CN116642361A - Heat recovery system and method for coagulation process of rubber polymer - Google Patents
Heat recovery system and method for coagulation process of rubber polymer Download PDFInfo
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- CN116642361A CN116642361A CN202310628221.2A CN202310628221A CN116642361A CN 116642361 A CN116642361 A CN 116642361A CN 202310628221 A CN202310628221 A CN 202310628221A CN 116642361 A CN116642361 A CN 116642361A
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- 238000005345 coagulation Methods 0.000 title claims abstract description 152
- 230000015271 coagulation Effects 0.000 title claims abstract description 152
- 229920000642 polymer Polymers 0.000 title claims abstract description 76
- 229920001971 elastomer Polymers 0.000 title claims abstract description 61
- 239000005060 rubber Substances 0.000 title claims abstract description 60
- 238000000034 method Methods 0.000 title claims abstract description 55
- 230000008569 process Effects 0.000 title claims abstract description 35
- 238000011084 recovery Methods 0.000 title claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 267
- 238000009833 condensation Methods 0.000 claims abstract description 124
- 230000005494 condensation Effects 0.000 claims abstract description 124
- 239000002245 particle Substances 0.000 claims abstract description 68
- 239000007788 liquid Substances 0.000 claims abstract description 39
- 230000001502 supplementing effect Effects 0.000 claims abstract description 8
- 238000003756 stirring Methods 0.000 claims description 48
- 239000002904 solvent Substances 0.000 claims description 42
- 150000001993 dienes Chemical class 0.000 claims description 27
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 claims description 16
- RRHGJUQNOFWUDK-UHFFFAOYSA-N Isoprene Chemical compound CC(=C)C=C RRHGJUQNOFWUDK-UHFFFAOYSA-N 0.000 claims description 16
- 229920002554 vinyl polymer Polymers 0.000 claims description 13
- 229920001400 block copolymer Polymers 0.000 claims description 11
- 229920001519 homopolymer Polymers 0.000 claims description 11
- 229920005604 random copolymer Polymers 0.000 claims description 11
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 claims description 10
- 239000000693 micelle Substances 0.000 claims description 9
- 238000002156 mixing Methods 0.000 claims description 8
- 239000004215 Carbon black (E152) Substances 0.000 claims description 6
- 229930195733 hydrocarbon Natural products 0.000 claims description 6
- 150000002430 hydrocarbons Chemical class 0.000 claims description 6
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 5
- XYLMUPLGERFSHI-UHFFFAOYSA-N alpha-Methylstyrene Chemical compound CC(=C)C1=CC=CC=C1 XYLMUPLGERFSHI-UHFFFAOYSA-N 0.000 claims description 5
- 150000001924 cycloalkanes Chemical class 0.000 claims description 5
- 238000005086 pumping Methods 0.000 claims description 5
- 239000005062 Polybutadiene Substances 0.000 claims description 4
- 229920002857 polybutadiene Polymers 0.000 claims description 4
- 229920001195 polyisoprene Polymers 0.000 claims description 4
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 3
- 239000000463 material Substances 0.000 abstract description 10
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000004064 recycling Methods 0.000 abstract description 4
- 239000003292 glue Substances 0.000 description 17
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 14
- 230000000052 comparative effect Effects 0.000 description 13
- 230000000694 effects Effects 0.000 description 12
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 6
- 238000001035 drying Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 244000043261 Hevea brasiliensis Species 0.000 description 3
- 230000009471 action Effects 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000006185 dispersion Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 239000012530 fluid Substances 0.000 description 2
- 229920003052 natural elastomer Polymers 0.000 description 2
- 229920001194 natural rubber Polymers 0.000 description 2
- 238000006116 polymerization reaction Methods 0.000 description 2
- 239000013557 residual solvent Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 229920003051 synthetic elastomer Polymers 0.000 description 2
- 239000005061 synthetic rubber Substances 0.000 description 2
- -1 vinyl aromatic hydrocarbon Chemical class 0.000 description 2
- 244000025254 Cannabis sativa Species 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 229920006125 amorphous polymer Polymers 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000005354 coacervation Methods 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 229920001577 copolymer Polymers 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000009477 glass transition Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000010410 layer Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000002861 polymer material Substances 0.000 description 1
- 230000000379 polymerizing effect Effects 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 239000002356 single layer Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000005514 two-phase flow Effects 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D21/0001—Recuperative heat exchangers
- F28D21/0014—Recuperative heat exchangers the heat being recuperated from waste air or from vapors
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B23/00—Heating arrangements
- F26B23/10—Heating arrangements using tubes or passages containing heated fluids, e.g. acting as radiative elements; Closed-loop systems
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Processes Of Treating Macromolecular Substances (AREA)
Abstract
The application provides a heat recovery system in the coagulation process of rubber polymers, wherein: the concentrator is provided with a hot water outlet, the hot water outlet of the concentrator is connected with a liquid inlet of the mixer or a liquid inlet of the first condensation kettle through a pipeline, and a hot water pump is arranged on the pipeline; the pipeline connecting the concentrator and the third condensation kettle is externally connected with a low-temperature hot water inlet pipe for supplementing low-temperature hot water to the third condensation kettle, or the middle upper part of the third condensation kettle is externally connected with a low-temperature hot water inlet pipe for supplementing low-temperature hot water to the third condensation kettle. The application also discloses a heat recovery method in the coagulation process of the rubber polymer. According to the application, through the concentrator, more high-temperature hot water can be separated out and returned to the first condensation kettle or the mixer, so that the purpose of recycling heat energy is achieved, and the energy consumption and material consumption of the condensation section are reduced as a whole. And low-temperature hot water is added into the third condensation kettle to maintain the normal material particle concentration of the device operation, so that the normal operation of the device is ensured.
Description
Technical Field
The application relates to the field of chemical industry, in particular to a heat recovery system and a heat recovery method in a coagulation process of rubber polymers.
