WO2006004005A1 - 熱可塑性樹脂組成物および成形体 - Google Patents
熱可塑性樹脂組成物および成形体 Download PDFInfo
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- WO2006004005A1 WO2006004005A1 PCT/JP2005/012105 JP2005012105W WO2006004005A1 WO 2006004005 A1 WO2006004005 A1 WO 2006004005A1 JP 2005012105 W JP2005012105 W JP 2005012105W WO 2006004005 A1 WO2006004005 A1 WO 2006004005A1
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
- C08L67/00—Compositions of polyesters obtained by reactions forming a carboxylic ester link in the main chain; Compositions of derivatives of such polymers
- C08L67/02—Polyesters derived from dicarboxylic acids and dihydroxy compounds
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
- C08L69/00—Compositions of polycarbonates; Compositions of derivatives of polycarbonates
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08K—Use of inorganic or non-macromolecular organic substances as compounding ingredients
- C08K7/00—Use of ingredients characterised by shape
- C08K7/02—Fibres or whiskers
Definitions
- the present invention is excellent in color tone, hydrolysis resistance, thermal stability, moldability, impact resistance, chemical resistance, dimensional stability, and coloration during production and molding is suppressed, and after molding TECHNICAL FIELD
- the present invention relates to a thermoplastic resin composition with reduced warpage and a molded article comprising the thermoplastic resin composition.
- Polybutylene terephthalate which is a typical engineering plastic among thermoplastic polyester resin, is easy to mold and has physical properties such as mechanical properties, heat resistance, chemical resistance, and fragrance retention. Because of its excellent chemical properties, it is widely used in injection-molded products such as automobile parts, electrical and electronic parts, and precision equipment parts.
- aromatic polycarbonate is also widely used as an engineering plastic with excellent impact resistance, heat resistance, dimensional stability, low warpage, flame resistance, etc., for OA parts, automotive parts, building materials, etc. Has been.
- polybutylene terephthalate has the above-mentioned advantages, but in terms of impact resistance, dimensional stability, low warpage, etc., aromatic polycarbonate is in terms of chemical resistance, moldability, etc. Has weaknesses. Therefore, in order to make use of the advantages by supplementing such mutual weaknesses, it is widely used as a so-called polymer alloy in which both are mixed in a molten state (for example, Non-Patent Document 1).
- Patent Document 1 In order to solve the above problem, use of polybutylene terephthalate having a specific end group concentration has been proposed (Patent Document 1). However, simply adjusting the concentration of the end groups has the following problems.
- Non-patent document 1 Encyclopedia of engineering plastics (Ihouchi edition, published on December 15, 1988, Gihodo Publishing Co., Ltd., P. 200)
- Patent Document 1 Japanese Patent Application Laid-Open No. 2004-18558
- the present invention has been made in view of the above circumstances, and its purpose is excellent in color tone, mechanical properties, thermal stability, moldability, chemical resistance, dimensional stability, and at the time of production and molding.
- Another object of the present invention is to provide a thermoplastic resin composition in which generation of gas at the time is suppressed.
- the inventors of the present invention can easily solve the above problems by controlling the content of the titanium catalyst in the polybutylene terephthalate to a specific range. The inventors have found that this can be solved, and have completed the present invention.
- the first gist of the present invention is that the polybutylene terephthalate (A) and the aromatic polymer A thermoplastic resin composition comprising 1Z19 to 19Z1 (weight ratio) of carbonate (B), wherein the polybutylene terephthalate has a titanium content of more than 33 ppm and not more than 75 ppm as titanium atoms.
- the present invention relates to a thermoplastic rosin composition characterized by comprising terephthalate.
- thermoplastic resin composition according to a preferred embodiment of the present invention further contains a fibrous reinforcing filler, the proportion of which is comprised of polybutylene terephthalate (A) and aromatic polycarbonate (B). 0.1 to 150 parts by weight per 100 parts by weight in total.
- a fibrous reinforcing filler the proportion of which is comprised of polybutylene terephthalate (A) and aromatic polycarbonate (B). 0.1 to 150 parts by weight per 100 parts by weight in total.
- the second gist of the present invention resides in a molded article comprising the above-mentioned thermoplastic resin composition.
- thermoplastic resin having excellent color tone, mechanical properties, thermal stability, moldability, chemical resistance, and dimensional stability, and also suppressing generation of gas during production and molding.
- a fat composition is provided.
- FIG. 1 is an explanatory diagram of an example of an esterification reaction process or a transesterification reaction process employed in the present invention.
- FIG. 2 is an explanatory diagram of an example of a polycondensation process employed in the present invention.
- the polybutylene terephthalate (A) (hereinafter sometimes abbreviated as PBT) used in the present invention will be described.
- the PBT used in the present invention, terephthalic acid unit and 1, 4-butanediol units is a polyester having an ester bond structure consists 50 mole 0/0 or terephthalic acid units dicarboxylic acid units, diol units More than 50 mol% of the polymer consists of 1,4 butanediol unit strength.
- the proportion of terephthalic acid units in all dicarboxylic acid units is preferably 70 mol% or more, more preferably 80 mol%.
- the proportion of 1,4 butane diol units in the total diol units is preferably 70 mol% or more, more preferably 80 mol% or more, particularly preferably 95 mol%. That's it.
- the amount of terephthalic acid units or 1,4 butanediol units is less than 50 mol%, the crystallization rate of PBT decreases, resulting in poor moldability.
- the dicarboxylic acid component other than terephthalic acid is not particularly limited.
- phthalic acid, isophthalic acid, 4,4'-diphenyldicarboxylic acid, 4,4'-diphenyl ether Fragrances such as dicarboxylic acid, 4,4 'monobenzophenone dicarboxylic acid, 4,4'-diphenoxyethane dicarboxylic acid, 4,4'-diphenylsulfone dicarboxylic acid, 2,6 naphthalenedicarboxylic acid Dicarboxylic acid, 1,2-cyclohexanedicarboxylic acid, 1,3 cyclohexanedicarboxylic acid, 1,4-cyclohexanedicarboxylic acid and other alicyclic dicarboxylic acids, malonic acid, succinic acid, dartaric acid, adipic acid And aliphatic dicarboxylic acids such as pimelic acid,
- dicarboxylic acid components can be introduced into the polymer skeleton as a dicarboxylic acid or using a dicarboxylic acid derivative such as a dicarboxylic acid ester or dicarboxylic acid halide as a raw material.
