CN104097312A - Exhaust-driven extruder and method for producing polymer by using the extruder - Google Patents
Exhaust-driven extruder and method for producing polymer by using the extruder Download PDFInfo
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- CN104097312A CN104097312A CN201310119492.1A CN201310119492A CN104097312A CN 104097312 A CN104097312 A CN 104097312A CN 201310119492 A CN201310119492 A CN 201310119492A CN 104097312 A CN104097312 A CN 104097312A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
- B29C48/50—Details of extruders
- B29C48/505—Screws
- B29C48/625—Screws characterised by the ratio of the threaded length of the screw to its outside diameter [L/D ratio]
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/92—Measuring, controlling or regulating
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/03—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor characterised by the shape of the extruded material at extrusion
- B29C48/04—Particle-shaped
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
- B29C48/395—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die using screws surrounded by a cooperating barrel, e.g. single screw extruders
- B29C48/40—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die using screws surrounded by a cooperating barrel, e.g. single screw extruders using two or more parallel screws or at least two parallel non-intermeshing screws, e.g. twin screw extruders
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
- B29C48/50—Details of extruders
- B29C48/505—Screws
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
- B29C48/50—Details of extruders
- B29C48/505—Screws
- B29C48/535—Screws with thread pitch varying along the longitudinal axis
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
- B29C48/50—Details of extruders
- B29C48/505—Screws
- B29C48/55—Screws having reverse-feeding elements
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
- B29C48/50—Details of extruders
- B29C48/68—Barrels or cylinders
- B29C48/681—Barrels or cylinders for single screws
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
- B29C48/50—Details of extruders
- B29C48/76—Venting, drying means; Degassing means
- B29C48/765—Venting, drying means; Degassing means in the extruder apparatus
- B29C48/766—Venting, drying means; Degassing means in the extruder apparatus in screw extruders
- B29C48/767—Venting, drying means; Degassing means in the extruder apparatus in screw extruders through a degassing opening of a barrel
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F220/00—Copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and only one being terminated by only one carboxyl radical or a salt, anhydride ester, amide, imide or nitrile thereof
- C08F220/02—Monocarboxylic acids having less than ten carbon atoms; Derivatives thereof
- C08F220/10—Esters
- C08F220/12—Esters of monohydric alcohols or phenols
- C08F220/14—Methyl esters, e.g. methyl (meth)acrylate
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C2948/00—Indexing scheme relating to extrusion moulding
- B29C2948/92—Measuring, controlling or regulating
- B29C2948/92504—Controlled parameter
- B29C2948/92704—Temperature
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
- Extrusion Moulding Of Plastics Or The Like (AREA)
Abstract
The invention discloses an exhaust-driven extruder and a method for producing a polymer by using the extruder. The exhaust-driven extruder comprises a barrel, a screw shaft and screw threads hovering on the screw shaft. One end of the barrel is provided with a feed inlet; a devolatilization port, a main material outlet and a residual material outlet are sequentially arranged from the feed inlet to the other end of the barrel; the screw shaft is inserted in the barrel; the screw threads comprise forward screw threads and reverse screw threads; the forward screw threads are arranged between the feed inlet and the main material outlet, and the reverse screw threads are arranged between the residual material outlet and the main material outlet. The invention can be used for the preparation of polymers, and can effectively avoid the problems of monomer leakage and material adhesion to sealing part of the shaft, therefore the extruder can running stably and continuously for a long term. The invention solves the problems of shaft sealing and material packing of the rotary screw part, when a polymer solution containing a large amount of volatile components enters into the exhaust-driven extruder for devolatilization, so that the production device can stably run for a long time.
Description
Technical field
The present invention relates to the vented extruder using when continuous polymerization technique is produced (methyl) acrylic polymer, and use the method for this device preparation (methyl) acrylic polymer (PMMA).
Background technology
The performances such as it is high, ageing-resistant that poly-(methyl) acrylic polymer has light transmittance, shock-resistant, are widely used in LCD, and plasma shows, lamp box advertisement, optical fibre illumination, optical mirror slip, the fields such as fiber optic communication.
