CN1050087C - Direct extruding shaping method for thermoplastic resin - Google Patents
Direct extruding shaping method for thermoplastic resin Download PDFInfo
- Publication number
- CN1050087C CN1050087C CN93106783A CN93106783A CN1050087C CN 1050087 C CN1050087 C CN 1050087C CN 93106783 A CN93106783 A CN 93106783A CN 93106783 A CN93106783 A CN 93106783A CN 1050087 C CN1050087 C CN 1050087C
- Authority
- CN
- China
- Prior art keywords
- thermoplastic resin
- resin
- monomer
- extrusion
- shaping method
- Prior art date
- Legal status (The legal status 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 status listed.)
- Expired - Fee Related
Links
Images
Abstract
The present invention relates to a direct extrusion forming manufacturing method for thermoplastic resin, which is characterized in that a thermoplastic resin solution with resin in a containing quantity of 20 to 98%(by weight) is loaded into a devolatilizing device, and volatile ingredients of the thermoplastic resin are pumped from the devolatilizing device to a main material conveying pipe after devolatilized by the devolatilizing device. The tail end of the main material conveying pipe is divided into at least more than two branches, and at least one branch in the two branches is connected with a resin extrusion forming device to extrude and form a manufactured product; in addition, at least the other branch is connected with a pressure adjusting device to adjust the pressure and the flow rate of the thermoplastic resin conveyed to the thermoplastic resin extrusion forming device, and thus, the present invention has the advantages of manufacturing process simplification and extrude forming manufactured product quality improvement.
Description
The invention relates to a kind of manufacture method of directly in polymerization (polymerization) process, carrying out thermoplastic resin extrusion molding (extrusion), be meant especially and can add a pressure regulation device and at least one resin extrusion molding device, with the manufacture method of the manufacture process of simplifying the thermoplastic resin extrusion molding in this manufacture process.
At present as plastic plate; plastic tube; plastic sheeting; in the manufacture process of thermoplastic resins such as abnormity extruded product; generally all be to extrude slivering by the preliminary thermoplastic resin of polymerization and devolatilization process gained such as (devolatilization) through a line material extrusion device (strand extruder) earlier; then through the but cooling procedure of system of water cooling system or air cooling; be cut into little plastic pellet by pelleter again; and use the particle diameter screening machine to be screened; then just the plastic pellet (pellets) of gained is deposited to storage tank via induction system; by the time desire plate squeezing; when squeezing pipe or film forming, in storage tank, take out plastic pellet again with the moulding above-mentioned material.With plastics extrusion boards such as polymethyl methacrylate (polymethyl methacrylate), polystyrene (polystrene) plates is example, plastic pellet from the storage tank taking-up, also must deliver to mixer earlier and add auxiliary material and colorant, and use the drier removal moisture drying to remove contained steam in the plastic raw materials, and then feeding is to the hopper of main plate squeezing machine, utilize its screw rod heating and extruding and fusion, thereafter (for example T pattern head T-Die) extrudes into plate with cylinder plate squeezing machine through suitable die head again.
Above-mentioned plastic raw materials extrusion molding manufacture process has following several shortcomings at least:
One, in this manufacture process, the plastic raw materials of polymerization and devolatilization gained must be earlier through cooling, pelletizing, conveying, storage, then again batching, dry, melt extrude, to make the material of various types, it is not only loaded down with trivial details, and the aforementioned complicated apparatus of whole manufacture process palpus process system, parameter is many and wayward, as long as wherein there is an appliance arrangement to go wrong, just can incur loss through delay the manufacture process of its back segment.In addition, plastic pellet has dust mostly and forms and harmful operating personnel's health in pipeline is carried or during batching.
Two, must use the storage tank that designs through suitably, to guarantee the quality during plastic pellet is deposited in it.
Three, cooling, pelletizing, conveying, storage, and dry, extrude the investment of equipment such as fusion, the dry sound that is produced, spent electric energy, heat energy, problems such as the waste gas that its process produced in addition, waste water all are the unavoidable shortcomings of above-mentioned traditional manufacture process.
Four, in above-mentioned manufacture process,,, cause the thermoplastic resin variable color so may cause thermoplastic resin partly to decompose deterioration because heating (just has more the program that one screw rod extruded) often.
