CN104339469A - Devolatilization method and equipment for thermoplastic elastomer - Google Patents
Devolatilization method and equipment for thermoplastic elastomer Download PDFInfo
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- CN104339469A CN104339469A CN201310345191.0A CN201310345191A CN104339469A CN 104339469 A CN104339469 A CN 104339469A CN 201310345191 A CN201310345191 A CN 201310345191A CN 104339469 A CN104339469 A CN 104339469A
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- 238000000034 method Methods 0.000 title claims abstract description 50
- 229920002725 thermoplastic elastomer Polymers 0.000 title claims abstract description 41
- 238000001035 drying Methods 0.000 claims abstract description 67
- 238000001125 extrusion Methods 0.000 claims abstract description 7
- 238000005469 granulation Methods 0.000 claims abstract description 6
- 230000003179 granulation Effects 0.000 claims abstract description 6
- 239000000693 micelle Substances 0.000 claims description 62
- 239000003292 glue Substances 0.000 claims description 37
- 230000001681 protective effect Effects 0.000 claims description 19
- 238000007664 blowing Methods 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 25
- 239000002245 particle Substances 0.000 abstract description 8
- 239000007788 liquid Substances 0.000 abstract description 7
- 238000004140 cleaning Methods 0.000 abstract description 4
- 239000011148 porous material Substances 0.000 description 10
- 238000009825 accumulation Methods 0.000 description 9
- 239000000839 emulsion Substances 0.000 description 9
- 238000012856 packing Methods 0.000 description 9
- 229920001971 elastomer Polymers 0.000 description 7
- 238000005453 pelletization Methods 0.000 description 7
- 239000005060 rubber Substances 0.000 description 7
- 238000007599 discharging Methods 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 239000002904 solvent Substances 0.000 description 6
- 238000009835 boiling Methods 0.000 description 5
- 230000001276 controlling effect Effects 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 238000006116 polymerization reaction Methods 0.000 description 5
- CJZGTCYPCWQAJB-UHFFFAOYSA-L calcium stearate Chemical compound [Ca+2].CCCCCCCCCCCCCCCCCC([O-])=O.CCCCCCCCCCCCCCCCCC([O-])=O CJZGTCYPCWQAJB-UHFFFAOYSA-L 0.000 description 4
- 235000013539 calcium stearate Nutrition 0.000 description 4
- 239000008116 calcium stearate Substances 0.000 description 4
- 239000008187 granular material Substances 0.000 description 4
- 229920000642 polymer Polymers 0.000 description 4
- 230000033001 locomotion Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- -1 offset plate Substances 0.000 description 3
- 230000000737 periodic effect Effects 0.000 description 3
- 229920003023 plastic Polymers 0.000 description 3
- 239000004033 plastic Substances 0.000 description 3
- 238000012805 post-processing Methods 0.000 description 3
- 239000011347 resin Substances 0.000 description 3
- 229920005989 resin Polymers 0.000 description 3
- 238000005507 spraying Methods 0.000 description 3
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 2
- 239000004698 Polyethylene Substances 0.000 description 2
- 239000000853 adhesive Substances 0.000 description 2
- 230000001070 adhesive effect Effects 0.000 description 2
- 239000002390 adhesive tape Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000007701 flash-distillation Methods 0.000 description 2
- 238000010528 free radical solution polymerization reaction Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- RGSFGYAAUTVSQA-UHFFFAOYSA-N pentamethylene Natural products C1CCCC1 RGSFGYAAUTVSQA-UHFFFAOYSA-N 0.000 description 2
- 125000004817 pentamethylene group Chemical group [H]C([H])([*:2])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[*:1] 0.000 description 2
- 238000004513 sizing Methods 0.000 description 2
- 229920000468 styrene butadiene styrene block copolymer Polymers 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 229920002554 vinyl polymer Polymers 0.000 description 2
- ATKFMEGWDYLXBP-UHFFFAOYSA-N 2-(2,4,5-trichlorophenoxy)ethanol Chemical compound OCCOC1=CC(Cl)=C(Cl)C=C1Cl ATKFMEGWDYLXBP-UHFFFAOYSA-N 0.000 description 1
- 229920000178 Acrylic resin Polymers 0.000 description 1
- 239000004925 Acrylic resin Substances 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical group C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Natural products N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000005422 blasting Methods 0.000 description 1
- 230000002596 correlated effect Effects 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 150000001993 dienes Chemical class 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 229920006351 engineering plastic Polymers 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 150000002222 fluorine compounds Chemical class 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000011505 plaster Substances 0.000 description 1
- 229920002589 poly(vinylethylene) polymer Polymers 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 229920001296 polysiloxane Polymers 0.000 description 1
- 229920002742 polystyrene-block-poly(ethylene/propylene) -block-polystyrene Polymers 0.000 description 1
- 229920000346 polystyrene-polyisoprene block-polystyrene Polymers 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000013557 residual solvent Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 229920001935 styrene-ethylene-butadiene-styrene Polymers 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229920006346 thermoplastic polyester elastomer Polymers 0.000 description 1
- 125000000391 vinyl group Chemical group [H]C([*])=C([H])[H] 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B9/00—Making granules
- B29B9/02—Making granules by dividing preformed material
- B29B9/06—Making granules by dividing preformed material in the form of filamentary material, e.g. combined with extrusion
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B13/00—Conditioning or physical treatment of the material to be shaped
- B29B13/06—Conditioning or physical treatment of the material to be shaped by drying
- B29B13/065—Conditioning or physical treatment of the material to be shaped by drying of powder or pellets
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
Abstract
The invention relates to a devolatilization method and equipment of a thermoplastic elastomer; directly feeding the water colloidal particles subjected to vibration dewatering into a conical centrifugal dryer of a primary drying section for devolatilization, feeding the devolatilized dry colloidal particles into a granulation section, granulating by a screw extruder, and then feeding into a conical centrifugal dryer of a secondary drying section for further drying; the temperature of the hot drying air is 40-120 ℃, and the air quantity is 10-600L/s; the extrusion temperature of the screw extruder is 100-200 ℃, and the extrusion pressure is 1-10 MPa; the conical centrifugal dryer is also provided with a hot air pipe, an air outlet, a cleaning port and a liquid level tank; the method has the advantages of short process flow, small occupied area of equipment, thorough devolatilization, stable index control, low gel content of products, high bulk density and the like.
