CN103158208B - Method and equipment suitable for drying ABS graft polymer - Google Patents
Method and equipment suitable for drying ABS graft polymer Download PDFInfo
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- CN103158208B CN103158208B CN201110421162.9A CN201110421162A CN103158208B CN 103158208 B CN103158208 B CN 103158208B CN 201110421162 A CN201110421162 A CN 201110421162A CN 103158208 B CN103158208 B CN 103158208B
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- 229920000578 graft copolymer Polymers 0.000 title claims abstract description 64
- 238000001035 drying Methods 0.000 title claims abstract description 47
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- 229920005989 resin Polymers 0.000 claims abstract description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 32
- 238000001816 cooling Methods 0.000 claims abstract description 12
- 230000018044 dehydration Effects 0.000 claims abstract description 12
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 12
- 239000000314 lubricant Substances 0.000 claims abstract description 9
- 239000003963 antioxidant agent Substances 0.000 claims abstract description 7
- 230000003078 antioxidant effect Effects 0.000 claims abstract description 7
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- 238000010438 heat treatment Methods 0.000 claims abstract description 4
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- PZRWFKGUFWPFID-UHFFFAOYSA-N 3,9-dioctadecoxy-2,4,8,10-tetraoxa-3,9-diphosphaspiro[5.5]undecane Chemical compound C1OP(OCCCCCCCCCCCCCCCCCC)OCC21COP(OCCCCCCCCCCCCCCCCCC)OC2 PZRWFKGUFWPFID-UHFFFAOYSA-N 0.000 claims description 7
- RKISUIUJZGSLEV-UHFFFAOYSA-N n-[2-(octadecanoylamino)ethyl]octadecanamide Chemical compound CCCCCCCCCCCCCCCCCC(=O)NCCNC(=O)CCCCCCCCCCCCCCCCC RKISUIUJZGSLEV-UHFFFAOYSA-N 0.000 claims description 7
- 230000000694 effects Effects 0.000 claims description 6
- BGYHLZZASRKEJE-UHFFFAOYSA-N [3-[3-(3,5-ditert-butyl-4-hydroxyphenyl)propanoyloxy]-2,2-bis[3-(3,5-ditert-butyl-4-hydroxyphenyl)propanoyloxymethyl]propyl] 3-(3,5-ditert-butyl-4-hydroxyphenyl)propanoate Chemical compound CC(C)(C)C1=C(O)C(C(C)(C)C)=CC(CCC(=O)OCC(COC(=O)CCC=2C=C(C(O)=C(C=2)C(C)(C)C)C(C)(C)C)(COC(=O)CCC=2C=C(C(O)=C(C=2)C(C)(C)C)C(C)(C)C)COC(=O)CCC=2C=C(C(O)=C(C=2)C(C)(C)C)C(C)(C)C)=C1 BGYHLZZASRKEJE-UHFFFAOYSA-N 0.000 claims description 5
- 230000004927 fusion Effects 0.000 claims description 2
- 239000011145 styrene acrylonitrile resin Substances 0.000 claims description 2
- HQKMJHAJHXVSDF-UHFFFAOYSA-L magnesium stearate Chemical compound [Mg+2].CCCCCCCCCCCCCCCCCC([O-])=O.CCCCCCCCCCCCCCCCCC([O-])=O HQKMJHAJHXVSDF-UHFFFAOYSA-L 0.000 claims 2
- 235000019359 magnesium stearate Nutrition 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 26
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- 235000012438 extruded product Nutrition 0.000 abstract 1
- 239000008187 granular material Substances 0.000 abstract 1
- 230000008016 vaporization Effects 0.000 abstract 1
- 229920000122 acrylonitrile butadiene styrene Polymers 0.000 description 81
- 229920001971 elastomer Polymers 0.000 description 26
- 239000005060 rubber Substances 0.000 description 26
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- 239000000047 product Substances 0.000 description 18
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- 239000000126 substance Substances 0.000 description 15
- 239000000839 emulsion Substances 0.000 description 14
- 239000000463 material Substances 0.000 description 13
- 208000005156 Dehydration Diseases 0.000 description 10
- 238000005406 washing Methods 0.000 description 9
- 238000005453 pelletization Methods 0.000 description 8
- 229920000642 polymer Polymers 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- RZVAJINKPMORJF-UHFFFAOYSA-N Acetaminophen Chemical compound CC(=O)NC1=CC=C(O)C=C1 RZVAJINKPMORJF-UHFFFAOYSA-N 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
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- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 3
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000008188 pellet Substances 0.000 description 3
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- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 description 1
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- 239000001307 helium Substances 0.000 description 1
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- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
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- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
- Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
- Processes Of Treating Macromolecular Substances (AREA)
Abstract
