NL2032626B1 - Device for producing flame-retardant expandable polystyrene by bulk polymerization - Google Patents

Device for producing flame-retardant expandable polystyrene by bulk polymerization Download PDF

Info

Publication number
NL2032626B1
NL2032626B1 NL2032626A NL2032626A NL2032626B1 NL 2032626 B1 NL2032626 B1 NL 2032626B1 NL 2032626 A NL2032626 A NL 2032626A NL 2032626 A NL2032626 A NL 2032626A NL 2032626 B1 NL2032626 B1 NL 2032626B1
Authority
NL
Netherlands
Prior art keywords
polymerization reactor
materials
retardant
pump
polymerization
Prior art date
Application number
NL2032626A
Other languages
Dutch (nl)
Inventor
Zhou Zhide
Su Zhongmin
Zhou Xinchun
Li Guiyin
Liu Huizhi
Original Assignee
Univ Guangdong Petrochem Tech
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Univ Guangdong Petrochem Tech filed Critical Univ Guangdong Petrochem Tech
Application granted granted Critical
Publication of NL2032626B1 publication Critical patent/NL2032626B1/en

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/1862—Stationary reactors having moving elements inside placed in series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
    • B01F27/91—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with propellers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
    • B01F33/80—Mixing plants; Combinations of mixers
    • B01F33/81—Combinations of similar mixers, e.g. with rotary stirring devices in two or more receptacles
    • B01F33/811—Combinations of similar mixers, e.g. with rotary stirring devices in two or more receptacles in two or more consecutive, i.e. successive, mixing receptacles or being consecutively arranged
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
    • B01F33/80—Mixing plants; Combinations of mixers
    • B01F33/836—Mixing plants; Combinations of mixers combining mixing with other treatments
    • B01F33/8362—Mixing plants; Combinations of mixers combining mixing with other treatments with chemical reactions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C44/00—Shaping by internal pressure generated in the material, e.g. swelling or foaming ; Producing porous or cellular expanded plastics articles
    • B29C44/34—Auxiliary operations
    • B29C44/3461—Making or treating expandable particles
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J9/00—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof
    • C08J9/04—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof using blowing gases generated by a previously added blowing agent
    • C08J9/12—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof using blowing gases generated by a previously added blowing agent by a physical blowing agent
    • C08J9/14—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof using blowing gases generated by a previously added blowing agent by a physical blowing agent organic
    • C08J9/141—Hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J9/00—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof
    • C08J9/16—Making expandable particles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F2101/00—Mixing characterised by the nature of the mixed materials or by the application field
    • B01F2101/2805—Mixing plastics, polymer material ingredients, monomers or oligomers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C44/00—Shaping by internal pressure generated in the material, e.g. swelling or foaming ; Producing porous or cellular expanded plastics articles
    • B29C44/34—Auxiliary operations
    • B29C44/3442—Mixing, kneading or conveying the foamable material
    • B29C44/3446—Feeding the blowing agent
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
    • B29K2025/00—Use of polymers of vinyl-aromatic compounds or derivatives thereof as moulding material
    • B29K2025/04—Polymers of styrene
    • B29K2025/06—PS, i.e. polystyrene
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2203/00—Foams characterized by the expanding agent
    • C08J2203/14—Saturated hydrocarbons, e.g. butane; Unspecified hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2325/00—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by an aromatic carbocyclic ring; Derivatives of such polymers
    • C08J2325/02—Homopolymers or copolymers of hydrocarbons
    • C08J2325/04—Homopolymers or copolymers of styrene
    • C08J2325/06—Polystyrene
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Abstract

Disclosed is a device for producing flame-retardant expandable polystyrene (EPS) by bulk 5 polymerization includes 2 polymerization reactors connected in series, wherein the polymerization reactors are connected with a heating devolatilizer via a discharging pump; a condenser and a vacuum collecting tank are connected at the upper end of the heating devolatilizer; a dynamic mixer, a melt heat exchanger, a pump and a high-pressure underwater pelletizing system are connected successively with the heating devolatilizer at the bottom via a pump. 92.0 kg of styrene, 10 5.0 kg of ethylbenzene, 1.0 kg of white oil, 0.5 kg of tributyl phosphate, 1.0 kg of low molecular weight polyethylene, 6.0 kg of pentane, and 0.9 kg of octabromodiphenyl ether (flame retardant) are preferred for the device. The obtained flame-retardant EPS has good impact resistance and tensile strength, with a particle diameter strictly controlled between 0.7 mm and 1.0 mm.