For overcoming these shortcomings, just above-mentioned manufacture process must be simplified, just omit cooling, pelletizing, conveying, storage, and dry, numerous and diverse intermediate steps such as melt extrude, carry out forming process and directly the melting thermoplastic resin of polymerization and volatilization back gained is delivered to thermoplastic resin shaped device (for example plate squeezing machine).Yet this manufacture process of simplifying in the present problem that technological phase ran into is, with the plastics extrusion board is example, when the melting thermoplastic resin of gained is directly delivered to the plate squeezing mechanism plate behind polymerization and the devolatilization, because the flow with devolatilization groove pumps hot moldable resin is wayward, therefore also be difficult to obtain to pressure stable and flow by the thermoplastic resin that it pumped, increase plate squeezing die head or the plate squeezing machine difficulty unstability in operation control simultaneously; And,,, then will cause prepared plastic plate to form ripple, so that can't obtain the plastic plate of surfacing, thickness homogeneous because of improper its mass flow discrepancy that makes of operation control if thermoplastic resin is when flowing out plate squeezing machine discharging opening.
Because traditional plastic shaping process exists aforementioned various shortcoming and technical difficulty, therefore, the present invention proposes a kind of simplification manufacture process of thermoplastic resin extrusion moulding product, it can omit cooling, pelletizing, carry, store, and it is dry, extrude the numerous and diverse intermediate steps such as fusion and the waste of the energy, and the thermoplastic resin extrusion molding apparatus of directly the melting heat moldable resin of polymerization and volatilization gained being delivered to various types carries out forming process, and can overcome and wave the unsettled technical problem of alopecia groove stock, and obtain the good thermoplastic resin extrusion moulding product of quality.
Therefore, main purpose of the present invention is to provide a kind of direct extrusion method of thermoplastic resin extrusion moulding product, and it can make manufacture process simplify, save the investment of equipment and the consumption of the energy, and resulting product is had fine qualities.
To achieve these goals, the invention provides the manufacture method of the direct extrusion molding of a kind of thermoplastic resin, comprising will be by aromatic vinyl base system monomer, unsaturated nitrile is a monomer, the methacrylate ester monomer is selected at least a alkenyl monomer 50-100% (weight), and the monomer mixture that can be formed with the vinyl compound 0-50% (weight) of its combined polymerization carries out monomer polymerization and obtains the thermoplastic resin solution that resin content is 20-98% (weight), be that the thermoplastic resin solution of 20-98% (weight) is sent into the devolatilization device and used and slough volatile component then with resin content, then thermoplastic resin is pumped to main conveying pipeline from the devolatilization device, directly utilizes extrusion molding apparatus to make extrusion moulding product again; The principal character of this method is: the molten thermoplastic resin is divided into two or more tributary after by main conveying pipeline, wherein has at least a tributary to be connected to extrusion molding apparatus, and has at least one tributary to be connected to pressure regulation device in addition.Adopt the inventive method can simplify the quality of process, saving manpower, the energy and raising product.
Manufacture method of the present invention compared with prior art has following advantage:
The present invention has broken through the numerous and diverse shortcoming of traditional hot moldable resin extrusion molding manufacture process, and it is simplified significantly, does not influence the quality of product simultaneously.The present invention not only can invest with the less energy, less equipment and obtain the good sheet material of thickness homogeneous, outward appearance and color, but diversification production, just can utilize the product of next step producer's demand production different types, for example connect the plastic sheet material of plate squeezing die head, film, squeeze then tubulation or connect the special-shaped extrusion die of other types of pipe die head but connect, and line material extrusion device not only possesses the pressure and the flow of thermoplastic resin material of regulation and control whole system, but and granulation to continue for next step processing use.
In addition, another advantage of the present invention is when breaking down when extrusion molding apparatus or stopping because of other reasons, only need the gear pump that flows to extrusion molding apparatus cuts out, and the thermoplastic resin that the devolatilization groove pumps still can be extruded with line material extrusion device, so not only can reduce the loss of plate squeezing raw material, and the thermoplastic resin in the devolatilization groove can not accumulated yet, and can continue to produce (if the thermoplastic resin accumulation is too of a specified duration, not only thermoplastic resin is understood deterioration, and necessary end (the shut down) of whole thermoplastic resin reaction, cause a large amount of losses.
Below in conjunction with the preferable possible embodiments of description of drawings.
Brief description of drawings:
Fig. 1 is the detail flowchart of a preferred embodiment of the present invention.
Fig. 2 is the detail flowchart of another preferred embodiment of the present invention.
Be fit to comprise plastic plate, plastic tube, plastic sheeting, special-shaped extruded product etc. with the thermoplastic resin extrusion moulding product of the inventive method manufacturing.As shown in Figure 1, the present invention is with general plastics polymerization process, for example mass polymerization (bulk polymerization), solution polymerization process (solution polymerization) etc., first polymerization obtains desired thermoplastic resin, and the monomer whose conversion ratio is at least more than 20% (weight).