The production technology of poly-(methyl) acrylic polymer adopts suspension polymerisation and solution polymerization process more.Suspension method and solwution method, owing to all there is solvent or decentralized medium, make all to contain a small amount of little molecule (1-3% left and right) in its final products, and this optical property on PMMA has been brought serious impact.A small amount of small molecule solvent can cause in resin sends out mist phenomenon, causes the light transmission of resin to decline.Simultaneously, be present on a small quantity the little molecule (as solvent etc.) in poly-(methyl) acrylate, because micromolecular transition process is inevitable, can cause the surface of plastic products form small defect or form stress, finally also can cause the distortion of optical property.Therefore, optical goods as high-grade in LGP, diffuser plate etc., adopt poly-(methyl) acrylate that substance law is produced to prepare more.
But polymerisation in bulk also exists following shortcoming: 1) fuel factor is relatively large, auto-acceleration effect causes product to have bubble, variable color, and temperature control when serious, causes implode, and product difficulty up to standard is strengthened; 2) because system viscosity constantly increases with polymerization, mix and the difficulty of conducting heat, sometimes also there will be " gel effect " to cause rate of polymerization automatically to be accelerated, if control improperly, will cause implode; 3) molecular weight of product distribution is wide, unreacted monomer very obstinate, products machinery degradation etc.
Therefore in industrial processes, normally first make monomer in polymerization reaction kettle, carry out prepolymerization, through prepolymerization, obtain the reactant mixture containing a certain amount of polymer.The mixture of (methyl) acrylic polymer poly-by containing and unreacted (methyl) acrylate monomer takes out continuously from reactor, enters in vented extruder.Extruder inside is decompression state, and unpolymerized volatile monomers is discharged, and is gathered (methyl) acrylic polymer.
The material of general screw-type extruder is to enter extruder by screw rod root, under the conveying effect of screw rod, to the end of screw rod, advances, and finally from the outlet of screw rod end, extrudes.But when continuous bulk polymerization reacts, from prepolymerization still, enter the mixture for polymer and monomer of vented extruder, wherein contain a large amount of unreacted monomers, and the viscosity of material is lower, therefore easily causes material in leakage and the accumulation of screw shaft sealing.
While using vented extruder, for fear of material, at screw shaft, seal the accumulation at position and the leakage of monomer, to having relatively high expectations of the shaft sealing of screw rod.Patent CN200410081147 provides a kind of employing Wilson seal, and near sealing side, is being provided with the vented extruder of gas introduction port, to avoid leakage and material in the accumulation at sealing position.While adopting Wilson seal, in order to prevent the leakage of axle gas under High Rotation Speed, needing increases the pressure on sealing contact interface, but the frictional heating problem producing therefrom is but difficult to solve.
Summary of the invention
The object of this invention is to provide a kind of vented extruder and use this extruder to manufacture the method for polymer, the above-mentioned defect existing to overcome prior art.
Vented extruder of the present invention, comprise cylindrical shell, screw shaft and the screw thread spiraling on described screw shaft, it is characterized in that: one end of described cylindrical shell is provided with charging aperture, from charging aperture to the other end of described cylindrical shell, be provided with successively devolatilization mouth, main material outlet and salvage stores outlet, described screw shaft is inserted in described cylindrical shell, described screw thread consists of forward screw thread and reverse thread, described forward screw thread is arranged on charging aperture place between main material outlet, and described reverse thread is arranged between salvage stores outlet and main material outlet;
Term " forward screw thread, reverse thread ", refers to, the screw thread that direction of rotation is contrary, and forward screw thread is for turning clockwise, and reverse thread is for being rotated counterclockwise, on the contrary forward screw thread is for being rotated counterclockwise, and reverse thread is for turning clockwise.
Vented extruder of the present invention can be for the preparation of polymer, especially can be for the preparation of poly-(methyl) acrylic polymer.
The scheme that the present invention adopts is the entrance of vented extruder material to be located to the end of screw rod, and the outlet of material is located at the position near screw rod root.Vented extruder is connected by sealing flange with prepolymerization still, does not need like this to consider that screw rod rotates the movable sealing problem causing, and only considers the static seal problem that flange connects.And static seal is more simple and reliable than movable sealing, good seal performance, this is one of advantage of the present invention.For the conveying that enters the material of extruder, can adopt the mode of left-hand thread or change the conveying that the methods such as screw rod direction of rotation realize material easily.When mass transport arrives screw rod root, by reverse thread, material is extruded by the side of extruder.Owing to being drained near the volatile monomer in screw rod root place, material viscosity is very high, the problem that does not exist monomer to leak.The screw thread of screw rod root is reverse thread simultaneously, stops full-bodied material to screw rod root motion, and is provided with defective material outlet at screw rod root place, so that the material that enters on a small quantity screw rod root is discharged.