Description
Technical field
The present invention relates to a kind of post processing devolatilization method and equipment of thermoplastic elastomer (TPE), main involving vibrations dewater, one-level drying, granulation, the operation such as secondary drying.
Background technology
Thermoplastic elastomer (TPE) (TPE) is a kind of macromolecular material between rubber and resin, and it not only can replace partial rubber, and plastics can also be made to obtain modification.The dual property of the rubber that thermoplastic elastomer (TPE) has and plastics and broad characteristic, make it in rubber industry, be widely used in various industrial goods such as the manufacture everyday articles such as rubber overshoes, adhesive plaster and sebific duct, adhesive tape, adhesive tape, offset plate, glue part and adhesive etc.Meanwhile, thermoplastic elastomer (TPE) also can replace rubber to be used in the interchangeable heat plastic resins such as PVC, PE, PP, PS even the modification aspect of the engineering plastics such as PU, PA, CA in a large number.
Thermoplastic elastomer (TPE) kind continues to bring out, and at present, oneself develops into the large class of l0 more than 30 kind.The TPE of suitability for industrialized production has in the world: phenylethylene (SBS, SIS, SEBS, SEPS), olefines (TP0, TPV), diene class (TPB, TPI), polyvinyl chloride-base (TPVC, TCPE), ammonia ester class (TPU), ester class (TPEE), amide-type (TPAE), Organic fluoride class (TPF), silicone based and vinyl etc.
Method of producing thermoplastic elastomer can be divided into polymerization and blended two large classes.Polymerization is main in polymerisation in solution mode, blended mainly based on rubber and resin machinery blending method.
Polymerisation in solution production process mainly comprises feed purification, polymerization and glue post processing three parts.Polymerization technique can adopt interval or continuous polymerization technique, and the method that glue post processing removes moisture and residual solvent (devolatilization) is divided into conventional wet devolatilization method and dry method devolatilization method substantially.Dry method devolatilization method is still in the development phase, reports there are no industrialization.
Conventional wet devolatilization main flow following (shown in accompanying drawing 1): in the micelle of thermoplastic elastomer (TPE) glue by formation after elutriation cohesion, containing 0.01 ~ 0.03%(m/m) solvent naphtha and 50 ~ 90%(m/m) water, this micelle by surge tank, 1# vibrating-dewatering screen, wash and stir tank, the process of 2# vibrating-dewatering screen after, the volatile matter in micelle is down to 30 ~ 50%(m/m); The micelle of being come by 2# vibrating-dewatering screen enters extruding-desiccation machine, under uniform temperature and pressure condition, carry out extrusion dehydration, and the polymer extruded is cut into little micelle by the cutting knife rotated with axle, and the volatilization in little micelle is divided into 5 ~ 15%(m/m); Little micelle enters expansion-exsiccation machine, under the condition of high temperature, high pressure after expansion-exsiccation machine extrusion expansion, sizing material is extruded and flash distillation from expansion drying machine nozzle, and be cut into the micelle of certain particle diameter by the pelleter that inverter motor independent on eccentric shaft drives, its volatile matter reaches 1%(m/m simultaneously); Under hot blast effect, micelle, through 1# vibrated fluidized bed, 2# vibrated fluidized bed, 3# vibrated fluidized bed, removes the volatile matter be not flashed when expansion-exsiccation machine is extruded, and makes volatile matter control to 0.5%(m/m) within; The material that drying is disposed enters grater, and the product of broken caking, then enters packaged unit of weighing.Find in practical application, it is long to there is technological process in conventional wet devolatilization method, and equipment takes up an area many, and devolatilization is thorough, volatile matter norm controlling is unstable, the problems such as product gel content is high, bulk density is little.
