JP5644038B2 - Resin composition - Google Patents

Description

  The present invention relates to a polyphenylene sulfide resin composition, and more particularly to a polyphenylene sulfide resin composition having a high crystallization rate and improved dimensional stability and processability upon heating, and a method for producing the same.

  Polyphenylene sulfide (hereinafter abbreviated as PPS) is attracting attention as an electrical / electronic device member and an automotive device member by taking advantage of its excellent heat resistance, chemical resistance and flame retardancy. Further, it can be molded into various molded parts, films, sheets, fibers, etc. by injection molding, extrusion molding, etc., and is widely used in fields requiring heat resistance, chemical resistance, and flame resistance.

  A method for producing PPS is disclosed in Patent Document 1 and the like. However, it is generally known that PPS produced by these production methods is fragile and requires a high molding processing temperature (particularly the mold temperature).

  As a method for improving the processability of PPS, a method of adding an oligomeric ester (Patent Document 2), a method of adding a monomeric carboxylic acid ester (Patent Document 3), a method of adding another thioether (Patent Document 4) ), A method of adding polyalkylene glycol (Patent Document 5). However, in any of the methods, the heat resistance of the additive is poor so that evaporative gas or decomposition gas is generated during the molding process, or because the additive has a low molecular weight, the additive moves to the surface of the molded product. It has a problem of contaminating the surface of the molded product.

On the other hand, PPS has high heat resistance and a crystal melting temperature as high as 280 ° C. Therefore, in order to obtain fluidity, it is necessary to set the molding temperature to 300 ° C. or higher. For this reason, when trying to obtain a composite material with another general-purpose engineering plastic, the general-purpose engineering plastic is decomposed, so that there is a problem that the material is limited.
Japanese Patent Publication No. 45-3368 JP 62-45654 A JP-A-62-230848 JP-A-62-230849 JP-A-6-207102

  The present invention provides a PPS resin composition having high fluidity, in addition to excellent properties such as heat resistance, chemical resistance and flame retardancy of PPS, in addition to high crystallization speed, further improving thermal characteristics. It is intended.

The above-mentioned problem is composed of PPS 92 to 99.9% by weight and polyalkylene terephthalate 0.1 to 8% by weight with an intrinsic viscosity of 0.5 to 1.1. This is solved by the resin composition characterized in that the temperature-falling crystallization temperature measured in (2) is 230 to 250 ° C.

  Specifically, the use of the PPS resin of the present invention is a fiber, a film, a resin molded product, etc., and can provide PPS excellent in crystallinity, fluidity, and dimensional stability during heating.

  Hereinafter, the present invention will be described in detail.

The first invention is constituted from 92 to 99.9% by weight of polyphenylene sulfide and poly ethylene terephthalate 0.1 to 8 wt%, it was measured at a temperature decreasing rate 16 ° C. / min in differential scanning calorimetry (DSC) measurements The resin composition is characterized in that the temperature-falling crystallization temperature is 230 to 250 ° C.

  PPS which is a main component of the resin composition of the present invention is a polymer having a repeating unit represented by the following structural formula, and 70 mol% of a polymer containing the repeating unit represented by the following structural formula from the viewpoint of heat resistance. More preferably, 90 mol% or more is preferable.

  In addition, the PPS resin can comprise 30 mol% or less of the repeating units with repeating units having the following structural formula.

  The resin composition of the present invention is characterized in that PPS is composed of 92 to 99.9% by weight. By making PPS 92 weight% or more, it can be set as PPS excellent in characteristics, such as heat resistance, chemical resistance, and a flame retardance.

The resin composition of the present invention include poly ethylene terephthalate.

Po triethylene terephthalate has excellent thermal stability, and can be used more preferably because it is relatively inexpensive polymers.

The resin composition of the present invention is characterized in that poly ethylene terephthalate is composed of 0.1 to 8 wt%. Poly ethylene terephthalate in this range, flowability and crystallinity of the resin composition is dramatically improved (see Figure). Originally, PPS has a high melting point of 285 ° C., and it is necessary to heat it to 300 ° C. or higher in order to obtain fluidity. It has been found that by using the resin composition of the present invention, the melting point does not change, but the fluidity at the melting point or higher is dramatically improved and fluidized even at 290 ° C. By using such a resin composition, it was possible to achieve both moldability and dimensional stability.

