs, and poor production continuity. Existing SIBS production technologies cannot meet the requirements for high efficiency and low consumption. Therefore, there is an urgent need to develop a SIBS production process that is efficient, environmentally friendly, energy-saving, and has a simple process flow. Summary of the Invention

[0007] The present disclosure provides a novel SIBS preparation method and apparatus, thereby solving the problems of low production efficiency, high energy consumption and high maintenance and management costs in the prior art.

[0008] In one aspect, the present disclosure provides a SIBS swirl strengthening method, the method comprising the following steps:

[0009] (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;

[0010] (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;

[0011] (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;

[0012] (D) Cyclone separation and coagulation: adding the uniformly mixed glue obtained in step (C) to a cyclone classifier, and coagulating the glue by cyclone separation to separate the tetrablock copolymer composed of styrene, isoprene, butadiene and cyclohexane from the glue in the form of colloidal water; and

[0013] (E) Post-treatment: The condensed particles obtained in step (D) are added to a non-phase change drying system to remove moisture from the surface and pores of the particles. The residual water is sent to an RTO (regenerative thermal oxidation furnace) for treatment. The particles in the product packaging silo are fed into a packaging system to obtain the final product SIBS.

[0014] In a preferred embodiment, the method further comprises: solution purification: recovering the solvent used in the cyclone fractionator in step (D) and recycling it after treatment.

[0015] In another preferred embodiment, in step (A), 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 97%, and the water content is reduced to below 20 ppm, based on the weight of the crude raw material.

[0016] 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.

[0017] 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.

[0018] In another preferred embodiment, in step (B), the styrene conversion rate reaches 99%, the isoprene conversion rate reaches 99%, and the concentration of the rubber obtained by the reaction is 15%-20%.

[0019] In another preferred embodiment, in step (C), dynamic mixing in the dynamic blending tank increases the mixing rate by increasing the contact area; in step (D), the cyclone separation and coagulation process utilizes the density difference between substances and centrifugal force for separation, the operating temperature of the cyclone separation and coagulation process is 90-115°C, and the solid content of the colloid particles after cyclone separation and coagulation is 30%-50%.

[0020] In another preferred embodiment, in step (E), the condensed colloidal particles are added to a cyclone separator of a non-phase change drying system for rotation, and the particles rotate in the cyclone separator at a speed of 15,000-60,000 rpm; the pellets 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.

[0021] In another preferred embodiment, in step (E), the non-phase change drying system has a sorting function, and obtains colloidal particles of different molecular weights by controlling the carrier gas temperature; the non-phase change drying system uses low-temperature drying means, and when the carrier gas temperature is 40°C-70°C, the moisture content of the colloidal particles after drying is less than 1%; 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 swirl intensification 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 classifier connected to the dynamic blending tank is used to perform cyclone separation and coagulation in step (D): adding the uniformly blended glue obtained in step (C) to the cyclone classifier and coagulating the glue by cyclone separation to separate the tetrablock copolymer composed of styrene, isoprene, butadiene and cyclohexane from the glue in the form of colloidal water; 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 (E): the agglomerated colloid particles obtained in step (D) are added to the non-phase-change drying system to remove moisture from the surface and pores of the colloid particles, and the residual water is sent to the RTO (regenerative thermal oxidation furnace) for treatment. The granules in the product packaging silo are fed into 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 present disclosure provides a novel method for preparing SIBS elastomers, wherein the monomer refining unit mainly utilizes the novel microchannel pulsating oscillation separation technology and the shape-agglomeration demulsification technology to remove impurities from the raw materials, thereby improving the precision of the raw materials and thus improving the product quality.

[0030] (2) The microchannel reactor used in the microchannel reaction polymerization unit has the characteristics of high-speed mixing and efficient heat transfer. At the same time, the degree of polymerization reaction can be controlled by controlling the reaction temperature and time. The reaction energy consumption is 1 / 3 of the original process, achieving green and efficient production.

[0031] (3) The use of the new cyclone dynamic mixing tank improves the mixing efficiency and the vertical mixing effect, thereby improving the mixing quality.

[0032] (4) The cyclone separation technology used mainly utilizes the density difference between objects and the effect of centrifugal force to achieve the separation of solid, liquid and gas. It is a continuous reaction process with high production efficiency, which shortens the production cycle and improves equipment utilization.