Description

DEVICE FOR PRODUCING FLAME-RETARDANT EXPANDABLE POLYSTYRENE BY BULK
POLYMERIZATION
TECHNICAL FIELD
The present invention relates to the technical field of expandable polystyrene resin, and in particular to a device for producing flame-retardant expandable polystyrene.
BACKGROUND
In the prior art, expandable polystyrene (EPS) is produced using styrene as the main raw material through a suspension batch polymerization process, including the following main steps: dispersing liquid styrene monomer in an aqueous medium by using a suspension dispersant, adding an initiator to initiate a polymerization reaction, and adding a foaming agent to complete the polymerization reaction when the conversion rate falls within a certain range; conducting washing, drying and sieving. CN105294041A discloses a homogeneous modified fireproof insulation board, wherein the diameter of beads obtained by this suspension technology varies widely from 0.1 mm to 4 mm; the incorporation of a nucleating agent and/or a flame retardant into beads is difficult, and may inhibit the polymerization reaction; the polymerization reaction is conducted in an aqueous medium, and a suspension dispersant requires to be added, resulting in a large amount of sewage and environmental protection problems; the product quality stability is poor.
SUMMARY
In order to solve the above-mentioned technical problem, the present invention provides a device and method for producing flame-retardant EPS by bulk polymerization, so that the product obtained with a particle diameter of 0.7-1.0 mm, achieves the same flame-retarding effect as products prepared based on a suspension method when 0.9% of octabromodiphenyl ether (flame retardant) is used.
The present invention solves this technical problem through the following technical solution:
The present invention adopts a bulk polymerization process to produce flame-retardant
EPS, and the device used includes a polymerization reactor 1 and a polymerization reactor 2, wherein the polymerization reactor 1 and the polymerization reactor 2 are connected in series via a discharging pump; material inlets are arranged at upper heads of the polymerization reactors respectively, reaction stirrers are arranged in the middle parts of the upper heads respectively, and the upper heads are communicated with condensers respectively; the reaction stirrers are variable-frequency stirrers with rotational speeds adjusted depending on the viscosity of the materials; the lower end of the polymerization reactor 2 is connected with a heating devolatilizer via a discharging pump; a condenser is connected at the upper end of the heating devolatilizer, and the condenser is connected with a vacuum collecting tank; the bottom of the heating devolatilizer is connected with a dynamic mixer via a pump, and the dynamic mixer is connected with a melt heat exchanger; the melt heat exchanger is connected with a high-pressure underwater pelletizing system via a pump; a hole diameter of high-temperature die heads in the high-pressure underwater pelletizing system is 0.8 mm.
A connector for adding a molten flame retardant masterbatch is installed at the front end of the dynamic mixer; a material backflow preventer is arranged at the connector to prevent the materials from flowing back; the flame retardant masterbatch is melted by a screw extruder and injected into the mixer for mixing with a polystyrene foaming agent, so that a flame retardant is embedded in a molecular chain of polystyrene.
When the device is used to produce flame-retardant EPS, styrene, a solvent and an additive are added into the polymerization reactor 1 in proportion, the temperature of the materials in the polymerization reactor 1 is controlled at 120-150°C, the stirring speed is controlled at 40-80 rpm, and cooling is started for refluxing; the materials are polymerized in the polymerization reactor 1 for 1.5-2 h; then, the materials are delivered to the polymerization reactor 2 by the discharging pump, the temperature of the material in the polymerization reactor 2 is controlled at 180-180°C, cooling is started for refluxing, the stirring speed is controlled at 15-20 rpm, and the polymerization reaction is continued for 1.5-2 h. When a styrene conversion rate in the polymerization reactor 2 reaches 60-70%, the materials in the polymerization reactor 2 are delivered to the top of the heating devolatilizer via the discharging pump, the temperature of the heating devolatilizer is controlled at 220-250°C, the vacuum is controlled at -0.098 MPa, and flash evaporation is conducted; vapor containing the unreacted styrene, solvent and other light components is removed and delivered into the condenser for cooling and refluxing, and the condensate flows into the vacuum collecting tank and is recycled into the polymerization reactor 1 for polymerization reaction. A first fluid of polystyrene obtained through flash evaporation is delivered into the mixer via the pump; meanwhile, a second fluid of foaming agent and flame retardant is also delivered into the mixer via the connector; the two fluids are mixed uniformly and delivered into the melt heat exchanger, and the temperature of the material in the melt heat exchanger is controlled at 180-205°C; next, the materials are delivered into the high-pressure underwater pelletizing system via the pump, and flame-retardant EPS particles are obtained through pelletizing and drying.