Summary of the invention
The object of this invention is to provide a kind of devolatilization method and equipment of thermoplastic elastomer (TPE).Adopt wet method devolatilization method, involving vibrations screens out the operations such as water, one-level drying, granulation, secondary drying.It is short that the method has technological process, and equipment takes up an area few, and devolatilization is thorough, volatile matter norm controlling is steady, the features such as product gel content is low, bulk density is large.
As the conical centrifuge drying machine of nucleus equipment of the present invention, comprise exterior protection cover and embedded with conical screen centrifuge, compass screen surface is densely covered with 20 order ~ 80 object sieve apertures.Be provided with active bearings in protective cover tail shell middle part, active bearings is by power-equipment driven rotary, and little sieve mouth is connected with active bearings.Be provided with driven bearing in protection capouch inner casing middle part, shaker screen mouth is connected with driven bearing.Dryer inner is formed primarily of 3 regions, the dry micelle collecting region namely surrounded by protection capouch shell and protection capouch inner casing, the centrifugal drying district that compass screen surface inside is surrounded, the aqueous vapor accumulation region that protective cover side shell and compass screen surface outside are surrounded.
Dryer inner is provided with warm-air pipe, and warm-air pipe inserts from protection capouch shell middle part along screen centrifuge axis, and to little sieve mouth place, warm-air pipe outer end connects air-heater, and air-heater blasts hot blast in warm-air pipe, and inner end is closed by warm-air pipe underseal.Warm-air pipe sidewall is provided with hot blast hole, for ensureing that each hot blast hole wind-force is suitable, hot blast hole arranging density reduces in direction outward gradually from warm-air pipe inner end, or aperture, hot blast hole reduces in direction outward gradually from warm-air pipe inner end.
Protective cover side shell is provided with exhaust outlet, can discharge superfluous water gas mixture in aqueous vapor accumulation region in time.Be provided with wind pressure balancer in little sieve mouth outside, wind pressure balancer, to the blowing of screen centrifuge inside, to balance little sieve mouth place blast, prevents hot blast to run off from this, and ensures that the charging of glue grain is smooth.
Be provided with clean-up port bottom the shell of protective cover side, inside is level tank, and liquid level is controlled by external draining valve and water pump, and discharge liquid and reuse as recirculated water, clean-up port is used for periodic cleaning level tank, particularly clears up the micelle granule thrown away from sieve aperture.
Containing 80% ~ 85%(m/m in the thermoplastic elastomer (TPE) glue that solution polymerization obtains) low boiling point solvent and 15% ~ 20%(m/m) polymer.In elutriation cohesion workshop section, after low boiling point solvent is removed by boiling, the pore structure micelle loosened very much, containing 50% ~ 90%(m/m in these pore structures) water and a small amount of solvent.First this micelle is sent into the vibration workshop section that dewaters and is carried out preliminary devolatilization, makes volatile matter content be down to 30% ~ 50%(m/m).
The vibration glue grain that workshop section sends here that dewaters is admitted to one-level drying section, start wind pressure balancer, dry to little sieve aperture, glue grain to enter after conical centrifuge sieves inner centrifugal drying district along feed well from little sieve mouth, actuating motor, drive screen centrifuge to make High Rotation Speed along its axis by active bearings, meanwhile, start air-heater and blast hot blast in warm-air pipe.Hot blast, from the hot blast hole blowout warm-air pipe, forms certain blast to compass screen surface, and the blast movement locus of component to regulation and control glue grain that be vertical along compass screen surface and tangential direction has certain effect, and in addition, hot blast plays acceleration drying functions to glue grain.Glue grain againsts compass screen surface under centrifugal force and hot wind acting in conjunction, high-speed screw circular motion is made around axis, and move to shaker screen mouth, in its surface and internal pore structure, contained volatile matter is centrifuged and throws away or blown out by hot blast, the air-water mixture formed passes through sieve aperture, enter aqueous vapor accumulation region, a part is discharged by exhaust outlet, and another part is condensed to be collected among level tank.
By controlling screen centrifuge rotating speed, hot blast temperature and air quantity, glue grain is made in centrifugal drying district, to stop the long enough time and reach drying purpose.Dry micelle throws away along shaker screen mouth tangential direction, enters dry micelle collecting region, is collected, after the discharging opening of low spot is derived, send into prilling section by protection capouch inner casing and protection capouch shell.
At prilling section, dry micelle enters screw extruder inside by splicing funnel, extruding pelletization under uniform temperature and pressure, for preventing the adhesion between micelle, a certain amount of calcium stearate emulsion is sprayed to cutter head and micelle, moisture in emulsion can improve the volatile matter of product, and for removing this part moisture, micelle is admitted to secondary drying workshop section.In secondary drying workshop section, above-mentioned micelle, after the horizontal of similar structures or vertical drier inner drying, is sent to packing department.
