WO2017179584A1 - Procédé de fabrication d'une composition de résine et machine biaxiale de malaxage et d'extrusion - Google Patents

Procédé de fabrication d'une composition de résine et machine biaxiale de malaxage et d'extrusion Download PDF

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Publication number
WO2017179584A1
WO2017179584A1 PCT/JP2017/014854 JP2017014854W WO2017179584A1 WO 2017179584 A1 WO2017179584 A1 WO 2017179584A1 JP 2017014854 W JP2017014854 W JP 2017014854W WO 2017179584 A1 WO2017179584 A1 WO 2017179584A1
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Prior art keywords
screw
zone
cylinder
resin
kneading
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PCT/JP2017/014854
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English (en)
Japanese (ja)
Inventor
眞田　隆
幸司 亀尾
勇治 福田
嘉隆 木村
大吾 佐賀
Original Assignee
住友化学株式会社
株式会社日本製鋼所
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Publication of WO2017179584A1 publication Critical patent/WO2017179584A1/fr

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    • 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
    • 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
    • B29B7/58—Component parts, details or accessories; Auxiliary operations
    • B29B7/60—Component parts, details or accessories; Auxiliary operations for feeding, e.g. end guides for the incoming material
    • B29B7/603—Component parts, details or accessories; Auxiliary operations for feeding, e.g. end guides for the incoming material in measured doses, e.g. proportioning of several materials
    • 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
    • B29B7/84—Venting or degassing ; Removing liquids, e.g. by evaporating components
    • B29B7/845—Venting, degassing or removing evaporated components in devices with rotary stirrers
    • 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
    • B29B7/86—Component parts, details or accessories; Auxiliary operations for working at sub- or superatmospheric pressure
    • 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
    • B29B7/00—Mixing; Kneading
    • B29B7/80—Component parts, details or accessories; Auxiliary operations
    • B29B7/88—Adding charges, i.e. additives
    • B29B7/94—Liquid charges
    • 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
    • B29C48/285—Feeding the extrusion material to the extruder
    • 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
    • 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
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B9/00—Making granules
    • B29B9/02—Making granules by dividing preformed material
    • B29B9/06—Making granules by dividing preformed material in the form of filamentary material, e.g. combined with extrusion

Definitions

  • the present invention relates to a method for producing a resin composition and a twin-screw kneading extruder. More specifically, the present invention relates to a method for producing a resin composition in which a thermoplastic resin and powder are melt-kneaded using a biaxial kneader, and the resin composition is produced stably and with high productivity. In addition, the present invention relates to a method for reducing the amount of a volatile organic compound (Volatile Organic Compounds: abbreviated as VOC) remaining in a resin composition.
  • VOC volatile Organic Compounds
  • Thermoplastic resins such as polypropylene are relatively inexpensive, lightweight, and excellent in properties such as molding processability, mechanical properties, heat resistance, cold resistance, and long-term durability.
  • Various containers, food packaging materials, and household goods It is used in a wide range of applications, such as textiles for carpets and sofas, interior and exterior materials for automobiles, materials for household appliances, and building materials such as interior materials for buildings or houses.
  • VOC volatile organic compounds
  • thermoplastic resin As a method of reducing VOC in a thermoplastic resin, there is a method of drying and devolatilizing a thermoplastic resin which is a raw material before producing a resin composition by melt kneading, or drying and devolatilizing a resin composition after melt kneading. Although it is general, there are cases where it is not economical in view of the introduction of equipment such as a drying silo suitable for the production scale and the running cost for hot air or hot air drying. Also known is a method of reducing VOC by melt-kneading the resin composition produced by melt-kneading and water-injecting foam devolatilization again, but it is necessary to carry out melt-kneading twice. Therefore, it cannot be said to be an efficient method for producing a resin composition having a low VOC content.
  • the following is known as a technique for reducing VOC by performing water injection foam devolatilization.
  • a vacuum expansion zone is provided between the water injection dispersion zone and the devolatilization zone for the purpose of efficiently removing VOC from the molten resin, and between the vacuum expansion zone and the devolatilization zone, A water injection foaming devolatilization method in which a decompression ring having a slit is arranged is described.
  • Patent Document 2 in order to obtain a high screw rotation speed, water injection pressure, and water dispersibility for improving devolatilization efficiency, a seal ring is disposed only at one location downstream of the water injection dispersion zone. The water injection foam devolatilization method is described.
  • the conveying screw of the devolatilization unit has a half-angle flight shape for the purpose of suppressing heat generation of the resin due to shear friction and extending the residence time of the resin.
  • a conveying and kneading method is described in which gaps are formed on both sides of the flight so that a part of the resin flows backward from the downstream side to the upstream side.
  • Patent Document 4 improves the devolatilization efficiency by arranging a water injection dispersion zone consisting of a water dispersion foaming zone and a stirring zone for the purpose of speeding up the increase in the resin temperature near the bubble-resin interface in the water injection devolatilization step.
  • the water injection devolatilization method is described.
  • Japanese Patent Publication “JP 7-164509 A (published on June 27, 1995)” Japanese Patent Publication “Japanese Patent Laid-Open No. 10-249913 (published on September 22, 1998)” Japanese Patent Publication “Japanese Patent Laid-Open No. 11-277604 (published on Oct. 12, 1999)” Japanese Patent Publication “JP 2002-326273 A (published on November 12, 2002)”
  • an object of the present invention is a method for producing a resin composition in which a thermoplastic resin and powder are melt-kneaded, and the resin composition is produced stably and with high productivity.
  • An object of the present invention is to provide a method for reducing the amount of VOC remaining therein.
  • the present inventors have intensively studied and completed the present invention.
  • the present invention provides any of the following. 1) A method for producing a resin composition using a biaxial kneading extruder, wherein the resin composition contains a thermoplastic resin and powder as raw materials of the resin composition, and the biaxial
  • the kneading extruder includes a cylinder, a screw-type side feeder connected to the cylinder, a weight-type feeder connected to the screw-type side feeder, and a screw installed in the cylinder.