[0033] (5) The non-phase-change cyclone drying system mainly utilizes the centrifugal force generated by the high-speed rotation of the particle flow field characteristics for drying. This method solves the problem of high energy consumption caused by conventional heating evaporation, which must overcome the latent heat of vaporization of water in the colloid particles and thus cause phase change. The processing energy consumption is approximately 1 / 5-1 / 15 of that of heating phase change evaporation.

[0034] (6) The SIBS product prepared is a high melt index, high transparency SIBS elastomer. By optimizing the SIBS preparation process, the production process is simplified, the product quality is improved, and the production efficiency is improved. At the same time, the high energy consumption problem in the previous process is solved. This is a green, efficient and continuous production method. In addition, the equipment construction and operation management costs in this process are low, and the economic benefits are high, making it suitable for industrial production. BRIEF DESCRIPTION OF THE DRAWINGS

[0035] The accompanying drawings are used to provide further understanding of the present disclosure. They only constitute a part of this specification to further explain the present disclosure and do not constitute a limitation of the present disclosure.

[0036] Figure 1 It is a schematic diagram of the overall process flow of the SIBS cyclone strengthening method according to a preferred embodiment of the present disclosure.

[0037] Reference numerals:

[0038] 1: Microchannel separator

[0039] 2: Shape Coalescer

[0040] 3: Microchannel reactor (3-1, 3-2, 3-3, 3-4)

[0041] 4: Glue buffer tank

[0042] 5: Micro-droplet extraction tank

[0043] 6: Dynamic mixing tank

[0044] 7: Cyclone Classification Separator

[0045] 8: Non-phase change drying system

[0046] 9: Packaging system

[0047] 10: Refining Tower (10-1, 10-2)

[0048] 11: Condenser

[0049] 12: Tundish

[0050] 13: Reflux tank

[0051] 14: Heavy component storage tank

[0052] 15: Butadiene product tank

[0053] 16: Deweighting Tower

[0054] 17: Isoprene product tank

[0055] 18: Refined solvent tank

[0056] 19: Separation tank

[0057] 20: Exhaust gas condenser

[0058] 21: Stripping unit mixer

[0059] 22: Dehydration extruder

[0060] 23: Hot water tank

[0061] 24: Dewatering screen DETAILED DESCRIPTION

[0062] 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.

[0063] After extensive and in-depth research, the applicants of the present invention discovered that the existing SIBS production process suffers from excessive energy consumption, large investment, low efficiency, and poor process continuity. However, the use of cyclone enhancement technology, combined with microchannel separation, shape coalescence, microchannel reaction, and non-phase change drying, not only improves product quality but also achieves energy savings and efficient production. This process is short and continuous, requires less equipment, occupies a small footprint, and provides a clean operating environment, low energy consumption, and high efficiency. Based on these findings, the present invention was completed.

[0064] In a first aspect of the present disclosure, a SIBS cyclone strengthening method is provided, the method comprising the following steps:

[0065] (A) Monomer Refining Based on a Microchannel Separator and Shape Coalescer: Crude styrene, crude isoprene, crude butadiene, and crude cyclohexane raw materials are respectively fed into a monomer refining unit composed of a microchannel separator and a shape coalescer to remove impurities therein and obtain refined raw materials;

[0066] (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;

[0067] (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;

[0068] (D) Cyclone separation and coagulation: adding the uniformly mixed glue obtained in step (C) to a cyclone classifier, and coagulating the glue by cyclone separation to separate the tetrablock copolymer composed of styrene, isoprene, butadiene and cyclohexane from the glue in the form of colloidal water; and

[0069] (E) Post-processing: The condensed particles obtained in step (D) are added to a non-phase change drying system and rotated at high speed in a cyclone separator to remove moisture from the surface and pores of the particles. The residual water is sent to an RTO (regenerative thermal oxidation furnace) for treatment. The particles in the product packaging silo are fed into the packaging system for metering, sewing, sealing, metal inspection, re-inspection, palletizing, and storage of the finished products to obtain the final product SIBS.

[0070] In the present disclosure, the method further comprises: solution purification: recovering the solvent used in the cyclone fractionator in step (D) and recycling it after treatment.