Detailed explanation polymerization processing procedure of the present invention is to be monomer from unsaturated nitrile, select one or more alkenyl monomer 50～100% (weight) in aromatic vinyl base system monomer and the methacrylate ester monomer, and can with the vinyl compound 0～50% (weight) of its combined polymerization, and cooperate the rubber of 0～20% (weight) (to reach following weight % herein, all forming 100 weight % with total pan feeding is benchmark) in reactive tank, carry out body or solution polymerization, the use amount of solvent is by 0～80% (weight), and the solvent of use can be ethylo benzene, toluene, benzene, MEK, acetone, hexane, cyclohexane, dimethylbenzene, propyl benzene, isobutylbenzene, cumene, methyl alcohol, ethanol etc.Reactive tank can be continuous stirring formula reactive tank (CSTR) or plug flow reactive tank (plug flow rector) or the two and use.The reactive tank number can be one or more reactive tank, carries out polymerization in the mode of serial or parallel connection.Aforementioned unsaturated nitrile is that monomer can be acrylonitrile, Alpha-Methyl acrylonitrile, methacrylonitrile, malononitrile, anti-butene nitrile etc., and available a kind or 2 kinds; Wherein, be good with acrylonitrile usually.
And aromatic vinyl base system monomer can be: styrene, AMS, α-chlorostyrene, P-t-butylstyrene, P-methyl styrene, O-chlorostyrene, P-chlorostyrene, 2,5 dichlorostyrenes, 3,4-dichlorostyrene, P-bromstyrol, O-bromstyrol, 2,5-Dowspray 9,3,4-Dowspray 9,2,4,6-tribromo-benzene ethene, 2-isopropenyl naphthalene etc., and available more than a kind or 2 kinds; Wherein, comparatively good with styrene or AMS usually.
And the methacrylate ester monomer can be: methyl methacrylate, EMA, propyl methacrylate, butyl methacrylate, methacrylic acid benzene methyl, methacrylic acid be ester, methacrylic acid ring ester in the sixth of the twelve Earthly Branches, metering system dodecyl gallate, methacrylic acid 2-hydroxyl ethyl ester, GMA and dimethylaminoethyl methacrylate etc.; Wherein, be good with methyl methacrylate again.
Except aforementioned unsaturated nitrile is a monomer, aromatic vinyl base system monomer, outside the methacrylate ester monomer, still can add copolymerizable vinyl compound, this copolymerizable vinyl compound can be: maleimide is a monomer, for example: maleimide, N-methyl maleimide, N-isopropyl maleimide, the N-butyl maleimide, N-hexyl maleimide, N-octyl group maleimide, N-dodecyl maleimide, N-hexamethylene maleimide, N-phenylmaleimide, N-2,3 or 4-tolyl maleimide, N-2,3 or 4-ethylbenzene base maleimide, N-2,3 or 4-butyl benzene maleimide, N-2,6-tolyl maleimide, N-2,3 or 4-chlorobenzene maleimide, N-2,3 or 4-bromophenyl Malaysia acid imide etc.And other copolymerizable monomer still have: the acrylic ester monomer, anhydrous maleic acid, anhydrous methine succinic acid, anhydrous methyl-maleic acid, unsaturated carbonic acid such as anhydrous neocerotic acid and one and dihydroxy ester and its ester are monomer, ethene, propylene, butylene, the 1-amylene, 1, the 4-methylpentene, 1-ethlyene dichloride base, ethlyene dichloride fork tetrafluoroethylene, one chlorine three is fluoridized ethene, the hexafluoro propylene, butadiene, acrylic amine, isobutenyl amine, the vinyl acetate base, vinyl-nitrogen five rings ketone, vinyl nitrogen triolefin six rings, vinyl two semicarbazides, vinyl ethers, vinyl ketone, the benzo cyclopropylene, naphtho-ethene etc., and available a kind or 2 kinds, wherein, aforementioned acrylic monomer can be: methyl acrylate, ethyl acrylate, propyl acrylate, butyl acrylate, the acrylic acid benzene methyl, Hexyl 2-propenoate, cyclohexyl acrylate, dodecyl acrylate, acrylic acid 2-hydroxyl ethyl ester, glycidyl acrylate and dimethylaminoethyl acrylate etc., wherein, be good with methyl acrylate again.