  • the cylinder includes a supply port, a connection port of the screw-type side feeder, a first vent port, a water injection port, and a second vent port in order from the upstream side of the cylinder.
  • the screw includes a first kneading zone located between the supply port and the connection port of the screw-type side feeder, and the screw-type side-feed.
  • a second kneading zone located between the connection port of the feeder and the first vent port, and a water injection devolatilization zone located downstream of the first vent port, the water injection devolatilization zone Is composed of, in order from the upstream of the cylinder, a full pressure increase zone, a water injection dispersion zone where the water injection port is located, and a vacuum expansion zone where the second vent port is located.
  • the thermoplastic resin has a transition temperature of less than 200 ° C.
  • the powder comprises an inorganic filler having an apparent density of 0.1 to 1.5 g / ml and an apparent density of 0.1 to 1.0 g / ml and one or more kinds of powder selected from the group consisting of thermoplastic resin powders having a transition temperature of 200 ° C. or higher, and the conveying ability of the screw-type side feeder is from the weight-type feeder to the screw-type
  • the effective volume per unit time of the powder supplied to the side feeder is 1.2 times or more.
  • the amount of water supplied to the water injection dispersion zone is Less than 5 parts by weight or more 0.1 parts by weight based on the total feed weight of the raw material into the Nda, resin pressure in the water injection dispersion zone is 1MPa or more, the production method.
  • thermoplastic resin in the cylinder A supply port for supplying to the cylinder, a connection port of the screw-type side feeder for connecting the screw-type side feeder for supplying the powder into the cylinder, and a gas or a volatile component in the cylinder.
  • a first vent port for removal outside the cylinder, a water injection port for supplying water to the resin composition, A second vent port for vaporizing the volatile component in the resin composition together with the water and devolatilizing, and the inside of the cylinder and the screw are connected to the supply port and the screw-type side feeder.
  • a twin-screw kneading extruder comprising a devolatilization zone.
  • a resin composition can be produced stably with high productivity, and the amount of VOC remaining in the resin composition can be reduced.
  • the resin composition targeted for the production of the present invention is a resin composition containing a powdered resin reinforcing material.
  • the resin composition obtained by the production method of the present invention may be provided as a resin compound product having a pellet shape or the like.
  • the resin composition obtained by the production according to the present invention is widely used as an industrial member such as an automobile part, and specifically, is used for an interior material of an automobile.
  • thermoplastic resin used as a raw material of the resin composition according to the present invention is a thermoplastic resin having a transition temperature of less than 200 ° C.
  • the transition temperature of the thermoplastic resin is the melting peak temperature of the resin in the case of a crystalline thermoplastic resin, and the glass transition temperature of the resin in the case of an amorphous thermoplastic resin.
  • the temperature can also be determined by differential scanning calorimetry.
  • thermoplastic resins include polyolefin resins (high density polyethylene, low density polyethylene, polypropylene, etc.), cyclic olefin resins, aliphatic polyester resins (polylactic acid, etc.), aliphatic polycarbonates, poly Examples include oxymethylene and styrene resins.
  • polyoxymethylene include polyacetal and the like
  • examples of styrene resins include polystyrene, SEBS (styrene / ethylene / butylene / styrene block copolymer), and acrylonitrile / butadiene / styrene copolymer. Etc. These may be used alone or in combination with a plurality of resins.
  • the shape supplied to this manufacturing method may be a pellet or a powder (powder).
  • the powder that can be used as a raw material for the resin composition of the present invention includes an inorganic filler having an apparent density of 0.1 to 1.5 g / ml, an apparent density of 0.1 to 1.0 g / ml, and a transition temperature of 200 ° C. It is selected from the group consisting of the above thermoplastic resin powders (hereinafter sometimes simply referred to as “thermoplastic resin powder”). Only one type of powder may be used, or a plurality of types may be used.
  • ⁇ indicating a numerical range indicates a numerical range including the lower limit and the upper limit (that is, above and below) unless otherwise specified.
  • the inorganic filler having the above-described conditions include natural silicic acid or silicate, carbonate, hydroxide, oxide, particulate filler, flaky filler, fibrous filler, and carbon.
  • natural silicic acid or silicate include talc, kaolinite, clay, pyrophyllite, sericite, bentonite and silica.
  • carbonates include calbium carbonate, magnesium carbonate, hydrotalcite and the like.
  • the hydroxide include aluminum hydroxide and magnesium hydroxide.
  • the oxide include zinc white, iron oxide, magnesium oxide, aluminum oxide, titanium oxide and mullite.
  • the particulate filler examples include a synthetic filler such as hydrous silicate or anhydrous silicate, or a particulate filler such as silicate.
  • examples of the flaky filler include mica
  • examples of the fibrous filler include basic magnesium sulfate whisker, calcium titanate whisker, potassium titanate whisker, aluminum borate whisker, and wollastonite. , Sepiolite, zeolite, attapulgite, zonotlite, rock wool, glass wool, glass fiber and carbon fiber.
  • the apparent density of the inorganic filler is 0.1 to 1.5 g / ml, preferably 0.1 to 1.0 g / ml, more preferably 0.1 to 0.8 g / ml.
  • the apparent density means a density expressed by weight per unit volume
  • the apparent density of the powder indicates an apparent density measured by the method of JIS K7365: 1999.
  • (apparent density) / (true density) is preferably 0.3 or less, more preferably 0.25 or less, and still more preferably 0.00. Those that are 2 or less are used.
  • the inorganic filler having an (apparent density) / (true density) of 0.3 or less has an effect of improving productivity by the production method of the present invention. It is preferable in that it is more noticeable.
  • the “true density” is a density calculated from the volume of the container excluding the gap portion when the container is filled with the powder, and in this application the true density of the powder is JIS Z8807. : The density measured by the method of 2012 is pointed out.
  • the thermoplastic resin powder that can be used as a raw material for the resin composition of the present invention is a thermoplastic resin powder having an apparent density of 0.1 to 1.0 g / ml and a transition temperature of 200 ° C. or higher.