The invention relates to a method suitable for drying an ABS graft polymer; adding wet ABS graft polymer powder with water content of 10-40 wt% formed after a dehydration procedure, a lubricant, an antioxidant and SAN resin into a double-screw extruder, gradually melting and plasticizing the ABS graft polymer under the actions of conveying and shearing of a screw and heating of a cylinder, completely vaporizing moisture, and separating water vapor out through an exhaust system and a vacuum system; extruding the molten ABS graft polymer through a die head, and cooling and cutting into granules to form ABS dry colloidal particles; the ABS dry colloidal particles produced by the process are convenient to store and convey, the environmental pollution is reduced, the produced ABS dry colloidal particles can be blended with SAN resin and other additives such as flame retardants, coloring agents and the like, the production process is independent, the operation is flexible, and the defects of single type and complex operation of wet-process extruded products are overcome.
Description
Technical field:
The present invention relates to a kind of method and apparatus being suitable for ABS graft polymer drying.
Background technology:
ABS is the two phase structure that rubber is dispersed in SAN resin-phase mutually.Current ABS production technology mainly emulsion graft polymerization-body SAN blending technique and continuous bulk technique in the world, continuous bulk technique does not use water, therefore there is not dry problem, but continuous bulk complex process, device structure is special and product category is few, application is restricted, and therefore this technique is not widely adopted.Possess skills maturation, properties of product of emulsion graft polymerization-body SAN blending ABS production technology are excellent, wide in variety, and the features such as grade transition is easy, the ABS product of current more than 80% is by this explained hereafter.
Emulsion graft polymerization-body SAN blending technique comprises the synthesis of ABS graft polymer and synthesis two parts of SAN resin, wherein SAN resin is synthesized by bulk process usually, and ABS graft polymer is by the first synthesizing polybutadiene rubber particle of emulsion polymerization technique, then at the outer graft phenylethene of rubber particles and acrylonitrile, ABS graft polymer is formed.ABS graft polymer and SAN resin are by mixing formation ABS resin.Traditional emulsion graft polymerization-body SAN blending technique ABS glycerol polymerization is polymerized separate with SAN, blended by extruder again after producing ABS graft polymer dry powder and SAN resin particle, each technique unit of this technique is independent, operating flexibility is large, the production trade mark is many, produce flexibly, be suitable for the production of PP Pipe Compound, the special trade mark, small lot, color-tinted product.This technique is also referred to as dry process.
Current ABS graft polymer production process is mainly still by air boiling bed drying process, this technical process is: the ABS graft polymer slurries condensed are carried out cleaning and filtering to vacuum belt filter by transport pump, the electrolyte that removing course of reaction adds, the water-soluble substanceses such as emulsifying agent, and slurries are filtered, form the filter cake of water content about 50%wt, filter cake falls into by gravity and extrudes dewaterer or centrifugal dehydrator, further dehydration is to 10-30%wt, material after dehydration becomes fine powder through crusher in crushing, fine powder adds fluid-bed dryer, dried powder water content is less than 1%wt, dry mash is stored in feed bin, anti-bridge formation feed bin and air bubble concussion is adopted for preventing from building bridge, wind is utilized to send the feeding of pipeline interval according to extruder operational circumstances in use procedure.Drier gas is by Steam Heating, be blown into drier by bottom after blower fan pressurization, form powder fluidized state, side's gas after cyclone separator is separated enters scrubbing tower on the dryer, after washing, gas enters air, processing containing dust waste water is unified of washing.Whole drying process can divide four parts: one is cleaning and the filtration of ABS graft polymer slurries, two is dehydrations, three is boiled bed dryings, and four is storages of dry mash, and what wherein there are major safety risks is the storage course of conveying of boiled bed drying process and dry mash.Continuous fluidized bed drying process, most employing air oxygen detrition, dry run energy consumption is high, material consumption is high, and environmental pollution is serious, and there is the potential safety hazard of powder combustion explosion, and domestic and international enterprise super-dry device all occurs and dodges quick-fried or powder pyrophoricity accident; For preventing dust accumulation generation decomposition from causing combustion explosion, drier needs periodic cleaning; It is aging that dry run also makes powder occur, and reduces properties of product; In the conveying and processing procedure of ABS graft polymer dry powder, also can produce a large amount of dust, can harm be produced to working environment; Adopt boiled bed drying technique to be also subject to the restriction of capacity of equipment simultaneously, make dry run become the bottleneck of whole technique.