And the rubber composition of aforementioned participation polymerization can be the rubber-like resin, be to be elastomeric resin at normal temperature, be polybutadiene, styrene one assorted butadiene or bulk copolymerization thing, hydrogenated styrene-assorted butadiene or bulk copolymerization thing, acrylonitrile-butadiene copolymer, neoprene, chloroprene rubber, isobutene rubber, natural rubber, ethylene-propylene rubber, ethylene-propylene-copolymerization diene rubber, haloflex, ethlyene dichloride-propylene-copolymerization diene rubber, acrylic rubber, the ethene-vinyl acetate base co-polymer, the ethylene-methyl methacrylate methyl, ethyl, propyl group, the methacrylate copolymer of shrink drier oil base or dimethyl amido ethyl etc., propylene-vinyl acetate base-methacrylate glycidol copolymer, ethylene-propylene acid methyl-methacrylate glycidol copolymer, the polyvinyl butanols, polyester elastomer, polyamide elastomer or the like, available its bridge formation thing or the thing of not building bridge, also available two or more mixture.
The mixed liquor of above-mentioned monomer or monomer and rubber is carried out polymerisation obtain the thermoplastic resin solution that the resin amount is 20～98% (weight), this thermoplastic resin solution is admitted to the devolatilization device and removes, as: devolatilization sexual elements such as residual monomer, solvent, and can obtain the molten thermoplastic resin.Being suitable for resin of the present invention is phenylethylene resin series, methacrylate ester resin etc.; Wherein phenylethylene resin series can be polystyrene (polystyrene), rubber-modified phenylethylene resin series, styrene-butadiene-acrylonitrile resin (styrene-butadiene-acrylonitrile resin), styrene-EPDM-acrylonitrile resin (styrene-EPDM-acrylonitrile resin), cinnamic acrylic ester system-acrylonitrile resin (styrene-acrylate-acrylonitrile resin), or SAN (styrene-acrylonitrile resin); And the methacrylate ester resin can be methyl methacrylate-methyl acrylate resin, methyl methacrylate-ethyl acrylate resin, or derivatives thereof, methyl methacrylate-styrene resin, methyl methacrylate-SAN, polymethyl methacrylate, or rubber-modified methacrylate ester resin
As shown in Figure 1, the general last employed terminal installation of plastics polymerization process often be a devolatilization groove 1, its can with through polymerization and must thermoplastic resin in contained residual monomer and solvent removal clean.Devolatilization groove 1 bottom is connected with main conveying pipeline 4, between devolatilization groove 1 and the main conveying pipeline 4 and be provided with a measurement gear pump 3 (gear pump), the melting thermoplastic resin facility of handling gained through devolatilization is used tricks that flux gear pump 3 is sent devolatilization groove 1 and is continued to carry by main conveying pipeline 4.
As previously mentioned, if for save necessary traditionally cooling, pelletizing, conveying, storage, and dry, extrude pilot process such as fusion, and after thermoplastic resin leaves devolatilization groove 1, by main conveying pipeline 4 it all is delivered to as plate squeezing die head or crowded pipe die head immediately, or extrusion molding apparatus such as plate squeezing machine, tube extruding machine, then because the measuring pump 3 of devolatilization groove 1, the pressure of wayward thermoplastic resin material and flow, this will influence the stability of thermoplastic resin material pressure and flow in the extrusion molding apparatus, and then cause the products obtained therefrom quality impure.Therefore, in the present invention, main conveying pipeline 4 ends just are divided into the tributary more than two at least.According to a preferred embodiment of the present invention, as shown in Figure 1, be that thermoplastic resin stream is divided into three tributaries, just the tributary 10,10 ' and 11.Tributary 10,10 ' is to be connected to extrusion molding apparatus 50,50 ' so that directly thermoplastic resin is carried out the extrusion molding process.Yet in order to control and regulate extrusion device 50, the pressure and the flow of thermoplastic resin in 50 ', so tributary 11 is connected to a pressure regulation device, pressure controller 52 before this pressure regulation device preferably includes a line material extrusion device 51 (strand extruder) and is installed in line material extrusion device 51, line material extrusion device 51 can be banded extruder (strand extruder) or be the direct porous dies of extrusion shape plastics, this banded extruder is single or the extruder that combines of two or many screw rods and aforementioned porous dies, and pressure controller 52 can be orifice valves (orifice), needle valve (needle valve), gate valve (gate valve) or globe valve (globevalve) etc.Because 11 inside, tributary just have the pressure that advances resin, so this line material extrusion device 51 directly replaces with a porous dies, can be provided with the banded extruder of augering screw, directly extrusion molding strip plastics as inside.In addition, as shown in Figure 2, pressure-regulating device also can be pressure controller 52 to be housed and the pipeline 11 ' that is back to devolatilization groove 1.Each tributary 10,10 ' or 11 and main conveying pipeline 4 between connecting line in, can be provided with and have the expansion joint that adapts to the ability of expanding with heat and contract with cold.Because having to adjust pressure is the line material extrusion device 51 of purpose or the setting of return line 11 ', therefore pump the pressure of thermoplastic resin when the measuring pump 3 of devolatilization groove 1, when flow increases, just can utilize pressure controller 52 to downgrade the resistance of extruding of line material extrusion device 51, with the thermoplastic resin flow that increases via tributary 11 leading line material extrusion devices 51, or lead back devolatilization groove 1 via return line 11 ' as shown in Figure 2, thereby make all the other be connected extrusion device 50,50 ' tributary 10, thermoplastic resin pressure on 10 ', flow still can be kept stable.In like manner, when the pressure, flow that pumps thermoplastic resin when devolatilization groove 1 reduces, then still increase extruding resistance, the thermoplastic resin extrusion capacity of the line material extrusion device 51 on the tributary 11 being reduced of line material extrusion devices 51 or return line 11 ' with pressure controller 52, two thermoplastic resins that are connected on the extrusion molding apparatus 50,50 ' tributary 10,10 ' in addition then, its pressure, flow still can be kept necessarily.