Background
The Rubber (Rubber) is a high-elasticity polymer material with reversible deformation, is elastic at room temperature, can generate larger deformation under the action of small external force, and can recover the original shape after the external force is removed. Rubber is a completely amorphous polymer with a low glass transition temperature (T g) and often a large molecular weight, greater than several hundred thousand.
Rubber is classified into natural rubber and synthetic rubber. The natural rubber is prepared by extracting colloid from plants such as rubber tree, rubber grass, etc.; the synthetic rubber is obtained by polymerizing various monomers. Rubber products are widely used in industry or life.
At present, some common rubber polymer production processes generally comprise polymerization, coagulation, post-treatment and other processes, wherein:
in the condensing unit, the solvent in the polymer is flash-separated by using steam and hot water through a water separation method, and the obtained water-containing polymer is subjected to post-treatment processes such as drying, so as to obtain the rubber polymer. The existing condensing unit generally adopts three-kettle condensation or four-kettle condensation, and the multi-kettle condensation operation can reduce steam consumption and improve the solvent removal effect. The partial condensation technology adds a concentrator on the basis of three kettles condensation, thereby further reducing steam consumption, prolonging condensation residence time and improving solvent recovery rate.
The application discloses a condensation process for producing a polymerization product, which combines three kettles differential pressure condensation and a colloidal particle concentration technology, and a concentrator is arranged between a second condensation kettle and a third condensation kettle to concentrate colloidal particle water, so that a novel energy-saving and consumption-reducing SBS condensation process is formed, the contradiction between energy saving and consumption reduction can be effectively relieved, and the purposes of reducing solvent consumption and steam consumption are achieved. However, the technical scheme has the following defects: 1. only the concentration of the third condensation kettle is concentrated; 2. hot water is not recycled; 3. the colloidal particle water after passing through the concentrator enters a third coagulation kettle after being concentrated, and the concentration of polymer colloidal particles is increased due to the reduction of water quantity, so that the material conveying is difficult; 4. when the operation is improper or the high-temperature hot water is recycled too much, the stirring power is improved, the energy consumption is increased, the normal operation of the device is further influenced, and even the stirring current overload of the third coagulation kettle is caused.
Disclosure of Invention
The application aims to: aiming at the technical problems in the prior art, the application provides a heat recovery system and a heat recovery method in the coagulation process of rubber polymers, wherein:
according to the application, part of the after-treatment recycled low-temperature hot water is added into the third condensation kettle behind the concentrator, so that the concentration of the polymerized particles and the fluidity of the fluid in subsequent equipment can be maintained, the operation state of the condensation kettle is basically unchanged, and the original equipment can normally run. The implementation of the application can make up the influence of the concentrator on the third condensation kettle after the great concentration, the concentrator can separate more high-temperature hot water to return to the first condensation kettle, and the heat energy of the high-temperature hot water is recycled as much as possible.
The high-temperature hot water separated by the concentrator is recycled and returned to the first condensation kettle or the mixer and then enters the first condensation kettle, and the temperature of the high-temperature hot water is 95-110 ℃; in the prior art, the low-temperature hot water of the post-treatment unit is generally recycled and returned to the first condensation kettle or the mixer and then enters the first condensation kettle, and the low-temperature hot water separated by the concentrator is recycled by the first condensation kettle to replace part of the returned low-temperature hot water, so that part of heat energy can be saved.
Another advantage is that the glue solution feeding mixer before the high-temperature hot water enters the first coagulation kettle can increase the temperature of the mixed material entering the first coagulation kettle, reduce the viscosity of the material, and improve the dispersion effect of the material of the first coagulation kettle in water, thereby reducing the resistance of the solvent diffusing out of the glue solution and being beneficial to solvent removal.
The technical scheme is as follows: a heat recovery system for the coagulation process of rubber polymers comprises the following components:
a mixer for mixing low-temperature hot water and a polymer solution, or for mixing low-temperature hot water, high-temperature hot water and a polymer solution;
the liquid outlet of the mixer is communicated with the liquid inlet of the first condensation kettle, the top of the first condensation kettle is provided with a gas outlet, the bottom of the first condensation kettle is provided with a liquid outlet, and the middle lower part of the first condensation kettle is provided with a gas inlet;
the liquid outlet of the first condensation kettle is connected with the liquid inlet of the second condensation kettle through a first two-pipe, a first kettle colloidal particle water pump is arranged in the first two-pipe, the top of the second condensation kettle is provided with a gas outlet, the gas outlet of the second condensation kettle is connected with the gas inlet of the first condensation kettle through a pipe, and the bottom of the second condensation kettle is provided with a liquid outlet and a low-pressure steam pipe;
the third is condensed cauldron, the liquid outlet of second is condensed the cauldron with the liquid inlet of third is condensed the cauldron and is passed through the second third pipeline and link to each other, be equipped with two cauldron micelle water pumps in the second third pipeline two cauldron micelle water pumps with be equipped with the concentrator on the pipeline between the third is condensed the cauldron, the top of third is condensed the cauldron is equipped with the gas outlet, the gas outlet of third condense the cauldron pass through the pipeline with the air inlet of first condensing the cauldron links to each other, the bottom of third is condensed the cauldron is equipped with the liquid outlet, the liquid outlet of third is condensed the cauldron and is passed through the external three cauldron micelle water pumps of pipeline, wherein:
the concentrator is provided with a hot water outlet, the hot water outlet of the concentrator is connected with a liquid inlet of the mixer or a liquid inlet of the first condensation kettle through a pipeline, and a hot water pump is arranged on the pipeline;
the pipeline connecting the concentrator and the third condensation kettle is externally connected with a low-temperature water inlet pipe for supplementing low-temperature water to the third condensation kettle, or
The middle upper part of the third condensation kettle is externally connected with a low-temperature hot water inlet pipe for supplementing low-temperature hot water to the third condensation kettle.
Further, a hot water outlet of the concentrator is positioned at the middle lower part or the bottom of the concentrator;
further, the first condensation kettle is provided with a stirring shaft, and at least one stirring blade is arranged on the stirring shaft;
the second coagulation kettle is provided with a stirring shaft, and at least one stirring blade is arranged on the stirring shaft;
the third coagulation kettle is provided with a stirring shaft, and at least one stirring blade is arranged on the stirring shaft.