- the diol component other than 1,4 butanediol there is no particular limitation on the diol component other than 1,4 butanediol.
- lactic acid, glycolic acid, m-hydroxybenzoic acid, ⁇ -hydroxybenzoic acid, 6-hydroxy 2-naphthalenecarboxylic acid, p-j8- Hydroxycarboxylic acids such as droxyethoxybenzoic acid, alkoxycarboxylic acids, stearic alcohol, benzyl alcohol, stearic acid, benzoic acid, t-butylbenzoic acid, monofunctional components such as benzoylbenzoic acid, tripotentylvaleric acid, trimellitic acid Trifunctional or higher polyfunctional components such as trimesic acid, pyromellitic acid, gallic acid, trimethylolethane, trimethylolpropane, glycerol and pentaerythritol can be used as the copolymerization component.
- the PBT used in the present invention is obtained by using 1,4 butanediol and terephthalic acid (or dialkyl terephthalate) as raw materials and using a titanium compound as a catalyst.
- titanium catalyst examples include inorganic titanium compounds such as titanium oxide, tetrasalt and titanium, titanium alcoholates such as tetramethyl titanate, tetraisopropyl titanate, and tetrabutyl titanate, and titanium such as tetraphenyl titanate. Examples include phenolate. Of these, tetrabutyl titanate is preferred, and tetrabutyl titanate is preferred.
- tin may be used as a catalyst.
- Tin is usually used as a tin compound, and specific examples thereof include dibutyltin oxide, methylphenol tin oxide, tetraethyltin, hexethylditin oxide, cyclohexhexenoresin stanoxide, Didodecyltin oxide, triethyltin oxide, idiox oxide, triphenyltin hydride oxide, triisobutyltin acetate, dibutyltin diacetate, diphenyltin dilaurate, monobutyltin trichloride, tributyltin chloride, dibutyltin sulfide, butylhydroxytin oxide, Examples include methyl stannic acid, ethyl stannic acid, and butyl stannic acid.
- the amount of addition is usually 200 ppm or less, preferably 10 ppm or less, more preferably 10 ppm or less, more preferably 10 ppm or less as tin atoms. .
- magnesium compounds such as magnesium acetate, magnesium hydroxide, magnesium carbonate, magnesium oxide, magnesium alkoxide, magnesium hydrogen phosphate, calcium acetate, calcium hydroxide, calcium carbonate, calcium oxide
- magnesium compounds such as magnesium acetate, magnesium hydroxide, magnesium carbonate, magnesium oxide, magnesium alkoxide, magnesium hydrogen phosphate, calcium acetate, calcium hydroxide, calcium carbonate, calcium oxide
- trioxide Antimony compounds such as antimony, germanium compounds such as germanium dioxide and germanium tetroxide, manganese compounds, zinc compounds, zirconium compounds, cobalt compounds, orthophosphoric acid, phosphorous acid, hypophosphorous acid, polyphosphoric acid, their esters and metal salts Reaction aids such as phosphorus compounds, sodium hydroxide and sodium benzoate may be used.
- a characteristic of PBT used in the present invention resides in that the titanium content is more than 33 ppm and not more than 75 ppm as titanium atoms.
- the above values are the weight ratio of atoms to PBT.
- the lower limit of the titanium content is preferably 35 ppm, more preferably 40 ppm, and the upper limit is preferably 60 ppm, more preferably 50 ppm. If the titanium content is too low, the polymerization reaction rate of PBT will decrease, so the polymerization reaction will have to proceed at a high temperature for a long time, and only the deterioration of PBT color and thermal degradation will be promoted. The reaction does not proceed during kneading with the aromatic polycarbonate, which causes the mechanical properties of the polymer alloy to deteriorate.
- the titanium content is too high, it will be difficult to control the transesterification reaction, resulting in gas generation during kneading and molding and poor heat stability, and the polymer alloy with the aromatic polycarbonate will be difficult to control. It causes instability of physical properties, deterioration of thermal stability, and deterioration of mechanical properties. Furthermore, since the titanium compound tends to react with the hydroxyl group of the aromatic polycarbonate and color, the color tone is also deteriorated.
- the content of metal atoms such as titanium atoms is measured using a method such as atomic emission, atomic absorption, or inductively coupled plasma (ICP) after recovering the metal in the polymer by a method such as wet ashing. I can do it.
- a method such as atomic emission, atomic absorption, or inductively coupled plasma (ICP) after recovering the metal in the polymer by a method such as wet ashing. I can do it.
- the concentration of the terminal carboxyl group of the PBT used in the present invention is usually 50 ⁇ eqZg or less, preferably 1 to 40 ⁇ eq / g, more preferably 1 to 30 ⁇ eq / g, particularly preferably ⁇ . It is 10-25 ⁇ eqZg.
- the terminal carboxyl group concentration is too high, the hydrolysis resistance tends to deteriorate and the compatibility with the aromatic polycarbonate tends to deteriorate.
- the terminal carboxyl group concentration of PBT can be determined by dissolving PBT in an organic solvent and titrating with an alkali solution such as a sodium hydroxide solution.
- the concentration of the terminal bull group of PBT used in the present invention is usually 0.1 to 15 eq / g, preferably 0.5 to: LO / z eqZg, more preferably 1 to 8 eqZg. . If the terminal bull group concentration is too high, it may cause color deterioration. Terminal vinyl group due to thermal history during molding Since the concentration tends to increase further, when the molding temperature is high, the color tone is further deteriorated in the case of a production method having a recycling process.
- a methoxycarbonyl group derived from the raw material may remain at the end of the PBT, and particularly when dimethyl terephthalate is used as the raw material.
- the methoxycarbonyl terminal generates toxic methanol, formaldehyde, and formic acid by heat generated during molding.
- formic acid can hurt metal molding equipment and associated vacuum equipment.
- the concentration of the terminal methoxycarbonyl group in the PBT used in the present invention is preferably 0.5 eq Zg or less, more preferably 0.3 / z eqZg or less, particularly preferably 0.2 / z eqZg or less, Optimum ⁇ or less than 0.1 eq / g.
- the intrinsic viscosity of the PBT used in the present invention is usually 0.60 to 2.50 dL / g, preferably 0.7 0 to 2. OOdL / g, more preferably 0.080 to L. 20 dL / g, particularly preferably ⁇ or 0.80: L 1 0. If the intrinsic viscosity is less than 0.60 dLZg, the mechanical strength of the molded product will be insufficient, and if it exceeds 50 dLZg, the melt viscosity will increase and the fluidity will deteriorate, resulting in poor moldability and surface properties of the product. Tend to be bad.
