CN217257511U

CN217257511U - Equipment for producing high-gloss polystyrene

Info

Publication number: CN217257511U
Application number: CN202221153998.5U
Authority: CN
Inventors: 金丰富; 易健丰; 滕庆; 张国柱; 曹志仁; 杨蜀黔; 朱晓东
Original assignee: Lianyungang Petrochemical Co Ltd
Current assignee: Lianyungang Petrochemical Co Ltd
Priority date: 2022-05-14
Filing date: 2022-05-14
Publication date: 2022-08-23
Anticipated expiration: 2032-05-14

Abstract

The utility model discloses a produce equipment of high gloss polystyrene, belong to polystyrene production facility technical field, including conveyer and bale splitter, be equipped with the agitator in the sol jar, the sol jar is linked together through pipeline and glue solution filter, the glue solution filter is linked together through pipeline and storage tank, the storage tank is linked together through pipeline and filter, the filter is linked together through pipeline and feeding pre-heater, first devolatilization ware is linked together through pipeline and second devolatilization ware, the second devolatilization ware is linked together through pipeline and eager grain equipment, the devolatilization ware is linked together through pipeline and vacuum unit, vacuum unit is linked together through pipeline and circulation fluid reservoir, the circulation fluid reservoir is linked together through pipeline and feeding pre-heater, first prepolymerization cauldron, second prepolymerization cauldron is linked together through pipeline and vacuum unit. Solves the problem that the prior equipment can not produce high-gloss polystyrene and is mainly applied to the production of the high-gloss polystyrene.

Description

Equipment for producing high-gloss polystyrene

Technical Field

The utility model belongs to the technical field of polystyrene production facility, concretely relates to produce high gloss polystyrene equipment.

Background

With the improvement of living standard of people, high-gloss household electrical appliance products are more and more popular, and especially in the fields of flat-panel televisions, telephones, refrigerators, computers and the like, high-gloss shells become mainstream products in the market. The HIPS highlight product has outstanding gloss performance, the impact strength can meet the product performance requirement, and the HIPS highlight product can be widely used for replacing highlight ABS products and used for shells of household appliances such as air conditioners, washing machines, refrigerators and the like.

Although HIPS has higher impact strength, the addition of rubber results in a reduction in the gloss of the product. In the conventional HIPS resin, the particle size of rubber particles is generally 3-4 μm, and the size of the rubber particle size is a main factor for determining the glossiness of the material. Therefore, HIPS with high gloss can be obtained by adjusting the particle size of rubber to influence the light reflectivity, and a device capable of producing high-gloss polystyrene is needed to replace the existing device.

SUMMERY OF THE UTILITY MODEL

To prior art's defect, the utility model aims to provide a produce high gloss polystyrene equipment, utilize this device to produce gloss (60 degrees angles) and reach 80% ~ 90% high gloss HIPS, the utility model discloses the technical scheme who adopts as follows:

the utility model provides a produce high gloss polystyrene equipment, includes conveyer and bale splitter, conveyer and bale splitter are supporting mutually, the bale splitter be linked together through elephant trunk and sol jar, sol jar in be equipped with the agitator, auxiliary agent A is an indispensable auxiliary agent in high gloss HIPS production, scheme before this is added by the prepolymerization cauldron, nevertheless because of the effective volume of prepolymerization cauldron is little, the dwell time of material in the cauldron is short, leads to auxiliary agent A and styrene rubber solution can not abundant misce bene, leads to the HIPS gloss unstability of producing, in view of above-mentioned shortcoming the utility model discloses adjust auxiliary agent A's the position of adding to from the rubber dissolving tank by the prepolymerization cauldron and add. Adding the novel auxiliary agent into a rubber dissolving tank according to the proportion of 0.5-0.6%, and fully and uniformly mixing the auxiliary agent and the rubber solution under the stirring action of the rubber dissolving tank. The rubber dissolving tank is communicated with the first conveying pump, the first conveying pump is communicated with the filter, the filter is communicated with the storage tank through a pipeline, the storage tank is communicated with the second conveying pump through a pipeline, the second conveying pump is communicated with the feeding preheater through a pipeline, the feeding preheater is communicated with the first pre-polymerization kettle through a pipeline, the first pre-polymerization kettle is communicated with the second pre-polymerization kettle through a pipeline, and a third conveying pump is arranged on the pipeline communicated with the first pre-polymerization kettle. And (3) increasing the maximum rotating speed of the stirrer of the first prepolymerization kettle, enabling the mixed solution to enter the first prepolymerization kettle, adding an initiator, and enabling the peroxide initiator and the mixed solution to be uniformly mixed in the first prepolymerization kettle under a shearing force field. Pre-polymerizing styrene monomer in a first pre-polymerizing reactor in a shearing force field, and controlling the reaction temperature of the pre-polymerizing reactor at 110-115 deg.c to obtain pre-polymerized liquid system containing polystyrene and without phase transition; the reaction residence time is 0.6-1 h; the conversion rate is 15-20%. The design of a second prepolymerization reactor is improved while a second prepolymerization reactor is additionally arranged, and the lowest layer of stirring blades is changed into an anchor type from a paddle type, so that the maximum rotating speed of the stirrer is increased. The prepolymerization liquid system generated by the first prepolymerization kettle further generates polymerization reaction of styrene monomers in the second prepolymerization kettle under a shearing force field, the reaction temperature of the prepolymerization kettle is controlled to be 118-125 ℃, the reaction residence time is 1.5-2 h, and the total conversion rate of the styrene monomers is controlled to be 25-30% until phase separation occurs, so that the rubber area particle size of 0.45-0.75 mu m and the rubber volume particle size of 0.85-1 mu m are obtained. Second prepolymerization cauldron be linked together through pipeline and plug flow reactor group, the continuous pipeline on be equipped with delivery pump four, plug flow reactor group include four plug flow reactors, plug flow reactor on all install agitating unit, every plug flow reactor between be linked together through the pipeline, last plug flow is linked together through the pipeline with polymer preheater, polymer preheater be linked together through pipeline and first devolatilizer, first devolatilizer be linked together through pipeline and second devolatilizer, continuous pipeline on be equipped with delivery pump five in proper order, second devolatilizer be linked together through pipeline and grain cutting equipment, continuous pipeline on be equipped with delivery pump six. The devolatilization preheater is a high-efficiency heat exchanger with an inner plug-in, the requirement of rapid heating can still be met at the production load of 110 percent, the temperature control adopts a control mode of cascade connection of hot oil and outlet material temperature, the opening degree of a hot oil regulating valve of the devolatilization preheater is automatically adjusted through the outlet material temperature of the devolatilization preheater, and the devolatilization preheater is provided with an independent high-temperature oil delivery pump and is not influenced by other working conditions of a devolatilization section. The first prepolymerization kettle and the second prepolymerization kettle are communicated with a vacuum unit through pipelines, and the first devolatilization device and the second devolatilization device are respectively communicated with the vacuum unit through pipelines.

The utility model has the advantages that:

the utility model discloses production flow is simple, novel in design, break away from traditional polymerization facility to the restriction of high gloss HIPS production method, has not only practiced thrift the one-time investment of production line construction, has also developed the latent energy of current device simultaneously, has accomplished a special multipotency. Through the utility model discloses a institutional advancement can produce the HIPS of high gloss, and it is more convenient that whole flow operation gets up, uses comparatively extensively, and the practicality is strong. Have higher feasibility, through the utility model discloses a glossiness (60 degrees angle) that equipment produced reaches 80% ~ 90% according to national standard plastics mirror surface gloss test method survey, and the impact strength who surveys according to national standard plastics cantilever beam arm impact strength's determination standard reaches 9 ~ 11kJ/m 2. The high gloss HIPS product meets the requirements of users of downstream industries such as air conditioners, washing machines, refrigerators and other household appliance shells. And thereby pass through the utility model discloses output high gloss HIPS product can improve whole economic benefits, is suitable for comprehensive popularization and application.

Drawings

FIG. 1 is a schematic diagram of an apparatus for producing high-gloss polystyrene according to the present invention;

FIG. 2 is a schematic diagram of the operation of the apparatus for producing high-gloss polystyrene according to the present invention.

Detailed Description

Example 1

As shown in fig. 1-2:

