CN217392374U - Production system of acrylonitrile-acrylic ester-styrene copolymer resin - Google Patents

Production system of acrylonitrile-acrylic ester-styrene copolymer resin Download PDF

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CN217392374U
CN217392374U CN202220295440.4U CN202220295440U CN217392374U CN 217392374 U CN217392374 U CN 217392374U CN 202220295440 U CN202220295440 U CN 202220295440U CN 217392374 U CN217392374 U CN 217392374U
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suspension polymerization
reaction kettle
polymerization reaction
production system
temperature control
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王明花
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Abstract

The present application relates to a production system of acrylonitrile-acrylate-styrene copolymer resin, comprising: an emulsion polymerization reaction kettle, a suspension polymerization reaction kettle, a dehydration device and a drying device; the suspension polymerization reaction kettle is also provided with a suspension polymerization reaction kettle jacket for controlling the temperature in the suspension polymerization reaction kettle and a first circulating temperature control loop communicated with the suspension polymerization reaction kettle jacket, and a first temperature control device is arranged in the first circulating temperature control loop. The production system can conveniently control the temperature of the reaction kettle through the jacket arranged on the emulsion polymerization reaction kettle and the suspension polymerization reaction kettle and the circulating temperature control loop communicated with the jacket, and can relieve the uneven internal temperature of the reaction kettle and the scaling of the kettle wall caused by overhigh temperature of the kettle wall; the devolatilization device can conveniently remove residual monomer components and the like in the polymerization product slurry, and recycle the recovered monomer components and the like to the suspension polymerization reaction kettle for reuse.

Description

Production system of acrylonitrile-acrylic ester-styrene copolymer resin
Technical Field
The utility model relates to a production system of polymer resin, especially relate to production system of acrylonitrile-acrylic ester-styrene-terpolymer resin.
Background
The acrylonitrile-acrylate-styrene-terpolymer has a structure similar to that of Acrylonitrile Butadiene Styrene (ABS) resin, and is a structurally stable core-shell graft copolymer formed by grafting styrene and acrylonitrile copolymer on a shell by using polyacrylate with stable structure as a core. The mechanical property of the ABS resin is similar to that of ABS resin, and the ABS resin has good weather resistance and impact resistance. In addition, the acrylonitrile-acrylate-styrene-terpolymer resin also has remarkable heat resistance and chemical resistance, and is engineering plastic with wide application.
The production system of the acrylonitrile-acrylate-styrene copolymer resin with the acrylate content of 10-50 wt% is needed in the field, so that the phenomenon that a large amount of scales are formed on the wall of a suspension polymerization reaction kettle in the production process and the use of the reaction kettle is influenced, and meanwhile, the system can stably produce resin products with proper particle size distribution and can be directly used for downstream forming processing.
Disclosure of Invention
The present application provides a production system of acrylonitrile-acrylate-styrene copolymer resin, characterized in that the production system comprises:
the device comprises an emulsion polymerization reaction kettle, wherein an emulsion polymerization raw material feeding hole for feeding emulsion polymerization raw materials is formed in the upper part of the emulsion polymerization reaction kettle; the lower part of the emulsion polymerization reaction kettle is provided with a latex feed liquid discharge port for discharging product latex feed liquid;
the device comprises a suspension polymerization reaction kettle, a suspension polymerization reaction kettle and a polymerization reaction kettle, wherein the suspension polymerization reaction kettle is provided with a suspension polymerization raw material feeding hole for feeding a suspension polymerization raw material and a polymerization resin discharging hole for discharging a suspension polymerization product, and the suspension polymerization raw material feeding hole is communicated with a latex material liquid discharging hole of the emulsion polymerization reaction kettle in a fluid manner, so that the latex material liquid from the emulsion polymerization reaction kettle can enter the suspension polymerization reaction kettle;
a dewatering device configured such that the devolatilized treated suspension polymerization product slurry can be dewatered in the dewatering device;
a drying device, which is communicated with the dehydration device, so that the dehydrated polymer material is dried in the drying device;
the system comprises a suspension polymerization reaction kettle, a first circulation temperature control loop and a second circulation temperature control loop, wherein the suspension polymerization reaction kettle is also provided with a suspension polymerization reaction kettle jacket for controlling the temperature in the suspension polymerization reaction kettle, the first circulation temperature control loop is communicated with the suspension polymerization reaction kettle jacket, a first temperature control device is arranged in the first circulation temperature control loop, and the first temperature control device is a heat exchanger and/or a steam-water mixer.
In one embodiment, the emulsion polymerization reactor is further provided with an emulsion polymerization reactor jacket for the emulsion polymerization reactor and a second circulation temperature control loop communicated with the emulsion polymerization reactor jacket, wherein a second temperature control device is arranged in the second circulation temperature control loop, and the second temperature control device is a heat exchanger and/or a steam-water mixer.
In one embodiment, a baffle is disposed within the emulsion polymerization reactor, and the ratio of the height of the baffle to the height of the straight wall of the emulsion polymerization reactor is from 0.6 to 1.0: 1; the volume of the emulsion polymerization reaction kettle is 10-50m 3 The maximum working pressure is 140 kpa.