In the present invention, extrusion molding apparatus 50,50 ' can be any thermoplastic resin extrusion molding apparatus beyond banded extruder or the porous dies, plate squeezing die head for example, squeeze the pipe die head, film forming, special-shaped extrusion device etc., and, tributary 10,10 ' removes extrusion molding apparatus 50, outside 50 ', add screen pack 31 and proportioning device 32 before can further being included in it, gear pump for example, single screw extrusion machine (single-screw extruder) or double screw extruder (twin-screw extruder) etc., with the impurity in the filtering thermoplastic resin, and the control of thermoplastic resin pump output is fixing.So, thermoplastic resin just can pressure stable, flow is by extrusion molding apparatus 50,50 ', with the moulding plastics plate, plastic tube, film, or the moulding of special-shaped extruded product, embodiment as shown in Figure 1, extrusion molding apparatus 50,50 ' all directly is a T type plate squeezing die head 38, it can extrude into resin plate object 39, and utilize roller to adjust its thickness, because of this tributary 10,10 ' the inner pressure that has the propelling resin itself, therefore, pull die head 38 unlike as the plate squeezing machine though this T type squeezes, to have augering screw, also can make resin extrude into plate object 39 via this T type plate squeezing die head 38.
In addition, line material extruder 51 also has and produces the function that plastics are extruded bar except that can regulating tributary 10,10 ' pressure, flow simultaneously.As shown in Figure 1,52 of line material extrusion device 51 and pressure controllers are equiped with filter screen 53, quality with the material bar 54 that guarantees to be extruded by the extrusion die head of line material extrusion device 51, and the material bar of being extruded 54 is after water-cooled, granulation, and its pelletized product still can provide next step name of carrying out to plant processing (as injection moulding, extrusion molding, thermoforming etc.).
In addition, demand for the outward appearance that adapts to product, color, rerum natura etc., the present invention can add necessary additive in thermoplastic resin extrusion molding process, used additive can be lubricant, heat stabilizer, antioxidant, plasticizer, processing aid, ultra-violet absorber, light stabilizer, colorant (as dye well pigment), toner (bluing agent) filler or fire retardant, flame retardant, carbon fiber, glass fibre etc.In the present invention, main conveying pipeline 4 is before being divided into tributary 10,10 ' and 11, can be provided with the first additive injection device, and the extrusion device on each tributary 10,10 ' 50,50 ' and 32 of proportioning devices under it, two second additive injection devices are also arranged respectively.The first additive injection device comprises material storage barrel 6, measuring pump 7, it is by the road 8 and inject main conveying pipeline 4 by inlet 5, and static mixer 9 (staticmixer) is set on the main conveying pipeline 4 inlet 5 after makes the plastic raw materials composition behind the adding additive distribute more evenly.Simultaneously, the measuring pump 3 of devolatilization groove 1 and the measuring pump 7 of the first additive injection device also are provided with detector, in order to adjust the injection rate ratio of additive.In like manner, each second additive injection device comprises material storage barrel 34, measuring pump 35, pipeline 36 and inlet 33, therefore the additive for preparing in advance and deposit in the material storage barrel 34 just can utilize measuring pump 35 to be pumped to 36 injection tributaries 10 or 10 ' by the road, and utilize the static mixer of being installed between proportioning device 32 and extrusion device 50 (or extrusion device 50 ') 37 that mixing of materials is even, and then make the thermoplastic resin raw material that is mixed with additive enter extrusion device 50,50 ', with the various extrusion moulding products of moulding.
Below in conjunction with embodiment the present invention is described in further detail, and compared with comparative example.
