WO2012137666A1 - ガラス繊維強化熱可塑性樹脂組成物ペレットの製造方法 - Google Patents

ガラス繊維強化熱可塑性樹脂組成物ペレットの製造方法 Download PDF

Info

Publication number
WO2012137666A1
WO2012137666A1 PCT/JP2012/058400 JP2012058400W WO2012137666A1 WO 2012137666 A1 WO2012137666 A1 WO 2012137666A1 JP 2012058400 W JP2012058400 W JP 2012058400W WO 2012137666 A1 WO2012137666 A1 WO 2012137666A1
Authority
WO
WIPO (PCT)
Prior art keywords
thermoplastic resin
screw
glass fiber
kneading
reinforced thermoplastic
Prior art date
Application number
PCT/JP2012/058400
Other languages
English (en)
French (fr)
Japanese (ja)
Inventor
邦紘 平田
石田　大
元一 平郡
Original Assignee
ポリプラスチックス株式会社
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by ポリプラスチックス株式会社 filed Critical ポリプラスチックス株式会社
Priority to CN201280017404.0A priority Critical patent/CN103459110B/zh
Publication of WO2012137666A1 publication Critical patent/WO2012137666A1/ja

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J3/00—Processes of treating or compounding macromolecular substances
    • C08J3/20—Compounding polymers with additives, e.g. colouring
    • C08J3/203—Solid polymers with solid and/or liquid additives
    • 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
    • B29B7/00—Mixing; Kneading
    • B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
    • B29B7/34—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices
    • B29B7/38—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary
    • B29B7/46—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with more than one shaft
    • B29B7/48—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with more than one shaft with intermeshing devices, e.g. screws
    • B29B7/482—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with more than one shaft with intermeshing devices, e.g. screws provided with screw parts in addition to other mixing parts, e.g. paddles, gears, discs
    • B29B7/483—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary with more than one shaft with intermeshing devices, e.g. screws provided with screw parts in addition to other mixing parts, e.g. paddles, gears, discs the other mixing parts being discs perpendicular to the screw axis
    • 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
    • B29B7/00—Mixing; Kneading
    • B29B7/80—Component parts, details or accessories; Auxiliary operations
    • B29B7/88—Adding charges, i.e. additives
    • B29B7/90—Fillers or reinforcements, e.g. fibres
    • 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
    • B29B9/12—Making granules characterised by structure or composition
    • B29B9/14—Making granules characterised by structure or composition fibre-reinforced
    • 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
    • B29C48/56—Screws having grooves or cavities other than the thread or the channel
    • 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
    • B29C48/57—Screws provided with kneading disc-like elements, e.g. with oval-shaped elements
    • 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
    • B29C48/585—Screws provided with gears interacting with the flow
    • 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
    • B29C48/59—Screws characterised by details of the thread, i.e. the shape of a single thread of the material-feeding screw
    • B29C48/60—Thread tops
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2367/00—Characterised by the use of polyesters obtained by reactions forming a carboxylic ester link in the main chain; Derivatives of such polymers
    • C08J2367/02—Polyesters derived from dicarboxylic acids and dihydroxy compounds

