WO2005121211A1 - 芳香族ポリカーボネートを効率的に製造する方法 - Google Patents
芳香族ポリカーボネートを効率的に製造する方法 Download PDFInfo
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- WO2005121211A1 WO2005121211A1 PCT/JP2005/010854 JP2005010854W WO2005121211A1 WO 2005121211 A1 WO2005121211 A1 WO 2005121211A1 JP 2005010854 W JP2005010854 W JP 2005010854W WO 2005121211 A1 WO2005121211 A1 WO 2005121211A1
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- 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
- C08G64/205—General preparatory processes characterised by the apparatus used
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- 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
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- 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
- C08G64/04—Aromatic polycarbonates
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- 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
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- 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
Definitions
- the present invention relates to a method for efficiently producing an aromatic polycarbonate. More specifically, the present invention has a specific structure after absorbing a specific amount of an inert gas into a molten prepolymer of an aromatic polycarbonate obtained by reacting an aromatic dihydroxy conjugate with diaryl carbonate.
- the present invention relates to a method for efficiently producing a high-quality and high-performance aromatic polycarbonate with an industrial scale production of 1 ton or more per hour by performing polymerization using a guide contact falling polymerization apparatus.
- the method of the present invention By the method of the present invention, high-quality and high-performance aromatic polycarbonates having no coloring and excellent mechanical properties can be produced at an output of 1 ton or more per hour for a long period (for example, 5,000 hours). For a long period of time) and can be produced stably without variation in molecular weight. Therefore, the method of the present invention is very advantageously used for industrial production of aromatic polycarbonate.
- aromatic polycarbonates have been widely used in many fields as engineering plastics having excellent heat resistance, impact resistance, transparency, and the like.
- Various studies have hitherto been made on the method for producing the aromatic polycarbonate, and among them, an aromatic dihydroxy compound such as 2,2-bis (4-hydroxyphenyl) propane (hereinafter referred to as bisphenol A and bisphenol A) has been studied.
- bisphenol A and bisphenol A 2,2-bis (4-hydroxyphenyl) propane
- phosgene are being industrialized by the interfacial polycondensation method (so-called “phosgene method”).
- a method for producing an aromatic polycarbonate from an aromatic dihydroxy conjugate and diaryl carbonate includes, for example, an aromatic dihydroxy conjugate (for example, bisphenol A) and diaryl.
- An aromatic dihydroxy conjugate for example, bisphenol A
- diaryl for example, A melting method in which a transesterification of a carbonate (for example, diphenyl carbonate) in a molten state and polymerization is carried out while extracting an aromatic monohydroxy compound (for example, phenol) formed has been known.
- the melting method has advantages such as not using a solvent, but has the following problems.
- JP-B-53-5718 (corresponding to U.S. Pat. No. 3,888,826)) and a method using a combination of a centrifugal thin-film evaporator and a horizontal twin-screw polymerizer (Japanese Patent Application Laid-Open No. No. 153923) is known.
- the reaction is performed at a high temperature of about 300 ° C, so that the obtained polymer tends to be colored or deteriorated in physical properties. ⁇ ⁇ ⁇ ⁇ Coloring of the polymer and deterioration of physical properties are likely to occur due to leakage of foreign substances. Therefore, there are still many problems to be solved in order to stably produce high-quality polycarbonate for a long time by a method using mechanical stirring.
- an inert gas when producing an aromatic polycarbonate.
- an inert gas atmosphere for example, US Pat. No. 2,964,297, US Pat. No. 3,153,008
- inert gas is used only for the purpose.
- a method of using a large amount of an inert gas to extract an aromatic monohydroxylated compound such as phenol produced by an equilibrium polycondensation reaction out of a polymerization system is also known.
- the oligocarbonate lkg per lm 3 active gas normal pressure is continuously introduced into the polymerization vessel heated under pressure with oligocarbonate melt to transport the sub eggplant that phenol and the like in equilibrium polycondensation reaction
- there is a method for producing an aromatic polycarbonate Japanese Patent Application Laid-Open No. 06-206997 (corresponding to US Pat. No. 5,384,389)).
- a method for producing an aromatic polycarbonate using a large amount of inert gas as a carrier is a method in which the inert gas used in the polymerization is repeatedly used in the polymerization. It becomes necessary to separate the hydroxy conjugate, and a large separation facility is required.
- the present inventors have developed a method using a guide contact falling type polymerization apparatus in which a molten pre-polymer is polymerized while falling by its own weight along a guide such as a wire without performing mechanical stirring. He found that these issues could be completely solved and filed an application first.
- the problem to be solved by the invention is to obtain a high-quality, high-quality, high-color, high-mechanical physical property from a molten prepolymer of an aromatic polycarbonate obtained by reacting an aromatic dihydroxy compound with diaryl carbonate. It is an object of the present invention to provide a specific method capable of producing an aromatic polycarbonate of high performance at an industrial scale production of 1 ton or more per hour, with a small variation in molecular weight, for a long time, in a stable and efficient manner.