In one embodiment, the emulsion polymerization reaction kettle is internally provided with a stirrer, the stirrer is a slant paddle type stirrer with 1-3 layers of blades, the ratio of the diameter D of the tip of each blade to the diameter D of the inner wall of the emulsion polymerization reaction kettle is 0.2-0.6:1, and the stirring speed is 50-150 rpm.
In one embodiment, the emulsion polymerization reaction kettle is also provided with an oxygen-containing gas feeding device with a system for controlling the oxygen content above the liquid level, a nitrogen feeding device with a control system for adjusting the total pressure above the liquid level within the range of 0 to 140kpa, and a reduced-pressure vacuumizing device within the range of 0 to 60kpa, wherein the reduced-pressure vacuumizing device comprises a part for condensing and recycling volatile matters in tail gas.
In one embodiment, the production system further comprises:
the emulsion feed liquid filtering and treating equipment is configured to enable the emulsion feed liquid to be further treated by the emulsion feed liquid filtering and treating equipment before entering the suspension polymerization reaction kettle.
In one embodiment, a baffle is disposed within the suspension polymerization reactor, and the ratio of the height of the baffle to the height of the straight wall of the suspension polymerization reactor is from 0.6 to 1.0: 1, the ratio of the width of the baffle plate to the inner diameter of the kettle is (0.005-0.1): 1; the volume of the suspension polymerization reaction kettle is 20-80m 3 The working pressure is-60 kpa vacuum to 140kpa positive pressure.
In one embodiment, the suspension polymerization reactor is provided with a stirrer, the stirrer is a pitched blade type stirrer with 1-3 layers of blades, the ratio of the diameter D of the tip of each blade to the diameter D of the inner wall of the emulsion polymerization reactor is 0.2-0.6:1, and the stirring speed is 50-150 rpm.
In one embodiment, the suspension polymerization reaction kettle is further provided with a nitrogen adding device with a control system for adjusting the total pressure above the liquid level within the range of 0-140kpa, and a reduced-pressure vacuumizing device within the range of 0-60 kpa, wherein the reduced-pressure vacuumizing device comprises a part for condensing and recycling volatile matters in tail gas.
In one embodiment, the production system further comprises a third filtration treatment apparatus for filtration treatment of the devolatilized treated suspension polymerization product slurry, disposed upstream of the dewatering device.
In one embodiment, the dewatering device is selected from one or more of a continuous centrifuge apparatus, a continuous pressure filter;
the operating conditions of the continuous centrifuge apparatus include: the temperature is 40-60 ℃, the pressure is 3-5kpa, and the rotating speed is 1000-;
the operating conditions of the continuous pressure filter comprise: the pressure is 120-1000kpa, and the thickness of the filter cake is 10-250 mm.
In one embodiment, the drying means is selected from one or more of a spiral-lift drying bed, a fluidized drying bed, a rake dryer.
In one embodiment, the drying apparatus is configured such that the average residence time of the polymer mass in the drying apparatus is from 5 to 50 minutes, the operating temperature is from 50 to 150 ℃, and a nitrogen recycle system is formulated.
In one embodiment, the production system further comprises:
a devolatilizer disposed between the suspension polymerization reactor and the dehydration device, wherein the devolatilizer is provided with a feed port for feeding the suspension polymerization product and a discharge port for discharging the devolatilized suspension polymerization product, the feed port of the devolatilizer is communicated with the discharge port of the polymerization resin of the suspension polymerization reactor, so that the suspension polymerization product discharged through the discharge port of the polymerization resin of the suspension polymerization reactor can be stripped in the devolatilizer, and a vapor phase outlet of the devolatilizer is connected with a volatile vapor condensation recovery device.
In one embodiment, the production system further comprises:
a suspension polymerization product slurry filtration treatment apparatus configured such that the suspension polymerization product also passes through the suspension polymerization product slurry filtration treatment apparatus prior to entering the devolatilizer.
In one embodiment, the devolatilizer is a stripper;
volatile matter vapour condensation recovery unit includes:
a condenser configured to communicate with a stripped material outlet of the stripper column such that stripped material exiting the stripper column is cooled in the condenser;
the condenser is provided with a condensed liquid phase outlet which is communicated with the suspension polymerization reaction kettle, so that a condensed liquid phase flow discharged from the condensed liquid phase outlet circulates back to the suspension polymerization reaction kettle.
In one embodiment, the devolatilizer operates under the following conditions: the vacuum degree is between-5 kpa and-60 kpa, and the temperature is between 50 and 80 ℃.
In one embodiment, the devolatilizer is a plate stripper, having a diameter/height ratio of 0.01 to 0.3; or the stirred tank is provided with a decompression vacuumizing device, wherein the stirred tank is provided with a jacket for controlling the temperature in the stirred tank and a third circulating temperature control loop communicated with the jacket of the stirred tank, the third circulating temperature control loop is internally provided with a third temperature control device, and the third temperature control device is a heat exchanger and/or a steam-water mixer.