Definitions

  • the present invention relates to a method for producing glass fiber reinforced thermoplastic resin composition pellets.
  • thermoplastic resin composition pellets As a method for producing glass fiber reinforced thermoplastic resin composition pellets by mixing and kneading glass fibers with a thermoplastic resin, first, a thermoplastic resin is supplied to an extruder and the thermoplastic resin is melted. Next, glass fibers are supplied to the molten thermoplastic resin, and the thermoplastic resin and glass fibers are mixed and kneaded in an extruder. Finally, a method of cooling and granulating the mixture is common.
  • the extruder generally, a single-screw extruder and a fully meshed twin-screw extruder in the same direction (hereinafter sometimes referred to as a twin-screw extruder) are used. Compared with a single screw extruder, a twin screw extruder has higher productivity and freedom of operation, and therefore, a twin screw extruder is more preferably used for producing glass fiber reinforced thermoplastic resin pellets. .
  • the glass fiber used in the production of the glass fiber reinforced thermoplastic resin composition pellets is a monofilament having a diameter of 6 ⁇ m to 20 ⁇ m, which is bundled into about 300 to 3000 pieces and wound on a roving, or the roving has a length of 1 Cut to 4 mm (hereinafter sometimes referred to as chopped strands).
  • thermoplastic resin Since chopped glass can be used more easily, in the case of producing glass fiber reinforced thermoplastic resin composition pellets industrially, the thermoplastic resin is supplied to a twin screw extruder, and after the thermoplastic resin is melted, The most common method is to supply chopped glass from the middle of a shaft extruder, mix and knead a molten thermoplastic resin and glass fiber, extrude the mixture, and cool and solidify.
  • the productivity of the glass fiber reinforced thermoplastic resin composition pellets using the above twin screw extruder is determined by the plasticizing and mixing and kneading ability of the twin screw extruder.
  • the plasticizing ability of the twin screw extruder depends on the screw design, the torque generated by the screw, the groove depth of the screw (the difference between the outer diameter and the valley diameter of the screw), the rotational speed of the screw, and the like.
  • Patent Document 1 discloses a twin screw extruder that has a high plasticizing ability and is excellent in productivity by defining a value obtained by dividing the distance between the centers of two screws by the cube of three as a torque density.
  • the mixing and kneading ability of the twin screw extruder depends on the screw design.
  • the residence time decreased with the improvement of the plasticizing ability of the twin screw extruder. For this reason, development of a screw design having an efficient mixing and kneading ability in a short time is required.
  • studies on techniques for increasing the plasticizing ability and kneading ability of a twin-screw extruder have been conducted.
  • a monofilament bundle is used as described above. This is because, in the method of supplying glass fibers to a twin-screw extruder without forming a bundle of monofilaments, the monofilament becomes cottony, loses fluidity, and is difficult to handle.
  • the chopped strand is mixed and kneaded in a twin-screw extruder until it is fibrillated and becomes a monofilament. At the same time, the chopped strand is broken by a screw or the like until the monofilament length reaches an average of 200 ⁇ m to 800 ⁇ m.
  • the monofilament will not be defibrated, and a part or all of the chopped strand that is in the state of a monofilament aggregate (undefibrated glass fiber bundle) will be resin composition It remains in the product pellet. If some or all of the chopped strands remain in the glass fiber reinforced thermoplastic resin composition pellets, in injection molding, some or all of the chopped strands may be clogged in the gate, making injection molding impossible, or injection molding. Even if it is possible, some or all of the chopped strands are present in the molded product, resulting in poor appearance or reduced function.
  • glass fiber reinforced thermoplastic resin compositions used as parts are required to be thin and molded into complex shapes.
  • the gate nozzle of a molding machine that performs such precision molding is often 1 mm or less.
  • the presence of undefined glass fiber bundles becomes a very serious defect.
  • the present invention has been made in order to solve the above-mentioned problems.
  • the object of the present invention is to increase the productivity of glass fiber reinforced thermoplastic resin composition pellets as compared with the prior art, and to collect the monofilaments in the manufactured pellets. It is providing the manufacturing method of the glass fiber reinforced thermoplastic resin composition pellet which can make very low the probability that (un-defibrated glass fiber bundle) remains.
  • the inventors of the present invention have made extensive studies to solve the above problems.
  • the physical quantities obtained by numerical analysis such as average shear stress history, average shear strain history, specific energy, shortest particle outflow time, etc., are the number N of pellets containing undefined glass fiber bundles (per unit weight). It is found that there is no clear correlation with the number of pellets containing undefined glass fiber bundles) and the smallest value among the time integral values of shear stress applied to each glass fiber bundle derived by the particle tracking method. minimum shear stress history value T min is has been found that there is a correlation between the pellets number N containing non-fibrillated glass fiber bundles.
  • the shear stress generated in the twin screw extruder is analyzed, and when the ratio (Q / Ns) between the discharge amount Q and the screw rotation speed Ns is constant, the minimum shear stress history value T min is controlled.
  • the present inventors have found that the number N of pellets per unit amount including undefined glass fibers can be controlled. Further, even if the ratio (Q / Ns) is not constant, the number N of pellets per unit amount including undefined glass fibers can be expressed by a specific formula using the T min and (Q / Ns). I found out.
  • the screw for kneading the thermoplastic resin and the glass fiber has a screw element having a specific shape, and can produce the glass fiber reinforced thermoplastic resin composition pellets under specific conditions, thereby solving the above-mentioned problem.
  • the present invention has been completed. More specifically, the present invention provides the following.
  • thermoplastic resin pellets using a twin screw extruder provided with screws that rotate and mesh with each other, wherein the thermoplastic resin is supplied to the extruder and heated.
  • a kneading step of kneading the plasticized thermoplastic resin with a screw an extrusion step of extruding the glass fiber reinforced thermoplastic resin composition after the kneading step, and the extruded glass fiber reinforced thermoplastic resin composition.
  • the screw includes one or more reverse feed screw elements each having a flight portion in which an arcuate cutout is formed.