Adopt vented extruder of the present invention, can effectively avoid monomer to leak, material is attached on the problem of shaft sealing, so can be long-term, stably continuous operation.The invention solves contain a large amount of volatile components polymer solution when entering vented extruder devolatilization, the sealing problem of the screw portion of rotation and heap buildup problem, process units can be moved steadily in the long term.
Accompanying drawing explanation
Fig. 1 is vented extruder structural representation.
The specific embodiment
Referring to Fig. 1, vented extruder of the present invention, comprises cylindrical shell 20, screw shaft 2 and the screw thread spiraling on described screw shaft 2; It is characterized in that:
One end of described cylindrical shell 20 is provided with charging aperture 1, from charging aperture 1 to the other end of described cylindrical shell 20, be provided with successively devolatilization mouth 3, main material outlet 4 and salvage stores outlet 5, described screw shaft 2 is inserted in described cylindrical shell 20, described screw thread consists of forward screw thread 6 and reverse thread 7, described forward screw thread 6 is arranged on charging aperture 1 place between main material outlet 4, and described reverse thread 7 is arranged between salvage stores outlet 5 and main material outlet 4;
Described devolatilization mouth 3 is connected with vacuum generating device;
Term " forward screw thread, reverse thread ", refers to, the screw thread that direction of rotation is contrary, and forward screw thread is for turning clockwise, and reverse thread is for being rotated counterclockwise, on the contrary forward screw thread is for being rotated counterclockwise, and reverse thread is for turning clockwise;
Preferably, on the left side and the screw shaft 2 between the right side of main material outlet 4 of described salvage stores outlet 5, be distributed with baffle plate 8;
Preferably, the quantity of described devolatilization mouth 3 is 1～3;
Preferably, the ratio of the length L 1 of the length L of forward screw thread 6 and reverse thread 7 is:
L∶L1=15∶1～20：1；
Described vented extruder can be for the preparation of polymer, especially can be for the preparation of poly-(methyl) acrylic polymer, and preparation method comprises the steps:
By the mixture of monomer and polymer, from the charging aperture 1 of described vented extruder, enter vented extruder, due to pressurized state in extruder, therefore, unconverted monomer flashes to vaporific from devolatilization mouth 3 discharges in decompression state;
Described mixture constantly travels forward by the rotary squeezing of screw shaft 2, and principal goods material is by main material outlet 4, and salvage stores is discharged by salvage stores outlet 5;
Described principal goods material and salvage stores are poly-(methyl) acrylate polymer;
The relative vacuum degree at devolatilization mouth 3 places is-0.04～-0.099MPa;
The temperature at material inlet 1 place is 200～220 ℃; The temperature at devolatilization mouth 3 places is 220～240 ℃; The temperature at main material outlet 4 places is 240～260 ℃, and the temperature that salvage stores exports 5 places is 240～260 ℃;
The time of staying of material is 3～10min;
The time of staying is defined as follows: the time of staying is that material starts to extruding the required time from extruder completely from entering extruder.
The preparation method of the mixture of described monomer and polymer is conventional, can be referring to Wen Xuming, and Chu Jiurong and Xu Chuanxiang, the research of Preparation Techniques of Low Loss Step-Index Polymer Optical Fiber. XI AN JIAOTONG UNIVERSITY Subject Index, the 2002.36 (8): the 5th page; Kaino, T., et al., Low-loss plastic optical fibers.Applied Optics, 1981.20 (17): p.2886-2888 wait the method for bibliographical information, be summarized as follows:
(methyl) acrylic ester monomer, initator and chain-transferring agent are added in polymerization reaction kettle continuously, at 120～160 ℃, react 2～8 hours, obtain the mixture of monomer and polymer;
Described methyl) acrylic ester monomer is selected from (methyl) alkyl acrylate of carbon number 1～18 alkyl, is preferably more than one in (methyl) methyl acrylate, (methyl) ethyl acrylate, (methyl) n-butyl acrylate, (methyl) 2-EHA or (methyl) octadecyl acrylate;
In the mixture of described monomer and polymer, the weight content of monomer is 30～70%;
Described initator has no special requirements, and all azo compound and peroxide that can cause radical polymerization all can be used.Initator can be used alone, also use capable of being combined.Preferred initator is for being the initator of 30 seconds～30 minutes in polymeric reaction temperature half-life, and preferred initator is azodiisobutyronitrile, ABVN, azo two methyl isobutyrates, t-butyl peroxy laurate or t-butyl peroxy acetic acid esters etc.