the utility model provides a produce high gloss polystyrene equipment, includes conveyer 1 and bale splitter 2, conveyer 1 and bale splitter 2 are supporting mutually, bale splitter 2 be linked together through elephant trunk and sol jar 5, sol jar 5 in be equipped with agitator 5-1, sol jar 5 and delivery pump 18 be linked together through the pipeline, delivery pump 18 be linked together through pipeline and filter 19, filter 19 be linked together through pipeline and storage tank 6, storage tank 6 be linked together through pipeline and delivery pump two 20, delivery pump two 20 be linked together through pipeline and feeding 7, feeding preheater 7 be linked together through pipeline and first pre-polymerization cauldron 8, first pre-polymerization cauldron 8 be linked together through pipeline and second pre-polymerization cauldron 9, the pipeline that links to each other on be equipped with delivery pump three 21, second pre-polymerization cauldron 9 be linked together through pipeline and plug flow reactor group, the continuous pipeline is provided with a conveying pump IV 22, the plug flow reactor group comprises four plug flow reactors 10, the plug flow reactors 10 are provided with stirring devices 10-1, each plug flow reactor 10 is connected in series through a pipeline to form a plug flow reactor group, the fourth plug flow reactor is communicated with a polymer preheater 11 through a pipeline, the polymer preheater 11 is communicated with a first devolatilizer 12 through a pipeline, the first devolatilizer 12 is communicated with a second devolatilizer 13 through a pipeline, the continuous pipeline is provided with a conveying pump V27, the second devolatilizer 13 is communicated with a granulating device through a pipeline, the continuous pipeline is provided with a conveying pump VI 28, the first additive feeding tank 14 is communicated with the first prepolymerization reactor 8 through a pipeline, the first additive feeding tank 14 is communicated with the second prepolymerization reactor 9 through a pipeline, a communicating pipeline is provided with a delivery pump eight 23, an auxiliary agent feeding tank two 15 is communicated with the first prepolymerization reactor 8 through a pipeline, the auxiliary agent feeding tank two 15 is communicated with the second prepolymerization reactor 9 through a pipeline, a communicating pipeline is provided with a delivery pump nine 24, an auxiliary agent feeding tank three 16 is communicated with the first prepolymerization reactor 8 through a pipeline, an auxiliary agent feeding tank three 16 is communicated with the second prepolymerization reactor 9 through a pipeline, the communicating pipeline is provided with a delivery pump ten 25, an auxiliary agent feeding tank four 17 is communicated with a penultimate plug flow reactor 10 through a pipeline, the communicating pipeline is provided with a delivery pump eleven 26, the first devolatilizer 12 and the second devolatilizer 13 are respectively communicated with a vacuum unit 3 through pipelines, the vacuum unit 3 is communicated with a circulating liquid tank 4 through a pipeline, the circulating liquid tank 4 is communicated with a feeding preheater 7 through a pipeline, the communicating pipeline is provided with a delivery pump seven 29, the first prepolymerization reactor 8 and the second prepolymerization reactor 9 are respectively communicated with the vacuum unit 3 through pipelines.

The working principle of the utility model is as follows:

cutting a colloidal sol unit: polybutadiene rubber is conveyed into a rubber cutting machine 2 through a conveying belt of a conveyor 1, rubber blocks are cut into rubber particles in the rubber cutting machine 2, the rubber particles fall into a rubber dissolving tank 5 which is provided with a nitrogen seal and filled with styrene through a chute, a stirrer 5-1 is arranged in the rubber dissolving tank 5, the rubber particles are dissolved into the styrene after being stirred for a certain time to form a styrene-rubber co-solution, meanwhile, 0.5-0.6% of an auxiliary agent A is added into the styrene-rubber and fully and uniformly mixed under the action of the stirrer 5-1, and after the styrene-rubber and the auxiliary agent A solution are completely dissolved, the styrene-rubber and the auxiliary agent A solution are conveyed into a material storage tank 6 through a first conveying pump 18 and a filter 19 to be stored for later use.

First prepolymerization vessel: and mixing the glue solution from the second glue solution delivery pump 20 with circulating liquid, preheating the mixture to a set temperature through a feeding preheater 7, and then feeding the mixture into a first prepolymerization reactor 8 for prepolymerization, wherein an antioxidant, an initiator, white oil and other auxiliary agents required by the formula are also required to be added into the first prepolymerization reactor 8. The temperature of the first prepolymerization reactor 8 is controlled between 110 ℃ and 115 ℃ and the pressure is controlled at 610mmHgA during the prepolymerization process. The temperature of the prepolymerization is controlled by adjusting the temperature of the rubber solution feed preheater, controlling the pressure in the first prepolymerization vessel 8 and controlling the temperature of the jacket hot oil of the first prepolymerization vessel 8, and various additives are added to the first prepolymerization vessel 8 at this stage.

Second prepolymerization vessel: the pre-polymerized material is sent into the second pre-polymerization kettle 9 by a third delivery pump 21, the pre-polymerization temperature of the second pre-polymerization kettle 9 is raised to 125-135 ℃, and then graft polymerization is carried out again, and the temperature of the reaction kettle is controlled between 125-135 ℃ and the pressure is controlled at 460mmHgA in the polymerization process. The temperature of the polymerization reaction is controlled by adjusting the pressure of the second prepolymerization reactor 9, and the prepolymerization reactor is controlled at a specific liquid level to control the retention time, and various additives are added into the second prepolymerization reactor 9 at this stage.

Polymerization unit: the styrene reaction material after prepolymerization is sent to a back 4 series vertical plug flow reactor groups by a four 22 delivery pump, and the reaction temperature of the plug flow reactor is controlled to be 130 ℃, 145 ℃, 155 ℃ and 165 ℃ in sequence. Each plug flow reactor 10 is provided with a stirring device 10-1 with matched power, so that the materials in the reactor are uniformly stirred and heat dissipation is facilitated. Each plug flow reactor is provided with a temperature control system. Zinc stearate is added as a release agent to the penultimate plug flow reactor at this stage.