- the intrinsic viscosity of PBT is too high or too low, the dispersibility when melt-kneaded with an aromatic polycarbonate tends to be poor.
- the above intrinsic viscosity is a value measured at 30 ° C. using a mixed solvent of phenol Z tetrachloroethane (weight ratio 1Z1).
- PBT production methods are roughly classified into a so-called direct polymerization method using dicarboxylic acid as a main raw material and a transesterification method using dialkyl dicarbonate as a main raw material.
- the former has the difference that water is produced by the initial esterification reaction, and the latter produces alcohol by the initial transesterification reaction.
- the PBT production method includes a raw material supply or a polymer dispensing form force batch method Broadly divided into continuous methods.
- the initial esterification reaction or transesterification reaction is performed in a continuous operation, and the subsequent polycondensation is performed in a batch operation.
- the initial esterification reaction or transesterification reaction is performed in a batch operation, and the subsequent polycondensation is performed.
- the direct polymerization method is preferred from the viewpoints of raw material availability, ease of distillate treatment, superiority of raw material units, and the improvement effect of the present invention.
- a method of continuously supplying raw materials and continuously performing esterification reaction or transesterification reaction is adopted. To do.
- the so-called continuous method is preferred, in which the polycondensation reaction subsequent to the esterification reaction or transesterification reaction is also carried out continuously.
- the esterification reaction tank in the esterification reaction tank, at least a portion of 1,4 butanediol is separated from terephthalic acid (or dialkyl terephthalate) in the presence of a titanium catalyst.
- a step of continuously esterifying (or ester exchange) terephthalic acid (or dialkyl terephthalate) and 1,4 butanediol while being supplied to (or transesterification reactor) is preferably employed.
- 1,4 butanediol supplied together with terephthalic acid or dialkyl terephthalate and Aside from terephthalic acid or dialkyl terephthalate, 1,4 butanediol is supplied to the esterification reactor or transesterification reactor.
- 1,4 butanediol is sometimes referred to as “separately supplied 1,4 butanediol”.
- “separately supplied 1,4 butanediol”, which is also composed of 1,4 butanediol force collected by a condenser or the like, may be referred to as “recycled 1,4 butanediol”. From the viewpoint of effective use of resources and simplicity of equipment, it is preferable to apply “recycled 1,4 butanediol” to “separately supplied 1,4 butanediol”.
- 1,4-butanediol distilled from the esterification reaction tank or the transesterification reaction tank contains water, alcohol, tetrahydrofuran (THF), dihydrofuran and the like in addition to the 1,4 butanediol component. Contains ingredients. Therefore, after collecting 1, 4 butanediol from the above-mentioned distillate with a condenser, etc., or collecting it, separate it from water, alcohol, THF and other components, purify it, and return it to the reaction vessel. Is preferred.
- the reaction liquid phase part refers to the liquid phase side of the gas-liquid interface in the esterification reaction tank or transesterification reaction tank.
- the reaction liquid phase part refers to the liquid phase side of the gas-liquid interface in the esterification reaction tank or transesterification reaction tank.
- the ratio of returning directly to the liquid phase part of the reaction liquid is preferably 30% by weight or more, more preferably 50% by weight or more, particularly preferably 80% by weight or more, and most preferably 90% by weight or more. If the amount of “separately supplied 1, 4 butanediol” returned directly to the reaction liquid phase is small, the titanium catalyst tends to be deactivated.
- the temperature of "separately fed 1,4 butanediol" when returning to the reactor is usually 50 to 220 ° C, preferably 100 to 200 ° C, more preferably 150 to 190 ° C. . If the temperature of “separately supplied 1,4-butanediol” is too high, the amount of THF by-product tends to increase, and if it is too low, the heat load increases and energy loss tends to occur.
- 10% by weight or more of the titanium catalyst used in the esterification reaction (or transesterification reaction) is terephthalic acid (or terephthalic acid). It is preferable to supply directly to the reaction liquid phase part independently of the dialkyl acid).
- the reaction liquid phase part indicates the liquid phase side of the gas-liquid interface in the esterification reaction tank or transesterification reaction tank, and the direct supply to the reaction liquid phase part uses a pipe etc. This means that the catalyst is supplied directly to the liquid phase part without going through the gas phase part of the reactor.
- the proportion of the titanium catalyst added directly to the reaction liquid phase is preferably 30% by weight or more, more preferably 50% by weight or more, particularly preferably 80% by weight or more, and most preferably 90% by weight or more.
- the titanium catalyst can be supplied directly to the reaction liquid phase part of the esterification reaction tank or the transesterification reaction tank with or without being dissolved in a solvent or the like, but the supply amount is stabilized. In order to reduce adverse effects such as heat denaturation due to the heat medium jacket of the reactor, it is preferable to dilute with a solvent such as 1,4 butanediol.
- the concentration at this time is usually 0.01 to 20% by weight, preferably 0.05 to 10% by weight, more preferably 0.08 to 8% by weight as the concentration of the titanium catalyst with respect to the whole solution.
- the water concentration in the solution is usually 0.05 to: L 0% by weight
- the temperature during preparation of the solution is usually 20 to 150 ° from the viewpoint of preventing inactivation and aggregation. C, preferably 30 to 100 ° C, more preferably 40 to 80 ° C.
- the catalyst solution is preferably mixed with separately supplied 1, 4 butanediol via a pipe, etc., and supplied to the esterification reaction tank or transesterification reaction tank in order to prevent deterioration, prevention of precipitation, and deactivation. ,.
- An example of a continuous method employing a direct polymerization method is as follows. That is, the dicarboxylic acid component having terephthalic acid as a main component and the diol component having 1,4 butanediol as a main component are mixed in a raw material mixing tank to form a slurry, and in one or a plurality of ester tanks, In the presence of a titanium catalyst, it is usually 180-260 ° C, preferably 200-245 ° C, more preferably 210-235.
- C temperature usually 10 to 133 kPa, preferably 13 to: L01 kPa, more preferably 60 to 90 kPa (absolute pressure, the same shall apply hereinafter), usually 0.5 to 10 hours, preferably 1 to
- the esterification reaction product obtained in 6 hours is continuously esterified, and the resulting oligomer as a reaction product is transferred to a polycondensation reaction tank, and in the presence of a polycondensation catalyst in one or more polycondensation reaction tanks.