In one embodiment, the production system produces an acrylonitrile-acrylate-styrene-terpolymer resin having the following weight-based particle size distribution:
the average value of the proportion of the particles with more than 30 meshes is 16.20 percent, the standard deviation is 7.66 percent,
the average value of the ratio of the particles with 30-60 meshes is 56.45 percent, the standard deviation is 8.21 percent,
the average value of the proportion of 60-80 mesh particles is 17.59%, and the standard deviation is 6.3%.
In one embodiment, the production system produces an acrylonitrile-acrylate-styrene-terpolymer resin having the following weight-based particle size distribution: the average value of the ratio of the particles of 30-80 meshes is 90%, the standard deviation is 8%, and the content of the acrylic ester is 10-50 wt%.
The production system can conveniently control the temperature of the reaction kettle through the jacket arranged on the emulsion polymerization reaction kettle and the suspension polymerization reaction kettle and the circulating temperature control loop communicated with the jacket, and can relieve the uneven internal temperature of the reaction kettle and the scaling of the kettle wall caused by overhigh temperature of the kettle wall; the devolatilization device can conveniently remove residual monomer components and the like in the polymerization product slurry, and recycle the recovered monomer components and the like to the suspension polymerization reaction kettle for reuse.
Drawings
FIG. 1 shows a schematic view of one embodiment of a production system of the present application;
FIG. 2 shows a schematic view of another embodiment of the production system of the present application.
Detailed Description
The present application is described in further detail below with reference to the figures and examples. The features and advantages of the present application will become more apparent from the description.
The word "exemplary" is used exclusively herein to mean "serving as an example, embodiment, or illustration. Any embodiment described herein as "exemplary" is not necessarily to be construed as preferred or advantageous over other embodiments. While the various aspects of the embodiments are presented in drawings, the drawings are not necessarily drawn to scale unless specifically indicated.
In addition, the technical features described below in the different embodiments of the present application may be combined with each other as long as they do not conflict with each other.
In this application, the terms "upstream" and "downstream" are used with reference to the direction of flow of the material. For example, when the reactant stream flows from bottom to top, "upstream" refers to a position located below, and "downstream" refers to a position located above. For example, when reactant flow is from the left to the right, "upstream" means a location to the left and "downstream" means a location to the right.
As shown in fig. 1 and 2, the present application provides a system for producing an acrylonitrile-acrylate-styrene copolymer resin, which includes an emulsion polymerization reaction tank 100, a suspension polymerization reaction tank 200, an optional devolatilizer 300, a dehydration unit 400, and a drying unit 500. These devices and their connections are described separately below.
The production system of the present application includes an emulsion polymerization reactor 100, and the emulsion polymerization reactor 100 may be a stirred tank polymerization reactor with a stirrer 103. The upper part of the emulsion polymerization reaction kettle 100 is provided with an emulsion polymerization raw material inlet 101 for feeding emulsion polymerization raw materials, and the inlet is used for feeding the emulsion polymerization raw materials to the emulsion polymerization reaction kettle 100. The lower part of the emulsion polymerization reaction kettle 100 is provided with an emulsion feed liquid discharge port 102 for discharging a product emulsion feed liquid, and the emulsion feed liquid is used for discharging the product emulsion feed liquid of emulsion polymerization and entering a downstream device.
Disposed within the emulsion polymerization reactor 100 is a baffle having a height to the straight wall height of the emulsion polymerization reactor in a ratio of about 0.6 to 1.0: 1, for example, about 0.6 to 0.9: 1. The volume of the emulsion polymerization reaction kettle is 10-50m 3 The maximum working pressure is 140 kpa.
The stirrer 103 is a slant paddle type stirrer having 1 to 3 layers of blades, the ratio of the blade tip diameter D to the inner wall diameter D of the emulsion polymerization reaction vessel 100 is 0.2 to 0.6:1, and the stirring speed is 50 to 150 rpm.
In one embodiment, the emulsion polymerization reactor 100 is further provided with an oxygen-containing gas feeding device 104 with a system for controlling the oxygen content above the liquid surface, a nitrogen feeding device 108 with a control system for adjusting the total pressure above the liquid surface, and a vacuum-pumping device 109 for controlling the oxygen content and the pressure of the emulsion polymerization system during the emulsion polymerization process. The nitrogen addition unit 108 was provided with a control system to regulate the total pressure above the liquid level in the range of 0 to 140 kpa. The pressure reduction vacuumizing device 109 generates pressure in the range of 0-60 kpa, and the pressure reduction vacuumizing device 109 comprises a part for condensing and recycling volatile matters in tail gas.
In one embodiment, the emulsion polymerization reactor 100 is further provided with an emulsion polymerization reactor jacket 105 for controlling the temperature in the emulsion polymerization reactor, and a second circulation temperature control loop 107 communicated with the emulsion polymerization reactor jacket 105, wherein a second temperature control device 106 is arranged in the second circulation temperature control loop, and the second temperature control device 106 is a heat exchanger and/or a steam-water mixer. The temperature in the emulsion polymerization reactor 100 can be controlled during the emulsion polymerization by the emulsion polymerization reactor jacket 105 and the second circulation temperature control loop 107 communicating with the emulsion polymerization reactor jacket, and for example, the temperature can be advantageously controlled at 40 to 75 ℃. The medium flowing in the emulsion polymerization reactor jacket 105 and the second circulation temperature control loop 107 communicating with the emulsion polymerization reactor jacket may be water or a steam-water mixture. The emulsion polymerization in the emulsion polymerization reactor may be carried out in stages at a temperature of 40 to 75 ℃ for 4 to 6 hours.