- the present inventors have produced a high-quality, high-performance aromatic polycarbonate having excellent mechanical properties without coloring from the above molten polycarbonate prepolymer, with a production rate of 1 ton or more per hour.
- the present inventors have studied to improve a guide contact flow-down type polymerization apparatus for polymerizing a molten pre-bolimer, which has been previously proposed, while falling along a guide such as a wire.
- one object of the present invention is to produce a high-quality aromatic polycarbonate having excellent mechanical properties without coloring from a molten pre-polymer of an aromatic polycarbonate obtained by reacting an aromatic dihydroxy compound with diaryl carbonate.
- Another object of the present invention is to provide a method for producing a stable and efficient product with a production volume of 1 ton or more per hour for a long period of time without variation in molecular weight.
- FIG. 1 is a schematic view of a preferred example of a guide contact-flow polymerization apparatus used in the present invention.
- FIG. 1 is also a schematic view of a preferred example of an inert gas absorbing device preferably used in the present invention.
- FIG. 2 shows a preferred example of a guide contact-flow polymerization apparatus in which the upper part defined by the upper peripheral side wall of the casing is cylindrical, and the upper part defined by the lower peripheral wall of the casing.
- FIG. 1 is a schematic view of a polymerization apparatus in which a tapered lower part is an inverted fiber type. The method for measuring the inner diameter D and length L of the cylindrical upper part of the casing of the polymerization apparatus, the inner diameter d of the outlet, and the length h of the guide are shown.
- the tapered lower part of the casing of the polymerization reaction zone or in the case of an inert gas absorber, the tapered lower part of the casing of the inert gas absorption zone
- the present invention provides
- a method for efficiently producing an aromatic polycarbonate comprising the following steps (I) to (III):
- An inert gas-absorbing molten pre-bolimer supply port An inert gas-absorbing molten pre-bolimer supply zone located next to the supply port and communicating with the supply port, and an inert gas-absorbing molten prepolymer supply zone located next to the inert gas-absorbing molten prepolymer supply zone.
- a casing having a polymerization reaction zone communicating with the gas-absorbing molten pre-polymer feed zone, and an aromatic polycarbonate outlet located next to the polymerization reaction zone and communicating with the polymerization reaction zone;
- a vacuum device provided in connection with the polymerization reaction zone of the casing, and a discharge device provided in connection with the discharge port of the casing
- the polymerization reaction zone has a space and a guide fixed and extending downward therein, and the polymerization reaction zone is separated from the inert gas absorption molten prepolymer supply zone by a distribution plate having a plurality of holes.
- the inert gas absorbing molten pre-polymer feed zone communicates with the polymerization reaction zone through the plurality of holes of the distribution plate;
- a method comprising:
- the casing In the polymerization reaction zone of the guide contact falling polymerization device (a), the casing is inclined toward the upper portion defined by the upper peripheral side wall and the discharge port, and the upper peripheral side wall force is continuous. And a tapered lower portion defined by a lower peripheral wall extending downward.
- the outlet is at the bottom of the tapered lower portion, whereby the manufactured aromatic polycarbonate falling from the guide is formed by the lower portion. Flows down to the outlet along the inner surface of the lower peripheral wall of the tapered lower portion,
- the guide contact falling polymerization apparatus (a) has the following properties (1) to (5): (1)
- the opening area A (m 2 ) of the horizontal section of the upper part of the casing is represented by the following formula:
- the guide contact falling polymerization apparatus (a) has the following formula:
- A is as defined in the characteristic (1), and B represents the minimum opening area (m 2 ) of the cross section of the outlet.)
- Amount of aromatic polycarbonate produced is 1 ton or more per hour
- the upper part of the casing is cylindrical, the tapered lower part of the casing is inverted conical, the outlet is cylindrical and the inner diameter D (cm) and the length L ( cm), the inner diameter d (cm) of the discharge port, and the length h (cm) of the guide satisfy the following formula:
- At least one further guide contact falling polymerization device (b) having the properties (1) to (5) is connected to the guide contact falling polymerization device (a); In the case of using a further guide contact falling polymerization device (b), the plurality of further guide contact falling polymerization devices (b) are connected in series, and the at least one further contact contact polymerization device (b) is connected in series.
- the above steps (I) and (III) are performed in the guide contact falling polymerization apparatus (b), whereby the degree of polymerization of the aromatic polycarbonate produced in the guide contact falling polymerization apparatus (a) is determined. 4. The method according to any one of the above items 1 to 3, wherein
- An additional guide contact falling polymerization device (b) is connected to the guide contact falling polymerization device (a), and the external total surface area SI of the guide of the guide contact falling polymerization device (a) (m 2 ) and the external total surface area S 2 (m 2 ) of the guide of the further guide contact falling polymerization device (b), wherein the following formula ( 4 ) is satisfied,
- the aromatic polycarbonate is treated with an inert gas before the aromatic polycarbonate is supplied to the further guide contact falling polymerization apparatus (b), so that the aromatic polycarbonate absorbs the inert gas.