  • Specific examples of the thermoplastic resin powder include polyphenylene ether, polyphenylene sulfide, polyether ketone, polyamide resins (such as nylon 6 and nylon 66), and aromatic polyester resins (polyethylene terephthalate, polybutylene terephthalate, polybutylene). Naphthalate, etc.), aromatic polycarbonate, liquid crystal polymer and the like.
  • the effects of the present invention are particularly high, such as polyphenylene ether, polyphenylene sulfide, and liquid crystallinity, which have a high melting point and glass transition temperature, do not enter a melt-flow state up to a relatively high temperature, and maintain powder fluidity.
  • examples thereof include polymers.
  • the ratio of the raw materials supplied to the biaxial kneading extruder described later is the total weight of the thermoplastic resin having a transition temperature of less than 200 ° C. and the powder.
  • the preferred range of the powder is 5 to 80% by weight, more preferably 10 to 70% by weight, still more preferably 15 to 60% by weight.
  • Optional component In the resin composition to be produced according to the present invention, other optional components may be blended in addition to the above-described components.
  • optional components include elastomers, and more specifically, olefin-based, styrene-based, acrylic-based, urethane-based or engineering plastic (engineering plastic) -based elastomers.
  • olefin elastomer examples include ethylene- ⁇ -olefin copolymers such as an ethylene-propylene copolymer, an ethylene-butene copolymer, and an ethylene-octene copolymer.
  • antioxidants such as an agent, a foaming agent, a processing aid, a neutralizing agent, a heavy metal deactivator, a nucleating agent, an antifogging agent, an antibacterial agent, and an antifungal agent.
  • the impact strength of the produced resin composition can be improved or flexibility can be imparted.
  • thermoplastic resin having a transition temperature of less than 200 ° C. is 20 to 95 parts by weight, more preferably 30 to 90 parts by weight, and still more preferably 40 to 85 parts by weight.
  • the preferred range of the powder is 5 to 80 parts by weight, more preferably 10 to 70 parts by weight, and still more preferably 15 to 60 parts by weight.
  • thermoplastic resin pellets may be further used as a raw material.
  • thermoplastic resin pellets having an (apparent density) / (true density) of 0.9 or more can be mentioned.
  • the transition temperature of the resin pellet is arbitrary.
  • the ratio of the supply amount of the resin pellet in the raw material includes the thermoplastic resin having a transition temperature of less than 200 ° C. and the resin pellet.
  • the total supply amount with the thermoplastic resin of less than 200 ° C. is calculated as the supply amount of the thermoplastic resin having a transition temperature of less than 200 ° C. as the raw material of the resin composition according to the present invention.
  • the powder as a raw material of the resin composition is at least one powder selected from the group consisting of talc, kaolinite and clay, and the thermoplastic resin having a transition temperature of less than 200 ° C. Polyolefin resin.
  • the present invention is a method for producing the above-described resin composition. More specifically, the present invention relates to a method for producing a resin composition using a biaxial kneading extruder having a predetermined structure, which will be described later. 1) Biaxial kneading extrusion of raw materials (thermoplastic resin or powder) 2) a supply process for supplying into the cylinder of the machine, 2) a melt-kneading process for melting and kneading the raw material supplied into the cylinder to produce a resin composition, and 3) water for the resin composition produced in the melt-kneading process.
  • FIG. 1 is a diagram showing a schematic configuration of an exemplary apparatus for carrying out a manufacturing method according to the present invention.
  • the twin-screw kneading extruder 100 includes a cylinder 50, a screw-type side feeder 2 connected to the cylinder 50, a weight-type feeder 3 connected to the screw-type side feeder 2, And a screw 30 installed in the cylinder 50.
  • the cylinder 50 includes a supply port 1, a connection port for the screw-type side feeder 2, a first vent port 4, a water injection port 5, and a second vent port 6 in order from the upstream side of the cylinder.
  • the inside of the cylinder 50 and the screw 30 include a first kneading zone 9 located between the supply port 1 and the connection port of the screw-type side feeder 2, and a connection port of the screw-type side feeder 2 and the first vent port 4.
  • a second kneading zone 10 located in between and a water injection and devolatilization zone 15 located downstream of the first vent port 4 are configured.
  • the water injection devolatilization zone 15 includes a third kneading zone 11 and a decompression / expansion zone 14 in order from the upstream side, and the third kneading zone 11 further includes a full pressure increase zone 12 and a water injection side in order from the upstream side.
  • the dispersion zone 13 is included.
  • the water injection port 5 is provided so as to open to the water injection dispersion zone 13, and the second vent port 6 is provided so as to open to the reduced pressure expansion zone 14.
  • the inside of the cylinder 50 and the screw 30 upstream of the first kneading zone 9 is a first transport zone
  • the transport zone between the first kneading zone 9 and the second kneading zone 10 is a second transport zone.
  • a conveyance zone between the second kneading zone 10 and the third kneading zone 11 is defined as a third conveyance zone.
  • the water injection devolatilization zone 15 is also a 4th conveyance zone.
  • the fourth transport zone may be from the water injection devolatilization zone 15 to a transport zone further provided downstream of the water injection devolatilization zone 15.
  • the expressions “upper” and “lower” when describing the positional relationship between the two configurations in the vertical direction, for example, the expressions “upper” and “lower” are used, and each configuration is positioned in contact with or apart from each other. means.
  • the direction of the arrow shown in the lower part of FIG. 1 means the flow direction when the resin material is transferred in the apparatus, and there are a certain part of the apparatus and other parts.
  • the positional relationship at a certain point in one member of the apparatus it is referred to as “upstream” and “downstream” or “upstream” and “downstream” with respect to the flow direction of the resin material.
  • the most upstream and downstream end faces in one member are expressed as “upstream end” and “downstream end”, respectively.
  • This step is a step of supplying the raw material into the cylinder 50.
  • the thermoplastic resin supplying step of supplying the above-described thermoplastic resin into the cylinder 50 continuously or intermittently, and the thermoplastic resin Is a step of performing the powder supply step in parallel with the above-described powder supply continuously or intermittently into the cylinder 50 to which is supplied.
  • This step is a step of supplying the thermoplastic resin from the supply port 1 into the cylinder 50.