Further, the concentrator is one of a single sleeve type concentrator, a T type concentrator, a barrel type concentrator or a cross sleeve type concentrator.
A heat recovery method for the coagulation process of a rubber polymer, based on any one of the above-mentioned heat recovery systems for the coagulation process of a rubber polymer, comprises:
(1) Separating a portion of the high temperature hot water from the micellar water from the second coagulation kettle by a concentrator and pumping the portion of the high temperature hot water into a mixer or the first coagulation kettle by a hot water pump, wherein:
the temperature of the high-temperature hot water is 95-110 ℃;
(2) Adding hot, low temperature water through a second third conduit or directly to a third coagulation kettle, wherein:
the temperature of the low-temperature hot water is 70-90 ℃;
the volume ratio of the low-temperature hot water to the colloidal particle water entering the third coagulation kettle is (2-20): 100.
further, in the step (1), when the high-temperature hot water is pumped into the mixer by the hot water pump, the weight ratio of the high-temperature hot water and the low-temperature hot water entering the mixer is 1:0.1 to 10.
Further, the operating pressure of the first condensation kettle is 0.001-0.03 MPa, and the temperature is 82-95 ℃.
Further, the operating pressure of the second coagulation kettle is 0.03-0.09 MPa, and the temperature is 103-115 ℃.
Further, the operating pressure of the third coagulation kettle is-0.001-0.005 MPa, and the temperature is 95-100 ℃.
Further, the process is suitable for producing conjugated diene homopolymers or conjugated diene and vinylarene rubber-based polymers, wherein:
the conjugated diene homopolymer is polyisoprene or polybutadiene;
the conjugated diene and vinyl aromatic rubber polymer is random copolymer or block copolymer of isoprene or butadiene and styrene, or:
the conjugated diene and vinyl aromatic rubber polymer is a random copolymer or a block copolymer of isoprene or butadiene and alpha-methyl styrene.
Further, the solvent used for producing the conjugated diene homopolymer or the conjugated diene and vinyl aromatic rubber polymer is an inert hydrocarbon solvent selected from one of alkane, cycloalkane and aromatic hydrocarbon.
The beneficial effects are that: the application has the following beneficial effects:
not only can realize all functions of the original device, but also can better recycle heat energy, reduce steam consumption and solvent loss, and achieve the effects of energy conservation and consumption reduction.
Drawings
FIG. 1 is a schematic diagram of an embodiment 1 of a heat recovery system for a rubber-based polymer coagulation process according to the present disclosure.
FIG. 2 is a schematic diagram of example 2 of a heat recovery system for a rubber-based polymer coagulation process.
Wherein:
the specific embodiment is as follows:
the following detailed description of specific embodiments of the application.
The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.
In the condensation process, the glue solution and the hot water are separated by the concentrator as much as possible to recycle the hot water on the basis of removing the solvent in the glue solution in the condensation kettle by a water separation method and the like, so that the aims of saving energy and reducing consumption are fulfilled. The method comprises 3 condensing kettles and a concentrator which are connected in series, wherein the concentrator is positioned on a feed pipe line of a third condensing kettle, and polymer glue solution and low-temperature hot water sequentially pass through a first condensing kettle, a second condensing kettle, a concentrator (separation and concentration), the third condensing kettle and other equipment to remove the solvent in the glue solution, and the high-temperature hot water separated by the concentrator enters a mixer in front of the first condensing kettle or returns to the first condensing kettle.
In the application, the following components are added:
(1) The coagulation kettle is provided with stirring equipment, stirring blades are single-layer or multi-layer, the polymer solution and low-temperature hot water enter a mixer M1 to be mixed and then enter a first coagulation kettle F1, the hot water fed into the mixer M1 comprises two parts, one part is the low-temperature hot water returned by a post-treatment unit, and the temperature is 70-90 ℃; the other part is high-temperature hot water separated by a concentrator T, and the temperature of the hot water is 95-110 ℃; the average temperature difference between the high-temperature hot water and the low-temperature hot water is about 15 ℃, the high-temperature hot water separated by the concentrator T is recycled and returned to the first condensation kettle F1 or enters the first condensation kettle F1 after being mixed with the feed by the mixer M1, so that on one hand, the energy consumption is saved by utilizing the heat energy of the temperature difference between the high-temperature hot water and the low-temperature hot water, and on the other hand, the feeding viscosity of the glue solution of the first condensation kettle F1 can be reduced by mixing the high-temperature hot water and the feed when the high-temperature hot water is recycled, the dispersion effect of the glue solution of the first condensation kettle F1 is improved, and the removal capacity of the solvent is improved. Under the heating action of hot water and steam, solid colloidal particles are separated out from the colloidal solution, the final polymer is converted from a liquid phase into solid particles to be dispersed in water, the size of the polymer colloidal particles is controlled to be 6-10 mm by adjusting the flow rate of the hot water and the temperature of the first coagulation kettle F1, and the colloidal particle water is discharged from the bottom of the kettle in a solid-liquid two-phase flow mode; the vapor phase solvent is discharged from the top of the first condensation kettle F1, and is condensed and recovered subsequently. The colloidal particle water from which most of the solvent is removed is pumped out from the bottom of the kettle through a first colloidal particle water pump P1 and enters the middle lower part of a second coagulation kettle F2; in the first coagulation tank F1, the rubber polymer solution is contacted with hot water and steam for the first time, wherein a part of hot water is fed from the tank top and another part of hot water is fed from the tank bottom and the feed mixer M1. The first colloidal particle water which is separated for the first time is discharged from the lower part of the first coagulation kettle F1 and is conveyed to the second coagulation kettle F2 through a pump;
(2) In the second coagulation kettle F2, the material conveyed by the first kettle colloidal particle water pump P1 is contacted with added steam for the second time, the solvent in the polymer is further removed, and the separated solvent and water vapor are discharged from the top of the second coagulation kettle F2 and enter the bottom of the first coagulation kettle F1 to serve as a heat source. External steam heated by the second coagulation kettle F2 coagulation system is added through the kettle bottom of the second coagulation kettle F2, and as the colloidal particles at the moment wrap the solvent, the temperature and the pressure of the second coagulation kettle F2 are higher than those of the first coagulation kettle F1, the condition for providing the solvent removal is better, the solvent in the colloidal particles can be further removed under the action of the steam, so that most of the residual solvent in the colloidal particles is removed, and the colloidal particle water separated from the bottom of the second coagulation kettle F2 is pumped out by a two-kettle colloidal particle water pump P2 and enters a concentrator T.