The process route solving the dry potential safety hazard the best of ABS graft polymer cancels boiled bed drying process; generally adopt wet-method extrusion technique (as described in patent CN96107286.5) in the world at present, i.e. the SAN resin of ABS graft polymer wet-milling and SAN resin particle or melting is blended by extruder.This process characteristic be ABS graft polymer without drying, directly the ABS graft polymer powder of certain water content (being generally 10-30%wt) and SAN resin are added extruder, in an extruder realize dehydration and melt blending.Owing to containing moisture in wet mash, limit the application of extrusion, therefore this technique is only suitable for the production of universal product, unit maximum productivity about 7 tons/hour, produce in enormous quantities for the single trade mark, owing to eliminating drying process, product whiteness obviously increases.The difficult point of this technique is the metering of wet mash, because the fluctuation of ABS water content in production process causes final products to feed in raw material the change of proportioning, directly affects product quality.If the fluctuation range of water content is excessive simultaneously, then affect the stable operation of wet-method extrusion technique.
Patent CN02145581.3 describes another kind of solution, namely the gas flow-fluidized bed drying means of nitrogen circulation is utilized, in gas flow-fluidized bed combination drying technology, the techniques such as nitrogen circulating system, gas scrubbing, cooling, dehumidifying are incorporated, the cool cycles devising washings utilizes and the recovery of ABS graft polymer powder in washings, thus achieves a kind of safe and reliable gas flow-fluidized bed drying means of closed circuit nitrogen circulation.The method efficiently solves the accident potential of ABS graft polymer drying system dust explosion, monomer combustion, improve the quality of product, but bring equipment investment increase simultaneously, plant running expense increases, the helium leak problem that to cause that operating personnel suffocate etc. new.
Drying process of the present invention eliminates boiled bed drying process, and the storage course of conveying of dry mash, thus eliminates safe hidden trouble.The difficult point extruding drying process is that in ABS graft polymer, rubber content is higher, and the existence of rubber reduces the melt fluidity of ABS resin, therefore in extrusion, occurs signs of degradation.
Summary of the invention:
The object of this invention is to provide a kind of method and apparatus being suitable for ABS graft polymer drying, drying means is extruded with ABS wet mash, replace traditional boiled bed drying technique, eliminate the powder combustion explosion hidden danger that dry run exists, there is technique simple, easy operation, efficiency are high, production process safety method.
The present invention is in emulsion graft polymerization production ABS graft polymer technical process, utilizes double screw extruder to replace fluid-bed dryer to realize the dry run of ABS graft polymer wet mash.Present invention process equipment is made up of charging system 1, twin-screw extrusion system 2, gas extraction system 3, vacuum system 4, granulation cooling system 5.
The method being suitable for ABS graft polymer drying of the present invention is: add in double screw extruder 2-1 by the ABS graft polymer wet mash forming water content 10-40%wt after dehydration procedure, by the conveying of screw rod and the effect of shearing and cylindrical shell heating, ABS graft polymer is fusion plastification gradually, moisture is vaporized completely, water vapour is separated by gas extraction system 3 and vacuum system 4, the ABS graft polymer of melting is extruded through die head, form the dry micelle of ABS through cooling and dicing again, then wind delivers to feed bin storage.Whole process is carried out continuously, and technical process is shown in Figure of description 1.