  • the thermoplastic resin supplied into the cylinder 50 in this step is transferred to the first kneading zone 9 through the first transport zone.
  • the first kneading zone 9 is a plasticizing region for plasticizing the thermoplastic resin. In this region, the first kneading zone 9 is melt-kneaded under the condition that the resin pressure in the first kneading zone 9 is 0.1 MPa or more, and the thermoplastic resin is plasticized. Make it.
  • a weight type feeder 16 may be connected to the supply port 1, and a thermoplastic resin may be supplied from the weight type feeder 16 through the supply port 1.
  • one or more other optional components such as an elastomer or an additive may be supplied together with the thermoplastic resin.
  • one or more weight type feeders 16 ′ and / or capacity type feeders 17 different from the weight type feeder 16 used for supplying the thermoplastic resin are connected to the supply port 1, and an elastomer or an additive 1 or the like is connected.
  • Two or more other components may be supplied through the supply port 1 from a different feeder for each component.
  • a weight-type feeder 16 ′ and a capacity-type feeder 17 that are different from the weight-type feeder 16 used for supplying the thermoplastic resin are connected to the supply port 1, and the elastomer is weighted.
  • the additive is supplied from the capacity feeder 16 ′ from the capacity feeder 17 through the supply port 1.
  • a biaxial kneading extruder 100 includes a screw 30 for transferring a resin composition in a cylinder 50.
  • the screw 30 of the twin-screw kneading extruder 100 according to the present invention is preferably a screw having two kneading segments from the viewpoint of increasing productivity.
  • the rotational speed of the screw 30 is, for example, 200 to 2000 rpm, and preferably 1000 to 1800 rpm. The higher the number of revolutions, the more frequently the gas-liquid interface is renewed and the lower the equilibrium concentration, so that the VOC devolatilization efficiency can be improved. However, if the rotational speed is too high, the resin deteriorates due to shearing heat generation. Therefore, it is necessary to appropriately adjust the rotational speed in view of the degree of heat generation. The devolatilization of VOC will be described later.
  • the twin-screw kneading extruder 100 is set so that the resin pressure in the first kneading zone 9 is 0.1 MPa or more, preferably 0.1 to 5 MPa, more preferably 0.1 to 1 MPa.
  • a predetermined resin pressure in the first kneading zone 9 may be maintained by appropriately installing a segment capable of adjusting the resin pressure in the first kneading zone 9 of the screw 30.
  • the segment disposed in the first kneading zone 9 includes a segment for sending resin (concept including a resin composition) in the downstream direction by rotating a screw, a segment for pushing the resin back in the upstream direction, or damming the resin.
  • Examples include a segment having an effect.
  • a segment that pushes the resin back in the upstream direction by the rotation of the screw a disk generally referred to as a reverse kneading disk (hereinafter referred to as “reverse disk”) whose reverse flight and twist angle exceed 90 ° with respect to the feed direction.
  • reverse disk a reverse kneading disk
  • a seal ring is mentioned as a segment which has an effect which dams up resin.
  • forward disks may be disposed at a position upstream of the center of the first kneading zone 9 of the screw 30.
  • a forward disk is a disk whose twist angle is less than 90 ° with respect to the feed direction. If the forward disk is disposed, the degree of plasticization of the thermoplastic resin can be adjusted while efficiently increasing the resin pressure.
  • a so-called orthogonal disk having a twist angle of 90 ° can be further arranged as necessary. Further, two or more of these segments may be arranged in combination.
  • the position where the orthogonal disk is arranged is preferably between the aforementioned reverse disk and the sequential disk, or between the sequential disk and the sequential disk.
  • the pressure in the first kneading zone 9 can be measured using a pressure sensor installed in the first kneading zone 9. It is preferable to install one to three pressure sensors in the center to the downstream region of the first kneading zone 9 filled with the resin in the cylinder 50 as necessary.
  • the pressure sensor must be installed in the cylinder 50 so as not to be damaged by the rotating screw. If the pressure sensor is located deeper in the direction of the screw 30 than the wall surface of the cylinder inner wall, the resin accumulates in the pressure sensor and accurately measures the pressure. Since it becomes impossible, it is preferable to install the tip of the pressure sensor at a position that matches the wall surface of the cylinder inner wall as much as possible.
  • This step is a step of supplying the powder from the screw-type side feeder 2 into the cylinder 50 to which the above-described thermoplastic resin is supplied.
  • the screw side feeder 2 is connected to a weight type feeder 3. Therefore, first, powder is supplied to the weight-type feeder 3, and the powder is transferred from the weight-type feeder 3 to the screw-type side feeder 2. Powder is supplied from the screw-type side feeder 2 into the twin-screw kneading extruder 100.
  • the conveying capacity of the powder of the screw-type side feeder 2 is preferably 1.2 times or more of the effective volume per unit time of the powder supplied from the weight-type feeder 3 to the screw-type side feeder 2, and more Preferably, it is 2 times or more, more preferably 4 times or more.
  • the upper limit of the powder conveyance capacity of the screw-type side feeder 2 depends on the design and durability of the apparatus, it is usually per unit time of the powder supplied from the weight-type feeder 3 to the screw-type side feeder 2.
  • the effective volume is 10 times or less.
  • the powder conveying ability of the screw-type side feeder 2 means the volume per unit time of the powder supplied from the screw-type side feeder 2 to the biaxial kneading extruder 100.
  • the product of the volume of space sent to the front of the feeder that is, the direction of the cylinder 50 in FIG. 1 and the screw rotation speed while the screw of the screw-type side feeder 2 makes one rotation, or the screw
  • the difference between the volume of the cylinder barrel per screw length of the screw of the side feeder 2 and the volume of the screw per lead length of the screw side feeder 2 and the screw rotation speed of the screw side feeder 2 are obtained. be able to.
  • the effective volume of the powder must be evaluated based on the volume actually supplied to the side feeder.
  • the effective volume per unit time of the powder supplied from the weight-type feeder 3 to the screw-type side feeder 2 is the weight of the powder supplied from the weight-type feeder 3 to the screw-type side feeder 2 per unit time. It can be determined as a value divided by the density.