The polymerization reaction time is a bottleneck for producing flame-retardant EPS by the bulk polymerization process. Therefore, the polymerization reactor 1 and the polymerization reactor 2 are connected in series, which can nearly double the overall capacity without adding other devices.
The materials delivered into the polymerization reactor 1 include the following components: 80-95 kg of styrene, 2-10 kg of solvent and 0.5-5 kg of additive. The materials delivered into the mixer also include: 3-8 kg of foaming agent; 0.5-4 kg of flame retardant.
Preferably, the styrene is 89-93 kg, and the ethylbenzene (solvent) is 5.0 kg; the additive contains one or more of white oil, tributyl phosphate, calcium stearate, MgO, and low molecular weight polyethylene (nucleating agent), amounting to 2.0-4.0 kg; the pentane (foaming agent) is 5.0-7.0 kg; the flame retardant contains one or more of brominated polystyrene, octabromo series flame retardant and tetrabromo series flame retardant, amounting to 0.7-1.0 kg.
Further preferably, 92.0 kg of styrene, 5.0 kg of ethylbenzene, 1.0 kg of white oil, 0.5 kg of tributyl phosphate, 1.0 kg of low molecular weight polyethylene, 6.0 kg of pentane, and 0.9 kg of octabromodiphenyl ether (flame retardant) are used. The obtained flame-retardant EPS has good impact resistance and tensile strength, with a particle diameter strictly controlled between 0.7 mm and 1.0 mm. Compared with ordinary EPS particle products, the product of the present invention merely requires 0.9% of octabromodiphenyl ether to satisfy national standard levels for flame retardance.
The present invention has the following features and advantages: 1. The device for producing flame-retardant EPS by bulk polymerization of the present invention enables the continuous production of flame-retardant EPS by bulk polymerization owing to mutual support and synergy of various components as well as operation methods and steps. Especially, the polymerization reactor 1 and the polymerization reactor 2 are connected in series, which can nearly double the capacity of the entire production line; a foundation is laid for the continuous production; the styrene conversion rate is controlled at 80-70% for discharging, mainly because the further increase in the styrene conversion rate is very slow and easily results in by-products, which is disadvantageous to product quality and production efficiency, the temperature and vacuum are controlled in the heating devolatilizer, which is advantageous to flash evaporation; vapor removed through flash evaporation enters the condenser for refluxing and recycling; the foaming agent and the flame retardant are mixed with polystyrene in the mixer, and the mixture is cooled by the melt heat exchanger, which facilitates quality stability; the flame-retardant EPS is obtained through cooling, pelletizing and drying in the high-pressure underwater pelletizing system, with a particle diameter strictly controlled between 0.7 mm and 1.0 mm, and merely requires 0.9% of octabromodiphenyl ether (flame retardant) to satisfy national standard levels for flame retardance, with favourable foaming performance, excellent appearance, and good flame retardance, impact resistance and tensile strength. 2. The continuous production of graphite-type EPS by the bulk polymerization requires no aqueous medium in the reaction process, generates less wastewater, and has good environmental protection effect.
BRIEF DESCRIPTION OF THE DRAWINGS
FIG. 1 is a schematic diagram of a device for producing flame-retardant EPS by bulk polymerization.
DETAILED DESCRIPTION OF THE EMBODIMENTS
The implementation of the technical solution of the present invention will be described below through specific embodiments.
FIG. 1 is a schematic diagram of a device for producing flame-retardant EPS by bulk polymerization of the present patent. In this specific embodiment, the device includes the following arrangements: a polymerization reactor (1-1) is connected in series with a polymerization reactor (1-2) via a discharging pump (4-1), material inlets are arranged at upper heads of the polymerization reactors (1-1) and (1-2) respectively, variable-frequency reaction stirrers (2-1) and (2-2) with adjustable rotational speeds are arranged in the middle parts of the upper heads respectively, and the upper heads are communicated with condensers (3-1) and (3-2) respectively; the lower end of the polymerization reactor (1-2) is connected with a heating devolatilizer (5) via a discharging pump (4-2), a condenser (7) is connected at the upper end of the heating devolatilizer (5), and the condenser (7) is connected with a vacuum collecting tank (8); the bottom of the heating devolatilizer (5) is connected with a dynamic mixer (9) via a pump (6), and the dynamic mixer (9) is connected with a melt heat exchanger (10); a flame retardant masterbatch connector (9-1) is arranged at the front end of the dynamic mixer (9), and a material backflow preventer is arranged at the connector (8-1); the melt heat exchanger (10) is connected with a high-pressure underwater pelletizing system (12) via a pump (11), and a hole diameter of high-temperature die heads in the high-pressure underwater pelletizing system (12) is 0.8 mm.