At present, the volatile matter General Requirements of commercially available thermoplastic elastomer (TPE) is less than 0.5%(m/m), top grade product control at 0.2%(m/m) left and right, still higher to certain applications field, devolatilization thoroughly will not cause the correlated performance of thermoplastic elastomer (TPE) and goods thereof to decline, and impact uses.In traditional wet method devolatilization method, after extruding-desiccation machine and expansion-exsiccation machine process, the original pore structure of glue intragranular disappears, although define again certain pore structure by the flash distillation effect of volatile matter, but its pore volume and puffed degree are far away from former glue grain, and, after high temperature, HIGH PRESSURE TREATMENT, part volatile matter is sandwiched by sizing material melting and transfers inner volatile matter to, inner volatile matter is difficult to remove, even if be also difficult to volatile matter to be down to 0.2%(m/m by the process of follow-up multilevel drying workshop section) within, and technology controlling and process is difficult, index fluctuation is large.In the present invention; glue grain is in the non-crimp of conical centrifuge dryer inner; keep the initial pore structure formed; in these pore structures, contained volatile matter belongs to surface (comprising outer surface and inner surface) volatile matter substantially; remove than being easier under conical centrifuge drying machine directly processes; dry micelle volatile matter after process is generally less than 0.1%(m/m), and index fluctuation is little, technique easily controls.
In conventional wet process for devolatilization, for reducing product volatile matter, generally improve each workshop section treatment temperature and pressure as far as possible, at expansion-exsiccation machine internal temperature often close to 200 DEG C, pressure is often close to 10MPa, this rises causing the gel content of product, even occurs plasticized granule, brings adverse effect to the performance of product.In the present invention, at prilling section, only need provide matched melt temperature and extrusion pressure with thermoplastic elastomer (TPE), avoid overtemperature, superpressure phenomenon, thus reach the object reducing product gel content.
In conventional wet devolatilization method, the particle extruded by expansion-exsiccation machine is half fluffy state, and now to cutter head and spraying particles calcium stearate emulsion, the moisture in emulsion will have part to infiltrate in micelle, transfer interior table water to.Interior table water comparatively appearance water removes difficulty, will affect the devolatilization effect of product.In the present invention, after screw extruder melt pelletization, dry micelle changes the micelle of compact structure into, attachment of moisture in emulsion is in micelle outer surface, be difficult to enter micelle inside, belong to appearance water, be easy to this part water to remove after this micelle sends into secondary drying workshop section.The finished product micelle of secondary drying workshop section process directly enters packing department.Generally can 0.05%(m/m be reached by the dry micelle volatile matter after two-stage drying process) left and right.
In the certain applications field of thermoplastic elastomer (TPE), improve the processed and applied that puffed degree index is conducive to product, but inevitably improve transport and the packing cost of product.For the application that puffed degree index request is not high, manage increase bulk density then to producer reduce transport and packing cost favourable.In conventional wet process for devolatilization, finished product micelle is half puffy, and bulk density is still less than normal.In the present invention, dry micelle, through screw extruder melt pelletization, changes compact texture into, and product bulk density significantly improves, and transport and packing cost reduce.
Accompanying drawing explanation
Fig. 1 is thermoplastic elastomer (TPE) conventional wet devolatilization schematic flow sheet;
Fig. 2 is thermoplastic elastomer (TPE) devolatilization method process module figure of the present invention, and wherein module C is depicted as horizontal cone whizzer longitudinal sectional view;
Fig. 3 is horizontal cone whizzer stereogram of the present invention;
Fig. 4 is horizontal cone whizzer front view of the present invention;
Fig. 5 is horizontal cone whizzer left view of the present invention;
Fig. 6 is horizontal cone whizzer right view of the present invention;
Fig. 7 is horizontal cone whizzer top view of the present invention;
Fig. 8 is horizontal cone whizzer upward view of the present invention;
Fig. 9 is the right inside shell front view of horizontal cone whizzer protective cover of the present invention;
Figure 10 is warm-air pipe stereogram of the present invention;
Figure 11 is thermoplastic elastomer (TPE) devolatilization method process module figure of the present invention, and wherein module C is depicted as vertical conical whizzer longitudinal sectional view;
Figure 12 is vertical conical whizzer stereogram of the present invention;
Figure 13 is vertical conical whizzer front view of the present invention;
Figure 14 is vertical conical whizzer left view of the present invention;
Figure 15 is vertical conical whizzer right view of the present invention;
Figure 16 is vertical conical whizzer top view of the present invention;
Figure 17 is vertical conical whizzer upward view of the present invention;
Figure 18 is inner casing front view on vertical conical whizzer protective cover of the present invention;
Figure 19 is chuck warm-air pipe stereogram of the present invention;
Figure 20 is conical centrifuge of the present invention sieve stereogram;
Figure 21 is conical centrifuge of the present invention sieve front view;
Figure 22 is toroidal screen centrifuge stereogram of the present invention;
Figure 23 is toroidal screen centrifuge front view of the present invention;
Figure 24 is the rim of a bowl shape screen centrifuge stereogram of the present invention;
Figure 25 is the rim of a bowl shape screen centrifuge front view of the present invention.