  • the torque density which is a value obtained by dividing the torque of the screw in the single reverse feed screw element by the cube of the inter-center distance between the engaging screws, is 11 (Nm / cm 3 ) or more,
  • Q / Ns is divided by the cube of the center-to-core distance between the engaging screws.
  • thermoplastic resin composition pellets according to (1) or (2), wherein the thermoplastic resin is composed of a polybutylene terephthalate resin.
  • thermoplastic resin pellet according to (1) or (2) wherein the thermoplastic resin is composed of a liquid crystalline resin.
  • the productivity of the glass fiber reinforced thermoplastic resin composition pellets is increased more than before, and the probability that monofilament aggregates (undefined glass fiber bundles) remain in the manufactured pellets is very high. Can be lowered.
  • FIG. 1 is a schematic diagram illustrating an example of a screw configuration of an extruder.
  • FIG. 2 is a diagram schematically illustrating a reverse feed single screw element having a flight portion in which an arcuate cutout is formed.
  • FIG. 3 is a schematic diagram showing the screw configuration of the extruder used in the examples.
  • FIG. 4 is a diagram showing a specific screw pattern used in the example.
  • FIG. 5 is a diagram showing a specific screw shape used in the example.
  • FIG. 1 is a schematic diagram illustrating an example of a screw configuration of an extruder.
  • FIG. 2 is a diagram schematically illustrating a reverse feed single screw element having a flight portion in which an ar
  • FIG. 8 shows the minimum shear stress history value (Pa ⁇ sec) independent of the Q / Ns of the extruder used in the examples, and the number of pellets in which part or all of the glass fiber bundle is not defibrated (pieces / pellet 10 kg). It is a figure which shows the relationship (correlation line).
  • FIG. 8 shows the minimum shear stress history value (Pa ⁇ sec) independent of the Q / Ns of the extruder used in the examples, and the number of pellets in which part or all of the glass fiber bundle is not defibrated (pieces /
  • FIG. 9 is a diagram showing a distribution of shear stress history values for each type of screw element.
  • FIG. 10 is a diagram showing the relationship between the discharge rate and the number of pellets containing undefined glass fibers.
  • FIG. 11 is a diagram showing the relationship between the discharge amount and the discharge resin temperature (the temperature of the resin composition discharged from the die).
  • FIG. 12 is a diagram showing an operation region (maximum discharge amount) in which no undefined glass fiber bundle remains in the manufactured pellet.
  • the manufacturing method of the glass fiber reinforced thermoplastic resin composition pellet of the present invention includes the following steps.
  • a plasticizing process in which a thermoplastic resin is supplied to an extruder and heated, kneaded and plasticized. After the plasticization step, one or more glass fiber bundles are supplied to the extruder, and the glass fiber bundles and the plasticized thermoplastic resin are screwed together with the screws while the glass fiber bundles are defibrated.
  • a pelletizing step of pelletizing the extruded glass fiber reinforced thermoplastic resin composition.
  • the production method of the present invention uses a screw having a specific screw element in the kneading step.
  • FIG. 1 shows a twin-screw extruder including a cylinder 1, a screw 2 disposed in the cylinder, and a die 3 provided at a downstream end portion of the cylinder 1.
  • FIG. 1 also shows the screw configuration of the screw 2.
  • the screw 2 includes a supply unit 20, a plasticizing unit 21, a transport unit 22, and a kneading unit 23 in this order from the upstream side. A plasticizing process is performed in the supply unit 20 and the plasticizing unit 21.
  • a kneading step is performed in the conveying unit 22 and the kneading unit 23.
  • the extrusion process is performed after the kneading section 23.
  • a pelletization process is performed after the glass fiber reinforced thermoplastic resin composition is extruded from the die
  • the cylinder 1 in which the screw 2 is disposed includes a hopper 10 for supplying a raw material such as a thermoplastic resin to the supply unit 20 and a feed port for supplying auxiliary materials such as a glass fiber bundle to the conveyance unit 22. 11 and a vacuum vent 12 having vacuuming means such as a vacuum pump for performing vacuum deaeration at a predetermined degree of vacuum.
  • thermoplastic resin supplied from the hopper 10 is transferred and melted to make a homogeneous melt.
  • thermoplastic resin will be described, and then the details of the plasticizing process until the thermoplastic resin supplied from the hopper becomes a homogeneous melt will be described.
  • thermoplastic resin The kind of thermoplastic resin is not particularly limited. Specific examples of the thermoplastic resin include polypropylene, polyacetal, liquid crystal resin, polybutylene terephthalate, polyethylene terephthalate, polyphenylene sulfide, nylon 66, and the like. Among these thermoplastic resins, the lower the viscosity, the more likely the problem of undefining the glass fiber bundle is. This is because if the viscosity is low, shear stress hardly occurs in the molten state, and the glass fiber bundle in which the monofilaments are converged is difficult to be defibrated. Examples of the low-viscosity resin include polybutylene terephthalate, liquid crystal resin, polyethylene terephthalate, and nylon 66.
  • thermoplastic tree used as a raw material is shaped into a pellet.
  • thermoplastic resin composition containing other components may be used into the pellet form.
  • the plasticizing process is performed in the supply unit 20 and the plasticizing unit 21 of the screw 2.
  • the screw element used in the supply unit 20 include a transport element made of a flight.
  • the screw element used for the plasticizing portion 21 generally include a combination of screw elements such as reverse flight, seal ring, forward kneading disk, and reverse kneading disk.
  • Supplied part 20 transfers resin pellets.
  • the supply unit 20 functions to transfer the resin pellets from the hopper 10 side to the die 3 direction side. In general, preheating by an external heater is performed as a melting preparation stage. Further, since the resin pellet is sandwiched between the rotating screw 2 and the cylinder 1, a frictional force is applied to the resin pellet to generate frictional heat. The resin pellets may start to melt due to the preheating or frictional heat. In some cases, the supply unit 20 needs to adjust the groove depth of the screw 2 and adjust the preheating temperature by a conventionally known method so that the transfer of the resin pellets proceeds smoothly.
  • the plasticizing unit 21 applies pressure to the resin pellets transferred from the supply unit 20 to melt the resin pellets.
  • the resin pellets are further transferred forward (in the direction from the hopper 10 to the die 3) while melting.
  • the kneading step After the plasticizing step, one or more glass fiber bundles are supplied to an extruder and the glass fiber bundle is defibrated and melted in the plasticizing step with the defibrated glass fibers. And knead.
  • the kneading step is performed by the conveying unit 22 and the kneading unit 23 of the screw 2.
  • a screw element used by the conveyance part 22 the element for conveyance which consists of a forward flight is mentioned, for example.