When the emulsion polymerization is started in the emulsion polymerization reaction kettle 100, the materials are fed according to the mixture ratio, and the materials comprise acrylate monomers such as butyl acrylate, and other necessary additives such as an initiator, so as to prepare the emulsion feed liquid meeting the requirements. During the polymerization, the oxygen concentration and the pressure (pressurized by nitrogen) above the emulsion polymerization reactor 100 were monitored, and the oxygen content and the reaction pressure in the reactor were kept constant by introducing oxygen and nitrogen. When the content of the acrylate monomer in the reactant is less than 3000ppm, a terminator can be added to stop the reaction, and the latex feed liquid is obtained.
In one embodiment, the production system of the present application further comprises an emulsion feed liquid filtering and processing device 110, wherein the emulsion feed liquid filtering and processing device 110 is disposed downstream of the emulsion polymerization reactor 100 and upstream of the suspension polymerization reaction reactor 200, so that the emulsion feed liquid is further processed by the emulsion feed liquid filtering and processing device 110 before entering the suspension polymerization reaction reactor 200.
The production system of the present application includes a suspension polymerization reactor 200. The suspension polymerization reactor 200 may be a stirred polymerization reactor with a stirrer 203. The suspension polymerization reactor 200 is provided with a suspension polymerization raw material feed port 201 for feeding a suspension polymerization raw material, for feeding the suspension polymerization raw material to the suspension polymerization reactor 200. The suspension polymerization raw material feed port 201 may be provided in the upper and/or lower portion of the suspension polymerization reactor 200 as required. In one embodiment, the suspension polymerization raw material feed port 201 has a plurality of ports, wherein the feed port for feeding the latex feed liquid is provided in the upper and/or lower portion of the suspension polymerization reaction tank 200. The suspension polymerization reactor 200 is provided at a lower portion thereof with a polymerization resin discharge port 202 for discharging a suspension polymerization product, and the suspension polymerization product is discharged to a downstream apparatus.
In one embodiment, the suspension polymerization reactor 200 is further provided with a suspension polymerization reactor jacket 205 for controlling the temperature in the suspension polymerization reactor, and a first circulating temperature control loop 207 in communication with the suspension polymerization reactor jacket 205, wherein the first circulating temperature control loop is provided with a first temperature control device 206, and the first temperature control device 206 is a heat exchanger and/or a steam-water mixer. By means of the suspension polymerization reactor jacket 205 and the first circulation temperature control circuit 207 communicating with said suspension polymerization reactor jacket 205, the temperature inside the suspension polymerization reactor 200 can be controlled during the suspension polymerization, for example, the temperature can be advantageously controlled at 40 to 75 ℃, whereby fouling inside the reactor can be avoided. The medium flowing in the suspension polymerization reactor jacket 205 and the first circulating temperature control loop 207 communicating with the suspension polymerization reactor jacket 205 may be water or a steam-water mixture. The suspension polymerization in the suspension polymerization reactor may be carried out at a temperature of 40 to 75 ℃ for 4 to 10 hours.
Baffles are disposed within the suspension polymerization reactor 200, the ratio of the height of the baffles to the height of the straight wall of the suspension polymerization reactor being from about 0.6 to 1.0: 1, e.g., about 0.6-0.9: 1; the width of the baffle is about 0.005-0.1 of the internal diameter of the tank. The volume of the suspension polymerization reactor is about 20-80m 3 The operating pressure may be from-60 kpa vacuum to 140kpa positive pressure (gauge).
The stirrer 203 is a slant paddle type stirrer having 1-3 layers of blades, the ratio of the blade tip diameter D to the inner wall diameter D of the suspension polymerization reaction kettle 200 is 0.2-0.6:1, and the stirring speed is 50-150 rpm.
In one embodiment, the suspension polymerization reactor 200 is further provided with a nitrogen adding device 208 and a vacuum pumping device 209 with control systems for adjusting the total pressure above the liquid level, and the nitrogen adding device and the vacuum pumping device are respectively used for controlling the pressure in the suspension polymerization process. The nitrogen addition unit 208 is provided with a control system to regulate the total pressure above the liquid level in the range of 0 to 140 kpa. The pressure reducing vacuum-pumping device 209 generates pressure in the range of 0 to-60 kpa, and the pressure reducing vacuum-pumping device 209 comprises a part for condensing and recycling volatile components in the tail gas.
When the suspension polymerization starts in the suspension polymerization reaction kettle 200, the materials are fed according to the mixture ratio, the materials comprise latex feed liquid from the emulsion polymerization reaction kettle 100, styrene and acrylonitrile monomers, and other necessary auxiliary agents such as an initiator, and the suspension polymerization product meeting the requirements is prepared. During the polymerization, the pressure of the suspension polymerization reactor 200 was monitored (pressurized with nitrogen gas) and the reaction pressure in the reactor was kept constant by introducing nitrogen. When the conversion rate of the styrene monomer in the suspension polymerization reaction kettle reaches more than 98 percent, the reaction can be stopped to obtain a suspension polymerization product.