  • the “bulk density of the powder” means that the powder is measured from the same height as when the powder is actually supplied from the weight-type feeder 3 to the screw-type side feeder 2, and a measuring container such as a measuring cylinder is used. And the weight of the powder in the measuring container is divided by the volume of the powder measured in the measuring container.
  • the conveying capacity of the screw-type side feeder 2 is preferably at least twice the effective volume per unit time of the powder supplied from the weight-type feeder 3 to the screw-type side feeder 2.
  • the screw-type side feeder 2 when the powder is supplied to the biaxial kneading extruder 100 with the screw-type side feeder 2, resin pellets or the like different from the powder may be supplied together with the powder.
  • the conveying capacity of the screw-type side feeder 2 is sufficiently larger than the total amount of the effective volume of the powder supplied from the weight-type feeder 3 to the screw-type side feeder 2 and the volume of the resin pellets, the screw-type side feeder 2 There is no need to consider the volume of the resin pellets when setting the feeding capacity of the feeder.
  • the powder and the resin pellets of 25 parts by weight or more with respect to 100 parts by weight of the powder pass from the weight type feeder through the screw type side feeder. It is preferable to be supplied to the biaxial kneading extruder 100.
  • the resin pellet supplied from the weight type feeder 3 through the screw type side feeder 2 into the cylinder 50 is preferably 200 parts by weight or less with respect to 100 parts by weight of the powder.
  • Examples of the resin pellet supplied from the weight type feeder 3 through the screw type side feeder 2 to the biaxial kneading extruder 100 include thermoplastic resin pellets having an (apparent density) / (true density) of 0.9 or more. There is no restriction on the transition temperature. Furthermore, the above-described thermoplastic resin may be additionally supplied together with the powder through the screw-type side feeder 2.
  • one or more weight-type feeders 3 'and / or capacity-type side feeders are connected to the screw-type side feeder 2, and the above-mentioned thermoplastic resin and / or a plurality of types of optional components are added to each component.
  • a weight-type feeder 3 ′ is connected to the screw-type side feeder 2, and thermoplastic resin is added into the biaxial kneading extruder 100 through the weight-type feeder 3 ′ and the side feeder 2. Supply.
  • thermoplastic resin supplied from the supply port 1 in the above steps and the powder supplied using the screw-type side feeder 2 are conveyed to the second kneading zone 10 through the second conveyance zone.
  • thermoplastic resin which may be a resin composition
  • the above-described thermoplastic resin is melt-kneaded in the cylinder 50 (more specifically, the first to third kneading zones, particularly the first to second kneading zones). It is a process to do.
  • the thermoplastic resin and the powder conveyed to the second kneading zone 10 are kneaded, and the powder is uniformly dispersed in the thermoplastic resin, thereby including the thermoplastic resin and the powder.
  • a resin composition is produced.
  • the biaxial kneading extruder 100 is operated so that the resin pressure in the second kneading zone 10 is less than 5 MPa, preferably less than 3 MPa, more preferably less than 1 MPa.
  • the resin pressure in the second kneading zone 10 is preferably 0.02 MPa or more, and more preferably 0.1 MPa or more.
  • the resin pressure in the first kneading zone at this time is as described above.
  • a predetermined resin pressure in the second kneading zone 10 may be maintained by appropriately installing a segment capable of adjusting the resin pressure in the second kneading zone 10 of the screw 30.
  • a segment capable of adjusting the resin pressure in the second kneading zone 10 of the screw 30 For example, in the second kneading zone 10, for example, on the downstream side of the center in the second kneading zone 10, a segment that pushes back the resin in the upstream direction by rotation of the screw or a segment that has an effect of blocking the resin is disposed. By doing so, the resin pressure may be maintained.
  • the gap distance (chip clearance) from the stirring edge, which is the outermost peripheral end surface of the segment such as an inverted disk installed downstream of the second kneading zone 10, to the inner wall of the cylinder is equal to the gap distance from the normal flight top to the inner wall of the cylinder. It is common. However, the gap distance of the kneading disk used in the second kneading zone 10 is preferably 2 to 3 times the usual distance. With such a gap distance, the resin pressure in the second kneading zone 10 can be controlled within the pressure range described above.
  • the thickness in the axial direction (disk width) of each kneading disk is usually about 0.1D to 0.2D (D is the screw diameter) in many cases.
  • D is the screw diameter
  • the thermoplastic resin and the powder are melt-kneaded so that the powder is uniformly dispersed in the thermoplastic resin.
  • the gas or volatile component is removed to the outside of the biaxial kneading extruder 100 from the first vent port 4 downstream from the second kneading zone 10.
  • a gas or a volatile component may be released to the atmosphere from the first vent port 4, and a vacuum pump may be connected to the first vent port 4 and sucked under reduced pressure. Next, it transfers to the 3rd kneading zone 11 through the 3rd conveyance zone.
  • the resin composition obtained by kneading in the above-described step is supplied with water from the water inlet 5 to the water pouring and dispersing zone 13 in the third kneading zone 11 to knead and disperse the resin composition.
  • the volatile component in the resin composition is vaporized together with water and removed from the second vent port 6.
  • the resin in the kneading and dispersing step, is further filled in the cylinder 50 and the pressure is increased to a desired pressure, and water is supplied to the resin composition by supplying water to the resin composition. It includes a water injection dispersion step for mixing and dispersing, and a pressure reduction expansion step for removing the VOC contained in the resin by foaming the water mixed and dispersed in the resin under reduced pressure in the water injection dispersion step.
  • a water injection dispersion step for mixing and dispersing
  • a pressure reduction expansion step for removing the VOC contained in the resin by foaming the water mixed and dispersed in the resin under reduced pressure in the water injection dispersion step.
  • ⁇ Charge boosting process> The resin obtained in the above process is further transferred downstream of the first vent port 4. Subsequently, in the filling pressure increasing step, the resin composition is filled in the cylinder 50 in the filling pressure increasing zone 12, and the pressure is increased. Preferably, it is desirable to appropriately increase the resin pressure by appropriately arranging segments such as a forward disk.