  • screw element used in the kneading part 23 the combination of screw elements, such as a reverse flight, a seal ring, a forward kneading disk, a reverse kneading disk, is common.
  • At least a part of the kneading part 22 of the screw 2 is provided with a single reverse feed screw element having a flight part in which an arc-shaped notch is formed on the outer periphery.
  • the glass fiber bundle is a chopped strand in which 300 to 3000 monofilaments are bundled.
  • chopped strands in which 1100 pieces or 2200 pieces are bundled are preferably used.
  • the diameter of the monofilament is not particularly limited, but is preferably in the range of 6 ⁇ m to 20 ⁇ m, and those having a diameter of 6 ⁇ m, 10 ⁇ m, and 13 ⁇ m are widely distributed in the market.
  • a bundle of monofilaments can be continuously fed to the twin screw extruder while roving.
  • the chopped strand from which roving is cut is easy to handle in transportation and supply to a twin screw extruder.
  • the glass fiber bundle and the molten resin introduced from the feed port 11 are conveyed to the kneading unit 23.
  • this conveyance part 22 it is an area
  • shear stress is applied to the glass fiber bundle and the molten resin.
  • the glass fiber bundle is defibrated and the monofilament and the molten resin are kneaded.
  • the glass fiber reinforced thermoplastic resin composition is extruded and how it is pelletized.
  • the glass fiber reinforced thermoplastic resin composition extruded into a rod shape from the die 3 can be cut and pelletized.
  • the cutting method is not particularly limited, and a conventionally known method can be used.
  • the discharge amount in the extrusion process corresponds to the discharge amount Q
  • the rotation speed of the screw corresponds to the rotation speed Ns.
  • ⁇ Screw element> As a conventional kneading part of a screw, a combination of screw elements such as a reverse flight, a seal ring, a forward kneading disk, and a reverse kneading disk is generally used. However, in the case of high discharge under conditions where Q / Ns is large, some glass fiber bundles are not defibrated and remain undefibrated.
  • the present invention is a production method determined by using as an index the shear stress history value received by each glass fiber bundle in the extruder.
  • the minimum shear stress history value T min is the minimum value of the shear stress history value each glass fiber bundle is subjected in a twin-screw extruder.
  • the following formula (IV) is derived based on the number of pellets including fiber glass fiber bundles.
  • the following formula (IV) is also useful in that the amount of pellets containing undefined glass fiber bundles can be studied with one formula even if the Q / Ns condition changes.
  • the quantity of the pellet containing an undefined glass fiber bundle can be examined with one numerical formula (IV).
  • the size of the twin-screw extruder is changed, it is necessary to derive the formula (IV) again.
  • a small twin screw extruder and a large twin screw extruder have different heat transfer amounts from the cylinders and heat energy applied to the molten resin. It is.
  • the screw diameter D is uniquely determined. Based on the screw diameter D, the arbitrarily determined lead length Le of the kneading part 23 of the screw, the discharge amount Q as the arbitrarily determined molding condition, and the screw rotational speed Ns, the minimum shear stress history value T min is derived.
  • the minimum shear stress history value T min can be derived using conventionally known three-dimensional flow analysis software in a twin-screw extruder. For example, it can be derived by particle tracking analysis as described in the examples.
  • the minimum shear stress history value T min is a time integration value obtained by performing time integration of shear stress.
  • the integration section is a section where shear stress is applied to the molten resin and the glass fiber bundle, and the extrusion shown in FIG. In the case of a machine, it is a section of the kneading unit 23.
  • the method for deriving the minimum shear stress history value Tmin is not particularly limited. A method of deriving using commercially available software, a method of deriving by experiment, and the like can be mentioned.
  • the number N of undefibrated pellets may be derived experimentally or using an analysis method or the like.
  • the horizontal axis is the minimum shear stress history value T min
  • the vertical axis is the number N of undefined pellets
  • a graph representing the above formula (IV) is created, thereby formula (IV) To derive.
  • Screw diameter D of the screw element vary from d1 to d2, the following equation (V) is established between the discharge amount Q M in the discharge amount Q m and a large extruder in a small extruder and, following equation (VI) is established between the screw rotation speed Ns M at a screw rotation speed Ns m and a large extruder a small extruder.
  • ⁇ and ⁇ in the above formulas (V) and (VI) are determined so that the specific energies applied to the molten resin are equal.
  • a method for determining ⁇ and ⁇ either a theoretical determination method or an experimental determination method may be used.
  • the parameter ⁇ is set so that the specific function, the total shear amount, the residence time, etc. of the objective function are the same between the small machine and the large machine.
  • ⁇ are derived. Assuming the difference in heat transfer between the small machine and the large machine, the parameters ⁇ and ⁇ can be derived so that the specific energy as the objective function matches between the small machine and the large machine.
  • the objective function is a specific energy, or a parameter indicating physical properties is adopted, and the parameter ⁇ is statistically set so that the objective function matches between a small machine and a large machine. And a method of calculating ⁇ .
  • a single screw element having a flight part with a notch formed on the outer periphery is preferable because the minimum shear stress history value Tmin tends to increase.
  • a single screw element itself having a flight part with a notch formed on the outer periphery is known, and is described, for example, in Patent Document (DE4134026A1).
  • the number of undefibrated pellets can be suppressed to a small value.
  • the screw elements having the notches it is possible to use a reverse-feeding one having an arc-shaped notch, and the value of the minimum shear stress history value Tmin is set to reverse flight, seal ring, forward knee. It can be larger than a combination of screw elements such as a ding disk and a reverse kneading disk, and is preferable because the glass fiber bundle can be defibrated in a shorter time than other screw elements.
  • this one-way reverse feed screw element has a flight part in which an arc-shaped notch satisfying the following inequalities (I) to (III) is formed on the outer periphery.
  • FIG. 2 shows a schematic diagram of the single feed reverse feed screw element, wherein (a) is a sectional view in the axial direction, and (b) is a side view.
  • the single reverse feed screw element 4 includes a flight part 40 and an arc-shaped notch 41 formed on the outer periphery of the flight part 40.