- continuously usually 210-280 ° C, preferably 220-260. C, more preferably 230-250.
- a temperature of C in at least one polycondensation reaction tank, it is usually 20 kPa or less, preferably 10 kPa or less, more preferably 5 kPa or less, and under stirring, usually 2 to 15 hours, preferably 3 to Allow polycondensation reaction in 10 hours.
- the polymer obtained by the polycondensation reaction is usually transferred from the bottom of the polycondensation reaction tank to a polymer extraction die and extracted in the form of a strand, which is cooled with water or after water cooling and then cut with a cutter to form pellets and chips. It is made into granular bodies, such as a shape.
- 1,4 butanediol supplied from the outside to the esterification reaction tank is a raw material slurry or solution, in addition to 1,4 butanediol supplied together with terephthalic acid or dialkyl terephthalate, These are the total of 1,4 butanediol that enters the reaction tank from outside the reaction tank, such as 1,4 butanediol supplied independently and 1,4 butanediol used as the solvent for the catalyst.
- BZTPA value is smaller than 1.1, the conversion rate is decreased and the catalyst is deactivated. When it is larger than 5.0, the thermal efficiency is decreased and the by-products such as THF are increased. It tends to be.
- the value of B / TPA is preferably ⁇ , preferably ⁇ 1.5 to 4.5, more preferably ⁇ to 2. 0 to 4.0, particularly preferably 3.1 to 3.8.
- An example of a continuous method employing the transesterification method is as follows. That is, in the presence or absence of a titanium catalyst in a transesterification reactor or tanks, usually 110 to 260 ° C, preferably 140 to 245. C, more preferably 180-220. The temperature of C, usually 10 to 133 kPa, preferably 13 to 120 kPa, more preferably 60 to: continuously under a pressure of LOlkPa, usually 0.5 to 5 hours, preferably 1 to 3 hours. After the exchange reaction, the resulting oligomer of the ester exchange reaction product is transferred to a polycondensation reaction tank, and is continuously present in the presence or absence of a polycondensation reaction catalyst in one or more polycondensation reaction tanks.
- 210-2 80. C preferably 220-260. C, more preferably 230-250.
- a temperature of C in at least one polycondensation reaction tank, it is usually 20 kPa or less, preferably 10 kPa or less, more preferably 5 kPa or less, with stirring, usually for 2 to 15 hours, preferably 3 to : Perform polycondensation reaction in L0 time.
- the molar ratio of dialkyl terephthalate to 1,4 butanediol preferably satisfies the following formula (II).
- (B) is the number of moles of 1,4-butanediol supplied from the outside to the esterification reactor per unit time
- DAT is the terephthalate supplied from the outside to the esterification reactor per unit time. Indicates the number of moles of dialkyl acid.
- BZDAT is preferably 1.1 to 1.8, more preferably 1.2 to 1.5.
- the esterification reaction or transesterification reaction is preferably performed at a temperature equal to or higher than the boiling point of 1,4 butanediol in order to shorten the reaction time.
- the boiling point of 1,4 butanediol depends on the reaction pressure, but it is 230 ° C at 101. lkPa (atmospheric pressure) and 205 ° C at 50 kPa.
- the esterification reaction tank or the transesterification reaction tank known ones can be used, and any type such as a vertical stirring complete mixing tank, a vertical heat convection mixing tank, a tower type continuous reaction tank, etc. Alternatively, it may be a single tank or a plurality of tanks of the same or different kinds in series or in parallel.
- a stirrer for which a reaction tank having a stirrer is preferable in addition to a normal type including a power unit, a bearing, a shaft, and a stirring blade force, a turbine stator type high-speed rotating stirrer, a disk mill type stirrer, a rotor mill A high-speed rotating type such as a mold stirrer can also be used.
- the form of stirring is not particularly limited, and in addition to a normal stirring method in which the reaction liquid in the reaction tank is directly stirred, such as at the top, bottom, and side of the reaction tank, the reaction liquid may be mixed with a pipe or the like. It is also possible to circulate the reaction liquid by taking the part out of the reactor and stirring it with a line mixer.
- the type of the stirring blade a known one can be selected. Specific examples include a propeller blade, a screw blade, a turbine blade, a fan turbine blade, a disk turbine blade, a fiddler blade, a full zone blade, and a max blend blade. It is done.
- a multi-stage reaction vessel is used, preferably 2 to 5 reaction vessels, and the molecular weight is sequentially increased.
- an initial esterification reaction or an ester exchange reaction is followed by a polycondensation reaction.
- a single reaction tank or a plurality of reaction tanks may be used, but a plurality of reaction tanks are preferably used.
- the form of the reaction tank may be any type such as a vertical stirring complete mixing tank, a vertical heat convection mixing tank, and a tower-type continuous reaction tank, and these may be combined. Among them, a reaction tank having a stirring device is preferable.
- a turbine stator type high-speed rotary stirrer As the stirring device, a turbine stator type high-speed rotary stirrer, a disk mill type stirrer, a rotor mill type stirrer, in addition to a normal type including a power unit, a bearing, a shaft, and a stirring blade force
- a normal type including a power unit, a bearing, a shaft, and a stirring blade force
- the type that rotates at high speeds can also be used.
- the form of stirring is not particularly limited, and in addition to a normal stirring method in which the reaction liquid in the reaction tank is directly stirred, such as at the top, bottom, and side of the reaction tank, It is also possible to circulate the reaction liquid by taking the part out of the reactor and stirring it with a line mixer.
- at least one of the polycondensation reactors is recommended to use a horizontal reactor that has a horizontal axis of rotation and excellent surface renewal and self-cleaning properties.
- the reaction tank in order to suppress coloring and deterioration, and to suppress an increase in the terminal of vinyl group or the like, in at least one reaction tank, it is usually 1.3 kPa or less, preferably 0.5 kPa or less, more preferably 0.3 kPa or less. Under a high vacuum of 225 to 255 ° C., preferably 230 to 250 ° C., more preferably 233 to 245 ° C.
- the polycondensation reaction step of PBT is a relatively low molecular weight by melt polycondensation!
- Solid phase polycondensation solid phase polymerization
- FIG. 1 is an explanatory view of an example of an esterification reaction step or transesterification reaction step employed in the present invention
- FIG. 2 is an explanatory view of an example of a polycondensation step employed in the present invention.