(3) Concentrator T: the device is positioned between a second condensation kettle F2 and a third condensation kettle F3, colloidal particle water from the second condensation kettle F2 is separated from part of high-temperature hot water through the device, if a sufficient pressure difference exists between a hot water outlet of the concentrator and the first condensation kettle F1, the high-temperature hot water is directly returned to the first condensation kettle F1 or the mixer M1, if the pressure difference is insufficient, the high-temperature hot water is sent to the first condensation kettle F1 or the mixer M1 through a hot water pump P3, and the temperature of the high-temperature hot water separated by the concentrator T is 95-110 ℃; the recycling of the high-temperature hot water can reduce the energy consumption of the condensation process, reduce the viscosity of the feed glue solution of the first condensation kettle F1, improve the solvent removal effect, and enable the colloidal particle water after separating hot water and concentrating to enter the third condensation kettle F3.
(4) In the third coagulation kettle F3, the colloidal particle water separated by the concentrator T is further removed as much as possible. In the third coagulation kettle F3, as the colloidal particle water contacts with steam twice in the first coagulation kettle F1 and the second coagulation kettle F2, and the solvent is removed by coagulation, the colloidal particle water entering the third coagulation kettle F3 has a higher temperature, and a certain amount of low-temperature hot water is added into the coagulation kettle through a third coagulation kettle feeding pipeline (namely a second three-pipeline) or directly, the temperature of the low-temperature hot water is 70-90 ℃, and the volume ratio of the low-temperature hot water to the colloidal particle water entering the third coagulation kettle F3 is (2-20): 100, the part of hot water is used for post-treatment, drying and separating the hot water so as to maintain the concentration of the polymer particles in the third coagulation kettle F3 and the fluidity of the fluid, so that the operation state is not changed greatly, the original equipment can normally run, and the overload of stirring current is prevented. The implementation of the technology can make up the influence on the third condensation kettle F3 after the concentration by a large margin by the concentrator T, the concentrator T can separate more high-temperature hot water to return to the first condensation kettle F1, and the heat energy of the high-temperature hot water is utilized as much as possible. The operating pressure of the third coagulation kettle F3 is lower than that of the second coagulation kettle F2, so that the solvent is further separated.
Further, the rubber polymer solution and hot water are mixed in a mixer M1 and then enter a first condensation kettle F1, and the high-temperature hot water entering the mixer M1 is generated by separating a concentrator T, wherein the temperature is 95-110 ℃; hot water with the temperature of 70-90 ℃ enters the mixer M1, and the ratio of the hot water with high temperature to the hot water with low temperature is 1:0.1 to 10 weight percent.
Further, the operation pressure of the first condensation kettle F1 is 0.001-0.03 MPa of gauge pressure, and the temperature is 82-95 ℃; the polymer solution, low-temperature hot water and high-temperature hot water are coagulated in a first coagulation kettle F1, most of the solvent is removed, rubber is precipitated in a particle shape and dispersed in water, and the size of polymer colloidal particles is controlled to be 6-10 mm by adjusting the flow rate of the hot water and the temperature of the first coagulation kettle F1.
Further, the colloidal particle water is discharged from the lower part of the first coagulation kettle F1 and then enters a second coagulation kettle F2, the operating pressure of the second coagulation kettle F2 is 0.03-0.09 MPa, and the temperature is 103-115 ℃;
further, the operating pressure of the third coagulation kettle F3 is-0.001-0.005 MPa, and the temperature is 95-100 ℃;
further, in the method of the present application, the rubber-based polymer is a conjugated diene homopolymer or a conjugated diene and vinyl aromatic hydrocarbon rubber-based polymer;
the conjugated diene homopolymer is polyisoprene or polybutadiene;
the copolymer of conjugated diene and vinyl aromatic hydrocarbon comprises a random copolymer and a block copolymer, and can be a random copolymer or a block copolymer of isoprene or butadiene and styrene, or a random copolymer or a block copolymer of isoprene or butadiene and alpha-methyl styrene.
Further, the solvent used is an inert hydrocarbon solvent selected from alkanes, cycloalkanes and/or aromatics. Solvents commonly used as such rubber polymer solutions are one or more of alkanes, cycloalkanes, and aromatics.
The following describes specific embodiments of the present application in detail. It should be understood that the detailed description and specific examples, while indicating and illustrating the application, are not intended to limit the application.
