SIBS non-phase-change swirl self-rotation method and device

Abstract

The present disclosure relates to a SIBS non-phase change cyclone self-rotation method and device, and provides a SIBS non-phase change cyclone self-rotation method, which includes the following steps: (A) monomer refining based on a microchannel separator and a shape coalescer; (B) microchannel reactor polymerization; (C) cyclone dynamic mixing and blending; (D) cyclone separation and condensation; and (E) post-treatment. A SIBS non-phase change cyclone self-rotation device is also provided. The method provided by the present disclosure solves the problem of high energy consumption in heating evaporation, and provides an efficient, low-energy and green drying method.

Description

Technical Field

[0001] The present invention belongs to the technical field of polymer materials, and relates to a method and device for preparing SIBS, and in particular to a method and device for preparing SIBS using a non-phase-change swirl rotation technology. Specifically, the present invention provides a method and device for preparing SIBS using a non-phase-change swirl rotation technology. Background Art

[0002] The new thermoplastic rubber SIBS (i.e. integrated elastomer) is composed of styrene, isoprene, butadiene and cyclohexane. As a polymer material, it has both the high elasticity of vulcanized rubber and the plasticity of plastic. Its special four-block molecular structure makes it have good cohesion, excellent adhesion and good compatibility. Because its processing is environmentally friendly and does not cause environmental pollution, it is a polymer material encouraged and supported by national policies.

[0003] With the development of economy and the improvement of science and technology, SIBS materials have been applied to the fields of adhesives, coatings and plastic modification. Pressure-sensitive adhesives and hot-melt adhesives prepared with SIBS as the main polymer are widely used in medical treatment, electrical insulation, packaging, protection, masking, marking, bonding and fixing, as well as interlayer bonding of composite bags. The demand for SIBS materials is increasing rapidly, but the current SIBS production process has the problems of high energy consumption and low efficiency. If mass production is carried out, a large amount of energy and resources will be wasted.

[0004] At present, many enterprises often use heating evaporation to further dry the particles during the production process. They provide enough heat to overcome the latent heat of vaporization of water in the particles, so that the water phase is completely vaporized into water vapor, thereby achieving the drying of the particles. However, due to the complexity of the entire set of process equipment, large space and high energy consumption, it is unable to solve the current problems of high production costs and low drying efficiency.

[0005] Since the SIBS preparation process generally has the problems of high energy consumption, low efficiency and high processing cost, and the existing drying technology using heating evaporation cannot meet the requirements of high-efficiency and low-cost production, the art urgently needs to develop a SIBS preparation process that is efficient, environmentally friendly, energy-saving and has a simple process flow. Summary of the invention

[0006] The present disclosure provides a novel SIBS non-phase change swirl self-rotation method and device, thereby solving the problems of low production efficiency, high energy consumption and high maintenance and management costs in the prior art.

[0007] In one aspect, the present disclosure provides a SIBS non-phase change swirl rotation method, the method comprising the following steps:

[0008] (A) Monomer refining based on 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 a refined raw material;

[0009] (B) Microchannel reactor polymerization: the refined raw material obtained in step (A) is added to a microchannel reactor, and after the reaction is completed, the generated glue solution is added to a glue solution 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, stirring and blending uniformly;

[0011] (D) Cyclone separation and coagulation: adding the uniformly mixed glue obtained in step (C) into a cyclone classifier, and coagulating the glue by cyclone separation, so that the tetrablock copolymer composed of styrene, isoprene, butadiene and cyclohexane is separated from the glue in the form of colloidal water; and

[0012] (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 particles in the product packaging silo are fed into the packaging system to obtain the final product, SIBS elastomer, wherein the condensed particles are added to a cyclone separator of the non-phase change drying system for rotation. The particle rotation speed in the cyclone separator is 15,000-60,000 rpm, and the particles stay in the cyclone separator for less than 10 seconds.