The cause is not clear, it is believed that poly ethylene terephthalate enters the resin composition between the PPS molecules are fluidized plasticized. In addition, by poly ethylene terephthalate enters between PPS molecules, a benzene ring of a benzene ring and PPS poly ethylene terephthalate is stacked, it is considered that to improve the crystallinity upon cooling. For this reason, the content of poly ethylene terephthalate is less than 0.1 wt%, the fluidity and crystallinity is degraded. On the other hand, if it is more than 8% by weight, the excellent properties of the PPS resin, such as heat resistance, chemical resistance and flame retardancy, cannot be obtained. Furthermore, the strength of the final product poly ethylene terephthalate becomes foreign matter is decreased. Preferably it is 0.1 to 5 weight%.

  The resin composition of the present invention is characterized in that the temperature-falling crystallization temperature (Tc ′) measured at a temperature-falling rate of 16 ° C./min by differential scanning calorimetry (DSC) measurement is 230 to 250 ° C. By setting it as such a range, the heat resistance of a resin composition improves, and the mechanical strength of the final product using this resin composition improves. Preferably it is 240-250 degreeC.

  The temperature increase crystallization temperature of the resin composition of the present invention measured by DSC measurement at a temperature increase rate of 16 ° C./min is not particularly limited, but moldability is improved by setting the temperature increase crystallization temperature (Tc) to 130 ° C. or less. Tend to improve.

The resin composition of the present invention preferably has a melt viscosity of 200 Pa · sec or less measured at a shear rate of 1216 sec ^{−1 at} 290 ° C. If it exceeds 200 Pa · sec, an unstable flow state is likely to occur during molding, and productivity tends to deteriorate particularly when molding with a large free surface such as melt spinning. By controlling the melt viscosity at the molding temperature to be low, the flow state is stabilized and productivity tends to be improved.

  The melt viscosity is a value measured by a capillary rheometer (Toyo Seiki Seisakusho Co., Ltd. Capillograph Type 1B).

  Since the resin composition obtained as described above has a crystallization rate that is significantly faster than that of conventional PPS, it can be sufficiently crystallized by injection molding even with a low-temperature mold to obtain a molded product having excellent heat resistance. be able to. In addition, when the resin composition of the present invention is formed into a fiber, the spinning temperature can be lowered, and since the crystallization speed is fast, the heat setting temperature of the drawing process can also be lowered, so that energy saving in the spinning process can be achieved. Great effect. Further, since molding and spinning can be performed at a low temperature, the contamination of the base is reduced as compared with the conventional PPS, and the productivity is improved.

  If necessary, the PPS composition of the present invention may include glass fiber, carbon fiber, ceramic fiber such as alumina fiber, aramid fiber, wholly aromatic polyester fiber, metal fiber, reinforcing filler such as potassium titanate whisker, calcium carbonate, Mica, talc, silica, barium sulfate, calcium sulfate, kaolin, clay, pyroferrite, bentonite, sericite, zeolite, nepheline cinnite, attapulgite, wollastonite, PMF, ferrite, calcium silicate, magnesium carbonate, dolomite, three Inorganic filler such as antimony oxide, zinc oxide, titanium oxide, magnesium oxide, iron oxide, molybdenum disulfide, graphite, gypsum, glass beads, glass powder, glass balloon, quartz, quartz glass, and organic and inorganic pigments Is also possible A.

  Examples of the glass fiber include a chopped strand having a fiber length of 1.5 to 12 mm, a fiber diameter of 3 to 24 μm, a milled fiber having a fiber diameter of 3 to 8 μm, and glass flakes and glass powder of 325 mesh or less.

  Also, release agents such as wax, silane and titanate coupling agents, lubricants, heat stabilizers, weathering stabilizers, crystal nucleating agents, foaming agents, rust inhibitors, ion trap agents, flame retardants, flame retardants An auxiliary agent or the like may be added as necessary.

  Furthermore, it is also possible to add a small amount of another polymer to the resin composition of the present invention to impart other physical properties. Polymers to be added include polyethylene, polybutadiene, polyisoprene, polychloroprene, polystyrene, polybutene, poly α-methylstyrene, polyvinyl acetate, polyvinyl chloride, polyacrylic ester, polymethacrylic ester, polyacrylonitrile, nylon 6, Polyamide such as nylon 66, nylon 610, nylon 12, nylon 11, nylon 46, polyester such as polyarylate, polyurethane, polyacetal, polycarbonate, polyphenylene oxide, polysulfone, polyethersulfone, polyallylsulfone, polyphenylene sulfide sulfone, polyetherketone , Polyphenylene sulfide ketone, polyetheretherketone, polyimide, polyamideimide, silicone resin, Carboxymethyl resins, homopolymers, such as fluorine resin, random or block, graft copolymers and mixtures thereof or a reformate, and the like.