  • the notch 41 is formed in a direction from the outer periphery of the flight part toward the axis of the screw element. 2 shows a case where the ellipse forms an arc shape, but the ellipse or the center of the circle forming the arc shape exists on the outer periphery of the flight part 40 (in FIG. 2A, the center of the ellipse is present). Indicated by O).
  • the notch has an arc shape, and the arc shape is formed by the circle or ellipse, so that there are advantages in manufacturing and minimizing a decrease in flight strength due to the notch.
  • the said circular arc shape should just be formed by said circle
  • the present invention is not limited to one in which the entire cutout is formed by the one circle or ellipse described above. However, it is preferable that substantially the entire arc shape is formed by one circle or ellipse.
  • the arc shape is most preferably a circle.
  • the range of the radius r is preferably 0.05D ⁇ r ⁇ 0.15D. If r is within the above range, the minimum shear stress history value Tmin tends to increase, which is preferable. A more preferable range of r is 0.06D ⁇ r ⁇ 0.12D.
  • the minimum shear stress history value T min tends to increase as the number of notches n increases.
  • the mechanical strength of the screw element decreases when the number of notches n increases excessively, it is preferable to adjust the number of notches n within the range of inequality (II).
  • a particularly preferable range of the number of notches n is 10 ⁇ n ⁇ 15, and the most preferable number of notches is 11.
  • the lead length Le of the screw element is not more than 0.3 times the screw diameter D of the screw element (Le is not more than 0.3D). If the lead length Le is 0.3D or less, even if the discharge rate Q is very high, undisrupted glass fibers tend not to be contained in the manufactured pellets. It should be noted that the discharge amount Q is very high, for example, when the screw element is provided with an axial length of 2D and a screw diameter D is 47 mm, the screw diameter is 47 mm. This is a twin screw extruder having a diameter D of 69 mm and is 800 kg / h or more. Even in such a high discharge area, problems due to the above-described undefined glass fibers can be suppressed.
  • the upper limit of the lead length Le of the screw element used in the present invention is preferably 0.3D or less, but the lower limit is preferably 0.1D or more. Setting it above this lower limit is preferable because the thickness of the flight part is maintained and the strength is maintained.
  • the function and shape of the single screw element having the flight part in which the arc-shaped notch is formed have been described above.
  • One of the features of the present invention is that the single line having the flight part in which the notch is formed.
  • the conventional low productivity can produce a glass reinforced resin composition without generating undefibrated glass.
  • pellets containing undefibrated glass are generated.
  • the torque density of the screw is set to 11 (Nm / cm 3 ) or more.
  • the torque density is 11 (Nm / cm 3 ) or more, the filling rate of the material in the extruder is increased, the energy density is reduced, and the temperature rise is low even if the rotational speed is higher than the conventional one.
  • a preferable range of the torque density is 13 (Nm / cm 3) or more 18 (Nm / cm 3) or less.
  • Q / Ns An important operating condition that affects whether or not unbreaked glass fibers are contained in the pellet is Q / Ns.
  • Q is the discharge amount and Ns is the screw rotation speed.
  • Q / Ns depends on the viscosity and specific energy of the glass fiber reinforced thermoplastic resin composition.
  • the upper limit of Q / Ns is determined by the torque density of extrusion and the meshing rate. When the torque density is high, the filling rate can be increased, and a large Q / Ns operating region can be adopted.
  • Q / Ns depends on the screw diameter of the extruder.
  • Q / Ns is scaled up according to the following relationship in a twin screw extruder having a constant meshing ratio.
  • D of the screw element becomes changed from d2 to D1
  • the screw rotation speed Ns 1 in a large extruder the following mathematical formula (VIII) is established.
  • Q 1 / Ns 1 (D 1 / d 2 ) ⁇ ⁇ (q 2 / ns 2 ) (VIII)
  • Q / Ns is an index of the filling rate, but if the meshing ratio is constant, the effective volume is proportional to the cube of the center-to-core distance between adjacent screws. It is proportional to the cube of the distance.
  • the effective volume refers to the volume of the space where the material can be filled in the twin-screw extruder.
  • Q / Ns depends on the size of the extruder as described above, but the value obtained by dividing the Q / Ns by the calculated value of the cube of the center-to-core distance between adjacent screws is the Q / Ns density.
  • the Q / Ns density is a constant value even if the size of the extruder is different.
  • the ratio of the outer diameter and the valley diameter of the screw is 1.54, the screw diameter is ⁇ 40 mm, and the diameter is ⁇ 70 mm.
  • the distance between the centers is the third power ( ⁇ 40 mm is 35.9 cm 3 , and ⁇ 70 mm is 192.4 cm 3 ).
  • it becomes a common value of 0.013 [kg / h / rpm / cm 3 ].
  • the present invention provides an element for a reverse feed flight having a flight part having a notch formed in the outer periphery of the kneading part under an operating condition where the Q / Ns density is 0.013 [kg / h / rpm / cm 3 ] or more. Is used to efficiently produce a glass-reinforced resin composition that does not contain glass undefibrated with high productivity.
  • a preferable Q / Ns density is 0.015 [kg / h / rpm / cm 3 ] or more and 0.018 [kg / h / rpm / cm 3 ] or less.
  • Carbon masterbatch glass fiber bundle 3 mm long chopped strand obtained by bundling 2200 monofilaments having a diameter of 13 ⁇ m
  • the composition is as follows. PBT is 67.5 mass%, carbon masterbatch is 2.5 mass%, glass fiber bundle is 30 mass%
  • Extrusion conditions are as follows.
  • Extruder Same direction full meshing type twin screw extruder TEX44 ⁇ II (manufactured by Nippon Steel) Screw diameter D of screw element is 0.047m Extrusion conditions; Barrel temperature; 220 ° C Screw design; (1) Outline The screw of the extruder can be represented as shown in FIG. 1, and the outline of the screw pattern shown in FIG. 3 is as follows.
  • the short diameter / 2 of the notch on the outer periphery of the BMS is 3 mm, and the long diameter / 2 (the direction in which the notch extends) is 4.15 mm.
  • FIG. 5 (a) has a kneading part b1 with a forward feed kneading disk having a length of 1.0D, and the kneading part b2 has a reverse feed flight with a length of 0.5D.
  • the screw shown in FIG. 5 (a) has a kneading part b1 with a forward feed kneading disk having a length of 1.0D, and the kneading part b2 has a reverse feed flight with a length of 0.5D.
  • the screw shown in FIG. 5 (c) has a single kneading part b1 having a notch having a length of 1.0D.
  • the screw shown in FIG. 5 (d) is a single reverse feed kneading disc with kneading part b1 having a notch length of 2.0D.
  • the kneading part b2 has a reverse feed flight with a length of 0.5D.
  • the screw shown in FIG. 5 (e) has a kneading part b1 with a notch with a length of 2.5D and a kneading part b2 0.5D length reverse feed
  • the analysis method is a finite volume method, a SOR method, or a SIMPLE algorithm.