- the raw material terephthalic acid is usually mixed with 1,4-butanediol in a raw material mixing tank (not shown) and transferred from the raw material supply line (1) to the reaction tank (A) in the form of slurry.
- the raw material is dialkyl terephthalate, it is usually fed to the reaction tank (A) in a molten state.
- the titanium catalyst is preferably made into a solution of 1,4 butanediol in a catalyst adjusting tank (not shown) and then supplied from the catalyst supply line (3).
- the catalyst supply line (3) is connected to the recycle line for 1,4 butanediol (2) and mixed. After that, a mode of supplying the liquid phase part of the reaction vessel (A) was shown.
- the gas that also distills from the reaction tank (A) is separated into a high-boiling component and a low-boiling component in the rectifying column (C) via the distillation line (5).
- the main component of the high boiling point component is 1,4 butanediol
- the main component of the low boiling point component is water and THF in the case of the direct polymerization method, and in the case of the transesterification method, ananolone, THF and water.
- the high-boiling components separated in the rectification column (C) are extracted from the extraction line (6), passed through the pump (D), and partly from the recirculation line (2) to the reaction tank (A) Part of it is returned to the rectifying tower (C) from the circulation line (7).
- the surplus is extracted from the extraction line (8).
- the light boiling components separated in the rectification column (C) are extracted from the gas extraction line (9), condensed in the capacitor (G), and passed through the condensate line (10) and then into the tank (F). Is temporarily stored.
- a part of the light boiling components collected in the tank (F) is returned to the rectification column (C) through the extraction line (11), the pump (E) and the circulation line (12), and the remainder is extracted. It is extracted outside through the exit line (13).
- the condenser) is connected to an exhaust device (not shown) via a vent line (14).
- the oligomer produced in the reaction tank (A) is withdrawn via a withdrawal pump (B) and a withdrawal line (4).
- the catalyst supply line (3) is connected to the recirculation line (2), but both may be independent.
- the raw material supply line (1) may be connected to the liquid phase part of the reaction tank (A).
- the oligomer supplied from the extraction line (4) shown in FIG. 1 is polycondensed under reduced pressure in the first polycondensation reaction tank (a) to become a prepolymer, and then extracted. It is supplied to the second polycondensation reaction tank (d) via the extraction gear pump (c) and the extraction line (L1), and further supplied to the third heavy line via the extraction gear pump (e) and the extraction line (L3). It is supplied to the condensation reaction tank (k).
- the third polycondensation reaction tank (k) is a horizontal reaction tank composed of a plurality of stirring blade blocks and equipped with a biaxial self-cleaning type stirring blade.
- polycondensation usually proceeds at a lower pressure than in the first polycondensation reaction tank (a), and in the third polycondensation reaction tank (k), polycondensation proceeds. Goes further and becomes a polymer.
- the obtained polymer is extracted in the form of a strand in which the die head (g) force is also melted through the extraction gear pump (m) and the extraction line (L5), cooled with water, and then rotated with a rotary cutter ( h) is cut by pellet It becomes.
- Reference numerals (L2), (L4), and (L6) are vent lines of the respective polycondensation reaction tanks (a), (d), and (k).
- the aromatic polycarbonate (B) (hereinafter sometimes abbreviated as PC) used in the present invention will be described.
- the PC used in the present invention may be branched and produced by reacting an aromatic hydroxy compound with a carbonic acid diester such as diphenyl carbonate or phosgene.
- Thermoplastic aromatic polycarbonate It is a polymer or copolymer.
- aromatic dihydroxy compounds examples include 2, 2 bis (4-hydroxyphenol) propane (
- the above aromatic dihydroxy compound has a structure substituted with a bromine atom or a group having a siloxane structure in addition to tetraalkylphosphonium sulfonate! / Yo ⁇ .
- monovalent aromatic hydroxy compounds and monovalent aromatic hydroxy compound derivatives such as their chloroformates can be used for the purpose of adjusting the molecular weight and end groups, and specific examples thereof are as follows. Examples include phenol, m- and p-methylphenol, m- and p-propylphenol, p-tert butylphenol, alkylphenols such as p-long chain alkyl-substituted phenol, and derivatives thereof.
- the PC used in the present invention has a polymer having a siloxane structure for the purpose of enhancing flame retardancy.
- a derivative such as dicarboxylic acid or dicarboxylic acid chloride can be copolymerized.
- two or more kinds of PCs may be used in combination.
- the terminal hydroxyl group concentration of the PC used in the present invention is usually 60 eqZg or less, preferably 1 to 50 ⁇ eq / g ⁇ , more preferably 5 to 50 ⁇ eq / g ⁇ , particularly preferably 10 to 45 ⁇ m. 20-40 eqZg is optimal even in eq / g ⁇ .
- the terminal hydroxyl group concentration is higher than 60 eqZg, coloring by titanium derived from PBT becomes intense, and the mechanical properties of the obtained thermoplastic resin composition tend to decrease.
- the terminal hydroxyl group concentration is too small, the compatibility with PBT decreases and the mechanical properties tend to deteriorate.
- the terminal hydroxyl group concentration of PC can be controlled by, for example, reaction conditions such as reaction temperature, catalyst, and composition.
- reaction conditions such as reaction temperature, catalyst, and composition.
- melt polymerization method in which a diester is reacted with carbonic acid, it can be controlled by, for example, the composition ratio of raw materials.
- PC obtained by any of the interfacial polymerization method and the melt polymerization method can be used, but from the viewpoint of easy control of the terminal hydroxyl group concentration, the PC obtained by the melt polymerization method is used. Is preferred.
- the molecular weight of the PC used in the present invention is usually 14000 to 40000, preferably ⁇ 15000 to the viscosity average molecular weight converted from the solution viscosity measured at a temperature of 25 ° C using methylene chloride as a solvent. 30000, more preferred ⁇ is 15000-23000.
- thermoplastic resin composition of the present invention comprises the above-described PBT and PC at 1Z19 to 19Z1 (weight ratio). If the ratio of both components is out of the above range, desired performance utilizing the characteristics of each component cannot be expressed.
- the ratio (weight ratio) between PBT and PC is preferably 1Z9 to 9Z1, and more preferably 1Z4 to 4Zl.
- the thermoplastic resin composition of the present invention may be composed only of the aforementioned PBT and PC, but can contain various components within a range not impairing the effects of the present invention.