ABS wet mash is added by wet mash feeder 1-1, and this feeder can be weight-loss type can be also positive displacement, regulates charging rate by variable-frequency motor.Degrading for preventing the ABS resin of high rubber content from extruding in dry run, adding the chemicals such as lubricant, antioxidant by a certain percentage while reinforced, adding a small amount of SAN resin if desired simultaneously.Added by weight-loss type chemicals feeder 1-2 after lubricant, antioxidant utilize super mixer to mix by a certain percentage, SAN resin particle is added by weight-loss type SAN resin feeder 1-3.Usually the lubricant selected comprises dolomol, N, N '-ethylene bis stearamide etc., the antioxidant usually selected comprises antioxidant 1010, antioxidant 618 etc.
For avoiding screw rod shearing to cause ABS graft polymer to degrade, double screw extruder 2-1 selects the Heterodromy double-screw extruder that shear strength is relatively little, reduces screw rod shearing intensity by adopting half engagement system.Half intermeshing counter-rotating twin-screw extruder working mechanism is different from engagement type, but be similar to single screw extrusion machine, namely by friction, viscous drag convey materials, because two screw rods not exclusively engage, between radial clearance larger, have larger leakage current, in batch mixing, exhaust, devolatilization etc., have certain application.For avoiding high temperature to cause ABS graft polymer to degrade, needing strictly to control extrusion temperature, being provided with cooling water system at extruder barrel for this reason.Double screw extruder is made up of 6 sections of cylindrical shells, and wherein first paragraph cylindrical shell connection loading hopper 2-2 is used for feeding in raw material, and third and fourth section of cylindrical shell is provided with exhaust outlet 2-3, and the 5th section of cylindrical shell is provided with vaccum exhaust outlet 2-4.
The effect of gas extraction system 3 is the steam being separated gasification, and the steam cooling of separating.Gas extraction system is made up of the twin-screw material spraying-preventing exhaust apparatus 3-1 be positioned at directly over extruder barrel, knockout drum 3-2, cooler 3-3, centrifugal blower 3-4.The liquid phase water of cooling enters waste water system, and gas phase enters air by centrifugal blower.
The effect of vacuum system 4 discharges moisture further, discharges low molecular weight volatile simultaneously and divide material, as monomers such as unreacted styrene.Vacuum system is made up of vacuum separation tank 4-1, water-ring vacuum pump 4-2, condensed water periodic exhaustion in knockout drum.
Granulation cooling system 5 is connected with the die head of the 6th section of barrel tip.Granulation cooling system connects different according to production capacity and selects different modes.For output lower than 50 kgs/hour extrude drying production line, granulating system adopts air cooling way or water cooling bracing pelletizing mode; For output be greater than 50 kgs/hour be less than 200 kgs/hour extrude drying production line, adopt water ring die face cutting mode; For output be greater than 200 kgs/hour extrude drying production line, adopt die face cutting form under water.Different according to granulation mode, in final products, water content is different, and under air-cooled condition, product water content is less than 0.05%wt; Under water-cooled condition, product water content is less than 1%wt.
Process conditions:
Extruder temperature is arranged:
| Cylindrical shell | 1 | 2 | 3 | 4 | 5 | Die head |
| Temperature DEG C | 50-80 | 70-110 | 100-150 | 130-180 | 150-200 | 200 |
Representative formula:
Note: in formula, ratio presses butt weight of material percentage calculation.