The following components are applied in the embodiment of the present invention: 92.0 kg of styrene, 5.0 kg of ethylbenzene, 1.0 kg of white oil, 0.5 kg of tributyl phosphate, 1.0 kg of low molecular weight polyethylene (nucleating agent), 6.0 kg of pentane (foaming agent), and 0.9 kg of octabromodiphenyl ether (flame retardant).
A method for producing flame-retardant EPS with the device includes the following steps:
First, a nucleating agent is prepared into a 10.0% solution by using styrene; styrene, an ethylbenzene solvent, white oil, tributyl phosphate and the nucleating agent are respectively measured with a flow meter and continuously delivered into the polymerization reactor (1-1), the temperature of the materials in the polymerization reactor (1-1) is controlled at 148°C, the rotational speed of the stirrer (2-1) is controlled at 40 rpm, and a polymerization reaction is conducted for 1.5 h; the condenser (3-1) is turned on, and vapor is cooled to flow into the polymerization reactor (1-1).
Then, the materials are delivered into the polymerization reactor (1-2) via the discharging pump (4-1), the temperature of the material is controlled at 168°C, the rotational speed of the stirrer (2-2) is controlled at 15 rpm, the condenser (3-2) is turned on, and vapor is cooled to flow back into the polymerization reactor (1-2); the polymerization reaction is continued for 1.5 h; the styrene conversion rate is 70.0% at this moment, the materials are delivered from the polymerization reactor (1-2) to the top of the heating devolatilizer (5) via the discharge pump (4-
2), the temperature of the heating devolatilizer (5) is controlled at 240°C, flash evaporation is completed within 1 min, the unreacted styrene, solvent and other light components are removed into the condenser (7) for cooling, the vacuum is controlled at -0.098 MPa, and the condensate flows into the vacuum collecting tank (8); the condensate is recycled into the polymerization 5 reactors (1) for the polymerization reaction, which can reduce monomer residues in EPS particles, lower costs and satisfy food-grade requirements.
A first fluid of polystyrene obtained through flash evaporation is delivered into the dynamic mixer (9) via the pump (8); meanwhile, a second fluid of pentane (foaming agent) and octabromodiphenyl ether is accurately measured and delivered into the dynamic mixer (9) via the connector (9-1), and the two fluids are uniformly mixed through high-speed shearing in the dynamic mixer (9).
The two fluids are mixed uniformly, and the temperature of the uniform mixture is decreased to 185°C by the melt heat exchanger (10).
Next, the materials are delivered into the high-pressure underwater pelletizing system (12) via the pump (11), wherein 60 high-temperature die heads with a hole diameter of 0.8 mm are arranged in the high-pressure underwater pelletizing system (12); the materials are scraped by blades into small particles of 0.7-1.0 mm, wherein both die heads and scraping blades are immersed in high-pressure cooling water at 40°C; and the finished product, i.e., EPS particles, is obtained through cooling, pelletizing and drying.
Through testing, the obtained flame-retardant EPS has an oxygen index of 32, satisfying requirements for class B1 fireproof materials. Data of EPS prepared by this method and EPS prepared by the suspension method are compared and analysed. Production consumption data are as shown in Table 1 and product performance test data are as shown in Table 2.
Table 1 Production consumption data
Material Unit Test data of producing Data of producing flame-
EPS by the method of the | retardant EPS by suspension rn mw omeerees | 0 | 8
Ki ehr | Fofov ofS | 8 | ow wd | Twonoes | 0 | wm
Table 2 Product performance test data
Index Test data of EPS prepared Data of EPS prepared by by the embodiment suspension method
Molecular weight (number-average 188,000 55,000 molecular weight)
Molecular weight (weight-average 396,000 molecular weight)
Particle size (mm) 0.80+0.05 0.3-4.5, multilevel particle diameters
It can be seen from Table 1 and Table 2 that the flame-retardant EPS with the equivalent flame-retarding effect can be obtained by adding 0.9% of octabromodiphenyl ether (flame retardant) through the bulk polymerization in the present invention, and the consumption of raw materials and the discharge of wastewater and waste gas are reduced. The continuous production by bulk polymerization is realized, so that production cost is reduced, and the product performance is greatly improved.