- the thermoplastic resin composition of the preferred embodiment of the present invention further contains a fibrous reinforcing filler in addition to the above-described PBT and PC.
- a fibrous reinforcing filler examples include inorganic fibers such as glass fibers, carbon fibers, silica-alumina fibers, zirco-ure fibers, boron fibers, boron nitride fibers, potassium nitride potassium titanate fibers, and metal fibers. Examples thereof include organic fibers such as aromatic polyamide fibers and fluorine resin fibers.
- These fibrous reinforcing fillers can be used in combination of two or more.
- inorganic fibers, particularly glass fibers are preferably used.
- the average fiber diameter of the fibrous reinforcing filler is usually 1 to: LOO ⁇ m, preferably 2 to 50 m, more preferably 3 to 30 ⁇ m, and particularly preferably 5 to 20 ⁇ m. is there.
- the average fiber length is usually 0.1 to 20 mm, preferably 1 to LOmm.
- the fiber-reinforced filler is preferably used after being surface-treated with a sizing agent or a surface treating agent in order to improve the interfacial adhesion with the resin.
- a sizing agent or surface treatment agent include functional compounds such as epoxy compounds, acrylic compounds, isocyanate compounds, silane compounds, and titanate compounds.
- the fiber reinforced filler can be surface-treated in advance with a bundling agent or a surface treatment agent, or a surface treatment can be performed by adding a sizing agent or a surface treatment agent when preparing a thermoplastic resin composition. You can also do it.
- the proportion of the fibrous reinforcing filler is usually 0.1 to 150 parts by weight, preferably 5 to: LOO parts by weight with respect to 100 parts by weight of the total of polybutylene terephthalate (A) and aromatic polycarbonate HB). It is.
- the proportion of the fibrous reinforcing filler is less than 0.1 part by weight, the effect of the blending of the fibrous reinforcing filler is not expressed, and when it exceeds 150 parts by weight, melt kneading and molding of the resin composition are not possible. It can be difficult.
- Other fillers can also be blended in the thermoplastic resin composition of the present invention.
- Other fillers include, for example, plate-like inorganic fillers, ceramic beads, asbestos, wollastonite, talc, clay, my strength, zeolite, kaolin, potassium titanate, barium sulfate, acid titanium, and oxide key. Examples include elemental, acid aluminum, and magnesium hydroxide.
- the plate-like inorganic filler By blending the plate-like inorganic filler, the anisotropy and warpage of the molded product can be reduced.
- the plate-like inorganic filler include glass flakes, mica, and metal foil. Of these, glass flakes are preferred.
- the amount of these fillers used is polybutylene terephthalate. It is usually 1 to: LOO parts by weight, preferably 5 to 50 parts by weight based on 100 parts by weight of the total of the rate (A) and the aromatic polycarbonate (B).
- the thermoplastic resin composition of the present invention includes 2,6-di-tert-butyl-4-octylphenol, pentaerythrityl-tetrakis [3- (3 ', 5,1 t-butyl 4,1 Hydroxyphenol) propionate], phenol compounds such as dilauryl 1,3,3, dithiodipropionate, thioether compounds such as pentaerythrityl-tetrakis (3-laurylthiodipropionate), triphenylphosphite, tris Antioxidants such as (noyulferyl) phosphite, tris (2,4-di-tert-butylphenol) phosphite and other phosphorus compounds, noraffin tuss, microcrystalline wax, polyethylene wax, montanic acid In addition, a long-chain fatty acid represented by ester of montanate and esters thereof, a release agent such as silicone oil, and the like may be added.
- a flame retardant can be blended with the thermoplastic resin composition of the present invention in order to impart flame retardancy.
- the flame retardant is not particularly limited, and examples thereof include organic halogen compounds, antimony compounds, phosphorus compounds, polysiloxane compounds, other organic flame retardants, and inorganic flame retardants.
- organic halogen compound include brominated polycarbonate, brominated epoxy resin, brominated phenoxy resin, brominated polyurethane ether resin, brominated polystyrene resin, brominated bisphenol A, pentabromobenzyl polyatariate. Rate and the like.
- the antimony compounds include triacid-antimony, pentaacid-antimony, sodium antimonate, and the like.
- Examples of the phosphorus compound include phosphoric acid ester, polyphosphoric acid, ammonium polyphosphate, and red phosphorus.
- Examples of other organic flame retardants include nitrogen compounds such as melamine and cyanuric acid.
- Examples of other inorganic flame retardants include aluminum hydroxide, magnesium hydroxide, silicon compounds, and boron compounds.
- thermoplastic resin composition of the present invention includes polyethylene, polypropylene, polystyrene, polyacrylonitrile, polymethacrylic acid ester, ABS resin, polyamide, polyphenylene sulfide, polyethylene terephthalate, liquid crystal polyester, polyacetal, polyethylene.
- Thermosetting resins such as thermoplastic resins such as lenoxide, phenol resins, melamine resins, silicone resins, and epoxy resins can be blended. These thermoplastic oils And thermosetting rosin can be used in combination of two or more.
- thermoplastic rosin composition of the present invention may contain conventional additives and the like.
- additives examples include a lubricant such as a heat stabilizer, a lubricant, a catalyst deactivator, a crystal nucleating agent, and a crystallization accelerator. These additives can be added during polymerization or after polymerization. Furthermore, in order to impart desired performance, stabilizers such as UV absorbers and weathering stabilizers, colorants such as dyes and pigments, antistatic agents, foaming agents, plasticizers, impact resistance improvers, etc. may be blended. I can do it.
- stabilizers such as UV absorbers and weathering stabilizers, colorants such as dyes and pigments, antistatic agents, foaming agents, plasticizers, impact resistance improvers, etc. may be blended. I can do it.
- thermoplastic resin composition of the present invention is usually produced by a melt kneading method using a single-screw or twin-screw extruder, but it improves dispersibility and improves mechanical properties.
- a twin screw extruder it is preferable to use a twin screw extruder.
- an extruder having a vent port in order to prevent a decrease in molecular weight during melt kneading.
- the method for supplying PBT and PC to the extruder is not particularly limited, but a method of supplying both in a batch by mixing both in advance, and mixing in a hopper of the extruder using a plurality of feeders. Examples thereof include a method of supplying, a method of supplying one resin to the extruder, a method of supplying the other resin from the middle of the extruder, and a method combining these.
- the catalyst concentration in the PBT is controlled within a certain range, the controllability of the transesterification reaction during melt kneading is greatly improved compared to the conventional case.