The effect of SAN resin is the melt flow property improving ABS graft polymer, is greater than 200 kgs/hour extruding dry production process and must add SAN resin for output.The addition of SAN resin is determined by extrudate color, then needs to increase SAN addition if there is yellowish, but total addition is no more than 10%wt.Because the water content of ABS graft polymer wet mash is unstable, cause the metering of ABS graft polymer wet mash inaccurate, therefore the ratio of ABS graft polymer (butt) and SAN resin cannot accurately be controlled, that is rubber content in product cannot accurately be grasped, metering for next step mixing extrusion is brought difficulty by this, therefore the least possiblely in principle add SAN resin, reduce the impact of water content fluctuation on product rubber content.By improving extruder screw combination, optimizing the process conditions such as extrusion temperature, rotating speed, adjustment antioxidant, lubricant ratio effectively can be improved and extrude drying effect, reduce the use amount of SAN resin.
Rubber content in ABS graft polymer wet mash is that the key factor of drying process and formula is extruded in impact, and along with the increase of rubber content, resin plasticizing mobile performance is deteriorated, and it is all the more difficult to extrude drying.Rubber content is generally with after ABS graft polymer drying, and the quality of rubber components accounts for the percent value of ABS graft polymer quality.For the ABS graft polymer powder of rubber content lower than 40%wt (butt), extruding dry run does not need to add SAN resin; For rubber content higher than 40%wt, lower than the ABS graft polymer powder of 65%wt (butt), SAN resin must be added under output is greater than 200 kgs/hour of situations.The present invention is suitable for the rubber content of ABS graft polymer not higher than 65%wt.
The screw speed of extruder is comparatively large on extruding dry product quality impact, and the present invention limits screw speed within 300rpm, therefore for obtaining the extruder that certain production capacity needs to select screw diameter larger.Relative to mixing extruder, due to restriction shear rate, extruding in dry run and need maintenance equipment to run under certain load condition, being about 50 kgs/hour as selected the incorgruous extruder output of twin-screw of 50mm.
Drying process of extruding of the present invention adopts based on the system process equipment of counter rotating half extruding machine with two screw rods engaging, and by adding antioxidant, lubricant and SAN resin, optimizes the measures such as expressing technique condition, effectively controls ABS graft polymer degraded.Water content can be made to be that 10-30%wt, rubber content are not down to below 1%wt higher than the ABS graft polymer water content of 65%wt by this technique, meet and extrude the requirement of blended production ABS resin.
The present invention improves emulsion graft polymerization method ABS graft polymer drying process, that invents extrudes the potential safety hazard that drying process thoroughly eliminates ABS graft polymer dry mash combustion explosion in boiled bed drying process, eliminates the problem such as bridge formation, leakage in powder Storing and conveying process.There is the advantages such as flow process is short, equipment simple, flexible operation, process.
Of the present inventionly extrude the bottleneck problem that drying process solves fluid-bed dryer production capacity, because the technological process of production is short, invest relatively little, extrude drying production line by increase simultaneously and can improve whole drying process production capacity and operating flexibility, eliminate the problem that fluid-bed dryer cleans and equipment fault causes whole production line to be stopped.
Replace ABS graft polymer dry mash by the dry micelle of the ABS of this explained hereafter, not only Storing and conveying is convenient, and reduces environmental pollution.Due to produce the dry micelle of ABS can with SAN resin and other additives as blended in fire retardant, colouring agent etc., therefore the ABS resin product of the different trade mark can be produced, production process is independent simultaneously, flexible operation, compensate for wet-method extrusion product category single, the shortcoming of complicated operation, with wet-method extrusion process ration, applicability of the present invention is stronger.
Accompanying drawing explanation
Figure 1A BS graft polymers extrudes drying process schematic diagram.
Wherein: 1-charging system: 1-1-wet mash feeder, 1-2-chemicals feeder, 1-3-SAN resin feeder; 2-twin-screw extrusion system: 2-1-double screw extruder, 2-2-loading hopper, 2-3-exhaust outlet, 2-4-vaccum exhaust outlet; 3-gas extraction system: 3-1-exhaust apparatus, 3-2-knockout drum, 3-3-cooler, 3-4-centrifugal blower; 4-vacuum system: 4-1-vacuum separation tank, 4-2-water-ring vacuum pump; 5-granulation cooling system.