Example 1
As shown in fig. 1, a heat recovery system for the coagulation process of a rubber-like polymer is composed of the following components:
a mixer M1 for mixing low-temperature hot water (temperature 70 to 90 ℃), high-temperature hot water (temperature 95 to 110 ℃) and a polymer solution;
the first coagulation kettle F1, the liquid outlet of the mixer M1 is communicated with the liquid inlet of the first coagulation kettle F1, the top of the first coagulation kettle F1 is provided with an air outlet, the bottom of the first coagulation kettle F1 is provided with a liquid outlet, and the middle lower part of the first coagulation kettle F1 is provided with an air inlet;
the liquid outlet of the first condensation kettle F1 is connected with the liquid inlet of the second condensation kettle F2 through a first two-pipe, a first kettle colloidal particle water pump P1 is arranged in the first two-pipe, the top of the second condensation kettle F2 is provided with an air outlet, the air outlet of the second condensation kettle F2 is connected with the air inlet of the first condensation kettle F1 through a pipe, and the bottom of the second condensation kettle F2 is provided with a liquid outlet and a low-pressure steam pipe;
the third is condensed cauldron F3, the liquid outlet of second is condensed cauldron F2 with the liquid inlet of third is condensed cauldron F3 and is passed through the second three pipeline and link to each other, be equipped with two cauldron micelle water pumps P2 in the second three pipeline be equipped with concentrator T on two cauldron micelle water pumps P2 with the pipeline between the third is condensed cauldron F3, the top of third is condensed cauldron F3 is equipped with the gas outlet, the gas outlet of third is condensed cauldron F3 pass through the pipeline with first air inlet of condensing cauldron F1 links to each other, the bottom of third is condensed cauldron F3 is equipped with the liquid outlet, the liquid outlet of third is condensed cauldron F3 and is passed through the external three cauldron micelle water pumps P4 of pipeline, wherein:
the concentrator T is provided with a hot water outlet, the hot water outlet of the concentrator T is connected with a liquid inlet of the mixer M1 through a pipeline, and a hot water pump P3 is arranged on the pipeline;
the pipeline connecting the concentrator T and the third condensation kettle F3 is externally connected with a low-temperature hot water inlet pipe for supplementing low-temperature hot water (the temperature is 70-90 ℃) to the third condensation kettle F3.
Further, the hot water outlet of the concentrator T is positioned at the middle lower part of the concentrator T. In another embodiment, the hot water outlet of the concentrator T is located at the bottom of the concentrator T.
Further, the first condensation kettle F1 is provided with a stirring shaft, and a stirring blade is arranged on the stirring shaft;
the second coagulation kettle F2 is provided with a stirring shaft, and a stirring blade is arranged on the stirring shaft;
the third coagulation kettle F3 is provided with a stirring shaft, and a stirring blade is arranged on the stirring shaft. In another embodiment, the first condensation kettle F1 is provided with a stirring shaft, two stirring paddles are arranged on the stirring shaft, and the stirring paddles are respectively positioned at the bottom and the middle of the stirring shaft;
the second coagulation kettle F2 is provided with a stirring shaft, two stirring paddles are arranged on the stirring shaft, and the stirring paddles are respectively positioned at the bottom and the middle of the stirring shaft;
the third coagulation kettle F3 is provided with a stirring shaft, two stirring paddles are arranged on the stirring shaft, and the stirring paddles are respectively positioned at the bottom and the middle of the stirring shaft.
Further, the concentrator T is a single-sleeve type concentrator. In another embodiment, the concentrator T is a T-type concentrator. In yet another embodiment, the concentrator T is a barrel concentrator. In other embodiments, the concentrator T is a cross-sleeve type concentrator.
Example 2
FIG. 2 is a schematic diagram of example 2 of a heat recovery system for a rubber-based polymer coagulation process. As shown in fig. 2, embodiment 2 is substantially the same as embodiment 1, except that:
the hot water outlet of the concentrator T is connected with the liquid inlet of the first condensation kettle F1 through a pipeline, and the mixer M1 is used for mixing low-temperature hot water (the temperature is 70-90 ℃) and polymer solution.
The middle upper part of the third condensation kettle F3 is externally connected with a low-temperature hot water inlet pipe for supplementing low-temperature hot water (the temperature is 70-90 ℃) to the third condensation kettle F3.
Example 3
A method for recovering heat during coagulation of a rubber-based polymer, based on the system for recovering heat during coagulation of a rubber-based polymer described in example 1, comprising:
(1) Separating a part of the hot water from the colloidal particle water from the second coagulation kettle by a concentrator T, and pumping the part of the hot water into the mixer by a hot water pump, wherein:
the temperature of the high-temperature hot water is 95 ℃;
(2) Adding low-temperature hot water into a third condensation kettle through a second three-pipeline, wherein:
the temperature of the low-temperature hot water is 70 ℃;
the volume ratio of the low-temperature hot water to the colloidal particle water entering the third coagulation kettle is 2:100.
further, in the step (1), when the high-temperature hot water is pumped into the mixer by the hot water pump, the weight ratio of the high-temperature hot water and the low-temperature hot water entering the mixer is 1:0.1.
further, the operating pressure of the first coagulation kettle is 0.001MPa, and the temperature is 82 ℃.
Further, the operating pressure of the second coagulation kettle is 0.03MPa, and the temperature is 103 ℃.
Further, the operating pressure of the third coagulation kettle is-0.001 MPa, and the temperature is 95 ℃.
Further, the process is suitable for producing conjugated diene homopolymers, wherein:
the conjugated diene homopolymer is polyisoprene. In another embodiment, the conjugated diene homopolymer is polybutadiene.
Further, the solvent used is an inert hydrocarbon solvent, which is an alkane.
Example 4
A method for recovering heat during coagulation of a rubber-based polymer, based on the system for recovering heat during coagulation of a rubber-based polymer described in example 1, comprising:
(1) Separating a part of the hot water from the colloidal particle water from the second coagulation kettle by a concentrator T, and pumping the part of the hot water into the mixer by a hot water pump, wherein:
the temperature of the high-temperature hot water is 110 ℃;
(2) Adding low-temperature hot water into a third condensation kettle through a second three-pipeline, wherein:
the temperature of the low-temperature hot water is 90 ℃;
the volume ratio of the low-temperature hot water to the colloidal particle water entering the third coagulation kettle is 20:100.
further, in the step (1), when the high-temperature hot water is pumped into the mixer by the hot water pump, the weight ratio of the high-temperature hot water and the low-temperature hot water entering the mixer is 1:10. in another embodiment, when the high temperature hot water is pumped into the mixer by the hot water pump, the weight ratio of the high temperature hot water and the low temperature hot water entering the mixer is 1:5.
further, the operating pressure of the first coagulation kettle is 0.03MPa, and the temperature is 95 ℃.
Further, the operating pressure of the second coagulation kettle is 0.09MPa, and the temperature is 115 ℃.