  • the resin composition to be transferred is pressurized in the filling pressure increase zone 12 in order to suppress the water injection and vaporization to some extent and disperse it in the resin. It is necessary to maintain the state.
  • a seal ring 8 may be disposed between at least one of the filling pressure increase zone 12 and the water injection dispersion zone 13 and at least one of the water injection dispersion zone 13 and the decompression expansion zone 14, preferably both. If the seal ring 8 is installed, the resin can be blocked. In the case where it is installed both between the filling pressure increase zone 12 and the water injection dispersion zone 13 and between the water injection dispersion zone 13 and the decompression expansion zone 14, seals at the upstream end and the downstream end of the water injection dispersion zone 13 are provided. Dam the resin with the ring. If it is the said structure, it will suppress that the resin kneaded flows back upstream, maintaining the state pressure
  • the water injection dispersion step is a step of mixing and dispersing water in the resin in the water injection dispersion zone 13 following the above-described filling pressure increasing step. Resin is transferred to the water injection dispersion zone 13. Water is injected from the water injection port 5 provided upstream of the center of the water injection dispersion zone 13. The water is injected by, for example, connecting the water injection port 5 to the water injection nozzle 5 'and further connecting the nozzle to a liquid pump or the like.
  • the amount of water supplied to the water injection dispersion zone is preferably 0.1 parts by weight or more and less than 5 parts by weight with respect to the total weight of the raw materials supplied into the cylinder 50, and 0.3 parts by weight or more.
  • the amount is more preferably less than 4 parts by weight, and still more preferably 0.5 parts by weight or more and less than 3 parts by weight. It is preferable to efficiently disperse water in the resin using a desired segment or the like disposed in the water injection dispersion zone 13.
  • a segment for example, a segment such as an orthogonal disk with little change in pressure state and a stirring effect can be cited.
  • the resin pressure in the water injection dispersion zone 13 is 1 MPa or more.
  • the resin pressure in the water injection dispersion zone 13 is preferably about 1 to 5 MPa, more preferably 1 to 4 MPa, and even more preferably 1 to 3 MPa.
  • the decompression expansion step is a step of removing VOC contained in the resin by foaming the water mixed and dispersed in the resin in the water injection dispersion step described above under reduced pressure.
  • the resin composition in which water is mixed and dispersed is transferred to the vacuum expansion zone 14.
  • the water mixed and dispersed in the resin is foamed under reduced pressure to greatly increase the bubble-resin interface.
  • the segment used in the decompression / expansion zone 14 may be only a flight screw having a conveyance capability, or may be a combination of two or more segments such as an orthogonal disk or a gear kneading disk and a mixing disk having a mixing effect. Good.
  • the vent port 6 may be connected to the opening provided in the upper part of the cylinder 50 through a vacuum pump for suction under reduced pressure, or from the side of the cylinder 50 for the purpose of suppressing bent-up or entrainment phenomenon of the molten resin.
  • vacuum devolatilization may be performed using the devolatilizer 7 equipped with the biaxial screw.
  • the method for producing a resin composition according to the present invention may further include a step of supplying an optional component depending on the purpose.
  • an optional component what was described in the item (arbitrary component) of the item of the above-mentioned raw material is mentioned.
  • additives may be supplied into the biaxial kneading extruder 100 from the supply port 1 in the first conveying zone of the biaxial kneading extruder 100 together with the thermoplastic resin, or in the second conveying zone. Or you may supply into the biaxial kneading extruder 100 from the supply port provided in the 3rd conveyance zone.
  • the additive is supplied together with the thermoplastic resin. May be.
  • one or more weight-type feeders 16 ′ and / or capacitive feeders 17 different from the weight-type feeder 16 used for supplying the thermoplastic resin are connected to the supply port 1, and a plurality of types of optional components are added to each of them.
  • one or more weight-type feeders 3 'and / or capacity-type side feeders are connected to the screw-type side feeder 2, and a plurality of kinds of optional components are different for each component.
  • the biaxial kneading extruder 100 may be supplied through the capacity-type side feeder and the screw-type side feeder 2.
  • a granulating step for connecting the granulating device or the like for pelletizing the resin composition to the downstream of the biaxial kneading extruder 100 and making the resin composition into a pellet shape is included. Also good.
  • a VOC residual amount measurement step of measuring the VOC residual amount in the obtained resin composition using a gas chromatograph or the like may be included as necessary.
  • twin screw kneading extruder 100 The main configuration and operation of the twin-screw kneading extruder 100 according to the present invention are as described above. Here, the changeable points of each configuration and configurations not shown will be described.
  • the biaxial kneading extruder 100 is a biaxial kneading extruder that kneads a resin composition raw material while melting it and extrudes the resin composition obtained by kneading in a shape such as a pellet shape. Therefore, two kneading screws 30 for kneading the resin are accommodated in the cylinder 50 so as to be freely rotatable.
  • the supply port 1 may have a configuration such as a hopper.
  • the screw-type side feeder 2 includes a biaxial screw-type side feeder.
  • a plurality of supply ports and screw side feeders for supplying each raw material into the cylinder 50 may be provided.
  • a drain pot and a vacuum pump may be further connected to the devolatilizer 7.
  • the screw configuration of the second kneading zone 10 is mainly a forward disk, and a wide disk is preferable. Further, it is preferable that the gap distance (chip clearance) is wider than usual.
  • the disk is preferably thinner in order to quickly increase the pressure to 1 MPa or more required for the water injection dispersion zone 13.
  • the thickness of the disk is thin in order to efficiently mix and disperse the water injected in a short section into the resin.
  • a full flight screw in the full pressure zone of the tip As an example, two full flight screws are used.
  • a square flight or half angle flight shaped screw or a single full flight screw may be used.
  • the biaxial kneading extruder 100 of the present invention is the above-mentioned [1. It can be suitably used in the production method described in the production method of the resin composition].
  • a granulation apparatus for pelletizing the resin composition is provided downstream of the twin-screw kneading extruder. Furthermore, an apparatus for measuring the remaining amount of VOC may be provided.