- the content of the halogen atom is lOppb or less, and the content of at least one metal compound selected from the group consisting of an alkali metal compound and an alkali earth metal compound is an alkali metal atom and an alkaline earth metal.
- the content of halogen atoms is 5 ppb or less, and The content of at least one metal compound selected from the group consisting of potassium earth metal compound power is 0.005 to 0.5 ppm in terms of the total amount of alkali metal atoms and alkaline earth metal atoms.
- the content of the halogen atom is lppb or less, and the content of at least one metal compound selected from the group consisting of an alkali metal compound and an alkali earth metal compound is an alkali metal atom and an alkaline earth metal.
- It comprises a plurality of aromatic polycarbonate main chains, and the plurality of aromatic polycarbonate main chains as a whole have at least one aromatic bond selected from the group consisting of ester bonds and ether bonds. preceding paragraph attached to the side chain, wherein the amount of said heterologous binding is 05-0 5 mol 0/0 0.5, relative to the carbonate bonds in the aromatic polycarbonate main chains of the plurality. 7 to:. L0
- the aromatic dihydroxy conjugate is a compound represented by the following formula.
- Ar represents a divalent aromatic group.
- the divalent aromatic group Ar is preferably, for example, one represented by the following formula.
- Ar 1 and Ar 2 each independently represent a divalent carbocyclic or heterocyclic aromatic group having 5 to 70 carbon atoms, and Y is a divalent having 1 to 30 carbon atoms. O) representing an alkane group
- Preferred specific examples of the heterocyclic aromatic group include an aromatic group having one or more ring-forming nitrogen, oxygen or sulfur atoms.
- the divalent aromatic group Ar 1 Ar 2 is, for example, Represents a group such as unsubstituted phenylene, substituted or unsubstituted biphenylene, and substituted or unsubstituted pyridylene.
- the substituent here is as described above.
- the divalent alkane group Y is, for example, an organic group represented by the following formula.
- R 4 is each independently hydrogen, C 1 to C: LO alkyl group, C 1 to C 10 alkoxy group, C 5 to C 10 cycloalkyl group, C 5 to C 10 carbon ring
- k represents an integer of 3 to 11
- R 5 and R 6 are independently selected for each X, independently of one another, represent hydrogen or an alkyl group having 1 to 6 carbon atoms, and X represents carbon .
- R 5 and R 6 other substituents such as a halogen atom, an alkyl group having 1 to 10 carbon atoms, and an alkoxy group having 1 to 10 carbon atoms as long as one or more hydrogen atoms do not adversely affect the reaction.
- substituents such as a halogen atom, an alkyl group having 1 to 10 carbon atoms, and an alkoxy group having 1 to 10 carbon atoms as long as one or more hydrogen atoms do not adversely affect the reaction.
- Examples of such a divalent aromatic group Ar include those represented by the following formula.
- R 7 and R 8 are each independently a hydrogen atom, a halogen atom, an alkyl group having 1 to 0 carbon atoms, an alkoxy group having 1 to 10 carbon atoms, a cycloalkyl group having 5 to 10 ring carbon atoms
- Hue M and n are integers from 1 to 4; when m is 2 to 4, each R 7 may be the same or different, and when n is 2 to 4
- Each R 8 may be the same or different.
- divalent aromatic group Ar may be represented by the following formula.
- ⁇ Ar 2 is as described above, and Z is a single bond or —O—, —CO—, —S—, -SO
- R 1 is as described above.
- Examples of such a divalent aromatic group Ar include those represented by the following formula.
- divalent aromatic group Ar examples include substituted or unsubstituted phenylene, substituted or unsubstituted naphthylene, and substituted or unsubstituted pyridylene.
- the aromatic dihydroxy compound used in the present invention may be a single kind or two or more kinds.
- a typical example of the aromatic dihydroxy conjugate is bisphenol A.
- a branched structure is introduced within a range that does not impair the object of the present invention.
- a trivalent aromatic trihydroxy conjugate may be used in combination.
- the diaryl carbonate used in the present invention is represented by the following formula.
- Ar 3 and Ar 4 each represent a monovalent aromatic group having 5 to 20 carbon atoms.
- Ar 3 and Ar 4 represent a monovalent carbocyclic or heterocyclic aromatic group, this Ar 3, Ar Oite, one or more hydrogen atoms, other that does not adversely influence the reaction
- 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.
- Ar 3 and Ar 4 include, for example, those represented by the following formulas.
- diaryl carbonate include substituted or unsubstituted diphenyl carbonates represented by the following formula.
- each of R 9 and R 1Q independently represents a hydrogen atom, an alkyl group having 1 to 10 carbon atoms, an alkoxy group having 1 to 10 carbon atoms, or a cycloalkyl having 5 to 10 ring carbon atoms.
- diaryl carbonates symmetric diaryl carbonates such as unsubstituted diphenyl carbonate and lower alkyl-substituted diphenyl carbonate such as ditolyl carbonate and di-tert-butyl carbonate are preferable.
