WO1998010019A1 - Composition de polycarbonate aromatique - Google Patents
Composition de polycarbonate aromatique Download PDFInfo
- Publication number
- WO1998010019A1 WO1998010019A1 PCT/JP1997/003046 JP9703046W WO9810019A1 WO 1998010019 A1 WO1998010019 A1 WO 1998010019A1 JP 9703046 W JP9703046 W JP 9703046W WO 9810019 A1 WO9810019 A1 WO 9810019A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- aromatic polycarbonate
- polymerization
- polymer
- supply port
- aromatic
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G64/00—Macromolecular compounds obtained by reactions forming a carbonic ester link in the main chain of the macromolecule
- C08G64/20—General preparatory processes
- C08G64/30—General preparatory processes using carbonates
- C08G64/307—General preparatory processes using carbonates and phenols
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
- C08L69/00—Compositions of polycarbonates; Compositions of derivatives of polycarbonates
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
- C08L51/00—Compositions of graft polymers in which the grafted component is obtained by reactions only involving carbon-to-carbon unsaturated bonds; Compositions of derivatives of such polymers
- C08L51/04—Compositions of graft polymers in which the grafted component is obtained by reactions only involving carbon-to-carbon unsaturated bonds; Compositions of derivatives of such polymers grafted on to rubbers
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
- C08L55/00—Compositions of homopolymers or copolymers, obtained by polymerisation reactions only involving carbon-to-carbon unsaturated bonds, not provided for in groups C08L23/00 - C08L53/00
- C08L55/02—ABS [Acrylonitrile-Butadiene-Styrene] polymers
Definitions
- the present invention relates to an aromatic polycarbonate composition. More specifically, the present invention relates to (1) a step of obtaining an aromatic polycarbonate (A) in a molten state, comprising: a 'molten mixture of an aromatic dihydroxy compound and diallyl carbonate'; At least one kind of polymerization raw material selected from the molten prepolymer obtained therefrom is subjected to a transesterification reaction in a polymerization vessel in the form of a liquid material to obtain a molten aromatic polycarbonate (A).
- the transesterification reaction of the polymerization raw material liquid, the evaporation surface area S (m 2 ) defined as the exposed surface area (m 2 ) of the polymerization raw material liquid is present in the polymerization vessel.
- the volume V (m 3 ) of the polymerization raw material liquid and the number average molecular weight of the aromatic polycarbonate to be produced! (2) adding the aromatic polycarbonate (A) in the molten state to the aromatic polycarbonate; A step of adding a different thermoplastic resin (B); and (3) a step of kneading the aromatic carbonate (A) and the thermoplastic resin (B). And an aromatic polycarbonate composition substantially the same as the above.
- Aromatic polycarbonate compositions are not only excellent in production efficiency, but also excellent in hue, and high quality aromatic polycarbonates with less silver generation and lowering of IZOD impact strength during molding. It is a carbonate composition.
- Aromatic polycarbonates are known as engineering plastics having excellent heat resistance, impact resistance, transparency, etc., and are widely used in many fields. In recent years, in particular, aromatic polycarbonate obtained by kneading aromatic polycarbonate and other resins to improve the formability of aromatic polycarbonate and the solvent resistance. Products are widely used in home appliances and automobiles.
- polymer alloy products produced from aromatic polycarbonate and other resins use an extruder to mix aromatic polycarbonate and other resins produced by the interfacial polycondensation method using phosgene. It is manufactured by kneading.
- toxic phosgene is produced because the above-mentioned method for producing aromatic polyester is an interfacial polycondensation method.
- the resulting aromatic polycarbonates are difficult to separate, such as impurities such as sodium chloride and residual methylene chloride. Because of this, when aromatic polycarbonate alloy products are manufactured using this, there are disadvantages such as a decrease in the thermal stability of the obtained products.
- aromatic polycarbonate alloy products are manufactured using this, there are disadvantages such as a decrease in the thermal stability of the obtained products.
- aromatic polycarbonate when aromatic polycarbonate is kneaded with another resin by an extruder, a high temperature is required for melting because a pellet-like or powder-like aromatic polycarbonate is used.
- the aromatic polycarbonate may be thermally degraded or the alloy product may be colored as a result.
- the Izod impact strength of the final aromatic poly-carbonate product is reduced. There was also a problem that the appearance of molded articles such as silver was poor.
- an aromatic dihydroxy compound and diaryl carbonate such as bisphenol A and diphenyl carbonate
- This is a transesterification method in which polymerization is performed while extracting phenol.
- the transesterification method is different from the interfacial polycondensation method in that it has the advantage that no solvent is used. There is an essential problem that it is difficult to remove the system out of the system, and it is difficult to increase the degree of polymerization. Therefore, raise the polymerization temperature and increase the viscosity of the polymer.
- the degree of polymerization is reduced to lower the degree of polymerization, but the resulting aromatic polycarbonate is colored, has a broad molecular weight distribution, and has a low impact resistance. Furthermore, even when used in combination with other resins, problems such as a reduction in color tone and Izod impact strength during molding and generation of silver occurred.
- polymerizers for producing aromatic polycarbonate by a transesterification method.
- the method of using a vertical stirring tank type polymerization vessel equipped with a stirrer is generally widely known.
- a vertical stirred tank type polymerization vessel has the advantages of high volumetric efficiency and simplicity.However, although polymerization can proceed efficiently on a small scale, it has been described above on an industrial scale. As described above, it is difficult to efficiently extract phenol produced as a by-product from the system as the polymerization progresses. However, if the polymerization rate becomes extremely low, there is a problem of radiation.
- a large-scale vertical stirring tank type polymerization vessel usually has a larger liquid depth ratio to the evaporation area than a small-scale polymerization vessel, that is, a so-called liquid depth.
- the pressure at the bottom of the tank increases.
- the lower part of the stirring tank has a liquid depth, so that it is polymerized at a substantially high pressure, phenol, etc. Is difficult to remove efficiently.
- Japanese Patent Publication No. 50-196600 discloses a method using a screw-type polymerization reactor having a vent part.
- Japanese Patent Publication No. 52-36 159 discloses a method using a compound twin screw extruder, and Japanese Patent Publication No. 53-571 18 (US Pat. Nos. 3,888,828).
- Japanese Patent No. 53-571 18 (Corresponding to No. 6) describes a method using a thin-film evaporator, for example, a screw evaporator or a centrifugal thin-film evaporator.
- Japanese Patent No. 39233 specifically discloses a method using a combination of a centrifugal thin-film evaporator and a horizontal stirring polymerization tank.
- horizontal polymerization vessels such as a screw-type evaporator and a horizontal stirring tank mainly improve the surface renewability of the rotary agitator as much as possible, thereby reducing the efficiency of phenol, etc. It is an attempt to extract it.
- Japanese Patent Publication No. 50-196600 states that "a relatively large and constantly renewing phase boundary occurs between a liquid reaction mixture and a gas or vapor space, The volatile reaction product that is separated from the liquid reaction product is removed very quickly. ”(Refer to the right of page 1 of the same publication, lines 19 to 22). It is suggested that the renewal and the like can be effectively extracted by the surface renewal effect. According to Japanese Patent Publication No.
- the surface renewal effect indicates the number of revolutions of the screw, the screw surface area of the reaction section, and the total pitch of the screw section of the reaction section.
- Raw material supply, and screw of the reaction section 1 pitch It is defined as a function of the total effective volume of the hit, and the importance of its value being within a predetermined range is pointed out.
- these polymerization reactors require a rotary stirring power such as a screw or a stirring shaft in order to enhance the surface renewability. As the viscosity increases, the viscosity increases markedly, requiring very large power. In addition, when the viscosity is high, when a large power is used, the polymer is subjected to a large shear, so that the molecular chain is cut.
- the rate of increase in the molecular weight is low, and Aromatic polycarbonate cannot be produced.
- the polymer had a significant adverse effect on polymer quality, such as coloring of the polymer due to a large share, and a decrease in heat resistance.
- the scale of the equipment is limited due to the limitation of the strength of the stirring shaft and the power, and the production of aromatic polycarbonate cannot be easily increased. There was also a problem on top.
- Japanese Patent Application Laid-Open No. 2-1539393 discloses a centrifugal thin film evaporator as a polycondensation reactor in the final stage of transesterification.
- the evaporative surface area per unit throughput of the reaction mixture can be increased, so that the residence time of the reaction mixture in the centrifugal thin film evaporator can be shortened, but it is generated.
- Some of the polymer adheres to the rotating shaft, blades, internal bearings, etc., and undergoes a long heat history.Therefore, there is a problem that blackened decomposed substances enter the polymer. One point is pointed out.
- the publication discloses a method in which a centrifugal thin film evaporator is used not at the final stage of the ester exchange reaction but at an intermediate stage.
- the centrifugal thin-film evaporator forms a thin film only on the inner wall of the evaporator, so that the volumetric efficiency of the polymerization device is extremely low, and if a sufficient reaction time is to be obtained, a sufficient reaction time is required.
- Another problem was that the actors were too large and industrially unfavorable.
- Japanese Patent Application Laid-Open No. 5-239331 discloses a combination of the centrifugal thin-film evaporator and a horizontal stirring polymerization tank.
- the aromatic polycarbonate obtained by the melt polymerization method is added to the aromatic polycarbonate while the aromatic polycarbonate is in a molten state.
- a step of obtaining an aromatic polycarbonate (A) in a molten state in which a molten mixture of an aromatic dihydroxy compound and a diaryl force is prepared.
- at least one kind of polymerization raw material selected from the molten prepolymer obtained therefrom is subjected to an ester exchange reaction in a polymerization vessel in the form of a liquid material to produce an aromatic polycarbonate in a molten state.
- V represents the volume (m 3 ) of the polymerization raw material liquid present in the polymerization vessel.
- n the number average molecular weight of the aromatic polycarbonate to be produced.
- an aromatic polycarbonate composition is produced by a method comprising the steps of: kneading (B) and, an extremely large stirring power is required in the above-described production process of the aromatic polycarbonate (A). Because of its high volumetric efficiency, it is not only excellent in production efficiency, but also excellent in hue, free of impurities and thermal decomposition products, and has a low Izod impact strength during molding and silver. It was found that a high-quality aromatic polycarbonate composition with little generation can be obtained. The present invention has been completed based on this new knowledge.
- a main object of the present invention is to provide an aromatic polycarbonate composition which is excellent not only in production efficiency but also in hue and less in generation of silver and lowering of impact strength at the time of molding. It is to be.
- FIG. 1 (a) is a schematic diagram showing one method of a polymerization method for obtaining an aromatic polycarbonate used in the present invention, wherein the requirements used for defining the above polymerization method are shown.
- re ⁇ in for the purpose of describing one is the evaporation surface area S (m 2) of; FIG. 1 (b), FIG] how to define the evaporation surface area S in the method (a) (m 2) In the schematic diagram shown;
- FIG. 2 (a) is a schematic diagram showing another method of the polymerization method for obtaining the aromatic polycarbonate (A) in a molten state used for obtaining the composition of the present invention.
- S (m 2 ) the evaporation surface area S (m 2 )
- FIG. 2 (b-1) is a schematic diagram showing a method of defining the evaporation surface area S (m 2 ) in the method of FIG. 2 (a);
- FIG. 2 (b-2) is another schematic diagram showing a method of defining the evaporation surface area S (m 2 ) in the method of FIG. 2 (a), and shows the polymerization reactor shown in FIG. 2 (b-1). As seen from above;
- FIG. 3 (a) shows the molten state used to obtain the composition of the present invention.
- Fig. 3 (b) is a schematic cross-sectional view showing an example of a polymerization vessel that can be used in a method for obtaining an aromatic polycarbonate (A); A sectional view along the ⁇ (b) ⁇ (b) line of FIG.