Next, the manufacturing method of the resin composition of this invention is demonstrated in detail.

Method for producing the resin composition of the present invention is characterized by melt-kneading from 92 to 99.9% by weight polyphenylene sulfide and poly ethylene terephthalate 0.1 to 8 wt% at a temperature of 280 to 350 ° C..

  The PPS used in the production method of the present invention is a polymer having a repeating unit represented by the following structural formula, and from the viewpoint of heat resistance, 70 mol% or more of a polymer containing the repeating unit represented by the following structural formula is used. Preferably it contains 90 mol% or more.

  From the viewpoint of heat resistance, a polymer containing 70 mol% or more, particularly 90 mol% or more of the repeating unit represented by the above structural formula is preferable. In addition, the PPS resin can comprise 30 mol% or less of the repeating units with repeating units having the following structural formula.

  The production method of the present invention is characterized in that PPS is 92 to 99.9% by weight. By making the supply amount of PPS within this range, the PPS content of the resin composition can be 92 to 99.9% by weight, and the obtained resin composition has heat resistance, chemical resistance and flame retardancy. Etc., and can have excellent characteristics of PPS.

  The shape of PPS used in the production method of the present invention is not particularly limited, and examples thereof include pellets, flakes, granules, and powders.

The method for producing the resin composition of the present invention include poly ethylene terephthalate is used.

Examples of the poly ethylene terephthalate, include polymers obtained by using a diol component and terephthalic acid component, the diol component, their derivatives with ethylene glycol Contact and ester-forming ability and the like, ethylene glycol or esters derivatives having a derivative thereof and terephthalic acid or ester-forming ability with a forming ability, the polycondensation of polyethylene terephthalate that obtained is used.

Production method of the present invention is characterized by poly ethylene terephthalate supplies in the range of 0.1 to 8 wt%. The supply amount of poly ethylene terephthalate in this range, it is the content of poly ethylene terephthalate resin composition to 0.1 to 8 wt%, crystalline swimming flowability of the resin composition is dramatically To improve.

The intrinsic viscosity of the polyalkylene terephthalate used in the production method of the present invention is Ru 0.5 to 1.1 Der. The intrinsic viscosity mentioned here can be replaced with the molecular weight of polyalkylene terephthalate, and the molecular weight corresponding to the intrinsic viscosity of 0.5 to 1.1 is 10,000 to 30,000. When the intrinsic viscosity is less than 0.5, the crystallinity tends to be lowered, and when it exceeds 1.1, the dispersibility is lowered and the mechanical properties of the resin composition tend to be lowered. More preferably, it is 0.6-1.0.

The shape of poly ethylene terephthalate used in the production method of the present invention is not limited in particular, for example, pellets, flakes, granules, powder and the like.

  The method of melt kneading of the present invention is not particularly limited, and a known heat-melt mixing device can be used.

  A single-screw extruder, a twin-screw extruder, a combination twin-screw extruder, a kneader / ruder, or the like can be used as the heat-melt mixing device. Among these, a twin screw extruder is preferably used because dispersibility of PPS and polyalkylene terephthalate is improved. More preferably, a twin screw extruder having two or more kneading zones is used.

  In the production method of the present invention, the method for supplying PPS and polyalkylene terephthalate to the kneader during kneading is not particularly limited. For example, PPS and polyalkylene terephthalate are previously blended and supplied to the kneader, PPS and polyalkylene Examples thereof include a method of supplying each terephthalate to a kneader while measuring each of the terephthalates, and a method of supplying polyalkylene terephthalate to the kneader supplied with PPS by side feed.

  The production method of the present invention is characterized by melt-kneading at a temperature of 280 to 350 ° C. The temperature referred to here is the temperature of the resin measured at the discharge unit. When the temperature is kneaded at a temperature lower than 280 ° C., the melt viscosity of PPS becomes high or the PPS becomes unmelted, so that the dispersibility is remarkably deteriorated and the physical properties of the final product are deteriorated. On the other hand, when the temperature exceeds 350 ° C., the polyalkylene terephthalate is severely decomposed, and decomposed products adhere to the die of the kneader, resulting in a decrease in productivity. Moreover, the color tone of the resin composition obtained is deteriorated or the strength of the final product is lowered. Preferably, it is 285-330 degreeC, More preferably, it is 290-320 degreeC.