Embodiment 1
Present embodiment is to utilize the inventive method (as shown in Figure 1) to make poly methyl methacrylate plastic plate (PMMA plate, polymethyl methacrylate), wherein the terminal installation of plastic tree polyisocyanate polyaddition process is a devolatilization groove 1, two extrusion molding apparatus 50,50 ' then are respectively T type plate squeezing die head 38, and the measuring pump 7,35 of devolatilization groove 1 and the used stock of first and second additive injection device is all reciprocating pump (reciprocating pump), and line material extrusion device 51 is a porous dies, and 52 of the pressure controllers of being installed before it are needle valve.
At first, mixed liquor 100 weight portions, ethyl benzene solvent 200 weight portions that methyl methacrylate monomer 97% (weight) and methacrylate monomer 3% (weight) are constituted and add necessary molecular weight regulator, polymerization initiator etc., to obtain polymethyl methacrylate resin content be 22% resin solution carries out after devolatilization handles through devolatilization groove 1 through reactive tank reaction, pumped out by gear pump 3, its outlet pressure is 95kg/cm
2, extrusion capacity is 750kg/hr, 250 ℃ of temperature.The poly methyl methacrylate plastic raw material before entering static mixer 9 along main conveying pipeline 4, can utilize reciprocating pump 7 with additive stearic acid (stearic acid) with flow 3.8kg/hr and 120 ℃, 96kg/cm
2Operating condition inject wherein from inlet 5, then make it methyl esters plastics and the additive of polymethyl fully be mixed again by static mixer 9.Thereafter, plastic raw materials is divided into three tributaries 10,10 ' and 11 and is imported into first and second extrusion forming device 50,50 ' and line material extrusion device 51 respectively.Line material extrusion device 51 can regulate on the one hand and stable tributary 10,10 ' in plastic raw materials flow, pressure, can be used to produce plastic strip on the other hand.With the pressure controller of needle valve as line material extrusion device 51, its aperture is 12%, makes the inlet pressure of line material extrusion device 51 be adjusted at 70～80kg/cm whereby
2Between.The temperature of line material extrusion device 51 is set in 250 ℃, and load is 200kg/hr, so can keep the pressure balance of whole system.By the strip plastics that line material extrusion device 51 is extruded, the bosh that usable temp is controlled between 50～60 ℃ is cooled off.Be cut into shot-like particle through pelleter again, just can get the poly methyl methacrylate plastic grain, use for next step reprocessing.
Plastic raw materials in the tributary 10,10 ' can inject the colorant additive with measuring pump 35 once more, and make its even mixing through static mixer 37 entering first and second extrusion molding apparatus 50,50 ' before.The operating condition of measuring pump 35 is 120 ℃ of temperature, pressure 56kg/cm
2, stock amount 150kg/hr.The extrusion temperature of first extrusion molding apparatus 50 is 240 ℃, pressure 60kg/cm
2, load is 250kg/hr, and T pattern head gap is 3.6mm, and the sheet metal thickness of being extruded is 1.8mm.The extrusion temperature of second extrusion molding apparatus 50 ' is 240 ℃, pressure 55kg/cm
2, load 300kg/hr, T pattern head gap 8mm, the sheet metal thickness of being extruded is 5mm.The sheet material that each extrusion molding apparatus is extruded can be controlled the thickness of sheet material again through the roller of three adjustable positions, the roller temperature is controlled at 90～96 ℃, and rotating speed is 1.6m/min, and then by the traction wheel traction, sheet material is steadily moved.Sheet material just can get final plastic plate goods according to the Len req severing again.
By the prepared plastic plate material of present embodiment, its sheet material thickness homogeneous, smooth surface and do not have wavyly, simultaneously outward appearance and color are also quite good.
The operating condition of table 1 embodiment 1 each unit
| First the moulding moulded device measuring pump of the second gear | |
| Temperature ℃ pressure kg/cm 2The T-shaped die gap mm thickness of slab of extrusion capacity kg/hr mm needle valve aperture % | 250 240 240 250 120 120 95 60 55 72 96 56 750 250 300 200 3.8 150 g/hr --- 3.6 8 --- --- --- --- 1.8 5 --- --- --- --- --- --- 12 --- --- |
Embodiment 2
Present embodiment is to utilize method of the present invention to make the PMMA plastic plate, but change over the operating condition of each unit as shown in table 2, its difference from Example 1 increases to 800kg/hr at devolatilization groove extrusion capacity by 750kg/hr, just increase devolatilization groove rate of discharge, whether the stability and the plastic plate quality of observing whole system pressure, flow-control keep good.Operating result shows that it is stable that the pressure of system, flow all are, and prepared plastic plate, and its surface, outward appearance, color are still quite good.