[0013] In a preferred embodiment, the method further comprises: solution refining: recovering the solvent used in the cyclone fractionation separator in step (D) and recycling it after treatment.

[0014] In another preferred embodiment, in step (A), the microchannel separator applies the mechanism of molecular adsorption, ion extraction and particle filtration and interception, and the raw material separation accuracy reaches 100nm, and the volume accuracy is improved by two orders of magnitude year-on-year; 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 20ppm, based on the weight of the crude raw material.

[0015] In another preferred embodiment, in step (A), the weight ratio of 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 styrene, refined isoprene, refined butadiene and refined cyclohexane obtained in step (A) are added to a microchannel reactor in a weight ratio of 1:2-5:2-5:24-26; the reaction pressure of the microchannel reactor is 0.05-0.5MPa, the reaction temperature is 50-130°C, and the reaction time is 20-110min.

[0017] In another preferred embodiment, in step (B), the styrene conversion rate reaches 99%, the isoprene conversion rate reaches 99%, and the concentration of the gum obtained by the reaction is 13%-20%.

[0018] In another preferred embodiment, in step (C), the dynamic mixing in the dynamic blending tank increases the contact area and thus improves the blending rate; in step (D), the cyclone separation and coagulation process utilizes the density difference between substances and the centrifugal force for separation, the operating temperature of the cyclone separation and coagulation process is 90-115°C, and the reaction pressure is 0.15-0.3MPa; the solid content of the colloid particles after cyclone separation and coagulation is 30%-50%.

[0019] In another preferred embodiment, in step (E), the pellets in the product packaging silo enter the packaging system and are metered, sewn, sealed, metal inspected, re-inspected, stacked, and the finished products are put into storage to obtain the final product SIBS elastomer, the molecular weight of which is 80,000-150,000.

[0020] In another preferred embodiment, in step (E), the non-phase change drying system has a sorting function, and obtains colloid particles with different molecular weights by controlling the carrier gas temperature; the non-phase change drying system uses low-temperature drying to reduce the moisture content of the colloid particles from 90% to 5%-30% when the carrier gas temperature is 40°C-60°C; 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.

[0021] On the other hand, the present disclosure provides a SIBS non-phase change swirl self-rotation device, the device comprising:

[0022] A monomer refining unit composed 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 composed of the microchannel separator and the shape coalescer to remove impurities therein and obtain refined raw materials;

[0023] 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 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;

[0024] 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 glue obtained in step (B) into the dynamic blending tank, stirring and blending uniformly;

[0025] The cyclone classification separator connected to the dynamic blending tank is used to perform the cyclone separation and coagulation in step (D): adding the uniformly blended glue obtained in step (C) into the cyclone classification separator, and coagulating the glue by cyclone separation, so that the tetrablock copolymer composed of styrene, isoprene, butadiene and cyclohexane is separated from the glue in the form of colloidal water; and

[0026] 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 for post-processing of 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, and the pellets in the product packaging silo are fed into the packaging system to obtain the final product SIBS elastomer, wherein the condensed colloid particles are added to the cyclone separator of the non-phase change drying system for rotation, the particle rotation speed in the cyclone separator is 15000-60000 rpm, and the colloid particles stay in the cyclone separator for less than 10s.

[0027] Beneficial effects:

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

[0029] (1) The non-phase-change cyclone drying system used in the present invention mainly utilizes the centrifugal force generated by the high-speed rotation of the particle flow field characteristics for drying, which solves the problem that conventional heating evaporation must overcome the latent heat of vaporization of water in the colloid particles to cause phase change and cause high energy consumption. The processing energy consumption is approximately 1 / 5-1 / 15 of that of heating phase change evaporation.

[0030] (2) The non-phase-change cyclone drying system used in the present invention has a sorting function. By performing cyclone self-rotation dehydration of the colloid particles at different air flow temperatures, colloid particles of different molecular weights can be obtained, which are suitable for the production of different products.