Further, the operating pressure of the third coagulation kettle is 0.005MPa, and the temperature is 100 ℃.
Further, the process is suitable for producing conjugated diene and vinylarene rubber-based polymers wherein:
the conjugated diene and vinyl aromatic rubber polymer is a random copolymer or a block copolymer of isoprene and styrene. In another embodiment, the conjugated diene and vinyl aromatic rubber-based polymer is a random copolymer or a block copolymer of butadiene and styrene.
Further, the solvent used is an inert hydrocarbon solvent which is a cycloalkane.
Example 5
A method for recovering heat during coagulation of a rubber-based polymer, based on the system for recovering heat during coagulation of a rubber-based polymer described in example 2, comprising:
(1) Separating a part of the high-temperature hot water in the colloidal particle water from the second coagulation kettle through a concentrator T, and pumping the part of the high-temperature hot water into the first coagulation kettle through a hot water pump, wherein:
the temperature of the high-temperature hot water is 100 ℃;
(2) Directly adding low-temperature hot water into a third condensation kettle, wherein:
the temperature of the low-temperature hot water is 80 ℃;
the volume ratio of the low-temperature hot water to the colloidal particle water entering the third coagulation kettle is 10:100.
further, the operating pressure of the first coagulation kettle is 0.02MPa, and the temperature is 90 ℃.
Further, the operating pressure of the second coagulation kettle is 0.06MPa, and the temperature is 103-115 ℃.
Further, the operating pressure of the third coagulation kettle is-0.001-0.005 MPa, and the temperature is 98 ℃.
Further, the process is suitable for producing conjugated diene and vinylarene rubber-based polymers wherein:
the conjugated diene and vinyl aromatic rubber polymer is a random copolymer or a block copolymer of isoprene and alpha-methylstyrene. In another embodiment, the conjugated diene and vinyl aromatic rubber-based polymer is a random or block copolymer of butadiene and alpha-methylstyrene.
Further, the solvent used is an inert hydrocarbon solvent which is an aromatic hydrocarbon
Example 6
A method for recovering heat during coagulation of a rubber-based polymer, based on the system for recovering heat during coagulation of a rubber-based polymer described in example 1, wherein:
feeding a rubber polymer SBS solution (cyclohexane is a solvent) to a mixer M1 in front of a first condensation kettle F1, wherein the mass percent of the polymer is 10%, the temperature is 80 ℃, the SBS solution is mixed with hot water at the mixer M1 at a flow rate of 25000kg/h, the hot water comprises high-temperature hot water and low-temperature hot water, the temperature of the hot water is 105 ℃ and the flow rate of 40000kg/h, the temperature of the low-temperature hot water is 90 ℃, the flow rate of 80000kg/h, the mixed material enters the first condensation kettle F1 at a flow rate of 145000kg/h, the mixed feeding temperature is 93.3 ℃, and the feeding of steam at the bottom of the first condensation kettle F1 (the components are cyclohexane and water) is 25000kg/h (the steam discharged from the tops of a second condensation kettle F2 and a third condensation kettle F3);
cyclohexane in the glue solution is steamed out in a first condensation kettle F1, cyclohexane and part of water vapor are discharged from the kettle top, colloidal particle water at the kettle bottom of the first condensation kettle F1 enters a second condensation kettle F2, external water vapor is introduced into the kettle bottom of the second condensation kettle F2, and the top-of-stillage vapor returns to the first condensation kettle F1;
the colloidal particle water at the bottom of the second condensation kettle F2 is pumped to a concentrator T, 40000kg/h of high-temperature hot water is separated by the concentrator and is returned to the first condensation kettle F1, the temperature of the high-temperature hot water is 105 ℃, the concentrated colloidal particle water is sent to a third condensation kettle F3, low-temperature hot water is added into the third condensation kettle, the colloidal particle water is further subjected to reduced pressure flash evaporation in the third condensation kettle F3, residual solvent is removed, the gas phase of the third condensation kettle F3 is returned to the bottom of the first condensation kettle F1, and the colloidal particle water obtained at the bottom of the third condensation kettle F3 is sent to a post-treatment unit, and a dry glue product is obtained through dehydration and drying.
Further, the first coagulation vessel F1 was operated at a pressure of 0.03MPa (gauge pressure) and a temperature of 92 ℃.
Further, the second coagulation kettle F2 operates at a pressure of 0.05MPa (gauge pressure) and at a temperature of 105 ℃; the bottom steam flow was 5700kg/h.
Further, the feeding rate of the concentrator T is 125160Kg/h, the separating hot water is 40000Kg/h, and the outlet colloidal particle water is 85160Kg/h.
Further, 10000kg/h of low-temperature hot water with the temperature of 90 ℃ is added into the inlet of the third condensation kettle F3, the operation temperature in the third condensation kettle F3 is 99 ℃, and the solvent is further distilled out from the top of the kettle; 92660kg/h of colloidal particle water at the bottom of the coagulation kettle. The power of the third coagulation kettle F3 is 90KW.
Further, the flow rate of the first tank colloidal particle water pump P1 is 141960Kg/h, the flow rate of the second tank colloidal particle water pump P2 is 125160Kg/h, the flow rate of the hot water pump P3 is 40000Kg/h, and the flow rate of the third tank colloidal particle water pump P4 is 92660Kg/h.
Further, 28040kg of steam (cyclohexane content: 79.44 wt%, the balance water) was collected from the steam outlet at the top of the first coagulation kettle F1, and the three-kettle colloidal particle water pump P4 of the third coagulation kettle F3 was fed to post-treatment and drying to obtain 2502.5kg of dry gel, wherein the cyclohexane content in the dry gel was 0.1 wt%. The steam consumption in the condensation section is as follows: 2.28t/t dry glue.
Comparative example 1 (relative to example 6)
Comparative example 1 employed a three-kettle coacervation and concentrator technique. Substantially the same as in example 6, the difference is only that:
the flow rate of the hot water returned by the concentrator T is different;
the third coagulation kettle F3 is not supplemented with low-temperature hot water.