  • the raw materials are not smoothly fed into the biaxial kneading extruder.
  • the present invention includes any of the following 1) to 9).
  • the kneading extruder includes a cylinder, a screw-type side feeder connected to the cylinder, a weight-type feeder connected to the screw-type side feeder, and a screw installed in the cylinder.
  • the cylinder includes a supply port, a connection port of the screw-type side feeder, a first vent port, a water injection port, and a second vent port in order from the upstream side of the cylinder.
  • the screw includes a first kneading zone located between the supply port and the connection port of the screw-type side feeder, and the screw-type side-feed.
  • a second kneading zone located between the connection port of the feeder and the first vent port, and a water injection devolatilization zone located downstream of the first vent port, the water injection devolatilization zone Is composed of, in order from the upstream of the cylinder, a full pressure increase zone, a water injection dispersion zone where the water injection port is located, and a vacuum expansion zone where the second vent port is located.
  • the thermoplastic resin has a transition temperature of less than 200 ° C.
  • the powder comprises an inorganic filler having an apparent density of 0.1 to 1.5 g / ml and an apparent density of 0.1 to 1.0 g / ml and one or more kinds of powder selected from the group consisting of thermoplastic resin powders having a transition temperature of 200 ° C. or higher, and the conveying ability of the screw-type side feeder is from the weight-type feeder to the screw-type
  • the effective volume per unit time of the powder supplied to the side feeder is 1.2 times or more.
  • the amount of water supplied to the water injection dispersion zone is Less than 5 parts by weight or more 0.1 parts by weight based on the total feed weight of the raw material into the Nda, resin pressure in the water injection dispersion zone is 1MPa or more, the production method.
  • the biaxial kneader-extruder is provided with a seal ring between at least one of the filling pressure increase zone and the water injection dispersion zone and between the water injection dispersion zone and the reduced pressure expansion zone 1) to 3).
  • the manufacturing method of the resin composition in any one of.
  • the powder and the resin pellets are supplied from the gravimetric feeder through the screw-type side feeder into the cylinder, and the amount of the resin pellets is 100 parts by weight of the powder.
  • the powder is at least one powder selected from the group consisting of talc, kaolinite and clay, and the thermoplastic resin having a transition temperature of less than 200 ° C. is a polyolefin resin 1) to 6)
  • the manufacturing method of the resin composition in any one of. 8)
  • a second vent port for vaporizing the volatile component in the resin composition together with the water and devolatilizing, and the inside of the cylinder and the screw are connected to the supply port and the screw-type side feeder.
  • a twin-screw kneading extruder comprising a devolatilization zone. 9) A granulation system comprising a twin-screw kneading extruder for producing pellets of a resin composition using the production method according to any one of 1) to 7).
  • a resin composition was produced in an apparatus having the same configuration as that of the biaxial kneading extruder 100.
  • the twin-screw kneading extruder 100 used was TEX44 ⁇ II manufactured by Nippon Steel Co., Ltd., which is a meshing type with a cylinder diameter of 47 mm.
  • the biaxial kneader-extruder had a cylinder and two screw shafts accommodated in the cylinder.
  • a biaxial screw-type side feeder was used as the screw-type side feeder 2.
  • a vacuum pump was connected to the first vent port 4.
  • the 2nd vent port 6 which connected the devolatilizer 7 from the side surface was provided.
  • the water injection port 5 is provided with a water injection nozzle 5 ′. Further, a weight type feeder 16, a weight type feeder 16 ′ and a capacity type feeder 17 were connected to the supply port 1. Further, the weight feeder 3 and the weight feeder 3 ′ were connected to the screw side feeder 2.
  • the screw corresponding to the first kneading zone 9 includes, in order from the upstream side, a forward (forward feed direction) disc, an orthogonal (neutral) disc, and a screw so that the resin pressure in the first kneading zone is 0.1 MPa or more.
  • Reverse (reverse feed direction) was arranged.
  • the thicknesses of the forward disk, orthogonal disk, and reverse disk were 0.2D (D is the screw diameter).
  • a forward disk was placed long from upstream so that the resin pressure in the second kneading zone 10 was less than 5 MPa, and finally a reverse disk was placed.
  • the forward disk and the reverse disk each had a thickness of 0.5D.
  • the part of the screw corresponding to the third kneading zone 11 is arranged by using a forward disk, an orthogonal disk and a reverse disk in order from the upstream side so that the resin pressure in the water injection dispersion zone 13 is 1 MPa or more.
  • the disc thickness was also 0.1D.
  • Talc was used as the powder.
  • the bulk density of talc was measured by simulating the state where the weight type feeder 3 is put into the screw type side feeder 2. That is, the weight of talc per unit volume is measured after dropping from a height of 2.3 m corresponding to the length of the shooter connecting the weight type feeder 3 and the screw type side feeder 2 and receiving it on the measuring cylinder. I asked for it. By this measurement, it was 0.51.
  • VOC remaining amount in the resin composition was evaluated by a head space method gas chromatograph using the obtained resin composition pellets.
  • the resin composition which does not devolatilize water by only melt kneading is used as a standard, it is preferable that the VOC remaining amount is small.
  • the total supply amount of polypropylene pellets, rubber pellets, and talc supplied into the biaxial kneading extruder 100 was 490 kg / hour.
  • the effective volume of talc supplied from the weight type feeder 3 to the screw type side feeder 2 was 144 L / hour, and the conveying capacity of the screw type side feeder 2 was 801 L / hour. That is, the conveying capacity of the screw-type side feeder 2 was about 5.6 times the volume per unit time of talc supplied from the weight-type feeder 3 to the screw-type side feeder 2.
  • the raw material was melt-kneaded at a screw rotation speed of 1350 rpm of the biaxial kneading extruder 100, and vacuum suction was performed from the first vent port and the second vent port without pouring water from the water injection port.
  • the amount of VOC remaining in the obtained resin composition pellets was set to 1.0 as a reference.
  • Example 1 Using the same apparatus as in Comparative Example 1, a resin composition was produced under different conditions.