[0031] (3) The present invention simplifies the production process, optimizes product quality, improves production efficiency, and solves the problem of high energy consumption in previous processes by optimizing the SIBS preparation process. In addition, the cost of equipment construction and operation management in this process is low and the economic benefit is high, so it is suitable for industrial production. 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 to further explain the present disclosure, and 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 non-phase change swirl self-rotation method according to a preferred embodiment of the present disclosure.

[0034] Figure 2 It is a schematic diagram of the overall process flow of a non-phase-change cyclone drying system according to a preferred embodiment of the present disclosure.

[0035] Figure 3 It is a schematic structural diagram of a cyclone separator in a non-phase-change cyclone drying system according to a preferred embodiment of the present disclosure.

[0036] Reference numerals:

[0037] 1: Microchannel separator

[0038] 2: Shape Coalescer

[0039] 3: Microchannel reactor (3-1, 3-2, 3-3, 3-4)

[0040] 4: Glue buffer tank

[0041] 5: Micro droplet extraction tank

[0042] 6: Dynamic mixing tank

[0043] 7: Cyclone Classification Separator

[0044] 8: Non-phase change drying system

[0045] 9: Packaging system

[0046] 10: Refining tower (10-1, 10-2)

[0047] 11: Condenser

[0048] 12: Intermediate tank

[0049] 13: Reflux tank

[0050] 14: Heavy component storage tank

[0051] 15: Butadiene product tank

[0052] 16: Weight-removal tower

[0053] 17: Isoprene product tank

[0054] 18: Refined solvent tank

[0055] 19: Separation tank

[0056] 20: Exhaust gas condenser

[0057] 21: Stripping unit mixer

[0058] 22: Dehydration extruder

[0059] 23: Hot water tank

[0060] 24: Dewatering screen

[0061] 101: Granulator

[0062] 102: Screw feeder

[0063] 103: Water-gas separator

[0064] 104: Cyclone separator

[0065] 105: Airflow generator

[0066] 106: Pipeline heater

[0067] 201: Import

[0068] 202: Overflow pipe

[0069] 203: Cyclone body

[0070] 204: Bottom flow mouth DETAILED DESCRIPTION

[0071] The endpoints and any values ​​of the ranges disclosed in this article 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 endpoint values ​​of each range, the endpoint values ​​of each range and the 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 as specifically disclosed in this article.

[0072] The applicant of the present invention has found through extensive and in-depth research that the existing fourdrier drying method has the problems of high energy consumption and low efficiency when dehydrating and drying the rubber particles, and the use of non-phase-change cyclone self-rotation drying technology can not only improve the product quality, but also achieve the purpose of energy-saving and efficient production. Based on the above findings, the present invention has been completed.

[0073] In a first aspect of the present disclosure, a SIBS non-phase change swirl rotation method is provided, the method comprising the following steps:

[0074] (A) Monomer refining based on 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 a refined raw material;

[0075] (B) Microchannel reactor polymerization: the refined raw material obtained in step (A) is added to a microchannel reactor, and after the reaction is completed, the generated glue solution is added to a glue solution buffer tank, and then extracted by a micro-droplet extraction tank containing an antioxidant;

[0076] (C) Cyclone dynamic mixing and blending: adding the extracted rubber solution obtained in step (B) into a dynamic blending tank, stirring and blending uniformly;

[0077] (D) Cyclone separation and coagulation: adding the uniformly mixed glue obtained in step (C) into a cyclone classifier, and coagulating the glue by cyclone separation, so that the tetrablock copolymer composed of styrene, isoprene, butadiene and cyclohexane is separated from the glue in the form of colloidal water; and

[0078] (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 particles in the product packaging silo are fed into a packaging system to obtain the final product, SIBS elastomer.

[0079] In the present disclosure, the method further comprises: solution refining: recovering the solvent used in the cyclone fractionation separator in step (D) and recycling it after treatment.

[0080] In the present disclosure, in step (A), the crude styrene and crude isoprene are crude purchased raw materials, and the main impurities are irregular particles and moisture.