- acid phosphates such as phosphites and phosphates, particularly mono (di) alkyl phosphates, can be used as catalyst deactivators. These additive amounts are usually 0.001 to 5 parts by weight, preferably 0.00.
- the molding method of the thermoplastic resin composition of the present invention is not particularly limited, and is a molding method generally used for thermoplastic resins, that is, injection molding, hollow molding, extrusion molding, press. A molding method such as molding can be applied.
- thermoplastic resin composition of the present invention is excellent in color tone, hydrolysis resistance, thermal stability, moldability, impact resistance, chemical resistance and dimensional stability, and at the time of production and molding. The coloration of is suppressed, and the industrial utility value is high.
- Example [0097] Hereinafter, the present invention will be described in more detail by way of examples. However, the present invention is not limited to the following examples as long as the gist thereof is not exceeded.
- the physical properties and evaluation methods used in the following examples are as follows.
- the acid value and saponification value power were also calculated by the following calculation formula (III).
- the acid value was obtained by dissolving the oligomer in dimethylformamide and titrating with a 0.1N KOHZ methanol solution.
- the saponification value was determined by hydrolyzing the oligomer with a 0.5N KOH / ethanol solution and titrating with 0.5N hydrochloric acid.
- Esterification rate ((Saponification value—Acid value) Z Genation value) X I 00 ⁇ (III)
- PBT was wet-decomposed with high-purity sulfuric acid and nitric acid for the electronics industry and measured using a high-resolution ICP (Inductively Coupled Plasma) —MS (MassSpectrometer) (manufactured by ThermoQuestnet).
- ICP Inductively Coupled Plasma
- MS MassSpectrometer
- the temperature was increased from room temperature to 300 ° C at a temperature increase rate of 20 ° CZ min, then the temperature was decreased to 80 ° C at a temperature decrease rate of 20 ° CZmin.
- the temperature of the thermal peak was defined as the temperature-falling crystallization temperature. The higher the Tc, the shorter the molding site where the crystallization speed is faster.
- Terminal carboxyl group concentration of PBT 0.5 g of PBT or oligomer was dissolved in 25 mL of benzyl alcohol and titrated using sodium hydroxide (DO. 01 mol ZL benzyl alcohol solution).
- a color difference meter ( ⁇ -300 ⁇ ) manufactured by Nippon Denshoku Co., Ltd. was used, and the b value in the L, a, b color system was evaluated. A lower value indicates less yellowing and a better color tone.
- Capillograph Type 1B is filled with pellets, preheated at 270 ° C for 5 minutes, and then measured for melt viscosity at a shear rate of 91 (sec-1) (melt Viscosity A) was held at that temperature for 30 minutes, and then the melt viscosity was measured again (melt viscosity B), and the ratio of these (melt viscosity BZ melt viscosity A) was calculated. Larger values indicate better melting and thermal stability.
- PBT was produced in the following manner.
- a slurry at 60 ° C mixed with 1.80 moles of terephthalic acid at a ratio of 1.80 moles of 1,4 butanediol was passed through the raw material supply line (1) in advance in the ester solution. It was continuously fed to a reaction vessel (A) for ester cake having a screw type stirrer filled with 99% PBT oligomer so as to be 40. OkgZh.
- the bottom component of the 185 ° C rectification column (C) is supplied at 18.4 kgZh from the recirculation line (2), and 6% of 65 ° C tetrabutyl titanate is used as the catalyst from the catalyst supply line (3).
- a 0 wt% 1,4-butanediol solution was fed at 127 gZh (40 ppm relative to the theoretical polymer yield). The water content in this solution was 0.20% by weight.
- the internal temperature of the reaction tank (A) is 230 ° C
- the pressure is 78 kPa
- the produced water, THF, and excess 1,4 butanediol are distilled from the distillation line (5),
- In (C) a high-boiling component and a low-boiling component were separated.
- the high-boiling component at the bottom of the column after the system is stabilized is 98% by weight or more of 1,4 butanediol.
- the extraction line (8) the liquid level in the rectification column (C) is constant. Part of it was extracted outside.
- low-boiling components were extracted from the top of the tower in the form of gas, condensed with a condenser (G), and extracted outside from the extraction line (13) so that the liquid level in the tank (F) was constant.
- a certain amount of the oligomer produced in the reaction tank (A) was removed using the pump (B) and the extraction line (4) The liquid level was controlled so that the average residence time of the liquid in the reaction tank (A) was 3. Ohr. Extraction line 4 forces The extracted oligomer was continuously supplied to the first polycondensation reaction tank (a). After the system was stabilized, the ester ratio of the oligomer collected at the outlet of the reaction vessel (A) was 97.4%.
- the internal temperature of the first polycondensation reaction tank (a) was 240 ° C, the pressure was 2.7 kPa, and the liquid level was controlled so that the residence time was 120 minutes.
- An initial polycondensation reaction was performed while extracting water, THF, and 1,4 butanediol from a vent line (L2) connected to a decompressor (not shown). The extracted reaction liquid was continuously supplied to the second polycondensation reaction tank (d).
- the internal temperature of the second polycondensation reaction tank (d) was 245 ° C, the pressure was 140 Pa, the liquid level was controlled so that the residence time was 60 minutes, and connected to a decompressor (not shown).
- the polycondensation reaction was further carried out while extracting water, THF, and 1,4 butanediol from the vent line (L4).
- the obtained polymer was continuously supplied to the third polycondensation reaction tank (k) via the extraction line (L3) by the extraction gear pump (e).
- the internal temperature of the third polycondensation reaction tank (k) was 239 ° C, the pressure was 600 Pa, the residence time was 80 minutes, and the polycondensation reaction was advanced.
- the obtained polymer was continuously extracted in a strand form from the die head (g) and cut with a rotary cutter (h).
- the terminal carboxyl group concentration of the obtained PBT was 22 eqZg.
- the obtained PBT had excellent color tone and low solution haze.
- the analysis values are summarized in Table 1.
- PC with viscosity average molecular weight of 21000 and terminal hydroxyl group concentration of 31 ⁇ eqZg obtained by the above PBT and melt polymerization method (Mitsubishi Engineering Plastics Co., Ltd., trade name “NOVAREX 7022J”) was mixed at a weight ratio of 7: 3 and melt-kneaded at 260 ° C using a Nippon Steel Corporation twin screw extruder (inner diameter 30 mm) to obtain a polymer alloy of PBT and PC.