Detailed description of the invention:
Embodiment 1
The ABS graft polymer emulsion of certain solid content is obtained by emulsion grafting polymerization process, the polymer clump that water content reaches 20-30%wt is obtained after cohesion, washing and extruder dehydration, ABS graft polymer rubber content is 60%wt, polymer clump is pulverized, put into wet mash feeder, dolomol, N, put into super mixer after N '-ethylene bis stearamide, antioxidant 1010, antioxidant 618 measure according to a certain percentage to mix, then take out and put into chemicals feeder.The Heterodromy double-screw extruder of screw diameter 50mm is selected to carry out extruding drying.
Operating process:
Extruder heats up and starts pellet device, gas extraction system centrifugal blower and exhaust apparatus, extruder main frame successively after stablizing.Slow raising extruder rotating speed is to 50rpm.
Start wet mash feeder, feeding capacity controls at 20 kgs/hour, and start chemicals feeder, feeding capacity controls at 1.0 kgs/hour simultaneously.
Vacuum system is started after extruder die head discharging.
Gradually extruder rotating speed is brought up to 120rpm after system stability.Suitably improve pelletizing rotating speed, improving wet mash feeder feeding capacity is 60 kgs/hour, improves chemicals feeding capacity in proportion simultaneously.
Process conditions:
Extruder operating condition is as following table:
| Cylindrical shell | 1 | 2 | 3 | 4 | 5 | Die head |
| Temperature DEG C | 80 | 90 | 120 | 150 | 180 | 190 |
Screw speed controls within 150rpm.
Add material formula:
Extrude dry after the pelletizing after air-cooled of material check rod, by the dry micelle of ABS that cuts and SAN resin blending extrusion on 50mm in the same way extruding machine with two screw rods engaging by a certain percentage.Blending temperature 200 DEG C, screw speed 100rpm, charging rate 50 kgs/hour.
Embodiment 2
By rubber content be the ABS graft polymer of 40%wt through washing, extrusion dehydration is the wet mash of 20-30%wt to water content, adds wet mash feeder after fragmentation.Dolomol, N, N '-ethylene bis stearamide, antioxidant 618 put into super mixer after measuring according to a certain percentage and mix, then take out and put into chemicals feeder.The Heterodromy double-screw extruder of screw diameter 50mm is selected to carry out extruding drying process.
Operating process:
Extruder heats up and starts pelletizing system, gas extraction system centrifugal blower and exhaust apparatus, extruder main frame successively after stablizing.Slow raising extruder rotating speed is to 50rpm.
Start wet mash feeder, feeding capacity controls at 20 kgs/hour, and start chemicals feeder, feeding capacity controls at 1.0 kgs/hour simultaneously.
Vacuum system is started after extruder die head discharging.
Gradually extruder rotating speed is brought up to 180rpm after system stability.Suitably improve pelletizing rotating speed, improving wet mash feeder feeding capacity is 100 kgs/hour, improves chemicals feeding capacity in proportion simultaneously.
Process conditions:
Extruder operating condition is as following table:
| Cylindrical shell | 1 | 2 | 3 | 4 | 5 | Die head |
| Temperature DEG C | 80 | 90 | 150 | 170 | 190 | 200 |
Screw speed controls within 200rpm.
Add material formula:
| Material | ABS graft polymer | Antioxidant 618 | Dolomol | N, N '-ethylene bis stearamide |
| Ratio %wt | 95 | 0.8 | 0.2 | 4 |
Extrude dry after the pelletizing after water-cooled of material check rod, by the dry micelle of ABS that cuts and SAN resin blending extrusion on 50mm in the same way extruding machine with two screw rods engaging by a certain percentage.Mixture rubber mass content and blending technology condition identical with embodiment 1.
Embodiment 3
The ABS graft polymer emulsion of certain solid content is obtained by emulsion grafting polymerization process, the polymer clump that water content reaches 20-30%wt is obtained after cohesion, washing and extruder dehydration, ABS graft polymer rubber content is 60%wt, polymer clump is pulverized, put into ABS wet mash feeder, dolomol, N, put into super mixer after N '-ethylene bis stearamide, antioxidant 1010, antioxidant 618 measure according to a certain percentage to mix, put into chemicals feeder after taking-up, SAN resin feeder put into by SAN resin.The Heterodromy double-screw extruder of screw diameter 75mm is selected to carry out extruding drying process.