The specific process flow is as follows:
mixing a rubber polymer SBS solution (10% by mass of polymer) with hot water at a flow rate of 25000kg/h in a mixer M1, wherein the hot water comprises high-temperature hot water and low-temperature hot water, the temperature of the hot water is 105 ℃, the flow rate is 40000kg/h, the temperature of the low-temperature hot water is 90 ℃, the flow rate is 90000kg/h, the temperature of the mixed material is 92.1 ℃, the flow rate of 145000kg/h is used for entering a first condensation kettle F1, and the steam feed (comprising cyclohexane and water) at the kettle bottom of the first condensation kettle F1 is 25300kg/h (the steam discharged from the kettle tops of a second condensation kettle F2 and a third condensation kettle F3);
further, the operating pressure of the first coagulation kettle F1 is 0.03MPa (gauge pressure) and the temperature is 92 ℃;
the second coagulation kettle F2 has an operating pressure of 0.05MPa (gauge pressure) and an operating temperature of 105 ℃; the steam flow rate fed by the steam feeding device is 6000kg/h;
the feeding rate of the concentrator T is 125450Kg/h, the separating hot water is 30000Kg/h, and the outlet colloidal particle water is 95450Kg/h.
The operating temperature of the third coagulation kettle F3 is 99 ℃; the inlet of the third coagulation kettle is not added with low-temperature hot water, 92950kg/h of colloidal particle water is discharged from the coagulation system, and the power of the third coagulation kettle F3 is 90KW.
The flow rate of the first kettle colloidal particle water pump P1 is 142250Kg/h, the flow rate of the second kettle colloidal particle water pump P2 is 125450Kg/h, the flow rate of the hot water pump P3 is 30000Kg/h, and the flow rate of the third kettle colloidal particle water pump P4 is 92950Kg/h.
Further, 28050kg of steam (hexane content is 79.40 wt% and the balance is water) is collected from a steam outlet at the top of the first coagulation kettle F1, and a three-kettle colloidal particle water pump P4 of the third coagulation kettle F3 pumps to post-treat and dry to obtain 2503.75kg of dry glue, wherein the hexane content in the dry glue is 0.12 wt%. The steam consumption in the condensation section is as follows: 2.40t/t dry glue.
Comparative example 2 (relative to example 6)
Comparative example 2 employed the prior art three-pot coagulation technique without a concentrator.
The specific process flow is as follows:
the rubber polymer SBS solution (polymer concentration 10% and solvent cyclohexane) was mixed with hot water (temperature 90 ℃ C., flow 60000 kg/h) at a flow rate of 7500kg/h and then fed into the first coagulation kettle F1 at a flow rate of 67500kg/h, and the flow rate of the steam supplied from the lower part of the kettle was kept at 675kg/h (mixture of solvent and steam discharged from the tops of the second coagulation kettle F2 and the third coagulation kettle F3);
the operating conditions of the first coagulation kettle F1 include: gauge pressure is 0.03MPa, and temperature is 90 ℃;
the colloidal particle water discharged from the first coagulation kettle F1 enters a second coagulation kettle F2 through a first colloidal particle water pump, and the flow rate of the first colloidal particle water pump is 59748kg/h;
the operating temperature of the second coagulation kettle F2 is 105 ℃; the steam flow rate fed was 2100kg/h (steam fed from an external steam device);
the colloidal particle water discharged from the second coagulation kettle F2 enters a third coagulation kettle F3 through a second colloidal particle water pump, and the flow rate of the second colloidal particle water pump is 61315kg/h
The operating conditions of the third coagulation kettle F3 include: gauge pressure is 0.003MPa, and temperature is 97 ℃;
and the colloidal particle water discharged from the third coagulation kettle F3 is discharged through a third colloidal particle water pump for aftertreatment, and the flow rate of the third colloidal particle water pump is 61265kg/h.
The coagulation system consumed 60000kg of water and 2250kg of steam in total, 7500kg of the rubber polymer SBS solution was treated, 8427kg of steam water (cyclohexane content 79.3 wt%) was collected from the steam outlet at the top of the first coagulation kettle F1, and the third colloidal particle water pump P5 of the third coagulation kettle F3 was fed to post-treatment and dried to obtain 751.25kg of dry rubber, in which the cyclohexane content was 0.25 wt%. The steam consumption in the condensation section is as follows: 2.80t/t dry glue.
Analysis of results:
according to example 6 and comparative example 1, it can be seen that the high-temperature hot water flow rate returned to the first coagulation kettle F1 in example 6 is 40000kg/h under the same treatment amount, whereas the high-temperature hot water flow rate returned to the first coagulation kettle F1 in comparative example 1 is 30000kg/h, and the effect of recycling the high-temperature hot water is on the one hand reflected on the feeding temperature of the first coagulation kettle F1, and the feeding temperature of the first coagulation kettle F1 in example 6 is 93.3 ℃ which is 1.2 ℃ higher than the feeding temperature of the first coagulation kettle F1 in comparative example 1, thereby improving the dispersion effect of the glue solution. Wherein:
the first effect is to facilitate solvent recovery, with respect to the cyclohexane content of the initial dry gel product, example 6 has a cyclohexane content of 0.1% by weight, whereas comparative example 1 has a cyclohexane content of 0.12% by weight.
The second effect is that the effect of recycling the final high-temperature hot water is reflected on the steam consumption, wherein the steam consumption is 5700kg/h in the embodiment 6 of the application, and the steam consumption is 6000kg/h in the comparative example 1; the purpose of further reducing steam consumption can be achieved. The application can realize all functions of the original device, can better utilize the heat energy of the high-temperature hot water, saves steam consumption and reduces the energy consumption and the material consumption of the device.
The third effect of the application is that by adding part of low-temperature hot water into the third coagulation kettle, the original equipment of the coagulation kettle can normally operate, and the overload of stirring current caused by overhigh colloidal particle concentration is prevented. The same power as in comparative example 1, but with 10000Kg/h more returned high temperature hot water.