- FIG. 4 (a) shows another example of a polymerization vessel that can be used in the method for obtaining the aromatic polycarbonate (A) in the molten state used for obtaining the composition of the present invention.
- FIG. 4 (b) is an enlarged sectional view taken along line IV (b) -IV (b) of FIG. 4 (a);
- FIG. 5 is a schematic diagram showing still another example of a polymerization vessel that can be used in the method for obtaining the aromatic polycarbonate (A) in the molten state used for obtaining the composition of the present invention.
- FIG. 6 (a) shows a polymerization which can be used in a method for obtaining an aromatic polycarbonate (A) in a molten state used for obtaining the composition of the present invention.
- Fig. 3 is a schematic sectional view showing still another example of the vessel;
- FIG. 6 (b) is a cross-sectional view taken along the line VI (b) -VI (b) of FIG. 6 (a);
- FIG. 7 (a) is a schematic cross-sectional view showing still another method of a polymerization method for obtaining an aromatic polycarbonate (A) in a molten state used for obtaining a composition of the present invention. This is to explain the evaporation surface area S (m 2 ), which is one of the requirements used to define the above polymerization method;
- FIG. 7 (b) is a schematic cross-sectional view showing a method of defining the evaporating surface area S (m 2 ) in the method of FIG. 7 (a);
- FIG. 8 is a schematic diagram showing two modes of a method for obtaining the aromatic polycarbonate composition of the present invention.
- FIG. 9 is a schematic view showing another method for obtaining the aromatic polycarbonate composition of the present invention. Explanation of reference numerals
- the method for obtaining the aromatic polycarbonate (A) in a molten state includes a molten mixture of an aromatic dihydroxy compound and diallyl carbonate, and
- At least one kind of polymerization raw material selected from the group consisting of is subjected to a transesterification reaction in a polymerization vessel, wherein the polymerization raw material is present in a liquid form in the polymerization vessel, and The polymerization raw material liquid being subjected to ester exchange is reacted in a state having an exposed surface,
- S represents an evaporation surface area (m 2 ) defined as an exposed surface area (m 2 ) of the polymerization raw material liquid;
- V represents the volume (m 3 ) of the polymerization raw material liquid present in the polymerization vessel.
- n the number average molecular weight of the aromatic polycarbonate to be produced.
- thermoplastic resin (B) different from the aromatic polycarbonate to the obtained aromatic polycarbonate (A) in a molten state
- An aromatic polycarbonate composition substantially the same as the composition produced by the method comprising:
- the method for obtaining the aromatic polycarbonate (A) in a molten state includes: a molten mixture of an aromatic dihydroxy compound and dialkyl carbonyl; Molten polymer obtained by a process comprising reacting an aromatic dihydroxy compound with a diallyl carbonate
- At least one polymerization raw material selected from the group consisting of is subjected to a transesterification reaction in a polymerization reactor, wherein the polymerization raw material is present in a liquid form in the polymerization reactor, and is subjected to a transesterification reaction in the polymerization reactor. Reacting the polymerization raw material liquid being subjected to steal exchange in a state having an exposed surface,
- the transesterification reaction of the polymerization raw material liquid is represented by the following formula (I)
- S represents an evaporation surface area (m 2 ) defined as an exposed surface area (m 2 ) of the polymerization raw material liquid;
- V represents the volume (m 3 ) of the polymerization raw material liquid present in the polymerization vessel.
- n the number average molecular weight of the aromatic polycarbonate produced.
- thermoplastic resin (B) different from the aromatic polycarbonate to the obtained aromatic polycarbonate (A) in a molten state
- thermoplastic resin (B) to the aromatic polycarbonate (A) in the step (2) and the kneading in the step (3) are performed by a first supply port and a second supply port.
- An extruder wherein the second supply port is located downstream of the first supply port when the extruder is viewed in the extrusion direction, and the aromatic polycarbonate ( A) and the thermoplastic resin (B) are supplied to the extruder from the first supply port and the second supply port, respectively, and are kneaded in the extruder, wherein the aromatic resin Recombinant composition.
- the rubber graphite weight obtained by graft copolymerizing a thermoplastic resin (B) with a rubbery polymer and at least one vinyl compound capable of being graphitized with the rubbery polymer. Coalescing 10 to 10
- a rubber-reinforced resin comprising 0 parts by weight and at least one type of vinyl polymer of 90 to 0 parts by weight, wherein the total amount of the rubber graft polymer and the at least one type of vinyl polymer is 10 parts by weight. 3.
- the rubber reinforced resin is an ABS resin 4.
- thermoplastic resin supplied to the extruder from the second supply port 8. The thermoplastic resin supplied to the extruder from the second supply port
- thermoplastic resin (B) supplied to the extruder from the second supply port is in an unmelted state, and the kneading temperature is 280 ° C or lower.
- Aromatic polycarbonate composition 10.
- a polymerizer suitable for achieving and maintaining the reaction conditions satisfying the relationship of the above formula (I) is used. If polymerization is carried out, a high-quality aromatic polycarbonate with excellent heat resistance and no coloring or impurities can be produced at a high polymerization rate without the necessity of rotating and stirring with a very large power. The thing was obviously helpful. Therefore, in the present invention, the polycarbonate obtained by the above excellent method is kneaded with a thermoplastic resin other than the aromatic polycarbonate while in a molten state.
- the aromatic dihydroxy compound is represented by the following formula: It is a compound shown.
- Ar represents a divalent aromatic group having 5 to 200 carbon atoms.
- the divalent aromatic group Ar is preferably, for example, one represented by the following formula.
- a r 1 and A r 2 each independently represent a divalent carbocyclic or heterocyclic aromatic group having 5 to 70 carbon atoms.
- Y represents a divalent alkane group having 1 to 30 carbon atoms.
- one or more hydrogen atoms is replaced by another substituent that does not adversely affect the reaction, for example, a halogen atom, an alkyl group having 1 to 10 carbon atoms. Substituted by an alkoxy group having 1 to 10 carbon atoms, a phenyl group, a phenoxy group, a vinyl group, a cyano group, an ester group, an amide group, a nitro group, etc. It may be something.
- heterocyclic aromatic group examples include an aromatic group having one or more ring-forming nitrogen, oxygen or sulfur atoms.
- the divalent aromatic groups Ar 1 and Ar 2 are, for example, groups such as substituted or unsubstituted phenylene, substituted or unsubstituted biphenylene, and substituted or unsubstituted pyridylene. Represents The substituent here is as described above.
- the divalent alkane group Y is, for example, an organic group represented by the following formula.
- RR 2 , R 3 , and R 4 are each independently hydrogen, an alkyl group having 1 to 10 carbon atoms, an alkoxy group having 1 to 0 carbon atoms, and a cycle having 5 to 10 carbon atoms.
- B represents an alkyl group, a carbocyclic aromatic group having 5 to 10 carbon atoms, and a carbocyclic aralkyl group having 6 to 10 carbon atoms
- k represents an integer of 3
- R 5 and R 6 represent Each X is individually selected and independently of one another, represents hydrogen or an alkyl group having 1 to 6 carbon atoms, and X represents carbon, and R ′, R 2 , R 3 , R 4 , R 5 , R
- other substituents such as a halogen atom, an alkyl group having 0 carbon atoms, an alkoxy group having 0 carbon atoms, a phenyl group, and the like, to the extent that one or more hydrogen atoms do not adversely affect the reaction
- Examples of such a divalent aromatic group A r include those represented by the following formula.
- R 7 and R 8 each independently represent a hydrogen atom, a halogen atom, an alkyl group having 1 to 10 carbon atoms, an alkoxy group having 1 to 10 carbon atoms, and a ring having 5 to 10 carbon atoms.
- M and n are an integer of 1 to 4, and when m is 2 to 4, each R 7 may be the same or different; However, when n is 2 to 4, each R 8 may be the same or different.
- divalent aromatic group Ar may be one represented by the following formula.
- Ar Ar 2 is the same as described above, and Z is a single bond or one O—, one CO—, one S—, one so 2— , one so—,
- Examples of such a divalent aromatic group A r include those represented by the following formula.
- aromatic dihydroxy compound used in the present invention may be a single kind or two or more kinds.
- Aromatic dihydroxy compound A typical example is bisphenol A.
- the dial carbonate used in the present invention is represented by the following formula:
- Ar 3 and Ar 4 are each a monovalent group having 5 to 200 carbon atoms. Represents an aromatic group.
- a r 3 and A r 4 may represent a monovalent carbocyclic or heterocyclic aromatic group, in A r 3, A r 4 of this, one or more hydrogen atoms, adversely affect the reaction
- Other substituents such as a halogen atom, a C0 alkyl group, a C0 alkoxy group, a phenyl group, a phenoxy group, a vinyl group, a cyano group, an ester group, It may be substituted by a mid group or a nitro group.
- Ar 3 and Ar 4 may be the same or different.
- Representative examples of the monovalent aromatic groups Ar 3 and Ar 4 include a phenyl group, a naphthyl group, a biphenyl group and a pyridyl group. These may be substituted with one or more substituents described above.
- Preferred Ar 3 and Ar 4 include, for example, those represented by the following formulas.
- R 9 and R ′ ° are each independently a hydrogen atom, a carbon number
- P and q are integers of 5, and when p is 2 or more, each R may be different, and when q is 2 or more, each R 1 Q may be different. There may be. )
- unsubstituted diphenyl carbonates and lower alkyls such as diphenyl carbonate di-t-butyl carbonate are preferred.
- a symmetrical type of dial force such as a substituted diphenyl carbonate is preferred, but a diphenyl carbonate having a simplest structure is particularly preferred. .
- These giryl carbonates may be used alone or in combination of two or more.
- the ratio of the aromatic dihydroxy compound and the dialkyl carbonate used depends on the type of the aromatic dihydroxy compound and the dialkyl carbonate used, and the type of polymerization. Temperature other Depending on the polymerization conditions, the diaryl carbonate is usually present in an amount of from 0.9 to 2.5 moles, preferably from 0.95 to 2.0 moles, per mole of the aromatic dihydroxy compound. Monore, more preferably 0.
- the number average molecular weight of the aromatic polycarbonate (A) obtained in the above step (1) of the present invention is generally in the range of 500 to 100,000, preferably 2,100.
- the range is from 00 to 30 and 00.
- a molten mixture of an aromatic dihydroxy compound and diallyl carbonate, and an aromatic dicarbonate are used as a raw material for obtaining the aromatic polycarbonate (A).
- the polymerization reaction proceeds to some extent only by heating and melting a mixture of an aromatic dihydroxy compound and diaryl carbonate. It is essentially a molten prepolymer.
- the polymerization raw material is often referred to as “prepolymer”.
- the prepolymer in the case where the degree of repolymerization of the prepolymer is being increased by the method of the present invention may be simply referred to as “polymer” hereinafter.
- a molten prepolymer as a polymerization raw material in the method of the present invention May be obtained by any known polymerization method.
- the evaporation surface area S (m 2 ) is an index representing the area of the interface between the polymer liquid phase and the gas phase in the polymerization vessel, and is defined as the area of the exposed surface of the liquid material for polymerization.
- the gas-liquid interface has a complicated form that is undulated by stirring, foaming, and the like, and it is difficult to accurately determine the area thereof.
- the liquid polymer is formed by stirring or foaming. Assuming that there is no stationary state, the area of the exposed surface, that is, the evaporation surface area S (m 2 ) is obtained.
- a horizontal liquid level or a falling liquid level in a static state without agitation or foaming is assumed.
- the area (m 2 ) of the horizontal liquid surface or the falling liquid surface is defined as the evaporation surface area S (m 2 ).
- the polymer in the polymerization vessel is partially or entirely on the surface of a solid object such as the wall of the polymerization vessel or the guide wall of the guide.
- a solid object such as the wall of the polymerization vessel or the guide wall of the guide.
- this is often referred to as “polymer-flowing wall surface”.
- the flow-down wall has a uniform thickness on the polymer-falling wall surface and is similar or similar to the shape of the wall surface (for example, high viscosity If the liquid polymer flows down the wire,
- the peripheral shape of the polymer is larger and similar to the periphery of the wire> flowing liquidsurface, that is, a flat surface if the polymer flow-down wall is flat, and a cylindrical shape if cylindrical.
- the area of the falling liquid surface (m 2 ) is the evaporation surface area S (m 2 ) of the falling liquid polymer.
- the number of polymer falling wall surfaces can be up to the order of 0 ⁇ m. Irregularities are ignored and the surface is assumed to be smooth.
- the polymer when flowing down the polymer downflow wall, the polymer does not spread and flows down at the same flow width as the flow downflow area, and the area of the flowing down liquid surface (evaporation of the flowing down liquid polymer) Area)
- a pre-polymer supplied from the pre-polymer supply port on the upper side of the cylindrical polymerization vessel falls down to the lower part of the polymerization vessel along the inner wall of the polymerization vessel with the same width as when exiting the supply port. Then, the area of the falling liquid surface (the evaporation surface area of the falling liquid polymer) (m 2 ) is obtained.
- the width of the prepolymer at the time of exiting the supply port is determined by the viscosity of the prepolymer, the supply speed, and the design conditions of the supply port.
- the gas-liquid interface is not included in the evaporation surface area S (m 2 ) of the present invention. If there is a portion where the polymer falls without contacting either the guide or the inner wall surface of the polymerization vessel, the exposed surface area of the polymer falls within the scope of the present invention.
- the evaporation surface area Not included. If there are multiple guide liquid surfaces, the evaporation surface area S (m 2 ) of the falling liquid polymer in the present invention is the evaporation surface area S (m 2 ) of each falling liquid polymer. 2 ).
- the area obtained by adding the horizontal liquid surface area to the above-mentioned falling liquid polymer one liquid surface area is the evaporation rate in the present invention.
- the surface area is S (m 2 ).
- the liquid volume V (m 3 ) in the present invention represents the volume of a polymer substantially involved in polymerization in a polymerization vessel.
- the polymer capacity of the piping and the like attached to the reactor for transfer and temporary storage is not included in the liquid capacity V (m 3 ) in the present invention.
- FIG. 1 (a) is a schematic diagram of the state of polymerization in a vertical stirring tank, and a prepolymer having a liquid volume of V (m 3 ) is stirred while being fed from the raw material supply port 5 in a thread form. It shows a state where a complicated wavy gas-liquid interface is formed by stirring and foaming.
- Figure 1 () Shows a state in which the gas-liquid interface 4 is made flat without stirring and foaming while maintaining the liquid volume V (m 3 ) in FIG. 1 (a).
- the area of the horizontal liquid surface 4 determined in the state of FIG. 1 (b) is the evaporation surface area S (m 2 ) in the present invention.
- the liquid volume V (m 3 ) is calculated based on the weight of the prepolymer fed to the polymerization reactor and the amount of the polymer extracted from the polymerization reactor or the aromatic monohydrogen produced as a by-product.
- the weight of the liquid in the polymerization vessel is determined by subtracting the weight of the evaporant such as the oxy compound and the weight of the prepolymer in the piping, and this is converted into the volume from the specific gravity of the liquid at the polymerization temperature. And can be measured by [The evaporate includes, in addition to the aromatic monohydroxy compound, a small amount of diallyl carbonate, an aromatic dihydroxy compound, and a very low molecular weight prepolymer, depending on the polymerization conditions and the like.
- the weight of the evaporated aromatic monohydroxy compound, etc. can be determined by condensing the entire amount of the aromatic monohydroxyl compound, etc., distilled from the polymerization reactor vent, and measuring the weight of the condensate. .
- the liquid specific gravity is assumed to be 1,100 kg / m 3 .
- the weight of the by-produced aromatic monohydroxy compound and the prepolymer in the pipe is subtracted from the weight of the prepolymer supplied to the polymerization vessel.
- the weight of the liquid in the polymerization vessel is determined from this, and this is converted to the volume from the liquid specific gravity (1, 100 kg Zm 3 ) at the polymerization temperature. This can be measured.
- Figure 2 (a) shows a state in which the prepolymer is polymerizing while falling in a wet wall shape in a cylindrical polymerization vessel.
- Fig. 2 (b-1) and Fig. 2 (b-2) show the flowing liquid surface with the liquid volume shown in Fig. 2 (a), which is not wavy but has a uniform thickness on the wall surface and an arc-shaped cross section. This is the state assuming that is formed.
- the area of the falling liquid surface 4 having an arc-shaped cross section obtained as the state of FIGS. 2 (b-1) and 2 (b-2) is the evaporation surface area S (m 2 ) of the present invention. is there.
- FIG. 1 shows a state in which the prepolymer is polymerizing while falling in a wet wall shape in a cylindrical polymerization vessel.
- Fig. 2 (b-1) and Fig. 2 (b-2) show the flowing liquid surface with the liquid volume shown in Fig. 2 (a), which is not wavy but has a
- the side surface in the thickness direction of the liquid, which is substantially perpendicular to the falling liquid surface 4 is not a surface having the same shape or a similar shape as the wall surface. Not included in m 2 ).
- the pre-polymer supplied from the raw material supply port to the polymerization reactor exited from the supply port without expanding the polymerization reactor wall surface in the circumferential direction of the wall surface. It is assumed that it is falling with the width of time.
- the liquid volume V (m 3 ) is calculated based on the weight of the prepolymer supplied to the polymerization reactor, the amount of the polymer extracted from the polymerization reactor, and the aromatic monohydro by-product.
- the weight of the liquid in the repolymerizer is determined by subtracting the weight of vaporized substances such as oxy-compounds and the prepolymer in the piping, and this is converted into a volume from the liquid specific gravity at the polymerization temperature. Can be measured.
- the aromatic monohydroxy compound that evaporates from the weight of the prepolymer fed to the polymerization reactor and the amount of plastic in the piping are reduced. Calculate the liquid weight in the polymerization vessel by subtracting the weight of the repolymer, etc., and convert this to the volume from the liquid specific gravity (1,100 kg / m 3 ) at the polymerization temperature. This can be measured.
- FIG. 7 (a) the polymer falls along the inside of the polymerization vessel along the two cylindrical guides and comes into contact with the polymer on the adjacent cylindrical guide as shown in the cross section.
- FIG. 3 is a schematic view of a horizontal cross section in a state where polymerization is performed.
- Fig. 7 (b) assumes that the liquid volume of Fig. 7 (a) is not a wavy surface, but a two-column cylindrical polymer overlaps to form a falling liquid surface 4.
- FIG. The broken line portion in FIG. 7 (b) is not included in the vaporized surface area S (m 2 ) of the present invention because it is not in contact with the gas phase.
- the area of the falling liquid surface 4 indicated by the solid line in FIG. 7B is defined as the evaporation surface area S (m 2 ) in the present invention.
- each value of the evaporation surface area S (m 2 ), the liquid volume V (m 3 ), and the number average molecular weight! ⁇ N of the obtained aromatic polycarbonate (A) is as follows: The following formula (I);
- the type of the polymerization reactor is not particularly limited as long as it can achieve and maintain the reaction conditions satisfying the relationship of the formula (I) of the present invention, but the polymer flows down along the guide. It is a particularly preferable method to use a polymerization vessel that allows the polymerization to proceed at least. It is even more preferred if the guide is more than one guide. As the guide, various shapes such as a flat plate, a column, a cone, and a chain can be used.
- the guide becomes hollow and polymerizes while dropping the polymer to the outside of the guide, and a method of introducing a heat carrier into the hollow part and the inner wall surface of the guide hollow part It is also possible to polymerize the polymer while dropping the polymer and put a heating medium outside the guide.
- the polymerization vessel capable of achieving and maintaining the reaction conditions satisfying the relationship of the formula (I) of the present invention is as follows.
- One device may be used, or two or more devices may be used in combination.
- the method in the step (1) of the present invention may be carried out in the case where the polymerization raw material used has a relatively high viscosity (specifically, when the number average molecular weight is about 1,500 or more). Particularly useful.
- a prepolymer having a number average molecular weight of about 1,500 is obtained by polymerizing an aromatic dihydroxy compound and dialkyl carbonate using a vertical mixing tank.
- a method of producing and polymerizing the prepolymer using a polymerization vessel satisfying the conditions of the present invention is one of the preferable embodiments of the present invention.
- FIGS. 3 (a) and (b), FIGS. 4 (a) and (b), FIGS. 5, 6 (a) and (b) show specific examples of the polymerizer that can be used in the present invention. Examples will be described, but the polymerizer that can be used in the present invention is not limited to these specific examples.
- FIGS. 3 (a) and 3 (b) show a type of polymerization reactor 1 having a plurality of flat guides 7 and polymerizing while dropping the polymer 13 along the flat guides 7.
- FIG. Fig. 3 (a) is a schematic vertical sectional view showing a cross section of the flat guide in the longitudinal thickness direction
- Fig. 3 (b) is a line EI (b) of Fig. 3 (a).
- )-It is a sectional view along ⁇ (b).
- the prepolymer 3 introduced from the raw material supply port 5 is distributed to a plurality of flat guides 7 by a distribution plate 6 having holes.
- the discharged polymer can be supplied again to the raw material supply port 5 to further increase the molecular weight.
- Polymerization can be carried out either batchwise or continuously. In the case of using a batch method, it is possible to polymerize the discharged polymer while repeatedly supplying it to the raw material supply port 5.
- a continuous method a prepolymer is continuously supplied to the raw material supply port 5 and a polymer having a higher polymerization degree is continuously discharged from the outlet 10 or a new prepolymer is used.
- the polymer is continuously supplied to the material supply port 5, a part of the discharged polymer is continuously extracted, and the remaining polymer is again supplied from the material supply port 5 together with a new bleed polymer.
- a continuous supply method may be used.
- the polymerization vessel is reheated and kept warm by a jacket or a heater (not shown).
- the guide 7 can be fixed to, for example, a wire fixed to the distribution plate 6 or a wire suspended from the upper inner wall of the polymerization vessel
- This type of polymerization reactor can easily increase the production amount of aromatic polycarbonate (A) by increasing the area of the plate-shaped guides or increasing the number of plate-shaped guides, thereby increasing the scale-up. This is advantageous for industrial implementation.
- FIG. 4 (a) and 4 (b) show a type in which a plurality of cylindrical guides 7A are provided, and the polymer 3 is dropped and polymerized along the cylindrical guides 7A.
- FIG. 4 (a) is a schematic vertical sectional view of the polymerization vessel 1
- FIG. 4 (b) is a sectional view taken along a line W (b) -N (b) in FIG. 4 (a).
- the prepolymer 3 introduced from the raw material supply port 5 is distributed to a plurality of cylindrical guides 7A by a distribution plate 6 having holes. From the prepolymer 3 that falls along the cylindrical guide 7A, the aromatic monohydroxy compound and the like as by-products evaporate from the evaporation surface 4.
- the inside of the polymerization vessel is controlled under reduced pressure, such as aromatic monohydroxy compounds and inert gas supplied from the gas supply port 8 if necessary. Emitted from vent 9.
- the polymer with a higher degree of polymerization is discharged at the outlet 10 while falling.
- the liquid volume V (m 3 ) in the polymerization vessel and the area S (m 2 ) of the evaporation surface satisfy the relationship of the formula (I) with respect to the number average molecular weight ⁇ ⁇ ⁇ of the polymer to be discharged. Is necessary. It is also possible to supply the discharged polymer again to the raw material supply port 5 to further increase the molecular weight.
- the polymerization can be carried out in a batch or continuous manner.
- a continuous method a method in which prepolymer is continuously supplied to the raw material supply port 5 and a polymer having a higher degree of repolymerization is continuously extracted from the discharge port 10 or a new prepolymer polymer is used. Is continuously supplied to the raw material supply port 5, a part of the discharged polymer is continuously extracted, and the remaining polymer is again continuously supplied from the raw material supply port 5 together with a new prepolymer.
- a method of supplying water The polymerization vessel is heated again by a jacket or heater (not shown) to keep it warm.
- the guide 7 ⁇ can be fixed to, for example, the distribution plate 6, or can be fixed to a wire suspended from the upper inner wall of the polymerization vessel.
- FIG. 5 is a schematic vertical sectional view of a type of polymerization vessel 1 having a plurality of conical guides 7B and polymerizing while polymer 3 is dropped along the conical guides 7B.
- the pre-polymer 3 introduced from the raw material supply port 5 first falls along the uppermost conical guide, then falls along the second-stage conical guide, and then falls downward.
- the transition to the conical guide reaches the polymerization reactor bottom. From the falling prepolymer 3, by-products such as aromatic monohydroxyl compounds are evaporated from the evaporation surface 4.
- the inside of the polymerization reactor is controlled under reduced pressure, and aromatic monohydroxy compounds and the like, and inert gas supplied from the gas supply port 8 as necessary are vent ports. Emitted from 9
- the polymer with a high degree of polymerization while falling is discharged from the outlet 10.
- the liquid volume V (m 3 ) in the polymerization vessel and the area S (m 2 ) of the evaporating surface satisfy the relationship of the formula (I) with respect to the number average molecular weight ⁇ ⁇ n of the discharged polymer. It is necessary. However, in this case, when moving from one conical guide to the conical guide of the next stage, the polymer does not contact the guide portion of the conical guide and flows down by free fall.
- the area of the exposed surface of that part is not included in the evaporation surface area specified in the present invention. It is also possible to supply the discharged polymer to the raw material supply port 5 again to further increase the molecular weight.
- the polymerization can be batch or continuous. In the case of a batch method, it is possible to polymerize the discharged polymer repeatedly while supplying it to the raw material supply port 5. is there.
- As a continuous method a method in which a prepolymer is continuously supplied to the raw material supply port 5 and a polymer having a higher degree of polymerization than the discharge port 10 is continuously extracted, or a new prepolymer is used.
- the polymer is continuously supplied to the material supply port 5, a part of the discharged polymer is continuously extracted, and the remaining polymer is again supplied from the material supply port 5 to a new prepolymer polymer. And a method of continuously supplying the same.
- the polymerization vessel is heated and kept warm by a jacket or a heater (not shown).
- the umbrella-shaped one shown at the center of the polymerization vessel is, for example, a rib fixed to a rod protruding from the inner wall of the polymerization vessel, the upper inner wall of the polymerization vessel. It can be fixed to a wire suspended from the ground.
- This type of polymerization vessel can easily scale up and increase the production of aromatic polycarbonate (A) by increasing the area of the conical guide 7B. However, it is advantageous when industrially implemented.
- FIGS. 6 (a) and 6 (b) are provided with a plurality of cylindrical tubular guides 7C, and do not allow the polymer 13 to drop along the inner wall surface of the cylindrical tubular guides 7C.
- Fig. 6 (a) shows a schematic vertical cross-sectional view of a polymerization vessel 1 of a type to be polymerized
- Fig. 6 (b) shows a line VI (b)-VI (b) in Fig. 6 (a).
- FIG. The pre-polymer 3 introduced from the raw material supply port 5 is provided with a plurality of cylindrical tubular guides 7 C (in the shell section 11) by overflow. Fixed to the upper and lower walls).
- the evaporation surface 4 of the cylindrical tubular guide 7C ⁇ is an aromatic monohydroxy compound that is a by-product. Etc. evaporate.
- the inside of the polymerization reactor is controlled under reduced pressure, and the aromatic monohydroxy compound, etc., and the inert gas supplied from the gas supply port 8 as necessary, are ventilated. Exit 9 is discharged. The polymer with a high degree of polymerization during the fall is discharged at the outlet 10.
- the liquid volume V (m 3 ) of the polymerizer ⁇ and the area S (m 2 ) of the evaporating surface satisfy the relationship of the formula (I) with respect to the number average molecular weight ⁇ ⁇ of the discharged polymer. It is necessary. It is also possible to supply the discharged polymer again to the raw material supply port 5 to further increase the molecular weight.
- the polymerization can be performed in a batch mode or a continuous mode. When the batch method is used, the discharged polymer can be repeatedly supplied to the raw material supply port 5 for polymerization.
- a prepolymer is continuously supplied to the raw material supply port 5, and a polymer having a higher polymerization degree at the outlet 10 is continuously extracted, or a new prepolymer is used.
- Polymer is continuously supplied to the raw material supply port 5, a part of the discharged polymer is continuously extracted, and the remaining polymer is again continuously supplied from the raw material supply port 5 together with a new prepolymer.
- the shell portion 11, which is the space outside the cylindrical tube-shaped guide 7C, is heated by a heat medium, and the heat medium supplied to the heat medium supply port 12 is Heat medium outlet 13 As the heat medium, a known medium can be used.
- various heating media described in the heat exchanger handbook pages 109 to 110 (edited by the heat exchanger handbook editorial board, published by Nikkan Kogyo Shimbun, 5th edition), and specific examples thereof include heated steam and molten salt, SK-OIL # 260, SK-OIL # 240, and SK-OIL # 170.
- This type of polymerization reactor can easily increase and scale up the production of aromatic polycarbonate by increasing the number of cylindrical tubular guides 7 C. This is advantageous when implementing it.
- the liquid volume V is preferably 5% or more of the total volume of the polymerization vessel. If it is less than 5%, the size of the polymerization vessel becomes large, which is not preferable when industrially practiced.
- the value of the evaporation surface area S (m 2 ) is calculated by the following formula ( ⁇ ) with respect to the value of the production rate Q (kg Z hr) of the aromatic polycarbonate (A):
- the present invention provides a particularly preferable method for producing the aromatic polycarbonate composition of the present invention on an industrial scale.
- the production rate Q of the aromatic polycarbonate (A) in the step (1) of the present invention is not particularly limited, but is usually 1 kg / hr or more, generally 3 kg / hr or more. .
- the polymerization temperature in step (1) is usually from 100 to 350 ° C, preferably from 150 to 290 ° C. It is selected in the temperature range of C.
- an aromatic monohydroxy compound is generated, and the reaction rate is increased by removing the aromatic monohydroxy compound out of the reaction system. Therefore, by introducing an inert gas such as nitrogen, argon, helium, carbon dioxide or a lower hydrocarbon gas which does not adversely affect the reaction, the aromatic monohydroxy compound to be produced is converted. A method of removing by accompanying these gases or a method of performing the reaction under reduced pressure are preferably used.
- the preferred reaction pressure varies depending on the type, molecular weight, polymerization temperature and the like of the aromatic polycarbonate (A) to be produced. When bisphenol A and diphenyl carbonate are used as the raw materials for the polycarbonate (A), when the number average molecular weight is less than 1,000, it is 6,660.
- P a (50 mm H g) to normal pressure is preferable, and 400 Pa (3 mm H g) to the number average molecular weight of 1,000 to 2,000
- the range of 6,660 Pa (50 mmHg) is preferable, and the range of 2,670 Pa (20 mmHg) or less when the number average molecular weight is more than 2,000.
- it is preferably 1,330 Pa (10 mmHg) or less, and more preferably, 2667 Pa (2 mmHg) or less.
- the method of carrying out the reaction under reduced pressure and while introducing the above-mentioned inert gas is also preferably used.
- the transesterification reaction can be carried out without adding a catalyst, but is carried out in the presence of a catalyst as necessary to increase the polymerization rate.
- the polymerization catalyst is not particularly limited as long as it is used in this field, but it may be an alkali such as lithium hydroxide, sodium hydroxide, potassium hydroxide, calcium hydroxide, or the like.
- Metal and alkaline earth metal hydroxides; boron and aluminum such as aluminum hydride, sodium borohydride, tetramethylammonium borohydride Alkali metal salts, alkaline earth metal salts, quaternary ammonium salts of hydrides; Al metal such as lithium hydride, sodium hydride, calcium hydride, etc.
- Lithium metal hydrides lithium methoxide, sodium ethoxide, canoledium methoxide Alkali metals such as toxides and alkoxides of earth metals; lithium phenoxide, sodium phenoxide, magnesium phenoxide Alkali metals and alkaline earth metals such as xide, LiO—Ar—OLi, NaO-Ar-ONa (Ar is aryl group) Loxoides; organic acid salts of alkaline metals and alkaline earth metals such as lithium acetate, calcium acetate, sodium benzoate; zinc oxide, zinc acetate, zinc phenoxy Zinc compounds such as boron; boric oxide, boric acid, sodium borate, trimethyl borate, triptyl borate, triphenyl borate, (R'R 2 R 3 R NB (R 1 R 2 R 3 R or (R 'RR SR) PB (R 1 R 2 R 3 R) E d ⁇ Mubo rate such (R ',
- Germanium compounds such as sulfuric acid, dialkylsthoxide, dianolequinoles ducanoleboxylate, acid tin, ethyltin tributoxide, etc., or an alkoxy group or an aryloxy group bonded thereto
- Tin compounds such as tin compounds, organic tin compounds; lead oxides, lead acetates, lead carbonates, basic carbonates, alkoxides or aryls of lead and organic lead Compounds of lead such as oxide Substances; quaternary ammonium salts, quaternary phosphonium salts, quaternary arsonium salts, etc .; compounds of ammonia; antimony oxides, antimony compounds such as antimony acetate; manganese acetate, Mangan compounds such as manganese carbonate and borane; titanium compounds such as titanium oxide and titanium alkoxide or aryloxide; zirconium acetate, zirconium oxide and zirconium oxide Examples of the catalyst include zi
- these catalysts may be used alone or in combination of two or more.
- the amount of these catalysts is to aromatic dihydric mud alkoxy compounds of the raw materials, usually 1 0 8-1 wt. / 0, and preferred rather is chosen at 1 0 7 to 1 0 1 wt% range.
- the material of the polymerization vessel used in step (1) of the present invention is not particularly limited, but the material constituting at least the inner wall surface of the polymerization vessel is usually selected from stainless steel, nickel, glass, and the like. It is. There is no particular limitation on the material of the guide used in the present invention. Examples of preferable materials include metal, glass, and ceramics. Examples of metals include stainless steel, stainless steel, nickel, titanium, chromium, or alloys such as nickel.
- the thermoplastic resin (B) other than the aromatic polycarbonate is used in the step (2).
- Addition and kneading in step (3) can be carried out using widely known techniques for the method of addition and kneading In the above method, the molten state obtained in step (1) is used. Since the aromatic polycarbonate (A) does not undergo any further heat history due to cooling and re-melting, etc., it is possible to minimize the thermal degradation of the polycarbonate.
- Specific methods for adding the thermoplastic resin (B) include a method of adding the thermoplastic resin in the line from the final polymerization vessel to the kneader, a method of adding the thermoplastic resin to the hopper of the kneader, and a supply port of the kneader. Powder, pellets, etc.
- a heat stabilizer, a phosphorus-based flame retardant, etc. may be added to the molten aromatic polycarbonate (A) and the molten state. It may be added to the thermoplastic resin (B) and kneaded with them.
- Examples of the kneading method include an in-line mixer such as a polymer mixer, a single-screw extruder, a twin-screw extruder, an extruder such as a multi-screw extruder, a kneader or a kneader-extruder.
- the method used is mentioned. Among these, a method using a co-rotating twin-screw extruder is preferable.
- the co-rotating twin-screw extruder has not only good self-cleaning properties but also a heat stabilizer and a phosphorus-based flame retardant. And at the same time, excellent additive dispersibility and excellent ejection ability can be achieved when using additives such as This is advantageous.
- the preferred kneading method is a method using a co-rotating twin-screw extruder having two or more supply ports, and a co-rotating type having two or more supply ports and one or more vent ports.
- a method using a twin-screw extruder is more preferable.
- thermoplastic resin (B) added to the aromatic polycarbonate (A) in the step (2) and the kneading in the step (3).
- An extruder having one supply port and a second supply port, wherein the second supply port is located downstream of the first supply port when the extruder is viewed in the extrusion direction.
- the size of the extruder and the positional relationship between the first supply port and the second supply port are as follows: It is preferable to dissolve the thermoplastic resin (B) so that it can be kneaded and mixed with the aromatic polycarbonate.
- the thermoplastic resin (B) supplied from the second supply port is in a molten state, the distance from the second supply port to the discharge port and the length of the extruder are not that of the thermoplastic resin (B). It may be shorter than the extruder used in the molten state.
- the screw diameter of the extruder is set to D.
- the distance from the first supply port to the second supply port is preferably 1 to 10 D, and more preferably 2 to 6 D.
- the distance from the second supply port to the discharge outlet is generally 5 to 50 D, and preferably 10 to 25 D.
- the overall length of the extruder is preferably between 15 and 30D.
- the method for supplying the aromatic polycarbonate (A) in the molten state obtained in the step () to the first supply port of the extruder is not particularly limited. Generally, it is supplied to the first supply port (eg, hopper port) of the extruder by free fall or using a gear pump. Excellent to achieve discharge capacity gear pump connected by full La Nji like to first supply port directly line, an aromatic Zokupo Li car Bone bets on 1 ⁇ 1 0 0 kg / cm 2 with a gear pump Preference is given to feeding the extruder through the line by applying pressure.
- a known method can be used for supplying the thermoplastic resin (B) from the second supply port of the extruder, and is not particularly limited. In the present invention, generally, the thermoplastic resin (B) can be supplied to the extruder by using a feeder preliminary extruder.
- thermoplastic resin (B) When the thermoplastic resin (B) is supplied using a feeder, a known feeder can be used. Feeder's Examples include a weight feeder and a capacity feeder. Any of these feeders may be directly connected to the second feed port of the extruder, and the other feeders [side feeders (side arms) in FIGS. 8 and 9] 2) can be connected to the second feed port of the extruder. That is, the supply of the thermoplastic resin (B) to the second supply port in the unmelted state is performed by, for example, adding the unmelted thermoplastic resin (B) to the weight feeder or the capacity feeder. After supplying the thermoplastic resin (B) to the weight feeder or the capacity feeder and weighing it, the other feeder (Fig. (Corresponding to side feeder 21 in FIG. 8 and FIG. 9).
- thermoplastic resin (B) When the thermoplastic resin (B) is supplied using the pre-extruder, the second supply port of the main extruder for kneading the aromatic polycarbonate (A) and the thermoplastic resin (B) is used.
- the unextruded thermoplastic resin (B) is supplied to the pre-extruder connected to the pre-extruder, and is melted before the thermoplastic resin (B) reaches the second supply port.
- the thermoplastic resin (B) is supplied to the second supply port of the main extruder.
- the method of supplying in an unfused state is preferable because the heat history is small, and in particular, the above-mentioned thermoplastic resin (B) is preferably used as a weight feeder or a capacity feeder. And other feeders [The side feeders in FIGS. 8 and 9
- the aromatic compound it is preferable to knead the polycarbonate (A) and the thermoplastic resin (B) together with a heat stabilizer and, if necessary, a phosphorus-based flame retardant.
- a heat stabilizer and, if necessary, a phosphorus-based flame retardant.
- thermoplastic resin (B) there is no particular limitation on the method of supplying the above-mentioned additives such as the heat stabilizer and the phosphorus-based flame retardant to the extruder, and they may be supplied to the extruder together with the thermoplastic resin (B).
- the extruder has more than two feed ports [ie the extruder feeds other than the first and second feed ports for aromatic polycarbonate (A) and thermoplastic resin (B)] In the case of having a mouth], the above additive alone can be supplied to the extruder.
- additives such as a heat stabilizer and a phosphorus-based flame retardant are supplied to the extruder from the second supply port together with the thermoplastic resin (B), for example, a hen shell mixer, a super mixer, a turn bull mixer, The mixture obtained by uniformly mixing with the thermoplastic resin (B) using a ribbon blender or the like may be supplied from the second supply port, or may be measured using a measuring feeder.
- Thermal stabilizer A phosphorus-based flame retardant may be supplied from the second supply port together with the thermoplastic resin (B).
- the extruder has at least one other supply port other than the above-mentioned first supply port and second supply port, at least one of the above-mentioned heat stabilizer and phosphorus-based flame retardant is used. It may be supplied from two other supply ports.
- the kneading temperature varies depending on the type of the thermoplastic resin (B) and the like, but is generally in the range of 200 to 380.
- the thermoplastic resin (B) used in the present invention may be any resin that can be mixed with an aromatic polycarbonate, and is not particularly limited. Absent. Specific examples of the thermoplastic resin (B) include polystyrene, poly ( ⁇ -methylstyrene), styrene ′ maleic anhydride copolymer, styrene.acrylonitrile.
- Aromatic vinyl resins such as styrene copolymer, styrene 'methyl methacrylate copolymer; styrene / butadiene / acrylonitrile copolymer (ABS resin); Crylate 'Styrene' Atarilononitrino copolymer ( ⁇ AS resin), EPDM (Ethylene 'Propylene'Gen ternary copolymer)' Styrene 'Acryloni Gum reinforced resins such as triol copolymer (AES resin) and HIPS (high impact polystyrene); polyethylene, polypropylene, polybutene, and polyme Chilpentene, Ethylene 'propylene copolymer, Ethylene.
- ABS resin styrene copolymer
- ⁇ AS resin Crylate 'Styrene' Atarilononitrino copolymer
- EPDM Ethylene '
- Propylene Polyolefin resin such as gen copolymer, etc .
- Polyester resins such as polyester resin; polyamide resins such as Nylon 6, Nylon 66, Nylon 610, Nylon 11 and Nylon 12; Acrylic resins such as polymethyl methacrylate; Gen-based rubbers such as polybutadiene and polyisoprene;
- Polyphenylene sulfide, Polyphenylene Polyether resins such as polyester, polyoxymethylene, polynorethone, polyethersulfone, and polyetheretherketone; and thermoplastic polyurethane.
- rubber reinforced resin such as ABS resin, polyethylene terephthalate, polybutylene terephthalate, Polypropylene, styrene ⁇ Acrylonitrile copolymer and polybutadiene are preferred, and ABS resin is particularly preferred.
- thermoplastic resin (B) a rubber-reinforced resin that is preferably used as the thermoplastic resin (B) will be described below.
- the rubber reinforced resin preferably used in the present invention is a rubber obtained by graft copolymerizing a rubber-like polymer with at least one vinyl compound capable of being copolymerized with the rubber-like polymer.
- a rubber-reinforced resin comprising 10 to 100 parts by weight of a graphite polymer and 90 to 0 parts by weight of at least one kind of vinyl polymer (the rubber graphitic polymer and the at least Also, the total amount of one type of polymer is 100 parts by weight.
- the above-mentioned bullet polymer may be a beer polymer produced by polymerizing at least one kind of the above-mentioned bullet compounds in the above-mentioned graphitization process.
- a vinyl polymer produced at the same time as the graphitization using a compound other than the beer compound to be used, or a separately prepared compound may be used.
- the rubber-reinforced resin may be added to the molten polycarbonate (A) in the form of a mixture as it is, or may be added to the molten polycarbonate (A) after melt-kneading.
- the rubbery polymer used in the present invention includes polybutadiene, Synthetic rubbers such as polyisoprene, polychloroprene, butadiene-styrene copolymer, butadiene-acrylonitrile copolymer, etc. It is an acrylic rubber such as propylene rubber, ethyl acrylate polymer, or butyl acrylate polymer, but is preferably a conjugated rubber, polybutadiene. Butadiene-styrene copolymer and butadiene-acrylonitrile copolymer. These can be used in combination of two or more.
- the content of the rubbery polymer in the rubber reinforced resin is generally 3 to 80% by weight. /. And preferably 5 to 50 weight. / 0 . If the amount is less than 5% by weight, a rubber-reinforced resin having sufficient impact resistance cannot be obtained, and if the amount exceeds 80% by weight, the fluidity and the gloss of the molded product of the aromatic polycarbonate composition at the time of molding are processed. Decreases and is not preferred.
- the preferred particle size of the rubber-like polymer in the rubber-reinforced resin is not particularly limited because it differs depending on the type of the vinyl polymer constituting the sea part in the rubber-reinforced resin having a sea-island structure.
- the particle size is 0.15 to 0.6 m, preferably 0.2 to 0.5 ⁇ , more preferably 0.2 to 0.2 m, as measured on the particles before photopolymerization. It is 5 to 0.45 ⁇ .
- the particle size is less than 0.15 ⁇ m, a rubber-reinforced resin with sufficient impact resistance cannot be obtained, and when the particle size exceeds 0.6 ⁇ , the aromatic polycarbonate composition can be obtained. Molded products manufactured from objects Gloss value is lowered.
- Examples of the rubber compound that can be copolymerized with the rubber-like polymer particles used in the present invention include aromatic vinyl compounds such as styrene, ⁇ -methylstyrene, and paramethylstyrene; Alkyl (meta) acrylates such as relate, methylacrylate, butylacrylate, ethyl acrylate, etc .; acrylate, methacrylate, etc.
- (Meth) acrylinoleic acids Cyanide vinyl compounds such as Atari mouth-trinole and methacrylonitrile; ⁇ , / 3-unsaturated carboxylic acids such as maleic anhydride Acids; ⁇ — phenyl mare mide, ⁇ — methyl mare mide, ⁇ — maleic compounds such as cyclohexyl mei lamid, etc .; dali such as glycidyl methacrylate If a compound containing a sidyl group However, preferred are aromatic vinyl compounds, alkyl (meth) acrylates, cyanated butyl compounds, and maleimide-based compounds. Chile, acrylonitrile, ⁇ —Feelmer Reid, and butyl acrylate. These vinyl compounds can be used alone or in combination of two or more.
- aromatic vinyl compounds such as styrene, ⁇ -methylen-st
- These vinyl compound polymers and copolymers can be used alone or in combination of two or more.
- the method for producing the rubber-reinforced resin is not particularly limited, and it can be produced by a known method.
- the ash content of the rubber-reinforced resin used in the present invention is 0.1% by weight. /. It is preferably below, more preferably 0.08% by weight.
- a rubber-reinforced resin having an ash content of more than 0.1% by weight is used, the molecular weight of the aromatic polycarbonate decreases during the production of the aromatic polycarbonate composition or when the above-mentioned composition is molded, and the composition becomes low. The impact resistance of the product is reduced. If silver is generated in the future, there may be a disadvantage.
- the rubber-reinforced resin is used as the thermoplastic resin (B), as described above, the rubber-reinforced resin is used in the unextruded state of the extruder in order to avoid unnecessary heat histories.
- a temperature of 280 ° C. or less When kneading at a temperature exceeding 280 ° C, the rubber component of the rubber-reinforced resin tends to deteriorate and agglomerate, and the mechanical properties of the obtained aromatic polycarbonate composition tend to decrease. .
- the blending amount of the thermoplastic resin (B) with the aromatic polycarbonate (A) is 1: 9 as the weight ratio of the thermoplastic resin (B) to the aromatic polycarbonate (A). It is preferably in the range of 9 to 99: 1, more preferably 10: 90 to 90: 10 and particularly preferably 10: 90 to 50. : In the range of 50.
- the heat stabilizer used in the present invention is not particularly limited, and those conventionally used in aromatic polycarbonates can be used.
- a phosphorus-based stabilizer a phenol-based stabilizer, an azo-based stabilizer, an epoxy-based stabilizer, a hindered-amine stabilizer, and the like can be used.
- Examples of the phosphorus-based stabilizer include a phosphorus-containing acid, a phosphite ester, a phosphinate ester, a phosphite ester, and a phosphonate ester.
- Examples of the phosphorus-containing acid include phosphoric acid, phosphorous acid, hypophosphorous acid, pyrrolic acid, polyphosphoric acid, and are represented by the following formula (HI).
- R 1 ′ represents an ethyl group, a butyl group, an octyl group, a cyclohexyl group, a 2-ethylhexyl group, a decyl group, a tridecyl group, a laurenole group, a pentaerythritol group, Alkyl group such as stearyl group; aryl group such as phenyl group and naphthyl group; or trinole group, P—t-butynolephenine group, 2,4—di-t-butylene It represents an alkylaryl group such as a bino group, a 26-di-butylphenyl group, a paranonylphenyl group, a dinoylphenyl group, etc.)
- phosphonic acid represented by the above formula (IV) examples include phenylphosphonic acid. These compounds may be used alone or in a mixture.
- phosphite esters examples include phosphite triesters and phosphite diesters represented by the following formulas (V) to ⁇ ).
- Phosphorus monoester examples include phosphite triesters and phosphite diesters represented by the following formulas (V) to ⁇ ).
- R 21 and R 23 are each independently a hydrogen atom; ethyl, butyl, octyl, cyclohexyl, 2-ethylhexyl; Alkyl groups such as ole group, decyl group, tridecyl group, rauryl group, pentaerythritol group and stearyl group; aryl groups such as phenyl group and naphthyl group; Or tril group, P-t-butylphenyl group, 2,4-di-t-butylphenyl group, 2, 6-di-t-butylphenyl group, norano-ninolephenyl group, Represents the Arukirua Li Lumpur groups such Gino alkenyl phenyl group, R '7, R 2 4 Waso respectively independently alkylene Les emission group, ⁇ re re down group, or ⁇ Li one Rua Ruki les emissions group Represents )
- linsant triester include tris (2,4-di-t-butylphenyl) phosphite and tris (noninoleffe).
- Phosphite Tris (Zininolefene) Phosphite, Triphenylphosphite, Tetraphenyldipropylene glycol phosphate , Tetra (tridecyl) 4,4'-iso-propylidene diphenyl diphosphite, bis (tridecinole) pentaerythritol diphosphite, bis (no Ninolef pentyl erythritol monophosphate phosphite, bis (2,4—di-t-butylphenyl) pentaerythritol rudiphosphite, bis (2,6— Di-t-butyl-4_methyl phenyl Pentaerythritol diphosphate, distearyl, penta
- Phosphorous ester having 4-di-t-butylphenyl group or 2,6-di-t-butylphenyl group is particularly preferred because it improves the hydrolysis resistance of aromatic polycarbonate.
- particularly preferred phosphorous acid triesters include tris (2,4-di-t-butylphenyl) phosphite, bis (2 , 4 — di-tert-butylphenyl) pentaerythritol diphosphite, bis (2,6-di-t-butyl-41-methylphenyl) pentaerythritol diphosphite Are listed.
- Preferred examples of the phosphite diester include an aromatic phosphite diester.
- Specific examples of the aromatic phosphite diester include diphenylhydrogenphosphite, bis (noninolephenyure), hydridogenphosphite, and bis (2,
- phosphorous acid monoesters include phenyldihydrogen phosphite, noninoleffe enignoresin hydrogen phosphite, and 2,4-dithiophene. Butyl phenylene phosphide and the like. These compounds may be used alone or as a mixture.
- phosphinic esters include the following formula (K) and Examples thereof include monophosphonic acid monoesters and phosphinic diesters represented by ().
- R 25 is ethyl, butyl, octyl, cyclohexyl, 2-ethylhexyl, decyl, tridecyl, rauryl, pentaerythritol
- Alkyl group such as phenyl group, stearyl group, etc .; aryl group such as phenyl group, naphthyl group; or trinole group, p-t-butylphenyl group, 2,4-di-t-butynolephenyl group , 2, 6 - di t - butylphenyl group, Bruno La Bruno Yuteuriru group, and display the Arukirua re Ichiru group such Gino Yucouiru group, R 2 6 R 27, R 28, R 29, R 31 and R 32 Waso
- R 3 represents an alkylaryl group such as a butylphenyl group, a 2,6-dibutynolephenyl group, a noranonylphenyl group or a dinonylphenyl group; Represents an alkylene group, an arylene group or an arylalkylene group.
- a specific example of such a compound is tetrakis 4,4'-biphenylenediphosphonate (2,4-di-t-butylphenyl). These compounds may be used alone or as a mixture.
- Examples of phosphoric acid esters include phosphoric acid monoesters and phosphoric acid diesters represented by the following formulas (XI)-(XIV)
- R 13 , R 1 ⁇ R 16 , R 17 , R 18 , R 19 , R 21 , R 23 R 24 are as defined above.
- phosphoric acid ester examples include diphenylhydrogenphosphate, bis (noninolefenyl) hydrogenphosphate, and bis (2,4-di-t).
- phosphoric acid monoesters include phenyldihydrogenphosphonate, nonylphenyldihydrogenphosphonate, and 2,4-g butylphenylhydrogenphosphate. And the like. These compounds are used alone Or mixed and used.
- Examples of the phosphonate include a phosphonate monoester represented by the following formula (XV).
- R 25 , R 27 , R 23 , R 3 U , R 31 and R 32 are as defined above.
- phenol-based stabilizer there can be mentioned a compound represented by the following formula (X ⁇ ⁇ ⁇ ⁇ ).
- each R 33 independently represents a hydrogen atom, a hydroxyl group, an alkoxyl group, or a substituted or unsubstituted hydrocarbon residue, provided that at least one of R 33 is substituted. Represents an unsubstituted hydrocarbon residue.
- Preferred phenolic stabilizers are those represented by the following formula (XVK).
- R 34 represents a methyl group or a t-butyl group
- R 35 represents a t-butyl group
- A represents a b-valent hydrocarbon or heterocyclic residue having 1 to 30 carbon atoms.
- A represents an integer of 1 to 4, and b represents an integer of 1 or more.
- phenolic stabilizers containing a phosphorus atom such as 3,5-di-t-butyl-14-hydroxybenzodinolephosphonate-ethylenol ester, bis (3,5-diene) 1-butylinole 4-hydroxyethyl phosphonate) Calcium and the like. These phenolic stabilizers may be used alone or as a mixture.
- R 36 - S ⁇ 2 - Sulf fin acid represented by R 37
- R 36 - S ⁇ 3 - R 37 (Ryoshikichu, R 36 is R j 1 is the same as R, and R 37 is the same as R ′ 2. )
- Sulfonic acid and its ester represented by the following formula (XK), etc.
- R 3 8 represents Al kill group R 3 9 having a carbon number of independently 1 2-1 8.
- benzenesulfinic acid p-tonolenesnolefonic acid
- benzenesnolefonic acid ⁇ -tonolenesnolefonic acid
- naphthalenesulphonic acid and those acids.
- bio-based stabilizers may be used alone or as a mixture.
- epoxy stabilizer examples include fats and oils such as epoxidized soybean oil and epoxidized linseed oil; phenyldaricidyl ether; A-noriglycidyl ether, t-butynolefenyloleglycidyl ether, bisphenol A diglycidyl ether, tetrabromobisphenol adiglycidyl ether, phthalic acid jig Glycidyl compounds such as glycidinoleester, hexidhydrophthalanolic acid diglycidinolester, etc .; 3,4,1-epoxycyclohexylmethylenolate 3,4,1-epoxycyclohexanoleboxylate, 3 , 4 — Epoxy 1-6 — Methinolecyclohexinole Methinole 3, 4 — Epoxycyclohexanecarboxylate 2, 3 — Epoxycyclohexylmethine 1, 3, 4
- hindered amine stabilizers include bis (2,2,6,6—tetramethy1-4—biperidyl) sebacate and bis (1,2,2,6,6). 6-Pentamethyl-4-biperidyl) sebacate, 2— (3,5—di-t-butyl _4—hydroxy benzyl) 1-2—n-butylmalonic acid bis (1, 2,2,6,6—Pentamethyl-4 4-biperidil) Tetraxie (2,2,6,6-tetramethyl-4—biperidil) 1,2,3 , 4 — butane Tetracarboxylate, you [2- ⁇ 3-(3, 5-di-tert-butyl-4-hydroxyhydropropane) propionyloxy ⁇ ethyl] 1-4- ⁇ 3- (3,5—di-t-butynole 4—hydroxyphenyl) propionyloxy ⁇ —2,2,6,6-tetramethyl piperidine, 8—benzinole 7,7,
- heat stabilizers may be used alone or in combination.
- a phosphorus-based stabilizer having an active hydrogen atom an azo-based stabilizer having an active hydrogen atom, sulfinate esters and sulfonate esters are preferably used.
- the phosphorus-based stabilizers having an active hydrogen atom include the above-mentioned phosphoric acids, phosphinic acids, phosphonic acids, phosphorous acid esters, phosphorous acid monoesters Phosphinic acid monoesters, phosphoric acid diesters, phosphoric acid monoesters, phosphonic acid monoesters and the like. Examples thereof include sulfinic acids and sulfonates.
- phosphorus-based stabilizers having an active hydrogen atom are preferred, and phosphorous diesters and phosphorous acid monoesters are particularly preferred.
- the amount of the heat stabilizer to be added is not particularly limited. However, it is generally used in the range of 0.0005 to 0.50 parts by weight based on 100 parts by weight of the total amount of the aromatic polycarbonate (A) and the thermoplastic resin (B).
- the heat stabilizer having an active hydrogen atom is preferably used in a range of 0.0005 to 0.015 parts by weight based on 100 parts by weight of the aromatic polycarbonate. Thus, a range of 0.0005 to 0.009 parts by weight is particularly preferred.
- heat stabilizers When heat stabilizers are used in combination, they can be freely combined, but the above-mentioned phosphorus-based stabilizers having an active hydrogen atom, zeo-based stabilizers having an active hydrogen atom, and sulfin At least one stabilizer selected from acid esters and sulfonate esters, and other phosphorus-based stabilizers, phenol-based stabilizers, zeolite-based stabilizers, epoxy It is preferable to combine at least one kind of stabilizer selected from the group consisting of a system stabilizer, a hindered amine system stabilizer and the like.
- At least one selected from a phosphorus-based stabilizer having an active hydrogen atom, an azo-based stabilizer having an active hydrogen atom, a sulfinate ester and a sulfonate ester is particularly advantageous to combine a stabilizer with at least one stabilizer selected from phosphorous acid triesters, phosphinic acid diesters and phenolic stabilizers.
- at least one stabilizer selected from phosphite diesters, phosphite monoesters and phosphite triesters, phosphinic acid It is particularly preferred to combine at least one stabilizer selected from diesters and phenolic stabilizers.
- the coloring and long-term heat aging resistance of the aromatic polycarbonate composition at the time of recycling molding are improved.
- the amount of these stabilizers to be added is not particularly limited, but is based on 100 parts by weight of aromatic polycarbonate.
- the at least one stabilizer selected from steles is generally in the range of 0.0005 to 0.015 parts by weight, preferably 0.0005.
- the stabilizer used in combination is generally aromatic polycarbonate (A) and thermoplastic resin.
- the phosphorus-based flame retardant used in the present invention is not particularly limited.
- trimethinolephosphate, triethylphosphate, tributylinolephosphate, and trimethyltin phosphate Octyl phosphate, tributin citrine phosphate, tri-tinole phosphate, tri-cinole phosphate, octyl di-ino phosphate phosphate, etc.
- Non-halogen phosphoric acid esters tris (chloroethynole) phosphate, bis (2,3 dibromopropinolate) 2,3—dichloropropyl phosphate; Phosphoric acid-containing phosphoric acid esters such as tris (dichloropropinole) phosphate and bis (chloropropinolate) monophosphyl phosphate; and the following formula: (XX) Include condensed-phosphate esters
- R 4 °, R 41 , R 42 and R 43 each independently represent a phenyl group, a cresyl group, a xylenyl group, a propylphenyl group, or a halogenated derivative thereof.
- B represents an arylene group derived from dihydroxy compounds such as resorcinol, hydroquinone, bisphenol A and their halogenated derivatives.
- jjj 3 and j 4 are each independently 0 or 1, and k represents an integer of 1 to 30.
- tricresyl phosphate and condensed phosphoric esters represented by the following formulas (XX!) To (XXIV) are preferred.
- the phosphorus-based flame retardant is 100 parts by weight based on 100 parts by weight of the total amount of the aromatic polycarbonate (A) and the thermoplastic resin (B). It is preferably used in the range of 1 to 25 parts by weight, particularly 5 to 20 parts by weight.
- additives may be added.
- other additives include release agents, weathering agents, coloring agents, flame retardants other than phosphorus-based flame retardants, fillers, acidic compounds, anti-dripping agents, and the like.
- These additives can be supplied to the extruder together with the thermoplastic resin (B) or the like in the same manner as in the case of the heat stabilizer and the phosphorus-based flame retardant described above. It is also possible to pelletize the aromatic polycarbonate composition of the present invention and, if necessary, re-melt and knead it with other additives to obtain a product.
- the measurement was performed by the following method.
- n Number average molecular weight (hereinafter abbreviated as n) and weight average molecular weight (hereinafter abbreviated as):
- the stability of the IZOD impact strength during molding is calculated as follows: IZOD impact strength retention before and after retention (%) [(IZOD impact strength of specimen before retention Z IZOD impact strength of specimen after retention) X 1 [0 0].
- the IZOD impact strength was measured according to ASTM-D256.
- Ash content was calculated according to the following formula
- Ash content crucible weight after incineration (g)-crucible weight (g)
- Example 1 For a 3.2 mm thick test piece obtained by injection molding at 250 ° C, according to ASTM D 1925, SM Color Computer, Model SM, manufactured by Suga Test Machine Co., Ltd., Japan Yellowness [Ye110 wness Index] was measured using —5. The measurement position was at the center of the test piece. The higher the YI value, the higher the yellowing.
- Example 1 SM Color Computer, Model SM, manufactured by Suga Test Machine Co., Ltd., Japan Yellowness [Ye110 wness Index] was measured using —5. The measurement position was at the center of the test piece. The higher the YI value, the higher the yellowing.
- PC aromatic polycarbonate
- Polymerization vessel 1 is ⁇ product 0. 5 7 m 3 der Li, thickness l mm, width 0. lm, a stearyl emissions less steel SUS 3 1 6 L manufactured by tabular guide 7 of length 7. 5 m 5
- the prepolymer 3 supplied to the polymerization vessel 1 is uniformly distributed on both sides of each flat guide 7 by the distribution plate 6.
- the outside of the polymerization vessel 1 becomes a jacket (not shown) and is heated by a heating medium.
- a device for stirring the prepolymer 3 in the polymerization vessel 1 is not provided.
- V [(w W 2 — W 3) P] V 0 where the meaning of each number is as follows.
- the evaporation surface area of the horizontal liquid level of the polymerization vessel bottom after 25 hours was 0.008 m 2 . Therefore, the evaporation surface area S after 25 hours was about 7.5 m 2 .
- the integrated amount of the prepolymer is calculated as the sum of the amount of aromatic polycarbonate discharged from the polymerization unit 1 and the amount of phenol and the like distilled out of the polymerization unit 1. Equally, the liquid volume V after 50 hours was the same as the liquid volume V after 25 hours.
- the evaporation surface area S after 50 hours was the same as the evaporation surface area S after 25 hours.
- the left side of the formula (I) was 1.70 and the right side was 1.000 both after 25 hours and after 50 hours.
- the liquid volume V is 26% of the content of the polymerization vessel 1.
- the production rate Q of the aromatic polycarbonate was 49.6 kg / hr.
- thermoplastic resin (B) rubber content: 39% by weight
- Acrylonitrile unit ratio 25 wt./. Ash content 0.08 wt%
- Graphite ratio 50% 5
- the extruder 16 was operated at a barrel temperature of 250 ° C. and a rotation speed of 200 rpm, and was degassed from the ventro 19 at a degree of vacuum of 100 mmHg.
- Example 3 Same as Example 1 except that the mixture of the rubbery graphitic polymer and the vinyl polymer used in Example 1 was used as the thermoplastic resin (B) without melt-kneading in advance. Was performed. Table 1 shows the results.
- Example 3 Same as Example 1 except that the mixture of the rubbery graphitic polymer and the vinyl polymer used in Example 1 was used as the thermoplastic resin (B) without melt-kneading in advance. Was performed. Table 1 shows the results. Example 3
- An aromatic polycarbonate composition was produced in the same manner as in Example 1 except that an aromatic polycarbonate was produced using a horizontal twin-screw stirring type polymerization vessel as the polymerization vessel.
- the horizontal twin-screw polymerization reactor has a 600-liter internal volume, a length of 3 m, a twin-screw stirring blade with a rotating diameter of 25 Omm, and a reaction temperature of 30.
- the conditions were 0 ° C, reaction pressure 0.1 mmHg, and rotation speed 15 rpm.
- the molecular weight w of the aromatic polycarbonate after the transition to the stable steady state operation was 25,800, which was slightly yellowish as compared with the composition obtained in Example 1.
- Table 1 shows the evaluation results of the obtained compositions. One of the moldings had brown spots.
- the conditions in the polymerization vessel are as follows: evaporation area S is 1.4 m 2 , liquid volume V is 0.24 m 3 , the left side of equation (I) is 0.76, and the right side is
- Example 5 The same operation as in Example 1 was performed except that 0.02 parts by weight of bis (noninolephenyl) hydrogenphosphite was used as the heat stabilizer. Table 1 shows the results. Example 5
- Table 1 shows the results obtained by performing the same operation as in Example] except that 0.2 parts by weight of tris (noylphenyl) phosphite was used as the heat stabilizer.
- Example 6
- an aromatic polycarbonate composition was produced.
- the system in Fig. 9 consists of a polymerization process and a melt-kneading process.
- the polymerization process was performed using the following apparatus.
- the polymerization is carried out in batch mode in the first polymerization reactors 28A and 28B, each of which has a volume of 100 liters and an anchor type stirring blade, and then has a volume of 50 liters.
- Anchor-type stirring blade The polymerization is continuously carried out in the second and third polymerization reactors 28 C and 28 D and the cylindrical polymerization reactor 1 having the following.
- this polymerization vessel 1 is a wire-on-contact falling polymerization vessel, and is a stainless steel SUS 31 with a thickness of lmm and a length of 8m.
- Five 6 L cylindrical guides 7 A are provided, and the pre-polymer 29 supplied to the polymerization vessel 1 is uniformly distributed to each guide by the distribution plate 6.
- Outside of polymerization machine 1 is a jacket
- the polymerization in the first polymerization reactors 28A and 28B of the stirred tank type was carried out at a reaction temperature of 180 ° C, a reaction pressure of atmospheric pressure, and a nitrogen gas flow rate of 1 liter Zhr.
- Bisphenol A as aromatic dihydroxy compound and diphenyl carbonate as diaryl carbonate (molar ratio of bisphenol A to 1.10) ) was charged into a stirred tank type first polymerization vessel 28A.
- the monomer mixture in the stirred tank type #polymerizer 28 A was polymerized in a molten state, and stirred for 4 hours to obtain a prepolymer 29 A.
- the outlet 3OA was opened, and 29 A of the prepolymer was supplied to a stirring tank type second polymerization vessel 28C having a capacity of 50 liters with a 10 liter volume Zhr.
- the stirring vessel While supplying the prepolymer 29 A obtained in the stirred tank type first polymerization vessel 28 A to the stirred tank type second polymerization vessel 28 C, the stirring vessel Similarly to the polymerization in the first polymerization reactor 28A, the first polymerization reactor 28B in the stirring tank is operated to polymerize bisphenol A and diphenyl carbonate. 29 B was obtained.
- the stirring vessel type first polymerization vessel 28 A becomes empty, the outlet 3 OA of the polymerization vessel 28 A is closed, the exit 30 B of the polymerization vessel 28 B is opened, and the prepolymer 29 B is discharged.
- the mixture was fed from the stirred tank type first polymerization device 28B to the stirred tank type second polymerization device 28C.
- the same polymerization raw material as above was charged into a polymerization vessel 28A.
- the polymerizer 28A was operated and charged. The polymer was polymerized as above.
- prepolymers 29 A and 29 B are alternately supplied from the stirred tank type first polymerization vessel 28 A and 28 B, and the reaction temperature is 240 °. C.
- the pre-polymers 29A and 29B were further subjected to continuous stirred tank polymerization to perform pre-polymerization.
- 29 C was obtained. After the volume of 29 C reaches 20 liters in the prepolymerizer in the stirred tank type second polymerization reactor 28 C, the prepolymerizer is maintained so that the internal volume of 20 liters is kept constant. Part of 29 C was continuously supplied to a stirred tank type third polymerization vessel 28 D.
- the prepolymer 29C was alternately supplied from the stirred tank type second polymerization vessel 28C, and the reaction temperature was 250 ° C and the reaction pressure was 2.0 mm. Under a polymerization condition of Hg and a nitrogen gas flow rate of 2 liter / hr, the prepolymer 29C was further subjected to continuous stirred tank polymerization to obtain a prepolymer 29D.
- the pre-polymer 29 D in the stirred tank type third polymerization vessel 28 D reaches 20 liters, the pre-polymer is maintained so that the internal volume of 20 liter is kept constant.
- a part of 29 D was continuously supplied to the first polymerization reactor 1 of a wire-one-contact falling type.
- the prepolymer 29 D was supplied to the polymerization reactor 1 through the inlet 5.
- polymerization was performed under the conditions of 255 ° C, a pressure of 1.0 mmHg, and a nitrogen gas flow rate of 1 liter r, and the aromatic polycarbonate was continuously discharged from the discharge port 10.
- the extruder 16 was supplied to the first supply port 17 of the extruder 16.
- Aromatic polycarbonate discharged from outlet 10 was w 23,500, Mn 9,000. Two hours later, the cylinder was calculated by subtracting the amount of prepolymer present in the circulation line and the amount of phenol discharged from polymerization reactor 1 from the amount of prepolymer initially charged. guide
- the liquid volume V of the prepolymer on the surface and in the polymerization vessel bottom is 0- 0 1 2 m 3 der Li, the evaporation surface area S determined in the same manner as in Example 1 was 2. 2 m 2.
- the left side of the formula (I) was 2.26, and the right side was 0.98.
- the melt-kneading step in the extruder 16 was performed by the following operation.
- the operation was performed at a temperature of 240 ° C. and a rotation speed of 200 rpm.
- the second supply port 18 is on the side of the extruder 6. From the second supply port 18, as a thermoplastic resin (B), a rubber-like graft polymer (rubber-like polymer) obtained by polymerizing butadiene-based rubber Z and polystyrene is used.
- the supply ratio from each supply port is adjusted so that the first supply port is 17 to 80 parts by weight, the second supply port is 18 to 20 parts by weight, and the liquid inlet port is 25 to 10 parts by weight. It was adjusted.
- the aromatic polycarbonate composition discharged from the extruder 16 is introduced into a strand cutter 24 via a cooling bath 23 to form a continuous pellet, and the pellet is formed.
- the composition of the present invention was obtained from the outlet 25. Table 1 shows the results.
- the aromatic polycarbonate composition of the present invention requires an extremely large stirring power in the production process of the aromatic polycarbonate (A) used in the composition, which is different from the conventional production method of the aromatic polycarbonate. Because of its high volumetric efficiency, it is not only excellent in production efficiency, but also excellent in hue, free of impurities and thermal decomposition products, and has a high Izod impact strength during molding. It is a high-quality aromatic polycarbonate composition with little deterioration or silver generation. INDUSTRIAL APPLICABILITY
- the aromatic polycarbonate composition of the present invention can be advantageously used for producing a polycarbonate alloy product having excellent appearance, strength, heat resistance and the like in the field of home appliances and automobiles. You.
Landscapes
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Polyesters Or Polycarbonates (AREA)
- Compositions Of Macromolecular Compounds (AREA)
- Processes Of Treating Macromolecular Substances (AREA)
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US09/000,229 US6107440A (en) | 1996-09-02 | 1996-09-01 | Aromatic polycarbonate composition |
AU40328/97A AU4032897A (en) | 1996-09-02 | 1997-09-01 | Aromatic polycarbonate composition |
JP51246398A JP3725173B2 (ja) | 1996-09-02 | 1997-09-01 | 芳香族ポリカーボネート組成物 |
DE69735632T DE69735632T2 (de) | 1996-09-02 | 1997-09-01 | Zusammensetzung eines aromatischen polycarbonates |
EP97937858A EP0927746B1 (en) | 1996-09-02 | 1997-09-01 | Aromatic polycarbonate composition |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP8/248509 | 1996-09-02 | ||
JP24850996 | 1996-09-02 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1998010019A1 true WO1998010019A1 (fr) | 1998-03-12 |
Family
ID=17179248
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP1997/003046 WO1998010019A1 (fr) | 1996-09-02 | 1997-09-01 | Composition de polycarbonate aromatique |
Country Status (9)
Country | Link |
---|---|
US (1) | US6107440A (ja) |
EP (1) | EP0927746B1 (ja) |
JP (1) | JP3725173B2 (ja) |
CN (1) | CN1097618C (ja) |
AU (1) | AU4032897A (ja) |
DE (1) | DE69735632T2 (ja) |
ES (1) | ES2262187T3 (ja) |
TW (1) | TW404968B (ja) |
WO (1) | WO1998010019A1 (ja) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2008050591A (ja) * | 2006-07-25 | 2008-03-06 | Mitsubishi Chemicals Corp | 芳香族ポリカーボネートの製造方法 |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH11342510A (ja) * | 1998-04-03 | 1999-12-14 | Teijin Chem Ltd | 光学用成形材料 |
ATE512197T1 (de) * | 2002-04-16 | 2011-06-15 | Cheil Ind Inc | Thermoplastische flammwidrige harzzusammensetzungen |
US7528213B2 (en) * | 2004-06-14 | 2009-05-05 | Asahi Kasei Chemicals Corporation | Method for efficiently producing an aromatic polycarbonate |
KR100665802B1 (ko) * | 2004-12-30 | 2007-01-09 | 제일모직주식회사 | 난연성 스티렌계 수지 조성물 |
DE102007024081A1 (de) * | 2007-05-22 | 2008-11-27 | Emitec Gesellschaft Für Emissionstechnologie Mbh | Verfahren und Vorrichtung zum Verdampfen eines Fluides |
CN106103545A (zh) | 2014-03-27 | 2016-11-09 | 沙特基础工业全球技术有限公司 | 熔融聚合聚碳酸酯淬灭 |
CN104987687B (zh) * | 2015-06-08 | 2018-04-27 | 金发科技股份有限公司 | 一种聚碳酸酯组合物及其制备方法 |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH06172611A (ja) * | 1992-12-09 | 1994-06-21 | Asahi Chem Ind Co Ltd | ガラス強化難燃ポリカーボネート樹脂組成物 |
JPH06240125A (ja) * | 1993-02-16 | 1994-08-30 | Teijin Chem Ltd | 抗菌性ポリカーボネート樹脂組成物 |
JPH0733854A (ja) * | 1993-07-23 | 1995-02-03 | Asahi Chem Ind Co Ltd | 難燃樹脂組成物 |
JPH07196873A (ja) * | 1993-12-28 | 1995-08-01 | Nippon G Ii Plast Kk | 難燃性樹脂組成物 |
JPH08176350A (ja) * | 1994-12-27 | 1996-07-09 | Ube Ind Ltd | ゴム組成物の連続的製造方法 |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS535718A (en) * | 1976-07-05 | 1978-01-19 | Mitsubishi Electric Corp | Control device for electric car |
JP2674813B2 (ja) * | 1988-12-06 | 1997-11-12 | 日本ジーイープラスチックス 株式会社 | ポリカーボネートの製造方法 |
JPH05239331A (ja) * | 1992-02-27 | 1993-09-17 | Nippon G Ii Plast Kk | ポリカーボネート系樹脂組成物の製造方法 |
JP3491767B2 (ja) * | 1993-12-21 | 2004-01-26 | 日本ジーイープラスチックス株式会社 | 低光沢性ポリカーボネート/abs樹脂組成物 |
EP0681002A3 (en) * | 1994-05-03 | 1996-04-10 | Gen Electric | Polycarbonate and low gloss graft polymer compositions. |
-
1996
- 1996-09-01 US US09/000,229 patent/US6107440A/en not_active Expired - Lifetime
-
1997
- 1997-09-01 CN CN97196833A patent/CN1097618C/zh not_active Expired - Lifetime
- 1997-09-01 ES ES97937858T patent/ES2262187T3/es not_active Expired - Lifetime
- 1997-09-01 JP JP51246398A patent/JP3725173B2/ja not_active Expired - Lifetime
- 1997-09-01 WO PCT/JP1997/003046 patent/WO1998010019A1/ja active IP Right Grant
- 1997-09-01 DE DE69735632T patent/DE69735632T2/de not_active Expired - Lifetime
- 1997-09-01 AU AU40328/97A patent/AU4032897A/en not_active Abandoned
- 1997-09-01 EP EP97937858A patent/EP0927746B1/en not_active Expired - Lifetime
- 1997-09-02 TW TW086112610A patent/TW404968B/zh not_active IP Right Cessation
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH06172611A (ja) * | 1992-12-09 | 1994-06-21 | Asahi Chem Ind Co Ltd | ガラス強化難燃ポリカーボネート樹脂組成物 |
JPH06240125A (ja) * | 1993-02-16 | 1994-08-30 | Teijin Chem Ltd | 抗菌性ポリカーボネート樹脂組成物 |
JPH0733854A (ja) * | 1993-07-23 | 1995-02-03 | Asahi Chem Ind Co Ltd | 難燃樹脂組成物 |
JPH07196873A (ja) * | 1993-12-28 | 1995-08-01 | Nippon G Ii Plast Kk | 難燃性樹脂組成物 |
JPH08176350A (ja) * | 1994-12-27 | 1996-07-09 | Ube Ind Ltd | ゴム組成物の連続的製造方法 |
Non-Patent Citations (1)
Title |
---|
See also references of EP0927746A4 * |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2008050591A (ja) * | 2006-07-25 | 2008-03-06 | Mitsubishi Chemicals Corp | 芳香族ポリカーボネートの製造方法 |
Also Published As
Publication number | Publication date |
---|---|
DE69735632T2 (de) | 2007-04-05 |
ES2262187T3 (es) | 2006-11-16 |
CN1226274A (zh) | 1999-08-18 |
JP3725173B2 (ja) | 2005-12-07 |
EP0927746A4 (en) | 2001-07-04 |
TW404968B (en) | 2000-09-11 |
EP0927746A1 (en) | 1999-07-07 |
AU4032897A (en) | 1998-03-26 |
CN1097618C (zh) | 2003-01-01 |
US6107440A (en) | 2000-08-22 |
EP0927746B1 (en) | 2006-04-05 |
DE69735632D1 (de) | 2006-05-18 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CN102782044B (zh) | 热塑性树脂组合物及将其成型而成的成型体 | |
CN103865248A (zh) | 聚碳酸酯树脂组合物和成型品 | |
EP2748225B1 (en) | Polycarbonate compositions and methods for the manufacture and use thereof | |
CN103459499B (zh) | 聚碳酸酯树脂组合物及其成型品 | |
JP3967674B2 (ja) | ポリカーボネートの樹脂のリサイクル法 | |
WO1998010019A1 (fr) | Composition de polycarbonate aromatique | |
JP4721591B2 (ja) | ポリカーボネート樹脂組成物 | |
CN110072918A (zh) | 借助相容剂制造含硅氧烷的嵌段共聚碳酸酯 | |
JPH05262970A (ja) | ポリカーボネート系樹脂組成物 | |
CN107207845A (zh) | 具有改善的加工性能的包含pe‑蜡的共聚碳酸酯组合物 | |
JP5251234B2 (ja) | 芳香族ポリカーボネート樹脂組成物の製造方法 | |
KR101411003B1 (ko) | 난연성 방향족 폴리카보네이트 수지 및 이의 제조방법 | |
JP4957311B2 (ja) | 芳香族ポリカーボネートの連続製造方法 | |
JP4759154B2 (ja) | ポリカーボネート組成物およびその製造方法 | |
US6906122B1 (en) | Flame-resistant polycarbonate blends | |
JP5037763B2 (ja) | ポリカーボネート樹脂組成物 | |
JP2003297305A (ja) | 電池パック | |
US5972273A (en) | Method for producing a homogeneous polycarbonate composition | |
EP1016688B1 (en) | Aromatic polycarbonate composition | |
JP5464166B2 (ja) | 炭酸ジエステルの精製方法及びポリカーボネート樹脂の製造方法 | |
JP3393167B2 (ja) | ポリカーボネート組成物の製造方法 | |
JP5037761B2 (ja) | 熱可塑性樹脂組成物 | |
JP3604047B2 (ja) | ポリカーボネート組成物の製造方法 | |
JP3434637B2 (ja) | ガイドを用いるポリカーボネート系樹脂の製造法 | |
JPH08225735A (ja) | ポリカーボネート組成物の製造方法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
WWE | Wipo information: entry into national phase |
Ref document number: 97196833.0 Country of ref document: CN |
|
WWE | Wipo information: entry into national phase |
Ref document number: 09000229 Country of ref document: US |
|
AK | Designated states |
Kind code of ref document: A1 Designated state(s): AL AM AT AU AZ BA BB BG BR BY CA CH CN CU CZ DE DK EE ES FI GB GE GH HU IL IS JP KE KG KR KZ LC LK LR LS LT LU LV MD MG MK MN MW MX NO NZ PL PT RO RU SD SE SG SI SK SL TJ TM TR TT UA UG US UZ VN YU ZW AM AZ BY KG KZ MD RU TJ TM |
|
AL | Designated countries for regional patents |
Kind code of ref document: A1 Designated state(s): GH KE LS MW SD SZ UG ZW AT BE CH DE DK ES FI FR GB GR IE IT LU MC NL PT |
|
DFPE | Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101) | ||
121 | Ep: the epo has been informed by wipo that ep was designated in this application | ||
WWE | Wipo information: entry into national phase |
Ref document number: 1997937858 Country of ref document: EP |
|
WWP | Wipo information: published in national office |
Ref document number: 1997937858 Country of ref document: EP |
|
REG | Reference to national code |
Ref country code: DE Ref legal event code: 8642 |
|
NENP | Non-entry into the national phase |
Ref country code: CA |
|
WWG | Wipo information: grant in national office |
Ref document number: 1997937858 Country of ref document: EP |