The operating condition of table 2 embodiment 2 each unit
| First the second gear pump arrangement device, 51 measuring | |
| Temperature ℃ pressure kg/cm 2The T-shaped die gap mm thickness of slab of extrusion capacity kg/hr mm needle valve aperture % | 250 240 250 120 120 120 99 62 57 75 100 58 800 250 300 250 4.0 150 g/hr --- 3.6 8 --- --- --- --- 1.8 5 --- --- --- --- --- --- 14 --- --- |
Comparative example 1
This comparative example does not adopt the pressure regulation device of line material extrusion device 51 or return duct 11 ', and two tributaries that the main conveying pipeline 4 that will be connected with devolatilization groove 1 is divided into all directly are directed at two extrusion molding apparatus 50,50 ', it still is two T type plate squeezing die heads, and, with the polymethyl methacrylate is thermoplastic resin, the moulding extrusion board.The operating condition that each unit of manufacture process (unit) sets is shown in table 3.
In this comparative example, owing to use as pressure, the flow of line material extrusion device or return line (release) pipeline of releasing, when causing the pump output of gear pump 3 of devolatilization groove 1 and pressure to change, two extrusion molding apparatus below its variable quantity directly influences, the sheet material plate face that causes whole process of production to extrude produces the phenomenon of ripple glaze even became uneven.If wherein an extrusion molding apparatus hinders when stopping for some reason, the thermoplastic resin in the devolatilization groove 1 will build up, and liquid level is raise, and cause having at last interrupt the result of polymerisation.
The operating condition of table 3 comparative example 1 each unit
Embodiment 3
| Devolatilization groove 1 first squeeze second squeeze | |
| Temperature ℃ pressure kg/cm 2Extrusion capacity kg/hr T pattern head gap mm thickness of slab mm | 250 240 240 120 95 65 60 96 750 350 400 3.8 --- 3.6 8 --- --- 1.8 5 --- |
Utilize manufacture process of the present invention to make PS plate (XPS).Mixed liquor and necessary molecular weight regulator that styrene (SM) monomer 90% (weight) and solvent 1% (weight) are constituted, the resin solution that obtains polystyrene resin containing ratio 52% through reaction is sent into devolatilization groove 1, but the molten resin only is divided into two tributaries 10,111 after leaving disengagement volatilization groove 1, be connected to first extrusion molding apparatus 50 and line material extrusion device 51 respectively, just only use an extrusion molding apparatus and a line material extrusion device to carry out the manufacturing of sheet material, and do not add any additives.The operating condition of each unit is as shown in table 4 in the manufacture process.The plastic sheet of gained still has suitable good surface appearance and color, and sheet material thickness uniformity.
The operating condition of table 4 embodiment 3 each unit
| Devolatilization groove 1 first is extruded | |
| Temperature ℃ pressure kg/cm 2The T-shaped die gap mm thickness of slab of extrusion capacity kg/hr mm needle valve aperture % | 210 205 215 74 54 56 500 225 275 --- 8 --- --- 5 --- --- --- 20 |
Claims (8)
1, the manufacture method of the direct extrusion molding of a kind of thermoplastic resin, comprising will be by aromatic vinyl base system monomer, unsaturated nitrile is a monomer, the methacrylate ester monomer is selected at least a alkenyl monomer 50～100% (weight), and can carry out monomer polymerization with the monomer mixture that the vinyl compound 0～50% (weight) of its combined polymerization is formed and obtain the thermoplastic resin solution that resin content is 20～98% (weight), be that the thermoplastic resin solution of 20～98% (weight) is sent into the devolatilization device and used and slough volatile component then with resin content, then thermoplastic resin is pumped to main conveying pipeline from the devolatilization device, directly utilizes extrusion molding apparatus to make extrusion moulding product again; The principal character of this method is: the molten thermoplastic resin is divided into two or more tributary after by main conveying pipeline, wherein has at least a tributary to be connected to extrusion molding apparatus, and has at least one tributary to be connected to pressure regulation device in addition.
2, the direct extruding shaping method of thermoplastic resin as claimed in claim 1 is characterized in that: described pressure regulation device is a porous dies.
3, the direct extruding shaping method of thermoplastic resin as claimed in claim 1 is characterized in that: described pressure regulation device is the pipeline that is back to this devolatilization device.
4, as claim 2 or the direct extruding shaping method of 3 described thermoplastic resins, it is characterized in that: described pressure regulation device also includes a pressure controller, and it can be needle valve, globe valve, gate valve or orifice valves.
5, the direct extruding shaping method of thermoplastic resin as claimed in claim 1 is characterized in that: the front end of described extrusion molding apparatus also is provided with the device of thermoplastic resin metering usefulness.