In figure, A-elutriation cohesion workshop section, B-vibrates the workshop section that dewaters, C-one-level drying section, D-melt pelletization workshop section, E-secondary drying workshop section, F-packing department, I-dry micelle collecting region, II-centrifugal drying district, III-aqueous vapor accumulation region, 1-warm-air pipe, 2-hot blast hole, 3-hot blast, 4-protects capouch inner casing, 5-protective cover side shell, 6-exhaust outlet, 7-protective cover tail shell, 8-compass screen surface, 9-wind pressure balancer, 10-glue grain, 11-feed well, 12-active bearings, 13-level tank, 14-recirculated water, 15-water pump, 16-draining valve, 17-clean-up port, 18-secondary conical centrifuge drying machine, 19-screw extruder, 20-splicing funnel, 21-discharging opening, 22-air-water mixture, 23-sieve aperture, the driven bearing of 24-, the dry micelle of 25-, 26-protects capouch shell, 27-air-heater, the little sieve mouth of 28-, 29-shaker screen mouth, 30-seal, 31-gear (or bayonet socket), 32-locating slot, 33-warm-air pipe underseal, pipe in 35-chuck warm-air pipe, 36-chuck warm-air pipe outer tube, 37-chuck warm-air pipe outer tube underseal, 38-axis, 39-chuck warm-air pipe outer tube closedtop, the outer arm of 40-chuck warm-air pipe.
Detailed description of the invention
By reference to the accompanying drawings technical scheme of the present invention is described: as the conical centrifuge drying machine of nucleus equipment of the present invention, comprises external cylindrical protective cover and embedded with conical screen centrifuge thereof, compass screen surface 8 is densely covered with sieve aperture 23.Protective cover tail shell 7 middle part is provided with active bearings 12, and active bearings 12 is connected driven rotary with power-equipment, and little sieve mouth 28 is connected by gear 31 with active bearings 12.Be provided with driven bearing 24 in protection capouch inner casing 4 middle part, shaker screen mouth 29 is connected by locating slot 32 with driven bearing 24.Dryer inner is formed primarily of 3 regions, namely protects the dry micelle collecting region I that capouch shell 26 surrounds with protection capouch inner casing 4, the centrifugal drying district II that compass screen surface 8 inside is surrounded, the aqueous vapor accumulation region III that protective cover side shell 5 and compass screen surface 8 outside are surrounded.
Conical centrifuge dryer inner is provided with warm-air pipe 1, warm-air pipe 1 inserts from protection capouch shell 26 middle part along axis 38, and to little sieve mouth 28 place, warm-air pipe 1 outer end connects air-heater 27, air-heater 27 blasts hot blast 3 in warm-air pipe 1, and inner end is closed by warm-air pipe underseal 33.Warm-air pipe 1 sidewall is provided with hot blast hole 2, and for ensureing that each hot blast hole 2 wind-force is suitable, hot blast hole 2 arranging density reduces in direction outward gradually from warm-air pipe inner end, or aperture, hot blast hole 2 reduces in direction outward gradually from warm-air pipe inner end.
Protective cover side shell 5 is provided with exhaust outlet 6, can discharge superfluous water gas mixture 22 in aqueous vapor accumulation region in time.Little sieve mouth 28 is provided with vane type wind pressure balancer 9, and wind pressure balancer 9, to the inner blowing of conical centrifuge sieve, to balance little sieve mouth 28 place blast, prevents hot blast 3 to run off from this, and ensures the smooth of glue grain 10 charging.
Clean-up port 17 is provided with bottom protective cover side shell 5, inside is level tank 13, and liquid level is controlled by external draining valve 16 and water pump 15, discharges liquid and reuses as recirculated water 14, the micelle granule thrown away from sieve aperture 23, for periodic cleaning level tank 13, is particularly cleared up in clean-up port 17.
The thermoplastic elastomer (TPE) glue that solution polymerization obtains is after elutriation cohesion workshop section A process, and first the glue grain 10 obtained is sent into the vibration workshop section B that dewaters and vibrated and dewater, and micelle volatile matter content is down to 30 ~ 50%(m/m).
The vibration glue grain 10 that workshop section B sends here that dewaters is admitted to one-level drying section C, start wind pressure balancer 9, dry to little sieve mouth 28, glue grain 10 to enter after conical centrifuge sieves inner centrifugal drying district II along feed well 11 from little sieve mouth 28, actuating motor, drive conical centrifuge to sieve by active bearings 12 and make High Rotation Speed along its axis 38, meanwhile, start air-heater 27 and blast hot blast 3 to warm-air pipe 1.Glue grain 10 againsts compass screen surface 8 under centrifugal force and the acting in conjunction of hot blast 3 wind-force, high-speed screw circular motion is made around axis 38, and move to shaker screen mouth 29, in its surface and internal pore structure, contained volatile matter is centrifuged and throws away or blown out by hot blast 3, the air-water mixture 22 formed is by sieve aperture 23, enter aqueous vapor accumulation region III, a part is discharged by exhaust outlet 6, and another part is condensed to be collected among level tank 13.