- diphenyl carbonate which is a diaryl carbonate having the simplest structure, is particularly preferred.
- diaryl carbonates may be used alone or in combination of two or more.
- the use ratio (preparation ratio) of the aromatic dihydroxy conjugate and the diaryl carbonate is determined by the types of the aromatic dihydroxy conjugate and the diaryl carbonate used, the polymerization temperature, and other polymerization conditions.
- the diaryl carbonate is usually 0.9 to 2.5 monoles, preferably 0.95 to 2.0 monoles, more preferably 0.98 per 1 mono of the aromatic dihydroxy conjugate.
- ⁇ : L is used in a ratio of 5 mol.
- the term "melted prepolymer" (hereinafter, referred to as “melted prepolymer”) produced from the aromatic dihydroxy conjugate and the diaryl carbonate refers to the aromatic dihydroxy conjugate. It means a melt in the course of polymerization having a lower degree of polymerization than an aromatic polycarbonate having a desired degree of polymerization, which is obtained by reacting with aryl carbonate, and may of course be an oligomer.
- the average degree of polymerization of the molten prepolymer of the aromatic polycarbonate used in the present invention may be any value as long as it is molten at the polymerization temperature, and may vary depending on its chemical structure. The force is usually about 2 to 2,000. .
- Such a molten prepolymer used as a polymerization raw material of the present invention may be obtained by any known method.
- the inert gas is absorbed by the molten prevolamer, whereby the molten prevolamer is added to the molten prepolymer in an amount of 0.0001 per kg of the molten prepolymer.
- Nl is the volume measured under standard temperature and pressure conditions
- treating the molten prepolymer with an inert gas refers to the treatment of the molten prepolymer.
- the step of treating the molten prepolymer with an inert gas is often referred to as an “inert gas absorption step”.
- the method for absorbing the inert gas into the molten prepolymer is not particularly limited as long as the method is carried out under conditions where the molten prepolymer is difficult to polymerize.
- it can be performed using an inert gas absorbing device.
- the amount of inert gas to be absorbed by the molten prepolymer is in the range of 0.001 to 1N liter, preferably 0.001 to 0.8N liter, and more preferably 0. 005-0. The range is 6 Nl. If the amount of the inert gas absorbed is less than 0.0001 N liter per 1 kg of the molten prepolymer, the effect of increasing the polymerization rate and the effect of the stable production of the aromatic polycarbonate are undesirably reduced. In the present invention, the amount of the inert gas to be absorbed need not be more than 1N liter per 1 kg of the molten prepolymer.
- the effect of increasing the polymerization rate is not only large, but also stable for a long period of time without variation in molecular weight. Was found to be very large.
- the amount of the inert gas absorbed by the molten polymer can usually be easily measured by directly measuring the amount of the supplied inert gas. If the molten gas is absorbed by the molten pre-polymer while the inert gas is passed through the absorber, the amount of the absorbed inert gas should be calculated from the difference between the supplied inert gas amount and the discharged inert gas amount. it can. It is also possible to supply a predetermined amount of molten pre-polymer to an absorption device charged with an inert gas at a predetermined pressure, and to measure the amount of pressure reduction of the absorption device caused by the absorption of the inert gas by the molten pre-polymer. It is.
- the conventional method of continuously supplying and flowing an inert gas into a polymerization vessel increases the polymerization rate because the polymerization reaction is an equilibrium reaction, so that an aromatic monohydroxy compound (such as phenol) is formed. It is understood that the partial pressure of the aromatic monohydroxyl conjugate (phenol or the like) in the polymerization vessel is reduced by the accompanying removal of) by the inert gas, and the polymerization proceeds advantageously in an equilibrium manner. ing. Therefore, in the conventional method, in order to increase the polymerization rate, the supply amount of the inert gas must be increased, and various problems associated with the use of a large amount of the inert gas (for example, recovery and reuse). It was difficult to avoid it.
- the inert gas When the inert gas is absorbed into the molten pre-polymer by the inert gas absorbing device, the inert gas is relatively uniformly dissolved in the molten pre-polymer, and Therefore, since the foaming state of the molten prepolymer in the polymerization zone is different from the foaming state in the conventional method and the internal force is relatively uniform, the uniformity in the polymer is increased, It is presumed that the mechanical properties are improved and the variation in molecular weight is reduced.
- the molten prepolymer is treated with an inert gas under a predetermined pressure using an inert gas absorbing device and under the conditions that the molten prepolymer is hardly polymerized! Therefore, the inert gas is absorbed.
- Absorbing the inert gas in the molten prevolumemer means dispersing and Z or dissolving the inert gas in the molten prevolumemer.
- Dispersion means a state in which an inert gas is mixed in a bubble form in a molten pre-polymer and forms a gas-liquid mixed phase.Dissolution means that the inert gas is mixed with the molten pre-polymer and a uniform liquid phase is formed. It means the state of forming.
- the inert gas be dissolved in the molten prepolymer, which is merely dispersed.