In the process of adding the material liquid into the suspension polymerization reaction kettle, the stirring speed of the stirrer 203 is half of the normal working stirring speed when the material liquid is added; when the material liquid level overflows the uppermost stirrer blade and is higher than the blade level, the stirring speed of the stirrer is recovered to the normal working stirring speed.
After the suspension polymerization, the suspension polymerization product may be subjected to a devolatilization process. As shown in FIG. 1, in one embodiment, the suspension polymerization reactor 200 is used for devolatilizing the contents of the suspension polymerization reactor after the suspension polymerization is completed, without separately providing a devolatilizing apparatus. In the devolatilization process, the temperature of the suspension polymerization product in the suspension polymerization reactor 200 may be increased by the suspension polymerization reactor jacket 205 and the first circulation temperature control loop 207 communicating with the suspension polymerization reactor jacket 205, thereby removing the volatile components therefrom. The high temperature steam can be advantageously converted to a medium of a suitable temperature by the first temperature control device 206, thereby avoiding the high temperature steam from directly contacting the suspension polymerization product in the devolatilization process or the high temperature steam from directly contacting the wall of the suspension polymerization reactor, thereby reducing the fouling of the suspension polymerization product in the suspension polymerization reactor.
As shown in fig. 2, in one embodiment, the production system further comprises a devolatilizer 300, the devolatilizer 300 being disposed between the suspension polymerization reactor 200 and the dehydration unit 400 for devolatilizing the suspension polymerization product from the suspension polymerization reactor 200. The devolatilizer 300 is provided with a feed port 301 for feeding a suspension polymerization product and a discharge port 302 for discharging a devolatilized suspension polymerization product, the devolatilizer feed port 301 being communicated with the polymerization resin discharge port 202 of the suspension polymerization reactor so that the suspension polymerization product discharged through the polymerization resin discharge port 202 of the suspension polymerization reactor can be devolatilized in the devolatilizer; the vapor phase outlet of the devolatilizer 300 is connected to a volatile vapor condensation recovery unit 310 for condensing the vapor mixture containing the polymerized monomers to recover unreacted polymerized monomers, etc. The volatile gas condensation recovery device 310 is also communicated with the feed port 201 of the suspension polymerization reaction kettle 200, so that the recovered polymerization monomers are recycled to the suspension polymerization reaction kettle 200 for reaction. The devolatilization process in the devolatilizer 300 is carried out at a vacuum of-30 kpa to-60 kpa and a temperature of 50-80 ℃.
In one embodiment, the production system further comprises a suspension polymerization product slurry filtration process apparatus 210, the suspension polymerization product slurry filtration process apparatus 210 disposed downstream of the suspension polymerization kettle 200 and upstream of the devolatilizer 300, the suspension polymerization product slurry filtration process apparatus 210 configured such that the suspension polymerization product is further processed by the suspension polymerization product slurry filtration process apparatus 210 prior to entering the devolatilizer 300.
In one embodiment, the devolatilizer 300 is a stripper, such that the devolatilization process occurs within the stripper. The volatile vapor condensing and recycling device 310 comprises a condenser which is configured to be communicated with a stripping material outlet of the stripping tower, so that the stripping material discharged from the stripping tower is cooled in the condenser; the condenser is provided with a condensed liquid phase outlet which is communicated with the suspension polymerization reaction kettle, so that a condensed liquid phase flow discharged from the condensed liquid phase outlet circulates back to the suspension polymerization reaction kettle. In one embodiment, the devolatilizer is a plate stripper, having a diameter/height ratio of 0.01 to 0.3.
In one embodiment, the devolatilization device is a stirred tank with a vacuum pump, wherein the stirred tank with the vacuum pump is provided with a jacket for controlling the temperature in the tank and a third circulating temperature control loop communicated with the jacket of the stirred tank, and the third circulating temperature control loop is provided with a third temperature control device which is a heat exchanger and/or a steam-water mixer.
In one embodiment, the production system further comprises a dewatering device 400, the dewatering device 400 being configured such that the devolatilized, treated suspension polymerization product slurry may be dewatered in the dewatering device. As shown in FIG. 1, the dehydration apparatus 400 may be communicated with the discharge port 202 of the suspension polymerization reactor 200, so that the suspension polymerization product subjected to devolatilization in the suspension polymerization reactor 200 is introduced into the dehydration apparatus 400 to be dehydrated. As shown in fig. 2, the dehydration apparatus 400 may be in communication with the devolatilizer 300 such that the devolatilized suspension polymerization product in the devolatilizer 300 is input to the dehydration apparatus 400 for dehydration.
In one embodiment, the production system further comprises a filtration treatment apparatus 320 for filtration treatment of the devolatilized, treated suspension polymerization product slurry, the filtration treatment apparatus 320 being disposed upstream of the dewatering device 400. The filtration process apparatus 320 can filter out lumps from the devolatilized suspension polymerization product slurry to facilitate subsequent dewatering.