- the obtained polymer alloy was excellent in color tone, mechanical strength, and thermal stability.
- Table 1 The results are summarized in Table 1.
- Example 1 the internal temperature of the second polycondensation reaction tank (d) was 246 ° C, the pressure was 180 Pa, the residence time was 80 minutes, the internal temperature of the third polycondensation reaction tank (k) was 243 ° C, The same procedure as in Example 1 was conducted except that the pressure was 900 Pa and the residence time was 90 minutes. PBT with a terminal carboxyl group concentration of 35 eqZg, excellent color tone and low solution haze was obtained. Using this PBT, the same as in Example 1 In this way, a polymer alloy was obtained. The obtained polymer alloy was excellent in color tone, mechanical strength, and thermal stability. The results are summarized in Table 1.
- Example 1 the terminal hydroxyl group concentration obtained by the interfacial polymerization method was 2 eqZgPC (Mitsubishi Engineering Plastics Co., Ltd., trade name “NOVAREX 7022J”). It was. A polymer alloy excellent in color tone, mechanical strength, and thermal stability was obtained. The results are summarized in Table 1.
- Example 1 the catalyst solution was supplied at 64 gZh, the internal temperature of the second polycondensation reaction tank (d) was 247 ° C, the pressure was 140 Pa, the residence time was 90 minutes, the third polycondensation reaction tank (k) The same procedure as in Example 1 was conducted except that the internal temperature was 247 ° C and the residence time was 90 minutes.
- the terminal beryl group concentration of the obtained PBT was high and the color tone deteriorated. In addition, the color tone and mechanical strength of the obtained polymer alloy also decreased. The results are summarized in Table 1.
- Example 1 except that the catalyst solution was supplied at 254 gZh, the pressure in the second polycondensation reaction tank (d) was 200 Pa, the pressure in the third polycondensation reaction tank (k) was 650 Pa, and the residence time was 70 minutes. The same operation as in Example 1 was performed. The terminal vinyl group concentration of the obtained PBT was poor in high color tone and solution haze. In addition, the color tone, mechanical strength, and thermal stability of the obtained polymer alloy were also lowered. The results are summarized in Table 1.
- a polymer alloy was obtained in the same manner as in Example 1 using the above PBT.
- the resulting polymer alloy has a low mechanical strength and a low thermal stability. The results are summarized in Table 1.
- Example 2 100 parts by weight of PBT and PC with a 7 to 3 weight ratio were batched. After putting in a par and melting, 30 parts by weight of glass fiber was added to another feeder to obtain a glass fiber reinforced polymer alloy. The results of the obtained glass fiber reinforced polymer alloy are shown in Table 2.
- a trade name “T-187” (diameter 13 m, length 3 mm) manufactured by Nippon Electric Glass Co., Ltd. was used.
- a glass fiber reinforced polymer alloy was obtained in the same manner as in Example 4 using PBT and PC used in Comparative Example 1. The results of the obtained glass fiber reinforced polymer alloy are shown in Table 2. Color and mechanical strength deteriorated.
- a glass fiber reinforced polymer alloy was obtained in the same manner as in Example 4 using PBT and PC used in Comparative Example 3. The results of the obtained glass fiber reinforced polymer alloy are shown in Table 2. Color tone, mechanical strength, and thermal stability deteriorated.
- Example 4 Comparative example 4 Comparative example 5 b value 9 11 13 Tensile strength (Mpa) 131 121 122 Tensile elongation (%) 2.5 2.4 2.3 Charbi impact value (kJ / m 2 ) 9.2 8.2 8.1 Melt viscosity reduction ratio (%) 48 47 39
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WO2007074603A1 (ja) * | 2005-12-27 | 2007-07-05 | Mitsubishi Chemical Corporation | 芳香族ポリカーボネート樹脂組成物および樹脂成形品 |
JP2007176969A (ja) * | 2005-12-27 | 2007-07-12 | Mitsubishi Chemicals Corp | 芳香族ポリカーボネート樹脂組成物および樹脂成形品 |
JP2007176970A (ja) * | 2005-12-27 | 2007-07-12 | Mitsubishi Chemicals Corp | 芳香族ポリカーボネート樹脂組成物および樹脂成形品 |
WO2011087141A1 (ja) * | 2010-01-15 | 2011-07-21 | 帝人化成株式会社 | ポリカーボネート樹脂組成物 |
JP2011144283A (ja) * | 2010-01-15 | 2011-07-28 | Teijin Chem Ltd | ポリカーボネート樹脂組成物 |
JP2012036323A (ja) * | 2010-08-10 | 2012-02-23 | Teijin Chem Ltd | 熱可塑性樹脂組成物 |
JP2013018864A (ja) * | 2011-07-11 | 2013-01-31 | Teijin Chem Ltd | ポリカーボネート樹脂組成物およびその成形品 |
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CN112625404B (zh) * | 2020-11-25 | 2022-03-01 | 金发科技股份有限公司 | 一种具有高强度、低翘曲和高热变形温度的玻纤增强pbt/pc合金及其制备方法和应用 |
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WO2007074603A1 (ja) * | 2005-12-27 | 2007-07-05 | Mitsubishi Chemical Corporation | 芳香族ポリカーボネート樹脂組成物および樹脂成形品 |
JP2007176969A (ja) * | 2005-12-27 | 2007-07-12 | Mitsubishi Chemicals Corp | 芳香族ポリカーボネート樹脂組成物および樹脂成形品 |
JP2007176970A (ja) * | 2005-12-27 | 2007-07-12 | Mitsubishi Chemicals Corp | 芳香族ポリカーボネート樹脂組成物および樹脂成形品 |
WO2011087141A1 (ja) * | 2010-01-15 | 2011-07-21 | 帝人化成株式会社 | ポリカーボネート樹脂組成物 |
JP2011144283A (ja) * | 2010-01-15 | 2011-07-28 | Teijin Chem Ltd | ポリカーボネート樹脂組成物 |
US8648165B2 (en) | 2010-01-15 | 2014-02-11 | Teijin Chemicals, Ltd. | Polycarbonate resin composition |
JP2012036323A (ja) * | 2010-08-10 | 2012-02-23 | Teijin Chem Ltd | 熱可塑性樹脂組成物 |
JP2013018864A (ja) * | 2011-07-11 | 2013-01-31 | Teijin Chem Ltd | ポリカーボネート樹脂組成物およびその成形品 |
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