  • a steady analysis is first performed, and an unsteady analysis is performed using this as an initial value.
  • tracer particles were arranged (about 5000 particles), and local information concerning the tracer particles was collected (particle tracking analysis).
  • Minimum value T min of the time integral value of the shear stress integrates the shear stress of local information relating to the tracer particles time, in which determining the minimum value of the total particle.
  • the correlation line is different for each Q / Ns. Therefore, the function of the formula (IV) is approximated by the method of least squares.
  • the approximate curve is shown in FIG. As shown in FIG. 8, it was possible to approximate with one correlation line independent of Q / Ns. Note that ⁇ was 3.0.
  • Formula (IV) can be used to study the amount of undefined glass fiber bundles contained in the pellet, and the screw element that the kneading unit has It was confirmed that the amount of undefined glass fiber bundles contained in the pellets can be examined with a single mathematical formula (IV) even if the types of are different.
  • a kneading disk (FIG. 5 (a) and (FIG. 5 (a) and ((5))) having a composition of 70% by mass of PBT resin and 30% by mass of glass fiber (glass monofilament diameter 13 ⁇ m) and used in a kneading part of a twin screw extruder (screw diameter 47 mm).
  • b) Evaluation of each simulation using the symbol FK) and a single reverse feed screw element (FIG. 5 (c) (d) (e) symbol BMS) having a notched flight part.
  • the distribution of the shear stress history value obtained by performing the time integration of the shear stress of the local information applied to the tracer particles by the same method as described in FIG.
  • the center of the notch is the outer peripheral part
  • a kneading part is composed of a single screw element having a flight part in which an arc-shaped notch is formed with a composition of 70% by mass of PBT resin and 30% by mass of glass fiber.
  • the simulation when used in the No. 23 was performed. Specifically, the relationship between the minimum shear stress history value T min obtained by the same method as in Evaluation 1 and the number of notches (groove number) n was obtained.
  • the minimum shear stress history value T min is high when the number n of notches per lead length Le is 13 to 15. As the number of notches n is larger, the minimum shear stress history value Tmin is higher. However, since the mechanical strength of the screw element decreases as the number of notches n increases, it can be said that 13 to 15 is preferable.
  • the center of the notch is on the outer periphery of the flight part, the shape of the notch is an ellipse, the short diameter / 2 of the notch on the outer periphery is 3 mm, and the long diameter / 2 (the direction in which the notch extends) is 3 mm, 4 mm, 4.
  • the results of Evaluation 4 are shown in Table 3.
  • the minimum shear stress history value T min has a maximum value when the major axis of the groove depth of the notch / 2 is 4 to 5 mm.
  • the short diameter / 2 of the notch on the outer periphery is 0.064D
  • the range of the long diameter / 2 in the groove depth direction is 0.085D to 0.11D.
  • the minimum shear stress history value increases as the radius increases even when the arc forms a circle.
  • the minimum shear stress history value is larger when the circular arc is formed than the ellipse is formed.
  • Example-1 In the examples, the following materials were used.
  • Carbon masterbatch glass fiber bundle 3 mm long chopped strand obtained by bundling 2200 monofilaments having a diameter of 13 ⁇ m
  • the composition is as follows. PBT is 67.5 mass%, carbon masterbatch is 2.5 mass%, glass fiber bundle is 30 mass%
  • Extruder Same direction complete meshing type twin screw extruder TEX44 ⁇ II (manufactured by Nippon Steel) Screw element diameter D is 0.047mm
  • the cylinder temperature is 220 ° C., and the extrusion conditions are listed in Table 6 below.
  • the specific screw pattern used in the examples is as shown in FIG.
  • the center of the notch is on the flight periphery.
  • Table 7 shows the results using the extruder shown in FIG. 5 (a)
  • Table 8 shows the results obtained using the extruder shown in FIG. 5 (b)
  • Table 9 shows the results obtained using the extruder shown in FIG. 5 (c).
  • Table 10 shows the results using the extruder shown in FIG. 5D
  • Table 11 shows the results obtained using the extruder shown in FIG.
  • FIG. 10 is a diagram showing the relationship between the discharge rate and the number of pellets containing undefined glass fibers.
  • 10 (a) and 10 (b) when FK is used in the kneading part, if Q / Ns is set to 0.8 or more, undefined bundles of glass may remain in many pellets. I can confirm.
  • FIG. 11A is a diagram showing a case where Q / Ns is 0.5 and 1.0
  • FIG. 11B is a diagram showing a case where Q / Ns is 0.8.
  • Q / Ns 0.5
  • the discharge amount is 300 kg / h
  • the discharge resin temperature is Since it exceeds 310 ° C.
  • the limit of the discharge amount is 300 kg / h.
  • the discharge resin temperature is less than 310 ° C. up to 700 kg / h, and if Q / Ns is increased, the productivity of high-quality pellets is dramatically improved.
  • FIG. 12 shows the operation region (maximum discharge amount) that is not performed.
  • the discharge rate at which the undefined glass fiber bundle does not remain in the pellet is the length (L / D) of the kneading disk (FK) used in the kneading part, and a single reverse feed having a flight part in which a notch is formed. Since it depends on the length (L / D) of the screw element (BMS), the relationship is shown by a straight line.
  • the resin has an inherent limit temperature at which the thermal decomposition becomes significant and the processing becomes a limit as the temperature rises. When the temperature of the resin reaches that temperature during pellet production, the discharge becomes a limit.
  • the kneading disk (FK) and the single-feed reverse screw element (BMS) having a flight part with a notch also increase the resin temperature as the length (L / D) used in the twin-screw extruder increases.
  • . 12 (a) to 12 (c) also show the limit of the resin temperature, and the intersection of the limit of the resin temperature and the limit at which the undefined glass fiber bundle does not remain in the pellet is the productivity. It is a limit.
  • FIGS. 12 (a) and 12 (b) the productivity when using a single reverse feed screw element (BMS) having a flight part with a notch used is a kneading disk (FK). It is shown that it is 2 to 4 times the case.
  • FIG.12 (c) shows the result when Q / Ns is as small as 0.5 with the same material and the same extruder.
  • the resin temperature rises greatly, and the productivity is limited at the temperature limit. It shows that there is no significant difference in productivity compared to the ding disc (FK).
  • the Q / Ns in FIGS. 12A and 12B are 1.0 and 0.8.
  • the above-described Q / Ns densities are 0.014 [kg / h / rpm / cm 3 ] and 0.018 [kg / h / rpm / cm 3 ], respectively.
  • Q / Ns is 0.5 and the Q / Ns density at this time will be 0.009 [kg / h / rpm / cm ⁇ 3 >].
  • a single reverse feed screw element having a flight part in which a notch is formed has a Q / Ns density of 0.013 [kg / h / rpm / cm 3 ] or more in an operating region. Since the defibrated glass fiber bundle is difficult to remain in the pellet, high productivity can be realized.