In one embodiment, the dewatering device 400 is selected from one or more of a continuous centrifuge apparatus, a continuous pressure filter. The dewatering device 400 can also be connected with a circulating water treatment device 410 for treating the filtrate obtained by the dewatering device 400. The filtrate may be used as wash water for a tail gas treatment device, or recycled to the emulsion polymerization reactor 100 and/or the suspension polymerization reactor 200, to reduce the subsequent wastewater treatment capacity. In one embodiment, the dehydration apparatus 400 is a continuous centrifuge device operating at a temperature of 40-60 deg.C, a pressure of 3-5kpa, and a rotation speed of 1000-.
In one embodiment, the dewatering device 400 is a continuous pressure filter, such as a rotary drum filter press. The surface of a rotary drum of the rotary drum filter press is provided with a filter tank, the filter tank is divided into different areas by a partition plate, and the different areas are divided into a feeding filter area, a washing area, a pre-drying area and a discharging area according to the process requirements. The rotary drum is externally provided with a shell, and a slurry inlet, a cleaning liquid inlet, a pre-drying gas inlet and a scraper are arranged on the shell at intervals. The partition plate is mounted on the surface of the drum, or on the inner surface of the housing facing the surface of the drum. The drum rotates for one circle to complete the processes of filtering, washing, pre-drying and discharging in sequence.
In one embodiment of the application, the slurry inlet is arranged at the lower part of the shell of the rotary drum, and the cleaning liquid inlet, the pre-drying gas inlet and the scraper are arranged on the shell at intervals in sequence from the slurry inlet in the anticlockwise direction. The surface of the rotary drum is provided with a clapboard which divides a filter tank on the surface of the rotary drum into a feeding filter area, a washing area, a pre-drying area and a discharging area. The drum rotates counterclockwise. And the polyphenyl ether slurry enters the rotary drum from the slurry inlet, is spread on the surface of the filter tank, forms polyphenyl ether filter cakes on the surface of the rotary drum through pressure filtration, and adds cleaning solution to perform spray washing after the filter cakes rotate to the cleaning solution inlet along with the rotary drum. And then blowing and drying by inert gas after the drum rotates to the position of the pre-drying gas inlet. When the filter cake is rotated to the position of the scraper, the filter cake falls off from the surface of the rotary drum under the action of gravity, and the filter cake which does not fall off is scraped off by the scraper. The slurry is continuously fed in and is matched with the rotary drum to continuously rotate, so that the continuous work of filtering, cleaning, pre-drying and discharging is realized.
Preferably, a pressure is provided in the drum housing, so that the filtration, washing and pre-drying are completed under the pressure of 120-1000kPa, preferably 200-600kPa, and the thickness of the filter cake is 10-250 mm.
For a rotary drum filter press, the preferred process conditions are: the pressure is 120-1000kpa, preferably 200-600 kpa; the washing amount of the cleaning liquid is 0.1 to 80Kg/Kg of filter cake, preferably 1 to 10Kg/Kg of filter cake; the consumption of the pre-drying purging inert gas is 0.01-50Nm 3 Perkg of filter cake, preferably 0.3 to 10Nm 3 Perkg of filter cake. The diameter of the rotary drum filter press can be 50-500cm, and the length of the filter tank arranged on the surface of the rotary drum can be 5-300 cm.
In one embodiment, the production system further comprises a drying device 500, wherein the drying device 500 is in communication with the dewatering device 400 such that the dewatered polymeric material is dried in the drying device 500. The drying device 500 is further provided with a nitrogen heating circulation system for supplying a drying medium for drying to the drying device. In one embodiment, the drying apparatus 500 is selected from one or more of a spiral-up drying bed, a fluidized drying bed, and a rake dryer. These drying devices may be each provided with a bag collector or the like for collecting the free acrylonitrile-acrylate-styrene-terpolymer resin. The collected acrylonitrile-acrylate-styrene-terpolymer resin is cooled to obtain the product acrylonitrile-acrylate-styrene-terpolymer resin which can be sent into a storage bin for temporary storage.
In one embodiment, the drying apparatus 500 is provided with a drying apparatus material input that communicates with the dewatering apparatus 400 such that the polymer material from the dewatering apparatus 400 is input into the drying apparatus 500 for drying. In one embodiment, the drying device 500 comprises a dryer inside which a screw drying shaft with blades is arranged, at a temperature of 50-250 ℃ and a flow rate of 1-20 tons/hour. The feed to the dryer was a screw conveyor to deliver the product wet powder to the dryer feed system inlet, and the dryer separated the polymer powder from the liquid by heating using a paddle screw drying shaft and jacket. The paddle of the screw shaft conveys the product to the lower part of the dryer, and the dried product is conveyed to the front part of the dryer through a rotary lock, the whole operation temperature is 45-250 ℃, and the feeding speed is 10-800L/min. And feeding the dried polymer powder into a storage bin. In one embodiment, the drying apparatus 500 is configured to have an average residence time of the polymer material therein of 5 to 50 minutes. In one embodiment, the drying apparatus 500 comprises a horizontal continuous non-rotating hub dryer with a material space of 5-25m 3 。
And the polymer dry powder conveying system conveys the polymer dry powder to a storage bin after cooling and temperature reduction from an outlet of the dryer. The product powder discharged from the dryer is sent to a bag filter by a powder cooler. The bag collector separates nitrogen gas and product powder, and nitrogen gas returns the air-blower, and the powder falls to the bottom, gets into little funnel through a rotatory lock valve. Product powder enters the product bin through a similar rotary lock valve through an air blast system.