6, the direct extruding shaping method of thermoplastic resin as claimed in claim 5 is characterized in that: the device of described thermoplastic resin metering usefulness can be gear pump, single screw extrusion machine, double screw extruder.
7, the direct extruding shaping method of thermoplastic resin as claimed in claim 1 is characterized in that: described thermoplastic resin can be phenylethylene thermoplastic resin, methacrylate thermoplastic resin.
8, the direct extruding shaping method of thermoplastic resin as claimed in claim 1; It is characterized in that: the resin that described thermoplastic resin solution is contained is to be the resin after earlier rubber-modified.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN93106783A CN1050087C (en) | 1993-06-11 | 1993-06-11 | Direct extruding shaping method for thermoplastic resin |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN93106783A CN1050087C (en) | 1993-06-11 | 1993-06-11 | Direct extruding shaping method for thermoplastic resin |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1096243A CN1096243A (en) | 1994-12-14 |
| CN1050087C true CN1050087C (en) | 2000-03-08 |
Family
ID=4986393
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN93106783A Expired - Fee Related CN1050087C (en) | 1993-06-11 | 1993-06-11 | Direct extruding shaping method for thermoplastic resin |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1050087C (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102172576A (en) * | 2010-12-30 | 2011-09-07 | 安泰科技股份有限公司 | Metal powder screening device and method |
| CN102909845A (en) * | 2012-11-06 | 2013-02-06 | 安徽奥博新材有限公司 | Wood plastic door production equipment |
| CN105182715A (en) * | 2015-08-25 | 2015-12-23 | 珠海天威飞马打印耗材有限公司 | Developing agent supply container and developing agent supply method thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4013745A (en) * | 1974-06-01 | 1977-03-22 | Dynamit Nobel Aktiengesellschaft | Process for the extrusion of a plastic foil having small variations in thickness |
| JPS5911322A (en) * | 1982-07-09 | 1984-01-20 | Toray Ind Inc | Production of rubber-modified maleimide copolymer |
| US4729858A (en) * | 1985-10-18 | 1988-03-08 | Fuji Photo Film Co., Ltd. | Magnetic liquid application method and apparatus |
-
1993
- 1993-06-11 CN CN93106783A patent/CN1050087C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4013745A (en) * | 1974-06-01 | 1977-03-22 | Dynamit Nobel Aktiengesellschaft | Process for the extrusion of a plastic foil having small variations in thickness |
| JPS5911322A (en) * | 1982-07-09 | 1984-01-20 | Toray Ind Inc | Production of rubber-modified maleimide copolymer |
| US4729858A (en) * | 1985-10-18 | 1988-03-08 | Fuji Photo Film Co., Ltd. | Magnetic liquid application method and apparatus |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1096243A (en) | 1994-12-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US6613871B2 (en) | Method for reducing the polymer content of effluent during the drainage of polymer/water mixtures | |
| CA2266420C (en) | Process for producing thermoplastics | |
| US5958316A (en) | Preparation of thermoplastics | |
| US5372765A (en) | Continuous process for extrusion of thermoplastic resin | |
| US4029300A (en) | Extruder of the degassing and modification type | |
| EP0886658A1 (en) | Multi-stage process for producing heat resistant dimensionally stable polymethacrylate moulding compounds | |
| EP3019548B1 (en) | Process for the manufacturing of abs-molding compositions | |
| JPS6213968B2 (en) | ||
| US5851463A (en) | Preparation of thermoplastics | |
| US20060034962A1 (en) | Device for extruding thermoplasts | |
| EP0734826B1 (en) | Process for producing thermoplastic resins | |
| CN1050087C (en) | Direct extruding shaping method for thermoplastic resin | |
| JPH0676448B2 (en) | Method for producing modified methacrylic resin molding material | |
| EP0771827A2 (en) | Process for producing silane-modified polyolefins and extruder apparatus therefor | |
| US5708133A (en) | Process for purifying polymer | |
| JP2021137979A (en) | Kneading device | |
| KR100324986B1 (en) | Purification Method of Polymer | |
| JPS6289710A (en) | Production of methacrylic resin | |
| EP0096555A2 (en) | Rubber-modified thermoplastic resins and production thereof | |
| US20210122086A1 (en) | Extrusion method for producing a thermoplastic molding compound, and device for carrying out the method | |
| EP0316760A2 (en) | Method and apparatus for manufacturing thermoplastic materials | |
| JPS5853907A (en) | Polymerizing method of acrylic monomer | |
| WO2022259476A1 (en) | Kneading apparatus | |
| CN113912782A (en) | Preparation process of high impact polymer containing conjugated diene monomer | |
| CN107573621B (en) | PVDF (polyvinylidene fluoride) stretched film containing core-shell rubber particles |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |