JP5534964B2 - Method for producing polyphenylene ether resin composition - Google Patents

Description

  The present invention relates to a method for producing a polyphenylene ether resin composition.

Usually, polyphenylene ether is obtained by oxidative polymerization of an alkylphenol compound, and its shape is in a powder state.
In addition, polyphenylene ether has high heat resistance, and can be polymerized with various thermoplastic resins, and is known to improve the heat resistance of various thermoplastic resins.
On the other hand, since polyphenylene ether has high heat resistance, the processing temperature for polymer alloying with various thermoplastic resins inevitably increases.
Usually, the temperature at which polyphenylene ether itself can be melt processed is 270 to 320 ° C., so polyphenylene ether undergoes discoloration and high molecular weight due to heat during the melt processing, and further, heat degradation occurs in the staying part inside the melt processing equipment. As the process proceeds, black spot foreign substances and carbides are generated in the resin composition, which may be a defect point in the deterioration of the mechanical properties of the molded product. For this reason, a method of removing these sunspot foreign matters using a filter during melt processing is employed.
Many of the melt processing methods described above are carried out by using an extruder. However, in some cases, shear heat generation is caused by passing a resin composition containing polyphenylene ether having a high melt viscosity through a filter in a molten state. Occurs, the resin temperature further rises, the deterioration (decomposition and crosslinking) of the resin component progresses, and induces a secondary problem such as a decrease in mechanical properties.

  The following Patent Document 1 discloses a resin composition in which a matrix is made of a polypropylene resin and a dispersed phase is made of a polyphenylene ether resin, which reduces the occurrence of unmelted material, unreacted material, and thermally deteriorated material, and increases mechanical strength. An excellent resin composition has been proposed, and a resin composition with few black spots can be obtained by melt-kneading using a functionalized polypropylene resin functionalized with a specific amount and a functionalized polyphenylene ether resin. Have been described.

  Similarly, Patent Document 2 below proposes a functionalized polyphenylene ether with reduced foreign matters and a composition thereof. Specifically, when a functionalized polyphenylene ether is reacted with a functionalized compound at a high temperature at which the conventional polyphenylene ether can be processed, discoloration and foreign matter are generated due to thermal degradation. A functionalized polyphenylene ether is obtained by carrying out at a temperature below the melting point, and a resin composition containing the functionalized polyphenylene ether, a polystyrene resin, and a polyamide resin has been proposed.

Further, Patent Document 3 below proposes a method of adding polyphenylene ether to melted polyamide and melt-kneading it in order to suppress black spots in a resin composition comprising polyamide, polyphenylene ether and an impact modifier. .
Further, as a method for reducing foreign matters such as carbides and gelled products generated during heat-melt kneading by an extruder, Patent Document 4 discloses that a thermoplastic resin and other thermoplastic resins, additives, and the like are used in an extruder. When producing a molding material by kneading, a method has been proposed in which a thermoplastic resin is supplied to an extruder and then nitrogen gas is supplied to the extruder before the resin melts.

  Furthermore, in Patent Document 5 below, in order to reduce the thermal deterioration of the resin composition when the resin composition is produced by a co-rotating twin screw extruder, the screw flight design and the kneading disc design used are barrels. Proposals have been made to combine parts with a thin tip and a thick part at the tip.

  Furthermore, in Patent Document 6 below, in order to obtain a pellet with a small amount of foreign matter such as gelled products and carbides by melting and kneading a powdered thermoplastic resin using a twin screw extruder, There has been proposed a production method characterized by deaeration in a solid state in a conveying region of an extruder preheated at a temperature lower than a transition temperature (Tg) or a melting point (Tm).

JP 2001-302873 A JP 2001-335646 A JP 2004-143242 A JP-A-6-206216 JP-A-8-258110 JP 2002-292626 A

Since polyphenylene ether is usually obtained in a powder form, the bulk density is inevitably small.
In addition, since the screw conveying capacity of the screw element of the extruder is low due to screw flight, particularly in the boundary region between the powder conveying region (the region where the resin component is not melted) and the melting region (the region where the resin component is melted). , Powdered polyphenylene ether stays as a semi-molten residue around the short diameter part of the screw (screw groove, groove wall part). One of the factors.

  The technique shown in the above-mentioned prior art is a variety of contrivances / improvements in order to suppress foreign substances such as gelled substances, sunspot foreign substances, and carbides that are generated during heat-melting processing when a resin composition is obtained by an extruder. Although it has been made, it is a problem peculiar to powdery polyphenylene ether (1) The powder conveyance ability is lowered due to the powder shape, and (2) the melt processing temperature tends to deteriorate the intended resin composition It cannot be said that sufficient examination and improvement have been made yet for the extrusion technology that overcomes the polymer degradation mechanism in which the two factors of high temperature are linked.

  Therefore, in the present invention, in view of the above circumstances, in a process of heat melting and kneading powdered polyphenylene ether and a thermoplastic resin other than the powdered polyphenylene ether with a twin screw extruder, (1) powder for powder shape Thermally deteriorated product (black spots) generated by the combination of two factors, that is, the body conveyance capability is lowered, and (2) the melt processing temperature is a high temperature at which the target resin composition is likely to deteriorate. Production of a polyphenylene ether resin composition that can be a precursor of foreign matter and carbides, and can suppress the occurrence of a residue around a short axis portion of a screw (screw groove, groove wall portion) in a semi-molten or molten state. It aims to provide a method.

  The cause of the occurrence of foreign matter such as sunspots and carbides due to polyphenylene ether present in the resin composition is that polyphenylene melted at a melting point (240 to 260 ° C.) or higher of powdered polyphenylene ether during melt processing by a twin screw extruder. Ether adheres to the minor axis of the screw as a semi-melt or melt (mixture of polyphenylene ether melt and powder), and remains that are left untransported, resulting in thermal degradation, which is caused by sunspots and carbides. When the resin composition is produced by melt-kneading powdered polyphenylene ether and other thermoplastic resin, the semi-melt or melted substance is fixed to the short axis part of the screw. We sought a manufacturing method that showed no event.

  In particular, there are two factors: (1) due to the powdery polyphenylene ether, (1) low conveying ability due to the powder shape, and (2) the melt processing temperature is a high temperature at which the intended resin composition is likely to deteriorate. In view of the above, the inventors studied diligently about the improvement of the powder transfer capability and the influence of the processing temperature of the thermoplastic resin on the melting point of the powdered polyphenylene ether.

As a result, in the extrusion process of the twin screw extruder, the powdered polyphenylene ether is supplied from the side of the twin screw extruder to the conveying region of the other thermoplastic resin by using a forced side feeder. Specifying the screw configuration of the extruder and specifying the barrel set temperature of the extruder having the screw configuration, the powdered polyphenylene ether is in a powdered solid state below the melting point, and other molten thermoplastic resin By mixing, it was found that generation of a semi-molten or molten polyphenylene ether adhering substance staying or remaining in the minor axis portion of the screw can be suppressed, and the present invention has been completed.
That is, the present invention is as follows.

[1]
(A) Powdered polyphenylene ether: 1 to 99% by mass,
(B) Thermoplastic resin other than the above (a): 99 to 1% by mass
A process for producing a polyphenylene ether resin composition comprising:
A step of kneading the component (a) and the component (b) using a twin-screw extruder;
The method for producing a polyphenylene ether resin composition in which the twin-screw extruder has the following extrusion regions (region 1), (region 2), and (region 3) each having first to third supply ports. .
(Region 1)
The region where the total amount of the component (b) or a part of the component (b) is supplied from the first supply port of the twin-screw extruder,
When the component (b) in the solid state is conveyed by a screw (I: solid conveyance step-1),
Melting and kneading the component (b) (II: melt mixing step)
Conveying the component (b) in a molten state (III: melt conveying step);
It has a part that executes the three steps of
The screw is
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(B) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 1.5. Reverse screw element,
(C) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0, 1 flight screw element with flight angle α of 100 to 120 degrees,
(D) The twist angle is 12.5 to 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading disc diameter. 2-flight positive kneading disc with D ratio Lb / D of 0.05 to 1.0,
(E) The ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 1.0, and the flight tip width Lb is the ratio of the kneading disc diameter D. A kneading disc having an Lb / D of 0.05 to 1.0,
as well as,
(F) The torsion angle is minus 12.5 to minus 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading Reverse kneading disc having a ratio Lb / D of the disc diameter D of 0.05 to 1.0,
Of 6 types of elements,
The combination of the elements includes only (A), (A) + (C), (A) + (C) + (D), (A) + (B) + (C) + (D) combination configuration, (A) + (B) + (C) + (D) + (E) combination configuration, (A) + (B) + (C) + (D) + (E) + (F) is any one of the combination configurations,
The extruder barrel set temperature of the twin-screw extruder is 300 ° C. or less at which the thermoplastic resin (b) can be melt processed.
(Region 2)
(III) in the region (III) is a region continuous to the part that performs the melt conveying step,
The biaxial shaft provided with the second supply port with the total amount of the component (a) or a part of the component (a) and the part or the remaining amount of the component (b) under the melt conveyance of the component (b) (I) solid conveying step-2 in (region 2) to be supplied from the side of the extruder using the forced side feeder 1;
(II) melt mixing step of (region 2) for melt-kneading the supplied component (a) and component (b);
The (a) component and the (b) component are conveyed in a molten state (region 2) in (III) melt conveying step,
Has a part to perform the three steps,
Using the forced side feeder 1, the powdery polyphenylene ether of the component (a) is supplied,
The screw of the twin screw extruder in the (I) solid conveying step-2 of the part where the component (a) and the component (b) melted and conveyed from the (region 1) merge,
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(C) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0, 1 flight screw with flight angle α of 100-120 degrees,
(D) The twist angle is 12.5 to 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading disc diameter. A positive kneading disc having a ratio Lb / D of 0.05 to 1.0,
as well as,
(E) The ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 1.0, and the flight tip width Lb is the ratio of the kneading disc diameter D. 4 types of screw elements of a kneading disc with Lb / D of 0.05 to 1.0,
A combination of at least one screw element selected from the group consisting of:
The extruder barrel set temperature of the part for performing the (I) solid conveyance step-2 is not higher than the melting point of the (a) powdery polyphenylene ether,
The component (a) supplied in the (I) solid conveying step-2 and the component (b) of the melt supplied from the (III) melt conveying step in (region 1) are the same as those in (region 2). ) (II) melt mixing step, (III) melt transporting step,
The (II) melt mixing step and (III) melt transport step are steps of melt kneading the component (a) and the component (b), respectively, and a step of melt transport to (region 3).
The screw used in the (II) melt mixing step and the (III) melt conveying step,
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(B) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 1.5. Reverse screw element,
(C) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0, 1 flight screw element with flight angle α of 100 to 120 degrees,
(D) The twist angle is 12.5 to 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading disc diameter. 2-flight positive kneading disc with D ratio Lb / D of 0.05 to 1.0,
(E) The ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 1.0, and the flight tip width Lb is the ratio of the kneading disc diameter D. A kneading disc having an Lb / D of 0.05 to 1.0,
(F) The torsion angle is minus 12.5 to minus 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading Reverse kneading disc having a ratio Lb / D of the disc diameter D of 0.05 to 1.0,
(G) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.2 to 0.8, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0. A mixing screw that is a positive screw and the screw flight part has 2 to 10 notches between the screw pitches P1;
(H) The ratio P1 / D of the screw pitch length P1 and the screw diameter D is 0.2 to 0.8, and the ratio L / D of the screw element length L to the screw diameter D is 0.3 to 1.5. A mixing screw having a reverse thread screw element, the screw flight part having 2 to 10 notches between the screw pitches P1,
as well as,
(I) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0. A mixing screw having a 1 flight screw and a screw flight portion having 2 to 10 notches between screw pitches P1;
It is made up of a combination of these nine elements.
The combination of the elements includes only (A), (A) + (C), (A) + (C) + (D), (A) + (B) + (C) + (D) combination configuration, (A) + (B) + (C) + (D) + (E) combination configuration, (A) + (B) + (C) + (D) + (E) + (F), and a combination thereof, and any one of the configurations in which the elements (G), (H), and (I) are arbitrarily combined,
The extruder barrel set temperature in the (II) melt mixing step and the (III) melt transport step is 300 ° C. or less at which the (b) thermoplastic resin can be melt processed.
(Region 3)
(III) in the (region 2) is a region continuous to the part that performs the melt conveying step,
A twin screw extruder in which the remaining amount of the component (a) and / or the remaining amount of the component (b) is provided as a third supply port while the component (b) and the component (a) are melted and conveyed. (I) solid conveyance process-3 of (region 3) to be supplied from the side using the forced side feeder 2;
The (a) component and / or the (b) component separately supplied in the (I) solid conveyance step-3 of the (region 3), and the (a) component + (b) conveyed from the (region 2). (II) the melt mixing step of (region 3), wherein the melt kneaded product of the components is further melt kneaded;
Furthermore, the (a) component and the (b) component are conveyed in a molten state (region 3) in (III) the melt conveying step,
Has a part to perform the three steps,
Using the forced side feeder 2, the powdery polyphenylene ether of the component (a) and / or the component (b) is supplied, and the supplied component and the molten and transported resin of the (region 2) The screw of the twin-screw extruder used in (I) solid conveying step-3 of (region 3) performed in the joining part is
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(C) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0, 1 flight screw with flight angle α of 100-120 degrees,
(D) The twist angle is 12.5 to 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading disc diameter. A positive kneading disc having a ratio Lb / D of 0.05 to 1.0,
as well as,
(E) The ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 1.0, and the flight tip width Lb is the ratio of the kneading disc diameter D. A kneading disc having an Lb / D of 0.05 to 1.0,
Consisting of a combination of at least one screw element selected from the group consisting of four types of screw elements,
The extruder barrel set temperature in (I) solid conveying step-3 in (Region 3) is not higher than the melting point of (a) powdery polyphenylene ether,
In the (I) solid conveying step-3, the component supplied separately and the melt of (b) component + (a) component supplied from the (III) melt conveying step of (region 2) Is sent to the (II) melt mixing step of (Area 3) and the (III) melt transfer step,
The (II) melt mixing step and the (III) melt conveying step in (Region 3) are respectively
The final melt-kneading step of the component (a) and the component (b), and a step of melting and conveying to the end outlet of the twin-screw extruder,
The screw used in the (II) melt mixing step of the (region 3) and the (III) melt transfer step,
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(B) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 1.5. Reverse screw element,
(C) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0, 1 flight screw element with flight angle α of 100 to 120 degrees,
(D) The twist angle is 12.5 to 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading disc diameter. 2-flight positive kneading disc with D ratio Lb / D of 0.05 to 1.0,
(E) The ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 1.0, and the flight tip width Lb is the ratio of the kneading disc diameter D. A kneading disc having an Lb / D of 0.05 to 1.0,
(F) The torsion angle is minus 12.5 to minus 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading A reverse kneading disk having a disk diameter D ratio Lb / D of 0.05 to 1.0, (G) a screw pitch length P1 to screw diameter D ratio P1 / D of 0.2 to 0.8, and a screw A mixing screw having a ratio L / D between the element length L and the screw diameter D of 0.3 to 3.0 and a screw flight portion having 2 to 10 notches between the screw pitches P1. ,
(H) The ratio P1 / D of the screw pitch length P1 and the screw diameter D is 0.2 to 0.8, and the ratio L / D of the screw element length L to the screw diameter D is 0.3 to 1.5. A mixing screw having a reverse thread screw element, the screw flight part having 2 to 10 notches between the screw pitches P1,
as well as,
(I) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0. A mixing screw having a 1 flight screw and a screw flight portion having 2 to 10 notches between screw pitches P1;
It is made up of a combination of these nine elements.
The combination of the elements includes only (A), (A) + (C), (A) + (C) + (D), (A) + (B) + (C) + (D) combination configuration, (A) + (B) + (C) + (D) + (E) combination configuration, (A) + (B) + (C) + (D) + (E) + (F), and a combination thereof, and any one of the configurations in which the elements (G), (H), and (I) are arbitrarily combined,
The extruder barrel set temperature in the (II) melt mixing step and the (III) melt conveying step is 300 ° C. or less at which the (b) thermoplastic resin can be melt processed.

[2]
(A) Powdered polyphenylene ether: 1 to 99% by mass,
(B) Thermoplastic resin other than the above (a): 99 to 1% by mass,
Including
For a total of 100 parts by mass of the component (a) + the component (b),
(C) Additive: A method for producing a polyphenylene ether resin composition further comprising 0.1 to 70 parts by mass,
A step of kneading the component (a), the component (b) and the component (c) using a twin screw extruder;
The twin-screw extruder has the following (region 1), (region 2), and (region 3) extrusion regions each having first to third supply ports,
The method for producing a polyphenylene ether resin composition according to [1], wherein the component (c) is supplied to at least one of the (region 1), (region 2), and (region 3).

[3]
The production of the polyphenylene ether resin composition according to [1] or [2], wherein the (a) powdery polyphenylene ether is particles having a bulk specific gravity of 0.2 to 0.8 or an average particle diameter of 1 to 2000 μm. Method.

[4]
(B): The thermoplastic resin other than (a) is selected from the group consisting of polyolefin, hydrogenated block copolymer, styrene resin, polyamide, polyester, polyphenylene sulfide, and liquid crystal polyester, or one or more of them The method for producing a polyphenylene ether resin composition according to any one of [1] to [3], which is a thermoplastic resin.

[5]
The additive of the component (c) is an admixture, a filler, a stabilizer, a release agent, a processing aid, a flame retardant, and an anti-drip agent capable of miscible with the component (a) and the component (b). Any one of [2] to [4], which is one or more additives selected from the group consisting of a nucleating agent, a UV blocking agent, a dye, a pigment, an antioxidant, a plasticizer, and an antistatic agent The manufacturing method of the polyphenylene ether resin composition as described in any one.

[6]
Supplying the liquid additive as the component (c) to (region 2) and / or (region 3) of the twin-screw extruder;
The method of supplying the liquid component (c) is the (II) melt mixing step or (III) melt transporting step of (region 2) and / or the (II) melt mixing step of (region 3) or ( III) A method in which a liquid nozzle is attached to the barrel of the part where the melt conveying step is performed, and the liquid (c) component is press-fitted with a liquid pump.
The screw of the twin-screw extruder in the part into which the component (c) is press-fitted,
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(G) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.2 to 0.8, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0. A mixing screw that is a positive screw and the screw flight part has 2 to 10 notches between the screw pitches P1;
(H) The ratio P1 / D of the screw pitch length P1 and the screw diameter D is 0.2 to 0.8, and the ratio L / D of the screw element length L to the screw diameter D is 0.3 to 1.5. A mixing screw having a reverse thread screw element, the screw flight part having 2 to 10 notches between the screw pitches P1,
as well as,
(I) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0. A mixing screw having a 1 flight screw and a screw flight portion having 2 to 10 notches between screw pitches P1;
[2] to [5], wherein the screw is composed of a single element or a plurality of combinations of the elements (A), (G), (H), and (I). ] The manufacturing method of the polyphenylene ether resin composition as described in any one of.

[7]
The twin-screw extruder has a configuration in which a vent port is provided in the barrel of the twin-screw extruder in all regions (region 1), (region 2), and (region 3), and the vent port is closed. The method for producing a polyphenylene ether resin composition according to any one of [1] to [6].

[8]
The twin screw extruder has a configuration in which a vent port is provided in the barrel of the twin screw extruder in at least one of the (region 1), (region 2), and (region 3). The method for producing a polyphenylene ether resin composition according to any one of [1] to [6], wherein the pressure is reduced to 1 to 700 Torr using a vacuum pump to degas volatile components.

[9]
A step of supplying the component (a) and / or the powdery component (c) to the (region 2) and (region 3) of the twin-screw extruder using a forced side feeder;
The method for supplying the component (a) and / or the powdery component (c) is provided with an opening hole for degassing on the upstream side of the upper lid of the barrel connected to the forced side feeder, and for degassing. The method for producing a polyphenylene ether resin composition according to any one of the above [1] to [8], which is a method of supplying while degassing from the opening hole.

[10]
A hopper is connected to the first supply port of (Area 1) of the twin-screw extruder, and a heavy-weight feeder is connected to the hopper, and the hopper is provided with an exhaust pipe above the hopper. It is assumed that the hopper is an airtight hopper, nitrogen gas is continuously introduced from a supply pipe provided at a lower portion of the hopper, and an oxygen concentration between the gravimetric feeder and the hopper is less than 0.3% by volume. The method for producing a polyphenylene ether resin composition according to any one of [1] to [9].

[11]
A hopper is connected to the forced side feeder 1 of (region 2) of the twin-screw extruder, a heavy weight feeder is connected to the hopper, and the hopper has an exhaust pipe installed on the hopper. It is assumed that the hopper is an airtight hopper, nitrogen gas is continuously introduced from a supply pipe provided at a lower portion of the hopper, and an oxygen concentration between the gravimetric feeder and the hopper is less than 0.3% by volume. The method for producing a polyphenylene ether resin composition according to any one of [1] to [10].

[12]
A hopper is connected to the forced side feeder 2 of (region 3) of the twin-screw extruder, and a heavy-weight feeder is connected to the hopper, and the hopper has an exhaust pipe above the hopper. It is an installed airtight hopper, and nitrogen gas is continuously introduced from a supply pipe provided at the lower part of the hopper, and the oxygen concentration between the weight type feeder and the hopper is 0.3% by volume. The method for producing a polyphenylene ether resin composition according to any one of the above [1] to [11].

[13]
The twin-screw extruder has a stock tank for stocking the component (b) to be supplied to the first supply port of the (region 1).
A hopper is connected to the first supply port, a weight type feeder is connected to the hopper, and the weight type feeder is connected to the stock tank,
Nitrogen gas is supplied to a supply path between the stock tank and the weight type feeder and between the weight type feeder and the hopper, and the oxygen concentration of the supply path is set to less than 0.3% by volume. [1] A process for producing a polyphenylene ether resin composition according to any one of [12].

[14]
The twin-screw extruder has a stock tank for stocking the component (a) and component (b) supplied to the second supply port of the (region 2),
A forced side feeder 1 is connected to the second supply port,
The forced side feeder 1 is connected to a hopper,
A weight type feeder is connected to the hopper,
The weight tank is connected to the stock tank,
Nitrogen gas is supplied to a supply path between the stock tank and the weight type feeder and between the weight type feeder and the hopper, and the oxygen concentration of the supply path is set to less than 0.3% by volume. 1] thru | or the manufacturing method of the polyphenylene ether resin composition as described in any one of [13].

[15]
The twin-screw extruder has a stock tank for stocking the component (a) and the component (b) supplied to the third supply port of the (region 3),
A forced side feeder 2 is connected to the third supply port,
A hopper is connected to the forced side feeder 2,
A weight type feeder is connected to the hopper,
The weight tank is connected to the stock tank,
Nitrogen gas is supplied to the supply path between the stock tank and the heavy-weight feeder and between the heavy-weight feeder and the hopper, and the oxygen concentration in the supply path is less than 0.3% by volume. 1] thru | or the manufacturing method of the polyphenylene ether resin composition as described in any one of [14].

[16]
The twin-screw extruder has a stock tank that stocks the component (c) to be supplied to at least one of the (region 1), (region 2), and (region 3),
A hopper and a weight type feeder are sequentially connected to the first supply port of the (region 1),
A hopper and a weight type feeder are sequentially connected to the second supply port of (region 2),
A hopper and a weight type feeder are sequentially connected to the third supply port of the (region 3),
In (Area 1), (Area 2), and (Area 3), the stock tank is connected to each weight feeder,
Nitrogen gas is supplied to the supply path between the stock tank and the weight type feeder and between the weight type feeder and the hopper in the region where the component (c) is supplied. The method for producing a polyphenylene ether resin composition according to any one of [2] to [15], wherein the content is less than 3% by volume.

[17]
The method for producing a polyphenylene ether resin composition according to any one of [1] to [16], wherein the twin-screw extruder is a meshing type co-rotating twin-screw extruder.

[18]
(B): The method for producing a polyphenylene ether resin composition according to any one of [1] to [17], wherein the thermoplastic resin other than (a) is a styrene resin.

[19]
(B): The polyphenylene ether resin composition according to any one of [1] to [17], wherein the thermoplastic resin other than (a) is a combination of a styrene resin and a hydrogenated block copolymer. Production method.

[20]
(B): Production of polyphenylene ether resin composition according to any one of [1] to [17], wherein the thermoplastic resin other than (a) is a combination of a polyolefin and a hydrogenated block copolymer. Method.

[21]
(B): The method for producing a polyphenylene ether resin composition according to any one of [1] to [17], wherein the thermoplastic resin other than (a) is polyamide.

[22]
(B): The method for producing a polyphenylene ether resin composition according to any one of [1] to [17], wherein the thermoplastic resin other than (a) is polyphenylene sulfide.

According to the method for producing a polyphenylene ether resin composition of the present invention, it is effective that a semi-molten or melted polyphenylene ether adhering substance stays or remains in the screw minor axis portion of a twin-screw extruder. Can be suppressed.
In addition, according to the method for producing a polyphenylene ether resin composition of the present invention, a polyphenylene ether resin composition having very few sunspot foreign substances can be obtained.

(A) (a)-(I) (a) The schematic side view of the element of the screw of the twin-screw extruder used with the manufacturing method of the polyphenylene ether resin composition of this embodiment is shown. (A) (b)-(I) (b) The schematic sectional drawing of the element of the screw of the twin-screw extruder used with the manufacturing method of the polyphenylene ether resin composition of this embodiment is shown. It is an extrusion process flowchart of the manufacturing method of the polyphenylene ether resin composition of this embodiment. (A), (b) The structure of the screw of the twin-screw extruder used in the manufacturing method of the polyphenylene ether resin composition of this embodiment, and explanatory drawing of the process performed by each part of a screw are shown.

Hereinafter, a mode for carrying out the present invention (hereinafter referred to as “the present embodiment”) will be described in detail.
In addition, this invention is not limited to the following description, It can implement by changing variously within the range of the summary.

[Method for producing polyphenylene ether resin composition]
In the method for producing the polyphenylene ether resin composition of the present embodiment,
(A) Powdered polyphenylene ether: 1 to 99% by mass,
(B) Thermoplastic resin other than the above (a): 99 to 1% by mass
A polyphenylene ether resin composition containing is produced.
(A) and (b) are kneaded using a twin-screw extruder, and the twin-screw extruder is (region 1), (region 2), and (region 3) described later. It has an extrusion area.

Moreover, in the manufacturing method of the polyphenylene ether resin composition of this embodiment, with respect to a total of 100 mass parts of said (a) component + said (b) component, (c) Additive: 0.1-70 mass. It is preferable that a part is included.
The component (c) is supplied to at least one of (region 1), (region 2), and (region 3).

(material)
First, the raw material used for the manufacturing method of the polyphenylene ether resin composition of this embodiment is demonstrated.
<Component (a): Powdered polyphenylene ether>
The method for producing the polyphenylene ether resin composition of the present embodiment uses powdered polyphenylene ether as a raw material.
The powdery polyphenylene ether of component (a) is composed of repeating units represented by the bond unit of the following formula (1), and has a polystyrene-reduced number average molecular weight of 1000 or more measured using GPC (gel permeation chromatography). It is preferably a homopolymer and / or copolymer polyphenylene ether (hereinafter abbreviated as PPE) in the range of 1500 to 50000, more preferably 1500 to 30000.

In the formula (1), R ₁ , R ₂ , R ₃ and R ₄ are each hydrogen, halogen, primary or secondary lower alkyl group having 1 to 7 carbon atoms, phenyl group, haloalkyl group, Are selected from the group consisting of an aminoalkyl group, a hydrocarbonoxy group and a halohydrocarbonoxy group in which at least two carbon atoms separate a halogen atom and an oxygen atom; May be.

Specific examples of the component (a) include poly (2,6-dimethyl-1,4-phenylene ether), poly (2-methyl-6-ethyl-1,4-phenylene ether), poly (2-methyl -6-phenyl-1,4-phenylene ether), poly (2,6-dichloro-1,4-phenylene ether) and the like, and 2,6-dimethylphenol and other phenols (for example, 2,6- Polyphenylene ether copolymers such as copolymers with 3,6-trimethylphenol and 2-methyl-6-butylphenol) may also be mentioned.
In particular, poly (2,6-dimethyl-1,4-phenylene ether), a copolymer of 2,6-dimethylphenol and 2,3,6-trimethylphenol is preferable, and poly (2,6-dimethyl-1 , 4-phenylene ether).

The polyphenylene ether as the component (a) can be produced by a known method and is not particularly limited. For example, it can be easily produced by oxidative polymerization of 2,6-xylenol using, for example, a complex of cuprous salt and amine by Hay described in US Pat. No. 3,306,874. In addition, it can be easily produced by the methods described in U.S. Pat. Nos. 3,306,875, 3,257,357, 3,257,358, JP-B 52-17880, JP-A-50-51197, and 63-152628. .
PPE obtained by these production methods is normally distributed as powdered polyphenylene ether, and this powdery polyphenylene ether is also used in the method for producing the polyphenylene ether resin composition of the present embodiment.

Component (a) used in the method for producing a polyphenylene ether resin composition of the present embodiment: The powdery polyphenylene ether is preferably particles having a bulk specific gravity of 0.2 to 0.8 or an average particle diameter of 1 to 2000 μm.
The bulk density is measured as a loose apparent density. For example, it can be measured as a packing density in a state where powder polyphenylene ether is naturally dropped into a 100 cc volume metal container using a powder tester (manufactured by Hosokawa Micron Corporation).
The average particle diameter can be calculated by sieving using various metal mesh screens having different openings in accordance with ISO 3310.

Furthermore, component (a): powdery polyphenylene ether is usually crystalline polyphenylene ether having a melting point.
With respect to crystalline polyphenylene ether, Journal of Polymer Science, Part A-2 (6) 1141-1148 (1968), European Polymer Journal (9) 293-300 (1973), Polymer (19) 81-84. Page (1978).
(A) Component: The melting point of the powdery polyphenylene ether can be determined by measurement using a differential thermal scanning calorimeter (DSC), and is a temperature-heat flow graph obtained when the temperature is raised at 20 ° C./min. The top peak temperature of the observed peak is defined as the melting point. When there are a plurality of peak top temperatures, the highest temperature is defined as the melting point.
Component (a): The melting point of the powdery polyphenylene ether is preferably 240 ° C to 260 ° C.

<(B): Thermoplastic resin other than the above (a)>
Component (b): The thermoplastic resin other than the above-mentioned (a) powdery polyphenylene ether is not limited to crystalline and amorphous, and may be one or a combination of two or more different thermoplastic resins.
In consideration of thermal degradation during melt processing of the powdery polyphenylene ether of component (a), the thermoplastic resin other than component (b): (a) is a thermoplastic resin having a melt processing temperature of 300 ° C. or lower. It is preferable.
Examples of the component (b) include polyolefins, hydrogenated block copolymers, styrene resins, polyamides, polyesters, polyphenylene sulfides, and liquid crystal polyesters.

As the component (b) polyolefin, isotactic polypropylene, poly (4-methyl-1-pentene), polybutene-1, high density polyethylene, ultrahigh molecular weight high density polyethylene, low density polyethylene, linear low density polyethylene, Copolymers of two or more compounds selected from ultra-low density polyethylene having a density of less than 0.90, ethylene, propylene, and other α-olefins, for example, ethylene / propylene copolymer, ethylene / butene-1 Examples of the copolymer include an ethylene / octene copolymer, a propylene / ethylene (random, block) copolymer, a propylene / 1-hexene copolymer, and a propylene / 4-methyl-1-pentene copolymer. These polyolefins may be used individually by 1 type, and may use 2 or more types together.
Of these polyolefins, isotactic polypropylene, propylene / ethylene block copolymer, propylene / ethylene random copolymer and polyethylene are preferred.
These polyolefins usually have elastomeric and resinous properties.

These polyolefins also include functional group-containing polyolefins obtained by adding various functional groups to polyolefins. As a method for adding a functional group to a polyolefin, a functional group-containing unsaturated compound such as a carboxyl group-containing unsaturated compound, an acid anhydride group-containing unsaturated compound, or an epoxy group (glycidyl group) -containing unsaturated compound is reacted with the polyolefin. A method is mentioned.
These functional group-containing unsaturated compounds that add functional groups to this polyolefin include carboxylic acid compounds such as acrylic acid, methacrylic acid, maleic acid, fumaric acid, itaconic acid, citraconic acid, maleic anhydride, and citraconic anhydride. Acid anhydride compounds such as itaconic anhydride, glycidyl methacrylate, glycidyl acrylate, vinyl glycidyl ether, glycidyl ether of hydroxyalkyl (meth) acrylate, glycidyl ether of polyalkylene glycol (meth) acrylate, glycidyl itaconate, etc. Compounds.
Among the various functional group-containing unsaturated compounds, maleic anhydride is more preferable.

The reaction between the polyolefin and the functional group-containing unsaturated compound is usually performed by a method of reacting the polyolefin in a heated and melted state (150 to 300 ° C.) with the functional group-containing unsaturated compound, or using an organic solvent. Examples include a method of reacting a polyolefin in a solution state or a slurry state with the functional group-containing unsaturated compound at room temperature (23 ° C.) to 200 ° C.
In the reaction described above, a radical initiator may be used.
Moreover, the other ethylenically unsaturated compound which can be copolymerized with the said functional group containing unsaturated compound, for example, styrene etc., may coexist.
The amount of the functional group-containing unsaturated compound used in the functionalization modification reaction of polyolefin, the amount of radical initiator used, and the reaction temperature are arbitrarily selected according to the amount of the functional group-containing unsaturated compound added. be able to.
Usually, the functional group-containing polyolefin has 0.05 to 30% by mass, preferably 0.1 to 20% by mass, more preferably 0.2 to 10% by mass (or copolymerization) of the functional group-containing unsaturated compound. Is.
The amount of the functional group in the functional group-containing polyolefin can be known by a Fourier transform infrared spectrophotometer (FTIR), proton NMR or the like.

As the hydrogenated block copolymer of component (b), the precursor is a block copolymer of a vinyl aromatic compound and a conjugated diene compound in each monomer unit, and is mainly composed of a vinyl aromatic compound (vinyl aromatic A block copolymer comprising a polymer block A having a compound content of at least 70% and a polymer block B mainly comprising a conjugated diene compound (having a content of at least 70% conjugated diene compound). Examples of the structure are shown.
In the block copolymer, the vinyl aromatic compound in the random copolymer portion may be distributed uniformly or in a tapered shape.
In the block copolymer, a plurality of portions where the vinyl aromatic compound is uniformly distributed and / or a portion where the vinyl aromatic compound is distributed in a tapered shape may coexist.
Further, a plurality of portions having different vinyl aromatic compound contents may coexist in the block copolymer.

(B) A block copolymer comprising a polymer block A mainly composed of a vinyl aromatic compound and a polymer block B mainly composed of a conjugated diene compound, which constitutes a hydrogenated block copolymer as a component, Examples thereof include block copolymers having the following structure.
(AB) _n , A- (BA) _n- B, B- (AB) _{n + 1} , [(AB) _k ] _{m + 1-} Z, [(AB) _k -A] _{m + 1-} Z, [(BA) _k ] _{m + 1-} Z, [(BA) _k- B] _{m + 1-} Z.
In the above formula, Z represents a residue of a coupling agent or a residue of an initiator of a polyfunctional organolithium compound.
n, k, and m are integers of 1 or more, and are generally 1 to 5.

Examples of the vinyl aromatic compound used in the vinyl aromatic compound-conjugated diene compound block copolymer include styrene, α-methylstyrene, vinyltoluene, p-tert-butylstyrene, and diphenylethylene. These may be used alone or in combination of two or more. Styrene is particularly preferable.
The vinyl aromatic compound content in the vinyl aromatic compound-conjugated diene compound block copolymer is usually 1 to 95% by mass, preferably 1 to 80% by mass, more preferably 5 to 70% by mass. It is.
Examples of the conjugated diene compound in the block copolymer include butadiene, isoprene, 1,3-pentadiene, 2,3-dimethyl-1,3-butadiene, and only one of these may be used. Two or more kinds may be used in combination. In particular, butadiene, isoprene and combinations thereof are preferable.

Moreover, the microstructure which is a polymerization form of the conjugated diene compound in the vinyl aromatic compound-conjugated diene compound block copolymer can be arbitrarily selected.
For example, in butadiene, the 1,2-vinyl bond is 2 to 85%, preferably 10 to 85%, more preferably 35 to 85%.
In isoprene, the total amount of 1,2-vinyl bonds and 3,4-vinyl bonds is 2-85%, preferably 3-75%, more preferably 3-60%. The 1,2-vinyl bond and 3,4-vinyl bond may be uniformly distributed in the conjugated diene compound polymer block or may be distributed in a tapered shape.
The conjugated diene compound polymer may be a polymer portion having a 1,2-vinyl bond content or a total amount of 1,2-vinyl bond and 3,4-vinyl bond, for example, 1,2-vinyl bond content or 1 , 2-vinyl bonds and 3,4-vinyl bonds may be present in a polymer block portion having a total amount of less than 30% and polymer block portions having a content of 30% or more, and conjugated dienes having different vinyl bond amounts. A plurality of polymer block portions of the compound may coexist.

The number average molecular weight (molecular weight in terms of polystyrene by gel permeation chromatography) of the vinyl aromatic compound-conjugated diene compound block copolymer, which is the precursor of the hydrogenated block copolymer of component (b), is usually 1000 to 1000000, preferably 10,000 to 500,000, more preferably 20000 to 300,000.
The vinyl aromatic compound-conjugated diene compound block copolymer as the precursor is obtained by anionic polymerization of a conjugated diene compound and a vinyl aromatic compound in a hydrocarbon solvent using an organic lithium compound as a polymerization initiator.

  As the hydrocarbon solvent, aliphatic, alicyclic and aromatic hydrocarbons can be used. For example, propane, isobutane, n-hexane, isooctane, cyclopentane, cyclohexane, benzene, toluene and the like can be mentioned, and n-hexane, cyclohexane and benzene are more preferable. These solvents may be used alone or as a mixed solvent of two or more.

Moreover, as an organic lithium compound which is a polymerization initiator used for polymerization, mono-organic lithium compounds such as n-propyllithium, isopropyllithium, n-butyllithium, sec-butyllithium, tert-butyllithium, dilithiomethane, Polyfunctional organolithium compounds such as 1,4-dilithiobutane, 1,4-dilithio-2-ethylcyclohexane, 1,2-dilithio-1,2-diphenylmethane, 1,3,5-trilithiobenzene can be used. These may be used alone or as a mixture of two or more.
The amount of these organic lithium compounds used is premised on a monodisperse polymer (weight average molecular weight / number average molecular weight = 1) according to the number average molecular weight of the target vinyl aromatic compound-conjugated diene compound block copolymer. It can be selected appropriately by calculation.

(B) 1,2-vinyl bond amount of the microstructure which is a polymerization form of the conjugated diene compound constituting the vinyl aromatic compound-conjugated diene compound block copolymer that is a precursor of the hydrogenated block copolymer of the component, Usually, ethers, tertiary amines, alkali metal alkoxides and the like are used to adjust the increase in 3,4-vinyl bond amount or to adjust the randomness in the vinyl aromatic compound-conjugated diene compound copolymer chain. Polar compounds can be used.
Examples of polar compounds include diethyl ether, ethylene glycol / dimethyl ether, ethylene glycol / di-n-butyl ether, ethylene glycol / n-butyl / tert-butyl ether, ethylene glycol / di-tert-butyl ether, diethylene glycol / dimethyl ether, and triethylene. Glycol / dimethyl ether, tetrahydrofuran, α-methoxymethyltetrahydrofuran, dioxane, 1,2-dimethoxybenzene, triethylamine, N, N, N ′, N′-tetramethylethylenediamine, potassium tert-amyl oxide, potassium tert-butyl oxide Etc. These compounds may be used alone or as a mixture of two or more.
The usage-amount of this polar compound is 0 mol or more with respect to 1 mol of organolithium compounds, Preferably it is 0-300 mol.

A hydrogenated catalyst and hydrogen gas are added to a vinyl aromatic compound-conjugated diene compound block copolymer, which is a precursor of a hydrogenated block copolymer as described above, in a hydrocarbon solvent to perform a hydrogenation reaction. Thus, a hydrogenated block copolymer in which the olefinically unsaturated bond derived from the conjugated diene compound present in the polymer is reduced to 90% or less, preferably 55% or less, more preferably 5% or less is obtained. be able to.
The hydrogenation reaction is not limited in its production method as long as it can reduce the olefinic unsaturated bond derived from the conjugated diene compound present in the vinyl aromatic compound-conjugated diene compound block copolymer, and any production method can be used. It may be a method.
Examples of the hydrogenation reaction include the methods described in British Patent No. 1020720, US Pat. Nos. 3,333,024 and 4,501,857.

  Examples of the component (b) styrene resin include atactic polystyrene, rubber-reinforced polystyrene (HIPS), a styrene-acrylonitrile copolymer (AS) having a styrene content of at least 50% by weight, and rubber thereof. Examples include reinforced AS resin and syndiotactic polystyrene.

  Examples of the polyamide of component (b) include polyamide 6, polyamide 6,6, polyamide 4,6, polyamide 11, polyamide 12, polyamide 6,10, polyamide 6,12, polyamide 6 / 6,6, polyamide 6 / 6,12, polyamide MXD (m-xylylenediamine) / 6, polyamide 6, I, polyamide 6/6, T, polyamide 6/6, I, polyamide 6,6 / 6, T, polyamide 6,6 / 6 , I, polyamide 6/6, T / 6, I, polyamide 6,6 / 6, T / 6, I, polyamide 6/12/6, T, polyamide 6, 6/12/6, T, polyamide 6 / Among polyamides such as 12/6, I, polyamide 6, 6/12/6, I and the like, polyamides that can be melt-processed at 300 ° C. or lower can be mentioned.

  Examples of the component (b) polyester include polyethylene terephthalate, polytrimethylene terephthalate, and polybutylene terephthalate.

As the polyphenylene sulfide (hereinafter abbreviated as PPS) as the component (b), the repeating unit of the arylene sulfide represented by the following general formula (2) is usually 50 mol%, preferably 70 mol%, more preferably 90 mol%. The polymer containing the above is mentioned.
[-Ar-S-] (2)
In the formula (2), Ar represents an arylene group, and examples of the arylene group include a p-phenylene group, an m-phenylene group, and a substituted phenylene group (the substituent is an alkyl group having 1 to 10 carbon atoms, a phenyl group) And p, p′-diphenylenesulfone group, p, p′-biphenylene group, p, p′-diphenylenecarbonyl group, naphthylene group and the like.

The PPS may be a homopolymer having one type of arylene group as a structural unit, and is a copolymer obtained by mixing two or more different arylene groups from the viewpoint of processability and heat resistance. There may be.
Usually, PPS having a repeating unit of p-phenylene sulfide is called linear polyphenylene sulfide. This linear polyphenylene sulfide is heat-treated at a temperature below the melting point of PPS in the presence of oxygen to effect oxidative crosslinking. PPS that has been promoted to moderately increase the polymer molecular weight and viscosity is called cross-linked polyphenylene sulfide. Both the linear type and the crosslinked type can be used alone, and further, the linear type PPS and the crosslinked type PPS may be used in combination.

The PPS is usually produced by a method in which a halogen-substituted aromatic compound such as p-dichlorobenzene is polymerized in the presence of sulfur and sodium carbonate, sodium sulfide or sodium hydrogen sulfide and sodium hydroxide or sulfide in a polar solvent. Examples thereof include a polymerization method in the presence of hydrogen and sodium hydroxide or sodium aminoalkanoate, and self-condensation of p-chlorothiophenol. In particular, a method of reacting sodium sulfide and p-dichlorobenzene in an amide solvent such as N-methylpyrrolidone or dimethylacetamide or a sulfone solvent such as sulfolane is suitable.
The above production method is a known method. For example, US Pat. No. 2,513,188, Japanese Patent Publication No. 44-27671, Japanese Patent Publication No. 45-3368, Japanese Patent Publication No. 52-12240, Japanese Patent Publication No. Sho 61- No. 225217, US Pat. No. 3,274,165, Japanese Patent Publication No. 46-27255, Belgian Patent No. 29437, Japanese Patent Laid-Open No. 5-222196, and the like.

As the liquid crystal polyester of component (b), a known polyester can be used as a thermotropic liquid crystal polymer.
For example, a thermotropic liquid crystal polyester mainly composed of p-hydroxybenzoic acid and polyethylene terephthalate, a thermotropic liquid crystal polyester mainly composed of p-hydroxybenzoic acid and 2-hydroxy-6-naphthoic acid, p-hydroxybenzoic acid Examples include a thermotropic liquid crystal polyester mainly composed of acid, 4,4′-dihydroxybiphenyl, and terephthalic acid, and can be melt processed at 300 ° C. or lower.

<(C) Additive>
(C) Component: As an additive, the incompatible component (a) and component (b) can be miscible with each other, filler, stabilizer, mold release agent, processing aid, flame retardant, drip Examples thereof include an inhibitor, a nucleating agent, a UV blocker, a dye, a pigment, an antioxidant, a plasticizer, and an antistatic agent, and these additives may be those known in the art.

As an admixture capable of miscible with the incompatible component (a) and the component (b) which are the components (c), either the component (a) or the component (b) is melt-kneaded. These components are positioned as components that can be stably emulsified and dispersed.
For example, polyphenylene ether added with maleic anhydride, which is an admixture capable of dispersing polyphenylene ether in polyamide, styrene / vinyl, which is an admixture capable of dispersing polyphenylene ether in polyphenylene sulfide or in polyester Examples include oxazoline compound copolymers and styrene / glycidyl methacrylate copolymers.
As described above, the admixture itself has good compatibility with the component (a) or the component (b), or reacts with the functional group of the component (a) or the component (b) itself. Those having possible functional groups can be used, and a wide range of compounds can be selected from low molecular compounds to high molecular compounds.

The filler which is (c) component is a component which gives many functions with respect to a resin composition.
For example, there are imparting rigidity, imparting heat resistance, imparting thermal conductivity, imparting conductivity, improving molding shrinkage, improving linear expansion, and the like, and these can be selected according to these purposes.
For example, inorganic salts, glass fibers (glass long fibers, chopped strand glass fibers), cellulose, glass flakes, glass beads, carbon long fibers, chopped strand carbon fibers, whiskers, mica, clay, talc, magnesium hydroxide, magnesium sulfate and Its fiber, silica, carbon black, titanium oxide, calcium carbonate, fly ash (coal ash), potassium titanate, wollastonite, thermal conductive material (graphite, aluminum nitride, boron nitride, alumina, beryllium oxide, silicon dioxide, oxidation Magnesium, aluminum nitrate, barium sulfate, etc.), conductive metal fibers, conductive metal flakes, conductive carbon black, conductive carbon fibers, and carbon nanotubes. It may be selected at least one kind.
These fillers are further treated with surface treatment agents such as silane coupling agents, titanate coupling agents, aliphatic carboxylic acids, and aliphatic metal salts, and organic treatments such as ammonium salts by an intercalation method. Or a product obtained by treating a resin such as urethane resin or epoxy resin as a binder.

  As the flame retardant of component (c), organophosphate ester compounds, phosphinic acid metal salts, magnesium hydroxide, ammonium polyphosphate flame retardants, melamine flame retardants, triazine flame retardants, aromatic halogen flame retardants, At least one selected from the group consisting of a silicone-based flame retardant and a fluorine-based polymer can be selected and used.

  As the stabilizer and antioxidant of the component (c), for example, octadecyl-3- (3,5-di-t-butyl-4-hydroxyphenyl) propionate, pentaerythritol tetrakis [methylene-3- (3,5 -Di-tert-butyl-4-hydroxyphenyl) propionate] methane, 1,3,5-trimethyl-2,4,6-tris (3,5-di-tert-butyl-4-hydroxybenzyl) benzene, tetrakis -(2,4-di-t-butylphenyl) 4,4-biphenylene-diphosphonite, tris (2,4-di-t-butylphenyl) phosphite, tetrakis [methylene-3- (dodecylthio) propionate ] Methane, 2,6-di-tert-butyl-4- (4,6-bis (octylthio) -1,3,5-triazin-2-ylamino) fe Thioethylenebis [3- (3,5-di-tert-butyl-4-hydroxyphenyl) propionate], 4,6-bis (octylthiomethyl) -O-cresol, 4,6-bis (dodecylthio) Methyl) -O-cresol, 1,3,5-tris (3,5-di-tert-butyl-hydroxybenzyl) -1,3,5-triazine-2,4,6- (1H, 3H, 5H) -Trione, N, N'-hexane-1,6-diylbis [3- (3,5-di-tert-butyl-4-hydroxyphenylpropionamide)], 1,2-bis (3,5-di- tert-butyl-4-hydroxyhydrocinnamoyl) hydrazine, oxamidobis- [ethyl-3- (3,5-di-tert-butyl-4-hydroxy-phenyl) propionate, 3- (N Salicyloyl) amino-1,2,4-triazole, decamethylenecarboxylic acid disalicyloyl hydrazide, isophthalic acid bis (2-phenoxypropionyl hydrazide), N-formyl-N′-salicyloyl hydrazine, oxalyl-bis-benzylidene -Hydrazide etc. are mentioned.

  Examples of the release agent of component (c) include polyethylene wax, silicone release agent, fluorine release agent, higher alcohol fatty acid ester (stearyl stearate, etc.), higher fatty acid ester release agent (sorbitan fatty acid ester). , Montanic acid ester wax, etc.) and higher fatty acid metal salt release agents (magnesium stearate, calcium montanate, etc.).

  Examples of the processing aid for component (c) include higher alcohol fatty acid esters (stearyl stearate and the like), fatty acid amide processing aids, polyethylene wax, oxidized polyethylene wax, montanic ester wax, and montanic acid calcium salt. It is done.

  Examples of the anti-drip agent of component (c) include a polymer obtained by modifying a tetrafluoroethylene resin or polytetrafluoroethylene (PTFE) with an acrylate ester.

  Examples of the nucleating agent (c) include 2,2-methylenebis (2,6-di-t-butylphenyl) sodium phosphate, sorbitol-based crystal nucleating agent, talc, silica, graphite, boron nitride and the like. Examples thereof include inorganic fine particles, metal oxides such as magnesium oxide, aluminum oxide, and zinc oxide.

Examples of the UV blocking agent (c) include inorganic ultraviolet absorbers such as titanium oxide, zinc oxide and cerium oxide, benzotriazole compounds, benzophenone compounds, salicylate compounds, cyanoacrylate compounds, triazine compounds, oxanilide compounds, and malon. Examples thereof include organic ultraviolet absorbers such as acid ester compounds and hindered amine compounds.
Examples of the benzotriazole compound include 2- (2′-hydroxy-5′-methylphenyl) benzotriazole, 2- [2′-hydroxy-3 ′, 5′-bis (α, α-dimethylbenzyl) phenyl]. -Benzotriazole, 2- (2'-hydroxy-3 ', 5'-di-tert-butyl-phenyl) -benzotriazole, 2- (2'-hydroxy-3'-tert-butyl-5'-methylphenyl) ) -5-chlorobenzotriazole, 2- (2′-hydroxy-3 ′, 5′-di-tert-butyl-phenyl) -5-chlorobenzotriazole), 2- (2′-hydroxy-3 ′, 5) '-Di-tert-amyl) -benzotriazole, 2- (2'-hydroxy-5'-tert-octylphenyl) benzotriazole, and 2,2'-methylenebis [4- ( 1,1,3,3-tetramethylbutyl) -6- (2N-benzotriazol-2-yl) phenol] and the like.
Examples of the benzophenone compound include 2,4-dihydroxybenzophenone, 2-hydroxy-4-methoxybenzophenone, 2-hydroxy-4-methoxybenzophenone-5-sulfonic acid, 2-hydroxy-4-n-octoxybenzophenone, 2 -Hydroxy-n-dodecyloxybenzophenone, bis (5-benzoyl-4-hydroxy-2-methoxyphenyl) methane, 2,2'-dihydroxy-4-methoxybenzophenone, and 2,2'-dihydroxy-4,4 Examples include '-dimethoxybenzophenone.
Examples of the salicylate compound include phenyl salicylate and 4-tert-butylphenyl salicylate.
Examples of the cyanoacrylate compound include ethyl-2-cyano-3,3-diphenyl acrylate and 2-ethylhexyl-2-cyano-3,3-diphenyl acrylate.
Examples of the oxanilide compound include 2-ethoxy-2′-ethyl oxalinic acid bis-arinide. Examples of the malonic acid ester compound include 2- (alkylidene) malonic acid esters, particularly 2- ( 1-arylalkylidene) malonic acid esters and the like.
Examples of hindered amine light stabilizers include bis (2,2,6,6-tetramethyl-4-pepyridyl) sebacate and bis (1-octyloxy-2,2,6,6-tetramethyl-4-pepyridyl). Sebacate, polycondensate of dimethyl succinate and 1- (2-hydroxyethyl) -4-hydroxy-2,2,6,6-tetramethylpepyridine, poly [{6- (1,1,3,3 -Tetramethylbutyl) amino-1,3,5-triazine-2,4-diyl} {(2,2,6,6-tetramethyl-4-pepyridyl) imino} hexamethylene {(2,2,6, 6-tetramethyl-4-pepyridyl) imino}], N, N′-bis (3-aminopropyl) ethylenediamine and 2,4-bis [N-butyl-N- (1,2,2,6,6- Pentamethyl-4-pepyrin Dil) amino] -6-chloro-1,3,5-triazine, 1,2,3,4-tetra (2,2,6,6-tetramethyl-4-pepyridyl) -butanetetracarboxyl Rate, 1,4-bis (2,2,6,6-tetramethyl-4-pepyridyl) -2,3-butanedione, tris- (2,2,6,6-tetramethyl-4-pepyridyl) trimellitate, 1,2,2,6,6-pentamethyl-4-pepyridyl-n-octoate, 1,2,2,6,6-pentamethyl-4-pepyridyl stearate, 4-hydroxy-1,2,2,6 , 6-pentamethylpepyridine, bis (1,2,2,6,6-pentamethyl-4-pepyridyl) sebacate, and 2- (3,5-t-butyl-4-hydroxybenzyl) -2-n- Butyl malonate bis (1, , 2,6,6-pentamethyl-4-Pepirijiru), and the like.

  Examples of the component (c) plasticizer include higher fatty acid ester compounds, phosphate ester compounds, paraffinic oils, naphthenic oils, and the like.

  Examples of the antistatic agent of component (c) include sorbitan fatty acid ester, organic acid monoglyceride, diglycerin fatty acid ester, alkylbenzene sulfonate, zinc N-methylstearyl dithiocarbamate and the like.

Examples of component (c) dyes and pigments include azo dyes and pigments, azo metal-containing dyes and pigments, naphthol azo dyes and pigments, azo lake dyes and pigments, azomethine dyes and pigments, anthraquinone dyes and pigments. Pigments, quinacridone dyes / pigments, dioxazine dyes / pigments, diketopyrrolopyrrole dyes / pigments, anthopyridone dyes / pigments, isoindolinone dyes / pigments, indanthrone dyes / pigments, perinone dyes / 1 or selected from the group consisting of a pigment, a perylene dye / pigment, an indigo dye / pigment, a thioindigo dye / pigment, a quinoline dye / pigment, a benzimidazolone dye / pigment, and a triphenylmethane dye / pigment Two or more organic dyes and pigments may be mentioned. The colors exhibited by these colorants are yellow, red, blue, green, black, and the like.
Examples of the inorganic pigment include titanium oxide, titanium yellow, yellow lead, ultramarine, cobalt blue, chrome green, bengara, and carbon black.

(Method for producing polyphenylene ether resin composition)
The polyphenylene ether resin composition obtained by the production method of the present embodiment is composed of the components (a) component + (b) component or (a) component + (b) component + (c) component described above. (A) component / (b) component = 1 to 99% by mass / 99 to 1% by mass, and (c) component is a total of 100 parts by mass of (a) component + (b) component. On the other hand, it shall contain in the ratio of 0.1-70 mass part.
These components (a) to (c) are composed of a twin-screw extruder described later, more preferably a meshing type co-rotating twin-screw extruder (region 1: reference numeral 12 in FIG. 2). , (Region 2: Reference numeral 13 in FIG. 2), (Region 3: Reference numeral 14 in FIG. 2), the mixture is melt-kneaded and extruded to obtain a polyphenylene ether resin composition.

In a conventionally known polyphenylene ether resin composition production technique, the set temperature of the twin screw extruder is set to 300 ° C. or higher because the glass transition temperature of polyphenylene ether is as high as about 210 ° C.
However, in the method for producing the polyphenylene ether resin composition of the present embodiment, since the powdery polyphenylene ether resin is used as the component (a), the solid conveying ability is remarkably reduced as compared with the pellet-shaped resin.
Specifically, when the resin processing step is divided into four stages of (I) solid conveyance step-1 → (II) melt mixing step → (III) melt conveyance step → (IV) stranding step, (I) Solid conveying step-1 → (II) Step in the middle of the melt mixing step, that is, in the region where the powdery polyphenylene ether is transferred from the powder state to the molten state by heat transfer from the extruder barrel The melted polyphenylene ether and the powdered polyphenylene ether coexist, and this coexisting material tends to form a semi-melted material fixed to the screw short diameter portion (screw groove, groove wall portion).
This semi-molten polyphenylene ether exists in a state of being wound as a melt around the short axis portion of the screw and is likely to remain on the screw without being conveyed. And if this state continues for a long time, heat degradation from the barrel of the extruder or heat transfer from the screw shaft causes the semi-molten polyphenylene ether to undergo thermal degradation, and the precursor formation of foreign matters such as sunspots and carbides due to the degradation occurs. Can be a thing.

  In the method for producing the polyphenylene ether resin composition of the present embodiment, the molten polyphenylene ether and the powdered polyphenylene ether coexist in the coexisting state and can remain as a residue in the screw minor axis portion, which can be a precursor product of these foreign substances. This reduces the generation of the semi-melt.

In the method for producing the polyphenylene ether resin composition of the present embodiment, the raw material is melt-kneaded using a twin screw extruder.
The twin-screw extruder includes a predetermined screw in a substantially cylindrical barrel.

1A to 1I are schematic side views of essential parts of a screw of a twin screw extruder used in the method for producing a polyphenylene ether resin composition of the present embodiment (FIGS. 1A to 1A). 1 (I) (a)) and schematic cross-sectional views (FIGS. 1A and 1B to 1I and 1B).
In FIG. 2, the extrusion process flowchart of the manufacturing method of the polyphenylene ether resin composition of this embodiment is shown.
3A and 3B show the configuration of the screw of the twin screw extruder used in the method for producing the polyphenylene ether resin composition of the present embodiment and the steps performed by each part of the screw.

As shown in FIG. 2, the twin-screw extruder has a first supply port 1 on the upstream side and a second supply port 2 on the downstream side with respect to the flow direction of the raw material, and further on the downstream side of the second supply port. A third supply port 3 is provided.
In addition, a vacuum vent port (not shown) is provided between each of these supply ports or between the third supply port 3 and the extruder outlet for degassing volatile components.
As shown in FIG. 2, a region between the first supply port 1 and the second supply port 2 is (region 1: reference numeral 12), and a region between the second supply port 2 and the third supply port 3 is (region). 2: Symbol 13), and the area between the third supply port 3 and the extruder outlet (region 3: symbol 14).
It is assumed that the vacuum vent port is provided in at least one region of (region 1: code 12), (region 2: code 13), and (region 3: code 14).

(Region 1: reference numeral 12) is a region where the first supply port 1 supplies the whole amount of the thermoplastic resin other than the component (b): component (a) or a part of the component (b). .
In (Region 1: Reference No. 12), the component (b) is executed by a process indicated by each function of (I) solid transport process-1 → (II) melt mixing process → (III) melt transport process. If necessary, (I) Solid conveying step-1 → (II) Melt mixing step → (III) Melt conveying step → (II) Melt mixing step → (III) Melting The melt mixing process and the melt transport process as shown in the object transport process may be divided and executed.

The barrel set temperature of (region 1: reference numeral 12) is 300 ° C. or less at which thermoplastic resins other than the component (b): component (a) can be melt processed.
By setting the barrel set temperature in (Region 1) to 300 ° C. or less, thermal deterioration of the resin component can be prevented.

In the present specification, the symbols (A) to (I) below are shown in FIG. 1 for the screws constituting (region 1: reference 12), (region 2: reference 13), and (region 3: reference 14). It corresponds to the screw elements shown in A) to (I).
3A and 3B show specific examples of the configuration of the screw, respectively, and the symbols (A) to (I) in FIGS. 3A and 3B are also shown in FIG. It corresponds to the screw element shown in (A) to (I).

Moreover, in this specification, about the process performed in the predetermined part of a screw, as shown to Fig.3 (a), (b), when dividing a screw into the site | part of C2-C12, (solid conveyance process- 1: Code 15-1), (Solid conveying process-2: Code 15-2), (Solid conveying process-3: Code 15-3), (Melt mixing process: Code 16), (Melt conveying process: Code) 17) can be carried out at the C2 to C12 sites of the screw, respectively.
In addition, the manufacturing method of the polyphenylene ether resin composition of this embodiment is not limited to the example shown to Fig.3 (a), (b).

The screw in (region 1: reference numeral 12)
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(B) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 1.5. Reverse screw element,
(C) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0, 1 flight screw element with flight angle α of 100 to 120 degrees,
(D) The twist angle is 12.5 to 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading disc diameter. 2-flight positive kneading disc with D ratio Lb / D of 0.05 to 1.0,
(E) The ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 1.0, and the flight tip width Lb is the ratio of the kneading disc diameter D. A kneading disc having an Lb / D of 0.05 to 1.0,
(F) The torsion angle is minus 12.5 to minus 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading Reverse kneading disc having a ratio Lb / D of the disc diameter D of 0.05 to 1.0,
These six types of elements are combined.
The screw of (region 1: code | symbol 12) is the structure of only (A), the combined structure of (A) + (C), the combined structure of (A) + (C) + (D), (A) + (B ) + (C) + (D), (A) + (B) + (C) + (D) + (E), (A) + (B) + (C) + (D ) + (E) + (F), and any one combination.

  The component (b) is conveyed in a molten state from the above (region 1: code 12) to (region 2: code 13) described later.

(Region 2: Symbol 13) is upstream of (Region 1: Symbol 12), and is continuously melted and kneaded with (b) component: thermoplastic resin other than the component (a) with respect to the molten conveyed product, From the second supply port 2, using the forced side feeder 1: code 5, the total amount of the powdery polyphenylene ether of the component (a) or a part of the component (a) and the part or the remaining amount of the component (b) Divided supply.
(Area 2: reference numeral 13) indicates that the powdered polyphenylene ether of component (a) is represented by each processing function of (I) solid transport process-2 → (II) melt mixing process → (III) melt transport process. This is the area where the process is executed.
If necessary, a melt mixing step as shown in (I) Solid conveying step-2 → (II) Melt mixing step → (III) Melt conveying step → (II) Melt mixing step → (III) Melt conveying step And the melt conveying step may be executed by dividing these steps finely.

  In particular, the powdery polyphenylene ether of the component (a) to be supplied and the molten (b) component conveyed from the (III) melt conveying step performed on the upstream side (region 1: reference numeral 12) join. The process performed in the part is referred to as (I) solid transport process-2 in (region 2), and (a) powdery polyphenylene ether in the solid state is added to the molten (b) component in the solid state without melting. This is a process of quickly mixing.

In (I) solid conveyance process-2 of (region 2: code 13), (a) powdery polyphenylene ether is supplied from the second supply port 2 using the forced side feeder 1 (code 5). In this case, since the bulk specific gravity of the powdered polyphenylene ether is small, a large amount of gas is also accompanied and supplied to the extruder, and the solid conveying ability is lowered.
In order to prevent a decrease in the solid conveying capacity, an opening hole for degassing (reference numeral 18 in FIG. 3) is provided on the upstream side of the upper lid of the extruder barrel at the site where the forced side feeder 1 (reference numeral 5) is connected. It is preferable to vent the gas from the opening hole.

(I) Solid conveying step-2 performed in (Area 2: reference numeral 13): The barrel set temperature of the extruder of reference numeral 15-2 is (a) not higher than the melting point of the powdery polyphenylene ether.
This set temperature is obtained by quickly mixing (a) powdered polyphenylene ether in a solid state with the component (b) in the molten state conveyed from upstream (region 1: reference numeral 12). This is an important temperature setting for preventing adhesion to the short axis portion of the screw in the molten state.
A preferred set temperature is 260 ° C. or lower, more preferably 240 ° C. or lower.
When the set temperature is equal to or higher than the melting point of (a) powdered polyphenylene ether, (I) Solid conveying step-2 performed in (Region 2: Reference 13): A large amount of semi-molten polyphenylene ether residue adheres.
In addition, the lower limit temperature of the set temperature is such that the molten (b) component conveyed from the upstream (region 1: reference numeral 13) is cooled by the solid state (a) powdered polyphenylene ether supplied here. The twin-screw extruder needs to be set to a temperature at which extrusion can be performed without causing torque over, and the set lower limit temperature needs to be selected depending on the type of the component (b) to be provided.

(I) Solid conveyance process-2 of (Area 2: code | symbol 13): The screw in the site | part which performs the code | symbol 15-2,
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(C) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0, 1 flight screw with flight angle α of 100-120 degrees,
(D) The twist angle is 12.5 to 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading disc diameter. A positive kneading disc having a ratio Lb / D of 0.05 to 1.0,
And (E) the twist angle is 80 to 100 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 1.0, the flight tip width Lb and the kneading disc diameter D 4 types of screw elements of a kneading disk having a ratio Lb / D of 0.05 to 1.0,
A combination of at least one screw element selected from the group consisting of:

In particular, (D) the screw structure composed of the positive kneading disk is (a) performed at the portion where the powdery polyphenylene ether is supplied. In order to execute (I) solid conveyance process-2: code 15-2 of (region 2: code 13), it is the most preferable screw configuration.
Thus, (a) powdery polyphenylene ether is melted and transported from (region 1: code 12) in the solid state in (I) solid transport process-2: code 15-2 of (region 2: code 13). After being mixed with the resin thus formed, in the next (region 2: reference numeral 13), the processing step (II) melt mixing step: reference numeral 16 → (III) melt transporting step: reference numeral 17 is performed.

(II) Melt mixing step performed in this (region 2: code 13): code 16 → (III) melt conveying process: the barrel set temperature of the extruder in code 17 is component (b) (a) The temperature is set to 300 ° C. or less at which thermoplastic resins other than the above can be melt processed.
By setting the barrel set temperature at 300 ° C. or lower, it is possible to prevent thermal degradation of the resin component. (I) Solid conveying step-2: A semi-molten polyphenylene ether residue is present in the screw short diameter portion of reference numeral 15-2. It can prevent adhesion.

The screw used in (II) melt mixing step → (III) melt conveying step performed in (region 2: code 13) is as follows:
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(B) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 1.5. Reverse screw element,
(C) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0, 1 flight screw element with flight angle α of 100 to 120 degrees,
(D) The twist angle is 12.5 to 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading disc diameter. 2-flight positive kneading disc with D ratio Lb / D of 0.05 to 1.0,
(E) The ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 1.0, and the flight tip width Lb is the ratio of the kneading disc diameter D. A kneading disc having an Lb / D of 0.05 to 1.0,
(F) The torsion angle is minus 12.5 to minus 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading A reverse kneading disk having a disk diameter D ratio Lb / D of 0.05 to 1.0, (G) a screw pitch length P1 to screw diameter D ratio P1 / D of 0.2 to 0.8, and a screw A mixing screw having a ratio L / D between the element length L and the screw diameter D of 0.3 to 3.0 and a screw flight portion having 2 to 10 notches between the screw pitches P1;
(H) The ratio P1 / D of the screw pitch length P1 and the screw diameter D is 0.2 to 0.8, and the ratio L / D of the screw element length L to the screw diameter D is 0.3 to 1.5. A mixing screw having a reverse thread screw element, the screw flight part having 2 to 10 notches between the screw pitches P1,
as well as,
(I) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0. A mixing screw having a 1 flight screw and a screw flight portion having 2 to 10 notches between screw pitches P1;
(A), (A) + (C) combined structure, (A) + (C) + (D) combined structure, (A) + (B) + (C) + (D) combined configuration, (A) + (B) + (C) + (D) + (E) combined configuration, (A) + (B) + (C) It is assumed that any one of + (D) + (E) + (F) and a combination of these elements (G), (H), and (I) is arbitrarily combined.

  After passing through (region 2: reference numeral 13), the composition is conveyed in a molten state to (region 3: reference numeral 14) described later.

  (Region 3: reference 14) is upstream (Region 2: reference 13), and the melted and kneaded material (b) and component (a) are continuously melted and kneaded as shown in FIG. In addition, from the third supply port 3, the forced side feeder 2: reference numeral 6 is used to divide and supply the remaining amount of the powdery polyphenylene ether of component (a) and / or the remaining amount of component (b). .

  In (region 3: reference numeral 14), as shown in FIG. 3, for the above-mentioned supply component, (I) solid conveying step-3: reference numeral 15-3 → (II) melt mixing step: reference numeral 16 → (III) Melt conveying step: The processing indicated by each processing function of reference numeral 17 is executed, and if necessary, (I) solid conveying step-3: reference numeral 15-3 → (II) melt mixing step: reference numeral 16 → (III) Melt conveying step: reference numeral 17 → (II) Melt mixing step: reference numeral 16 → (III) Melt conveying step: as shown by reference numeral 17, the melt mixing step and the melt conveying step are performed in finely divided steps. May be.

  The resin component supplied in (region 3: reference 14) and the upstream (region 2: reference 13) (III) melt transfer step: the portion where the molten resin component transferred from reference 17 merges Is called (I) solid conveyance process-3 (reference numeral 15-3) in (Area 3: reference 14), and is a process of quickly mixing a supply component in a solid state with a molten resin component.

In addition, in (I) solid conveyance process-3 in this (area | region 3: code | symbol 14), as shown in FIG. 2, using the forced side feeder 2 (code | symbol 6) from the 3rd supply port 3, (a) Powder When the polyphenylene ether is supplied, since the bulk specific gravity of the powder polyphenylene ether is small, a large amount of gas is also accompanied and supplied to the extruder.
In order to prevent this, an opening hole for degassing (reference numeral 19 in FIG. 3) is provided on the upstream side of the upper lid of the extruder barrel at the site where the forced side feeder 2 (reference numeral 6) is connected. It is preferable to perform degassing.

And the barrel preset temperature of the extruder which performs (I) solid conveyance process-3 of (Area 3: code | symbol 14), when (a) powdery polyphenylene ether of (a) component is included as a supply component, (a) powder It is set below the melting point of the polyphenylene ether.
This set temperature is obtained by quickly mixing the powdered polyphenylene ether in a solid state with the molten resin component conveyed from the upstream (region 2: reference numeral 13), and the powdered polyphenylene ether is melted in the short axis portion of the screw. This is an important temperature setting for preventing adhesion. The temperature is preferably 260 ° C or lower, more preferably 240 ° C or lower.
By setting such a set temperature, it is possible to effectively prevent a large amount of semi-molten polyphenylene ether residue from adhering to the short-diameter portion of the screw in (I) solid conveying step-3 in (Area 3: reference numeral 14). it can.

  Further, the lower limit temperature of the set temperature is that the molten resin component conveyed from upstream (region 2: reference numeral 13) is cooled by the solid state (a) powdered polyphenylene ether supplied here. The twin-screw extruder needs to be set to a temperature at which extrusion can be performed without causing torque over, and the set lower limit temperature needs to be selected depending on the type of the component (b) provided upstream.

And the screw in the site | part of (I) solid conveyance process-3 performed in (area | region 3: code | symbol 14) is the following.
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(C) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0, 1 flight screw with flight angle α of 100-120 degrees,
(D) The twist angle is 12.5 to 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading disc diameter. A positive kneading disc having a ratio Lb / D of 0.05 to 1.0,
as well as,
(E) The ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 1.0, and the flight tip width Lb is the ratio of the kneading disc diameter D. 4 types of screw elements of a kneading disc with Lb / D of 0.05 to 1.0,
It is comprised by the combination of at least 1 or more types of screw element chosen from the group which consists of.
In particular, (D) the screw configuration composed of the positive kneading disk is the most preferable screw configuration because (a) no screw residue is present in the portion for supplying the powdery polyphenylene ether.

As described above, for (a) powdery polyphenylene ether, (I) solid transport step-3: performed in (region 14: reference numeral 14) in a solid state (region 2: reference 13) After being mixed with the melt-conveyed resin, (II) melt mixing step: (16) → (III) melt transporting step: reference numeral 17 in (region 3: reference numeral 14) is successively performed. .
The barrel set temperature of the extruder in this (region 3: reference 14) (II) melt mixing step: reference 16 → (III) melt transfer step: reference 17 is the component (b) (a) The temperature is set to 300 ° C. or less at which thermoplastic resins other than the above can be melt processed.
By setting the barrel set temperature to 300 ° C. or less, it is possible to effectively prevent the heat deterioration of the resin component. It is possible to effectively prevent the tendency for a large amount of polyphenylene ether residue to adhere.

(II) Melt mixing step performed in (Area 3: reference numeral 14): Reference numeral 16 → (III) Melt conveying step: The screw at the site where reference numeral 17 is executed is
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(B) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 1.5. Reverse screw element,
(C) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0, 1 flight screw element with flight angle α of 100 to 120 degrees,
(D) The twist angle is 12.5 to 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading disc diameter. 2-flight positive kneading disc with D ratio Lb / D of 0.05 to 1.0,
(E) The ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 1.0, and the flight tip width Lb is the ratio of the kneading disc diameter D. A kneading disc having an Lb / D of 0.05 to 1.0,
(F) The torsion angle is minus 12.5 to minus 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading A reverse kneading disk having a disk diameter D ratio Lb / D of 0.05 to 1.0, (G) a screw pitch length P1 to screw diameter D ratio P1 / D of 0.2 to 0.8, and a screw A mixing screw having a ratio L / D between the element length L and the screw diameter D of 0.3 to 3.0 and a screw flight portion having 2 to 10 notches between the screw pitches P1;
(H) The ratio P1 / D of the screw pitch length P1 and the screw diameter D is 0.2 to 0.8, and the ratio L / D of the screw element length L to the screw diameter D is 0.3 to 1.5. A mixing screw having a reverse thread screw element, the screw flight part having 2 to 10 notches between the screw pitches P1,
as well as,
(I) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0. A mixing screw having a 1 flight screw and a screw flight portion having 2 to 10 notches between screw pitches P1;
And a combination of (A) + (C), (A) + (C) + (D), (A) ) + (B) + (C) + (D), (A) + (B) + (C) + (D) + (E), (A) + (B) + (C) ) + (D) + (E) + (F), and any combination of these elements (G), (H), and (I).

  (III) Melt conveying step performed in this (region 3: reference numeral 14): In reference numeral 17, all the components of the resin composition are melted and kneaded and discharged from the extruder through a die installed at the outlet of the extruder. Is done.

  In the method for producing the polyphenylene ether resin composition of the present embodiment, the component (c): additive is added to the above-described (region 1: reference 12), (region 2: reference 13), (region 3: reference 14). It can supply together with (a) component and (b) component from each supply port. Furthermore, it can also supply independently from the 3rd supply port 3 of (area | region 3: code | symbol 14).

  In addition, when supplying this (c) component, the screw structure and barrel preset temperature of an extruder are in the above-mentioned (area | region 1: code | symbol 12), (area | region 2: code | symbol 13), and (area | region 3: code | symbol 14). Performed under the conditions described.

In addition, (I) solid conveyance process-2: code | symbol 15-2, (I) solid of each of powder-form (c) component: an additive (area | region 2: code | symbol 13), (area | region 3: code | symbol 14), respectively. Conveyance step-3: In the case of supplying with a forced side feeder in reference numeral 15-3, since the additive of the powdery component (c) is also supplied to the extruder accompanied by many gases, the solid conveying ability is descend.
In order to prevent this, an opening hole for degassing (reference numeral 18 and reference numeral 19) is provided on the upstream side of the upper lid of the extruder barrel where the forced side feeder is connected, and the degassing is performed from the opening hole. Is preferred.

  And when adding (c) component in a liquid state, the supply port is (II) Melt mixing process: Code | symbol 16 or (III) Melt conveyance process: Code | symbol 17 of (Area 2: Code | symbol 13) and (II) Melt mixing step of (Region 3: reference 14): Reference numeral 16 or (III) Melt conveying step: A liquid addition nozzle is attached to the barrel of reference numeral 17, and the liquid component (c) is supplied to the plunger pump. It can be supplied by press-fitting with a liquid pump such as a gear pump.

(C) The screw of the twin-screw extruder in the part where the component is press-fitted,
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(G) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.2 to 0.8, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0. A mixing screw that is a positive screw and the screw flight part has 2 to 10 notches between the screw pitches P1;
(H) The ratio P1 / D of the screw pitch length P1 and the screw diameter D is 0.2 to 0.8, and the ratio L / D of the screw element length L to the screw diameter D is 0.3 to 1.5. A mixing screw having a reverse thread screw element, the screw flight part having 2 to 10 notches between the screw pitches P1,
as well as,
(I) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0. A mixing screw having a 1 flight screw and a screw flight portion having 2 to 10 notches between screw pitches P1;
These element types may be used singly or may have a screw configuration composed of a plurality of combinations.

  As the twin screw extruder used in the method for producing the polyphenylene ether resin composition of the present embodiment, it is preferable to use a meshing type co-rotating twin screw extruder.

Moreover, in the manufacturing method of the polyphenylene ether resin composition of this embodiment, all of (area | region 1: code | symbol 12), (area | region 2: code | symbol 13), and (area | region 3: code | symbol 14) of a twin screw extruder. Melting and kneading can also be performed with the vent port provided in the barrel of the region closed.
As a result, it is possible to prevent the resin from venting up during extrusion and to prevent thermal deterioration due to resin stagnation inside the vent port.
In particular, when producing a resin composition that easily vents up, it is preferable to employ a production method in which melt-kneading is performed with the vent port closed.

  In addition, when manufacturing the polyphenylene ether resin composition which is easy to generate | occur | produce a volatile substance at the time of extrusion, (area | region 1: code | symbol 12), (area | region 2: code | symbol 13), and (area | region 3: code | symbol 14) of a twin-screw extruder. It is preferable to manufacture in the state which provided the vent port in the barrel of the at least 1 area | region of this, and depressurized to 1-700 Torr using the vacuum pump from the vent port, and deaerated the volatile matter.

In addition, in the method for producing a polyphenylene ether resin composition, process control before the raw materials are charged into the twin-screw extruder is also important when consistently considering from raw material to composition pellet production.
Oxidation degradation is accelerated by melting and kneading the raw material resin accompanied by oxygen at a high temperature. The degradation product of the resin adheres to the short axis part of the screw by mixing oxidation degradation products into the polyphenylene ether resin composition. There is a risk of
In particular, powdered polyphenylene ether, which is one of the raw material resins, is in powder form, its bulk specific gravity is small, and its specific surface area is large, so it contains a large amount of oxygen and is oxidized and deteriorated by supplying it to a high-temperature extruder. Is expected to progress significantly.
For this reason, it is important to manage the oxygen concentration in the storage state and supply state of the raw material supplied during production. That is, it is preferable to manage the oxygen concentration of all raw materials from the raw material stock tank to the raw material supply port.

Specifically, each raw material is supplied to the twin-screw extruder in this order: stock tank → piping → heavy weight feeder with refill tank → piping → feed hopper → double-screw extruder. It is preferable to keep the oxygen concentration in the process line below 0.3% by volume.
In order to maintain this oxygen concentration, it is necessary to introduce an inert gas into each process line with improved airtightness, and it is usually preferable to introduce nitrogen gas and maintain the oxygen concentration below 0.3% by volume.

The raw material supply line leading to the first supply port 1 of the twin-screw extruder (region 1: reference numeral 12) is the inside of the stock tank 8, the inside of the piping under the stock tank 8, the inside of the refill tank of the heavy feed feeder, and the heavy feed feeder 7 to a supply path with improved airtightness between the hoppers, nitrogen gas is continuously introduced from a supply pipe provided at the lower part of the hopper, and the oxygen between the weight-type feeder and the hopper connected to each other It is preferable to control the concentration.
Specifically, it is preferable to control the oxygen concentration to less than 0.3% by volume by measuring with an oxygen concentration meter (for example, digital oximeter XO-326ALA manufactured by Shin Cosmos Electric Co., Ltd.) installed in the path.
The hopper is preferably an airtight hopper.

The raw material supply line leading to the second supply port 2 of (Section 2: Reference 13) of the twin screw extruder has a configuration in which a hopper is connected to the forced side feeder 1, and as a whole, the inside of the stock tank 8 and the stock tank 8 It is the supply path which raised the airtightness between the inside of lower piping, the refill tank of a heavy feed feeder, and the heavy feed feeder 7-hopper. It is preferable to continuously introduce nitrogen gas from a supply pipe provided at the lower part of the hopper to control the oxygen concentration between the weight type feeder and the hopper.
Specifically, it is preferable to measure with the oxygen concentration meter installed in the path and control the oxygen concentration to less than 0.3% by volume.
The hopper is preferably an airtight hopper.

Similarly, the raw material supply line leading to the third supply port 3 of the twin screw extruder (region 3: reference numeral 14) has a configuration in which a hopper is connected to the forced side feeder 2, and the inside of the stock tank 8 as a whole, This is a supply path that improves the airtightness between the inside of the piping under the stock tank 8, the inside of the refill tank of the heavy feed feeder, and the heavy feed feeder 7 to the hopper. It is preferable to continuously introduce nitrogen gas from a supply pipe provided at the lower part of the hopper to control the oxygen concentration between the weight type feeder and the hopper.
Specifically, it is preferable to measure with the oxygen concentration meter installed in the path and control the oxygen concentration to less than 0.3% by volume.
The hopper is preferably an airtight hopper.

  As shown in FIG. 2, the (region 1) has a stock tank 8 for stocking the component (b) supplied to the first supply port 1, and a hopper is connected to the first supply port 1. A weight type feeder 7 is connected to the hopper, and when the weight type feeder 7 is connected to the stock tank, between the stock tank and the weight type feeder, Further, it is preferable that nitrogen gas is supplied to a supply path between the weight type feeder and the hopper so that the oxygen concentration in the supply path is less than 0.3% by volume.

  In (region 2), as shown in FIG. 2, the second supply port 2 has a stock tank 8 for stocking the component (a) and component (b) supplied to the second supply port 2. , A forced side feeder 1 is connected, a hopper is connected to the forced side feeder 1, a heavy weight feeder 7 is connected to the hopper, and the stock tank 8 is connected to the heavy weight feeder 7. When connected and configured, nitrogen gas is supplied to a supply path between the stock tank 8 and the heavy-weight feeder 7 and between the heavy-weight feeder 7 and the hopper, and the supply The oxygen concentration in the path is preferably less than 0.3% by volume.

  In the (region 3), as shown in FIG. 2, the (a) component supplied to the third supply port 3 and the stock tank 8 for stocking the component (b) are provided. , A forced side feeder 2 is connected, a hopper is connected to the forced side feeder 2, a heavy weight feeder 7 is connected to the hopper, and the heavy weight feeder 7 includes When the stock tank 8 is connected, nitrogen gas is supplied to a supply path between the stock tank 8 and the heavy weight feeder 7 and between the heavy weight feeder 7 and the hopper, The oxygen concentration in the supply path is preferably less than 0.3% by volume.

  The twin screw extruder supplies the component (c) to the predetermined region when supplying the component (c) to at least one of the regions (region 1), (region 2), and (region 3). A stock tank 8 for stocking the component (c) is provided, and a hopper and a weight type feeder are sequentially connected to the first supply port of the (region 1), and the second of the (region 2). When the hopper and the weight type feeder are sequentially connected to the supply port, and the hopper and the weight type feeder are sequentially connected to the third supply port of the (region 3), Nitrogen gas is supplied to the supply path between the stock tank and the weight type feeder and between the weight type feeder and the hopper in the region where the component (c) is supplied. Less than 3% by volume It is preferable.

In addition, all these raw material supply paths have improved airtightness because the oxygen concentration is less than 0.3% by volume, and the space portion of the path for supplying the raw material by dropping the raw material is excluded by the volume of the raw material itself. Since gas is generated, it is preferable to provide an exhaust pipe for degassing.
For this reason, an exhaust pipe for degassing is installed so that the pressure does not increase in the raw material supply path whose airtightness is increased by continuously supplying nitrogen gas.
Specifically, an exhaust pipe for degassing is installed above the space inside the refill tank of the heavy-weight feeder 7 where the raw material falls from the stock tank 8 and above the space of the hopper where the raw material falls from the heavy-weight feeder 7. It is preferable.
When the oxygen concentration is less than 0.3% by volume, the total number of sunspot foreign substances in the obtained polyphenylene ether resin composition tends to be reduced.

[Characteristics of polyphenylene ether resin composition obtained by the method of the present embodiment]
In the method for producing the polyphenylene ether resin composition of the present embodiment described above, when the polyphenylene ether resin composition using powdered polyphenylene ether is produced using a twin screw extruder, the screw residue of the twin screw extruder is removed. It brings about the effect of reducing dramatically, and also brings about the effect of reducing the sunspot foreign material, carbide, etc. which are contained in the polyphenylene ether resin composition obtained by this method.

  As a method for confirming the screw residue of the twin screw extruder, for example, after producing a polyphenylene ether resin composition with a twin screw extruder for 3 hours, the twin screw is extracted from the extruder and the supplied powdered polyphenylene ether A method of visually confirming whether or not a part is wound around the short axis portion of the screw in a semi-molten state or a molten state can be employed, whereby the presence or absence of a residue can be determined.

If there is a screw residue, scrape the residue and measure it using a Fourier transform infrared spectrophotometer (FT-IR). Can be confirmed.
In addition, when the supplied powdery polyphenylene ether is in a powder form and remains in the short axis portion of the screw, semi-molten polyphenylene ether may exist under the powder.
In addition, when the powdery polyphenylene ether is below the metal of the screw base, the powdery polyphenylene ether is positioned as not being a screw residue.
The screw residue means that the supplied powdery polyphenylene ether changes in shape and remains in a semi-molten or molten state and wound around the short axis portion of the screw.

Further, as a method for confirming black spot foreign matter of the polyphenylene ether resin composition obtained by the method for producing the polyphenylene ether resin composition of the present embodiment, for example, the produced resin pellets are hot-pressed at 300 ° C. or less, and the diameter is 19 cm. , 3 discs with a thickness of 1 mm (a range of 19 cm ± 0.2 cm in diameter and a range of 1 mm ± 0.3 mm in thickness are allowed as the dimensional error of the disc) are made in total, 6 on each side of this disc (1700 cm ² equivalent) was used a lens with a spot size gauge loupe (e.g., Tokai Sangyo PEAK SCALE LUPE 20 times) and a method of measuring by observing the black spot foreign matter using.
Here, the black spot foreign matter includes, in addition to the obvious black traces present in the hot-pressed disc, including traces exhibiting a hue different from the disc base color, for example, a resin composition such as brown, yellow, white, etc. A hue portion different from the base of the object is counted as a black spot foreign material.
However, if the colorant, other additives, or one component of the resin composition is clearly poorly dispersed, it is not counted as a black spot foreign material.
Black spot foreign matter is counted according to the range of its diameter, and it is classified into the number of foreign matter with a diameter of less than 0.1 mm, the number of foreign matter with a diameter of 0.1 mm to less than 0.5 mm, and the number of foreign matters with a diameter of 0.5 mm or more. The total number of particles is expressed as the number of foreign objects (α).
In addition, the black spot foreign matter may have various shapes such as a circle, an ellipse, and a string, but when measuring the size of the black spot foreign matter, the length of the maximum diameter occupied by the shape is measured and counted. .
The number of foreign matters (α) in the polyphenylene ether resin composition obtained by the production method of the present embodiment usually tends to be reduced by 0.1 mm or more.

[Molded product of polyphenylene ether resin composition obtained by the method of the present embodiment]
The polyphenylene ether resin composition obtained by the production method of the present embodiment can be molded into various parts by various conventionally known methods such as compression molding, injection molding, extrusion molding, multilayer extrusion molding, profile extrusion molding, and hollow molding. Can be molded into a body.
Since the black spot foreign material in the resin composition is reduced, it is suitable for sheet, film and thin film applications.
Although there is no restriction | limiting in particular in the thickness of a sheet | seat and a film, 3-800 micrometers is preferable and 3-50 micrometers is more preferable.

(Use)
Sheets and films having these thicknesses include general sheet / film, stretched sheet / film, stretched aperture film, printed circuit board film, printed circuit board peripheral component, semiconductor package, data system magnetic tape, APS photographic film , Insulation materials such as film capacitors, motors and transformers, speaker diaphragms, automotive sheet sensors, wire cable insulation tape, TAB tape, generator slot liner interlayer insulation materials, toner agitators, lithium ion battery insulation washers, lithium ions Examples thereof include battery separators and in-vehicle lithium ion battery separators.

Examples of applications other than the sheet and film applications include secondary battery batteries, automobile mechanism parts, automobile exterior parts, and automobile interior parts.
Examples of automobile mechanism parts include air conditioner housings, heater housings, ducts, fuel tank protectors, connector housings, fuel filter housings, fuel filter caps, cooling fans, fan shrouds, timing belt covers, oil tanks, oil tank caps, radiators. A tank, an under cover, etc. are mentioned.
Examples of automotive exterior products include bumpers and bumper beams, low bumper stiffeners, side spoilers, front grills, rear garnishes, door outer handles, pillar covers, door mirror bodies, mat guards, splash boards, Examples include a cowl panel, a wheel cap, various clips, various fasteners, and a lamp housing.
Examples of automotive interior parts include instrument panels, door trim panels, console boxes, pillar trims, differential grills, meter-related parts (visors and cases), covers, rearview mirror bodies, seat bags, headrest guides, seat hinge covers, Seat belt related, trunk room cover / box, steering wheel, horn cover, shift lever, shift lever knob, pedals, etc.

  Furthermore, electric wires and cables obtained by coating metal conductors or optical fibers, fuel cases for solid methanol batteries, fuel cell water distribution pipes, water cooling tanks, boiler outer cases, ink printer printer peripheral parts and components, chassis, water piping It can be used as various molded products such as joints.

  Hereinafter, specific examples and comparative examples will be specifically described, but the present invention is not limited thereto.

<Raw material>
First, the raw material of the resin composition produced in the Example and comparative example which are mentioned later is shown.
[(A) component: powdery polyphenylene ether]
(A-1)
2,6-Dimethylphenol is oxidatively polymerized in a toluene solvent to give a reduced viscosity (0.5 g / dl, chloroform solution, measuring temperature 30 ° C.) of 0.51, a melting point of 259 ° C., and a bulk density of 0.53 Polyphenylene ether (a-2)
2,6-dimethylphenol is oxidatively polymerized in a toluene solvent, a powder having a reduced viscosity (0.5 g / dl, chloroform solution, measuring temperature 30 ° C.) of 0.34, a melting point of 257 ° C. and a bulk density of 0.48 Polyphenylene ether

[(B) component: other thermoplastic resin]
(B-1): Polystyrene Polystyrene G9504 manufactured by PSJ (melt flow rate measured at 200 ° C. and 5 kg load according to ISO1133 is 1.5 g / 10 min)
(B-2): High impact polystyrene High impact polystyrene H9152 manufactured by PSJ (melt flow rate measured at 200 ° C. and 5 kg load according to ISO 1133 is 5.5 g / 10 min)
(B-3): Homo-polypropylene Novatec PP EA9BT manufactured by Nippon Polypro Co., Ltd. (melt flow rate measured at 230 ° C. and 2.16 Kg load according to JIS-K7210 is 0.45)
(B-4): Homo-polypropylene Novatec PP MA4AHB manufactured by Nippon Polypro Co., Ltd. (melt flow rate measured at 230 ° C. and 2.16 Kg load according to JIS-K7210 is 5.9)

(B-5): hydrogenated block copolymer Polystyrene-hydrogenated polybutadiene-polystyrene structure (ABA), 42% bound styrene, 95,000 number average molecular weight of the whole polymer, The molecular weight distribution was 1.03, the number average molecular weight of the polystyrene part (A) was 19,900, the 1,2-vinyl bond amount of the polybutadiene before hydrogenation was 78%, and the hydrogenation rate of the polybutadiene part was 99.9%. .
Specifically, it was synthesized by the following procedure.
In a cyclohexane solvent in a reactor equipped with a stirrer substituted with nitrogen gas, n-butyllithium was added as a polymerization initiator and tetrahydrofuran as a 1,2-vinyl bond amount regulator of butadiene, and half of the total styrene used was added to the reactor. Feed to polymerize the polystyrene block.
Thereafter, all butadiene was supplied to the reactor, and butadiene was polymerized based on the living anion group of the polystyrene block chain to synthesize a polymer having a polystyrene-polybutadiene block structure.
Further, the remaining half of styrene was supplied to the reactor, and styrene was further polymerized based on the living anion group having a polybutadiene chain at the end, thereby polymerizing a block copolymer having a polystyrene-polybutadiene-polystyrene structure.
After completion of the polymerization, the hydrogenation reaction was carried out quantitatively by the method described in US Pat. No. 4,501,857 until the amount of ethylenically unsaturated bonds in the polybutadiene portion was less than 1%. A polymer was obtained.
To this polymer solution after the hydrogenation reaction, 0.3 part of 2,6-di-tert-butyl-p-cresol as a heat deterioration stabilizer was added to 100 g of the polymer, and cyclohexane as a solvent was removed by heating. A hydrogenated block copolymer component having a polystyrene-hydrogenated polybutadiene-polystyrene structure was obtained.

(B-6): Hydrogenated block copolymer Polystyrene-hydrogenated polybutadiene-polystyrene-hydrogenated polybutadiene structure (ABAB), bound styrene content 55%, whole polymer Number average molecular weight 99,000, molecular weight distribution 1.04, polystyrene part (A) number average molecular weight 27,100, 1,2-vinyl bond amount of polybutadiene before hydrogenation is 80%, hydrogenation rate of polybutadiene part Synthesized 99.9%.
The block copolymer before the hydrogenation reaction has the above-mentioned amount of bound styrene, the number average molecular weight of the whole polymer, and the amount of 1,2-vinyl bond in the polybutadiene part as described above. (B-6) is synthesized by the same method as (b-5) except that the polymer terminal polybutadiene = 3/1 (weight ratio) and butadiene is supplied in two parts so as to be polymerized. did.

(B-7): Polyphenylene sulfide DIC Corporation T-2G (300 ° C. measured melt viscosity 55 Pa · s)

[(C) component: additive]
(C-1): Styrene-glycidyl methacrylate copolymer Styrene and glycidyl methacrylate were radically copolymerized to synthesize a styrene-glycidyl methacrylate copolymer (weight average molecular weight 110,000) containing 5% by weight of glycidyl methacrylate.
(C-2): Aromatic condensed phosphate of liquid flame retardant
CR741 manufactured by Daihachi Chemical Industry Co., Ltd.

<Evaluation method>
Next, the evaluation method of the resin composition produced in the Example and comparative example which are mentioned later is shown.
[(1) Evaluation of screw residue after production]
The region where the resin composition was extruded for 3 hours with a twin screw extruder and all the resin inside the extruder was discharged after the extrusion was completed, and then the screw was immediately removed from the extruder, and the powdered polyphenylene ether was actually supplied. The screw structure in the part which performed (I) solid conveyance process, (II) melt mixing process, and (III) melt conveyance process of this was observed visually.
The observation results were evaluated according to the following criteria.
A: Powdery polyphenylene ether does not adhere at all, and the screw minor axis portion is in a metal base state.
B: Powdery polyphenylene ether is adhered, but when the powder is removed, the short axis part of the screw is in a metal base state.
C: Semi-molten state (powdered polyphenylene ether is attached, and when the powder is removed, the melted polyphenylene ether is wrapped around the minor axis of the screw)
D: Melted state (state in which polyphenylene ether clearly melted around the short axis portion of the screw)
If it was evaluation of A and B, it was judged that the screw residue was fully reduced.

[(2) Evaluation of black spot foreign matter in manufactured pellet]
The manufactured pellet-shaped resin composition was hot-pressed to obtain three disks having a diameter of 19 cm and a thickness of 1 mm.
Black spot foreign matter was measured on a total of 6 surfaces (equivalent to 1700 cm ² ) on each front and back of each disk.
The number of foreign objects (α) is counted according to the range of the diameter of the foreign object using a magnifying glass (PEAK SCALE LUPE 20 times manufactured by Tokai Sangyo Co., Ltd.) using a lens with a spot size gauge. The total number of foreign objects (α) and the number of foreign objects of 0.1 mm or more. It was measured.
The number of foreign matters was determined to be better as the number of foreign objects of 0.1 mm or more was smaller, and as the number of all foreign materials measured according to the above criteria was smaller.

<Resin composition>
[Examples 1 to 10], [Reference Example], [Comparative Examples 1 to 6]
The components (a), (b) and (c) shown in Tables 1 to 5 below were used.
The resin composition was manufactured based on the extrusion process flowchart shown in FIG. 2 using the twin-screw extruder (ZSK-40MC; L / D = 48, the product made by COPERION, Germany).
As shown in Tables 1 to 5 below, the oxygen concentration of the (a) component to (c) component supply line is controlled, the composition of the first supply port of the extruder, the composition of the second supply port and the third supply port And using the SCREW-1 and SCREW-2 extruder screws configured as shown in FIG. 3, control the set temperatures of the areas 1 to 3 and the portions where each step is performed as shown in Tables 1 to 5 Then, extrusion was performed at a screw rotation speed of 300 rpm for 3 hours to obtain resin composition pellets.

  As shown in Tables 1 to 5 above, all of the resin compositions of Examples 1 to 10 have sufficiently reduced screw residue, the number of foreign matters in the resin composition is small, and extremely good quality polyphenylene. An ether resin composition was obtained.

On the other hand, when the powdery polyphenylene ether is supplied from the second supply port on the side of the twin-screw extruder by comparing Example 1 with Comparative Example 1 and Example 2 with Comparative Example 2, the solid transport of the supply destination In the manufacturing method under the condition that the barrel set temperature in step-2 is set to be equal to or lower than the melting point of the powdery polyphenylene ether, there is no screw residue, but in the manufacturing method set to be higher than the melting point of the powdery polyphenylene ether, It was found that the melted polyphenylene ether remained around the short axis portion of the screw.
In addition, the black spot foreign matter existing in the production pellet is also reduced in the condition where the barrel set temperature in the solid conveying step-2 of the supply destination is set to be equal to or lower than the melting point of the powdered polyphenylene ether, and there are many screw residues. It turned out that the manufacturing method showed the tendency for the sunspot foreign material in a manufacturing pellet to increase.

  In addition, by comparing Example 5 with the reference example, the powdery polyphenylene ether was set to a melting point of the powdered polyphenylene ether from the second supply port and the third supply port on the side of the twin screw extruder. When supplied to the transport process-2 and the solid transport process-3, no wrapping / residue of the melted polyphenylene ether is observed in the short axis part of the screw, but the oxygen concentration of the powdered polyphenylene ether supply port is 0.3% by volume or more When it was, there existed a tendency for the total number of black spot foreign materials of the manufactured pellet to increase.

Further, Example 6 and Comparative Example 3, Example 7 and Comparative Example 4, Example 8 and Comparative Example 5, Example 9 and Comparative Example 7 were respectively compared, so that a powdered polyphenylene ether was twin-screw extruder. When the method of supplying from the first supply port and the method of supplying from the second supply port on the side of the twin screw extruder are compared under the same production conditions, the method of supplying the powdered polyphenylene ether from the first supply port It was found that the melted polyphenylene ether, which is a large amount of screw residue, remained in a state of being wound around the short axis portion of the screw in a portion near the melt mixing step at the most downstream portion of the solid conveying step-1. .
The production pellets obtained by this method had a large amount of black spot foreign matter, and many large black spot foreign matters were present.
On the other hand, the powdery polyphenylene ether was supplied from the second supply port on the side of the twin screw extruder, and the barrel set temperature of the supply destination solid conveying step-2 was set to the melting point of the powdered polyphenylene ether. The resin composition had no screw residue and showed a tendency to have less black spot foreign matter in the production pellets.

  The production method of the present invention has industrial applicability as a production technique of a polyphenylene resin composition having a very low impurity concentration with reduced screw residue.

DESCRIPTION OF SYMBOLS 1 1st supply port 2 2nd supply port 3 3rd supply port 4 Melt mixing process execution part 5 Forced side feeder 1
6 Forced side feeder 2
7 Heavy Feeder with Refill Tank 8 Stock Tank 9 Liquid Addition Port 10 Nitrogen Gas Supply Port 11 Exhaust Pipe 12 Region 1
13 Area 2
14 Region 3
15-1 Solid conveying process-1
15-2 Solid conveying step-2
15-3 Solid conveying step-3
16 Melting and mixing step 17 Melt conveying step 18 Degassing opening 19 provided on the upstream side of the barrel top lid 19 Degassing opening hole provided on the upstream side of the barrel top lid

Claims (22)

(A) Powdered polyphenylene ether: 1 to 99% by mass,
(B) Thermoplastic resin other than the above (a): 99 to 1% by mass
A process for producing a polyphenylene ether resin composition comprising:
A step of kneading the component (a) and the component (b) using a twin-screw extruder;
The method for producing a polyphenylene ether resin composition in which the twin-screw extruder has the following extrusion regions (region 1), (region 2), and (region 3) each having first to third supply ports. .
(Region 1)
The region where the total amount of the component (b) or a part of the component (b) is supplied from the first supply port of the twin-screw extruder,
When the component (b) in the solid state is conveyed by a screw (I: solid conveyance step-1),
Melting and kneading the component (b) (II: melt mixing step)
Conveying the component (b) in a molten state (III: melt conveying step);
It has a part that executes the three steps of
The screw is
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(B) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 1.5. Reverse screw element,
(C) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0, 1 flight screw element with flight angle α of 100 to 120 degrees,
(D) The twist angle is 12.5 to 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading disc diameter. 2-flight positive kneading disc with D ratio Lb / D of 0.05 to 1.0,
(E) The ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 1.0, and the flight tip width Lb is the ratio of the kneading disc diameter D. A kneading disc having an Lb / D of 0.05 to 1.0,
as well as,
(F) The torsion angle is minus 12.5 to minus 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading Reverse kneading disc having a ratio Lb / D of the disc diameter D of 0.05 to 1.0,
Of 6 types of elements,
The combination of the elements includes only (A), (A) + (C), (A) + (C) + (D), (A) + (B) + (C) + (D) combination configuration, (A) + (B) + (C) + (D) + (E) combination configuration, (A) + (B) + (C) + (D) + (E) + (F) is any one of the combination configurations,
The extruder barrel set temperature of the twin-screw extruder is 300 ° C. or less at which the thermoplastic resin (b) can be melt processed.
(Region 2)
(III) in the region (III) is a region continuous to the part that performs the melt conveying step,
The biaxial shaft provided with the second supply port with the total amount of the component (a) or a part of the component (a) and the part or the remaining amount of the component (b) under the melt conveyance of the component (b) (I) solid conveying step-2 in (region 2) to be supplied from the side of the extruder using the forced side feeder 1;
(II) melt mixing step of (region 2) for melt-kneading the supplied component (a) and component (b);
The (a) component and the (b) component are conveyed in a molten state (region 2) in (III) melt conveying step,
Has a part to perform the three steps,
Using the forced side feeder 1, the powdery polyphenylene ether of the component (a) is supplied,
The screw of the twin screw extruder in the (I) solid conveying step-2 of the part where the component (a) and the component (b) melted and conveyed from the (region 1) merge,
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(C) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0, 1 flight screw with flight angle α of 100-120 degrees,
(D) The twist angle is 12.5 to 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading disc diameter. A positive kneading disc having a ratio Lb / D of 0.05 to 1.0,
as well as,
(E) The ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 1.0, and the flight tip width Lb is the ratio of the kneading disc diameter D. 4 types of screw elements of a kneading disc with Lb / D of 0.05 to 1.0,
A combination of at least one screw element selected from the group consisting of:
The extruder barrel set temperature of the part for performing the (I) solid conveyance step-2 is not higher than the melting point of the (a) powdery polyphenylene ether,
The component (a) supplied in the (I) solid conveying step-2 and the component (b) of the melt supplied from the (III) melt conveying step in (region 1) are the same as those in (region 2). ) (II) melt mixing step, (III) melt transporting step,
The (II) melt mixing step and (III) melt transport step are steps of melt kneading the component (a) and the component (b), respectively, and a step of melt transport to (region 3).
The screw used in the (II) melt mixing step and the (III) melt conveying step,
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(B) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 1.5. Reverse screw element,
(C) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0, 1 flight screw element with flight angle α of 100 to 120 degrees,
(D) The twist angle is 12.5 to 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading disc diameter. 2-flight positive kneading disc with D ratio Lb / D of 0.05 to 1.0,
(E) The ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 1.0, and the flight tip width Lb is the ratio of the kneading disc diameter D. A kneading disc having an Lb / D of 0.05 to 1.0,
(F) The torsion angle is minus 12.5 to minus 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading Reverse kneading disc having a ratio Lb / D of the disc diameter D of 0.05 to 1.0,
(G) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.2 to 0.8, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0. A mixing screw that is a positive screw and the screw flight part has 2 to 10 notches between the screw pitches P1;
(H) The ratio P1 / D of the screw pitch length P1 and the screw diameter D is 0.2 to 0.8, and the ratio L / D of the screw element length L to the screw diameter D is 0.3 to 1.5. A mixing screw having a reverse thread screw element, the screw flight part having 2 to 10 notches between the screw pitches P1,
as well as,
(I) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0. A mixing screw having a 1 flight screw and a screw flight portion having 2 to 10 notches between screw pitches P1;
It is made up of a combination of these nine elements.
The combination of the elements includes only (A), (A) + (C), (A) + (C) + (D), (A) + (B) + (C) + (D) combination configuration, (A) + (B) + (C) + (D) + (E) combination configuration, (A) + (B) + (C) + (D) + (E) + (F), and a combination thereof, and any one of the configurations in which the elements (G), (H), and (I) are arbitrarily combined,
The extruder barrel set temperature in the (II) melt mixing step and the (III) melt transport step is 300 ° C. or less at which the (b) thermoplastic resin can be melt processed.
(Region 3)
(III) in the (region 2) is a region continuous to the part that performs the melt conveying step,
A twin screw extruder in which the remaining amount of the component (a) and / or the remaining amount of the component (b) is provided as a third supply port while the component (b) and the component (a) are melted and conveyed. (I) solid conveyance process-3 of (region 3) to be supplied from the side using the forced side feeder 2;
The (a) component and / or the (b) component separately supplied in the (I) solid conveyance step-3 of the (region 3), and the (a) component + (b) conveyed from the (region 2). (II) the melt mixing step of (region 3), wherein the melt kneaded product of the components is further melt kneaded;
Furthermore, the (a) component and the (b) component are conveyed in a molten state (region 3) in (III) the melt conveying step,
Has a part to perform the three steps,
Using the forced side feeder 2, the powdery polyphenylene ether of the component (a) and / or the component (b) is supplied, and the supplied component and the molten and transported resin of the (region 2) The screw of the twin-screw extruder used in (I) solid conveying step-3 of (region 3) performed in the joining part is
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(C) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0, 1 flight screw with flight angle α of 100-120 degrees,
(D) The twist angle is 12.5 to 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading disc diameter. A positive kneading disc having a ratio Lb / D of 0.05 to 1.0,
as well as,
(E) The ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 1.0, and the flight tip width Lb is the ratio of the kneading disc diameter D. A kneading disc having an Lb / D of 0.05 to 1.0,
Consisting of a combination of at least one screw element selected from the group consisting of four types of screw elements,
The extruder barrel set temperature in (I) solid conveying step-3 in (Region 3) is not higher than the melting point of (a) powdery polyphenylene ether,
In the (I) solid conveying step-3, the component supplied separately and the melt of (b) component + (a) component supplied from the (III) melt conveying step of (region 2) Is sent to the (II) melt mixing step of (Area 3) and the (III) melt transfer step,
The (II) melt mixing step and the (III) melt conveying step in (Region 3) are respectively
The final melt-kneading step of the component (a) and the component (b), and a step of melting and conveying to the end outlet of the twin-screw extruder,
The screw used in the (II) melt mixing step of the (region 3) and the (III) melt transfer step,
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(B) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 1.5. Reverse screw element,
(C) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0, 1 flight screw element with flight angle α of 100 to 120 degrees,
(D) The twist angle is 12.5 to 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading disc diameter. 2-flight positive kneading disc with D ratio Lb / D of 0.05 to 1.0,
(E) The ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 1.0, and the flight tip width Lb is the ratio of the kneading disc diameter D. A kneading disc having an Lb / D of 0.05 to 1.0,
(F) The torsion angle is minus 12.5 to minus 75 degrees, the ratio La / D of the kneading disc length La to the kneading disc diameter D is 0.3 to 2.0, the flight tip width Lb and the kneading A reverse kneading disk having a disk diameter D ratio Lb / D of 0.05 to 1.0, (G) a screw pitch length P1 to screw diameter D ratio P1 / D of 0.2 to 0.8, and a screw A mixing screw having a ratio L / D between the element length L and the screw diameter D of 0.3 to 3.0 and a screw flight portion having 2 to 10 notches between the screw pitches P1;
(H) The ratio P1 / D of the screw pitch length P1 and the screw diameter D is 0.2 to 0.8, and the ratio L / D of the screw element length L to the screw diameter D is 0.3 to 1.5. A mixing screw having a reverse thread screw element, the screw flight part having 2 to 10 notches between the screw pitches P1,
as well as,
(I) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0. A mixing screw having a 1 flight screw and a screw flight portion having 2 to 10 notches between screw pitches P1;
It is made up of a combination of these nine elements.
The combination of the elements includes only (A), (A) + (C), (A) + (C) + (D), (A) + (B) + (C) + (D) combination configuration, (A) + (B) + (C) + (D) + (E) combination configuration, (A) + (B) + (C) + (D) + (E) + (F), and a combination thereof, and any one of the configurations in which the elements (G), (H), and (I) are arbitrarily combined,
The extruder barrel set temperature in the (II) melt mixing step and the (III) melt conveying step is 300 ° C. or less at which the (b) thermoplastic resin can be melt processed. (A) Powdered polyphenylene ether: 1 to 99% by mass,
(B) Thermoplastic resin other than the above (a): 99 to 1% by mass,
Including
For a total of 100 parts by mass of the component (a) + the component (b),
(C) Additive: A method for producing a polyphenylene ether resin composition further comprising 0.1 to 70 parts by mass,
A step of kneading the component (a), the component (b) and the component (c) using a twin screw extruder;
The twin-screw extruder has the following (region 1), (region 2), and (region 3) extrusion regions each having first to third supply ports,
The method for producing a polyphenylene ether resin composition according to claim 1, wherein the component (c) is supplied to at least one of the (region 1), (region 2), and (region 3).   The method for producing a polyphenylene ether resin composition according to claim 1 or 2, wherein the (a) powdery polyphenylene ether is a particle having a bulk specific gravity of 0.2 to 0.8 or an average particle diameter of 1 to 2000 µm. (B): a thermoplastic resin other than (a)
4. One or two or more thermoplastic resins selected from the group consisting of polyolefin, hydrogenated block copolymer, styrene resin, polyamide, polyester, polyphenylene sulfide, and liquid crystal polyester. The manufacturing method of the polyphenylene ether resin composition of item. The additive of the component (c)
Admixtures, fillers, stabilizers, mold release agents, processing aids, flame retardants, anti-drip agents, nucleating agents, UV blockers, dyes capable of miscible with component (a) and component (b) 5. The production of a polyphenylene ether resin composition according to claim 2, wherein the additive is one or more additives selected from the group consisting of a pigment, an antioxidant, a plasticizer, and an antistatic agent. Method. (Region 2) and / or (Region 3) of the twin screw extruder,
Supplying a liquid additive as the component (c),
The method of supplying the liquid component (c) is the (II) melt mixing step or (III) melt transporting step of (region 2) and / or the (II) melt mixing step of (region 3) or ( III) A method in which a liquid nozzle is attached to the barrel of the part where the melt conveying step is performed, and the liquid (c) component is press-fitted with a liquid pump.
The screw of the twin-screw extruder in the part into which the component (c) is press-fitted,
(A) Ratio P1 / D of screw pitch length P1 and screw diameter D is 0.2 to 0.8, and ratio L / D of screw element length L to screw diameter D is 0.3 to 3.0. Positive screw element,
(G) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.2 to 0.8, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0. A mixing screw that is a positive screw and the screw flight part has 2 to 10 notches between the screw pitches P1;
(H) The ratio P1 / D of the screw pitch length P1 and the screw diameter D is 0.2 to 0.8, and the ratio L / D of the screw element length L to the screw diameter D is 0.3 to 1.5. A mixing screw having a reverse thread screw element, the screw flight part having 2 to 10 notches between the screw pitches P1,
as well as,
(I) The ratio P1 / D between the screw pitch length P1 and the screw diameter D is 0.3 to 2.0, and the ratio L / D between the screw element length L and the screw diameter D is 0.3 to 3.0. A mixing screw having a 1 flight screw and a screw flight portion having 2 to 10 notches between screw pitches P1;
The screw is configured by a single screw or a combination of a plurality of the elements (A), (G), (H), and (I). A method for producing the polyphenylene ether resin composition according to claim 1. The twin screw extruder has a configuration in which a vent port is provided in the barrel of the twin screw extruder in all the regions (region 1), (region 2), and (region 3).
The method for producing a polyphenylene ether resin composition according to any one of claims 1 to 6, wherein the vent port is closed. The twin-screw extruder has a configuration in which a vent port is provided in the barrel of the twin-screw extruder in at least one region of (Region 1), (Region 2), and (Region 3).
The method for producing a polyphenylene ether resin composition according to any one of claims 1 to 6, wherein the volatile component is degassed by reducing the pressure from 1 to 700 Torr using a vacuum pump from the vent port. A step of supplying the component (a) and / or the powdery component (c) to the (region 2) and (region 3) of the twin-screw extruder using a forced side feeder;
The method of supplying the component (a) and / or the powdery component (c) includes providing an opening hole for degassing on the upstream side of the upper lid of the barrel connected to the forced side feeder, and The method for producing a polyphenylene ether resin composition according to any one of claims 1 to 8, wherein the polyphenylene ether resin composition is supplied while degassing from the opening hole. A hopper is connected to the first supply port of (Area 1) of the twin screw extruder,
A weight type feeder is connected to the hopper,
The hopper is an airtight hopper in which an exhaust pipe is installed on the hopper.
Nitrogen gas is continuously introduced from a supply pipe provided at the lower part of the hopper, and the oxygen concentration between the weight type feeder and the hopper is less than 0.3% by volume,
The manufacturing method of the polyphenylene ether resin composition as described in any one of Claims 1 thru | or 9. A hopper is connected to the forced side feeder 1 of (region 2) of the twin-screw extruder, and a weight type feeder is connected to the hopper,
The hopper is an airtight hopper in which an exhaust pipe is installed on the hopper.
Nitrogen gas is continuously introduced from a supply pipe provided at the lower part of the hopper, and the oxygen concentration between the weight type feeder and the hopper is less than 0.3% by volume,
The manufacturing method of the polyphenylene ether resin composition as described in any one of Claims 1 thru | or 10. A hopper is connected to the forced side feeder 2 of (region 3) of the twin-screw extruder, and a weight type feeder is connected to the hopper,
The hopper is an airtight hopper with an exhaust pipe installed above the hopper,
Nitrogen gas is continuously introduced from a supply pipe provided at the lower part of the hopper, and the oxygen concentration between the weight type feeder and the hopper is less than 0.3% by volume,
The manufacturing method of the polyphenylene ether resin composition as described in any one of Claims 1 thru | or 11. The twin-screw extruder has a stock tank for stocking the component (b) to be supplied to the first supply port of the (region 1).
A hopper is connected to the first supply port, a weight type feeder is connected to the hopper, and the weight type feeder is connected to the stock tank,
Nitrogen gas is supplied to a supply path between the stock tank and the heavy weight feeder and between the heavy weight feeder and the hopper, and the oxygen concentration of the supply path is less than 0.3% by volume. The manufacturing method of the polyphenylene ether resin composition as described in any one of 1 thru | or 12. The twin-screw extruder has a stock tank for stocking the component (a) and component (b) supplied to the second supply port of the (region 2),
A forced side feeder 1 is connected to the second supply port,
The forced side feeder 1 is connected to a hopper,
A weight type feeder is connected to the hopper,
The weight tank is connected to the stock tank,
Nitrogen gas is supplied to a supply path between the stock tank and the heavy weight feeder and between the heavy weight feeder and the hopper, and the oxygen concentration of the supply path is less than 0.3% by volume. The manufacturing method of the polyphenylene ether resin composition as described in any one of 1 thru | or 13. The twin-screw extruder has a stock tank for stocking the component (a) and the component (b) supplied to the third supply port of the (region 3),
A forced side feeder 2 is connected to the third supply port,
A hopper is connected to the forced side feeder 2,
A weight type feeder is connected to the hopper,
The weight tank is connected to the stock tank,
Nitrogen gas is supplied to a supply path between the stock tank and the heavy weight feeder and between the heavy weight feeder and the hopper, and the oxygen concentration of the supply path is less than 0.3% by volume. The manufacturing method of the polyphenylene ether resin composition as described in any one of 1 thru | or 14. The twin-screw extruder has a stock tank that stocks the component (c) to be supplied to at least one of the (region 1), (region 2), and (region 3),
A hopper and a weight type feeder are sequentially connected to the first supply port of the (region 1),
A hopper and a weight type feeder are sequentially connected to the second supply port of (region 2),
A hopper and a weight type feeder are sequentially connected to the third supply port of the (region 3),
In (Area 1), (Area 2), and (Area 3), the stock tank is connected to each weight feeder,
Nitrogen gas is supplied to the supply path between the stock tank and the weight type feeder and between the weight type feeder and the hopper in the region where the component (c) is supplied. The method for producing a polyphenylene ether resin composition according to any one of claims 2 to 15, wherein the content is less than 3% by volume.   The method for producing a polyphenylene ether resin composition according to any one of claims 1 to 16, wherein the twin screw extruder is a meshing type co-rotating twin screw extruder.   The method for producing a polyphenylene ether resin composition according to any one of claims 1 to 17, wherein the thermoplastic resin other than (b) :( a) is a styrene resin.   The method for producing a polyphenylene ether resin composition according to any one of claims 1 to 17, wherein the thermoplastic resin other than (b) :( a) is a combination of a styrene resin and a hydrogenated block copolymer. .   The method for producing a polyphenylene ether resin composition according to any one of claims 1 to 17, wherein the thermoplastic resin other than (b) :( a) is a combination of a polyolefin and a hydrogenated block copolymer.   The method for producing a polyphenylene ether resin composition according to any one of claims 1 to 17, wherein the thermoplastic resin other than (b) :( a) is polyamide.   The method for producing a polyphenylene ether resin composition according to any one of claims 1 to 17, wherein the thermoplastic resin other than (b) :( a) is polyphenylene sulfide.