Operating process:
Extruder heats up and starts pellet device, gas extraction system centrifugal blower and exhaust apparatus, extruder main frame successively after stablizing.Slow raising extruder rotating speed is to 50rpm.
Start wet mash feeder, feeding capacity controls at 40 kgs/hour, and start chemicals feeder, feeding capacity controls at 2.0 kgs/hour simultaneously.
Vacuum system is started after extruder die head discharging.
Gradually extruder rotating speed is brought up to 150rpm after system stability.Suitably improve pelletizing rotating speed, improving wet mash feeder feeding capacity is 130 kgs/hour, improves chemicals feeding capacity in proportion simultaneously.
Process conditions:
Extruder operating condition is as following table:
| Cylindrical shell | 1 | 2 | 3 | 4 | 5 | Die head |
| Temperature DEG C | 80 | 90 | 120 | 150 | 180 | 190 |
Screw speed controls within 200rpm.
Formula:
Extrude dry after material adopt water ring die face cutting mode, by the dry micelle of ABS that cuts and SAN resin blending extrusion on 50mm in the same way extruding machine with two screw rods engaging by a certain percentage.Mixture rubber mass content and blending technology condition identical with embodiment 1.
Embodiment 4
The ABS graft polymer emulsion of certain solid content is obtained by emulsion grafting polymerization process, the polymer clump that water content reaches 20-30%wt is obtained after cohesion, washing and extruder dehydration, ABS graft polymer rubber content is 60%wt, polymer clump is pulverized, put into ABS wet mash feeder, dolomol, N, put into super mixer after N '-ethylene bis stearamide, antioxidant 1010, antioxidant 618 measure according to a certain percentage to mix, then take out and put into chemicals feeder, SAN resin feeder put into by SAN resin.Select the Heterodromy double-screw extruder of screw diameter 95mm.
Operating process:
Extruder heats up and starts pellet device, gas extraction system centrifugal blower and exhaust apparatus, extruder main frame successively after stablizing.Slow raising extruder rotating speed is to 50rpm.
Start wet mash feeder, feeding capacity controls at 40 kgs/hour, and start chemicals feeder, feeding capacity controls at 2.0 kgs/hour simultaneously.
Vacuum system is started after extruder die head discharging.
Gradually extruder rotating speed is brought up to 150rpm after system stability.Suitably improve pelletizing rotating speed, improving wet mash feeder feeding capacity is 280 kgs/hour, improves chemicals feeding capacity in proportion simultaneously.
Process conditions:
Extruder operating condition is as following table:
| Cylindrical shell | 1 | 2 | 3 | 4 | 5 | Die head |
| Temperature DEG C | 80 | 90 | 120 | 150 | 180 | 190 |
Screw speed controls within 200rpm.
Formula:
Extrude dry after material adopt die face cutting under water, by the dry micelle of ABS that cuts and SAN resin blending extrusion on 50mm in the same way extruding machine with two screw rods engaging by a certain percentage.Mixture rubber mass content and blending technology condition identical with embodiment 1.
Comparative example
The ABS graft polymer emulsion of certain solid content is obtained by emulsion grafting polymerization process, the polymer clump that water content reaches 20-30%wt is obtained after cohesion, washing and extruder dehydration, ABS graft polymer rubber content is 60%wt, polymer clump is pulverized, add boiled bed drying wherein, be dried to the dry mash that water content is less than 0.8%wt, at diameter be 50mm double screw extruder on SAN resin alloy, add the auxiliary agent identical with embodiment 1 time blended, blending condition is identical with embodiment 1.
The ABS resin that above embodiment obtains obtains various performance test batten by injector injection mo(u)lding, and injection temperature 200 DEG C, the process conditions such as injection pressure, speed, injection time are identical.
Adopt ASTM D256 standard testing notch impact strength; Adopt ASTM D638 test tensile strength; Stream index is melted in ASTM D1238 test; ASTM D790 is adopted to test bending strength and bending modulus.