Landscapes

  • 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)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
  • Extrusion Moulding Of Plastics Or The Like (AREA)
  • Processes Of Treating Macromolecular Substances (AREA)
  • Reinforced Plastic Materials (AREA)
PCT/JP2012/058400 2011-04-01 2012-03-29 ガラス繊維強化熱可塑性樹脂組成物ペレットの製造方法 WO2012137666A1 (ja)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201280017404.0A CN103459110B (zh) 2011-04-01 2012-03-29 玻璃纤维补强的热塑性树脂组合物颗粒的生产方法

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2011-082313 2011-04-01
JP2011082313A JP5536705B2 (ja) 2011-04-01 2011-04-01 ガラス繊維強化熱可塑性樹脂組成物ペレットの製造方法

Publications (1)

Publication Number Publication Date
WO2012137666A1 true WO2012137666A1 (ja) 2012-10-11

Family

ID=46969067

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP2012/058400 WO2012137666A1 (ja) 2011-04-01 2012-03-29 ガラス繊維強化熱可塑性樹脂組成物ペレットの製造方法

Country Status (5)

Country Link
JP (1) JP5536705B2 (zh)
CN (1) CN103459110B (zh)
MY (1) MY163186A (zh)
TW (1) TWI501859B (zh)
WO (1) WO2012137666A1 (zh)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20140306370A1 (en) * 2013-04-12 2014-10-16 Corning Incorporated Mixing segments for an extrusion apparatus and methods of manufacturing a honeycomb structure
JP2022542509A (ja) * 2019-07-29 2022-10-04 ランクセス・ドイチュランド・ゲーエムベーハー 低いｔｈｆ含量のポリブチレンテレフタレート

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2965889A1 (de) * 2014-07-11 2016-01-13 Covestro Deutschland AG Mischelemente mit verbesserter Dispergierwirkung
JP7432080B2 (ja) * 2018-09-13 2024-02-16 三菱エンジニアリングプラスチックス株式会社 樹脂ペレットの製造方法
WO2022176449A1 (ja) * 2021-02-16 2022-08-25 三菱エンジニアリングプラスチックス株式会社 繊維強化ポリブチレンテレフタレート樹脂組成物の製造方法
JP7361240B2 (ja) * 2021-10-06 2023-10-13 ポリプラスチックス株式会社 熱可塑性樹脂組成物の製造方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0860001A (ja) * 1994-06-14 1996-03-05 Toray Ind Inc 繊維強化熱可塑性樹脂ペレットおよびその製造方法
JPH10180841A (ja) * 1996-12-25 1998-07-07 Asahi Chem Ind Co Ltd 粉体のサイドフィード用押出機及びそれを用いた押出方法
JP2002018842A (ja) * 2000-07-10 2002-01-22 Sumitomo Chem Co Ltd 液晶性樹脂ペレットの製造方法
JP2002103327A (ja) * 2000-10-04 2002-04-09 Asahi Kasei Corp ガラス繊維強化ポリアミド樹脂の製造方法
WO2005099984A1 (ja) * 2004-04-15 2005-10-27 Polyplastics Co., Ltd. 繊維状充填剤の長さが制御された樹脂組成物ペレットの製造方法
WO2006123824A1 (ja) * 2005-05-18 2006-11-23 Polyplastics Co., Ltd. 繊維状充填剤高濃度配合樹脂組成物の製造方法及び樹脂組成物ペレット
JP2010000654A (ja) * 2008-06-19 2010-01-07 Japan Steel Works Ltd:The 繊維強化樹脂ペレットの製造方法及び装置