- the type of the inert gas absorbing device used in the present invention is not particularly limited as long as it can absorb these inert gases into the molten prepolymer.
- Known devices such as an absorption device, a liquid film cross-flow absorption type absorption device, a high-speed swirling flow type absorption device, a mechanical force type absorption device, and the like, while dropping the molten prevolimer along a guide in an inert gas atmosphere.
- the device include an absorbing device.
- a device that directly supplies and absorbs an inert gas into the pipe that supplies the molten prepolymer to the joint device It is particularly preferable to use a spray tower type absorption device or a device that absorbs while falling along a guide.
- the inert gas absorbing device used in the present invention a device of the same type as the guide contact falling type polymerization device used as the polymerization device is particularly preferable. Since the inert gas absorption device is operated under conditions that hardly allow polymerization to proceed, it is completely different from the polymerization device in terms of function.However, the outstanding feature of this type of device is that the molten gas flowing down the guide is melted. The extremely high surface area of the material per weight combined with the very good melt surface renewal and internal agitation allow very efficient inert gas absorption in a short time. That is.
- the inert gas absorption apparatus has a large capacity for processing molten prepolymer per unit time because there is almost no change in the viscosity of the molten prepolymer at the upper and lower portions of the guide.
- the inert gas absorption device can generally be smaller than the polymerization device.
- the number average molecular weights of the molten prepolymers before and after the inert gas absorption step are each set to MM.
- the change in molecular weight (M-M) in the inert gas absorption process is substantially less than 2,000
- the temperature at which the inert gas is absorbed by the molten prepolymer is not particularly limited as long as it is in a molten state.
- Power is usually 150 350 C, preferably 180 180 C, and particularly preferably 230 270 ° C. It is.
- the pressure Pg (Pa) at which the molten prepolymer is absorbed by the inert gas is preferably equal to or higher than the pressure used for producing the molten prepolymer. That is, the reaction pressure is equal to or higher than the reaction pressure used in producing the molten prepolymer of aromatic polycarbonate by reacting the aromatic dihydroxy conjugate with diaryl carbonate. It is preferable to absorb inert gas.
- Pg (Pa) is higher and higher than the pressure Pp (Pa) in the subsequent polymerization step.
- Pg (Pa) force When the relationship of the above formula is not satisfied, the effect of increasing the polymerization rate and the effect of stable production are reduced. It is particularly preferable that the pressure at which the inert gas is absorbed be normal pressure or pressurized, since the rate of absorption of the inert gas into the molten prepolymer is increased, and the absorption device can be reduced as a result. There is no particular limitation on the upper limit of the pressure of the inert gas absorption step, usually, 2 X 10 7 Pa or less, preferably 1 X 1 0 7 Pa or less, more preferably under a pressure of less than 5 X 10 6 Pa not Allow active gas absorption.
- a method of absorbing the inert gas into the molten pre-polymer by the inert gas absorbing device a method of absorbing most of the inert gas supplied to the inert gas absorbing step into the molten pre-polymer may be used.
- a method may be used in which a part of the inert gas is absorbed into the molten prepolymer.
- the former method for example, a spray tower type absorption device or a device that absorbs while dropping along a guide is used, and an inert gas in an amount substantially equal to the inert gas absorbed in the molten prepolymer is supplied.
- a spray tower type absorption device or a device that absorbs the molten prevolimer while dropping it along a guide is used as an inert gas absorbing device. Or more, and the excess inert gas is discharged through the inert gas absorbing device.
- the former method is particularly preferred from the viewpoint of reducing the amount of inert gas used.
- the molten prepolymer is continuously supplied to the absorber to absorb the inert gas, and the molten prepolymer that has absorbed the inert gas is continuously extracted. Any of the batch methods in which the prepolymer is charged in batches and the inert gas is absorbed can be used.
- inert gas is a general term for a gas that does not cause a chemical reaction with the molten prepolymer and is stable under polymerization conditions.
- specific examples of the inert gas include nitrogen and argon. , Helium, carbon dioxide, organic compounds that are gaseous at a temperature at which the prepolymer remains in a molten state, lower hydrocarbon gases having 1 to 8 carbon atoms, and the like, with nitrogen being particularly preferred.
- the guide contact falling polymerization apparatus used in the present invention is a polymerization apparatus that melts and flows down a prepolymer along a guide to carry out polymerization.
- a molten pre-polymer feed port a molten pre-polymer feed zone located next to the feed port and communicating with the feed port, a polymerization reaction zone located next to the molten pre-polymer feed zone and communicated with the molten pre-polymer feed zone, and the polymerization
- a casing having an aromatic polycarbonate outlet located next to the reaction zone and communicating with the polymerization reaction zone;
- a vacuum device provided in connection with the polymerization reaction zone of the casing, and a discharge device provided in connection with the discharge port of the casing
- the polymerization reaction zone has a space and a guide fixed therein and extending downward, wherein the polymerization reaction zone is connected to the polymerization reaction zone by the molten prepolymer polymer supply zone.