Claims (5)

CONCLUSIESCONCLUSIONS 1. Een inrichting voor het bereiden van brandvertragend expandeerbaar polystyreen (EPS) door bulkpolymerisatie, waarbij — het onderste einde van een polymerisatiereactor (1-1) in serie is verbonden met een polymerisatiereactor (1-2) via een afvoerpomp (4-1); — materiaalinlaten zijn aangebracht aan de koppen van de polymerisatiereactoren (1-1) en (1-2), — reactieroerders (2-1) en (2-2) aangebracht zijn in het middengedeelte van de koppen, — de koppen in verbinding staan met condensors (3-1) en (3-2); — het onderste uiteinde van de polymerisatiereactor (1-2) via een afvoerpomp (4-2) verbonden is met een verwarmingsontgasser (5), — een condensor (7) is verbonden met het bovenste uiteinde van de verwarmingsontgasser (5), — de condensor (7) verbonden is met een vacuümopvangreservoir (8); — de bodem van de verwarmingsontgasser (5) via een pomp (6) verbonden is met een dynamische mixer (9). — de dynamische mixer (9) verbonden is met een smeltwarmtewisselaar (10); — een vlamvertragende masterbatchconnector (9-1) is aangebracht aan de voorkant van de dynamische mixer (9), — een klep om materiaalterugstroom te verhinderen is aangebracht aan de connector (9-1); — de smeltwarmtewisselaar (10) via een pomp (11) is verbonden met een hoge druk onderwaterpelletiseersysteem (12); en — de diameter van de openingen van hogetemperatuurmatrijskoppen in het hoge druk onderwaterpelletiseersysteem (12) 0,8 mm bedraagt.An apparatus for producing fire-retardant expandable polystyrene (EPS) by bulk polymerization, wherein - the lower end of a polymerization reactor (1-1) is connected in series with a polymerization reactor (1-2) through a discharge pump (4-1) ; — material inlets are provided at the heads of the polymerization reactors (1-1) and (1-2), — reaction stirrers (2-1) and (2-2) are located in the central part of the heads, — the heads are connected with condensers (3-1) and (3-2); — the lower end of the polymerization reactor (1-2) is connected via a discharge pump (4-2) to a heat degasser (5), — a condenser (7) is connected to the upper end of the heat degasser (5), — the condenser (7) is connected to a vacuum collecting reservoir (8); - the bottom of the heating deaerator (5) is connected via a pump (6) to a dynamic mixer (9). - the dynamic mixer (9) is connected to a melt heat exchanger (10); — a flame-retardant masterbatch connector (9-1) is fitted to the front of the dynamic mixer (9), — a valve to prevent material backflow is fitted to the connector (9-1), - the melt heat exchanger (10) is connected via a pump (11) to a high pressure underwater pelletizing system (12); and - the diameter of the openings of high temperature die heads in the high pressure underwater pelletizing system (12) is 0.8 mm. 2. De inrichting volgens conclusie 1, waarbij de reactieroerders (2-1) en (2-2) roerders met variabele frequentie en regelbare snelheid zijn.The apparatus according to claim 1, wherein the reaction stirrers (2-1) and (2-2) are variable frequency adjustable speed stirrers. 3. De inrichting volgens conclusie 1 of 2, waarbij — de in de polymerisatiereactor (1-1) af te geven materialen omvatten: 89-93 kg styreen, 5,0 kg ethylbenzeen (oplosmiddel), en 2,0-4,0 kg additief dat een of meer van de volgende stoffen bevat: witte olie, tributylfosfaat, polyethyleen met een laag molecuulgewicht (kiemvormer), calciumstearaat en MgO; en — de in de dynamische mixer (9) af te geven materialen omvatten: 5.0-7,0 kg pentaan (schuimmiddel}, en 0,7-1,0 kg vlamvertrager die een of meer van de volgende vlamvertragers bevat: broompolystyreen, een vlamvertrager van de octabroomreeks en een vlamvertrager van de tetrabroomreeks.The apparatus according to claim 1 or 2, wherein - the materials to be delivered into the polymerization reactor (1-1) include: 89-93 kg styrene, 5.0 kg ethylbenzene (solvent), and 2.0-4.0 kg of additive containing one or more of the following: white oil, tributyl phosphate, low molecular weight polyethylene (nucleating agent), calcium stearate and MgO; and — the materials to be delivered into the dynamic mixer (9) include: 5.0-7.0 kg pentane (foaming agent}, and 0.7-1.0 kg flame retardant containing one or more of the following flame retardants: bromopolystyrene, a flame retardant of the octabromine series and a flame retardant of the tetrabromine series. 4. De inrichting volgens conclusie 1 of 2, waarbij — de in de polymerisatiereactor (1-1) af te geven materialen de volgende componenten omvatten: 92.0 kg styreen, 5,0 kg ethylbenzeen, 1,0 kg witte olie, 0,5 kg tributylfosfaat, en 1,0 kg polyethyleen met een laag molecuulgewicht (kiemvormer); en — de in de dynamische mixer (9) ) af te geven materialen omvatten: 6.0 kg pentaan {schuimmiddel}, en 0,9 kg octabroomdifenylether (vlamvertrager).The apparatus according to claim 1 or 2, wherein - the materials to be delivered in the polymerization reactor (1-1) include the following components: 92.0 kg styrene, 5.0 kg ethylbenzene, 1.0 kg white oil, 0.5 kg tributyl phosphate, and 1.0 kg low molecular weight polyethylene (nucleator); and - the materials to be delivered into the dynamic mixer (9) include: 6.0 kg pentane {foaming agent}, and 0.9 kg octabromodiphenyl ether (flame retardant). 