[0081] In the present disclosure, in step (A), the monomer refining process utilizes the rotation inside the emulsion droplets to perform physical coalescence and demulsification without adding chemical demulsifiers.

[0082] In the present disclosure, in step (A), the microchannel separator applies the mechanisms of molecular adsorption, ion extraction, and particle filtration and interception, and the raw material separation accuracy reaches 100nm, and the volume accuracy is improved by two orders of magnitude year-on-year.

[0083] In the present disclosure, 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.

[0084] In the present disclosure, 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, preferably 1:8:1.5:25.

[0085] In the present disclosure, in step (B), the refined styrene, refined isoprene, refined butadiene and refined cyclohexane obtained in step (A) are added to the microchannel reactor in a weight ratio of 1:2-5:2-5:24-26.

[0086] In the present disclosure, in step (B), water droplets in the microchannel reactor are sheared and broken, and rotated by the shearing action of the flow field to enhance mass transfer.

[0087] 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.

[0088] In the present disclosure, in step (B), the styrene conversion rate reaches 99%, the isoprene conversion rate reaches 99%, and the concentration of the gum obtained by the reaction is 13%-20%, for example, 13%, 15%, 15.5%, 16%, 16.8%, 17.9%, 19%, 20%.

[0089] In the present disclosure, in step (C), the dynamic mixing in the dynamic blending tank increases the blending rate by increasing the contact area.

[0090] In the present disclosure, in step (C), the cyclonic dynamic mixing replaces the traditional stirring force by the cyclonic field force, so that the colloid is mixed in a spiral motion, which increases the vertical surface force and thus improves the mixing efficiency.

[0091] In the present disclosure, in step (D), the cyclone separation and condensation process utilizes the density difference between substances and centrifugal force for separation, and the operating temperature of the cyclone separation and condensation process is 90-115° C. and the reaction pressure is 0.15-0.3 MPa.

[0092] In the present disclosure, in step (D), the solid content of the colloidal particles after cyclone separation and coagulation is 30%-50%.

[0093] In the present disclosure, in step (E), the condensed colloid particles are added to a cyclone separator of a non-phase change drying system for rotation, and the particle rotation speed in the three-dimensional rotating turbulent field of the cyclone separator is 15000-60000 rpm.

[0094] In the present disclosure, in step (E), the non-phase change drying system has a fast processing speed, and the residence time of the colloid particles in the cyclone separator is less than 10 seconds.

[0095] In the present disclosure, in step (E), the pellets in the product packaging silo enter the packaging system and are metered, sewn, sealed, metal inspected, re-inspected, stacked, and the finished product is put into storage to obtain the final product SIBS elastomer.

[0096] In the present disclosure, in step (E), the molecular weight of the obtained SIBS elastomer reaches 80,000-150,000.

[0097] In the present disclosure, in step (E), the non-phase change drying system has a sorting function, and colloidal particles of different molecular weights are obtained by controlling the carrier gas temperature.

[0098] In the present disclosure, in step (E), the non-phase change drying system uses hydrogen, nitrogen or steam as a carrier gas.

[0099] In the present disclosure, in step (E), the non-phase change drying system uses low-temperature drying to reduce the moisture content of the colloid particles from 90% to 5%-30% when the carrier gas temperature is 40°C-60°C; when the carrier gas temperature is 40°C-70°C, the drying efficiency of the colloid particles is rapidly improved, and the moisture content of the colloid particles after drying is less than 10%.

[0100] In the present disclosure, in step (E), the operating pressure of the non-phase change drying process is 0.1-0.7 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.

[0101] In the present disclosure, in step (E), the non-phase change drying system treatment process environment is completely closed and the reaction temperature is low, and the VOC (volatile organic compound) precipitation amount is close to zero.

[0102] In the present disclosure, in step (E), the non-phase change drying system utilizes the self-revolution coupling to induce the micro-interface oscillation centrifugal force to overcome the micro-interface capillary force, thereby achieving a drying mechanism that is fast, efficient, low-temperature and low-consumption.