- the guide contact falling polymerization apparatus (a) needs to have the following properties (1) to (5).
- the characteristic (1) as shown in FIG. 1, the opening area A (m 2 ) of the cross section in the horizontal plane (a—a ′ plane) of the casing 10 constituting the upper peripheral side wall of the polymerization reaction zone 5 must satisfy the following equation:
- A smaller than A is 0. 7m 2, and, Do can achieve production of interest, and, in order to achieve the production of Tsukko reduce the equipment cost, A is to 200 meters 2 below It is necessary.
- the A (m 2 ) and the minimum opening area B (m 2 ) of the cross section of the aromatic polycarbonate outlet 7 are Satisfies the following formula It is also necessary.
- the outlet 7 connects the bottom of the tapered lower part to an aromatic polycarbonate discharging device (usually a device such as a gear pump that can discharge high-viscosity substances).
- an aromatic polycarbonate discharging device usually a device such as a gear pump that can discharge high-viscosity substances.
- a pipe-shaped one having a circular, elliptical, or elliptical cross-sectional shape is preferable.
- the discharge port 7 may be a combination of these cross-sectional shapes between the bottom of the tapered lower portion and the discharge device, or the cross-sectional area may not be constant. Further, the discharge port 7 may be linear or may have a partially curved portion between the bottom of the tapered lower portion and the discharge device. It should be noted that there may be two or more outlets 7.
- AZB In order to discharge a melt having a high melt viscosity without deteriorating the quality of the produced aromatic polycarbonate or aromatic polycarbonate prepolymer having an increased degree of polymerization, AZB must satisfy the above formula (20 ⁇ A / B ⁇ 1,000).
- the angle C is preferably as close to 90 ° as possible because the amount of casing material used is small. Therefore, from the viewpoint of reducing equipment costs, it is preferable that the angle C be as close as possible to 90 °. It is considered.
- these melts having a high melt viscosity are discharged to the outlet 7 without deteriorating the quality of the aromatic polycarbonate falling from the lower end of the guide or the aromatic polycarbonate prepolymer having an increased degree of polymerization.
- the angle C must be in the range 120-165 °.
- the polymerization apparatus used in the present invention may have a plurality of different angles (C). This occurs, for example, if the horizontal cross section of the upper part of the casing in the polymerization reaction zone is elliptical or if the tapered lower part of the casing is asymmetric. In such a case, no matter where the angle (C) is measured, the above range (120 to 165) °).
- the length h (cm) of the guide is T3
- total external surface area S1 is 2-5 to be described later, is not particularly limited so Re range near the OOOm 2 (i.e., for example, 1 to total external surface area S1 is 2, OOOm 2 guides Even if this guide is used, the total external surface area S1 may be set to 2, OOOm 2 by using a plurality of guides.
- a perforated plate or wire mesh having a length h may be used. Can be used such that the horizontal cross section is spiraled).
- the length of each guide must be in the range of 150-3,000cm.
- the lengths of the guides may not be the same, but it is preferable that the lengths be as close as possible to reduce variation in the molecular weight.
- the number of guides can usually be from one to several million, depending on the shape of the guides.
- the number of force guides depending on the desired degree of polymerization or production amount is usually 100 to 1,000,000, preferably Is from 200 to 50,000.
- the external total surface area Sl (m 2 ) of the guide needs to satisfy the following equation.
- the external total surface area S1 of the guide refers to the area of the entire surface of the guide (hereinafter simply referred to as the external surface) on which the molten pre-polymer flows in contact.
- the external total surface area S1 is determined by the pipe-shaped guide. Outside And does not include the surface area of the inside surface of the pipe that does not allow the molten pre-polymer to flow down. If there are multiple guides, the total external surface area S1 means the sum of the areas of the external surfaces of all guides.
- a guide with a high surface area that satisfies the above properties (4) and (5) can allow a large amount of pre-bolimer to flow down even at a relatively low temperature, and can effectively renew the surface of a pre-bolimer that also flows down.
- a large amount of high-quality aromatic polycarbonate can be produced, and the inner wall and discharge port of the tapered lower part satisfying the above characteristics (3) and (2) are capable of producing a large amount of It is presumed that, since the residence time before the outlet of the produced aromatic polycarbonate is also discharged can be shortened, coloring and denaturation due to long-term residence will not occur.
- a more preferable range of the opening cross-sectional area A (m 2 ) of the horizontal cross section of the upper part of the casing is 0
- a more preferable range of the ratio between the A (m 2 ) and the minimum opening area B (m 2 ) of the cross section of the discharge port is 25 ⁇ A / B ⁇ 900, more preferably. Is 30 ⁇ A / B ⁇ 8
- a more preferable range of the angle C (°) between the upper peripheral side wall of the upper portion of the casing and the inner peripheral surface of the lower peripheral wall of the tapered lower portion is 125 ⁇ C ⁇ 160, more preferably. Is 135 ⁇ C ⁇ 165.