5. Een werkwijze voor de bereiding van brandvertragend EPS met behulp van de inrichting volgens willekeurig welke van de conclusies 1 - 4, die de volgende stappen omvat: stap 1: bereiden van een kiemvormer tot een oplossing van 10,0% met behulp van styreen; het mengen van styreen, een ethylbenzeen oplosmiddel en een additief, het continu toevoeren van het mengsel in een polymerisatiereactor (1-1), het regelen van de temperatuur van de materialen in de polymerisatiereactor (1-1) op 148°C en van de rotatiesnelheid van een roerder (2-1) op 40 omwentelingen per minuut, het aanzetten van een condensor (3-1) voor het terugvloeien, en het koelen van de damp die in de polymerisatiereactor (1-1) stroomt; het gedurende 100 minuten uitvoeren van een polymerisatiereactie; stap 2: vervolgens inbrengen van de materialen via een afvoerpomp (4-1) in een polymerisatiereactor (1-2) voor verdere reactie, waarbij de temperatuur van de materialen in een polymerisatiereactor (1-2) wordt geregeld op 160°C en de rotatiesnelheid van een roerder (2-2} op 15 omwentelingen per minuut wordt geregeld; het inschakelen van een condensor (3-2) voor het terugvloeien, en het koelen van de damp om in de polymerisatiereactor (1-2) te stromen; stap 3: wanneer de styreenconversie 70% bedraagt, het voeren van het materiaal uit de polymerisatiereactor (1-2) via de afvoerpomp (4-2) naar de top van een verwarmingsontgasser (5), het regelen van de temperatuur van de verwarmingsontgasser (5) op 240°C en het vacuüm op -0,098 MPa, voltooien van de ontspanningsverdamping binnen 1 min, en afkoelen door een condensor (7) om het niet-gereageerde styreen, het oplosmiddel en andere lichte bestanddelen die door de ontspanningsverdamping zijn verwijderd in een vacuümopvangreservoir (8) te laten stromen; stap 4: het via een pomp (6) in een dynamische mixer (9) brengen van een eerste vloeistof van polystyreen, verkregen door het verwijderen van het niet-gereageerde styreen, het oplosmiddel en andere lichte bestanddelen; het intussen inbrengen van een tweede vloeistof van pentaan (schuimmiddel) en octabroomdifenylether via een connector (9-1) in een dynamische mixer (9) en het gelijkmatig mengen van de twee vloeistoffen door afschuiving bij hoge snelheid in de dynamische menger (9); en stap 5:het verlagen van de temperatuur van de materialen tot 185°C door een smeltwarmtewisselaar (10), en het afleveren van de materialen in een hoge druk onderwaterpelletiseersysteem (12) via een pomp (11), waarbij 60 hogetemperatuurmatrijskoppen met een openingdiameter van 0,8 mm in de hoge druk onderwaterpelletiseersysteem (12) zijn aangebracht; het afschrapen van de materialen door messen tot kleine deeltjes van 0,7-1,0 mm, waarbij zowel de matrijskoppen als de schraapbladen worden ondergedompeld in hogedrukkoelwater van 40°C; en het verkrijgen van brandvertragende EPS-deeltjes door pelletiseren en drogen.A method for the preparation of fire-retardant EPS using the apparatus according to any one of claims 1 to 4, comprising the following steps: step 1: preparing a nucleator to a 10.0% solution using styrene ; mixing styrene, an ethylbenzene solvent and an additive, continuously feeding the mixture into a polymerization reactor (1-1), controlling the temperature of the materials in the polymerization reactor (1-1) to 148°C and rotating speed of a stirrer (2-1) at 40 rpm, turning on a condenser (3-1) for reflux, and cooling the vapor flowing into the polymerization reactor (1-1); conducting a polymerization reaction for 100 minutes; step 2: then introducing the materials through a discharge pump (4-1) into a polymerization reactor (1-2) for further reaction, controlling the temperature of the materials in a polymerization reactor (1-2) to 160°C and rotational speed of a stirrer (2-2} is controlled at 15 rpm; switching on a condenser (3-2) for reflux, and cooling the vapor to flow into the polymerization reactor (1-2); step 3: When the styrene conversion is 70%, feeding the material from the polymerization reactor (1-2) through the discharge pump (4-2) to the top of a heat degasser (5), controlling the temperature of the heat degasser (5 ) at 240°C and the vacuum at -0.098 MPa, completing flash evaporation within 1 min, and cooling through a condenser (7) to collect the unreacted styrene, solvent and other light components removed by flash evaporation in a to let the vacuum collection reservoir (8) flow; step 4: introducing through a pump (6) into a dynamic mixer (9) a first liquid of polystyrene obtained by removing the unreacted styrene, the solvent and other light components; meanwhile introducing a second liquid of pentane (foaming agent) and octabromodiphenyl ether through a connector (9-1) into a dynamic mixer (9) and uniformly mixing the two liquids by high speed shear in the dynamic mixer (9); and step 5: lowering the temperature of the materials to 185°C through a melt heat exchanger (10), and delivering the materials into a high pressure underwater pelletizing system (12) via a pump (11), where 60 high temperature die heads with an orifice diameter of 0.8 mm in the high pressure underwater pelletizing system (12); scraping the materials by knives into small particles of 0.7-1.0 mm, with both die heads and scraper blades immersed in high-pressure cooling water at 40°C; and obtaining fire retardant EPS particles by pelletizing and drying.
NL2032626A 2022-06-30 2022-07-28 Device for producing flame-retardant expandable polystyrene by bulk polymerization NL2032626B1 (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202210766797.0A CN115090245B (en) 2022-06-30 2022-06-30 Device for producing flame-retardant foamable polystyrene by bulk method