[0071] In the present disclosure, in step (A), the water reuse rate during the treatment process of the microchannel separator can reach 99%.

[0072] In the present disclosure, in step (A), the accuracy of the crude raw material after treatment by the microchannel separator exceeds 97%, even 98.5%, and the water content is reduced to below 20 ppm, based on the weight of the crude raw material.

[0073] 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, wherein the main impurities are irregular particles and moisture.

[0074] 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.

[0075] In the present disclosure, in step (B), the reaction pressure of the microchannel reactor is 0.05-0.5 MPa, preferably 0.1-0.35 MPa, for example, 0.15 MPa, 0.17 MPa, 0.21 MPa, 0.25 MPa, 0.30 MPa, 0.33 MPa, 0.35 MPa, more preferably 0.15-0.3 MPa.

[0076] In the present disclosure, in step (B), the reaction temperature of the microchannel reactor is 50-140°C, such as 50°C, 70°C, 90°C, 100°C, 110°C, 120°C, 140°C, preferably 50°C-130°C.

[0077] In the present disclosure, in step (B), the reaction time of the microchannel reactor is 20-110 min, for example, 20 min, 30 min, 50 min, 60 min, 70 min, 80 min, 90 min, 100 min, 110 min.

[0078] In the present disclosure, in step (B), water droplets are sheared and broken in the microchannel reactor, and rotated by the shearing action of the flow field to enhance mass transfer.

[0079] In the present disclosure, in step (B), the concentration of the SIBS glue obtained by the reaction is 13%-20%, for example, 13%, 15%, 15.5%, 16%, 16.8%, 17.9%, 19%, 20%, preferably 15%-20%.

[0080] In the present disclosure, in step (B), the styrene conversion rate reaches 99%, for example, 99.1%, and the isoprene conversion rate reaches 99%, for example, 99.75%.

[0081] In the present disclosure, in step (B), the investment cost of the microchannel reactor is 1 / 3 of the original process, and the maintenance cost is 1 / 50 of the original process.

[0082] In the present disclosure, in step (C), the dynamic mixing of the novel cyclone dynamic mixing tank mixes the glue liquid through the cyclone field, thereby increasing the contact area and thus increasing the mixing rate, thereby effectively improving the vertical stirring effect of the mixed glue liquid.

[0083] In the present disclosure, in step (D), the cyclone separation and coagulation process utilizes density differences between substances and centrifugal force for separation.

[0084] 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.

[0085] 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%.

[0086] In the present disclosure, in step (E), the rotation speed of the particles in the three-dimensional rotating turbulent flow field in the cyclone separator is 15,000-60,000 rpm.

[0087] In the present disclosure, in step (E), the non-phase change drying system has a sorting function, and colloidal materials with different molecular weights are obtained by controlling the carrier gas temperature; the operating pressure of the non-phase change drying process is 0.01-0.07MPa, for example, 0.1MPa, 0.16MPa, 0.20MPa, 0.25MPa, 0.30MPa, 0.35MPa, preferably 0.1MPa-0.3MPa.

[0088] In the present disclosure, in step (E), the non-phase change drying system uses low-temperature drying means, and when the carrier gas temperature is 40° C.-70° C., the moisture content of the granules after drying can be less than 1%.

[0089] In the present disclosure, in step (E), the non-phase-change cyclone drying technology belongs to a mechanical separation method, and the processing energy consumption is approximately 1 / 5-1 / 15 of that of the heating phase-change evaporation.

[0090] The method disclosed in the present invention can obtain high-quality SIBS elastomers, the molecular weight of which can reach 80,000 to 150,000.

[0091] In a second aspect of the present disclosure, a SIBS swirl intensification device is provided, the device comprising:

[0092] A monomer refining unit consisting of a microchannel reactor and a shaped coalescer connected thereto, for carrying out the above step (A);

[0093] 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);

[0094] A dynamic blending tank connected to the micro-droplet extraction tank, used to perform the above step (C);

[0095] A cyclone classifier connected to the dynamic blending tank, for performing the above step (D); and

[0096] 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 (E).

[0097] In the present disclosure, the monomer refining unit has a separation accuracy of fine particles of up to 100nm, and a 100nm pollutant removal rate of up to 90%. By dehydrating and performing oil-water separation treatment on the added crude styrene, crude isoprene, crude butadiene, and crude cyclohexane, refined styrene, isoprene, butadiene, and cyclohexane are obtained.