- the length h (cm) of the guide depends on factors such as the degree of polymerization of the raw material prepolymer, the polymerization temperature, the pressure, the degree of polymerization of the aromatic polycarbonate or prepolymer to be produced by the polymerizer, and the production amount.
- a more preferable range is 200 ⁇ h ⁇ 2800 (if there is more than one guide, the length of all guides is within this range), and more preferably, 250 ⁇ h ⁇ 2500 (however, if there are multiple guides, the length of all guides is within this range).
- the required external total surface area SI (m 2 ) of the entire guide also varies depending on the same factors as described above.
- the more preferable range is 4 ⁇ S ⁇ 4500 (however, multiple guides If there is, the length of all guides satisfies this equation.), And more preferably, 9 ⁇ S ⁇ 4000 (however, if there are multiple guides, all guides Satisfies this equation.).
- the case of the polymerization reaction zone may be any as long as it can withstand it.
- the shape of the opening of the upper horizontal section defined by the upper peripheral side wall of the casing is polygonal, elliptical, Any shape such as a circle and a circle may be used. Preferably, the shape is circular or close to it. Further, the opening in the horizontal cross section of the upper portion of the casing may have different shapes or cross sectional areas from the upper portion to the lower portion, or may have the same shape. The same is preferable from the viewpoint of the production of the polymerization apparatus.
- the upper portion defined by the upper peripheral side wall of the casing in the polymerization reaction zone of the present invention is preferably cylindrical.
- the tapered lower portion of the casing preferably has an inverted conical shape, and a cylindrical aromatic polycarbonate discharge port is preferably provided at the lowermost portion.
- the upper part of the casing in the polymerization reaction zone is cylindrical
- the tapered lower part of the casing is an inverted conical shape
- the outlet is cylindrical.
- the inner diameter D (cm) and the length L (cm) of the upper part of the casing, the inner diameter d (cm) of the discharge port, and the length h (cm) of the guide satisfy the following formula. Is preferred.
- a more preferable range of DZd is 6 ⁇ D / d ⁇ 45, more preferably,
- LZD 7 ⁇ D / d ⁇ 40. Further, a more preferable range of LZD is as follows:
- L (cm) is h — 10 ⁇ L ⁇ h + 250 (However, when there are multiple guides, the length of all guides satisfies this equation.) More preferably, h ⁇ L ⁇ h + 200 (however, when there are a plurality of guides, the length of all guides satisfies this equation).
- the molten prevolimer that has absorbed the specific amount of the inert gas as the raw material is supplied from the supply port via the molten prevolimer supply zone and the distribution plate.
- the degree of polymerization increases while flowing down along the guide.
- effective internal stirring and surface renewal are performed, and phenol or the like is effectively extracted, so that polymerization proceeds at a high speed. Since the melt viscosity increases with the progress of polymerization, the adhesive force to the guide increases, and the amount of melt adhering to the guide increases toward the lower part of the guide.
- the reason why an aromatic polycarbonate having a small variation in molecular weight can be obtained can be explained as follows.
- the amount of the melt adhering to the guide is a force that increases toward the lower part of the guide.
- the prepolymer has only an adhesive holding force corresponding to the melt viscosity of the guide. Therefore, at the same height of the guides, approximately the same amount of melt having substantially the same melt viscosity is supported by each guide.
- the molten zone since the molten zone is supplied continuously to the upper part of the guide, the molten zone has the same melt viscosity and the degree of polymerization is higher.
- the lower end of the guide is also continuous to the tapered lower part of the casing. It will fall down.
- aromatic polycarbonate of approximately the same degree of polymerization generated while flowing down the guide collects at the bottom of the tapered lower part of the casing. That is, an aromatic polycarbonate having no variation in molecular weight can be continuously produced. This is also one of the advantages of the polymerization apparatus used in the present invention.
- Aromatic polycarbonate collected at the bottom of the tapered lower portion of the casing passes through a discharge port, and is discharged by a discharge device (generally, a gear pump capable of sending a highly viscous substance; discharge pump 8 in FIG. 1). It is continuously extracted and usually drawn continuously through an extruder.
- a discharge device generally, a gear pump capable of sending a highly viscous substance; discharge pump 8 in FIG. 1.
- the distribution plate constituting the guide contact-flow polymerization apparatus used in the present invention is usually selected from a force such as a flat plate, a corrugated plate, or a plate having a thick central portion.
- a shape force such as a circle, an ellipse, a triangle, and a polygon is usually selected.
- the holes of the distribution plate are usually selected from shapes such as a circle, an ellipse, a triangle, a slit, a polygon, and a star.
- sectional area of the distributor plate holes is usually 0. 01: a LOOcm 2, preferably 0. 05 ⁇ : a is LOcm 2, range particularly preferably of 0. l ⁇ 5cm 2.
- the distance between the holes which is the distance between the center and the center of the hole, is usually l to 500 mm, preferably 25 to 100 mm.
- the hole of the distribution plate may be a hole penetrating the distribution plate or a case where a pipe is attached to the distribution plate. Moreover, it may be tapered.