Publications (1)

Publication Number Publication Date
NL2032626B1 true NL2032626B1 (en) 2023-05-16

Family

ID=83294954

Family Applications (1)

Application Number Title Priority Date Filing Date
NL2032626A NL2032626B1 (en) 2022-06-30 2022-07-28 Device for producing flame-retardant expandable polystyrene by bulk polymerization

Country Status (2)

Country Link
CN (1) CN115090245B (en)
NL (1) NL2032626B1 (en)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115960286B (en) * 2022-12-23 2023-11-03 常州瑞华化工工程技术股份有限公司 Control system and control method for reaction sampling of expanded polystyrene

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070112082A1 (en) * 2003-12-12 2007-05-17 Basf Aktiengesellschaft Moldable-foam moldings composed of expandable pelletized filled polymer materials
US20090039537A1 (en) * 2004-07-15 2009-02-12 Basf Aktiengesellschaft Method for the Production of Expandable Styrol Polymers Having Improved Expandability
CN101678565B (en) * 2007-05-18 2014-09-24 波利玛利欧洲股份公司 Process for the preparation of granules based on expandable thermoplastic polymers and relative product
CN105294041A (en) 2015-11-06 2016-02-03 合肥神舟建筑集团有限公司 Homogeneous modified fireproof heat insulation board
CN112661910A (en) * 2020-12-28 2021-04-16 江苏可立特工程设计研究有限公司 Impact-resistant polystyrene with capacity of more than 5 ten thousand tons and equipment and production process thereof