By controlling screen centrifuge rotating speed, hot blast 3 air quantity and temperature, glue grain 10 is made in centrifugal drying district II, to stop the long enough time and reach drying purpose.Dry micelle 25 throws away along shaker screen mouth 29 tangential direction, enters dry micelle collecting region I, is collected, derive rear feeding prilling section D from the discharging opening 21 of low spot by protection capouch inner casing 4 and protection capouch shell 26.
At prilling section D, it is inner that dry micelle 25 enters screw extruder 19 by splicing funnel 20, and extruding pelletization under uniform temperature and pressure, for removing the moisture introduced in prilling section D, micelle is admitted to secondary drying workshop section E.At secondary drying workshop section E, above-mentioned micelle, after the horizontal of similar structures or vertical drier 18 inner drying, is sent to packing department F.
This equipment body is formed by stainless steel.
Every design parameter involved in the present invention need be determined according to different material character and treating capacity, active bearings 12 rotating speed is 100 turns/and min ~ 800 turn/min; Compass screen surface 8 can be designed to the Deformational patterns such as horn mouth or the rim of a bowl; Compass screen surface 8 and axis 38 angle are 0 ° ~ 30 °, and long is 2m ~ 10m, and little sieve mouth 28 diameter is 0.05m ~ 0.5m; Sieve aperture 23 is 20 order ~ 80 orders; Hot blast 3 temperature is 50 DEG C ~ 120 DEG C, and air quantity is 10L/s ~ 600L/s; Warm-air pipe 1 caliber is 0.01m ~ 0.2m; In chuck warm-air pipe, pipe 35 caliber is 0.01m ~ 0.1m, and chuck warm-air pipe outer tube 36 caliber is 0.02m ~ 0.3m; Secondary cone whizzer volume size is 1/2 ~ 1 of one-level cone whizzer.
Conical centrifuge drying machine of the present invention also can be used in other chemical field, as the drying of polyethylene, acrylic resin equigranular particle, also can be used in food processing field, as the cleaning-drying etc. of seed.In addition, those of ordinary skill in the art can also make various distortion under the prerequisite not departing from present inventive concept.
Embodiment 1:
For horizontal cone screen centrifuge, be described in detail.
Polymerisation obtains weight average molecular weight 300,000, inlay character 30/70, contents of ethylene 16%(m/m) star-shaped sbs glue, containing 82%(m/m in glue) pentamethylene and 18%(m/m) polymer molecule.Glue, by elutriation cohesion workshop section A, after pentamethylene boiling being removed, obtains very fluffy micelle, containing 85%(m/m in these micelles) water and trace solvent.First this micelle is sent into the vibration workshop section B that dewaters and is tentatively dewatered, and makes volatile matter content be down to 51%(m/m) left and right.
The vibration glue grain 10 that workshop section B sends here that dewaters is admitted to one-level drying section C with 55kg/min conveying capacity, start pressure balancer 9, sieve mouth blowing left, glue grain 10 to enter after conical centrifuge sieves inner centrifugal drying district II along feed well 11 from little sieve mouth 28, actuating motor, drives conical centrifuge to sieve by active bearings 12 and rotates with 500 turns/min rotating speed along its axis 38, simultaneously, blast to warm-air pipe 1 hot blast 3 that temperature is 90 DEG C by air-heater 27, air quantity is 200L/s.Compass screen surface 8 and axis 38 angle are 10 °, and long is 6m, and little sieve mouth 28 diameter is 0.3m, and sieve aperture 23 is 50 orders, the long 6m of warm-air pipe 1, and internal diameter is 0.15m.Glue grain 10 is time of staying average out to 12min in centrifugal drying district II.
Dry micelle 25 throws away along shaker screen mouth 29 tangential direction, enters dry micelle collecting region I, is collected, derive rear feeding prilling section D from the discharging opening 21 of low spot by protection capouch inner casing 4 and protection capouch shell 26.
At prilling section D, it is inner that dry micelle 25 enters screw extruder 19 by splicing funnel 20, extruding pelletization under 150 DEG C and 5MPa pressure, and to cutter head and a small amount of calcium stearate emulsion of spraying particles, for removing the moisture that emulsion is brought, micelle is admitted to secondary drying workshop section E.At secondary drying workshop section E, above-mentioned micelle, after drying machine 18 inner drying of similar structures, is sent to packing department F.Secondary cone whizzer volume size is 3/4 of one-level cone whizzer.The volatilization of finished product SBS micelle is divided into 0.04%(m/m), bulk density is 0.47g/cm3.
Embodiment 2:
For vertical conical screen centrifuge, be described in detail.