The production process of acrylonitrile-acrylate-styrene-terpolymer resin using the production system comprises: emulsion polymerization is carried out in an emulsion polymerization reaction kettle, and then latex feed liquid is optionally treated by latex feed liquid filtering treatment equipment and then is introduced into a suspension polymerization reaction kettle for suspension polymerization. After the suspension polymerization has ended, a devolatilization treatment is carried out: the suspension polymerization product can be subjected to devolatilization treatment in a suspension polymerization reaction kettle, or can be introduced into a stripping tower for devolatilization treatment after being treated by suspension polymerization product slurry filtering treatment equipment; and (3) dehydrating the devolatilized polymerization product in a dehydrating device, and then introducing the dehydrated polymerization product into a drying device for drying treatment, so as to obtain a final acrylonitrile-acrylate-styrene-terpolymer resin product. The acrylonitrile-acrylate-styrene-terpolymer resin with the acrylate content of 10-50 wt% can be conveniently prepared by using the production system of the application. In one embodiment, the acrylonitrile-acrylate-styrene-terpolymer resin product produced using the production system of the present application has the following weight percent particle size distribution:
the average value of the proportion of the particles with more than 30 meshes is 16.20 percent, the standard deviation is 7.66 percent,
the average value of the ratio of the particles with 30-60 meshes is 56.45 percent, the standard deviation is 8.21 percent,
the average value of the proportion of 60-80 mesh particles is 17.59%, and the standard deviation is 6.3%.
In one embodiment, the acrylonitrile-acrylate-styrene-terpolymer resin product produced using the production system of the present application has the following weight percent particle size distribution: the average value of the ratio of the particles with 30-80 meshes is 90%, the standard deviation is 8%, and the content of the acrylic ester is 10-50 wt%.
In the description of the present application, it should be noted that the terms "upper", "lower", "inner", "outer", "front", "rear", "left", "right", and the like indicate orientations or positional relationships based on operational states of the present application, and are only used for convenience in describing and simplifying the present application, but do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present application.
In the description of the present application, it is to be noted that the terms "mounted," "connected," and "connected" are to be construed broadly unless otherwise explicitly stated or limited. The specific meaning of the above terms in the present application can be understood in a specific case by those of ordinary skill in the art.
The present application has been described above with reference to preferred embodiments, but these embodiments are merely exemplary and merely illustrative. On the basis of the above, the present application can be subjected to various substitutions and improvements, and the substitutions and the improvements are all within the protection scope of the present application.

Claims (18)

1. A production system of acrylonitrile-acrylate-styrene copolymer resin, characterized by comprising:
the device comprises an emulsion polymerization reaction kettle, wherein an emulsion polymerization raw material feeding hole for feeding emulsion polymerization raw materials is formed in the upper part of the emulsion polymerization reaction kettle; the lower part of the emulsion polymerization reaction kettle is provided with a latex feed liquid discharge port for discharging a product latex feed liquid;
the device comprises a suspension polymerization reaction kettle, a suspension polymerization reaction kettle and a polymerization reaction kettle, wherein the suspension polymerization reaction kettle is provided with a suspension polymerization raw material feeding hole for feeding a suspension polymerization raw material and a polymerization resin discharging hole for discharging a suspension polymerization product, and the suspension polymerization raw material feeding hole is communicated with a latex material liquid discharging hole of the emulsion polymerization reaction kettle in a fluid manner, so that the latex material liquid from the emulsion polymerization reaction kettle can enter the suspension polymerization reaction kettle;
a dewatering device configured such that the devolatilized treated suspension polymerization product slurry can be dewatered in the dewatering device;
a drying device, which is communicated with the dehydration device, so that the dehydrated polymer material is dried in the drying device;
the system comprises a suspension polymerization reaction kettle, a first circulation temperature control loop and a second circulation temperature control loop, wherein the suspension polymerization reaction kettle is also provided with a suspension polymerization reaction kettle jacket used for controlling the temperature in the suspension polymerization reaction kettle, the first circulation temperature control loop is communicated with the suspension polymerization reaction kettle jacket, a first temperature control device is arranged in the first circulation temperature control loop, and the first temperature control device is a heat exchanger and/or a steam-water mixer.
2. The production system according to claim 1, wherein the emulsion polymerization reactor is further provided with an emulsion polymerization reactor jacket for the emulsion polymerization reactor and a second circulation temperature control circuit in communication with the emulsion polymerization reactor jacket, and a second temperature control device is provided in the second circulation temperature control circuit, and the second temperature control device is a heat exchanger and/or a steam-water mixer.
3. The production system according to claim 1, wherein a baffle is provided in the emulsion polymerization reactor, and a ratio of a height of the baffle to a straight wall height of the emulsion polymerization reactor is 0.6 to 1.0: 1; the volume of the emulsion polymerization reaction kettle is 10-50m 3 The maximum working pressure is 140 kpa.