  In the production method of the present invention, the kneading time is not particularly limited, but is preferably 0.5 to 30 minutes. When the reaction time exceeds 30 minutes, the discoloration of the polymer and the thermal decomposition reaction may proceed and the physical property deterioration may become remarkable. On the other hand, if it is shorter than 0.5 minutes, the dispersion tends to be insufficient and the strength of the final product may not be sufficiently obtained.

The present invention will be specifically described below with reference to examples.
(1) Differential scanning calorimetry Measurement and calculation were performed according to JIS-K-7122 (1987) using differential scanning calorimetry (DSC). First, after maintaining at 320 ° C. for 2 minutes to completely melt, it was quenched with liquid nitrogen so that no crystals remained in the resin. Subsequently, the temperature was increased from 50 ° C. to 320 ° C. at 16 ° C./min, and subsequently observed when the temperature was decreased from 320 ° C. to 50 ° C. at a rate of 16 ° C./min after holding at 320 ° C. for 2 minutes. The temperature of the exothermic peak was determined.

Apparatus: DSC Q2000 manufactured by TA Instruments
Data analysis: Universal Analysis 2000 from TA Instruments
(2) Measurement was performed using a melt viscosity capillary rheometer using a die having a pore diameter of 1 mmφ and L / D = 10 at a shear rate of 1216 sec ⁻¹ .

Apparatus: Capillograph 1B type (3) intrinsic viscosity [η] manufactured by Toyo Seiki Seisakusho Co., Ltd.
The value calculated by the following formula was used from the solution viscosity measured at 25 ° C. at a concentration of 0.1 g / ml in orthochlorophenol.
η _sp / C = [η] + K [η] ² · C
Here, η _sp = (solution viscosity / solvent viscosity) −1, C is the dissolved polymer weight per 100 ml of solvent (g / 100 ml), and K is the Hangis constant (assuming 0.343). The solution viscosity and solvent viscosity were measured using an Ostwald viscometer.
(4), strength (cN / dtex), elongation (%)
Measured under the conditions of JIS L 1013 under the conditions of a test length of 25 cm and a pulling speed of 30 cm / min. (5) Heat shrinkage rate As a thermal stability index, a hot water bath whose temperature was adjusted to 98 ° C. The heat shrinkage percentage (%) relative to the initial length after standing for 30 minutes was obtained.

Each raw material polymer and oligomer were synthesized according to the following reference examples.
(6) MFR
The measurement temperature was 315.5 ° C. and the load was 5000 g, and the measurement was performed by a method according to ASTM-D1238-70.
[Reference Example 1] Production of PPS-1 In an autoclave equipped with a stirrer and a valve at the bottom, 8267 g (70.00 mol) of 47.5% sodium hydrosulfide aqueous solution, 2925 g (70.20 mol) of 96% sodium hydroxide, N-methyl-2-pyrrolidone (NMP) 13860.00 g (140.00 mol), sodium acetate 2187 g (26.67 mol), and ion-exchanged water 10500 g were charged, and nitrogen was passed at normal pressure to 240 ° C. for about 3 hours. The reaction vessel was cooled to 160 ° C. after distilling 14740 g of water and 280.0 g of NMP. The residual water content in the system per 1 mol of the charged alkali metal sulfide was 1.08 mol including the water consumed for the hydrolysis of NMP. The amount of hydrogen sulfide scattered was 0.023 mol per mol of the alkali metal sulfide charged.

  Next, 10324 g (70.24 mol) of p-dichlorobenzene (p-DCB) and 6452 g (65.17 mol) of NMP are added, the reaction vessel is sealed under nitrogen gas, and the mixture is stirred at 240 rpm with a temperature of 200 to 250 ° C. The temperature was raised to 0.8 ° C. at a rate of 0.8 ° C./min and held at 250 ° C. for 70 minutes. Next, the temperature was raised from 250 ° C. to 278 ° C. at a rate of 0.8 ° C./min, and maintained at 278 ° C. for 78 minutes. The extraction valve at the bottom of the autoclave was opened, the contents were flushed into a vessel equipped with a stirrer over 15 minutes while being pressurized with nitrogen, and stirred for a while at 250 ° C. to remove most of the NMP.