The ABS resin performance that embodiment 1-4 and comparison example obtain is as following table:
| Test event | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Comparative example |
| Rubber content in ABS resin, %wt | 13 | 13 | 13 | 13 | 13 |
| Hot strength, MPa | 51.6 | 52.3 | 50.9 | 51.6 | 52.4 |
| Bending strength, MPa | 91.2 | 91.8 | 89.4 | 91.0 | 92.7 |
| The modulus of elasticity in static bending, MPa | 2794 | 2802 | 2756 | 2788 | 2843 |
| Cantilever beam impact strength, J/m | 192 | 167 | 189 | 193 | 196 |
| Melt flow rate (MFR), g/10min | 21.4 | 20.3 | 21.2 | 20.2 | 21.5 |
| Whiteness | 56.8 | 57.0 | 55.7 | 54.2 | 57.5 |
| Test event | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Comparative example |
| Rubber content in ABS resin, %wt | 18 | 18 | 18 | 18 | 18 |
| Hot strength, MPa | 43.8 | 44.5 | 42.1 | 43.6 | 44.7 |
| Bending strength, MPa | 78.6 | 79.9 | 79.2 | 77.5 | 76.4 |
| The modulus of elasticity in static bending, MPa | 2378 | 2459 | 2381 | 2384 | 2431 |
| Cantilever beam impact strength, J/m | 400 | 289 | 410 | 389 | 410 |
| Melt flow rate (MFR), g/10min | 18.1 | 17.5 | 18.5 | 18.7 | 17.6 |
| Whiteness | 54.3 | 55.1 | 53.9 | 53.4 | 55.8 |
Found out by above data, extrude the dry micelle of ABS that drying process obtains and the ABS dry mash similar nature that boiled bed drying obtains, but in embodiment 2, the ABS graft polymer of 40%wt rubber content causes impact property on the low side due to the difference of Grafting Structure.
Claims (1)
1. one kind is suitable for the method for ABS graft polymer drying, it is characterized in that: after dehydration procedure, form water content 10-40%wt ABS graft polymer wet mash and lubricant, antioxidant, SAN resin are added in double screw extruder, by the conveying of screw rod and the effect of shearing and cylindrical shell heating, ABS graft polymer is fusion plastification gradually, moisture is vaporized completely, and water vapour is separated by gas extraction system and vacuum system; The ABS graft polymer of melting is extruded through die head, then forms the dry micelle of ABS through cooling and dicing;
By weight percentage: ABS graft polymer is 82-95%wt, SAN resin 0-10%wt, and antioxidant 1010 is 0.2-0.8%, antioxidant 618 is 0.2-1.0%, magnesium stearate lubricant 0.1-0.6%, lubricant N, N '-ethylene bis stearamide 4.0-6.0%;
Described twin-screw extrusion machine barrel is provided with 6 sections of cylindrical shells, and temperature is followed successively by: one section of cylindrical shell 50-80 DEG C, two sections of barrel temperature 70-110 DEG C, three sections of barrel temperature 100-150 DEG C, four sections of barrel temperature 130-180 DEG C, five sections of barrel temperature 150-200 DEG C, die head temperature 200 DEG C.
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| CN106042215A (en) * | 2016-07-04 | 2016-10-26 | 安徽斯威达建材科技有限公司 | Foam dryer |
| CN109772228A (en) * | 2018-11-21 | 2019-05-21 | 内蒙古世杰化工有限公司 | A kind of melting drying granulation crushing all-in-one machine |
| CN110922535A (en) * | 2019-07-20 | 2020-03-27 | 杨青岚 | Method for preparing ABS plastic by continuous body |
| CN113136007A (en) * | 2021-03-26 | 2021-07-20 | 林轩 | Preparation method of porous ABS graft polymer particles easy to dry |
| CN113337046B (en) * | 2021-07-23 | 2022-06-03 | 浙江智英石化技术有限公司 | Preparation method of ABS resin particles |
| CN114130303B (en) * | 2021-11-27 | 2023-11-14 | 南京创博机械设备有限公司 | TGIC efficient devolatilization and melt extrusion granulation integrated processing method |
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