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1163529C (en) * 2000-06-12 2004-08-25 吉林华标化学工业有限责任公司 Process for preparing high-property high-impactness polystyrene
CN101058621B (en) * 2007-05-16 2011-06-22 中国中化股份有限公司 Method of preparing ACS polymer based on continuous noumenon method
WO2009000872A1 (en) * 2007-06-28 2008-12-31 Basf Se Moulded foams made of expandable acrylonitrile copolymers
IT201600079947A1 (en) * 2016-07-29 2018-01-29 Versalis Spa Expandable polymeric composition containing ethylene-vinyl acetate copolymers
KR101912893B1 (en) * 2017-01-05 2018-10-29 (주)시그마소재 Flame retardant styrofoam produced by using flame retardant vinyl acetate polymer emulsion resin
CN215517232U (en) * 2020-12-28 2022-01-14 江苏可立特工程设计研究有限公司 Production equipment for transparent polystyrene with capacity of more than 5 ten thousand tons and production scale
CN113877498A (en) * 2021-09-30 2022-01-04 长春工业大学 Device and method for preparing SAN resin with stable composition and low volatile component
CN114262461A (en) * 2021-12-18 2022-04-01 秦发伟 Method for producing expandable polystyrene beads and method for producing foamed plastic using the beads

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070112082A1 (en) * 2003-12-12 2007-05-17 Basf Aktiengesellschaft Moldable-foam moldings composed of expandable pelletized filled polymer materials
US20090039537A1 (en) * 2004-07-15 2009-02-12 Basf Aktiengesellschaft Method for the Production of Expandable Styrol Polymers Having Improved Expandability
CN101678565B (en) * 2007-05-18 2014-09-24 波利玛利欧洲股份公司 Process for the preparation of granules based on expandable thermoplastic polymers and relative product
CN105294041A (en) 2015-11-06 2016-02-03 合肥神舟建筑集团有限公司 Homogeneous modified fireproof heat insulation board
CN112661910A (en) * 2020-12-28 2021-04-16 江苏可立特工程设计研究有限公司 Impact-resistant polystyrene with capacity of more than 5 ten thousand tons and equipment and production process thereof

Also Published As

Publication number Publication date
CN115090245A (en) 2022-09-23
CN115090245B (en) 2023-10-24

Similar Documents

Publication Publication Date Title
NL2032626B1 (en) Device for producing flame-retardant expandable polystyrene by bulk polymerization
US6319996B1 (en) Polymerization process using a dual shear mixing element
US3954722A (en) Manufacture of uniform polymers
US20130345328A1 (en) Process for the preparation of granules based on expandable thermoplastic polymers and relative product
CN101091901A (en) Helix stirred reactor with cryogen gong through inside, application, and technical method of polyreaction
US5551859A (en) Particulator
CN215517232U (en) Production equipment for transparent polystyrene with capacity of more than 5 ten thousand tons and production scale
CN101016465A (en) Process for preparing high viscosity modified asphalt
CN103421139A (en) Compatilizer and applications thereof
EP1771501A1 (en) Method for the production of expandable styrol polymers having improved expandability
CN106188374A (en) High nitrile SAN resin and production method thereof
NO873468L (en) MIXTURES OF ETHYLENE POLYMERS, PROCEDURES FOR MANUFACTURING AND USING THEREOF FOR PRODUCTION OF INDUSTRIAL ARTICLES
US3330818A (en) Elimination of fouling in ziegler polymerizations
CN104877056A (en) Polyvinyl chloride resin preparing method capable of reducing membranes of surfaces of particles and improving porosity
CN103450404A (en) ABS production technology through bulk polymerization method
CN106565876A (en) Continuous preparation method of controlled-molecular-weight brominated polystyrene
CN115253954B (en) Continuous reaction device and application
CN106188400A (en) A kind of preparation technology of polystyrene multi-component copolymer macromolecular material
CN1372572A (en) High impact polystyrene containing polyphenylene oxide
CN114917852B (en) Method for continuously producing graphite expandable polystyrene by bulk method
CN114984892B (en) Device for producing graphite foamable polystyrene by bulk method
CN113754806B (en) Preparation method of expanded polystyrene
CN104610506A (en) High-melt strength polypropylene and preparation method thereof
CN102443110B (en) Bulk polymerization production process of ABS (Acrylonitrile Butadiene Styrene) resin and application of static mixer
CN112495310B (en) System and process for strengthening propylene polymerization