[0103] In the present disclosure, in step (E), the non-phase change cyclone drying technology belongs to a mechanical separation method, which solves the problem that conventional heating evaporation must overcome the latent heat of vaporization of water in the colloid particles to cause phase change and cause high energy consumption. The processing energy consumption is approximately 1 / 5-1 / 15 of that of heating phase change evaporation.

[0104] In a second aspect of the present disclosure, a SIBS non-phase-change swirl self-rotation device is provided, the device comprising:

[0105] A monomer refining unit consisting of a microchannel reactor and a shaped coalescer connected thereto, for carrying out the above step (A);

[0106] 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);

[0107] A dynamic blending tank connected to the micro-droplet extraction tank, used to perform the above step (C);

[0108] A cyclone classifier connected to the dynamic blending tank, used to perform the above step (D); and

[0109] 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).

[0110] Please refer to the accompanying drawings below.

[0111] Figure 1 FIG. 1 is a schematic diagram of the overall process flow of the SIBS non-phase change swirl self-rotation method according to a preferred embodiment of the present disclosure. Figure 1 As 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 which are composed of a microchannel separator 1 and a shape coalescer 2 connected thereto; wherein, the styrene produced by the styrene refining unit is directly pumped from its shape coalescer 2 to the microchannel reactor 3; the butadiene produced by the butadiene refining unit is pumped from its shape coalescer 2 to the refining tower 10, the light component obtained by refining 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 heavy component obtained by refining 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 by the isoprene refining unit is pumped from its shape coalescer 2 to the refining tower 10, and the isoprene produced by 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 de-weighting tower 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 Enter the reflux tank 13, the light components are 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, cyclohexane is sent to the refining tower 10-2, the heavy components at the bottom of the tower are removed, the light components are 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, cyclohexane is sent to the fine solvent tank 18, and then pumped to the microchannel reactor 3;

[0112] The glue liquid produced by the microchannel reactor groups 3-1, 3-2, 3-3, and 3-4 is sent to the glue liquid 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 liquid 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 classification separator 7 for separation. The obtained product is sent to the reflux tank 13, and then sieved 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 The final SIBS product is obtained by entering the packaging system 9 for metering, sewing, sealing, metal inspection, re-inspection, palletizing, and finished product storage; 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 evenly, the gas phase is discharged from the top and sent to the tail gas condenser 20, and 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 dehydration screen 24 and the dehydration 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 the dispersant and returned to the stripping unit mixer 29 together.

[0113] Figure 2 FIG. 1 is a schematic diagram of the overall process flow of a non-phase-change cyclone drying system according to a preferred embodiment of the present disclosure. Figure 2 As shown, the wet rubber particles enter the granulator 101 for granulation and are then sent to the screw feeder 102 to be fed to the cyclone separator 104 for high-speed rotation to remove moisture from the surface of the rubber particles and in the pores. The removed moisture is discharged from the top of the cyclone separator 104 and enters the water-gas separator 103 to remove water and gas. The gas returns to the airflow generator 105 for reaction and is heated by the pipeline heater 106 and then circulated to the cyclone separator 104; the dry rubber particles are discharged from the bottom of the cyclone separator 104.

[0114] Figure 3 FIG. 1 is a schematic diagram of the structure of a cyclone separator in a non-phase-change cyclone drying system according to a preferred embodiment of the present disclosure. Figure 3 As shown, the cyclone separator includes: an inlet 201 , an overflow pipe 202 , a cyclone body 203 , and an underflow port 204 .

[0115] Example

[0116] The present invention will be further described below in conjunction with specific examples. However, it should be understood that these examples are only used to illustrate the present invention and do not constitute a limitation of the scope of the present invention. The test methods in the following examples that do not specify specific conditions are usually based on conventional conditions or the conditions recommended by the manufacturer. Unless otherwise stated, all percentages and parts are by weight.