As can be seen from example 6 and comparative example 2, the steam consumption per unit of dry gel is highest when the non-concentrator technique is used, the solvent content of comparative dry gel is best when the solvent separation effect of example 6 is used, the dry gel content of the product is 0.1% (weight percent), the cyclohexane content in the dry gel of comparative example 2 is 0.25% by weight, and the solvent recovery rate is lower than that of example 6.
The embodiments of the present application have been described in detail. However, the present application is not limited to the above-described embodiments, and various modifications may be made within the knowledge of those skilled in the art without departing from the spirit of the present application.
Claims (10)
1. A heat recovery system for the coagulation process of rubber polymers comprises the following components:
a mixer for mixing low-temperature hot water and a polymer solution or for mixing low-temperature hot water, high-temperature hot water and a polymer solution;
the liquid outlet of the mixer is communicated with the liquid inlet of the first condensation kettle, the top of the first condensation kettle is provided with a gas outlet, the bottom of the first condensation kettle is provided with a liquid outlet, and the middle lower part of the first condensation kettle is provided with a gas inlet;
the liquid outlet of the first condensation kettle is connected with the liquid inlet of the second condensation kettle through a first two-pipe, a first kettle colloidal particle water pump is arranged in the first two-pipe, the top of the second condensation kettle is provided with a gas outlet, the gas outlet of the second condensation kettle is connected with the gas inlet of the first condensation kettle through a pipe, and the bottom of the second condensation kettle is provided with a liquid outlet and a low-pressure steam pipe;
the third is condensed cauldron, the liquid outlet of second is condensed the cauldron with the liquid inlet of third is condensed the cauldron and is passed through the second third pipeline and link to each other, be equipped with two cauldron micelle water pumps in the second third pipeline two cauldron micelle water pumps with be equipped with the concentrator on the pipeline between the third is condensed the cauldron, the top of third is condensed the cauldron is equipped with the gas outlet, the gas outlet of third condense the cauldron pass through the pipeline with the air inlet of first condensing the cauldron links to each other, the bottom of third is condensed the cauldron is equipped with the liquid outlet, the liquid outlet of third is condensed the cauldron and is passed through the external three cauldron micelle water pumps of pipeline, its characterized in that:
the concentrator is provided with a hot water outlet, the hot water outlet of the concentrator is connected with a liquid inlet of the mixer or a liquid inlet of the first condensation kettle through a pipeline, and a hot water pump is arranged on the pipeline;
the pipeline connecting the concentrator and the third condensation kettle is externally connected with a low-temperature water inlet pipe for supplementing low-temperature water to the third condensation kettle, or
The middle upper part of the third condensation kettle is externally connected with a low-temperature hot water inlet pipe for supplementing low-temperature hot water to the third condensation kettle.
2. A process heat recovery system for the coagulation of a rubbery polymer as defined in claim 1 wherein the hot water outlet of said concentrator is located in the lower middle or bottom of said concentrator;
the concentrator is one of a single-sleeve type concentrator, a T-type concentrator, a barrel-type concentrator or a cross sleeve type concentrator.
3. The heat recovery system for the coagulation process of a rubber polymer as set forth in claim 1, wherein said first coagulation kettle is provided with a stirring shaft, and said stirring shaft is provided with at least one stirring blade;
the second coagulation kettle is provided with a stirring shaft, and at least one stirring blade is arranged on the stirring shaft;
the third coagulation kettle is provided with a stirring shaft, and at least one stirring blade is arranged on the stirring shaft.
4. A method for recovering heat during the coagulation of a rubber-like polymer, based on the coagulation process heat recovery system of a rubber-like polymer as defined in any one of claims 1 to 3, comprising:
(1) Separating a portion of the high temperature hot water from the micellar water from the second coagulation kettle by a concentrator and pumping the portion of the high temperature hot water into a mixer or the first coagulation kettle by a hot water pump, wherein:
the temperature of the high-temperature hot water is 95-110 ℃;
(2) Adding hot, low temperature water through a second third conduit or directly to a third coagulation kettle, wherein:
the temperature of the low-temperature hot water is 70-90 ℃;
the volume ratio of the low-temperature hot water to the colloidal particle water entering the third coagulation kettle is (2-20): 100.
5. the method for recovering heat during the coagulation process of a rubber-like polymer as defined in claim 4, wherein in the step (1), when the high-temperature hot water is pumped into the mixer by the hot water pump, the weight ratio of the high-temperature hot water to the low-temperature hot water fed into the mixer is 1:0.1 to 10.
6. The method for recovering heat during the coagulation of a rubber polymer as defined in claim 4, wherein the first coagulation kettle is operated at a pressure of 0.001 to 0.03MPa and a temperature of 82 to 95 ℃.
7. The method for recovering heat during the coagulation of a rubber polymer as defined in claim 4, wherein the second coagulation kettle is operated at a pressure of 0.03 to 0.09MPa and a temperature of 103 to 115 ℃.
8. The method for recovering heat during the coagulation of a rubber polymer as defined in claim 4, wherein the third coagulation kettle is operated at a pressure of-0.001 to 0.005MPa and a temperature of 95 to 100 ℃.
9. A process for recovering heat from a rubber polymer coagulation process as defined in claim 4, wherein said process is adapted for producing a conjugated diene homopolymer or a conjugated diene and vinyl aromatic rubber polymer wherein:
the conjugated diene homopolymer is polyisoprene or polybutadiene;
the conjugated diene and vinyl aromatic rubber polymer is random copolymer or block copolymer of isoprene or butadiene and styrene, or:
the conjugated diene and vinyl aromatic rubber polymer is a random copolymer or a block copolymer of isoprene or butadiene and alpha-methyl styrene.
10. A process for recovering heat from a rubber polymer coagulation process as defined in claim 9, wherein the solvent used for producing the conjugated diene homopolymer or the conjugated diene and vinyl aromatic rubber polymer is an inert hydrocarbon solvent selected from the group consisting of alkane, cycloalkane and aromatic hydrocarbon.
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