  The obtained solid and 76 liters of ion-exchanged water were placed in an autoclave equipped with a stirrer, washed at 70 ° C. for 30 minutes, and then suction filtered through a glass filter. Next, 76 liters of ion-exchanged water heated to 70 ° C. was poured into a glass filter, and suction filtered to obtain a cake.

  The obtained cake and 90 liters of ion-exchanged water were charged into an autoclave equipped with a stirrer, and the interior of the autoclave was replaced with nitrogen, and then the temperature was raised to 192 ° C. and held for 30 minutes. Thereafter, the autoclave was cooled and the contents were taken out.

The contents were subjected to suction filtration with a glass filter, and then 76 liters of ion-exchanged water at 70 ° C. was poured into the contents, followed by suction filtration to obtain a cake. The obtained cake was dried at 120 ° C. under a nitrogen stream to obtain dry PPS granules. The obtained MPS of PPS-1 was 298 g / 10 min.
[Reference Example 2] Production of PPS-2 The same procedure as in Reference Example 1 was conducted except that the amount of p-DCB charged was changed to 10250 g (69.76 mol). The obtained MPS of PPS-2 was 168 g / 10 min.
[Reference Example 3] Production of PET-1 A slurry of 1000 g of high-purity terephthalic acid (manufactured by Mitsui Chemicals) and 450 g of ethylene glycol (manufactured by Nippon Shokubai Co., Ltd.) was previously charged with about 1230 g of bis (hydroxyethyl) terephthalate, and the temperature was 250 ° C. The esterification reaction tank maintained at a pressure of 1.2 × 105 Pa was sequentially supplied over 4 hours, and after the completion of the supply, the esterification reaction was carried out over another 1 hour, and 1230 g of this esterification reaction product was added to the polycondensation tank. Transferred to.

  Subsequently, antimony trioxide is added to the polycondensation reaction tank to which the esterification reaction product has been transferred so that the amount of antimony trioxide becomes 230 ppm, and then the reaction system is heated from 250 ° C. to 285 ° C. while stirring the low polymer at 30 rpm. While gradually raising the temperature to 0 ° C., the pressure was reduced to 40 Pa.

The time to reach the final temperature and final pressure was both 60 minutes. When the predetermined stirring torque was reached, the reaction system was purged with nitrogen and returned to normal pressure, the polycondensation reaction was stopped, discharged into cold water in the form of a strand, and immediately cut to obtain 1000 g of a PET chip. The obtained polymer IV was 0.65.
[Reference Example 4] Production of PET-2 Polycondensation was carried out in the same manner as in Reference Example 3 except that the predetermined stirring torque was changed to obtain 1000 g of PET chip with IV = 0.51.
[Reference Example 5] Production of PET oligomer (hereinafter referred to as BHT) A slurry of 1000 g of high-purity terephthalic acid (manufactured by Mitsui Chemicals) and 450 g of ethylene glycol (manufactured by Nippon Shokubai Co., Ltd.) was previously charged in about 1230 g of bis (hydroxyethyl) terephthalate, The esterification reaction tank maintained at a temperature of 250 ° C. and a pressure of 1.2 × 10 5 Pa was sequentially supplied over 4 hours, and the esterification reaction was carried out for an additional hour after the completion of the supply.

After completion of the reaction, 1230 g was discharged into a stainless steel bat, air cooled, and then pulverized to obtain a PET oligomer powder. The obtained polymer IV was 0.32.
[Reference Example 6] Manufacture of Nylon 6 Charge 4000 g of ε-caprolactam aqueous solution with a solid content of 80% into a batch polymerization can with a ribbon wing stirrer with a total volume of 10 L. Extruded into a strand and further cut to obtain nylon 6 chips. This was extracted in a 95 ° C. hot water bath and dried under reduced pressure at 90 ° C. to obtain 3000 g of raw material nylon chips with ηr = 2.7.
Example 1
Supply 97% by weight of PPS granules and 3% by weight of PET chips to a bent type twin-screw kneader / extruder having two kneading zones heated to 300 ° C., with a shear rate of 100 sec ⁻¹ and a residence time of 1 minute. Melt extruded. The resin temperature during kneading was 300 ° C. From the kneader, it was discharged in the form of strands in cold water and immediately cut to obtain polymer chips of 97 wt% PPS and 3 wt% PET.