It is 410,000 that polymerisation obtains weight average molecular weight, and unison 72%, 1, the 2-of a being structural content is with 1,2-polybutadiene glue between 83%, containing 84%(m/m in glue) cyclohexane and 16%(m/m) polymer molecule.Glue, by elutriation cohesion workshop section A, after cyclohexane boiling being removed, obtains very fluffy micelle, containing 75%(m/m in these micelles) water and trace solvent.First this micelle is sent into the vibration workshop section B that dewaters and is tentatively dewatered, and makes volatile matter content be down to 45%(m/m) left and right, dewater glue grain that workshop section B sends here of vibration is admitted to vertical conical whizzer inner drying in one-level drying section C.
Vertical conical whizzer, comprises external cylindrical protective cover and embedded with conical screen centrifuge.Compass screen surface 8 is densely covered with the sieve aperture 23 of certain pore size.Be provided with active bearings 12 in protective cover tail shell 7 middle part, active bearings 12 is by motor driven rotary, and little sieve mouth 28 is connected by bayonet socket 31 with active bearings 12.Protection capouch inner casing 4 middle part is provided with driven bearing 24, and shaker screen mouth 29 is connected by locating slot 32 with driven bearing 24.Dryer inner is formed primarily of 3 regions, namely protects the dry micelle collecting region I that capouch shell 26 surrounds with protection capouch inner casing 4, the centrifugal drying district II that compass screen surface 8 inside is surrounded, the aqueous vapor accumulation region III that protective cover shell and compass screen surface 8 outside are surrounded.
Conical centrifuge dryer inner is provided with chuck warm-air pipe, and chuck warm-air pipe outer tube 36 outer end is closed by chuck warm-air pipe outer tube closedtop 39, and inner end is closed by chuck warm-air pipe outer tube underseal 37.Chuck warm-air pipe inserts along axis 38, to lower sieve mouth 44 place from protection capouch shell 26 middle part.Chuck warm-air pipe outer tube 36 sidewall is provided with hot blast hole 2, air-heater 27 blasts hot blast 3 in arm 40 outside chuck warm-air pipe, suitable for ensureing each hot blast hole 2 wind-force, hot blast hole 2 arranging density reduces in direction outward gradually from chuck warm-air pipe outer tube 35 inner end, or aperture, hot blast hole 2 reduces in direction outward gradually from chuck warm-air pipe outer tube 35 inner end.Pipe 35 outer termination splicing funnel 20 in chuck warm-air pipe, inner end is near little sieve mouth 28, and little sieve mouth 28 is closed by seal 30.
Protective cover side shell 5 is provided with exhaust outlet 6, can discharge superfluous water gas mixture 22 in aqueous vapor accumulation region III in time.Clean-up port 17 is provided with bottom the shell of protective cover side, inside is level tank 13, level tank 13 liquid level is controlled by external draining valve 16 and water pump 15, the liquid of discharging reuses as recirculated water 14, the micelle granule thrown away from sieve aperture 23, for periodic cleaning level tank 13, is particularly cleared up in clean-up port 17.
The vibration glue grain 10 that workshop section B sends here that dewaters is admitted to pipe 35 in chuck warm-air pipe with 20kg/min conveying capacity, and glue grain 10 falls into little sieve mouth 28 place.Actuating motor, drive conical centrifuge to sieve by active bearings 12 and rotate with 650 turns/min rotating speed along its axis 38, meanwhile, blasting temperature by air-heater 27 to chuck warm-air pipe outer tube arm 40 is 85 DEG C of hot blasts 3, and air quantity is 300L/s.Compass screen surface 8 and axis 38 angle are 15 °, and long is 4.5m, and little sieve mouth 28 diameter is 0.25m, and sieve aperture 23 is 60 orders, chuck hot blast pipe range 4.5m, and chuck warm-air pipe outer tube 36 internal diameter is 0.18m, and in chuck warm-air pipe, pipe 35 internal diameter is 0.14m.Glue grain 10 is time of staying average out to 9min in centrifugal drying district II.
Dry micelle 25 throws away along shaker screen mouth 29 tangential direction, enters dry micelle collecting region I, is collected, derive rear feeding prilling section D from the discharging opening 21 of low spot by protection capouch inner casing 4 and protection capouch shell 26.
At prilling section D, it is inner that dry micelle 25 enters screw extruder 19 by splicing funnel 20, and extruding pelletization under 120 DEG C and 3MPa pressure, to cutter head and a small amount of calcium stearate emulsion of spraying particles, for removing the moisture that emulsion is brought, micelle is admitted to secondary drying workshop section E.At secondary drying workshop section E, above-mentioned micelle is issued to drying purpose in drying machine 18 process of similar structures, afterwards, is sent to packing department F.Secondary cone whizzer volume size is 3/5 of one-level cone whizzer.
The volatilization of finished product micelle is divided into 0.03%(m/m), bulk density is 0.58g/cm
3.