[0098] In the present disclosure, the microchannel separator in the monomer refining unit based on the microchannel separator and the shape coalescer has three removal mechanisms: molecular adsorption, ion extraction, and particle filtration and interception. Oil droplets, pollutant ions, and water are removed through different mechanisms, thereby achieving the purpose of monomer refining.

[0099] In this disclosure, a microchannel reactor polymerizes the added refined monomers to produce a glue solution. A microchannel reactor is a small, multi-channel microstructured reactor where water droplets are sheared and fragmented, and then rotate under the shearing action of the flow field, enhancing mass transfer. It boasts mass and heat transfer properties that are 1-3 orders of magnitude superior to those of traditional chemical equipment.

[0100] In the present disclosure, the main device of the non-phase change drying system is a cyclone dehydrator, which mainly utilizes the pulsating rotation in the cyclone dehydrator to generate rapid oscillations, thereby changing the properties of the contact interface between the colloid surface and the water phase, and enhancing the drying process.

[0101] Please refer to the accompanying drawings below.

[0102] Figure 1 FIG. 1 is a schematic diagram of the overall process flow of the SIBS cyclone strengthening 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;

[0103] 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. 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 strengthening 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: adding the uniformly mixed glue obtained in step (C) to a cyclone classifier, and coagulating the glue by cyclone separation to separate the tetrablock copolymer composed of styrene, isoprene and butadiene from the glue in the form of colloidal water; and (E) Post-treatment: The condensed particles obtained in step (D) are added to a non-phase change drying system to remove moisture from the surface and pores of the particles. The residual water is sent to the RTO for treatment. The particles in the product packaging silo are sent to the packaging system to obtain the final product SIBS.

2. The method according to claim 1, wherein The method further comprises: solution refining: recovering the solvent used in the cyclone fractionating separator in step (D) and recycling it after treatment.

3. The method according to claim 1 or 2, wherein: In step (A), the water recycling 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 97%, and the water content is reduced to below 20 ppm, based on the weight of the crude raw material.

4. The method according to claim 1 or 2, 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.

5. The method according to claim 1 or 2, wherein In step (B), the refined raw material obtained in step (A) is added to a microchannel reactor at 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.

6. The method according to claim 1 or 2, wherein: In step (B), the styrene conversion rate reaches 99%, the isoprene conversion rate reaches 99%, and the concentration of the rubber solution obtained by the reaction is 15%-20%.

7. The method according to claim 1 or 2, wherein: In step (C), dynamic mixing in the dynamic blending tank increases the mixing rate by increasing the contact area; in step (D), the cyclone separation and coagulation process utilizes the density difference between the substances and the centrifugal force for separation. The operating temperature of the cyclone separation and coagulation process is 90-115°C, and the solid content of the colloid particles after cyclone separation and coagulation is 30%-50%.

8. The method according to claim 1 or 2, wherein: In step (E), the condensed colloidal particles are added to a cyclone separator of a non-phase change drying system for rotation, and the particles rotate in the cyclone separator at a speed of 15,000-60,000 rpm. The pellets in the product packaging silo are fed into the packaging system and then subjected to metering, sewing, sealing, metal inspection, re-inspection, palletizing, and finished product storage to obtain the final product SIBS.

9. The method according to claim 1 or 2, wherein: In step (E), the non-phase change drying system has a sorting function, and obtains colloidal particles of different molecular weights by controlling the carrier gas temperature; the non-phase change drying system uses low-temperature drying means, and when the carrier gas temperature is 40°C-70°C, the moisture content of the colloidal 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 strengthening 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 the cyclone separation and coagulation in step (D): adding the uniformly blended glue obtained in step (C) to the cyclone classification separator, and adopting the cyclone separation method to coagulate the glue, so that the tetrablock copolymer composed of styrene, isoprene and butadiene is separated from the glue in the form of colloidal water; 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 (E): the condensed colloid particles obtained in step (D) are added to the non-phase change drying system to remove moisture from the surface and pores of the colloid particles, the residual water is sent to the RTO treatment, and the granules in the product packaging silo are sent to the packaging system to obtain the final product SIBS.

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