  The thermal characteristics of the obtained polymer chip were measured by DSC and found to be Tc = 127 ° C. and Tc ′ = 243 ° C. The DSC curve is shown in FIG. The melt viscosity was 118 Pa · sec.

Subsequently, the obtained polymer chip was vacuum-dried at 150 ° C. for 10 hours, and supplied to a spinning machine connected with a twin-screw kneading extruder. The twin-screw kneading extruder connected to the spinning machine was set to a set temperature of 300 ° C. and a shear rate of 100 sec ⁻¹ . Further, spinning was performed under the conditions of a spinning temperature of 295 ° C., a nozzle diameter of 0.23 mm, a nozzle hole number of 24 holes, and 1000 m / min to obtain an undrawn yarn. As a result of spinning for 5 hours, the number of yarn breaks was 0 and the spinnability was good.

  Next, the obtained undrawn yarn was drawn at a drawing temperature of 90 ° C., a heat treatment temperature of 170 ° C., and a draw ratio of 2.6 times. The number of yarn breaks during stretching was 0, and the stretchability was good.

The obtained drawn yarn had a strength of 3.8 cN / dtex, an elongation of 35%, a heat shrinkage rate of 5.1%, and had good dimensional stability. The obtained yarn physical properties are shown in Table 1.
Examples 2-4
The same procedure as in Example 1 was performed except that the ratio of PPS and PET was changed to the ratio shown in Table 1. The obtained yarn physical properties are shown in Table 1.
Example 5
The same procedure as in Example 3 was performed except that PPS-1 was changed to PPS-2. The obtained yarn physical properties are shown in Table 1.
Example 6
It carried out like Example 3 except having changed PET-1 into PET-2. The obtained yarn physical properties are shown in Table 1.

Comparative Example 1
Only the PPS granules were supplied to a vented twin-screw extruder, and melt-extruded PPS chips were obtained in the same manner as in Example 1.

  When the thermal characteristics of the obtained chip were measured by DSC, they were Tc = 137 ° C. and Tc ′ = 225 ° C. The DSC curve is shown in FIG. Moreover, although it was going to measure shear viscosity, at 290 degreeC, there was no fluidity | liquidity and it could not measure.

The obtained PPS chip was spun in the same manner as in Example 1. However, the pack pressure increased and the yarn was not discharged, so that spinning could not be performed.
Comparative Example 2
The same procedure as in Example 1 was performed except that PPS was changed to 90% by weight and PET was changed to 10% by weight. In the spinning process, ballast occurred and yarn breakage occurred frequently. In addition, yarn breakage frequently occurred in the drawing process. The obtained yarn had low strength.
Comparative Example 3
The same procedure as in Example 3 was performed except that PET was changed to BHT . The results are shown in Table 2. The strength of the obtained fiber was lowered and the thermal stability was poor.
Comparative Example 4
The same procedure as in Example 3 was performed except that PET was changed to nylon 6 . The results are shown in Table 2. The strength of the obtained fiber was lowered and the thermal stability was poor.

Examples 7 and 8 and Comparative Example 5
The same procedure as in Example 1 was performed except that the kneading temperature was changed to the temperature shown in Table 3. The results are shown in Table 3. Within the scope of the claims of the present application, fibers having high strength and good thermal stability could be obtained. On the other hand, when the kneading temperature was high, there were many die stains during kneading and spinning, and yarn breakage occurred. Moreover, it was the tendency for intensity | strength to fall and thermal stability deteriorated.

DSC curve

Explanation of symbols

1: Example 1 PPS / PET kneading chip Temperature rise curve 2: Comparative Example 1 PPS kneading chip Temperature rise curve 3: Example 1 PPS / PET kneading chip Temperature reduction curve 4: Comparative Example 1 PPS kneading chip Caloric curve during temperature drop

Claims (2)

It is composed of 92 to 99.9 % by weight of polyphenylenelene sulfide and 0.1 to 8% by weight of polyalkylene terephthalate having an intrinsic viscosity of 0.5 to 1.1, and a temperature drop rate of 16 ° C. by differential scanning calorimetry (DSC) measurement. A resin composition having a cooling crystallization temperature of 230 to 250 ° C. measured at / min. 2. The resin composition according to claim 1, wherein the melt viscosity measured at 290 ° C. at a shear rate of 1216 sec ⁻¹ is 200 Pa · sec or less.

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