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4134026C2 (de) * 1991-10-15 1994-04-21 Werner & Pfleiderer Gleichdrallschneckenkneter
KR950003362A (ko) * 1993-07-21 1995-02-16 마에다 가츠노스케 섬유강화 열가소성수지구조물과 그 제조방법 및 압출기
JP4387036B2 (ja) * 2000-04-28 2009-12-16 旭化成ケミカルズ株式会社 一条逆ネジ切り欠きスクリュを用いた液状添加剤の混練方法
JP2002120271A (ja) * 2000-10-13 2002-04-23 Japan Steel Works Ltd:The スクリュ式二軸混練押出機用スクリュ
JP2004284195A (ja) * 2003-03-24 2004-10-14 Toshiba Mach Co Ltd 二軸押出機のスクリュ
JP3886467B2 (ja) * 2003-04-10 2007-02-28 株式会社日本製鋼所 スクリュ式混練押出機
JP2007007864A (ja) * 2005-06-28 2007-01-18 Toshiba Mach Co Ltd オンラインブレンド射出成形機の可塑化装置
KR100998619B1 (ko) * 2008-07-22 2010-12-07 신일화학공업(주) 연속식 압출기

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0860001A (ja) * 1994-06-14 1996-03-05 Toray Ind Inc 繊維強化熱可塑性樹脂ペレットおよびその製造方法
JPH10180841A (ja) * 1996-12-25 1998-07-07 Asahi Chem Ind Co Ltd 粉体のサイドフィード用押出機及びそれを用いた押出方法
JP2002018842A (ja) * 2000-07-10 2002-01-22 Sumitomo Chem Co Ltd 液晶性樹脂ペレットの製造方法
JP2002103327A (ja) * 2000-10-04 2002-04-09 Asahi Kasei Corp ガラス繊維強化ポリアミド樹脂の製造方法
WO2005099984A1 (ja) * 2004-04-15 2005-10-27 Polyplastics Co., Ltd. 繊維状充填剤の長さが制御された樹脂組成物ペレットの製造方法
WO2006123824A1 (ja) * 2005-05-18 2006-11-23 Polyplastics Co., Ltd. 繊維状充填剤高濃度配合樹脂組成物の製造方法及び樹脂組成物ペレット
JP2010000654A (ja) * 2008-06-19 2010-01-07 Japan Steel Works Ltd:The 繊維強化樹脂ペレットの製造方法及び装置

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20140306370A1 (en) * 2013-04-12 2014-10-16 Corning Incorporated Mixing segments for an extrusion apparatus and methods of manufacturing a honeycomb structure
US9586187B2 (en) * 2013-04-12 2017-03-07 Corning Incorporated Mixing segments for an extrusion apparatus and methods of manufacturing a honeycomb structure
JP2022542509A (ja) * 2019-07-29 2022-10-04 ランクセス・ドイチュランド・ゲーエムベーハー 低いｔｈｆ含量のポリブチレンテレフタレート
JP7325603B2 (ja) 2019-07-29 2023-08-14 ランクセス・ドイチュランド・ゲーエムベーハー 低いｔｈｆ含量のポリブチレンテレフタレート

Also Published As

Publication number Publication date
TW201302430A (zh) 2013-01-16
JP2012213997A (ja) 2012-11-08
MY163186A (en) 2017-08-15
CN103459110B (zh) 2015-07-29
TWI501859B (zh) 2015-10-01
JP5536705B2 (ja) 2014-07-02
CN103459110A (zh) 2013-12-18

Similar Documents

Publication Publication Date Title
JP5536705B2 (ja) ガラス繊維強化熱可塑性樹脂組成物ペレットの製造方法
CN100575029C (zh) 混合有高浓度的纤维状填充剂的树脂组合物的制备方法及树脂组合物颗粒
EP1768823B1 (en) Apparatus for plasticating thermoplastic resin including polypropylene
JP5457933B2 (ja) 押出成形用複合ペレットの製造方法，及び前記方法で製造された押出成形用の複合ペレット
DE69916894T2 (de) Verfahren und vorrichtung zum extrudieren von polycarbonat mit niedriger schüttdichte
WO2011136273A1 (ja) 押出成形用複合ペレットの製造方法，及び前記方法で製造された押出成形用の複合ペレット
JP5632236B2 (ja) シミュレーション装置、プログラム、及び記録媒体
JP5632235B2 (ja) ガラス繊維強化熱可塑性樹脂組成物ペレットの製造方法
JP5536704B2 (ja) ガラス繊維強化熱可塑性樹脂組成物ペレットの製造方法
US20050063246A1 (en) Mixing and kneading device for polymer compositions
JP2018161860A (ja) 熱可塑性樹脂組成物のペレットの製造方法
JP2014233865A (ja) 無機物高充填樹脂のペレット製造装置および無機物高充填樹脂のペレット製造方法
JP6914541B2 (ja) 熱可塑性樹脂組成物の成形機、および製造方法
JPS5839659B2 (ja) 熱可塑物押出成形方法
JP7361240B2 (ja) 熱可塑性樹脂組成物の製造方法
CN218557913U (zh) 一种用于bfs的挤出螺杆
JP2023079184A (ja) 熱可塑性樹脂組成物の成形品の成形機、および成形品の製造方法
JP4707377B2 (ja) 熱可塑性樹脂原料のフィルム等の成形方法
JPS63199623A (ja) 熱可塑性樹脂成形用スクリユ−
WO2017170112A1 (ja) 射出成形用原料の製造方法、及び樹脂成形体の製造方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 12767661

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: 1301005633

Country of ref document: TH

122 Ep: pct application non-entry in european phase

Ref document number: 12767661

Country of ref document: EP

Kind code of ref document: A1