Described chain-transferring agent is not particularly limited, and conventional is sulfur alcohol compound, and the chloride conventional chain-transferring agents such as compound all can be used for the present invention.Preferred chain-transferring agent is sulfur alcohol compound, as n-butyl mercaptan, n-octyl mercaptan or positive lauryl mercaptan etc.
The parts by weight of each component are:
100 parts of (methyl) acrylic ester monomers
0.001～0.01 part of initator
0.05～0.5 part of chain-transferring agent
Embodiment 1
Adopt the extruder shown in Fig. 1, structural parameters are as follows:
The ratio of the length L 1 of the length L of forward screw thread 6 and reverse thread 7 is: L: L1=15: 1;
The composition mass fraction of raw material
96 parts of methyl methacrylates (MMA)
4 parts of methyl acrylates (MA)
0.2 part of n-butyl mercaptan
The total amount of azo two methyl isobutyrate 30ppm(based on MMA and MA)
The total amount of di-tert-butyl peroxide 15ppm(based on MMA and MA)
The feedstock composition of above proportioning is dropped in polymerization reaction kettle continuously, set 125 ℃ of polymeric reaction temperatures, 5 hours time of staying,
Reacted monomer and polymeric blends out have the tubular reactor of static mixer to continue reaction by measuring pump by interior from polymeric kettle, 185 ℃ of pipe reaction actuator temperatures, obtain the mixture of reacted monomer and polymer, the weight content of monomer is 70%;
By tubular reactor, enter vented extruder, the temperature of material inlet 1 is 200 ℃, and the temperature at devolatilization mouth 3 places is 220 ℃; The temperature at main material outlet 4 places is 260 ℃, and the temperature that salvage stores exports 5 places is 260 ℃;
Near the be made as-0.06MPa of relative vacuum degree of the devolatilization mouth of material inlet side, away from the be made as-0.097MPa of relative vacuum degree of the devolatilization mouth of material inlet side.Material is extruded after pelletizing by extruder, can obtain methacrylate copolymer.
In vented extruder, the time of staying of material is 3min;
Adopt the method for the mensuration > > regulation of < < GB/T2410-2008 transparent plastic light transmittance and mist degree to detect, result is as follows:
The polymer of gained after testing light transmittance is 92%, mist degree 0.3%, and appearance transparent, foreign, without xanthochromia.
Embodiment 2
Adopt the extruder shown in Fig. 1, structural parameters are as follows:
The ratio of the length L 1 of the length L of forward screw thread 6 and reverse thread 7 is: L: L1=20: 1;
The composition mass fraction of raw material
Methyl methacrylate 98
Butyl acrylate 2
Positive hexyl mercaptan 0.2
Tert-butyl hydroperoxide 3,5,5-trimethyl is the total amount of ester 100ppm(based on MMA and BA)
The feedstock composition of above proportioning is dropped in polymerization reaction kettle continuously, set 140 ℃ of polymeric reaction temperatures, 2 hours time of staying.In reacted polymeric blends, the weight content of monomer is 30%;
From polymeric kettle, out by measuring pump, enter vented extruder, the temperature of material inlet 1 is 200 ℃, and the temperature at devolatilization mouth 3 places is 220 ℃; The temperature at main material outlet 4 places is 250 ℃, and the temperature that salvage stores exports 5 places is 250 ℃;
Near the be made as-0.04MPa of relative vacuum degree of the devolatilization mouth of material inlet side, away from the be made as-0.097MPa of relative vacuum degree of the devolatilization mouth of material inlet side.Material is extruded after pelletizing by extruder, can obtain methacrylate copolymer.
The time of staying of material is 10min;
Adopt the method for the mensuration > > document specifies of < < GB/T2410-2008 transparent plastic light transmittance and mist degree to detect, result is as follows:
The polymer of gained after testing light transmittance is 93%, mist degree 0.3%, and appearance transparent, foreign, without xanthochromia.