4. The production system according to claim 1, wherein the emulsion polymerization reaction vessel is provided with a stirrer, the stirrer is a pitched blade type stirrer with 1-3 layers of blades, the ratio of the diameter D of the tip of the blade to the diameter D of the inner wall of the emulsion polymerization reaction vessel is 0.2-0.6:1, and the stirring speed is 50-150 rpm.
5. The production system according to claim 1, wherein the emulsion polymerization reaction kettle is further provided with an oxygen-containing gas feeding device with a system for controlling the oxygen content above the liquid level, a nitrogen feeding device with a control system for adjusting the total pressure above the liquid level within the range of 0 to 140kpa, and a reduced-pressure vacuumizing device within the range of 0 to-60 kpa, and the reduced-pressure vacuumizing device comprises a part for condensing and recycling the volatile matters in the tail gas.
6. The production system of claim 1, further comprising:
the emulsion feed liquid filtering and treating equipment is configured to enable the emulsion feed liquid to be further treated by the emulsion feed liquid filtering and treating equipment before entering the suspension polymerization reaction kettle.
7. The production system according to claim 1, wherein a baffle is provided in the suspension polymerization reactor, and the ratio of the height of the baffle to the height of the straight wall of the suspension polymerization reactor is 0.6 to 1.0: 1, the ratio of the width of the baffle to the inner diameter of the kettle is 0.005-0.1: 1; the volume of the suspension polymerization reaction kettle is 20-80m 3 The working pressure is-60 kpa vacuum to 140kpa positive pressure.
8. The production system according to claim 1, wherein a stirrer is provided in the suspension polymerization reaction vessel, the stirrer is a pitched blade type stirrer having 1 to 3 layers of blades, the ratio of the diameter D of the tip of the blade to the diameter D of the inner wall of the emulsion polymerization reaction vessel is 0.2 to 0.6:1, and the stirring speed is 50 to 150 rpm.
9. The production system according to claim 1, wherein the suspension polymerization reaction kettle is further provided with a nitrogen adding device with a control system for adjusting the total pressure above the liquid surface within the range of 0-140kpa, and a reduced-pressure vacuum-pumping device within the range of 0-60 kpa, and the reduced-pressure vacuum-pumping device comprises a volatile component condensation recycling part in the tail gas.
10. The production system according to claim 1, further comprising a third filtration treatment apparatus for filtration treatment of the devolatilized treated slurry of suspended polymerization product, which is disposed upstream of the dewatering device.
11. The production system according to claim 1, wherein the dewatering device is selected from one or more of a continuous centrifuge, a continuous pressure filter;
the operating conditions of the continuous centrifuge apparatus include: the temperature is 40-60 ℃, the pressure is 3-5kpa, and the rotating speed is 1000-;
the operating conditions of the continuous pressure filter comprise: the pressure is 120-1000kpa, and the thickness of the filter cake is 10-250 mm.
12. The production system of claim 1, wherein the drying means is selected from one or more of a spiral-up drying bed, a fluidized drying bed, and a rake dryer.
13. The production system according to claim 1, wherein the drying device is operated at an operating temperature of 50-150 ℃ and is equipped with a nitrogen circulation system.
14. The production system of claim 1, further comprising:
a devolatilizer disposed between the suspension polymerization reactor and the dehydration unit, wherein the devolatilizer is provided with a feed port for feeding the suspension polymerization product and a discharge port for discharging the devolatilized suspension polymerization product, the feed port of the devolatilizer is communicated with the discharge port of the polymerization resin of the suspension polymerization reactor so that the suspension polymerization product discharged through the discharge port of the polymerization resin of the suspension polymerization reactor can be stripped in the devolatilizer, and a vapor phase outlet of the devolatilizer is connected with a volatile vapor condensation recovery unit.
15. The production system of claim 14, further comprising:
a suspension polymerization product slurry filtration treatment apparatus configured such that the suspension polymerization product also passes through the suspension polymerization product slurry filtration treatment apparatus prior to entering the devolatilizer.
16. The production system of claim 14, wherein the devolatilization apparatus is a stripper;
volatile matter vapour condensation recovery unit includes:
a condenser configured to communicate with a stripped material outlet of the stripper column such that stripped material exiting the stripper column is cooled in the condenser;
the condenser is provided with a condensed liquid phase outlet which is communicated with the suspension polymerization reaction kettle, so that a condensed liquid phase flow discharged from the condensed liquid phase outlet circulates back to the suspension polymerization reaction kettle.
17. The production system according to claim 14, characterized in that the devolatilization device operates under the following conditions: the vacuum degree is between-5 kpa and-60 kpa, and the temperature is between 50 and 80 ℃.
18. The production system according to claim 14, wherein the devolatilization device is a plate stripper having a diameter/height ratio of 0.01 to 0.3; or the stirred tank is provided with a decompression vacuumizing device, wherein the stirred tank is provided with a jacket for controlling the temperature in the tank and a third circulating temperature control loop communicated with the jacket of the stirred tank, the third circulating temperature control loop is provided with a third temperature control device, and the third temperature control device is a heat exchanger and/or a steam-water mixer.
CN202220295440.4U 2022-02-14 2022-02-14 Production system of acrylonitrile-acrylic ester-styrene copolymer resin Active CN217392374U (en)

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