Claims (7)
1. a thermoplastic elastomer (TPE) devolatilization method, involving vibrations dewaters, dry, granulation process, it is characterized in that: vibrate devolatilization in conical centrifuge drying machine that the glue grain that dewaters directly sends into one-level drying section (C), dry micelle (25) after devolatilization enters prilling section (D), and by screw extruder (19) granulation, the conical centrifuge drying machine sending into secondary drying workshop section (E) after granulation is again interior dry further;
Dry-heat air temperature is 40 DEG C ~ 120 DEG C, and air quantity is 10L/s ~ 600L/s;
Screw extruder (19) extrusion temperature is 100 DEG C ~ 200 DEG C, extrusion pressure 1MPa ~ 10MPa.
2. profit requires to it is characterized in that the equipment that the method described in 1 adopts: conical centrifuge drying machine comprises protective cover and embedded with conical screen centrifuge thereof; Compass screen surface (8) there is sieve aperture (23), protective cover is provided with active bearings (12) and driven bearing (24), active bearings (12) is connected with little sieve mouth (28), and driven bearing (24) is connected with shaker screen mouth (29), and active bearings (12) is by power-equipment driven rotary; Little sieve mouth (28) diameter is 0.05m ~ 0.5m; Sieve aperture (23) is 20 order ~ 80 orders; Active bearings (12) rotating speed is 100 turns/min ~ 800 turn/min; Compass screen surface (8) is long is 2m ~ 10m; Compass screen surface (8) and axis (38) angle are 0 ° ~ 30 °.
3. the equipment of method employing as claimed in claim 2, is characterized in that: conical centrifuge drying machine compass screen surface (8) is horn mouth or the rim of a bowl pattern.
4. the equipment of method employing as claimed in claim 2, it is characterized in that: conical centrifuge drying machine protective cover is provided with exhaust outlet (6), clean-up port (17) is arranged at bottom, and there is level tank (13) inside.
5. as claim 2 to as described in method adopt equipment, it is characterized in that: conical centrifuge drying machine is prone configuration, warm-air pipe (1) is provided with in conical centrifuge drying machine, warm-air pipe inserts from protection capouch shell (26) middle part along axis (38), to little sieve mouth (28) place, warm-air pipe outer end connects air-heater (27), air-heater blasts hot blast in warm-air pipe, inner end is closed by warm-air pipe underseal (33), warm-air pipe sidewall is provided with hot blast hole (2), hot blast hole arranging density reduces in direction outward gradually from warm-air pipe inner end, or aperture, hot blast hole reduces in direction outward gradually from warm-air pipe inner end, warm-air pipe caliber is 0.01m ~ 0.1m.
6. the equipment of method employing as claimed in claim 5, is characterized in that: the little sieve mouth (28) of conical centrifuge drying machine is outside equipped with wind pressure balancer (9), and wind pressure balancer (9) is to the inner blowing of conical centrifuge sieve; Little sieve mouth (28) place is provided with feed well (11).
7. the equipment of method employing as claimed in claim 2, it is characterized in that: conical centrifuge drying machine is vertical structure, inside be provided with chuck warm-air pipe, chuck warm-air pipe outer tube (36) wall there is hot blast hole (2), chuck warm-air pipe outer tube (36) outer end is closed by chuck warm-air pipe outer tube closedtop (39), inner end is closed by chuck warm-air pipe outer tube underseal (37), the outer arm (40) of the upper termination chuck warm-air pipe of chuck warm-air pipe outer tube (36), air-heater (27) blasts hot blast to outside chuck warm-air pipe in arm (40); In chuck warm-air pipe, pipe (35) caliber is 0.01m ~ 0.2m, and chuck warm-air pipe outer tube (36) caliber is 0.02m ~ 0.3m.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106220798A (en) * | 2016-08-30 | 2016-12-14 | 广东众和化塑有限公司 | A kind of high melting means, high transparency SIS elastomer and preparation method thereof |
| CN110774778A (en) * | 2018-07-25 | 2020-02-11 | 株式会社宫腰 | Ink drying device |
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| SU1490404A1 (en) * | 1987-01-06 | 1989-06-30 | Казанский Химико-Технологический Институт Им.С.М.Кирова | Centrifugal drier |
| CN1465474A (en) * | 2002-09-20 | 2004-01-07 | 中国石化集团巴陵石油化工有限责任公 | Post-treatment method for styrene group thermoplastic elastomer |
| CN102190832A (en) * | 2010-03-12 | 2011-09-21 | 青岛科技大学 | Poly-1-butene elastomer material and preparation method thereof |
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| SU1490404A1 (en) * | 1987-01-06 | 1989-06-30 | Казанский Химико-Технологический Институт Им.С.М.Кирова | Centrifugal drier |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106220798A (en) * | 2016-08-30 | 2016-12-14 | 广东众和化塑有限公司 | A kind of high melting means, high transparency SIS elastomer and preparation method thereof |
| CN106220798B (en) * | 2016-08-30 | 2019-02-26 | 广东众和化塑有限公司 | A kind of high melting means, high transparency SIS elastomer and preparation method thereof |
| CN110774778A (en) * | 2018-07-25 | 2020-02-11 | 株式会社宫腰 | Ink drying device |
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| CN104339469B (en) | 2016-08-10 |
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