Claims (10)
1. vented extruder, is characterized in that, comprises cylindrical shell (20), screw shaft (2) and the screw thread spiraling on described screw shaft (2), it is characterized in that: one end of described cylindrical shell (20) is provided with charging aperture (1), from charging aperture (1) to the other end of described cylindrical shell (20), be provided with successively devolatilization mouth (3), main material outlet (4) and salvage stores outlet (5), described screw shaft (2) is inserted in described cylindrical shell (20), described screw thread consists of forward screw thread (6) and reverse thread (7), described forward screw thread (6) is arranged on charging aperture (1) and locates between main material outlet (4), described reverse thread (7) is arranged between salvage stores outlet (5) and main material outlet (4).
2. vented extruder according to claim 1, is characterized in that, described devolatilization mouth (3) is connected with vacuum generating device.
3. vented extruder according to claim 1, is characterized in that, in described salvage stores outlet (5)
Left side and the screw shaft (2) between the right side of main material outlet (4) upper, be distributed with baffle plate (8).
4. vented extruder according to claim 1, is characterized in that, the quantity of described devolatilization mouth (3) is 1～3.
5. according to the vented extruder described in claim 1～4 any one, it is characterized in that, the ratio of the length L 1 of the length L of forward screw thread (6) and reverse thread (7) is: L: L1=15: 1～20:1.
6. according to the application of the vented extruder described in claim 1～5 any one, it is characterized in that, for the preparation of polymer.
7. the application of vented extruder according to claim 6, is characterized in that, for the preparation of poly-(methyl) acrylic polymer.
8. application according to claim 7, is characterized in that, comprises the steps:
By the mixture of monomer and polymer, from the charging aperture of described vented extruder, enter vented extruder, unconverted monomer flashes to vaporific from the devolatilization mouth discharge in decompression state;
Described mixture constantly travels forward by the rotary squeezing of screw shaft, and principal goods material is discharged by main material outlet, and salvage stores is discharged by salvage stores outlet;
Described principal goods material and salvage stores are poly-(methyl) acrylate polymer.
9. application according to claim 8, is characterized in that, the relative vacuum degree at devolatilization mouth place is-0.04～-0.099MPa.
10. according to the application described in claim 7～9 any one, it is characterized in that, the temperature at material inlet place is 200～220 ℃; The temperature at devolatilization mouth place is 220～240 ℃; The temperature in principal goods material exit is 240～260 ℃, and the temperature in salvage stores exit is 240～260 ℃, and the time of staying of material is 3～10min, and in the mixture of described monomer and polymer, the weight content of monomer is 30～70%.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201310119492.1A CN104097312A (en) | 2013-04-08 | 2013-04-08 | Exhaust-driven extruder and method for producing polymer by using the extruder |
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| CN201310119492.1A CN104097312A (en) | 2013-04-08 | 2013-04-08 | Exhaust-driven extruder and method for producing polymer by using the extruder |
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Cited By (3)
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| CN109006893A (en) * | 2018-08-14 | 2018-12-18 | 范勤荣 | Rice cake makes vending machine automatically |
| CN111887162A (en) * | 2020-08-11 | 2020-11-06 | 龙岩市万家兔业发展有限公司 | Efficient fattening breeding device for rabbits and breeding method thereof |
| CN114272878A (en) * | 2021-12-29 | 2022-04-05 | 万华化学集团股份有限公司 | Devolatilization and feeding two-in-one device, solution polymerization device and polymerization method |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1038051A (en) * | 1988-05-27 | 1989-12-20 | 罗迪阿公司 | Pressing method and single, double or multiple-screw extruder |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109006893A (en) * | 2018-08-14 | 2018-12-18 | 范勤荣 | Rice cake makes vending machine automatically |
| CN109006893B (en) * | 2018-08-14 | 2021-06-01 | 范勤荣 | Rice cake automatic making and selling machine |
| CN111887162A (en) * | 2020-08-11 | 2020-11-06 | 龙岩市万家兔业发展有限公司 | Efficient fattening breeding device for rabbits and breeding method thereof |
| CN114272878A (en) * | 2021-12-29 | 2022-04-05 | 万华化学集团股份有限公司 | Devolatilization and feeding two-in-one device, solution polymerization device and polymerization method |
| CN114272878B (en) * | 2021-12-29 | 2024-02-13 | 万华化学集团股份有限公司 | Devolatilization feeding two-in-one device, solution polymerization device and polymerization method |
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