[0117] Embodiment 1:

[0118] 1. Device Name

[0119] 40kg / h elastomer pilot production unit

[0120] 2. Process

[0121] like Figure 1 shown.

[0122] The material addition control ratio is shown in Table 1 below.

[0123] Table 1: Material addition control ratio

[0124]

[0125] 3. Implementation Effect

[0126] The process analysis data are shown in Table 2 below.

[0127] Table 2: Process analysis data

[0128]

[0129]

[0130] The above analysis data show that, by adopting the method of the present invention, each process index has reached the control requirements, and the produced finished rubber has also reached the physical and chemical indexes required by the market. The finished rubber yield reaches more than 99%, the isoprene conversion rate reaches 99.5%, the styrene conversion rate reaches 99.5%, and the butadiene conversion rate reaches 99.3%.

[0131] The above-listed embodiments are only preferred embodiments of the present disclosure and are not intended to limit the scope of implementation of the present disclosure. That is, all equivalent changes and modifications made according to the content of the patent scope of this application should be within the technical scope of the present disclosure.

[0132] All documents mentioned in this disclosure are cited as references in this application, just as each document is cited as reference individually. In addition, it should 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 these equivalent forms also fall within the scope defined by the claims attached to this application.

Claims

1. A SIBS non-phase change swirl rotation method, the method comprising the following steps: (A) Monomer refining based on 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 a refined raw material; (B) Microchannel reactor polymerization: the refined raw material obtained in step (A) is added to a microchannel reactor, and after the reaction is completed, the generated glue solution is added to a glue solution 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, stirring and blending uniformly; (D) Cyclone separation and coagulation: adding the uniformly mixed glue obtained in step (C) into a cyclone classifier, and coagulating the glue by cyclone separation, so that the copolymer composed of styrene, isoprene and butadiene is separated 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 particles in the product packaging silo are fed into the packaging system to obtain the final product, SIBS elastomer, wherein the condensed particles are added to a cyclone separator of the non-phase change drying system for rotation. The particle rotation speed in the cyclone separator is 15,000-60,000 rpm, and the particles stay in the cyclone separator for less than 10 seconds.

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

3. The method according to claim 1 or 2, characterized in that In step (A), the microchannel separator applies the mechanism of molecular adsorption, ion extraction and particle filtration and interception, and the raw material separation accuracy reaches 100nm; 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 20ppm, based on the weight of the crude raw material.

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

6. The method according to claim 1 or 2, characterized in that: 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 13%-20%.

7. The method according to claim 1 or 2, characterized in that: In step (C), dynamic mixing in the dynamic blending tank increases the contact area and thus increases the blending rate; 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 reaction pressure is 0.15-0.3MPa; the solid content of the colloid particles after cyclone separation and coagulation is 30%-50%.

8. The method according to claim 1 or 2, characterized in that: In step (E), the pellets in the product packaging silo enter the packaging system and are metered, sewn, sealed, metal inspected, re-inspected, stacked, and the finished product is put into storage to obtain the final product SIBS elastomer, the molecular weight of which is 80,000-150,000.

9. The method according to claim 1 or 2, characterized in that: 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 non-phase change swirl self-rotation device, the device comprising: A monomer refining unit consisting of a microchannel reactor (1) and a shape coalescer (2) 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 and obtain refined raw materials; A microchannel reactor (3) connected to the shape coalescer (2), a glue buffer tank (4) connected to the microchannel reactor (3), and a 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 coagulating the glue by a cyclone separation method, so that the copolymer composed of styrene, isoprene and butadiene is separated from the glue in the form of glue particle 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 for 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, and the granules in the product packaging silo are fed into the packaging system to obtain the final product SIBS elastomer, wherein the condensed colloid particles are added to the cyclone separator of the non-phase change drying system for rotation, the particle rotation speed in the cyclone separator is 15000-60000 rpm, and the colloid particles stay in the cyclone separator for less than 10 seconds.

Images