A devolatilization unit: the melt from the polymerization reaction enters a polymer preheater 11 to heat the polymer from 165 ℃ to 225-240 ℃, the polymer is sent to a first devolatilizer 12 through a distributor, and most of the unreacted monomers, the diluent ethylbenzene and other low volatiles are removed under high vacuum to obtain the HIPS polymer. The PS polymer devolatilized by the first devolatilizer 12 still contains 0.5 to 1 percent of residual monomers, and then is conveyed to the second devolatilizer 13 by a fifth conveying pump 27 through a distributor, and secondary devolatilization is carried out under the conditions of high temperature and high vacuum so as to reduce the residual styrene monomers in the PS melt to 300ppm or less.

And a pelletizing unit, wherein the polymer material in the second devolatilizer 13 is conveyed to the pelletizing unit through a conveying pump six 28 for pelletizing. The glossiness (60-degree angle) of the high-gloss polystyrene material produced by the device reaches 80-90% according to the national standard plastic mirror surface gloss test method, and the impact strength measured according to the national standard plastic cantilever beam arm impact strength test standard reaches 9-11 kJ/m 2.

The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of modifications can be made without departing from the principle of the present invention, and these modifications should also be regarded as the protection scope of the present invention.

Claims

1. The utility model provides a produce high gloss degree polystyrene equipment, includes conveyer (1) and bale splitter (2), conveyer (1) and bale splitter (2) are supporting mutually, its characterized in that, bale splitter (2) be linked together through elephant trunk and sol jar (5), sol jar (5) in be equipped with agitator (5-1), sol jar (5) be linked together through the pipeline with delivery pump (18), delivery pump (18) be linked together through pipeline and filter (19), filter (19) be linked together through pipeline and storage tank (6), storage tank (6) be linked together through pipeline and delivery pump two (20), delivery pump two (20) be linked together through pipeline and feeding preheater (7), feeding preheater (7) be linked together through pipeline and first prepolymerization cauldron (8), first prepolymerization cauldron (8) be linked together through pipeline and second prepolymerization cauldron (9), the pipeline that links to each other on be equipped with delivery pump three (21), second prepolymerization cauldron (9) be linked together through pipeline and plug flow reactor group, the pipeline that links to each other on be equipped with delivery pump four (22), plug flow reactor group include four plug flow reactors (10), plug flow reactor (10) on all install agitating unit (10-1), every plug flow reactor (10) between establish ties into plug flow reactor group through the pipeline, fourth plug flow reactor is linked together through pipeline and polymer preheater (11), polymer preheater (11) be linked together through pipeline and first devolatilizer (12), first devolatilizer (12) be linked together through pipeline and second devolatilizer (13), the continuous pipeline is provided with a conveying pump V (27), the second devolatilizer (13) is communicated with the granulating device through a pipeline, the continuous pipeline is provided with a conveying pump VI (28), the first additive feeding tank (14) is communicated with the first prepolymerization kettle (8) through a pipeline, the first additive feeding tank (14) is communicated with the second prepolymerization kettle (9) through a pipeline, the communicating pipeline is provided with a conveying pump V (23), the second additive feeding tank (15) is communicated with the first prepolymerization kettle (8) through a pipeline, the second additive feeding tank (15) is communicated with the second prepolymerization kettle (9) through a pipeline, the communicating pipeline is provided with a conveying pump V (24), the third additive feeding tank (16) is communicated with the first prepolymerization kettle (8) through a pipeline, the third additive feeding tank (16) is communicated with the second prepolymerization kettle (9) through a pipeline, the communicating pipeline is provided with a conveying pump V (25), and the additive feeding tank IV (17) is communicated with the penultimate plug flow reactor (10) through a pipeline, and the communicated pipeline is provided with an eleventh delivery pump (26).

2. The apparatus for producing high-gloss polystyrene as claimed in claim 1, wherein: the first devolatilization device (12) and the second devolatilization device (13) are respectively communicated with a vacuum unit (3) through pipelines, the vacuum unit (3) is communicated with a circulating liquid tank (4) through a pipeline, the circulating liquid tank (4) is communicated with a feeding preheater (7) through a pipeline, and a conveying pump seven (29) is arranged on the communicated pipeline.

3. The apparatus for producing high-gloss polystyrene according to claim 1, wherein: the first prepolymerization kettle (8) and the second prepolymerization kettle (9) are respectively communicated with the vacuum unit (3) through pipelines.