  • Example 2 A resin composition was produced under the same conditions as in Example 1 except that 4 parts by weight of water was injected from the water injection port 5 to the total supply weight of the raw materials. The amount of VOC remaining in the obtained resin composition pellets was good, being reduced to 0.51 on the basis of Comparative Example 1 where water injection was not volatilized.
  • Example 2 A resin composition was produced under the same conditions as in Example 1 except that 5 parts by weight of water was poured from the water inlet 5 into the total supply weight of the raw materials. As a result, the resin composition extruded from the biaxial kneader-extruder 100 was foamed, and pellets could not be produced.
  • Example 3 A resin composition was produced under the same conditions as in Example 1 except that the total supply amount of polypropylene pellets, rubber pellets, and talc supplied into the biaxial kneading extruder 100 was 600 kg / hour.
  • the effective volume of talc supplied from the weight type feeder 3 to the screw type side feeder 2 was 176 L / hour, and the conveying capacity of the screw type side feeder was 801 L / hour. That is, the conveying ability of the screw-type side feeder was about 4.6 times the volume per unit time of talc supplied from the weight-type feeder 3 to the screw-type side feeder 2.
  • the amount of VOC remaining in the obtained resin composition pellets was reduced to 0.68 on the basis of Comparative Example 1 in which water injection was not volatilized. Compared with Comparative Example 1, productivity was improved by 20%, and VOC was reduced by 31%, which was favorable.
  • Example 4 A resin composition was produced under the same conditions as in Example 2 except that the screw rotation speed of the biaxial kneading extruder 100 was 1650 rpm. The amount of VOC remaining in the obtained resin composition pellets was good, being reduced to 0.46 on the basis of Comparative Example 1 where water injection was not volatilized.
  • the present invention can be used in a method for producing a resin composition in which a thermoplastic resin and powder are melt-kneaded.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
  • Extrusion Moulding Of Plastics Or The Like (AREA)

Abstract

L'invention concerne un nouveau procédé de fabrication d'une composition de résine selon lequel une résine thermoplastique et une poudre sont fondues et malaxées l'une avec l'autre, ou similaire. Le procédé de fabrication selon la présente invention est un procédé de fabrication d'une composition de résine à l'aide d'une machine biaxiale de malaxage et d'extrusion. La machine biaxiale de malaxage et d'extrusion comprend un cylindre (50) conçu pour comprendre une première zone de malaxage (9), une seconde zone de malaxage (10) et une zone de déversement d'eau et de dégagement des matières volatiles (15). La zone de déversement d'eau et de dégagement des matières volatiles (15) comprend une zone de déversement d'eau et de dispersion (13). Le procédé comprend une étape consistant à alimenter la zone de déversement d'eau et de dispersion (13) en eau et à malaxer et disperser une composition de résine pour vaporiser et éliminer un constituant volatil présent dans la composition de résine en même temps que l'eau.
PCT/JP2017/014854 2016-04-15 2017-04-11 Procédé de fabrication d'une composition de résine et machine biaxiale de malaxage et d'extrusion WO2017179584A1 (fr)

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CN111961318A (zh) * 2020-08-20 2020-11-20 珠海格力绿色再生资源有限公司 一种增强型pbt树脂组合物及其制备方法和析出检测方法
WO2021237655A1 (fr) * 2020-05-26 2021-12-02 金发科技股份有限公司 Procédé et dispositif d'extrusion et de mélange de polymère assistés par additif liquide, et leur utilisation
CN113977908A (zh) * 2021-11-26 2022-01-28 中化泉州能源科技有限责任公司 一种双螺杆挤出机的组合螺杆及生产低气味聚烯烃的工艺
JP2022518566A (ja) * 2019-11-25 2022-03-15 エルジー・ケム・リミテッド 押出装置
CN115044986A (zh) * 2022-06-30 2022-09-13 武汉纺织大学 切片纺免干燥制备聚酯纤维或聚酰胺纤维的装置和方法
WO2022259984A1 (fr) * 2021-06-09 2022-12-15 株式会社日本製鋼所 Procédé et appareil de fabrication d'un matériau composite en résine
WO2023166780A1 (fr) * 2022-03-03 2023-09-07 株式会社日本製鋼所 Dispositif d'alimentation et machine de moulage par injection

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WO2023151996A1 (fr) * 2022-02-10 2023-08-17 Totalenergies Onetech Composition de polyéthylène pour moulage par injection

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JP2022518566A (ja) * 2019-11-25 2022-03-15 エルジー・ケム・リミテッド 押出装置
JP7233799B2 (ja) 2019-11-25 2023-03-07 エルジー・ケム・リミテッド 押出装置
WO2021237655A1 (fr) * 2020-05-26 2021-12-02 金发科技股份有限公司 Procédé et dispositif d'extrusion et de mélange de polymère assistés par additif liquide, et leur utilisation
CN111961318A (zh) * 2020-08-20 2020-11-20 珠海格力绿色再生资源有限公司 一种增强型pbt树脂组合物及其制备方法和析出检测方法
CN111961318B (zh) * 2020-08-20 2022-12-16 珠海格力绿色再生资源有限公司 一种增强型pbt树脂组合物及其制备方法和析出检测方法
WO2022259984A1 (fr) * 2021-06-09 2022-12-15 株式会社日本製鋼所 Procédé et appareil de fabrication d'un matériau composite en résine
CN113977908A (zh) * 2021-11-26 2022-01-28 中化泉州能源科技有限责任公司 一种双螺杆挤出机的组合螺杆及生产低气味聚烯烃的工艺
WO2023166780A1 (fr) * 2022-03-03 2023-09-07 株式会社日本製鋼所 Dispositif d'alimentation et machine de moulage par injection
CN115044986A (zh) * 2022-06-30 2022-09-13 武汉纺织大学 切片纺免干燥制备聚酯纤维或聚酰胺纤维的装置和方法
CN115044986B (zh) * 2022-06-30 2023-07-21 武汉纺织大学 切片纺免干燥制备聚酯纤维或聚酰胺纤维的装置和方法

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