- the guide that constitutes the guide contact falling polymerization apparatus used in the present invention refers to a material having a very large ratio of the length of the horizontal section to the average length of the outer circumference of the cross section. It represents.
- the ratio is usually in the range of 10 to: L, 000,000, preferably ⁇ 50 in the range of 50 to LOO, 000.
- the shape of the cross section of the guide in the horizontal direction is usually selected from shapes such as a circle, an ellipse, a triangle, a square, a polygon having five or more sides, and a star.
- the shape of the cross section may be the same or different in the length direction.
- the guide may be hollow.
- the guide may be a single guide such as a wire-like guide, a thin rod-like guide, a thin guide in which the molten pre-bolimer does not enter inside, or a pipe-like guide. A plurality of combinations may be used. Further, it may be a net-like thing or a punching plate-like thing. Furthermore, the guide has a spiral horizontal cross section.
- the surface of the guide may be partially smooth or uneven, and may have projections. I'm a little.
- the guide is a cylindrical one such as a wire, a thin one, or a rod, the thin one, a pipe-like one, a net-like one, or a punching plate-like one.
- a plurality of wire-like polymerization apparatuses which enables the production of high-quality aromatic polycarbonate on an industrial scale (production amount, long-term stable production, etc.)
- a wire mesh guide fixed at an appropriate upper and lower interval for example, an interval of lcm to 200cm, using a horizontal support member from the upper part to the lower part of a plurality of wire-like or thin rod-like guides or the above-mentioned thin pipe-like guide.
- Lateral supports not only help to keep the spacing between guides about the same, but also help to increase the strength of guides that are flat or curved overall, or that are three-dimensional. . These supports may be the same material as the guide, or may be different.
- one guide has a cylindrical shape with an outer diameter r (cm) or a pipe shape having a circular cross section in which the molten pre-bollima does not enter (hereinafter, these are collectively referred to as a cylindrical shape).
- r satisfies the following equation.
- the guide according to the present invention promotes the polymerization reaction while flowing down the molten prepolymer, but also has a function of holding the molten prepolymer for a certain time.
- the holding time is related to the polymerization reaction time, and as the melt viscosity increases as the polymerization proceeds, the holding time and the holding amount increase as described above.
- the amount by which the guide holds the molten pre-polymer is the same as the pre-polymer Depends on the external surface area of the guide with which it is in contact. Therefore, the amount depends on their outer diameter in the case of cylindrical guides.
- the guide installed in the guide contact-flow polymerization apparatus used in the present invention needs to have enough strength to support and hold the weight of the molten pre-polymer in addition to the weight of the guide itself. is there. In this sense, the thickness of the guide is important.
- the diameter (r) is preferably in the above range (0.1 to: Lcm).
- a more preferable range of r is 0.15 ⁇ r ⁇ 0.8, and a further preferable range is 0.2 ⁇ r ⁇ 0.6.
- ⁇ Materials include metals such as stainless steel, carbon steel, Hastelloy, nickel, titanium, chromium, aluminum and other alloys, and polymer materials with high heat resistance. Power is chosen. Particularly preferred is stainless steel.
- the guide surface is subjected to various treatments such as plating, lining, passivation treatment, acid washing, phenol washing, etc. as necessary!
- the positional relationship between the guide and the distribution plate and the positional relationship between the guide and the holes of the distribution plate are not particularly limited as long as the molten prepolymer can flow down into the guide in contact with the guide.
- the guide and the distributing plate are in contact with each other!
- the guide is provided corresponding to the hole of the distribution plate, but the present invention is not limited to this.
- Preferable specific examples of installing the guides corresponding to the holes of the distribution plate include (1) fixing the upper end of the guide to the upper inner wall surface of the polymerization apparatus or an appropriate position in the supply zone, and (2) Fixing the upper end of the guide to the periphery of the upper end of the hole of the distribution plate, and providing the guide with the guide passing through the hole of the distribution plate. Method, (3) a method of fixing the upper end of the guide to the lower surface of the distribution plate, and (4) a method of welding and fixing to a part of the hole of the distribution plate.
- a method of flowing down the molten prevolimer along the guide through the distribution plate a method of flowing down by the liquid head or its own weight, or by applying pressure using a pump or the like, the distribution plate force is also reduced by the molten plate. Extrusion and other methods can be used. Preferred is Using a supply pump, a predetermined amount of raw material prepolymer is supplied to the supply zone of the polymerization equipment under pressure, and the molten prevolumer guided to the guide via the distribution plate flows down along the guide by its own weight. It is.
- a molten prevolumemer obtained by absorbing an inert gas into a molten prevolimer obtained from an aromatic dihydroxy conjugate and diaryl carbonate is used as a guide.
- the temperature of the polymerization reaction is usually in the range of 80 to 350 ° C. Since the polymerization apparatus used in the present invention does not have a seal portion of a stirrer for mechanical stirring, the leakage of air and the like is very small, so that the reaction temperature can be set higher than that of a conventional mechanically stirred polymerization apparatus. Possible powers are around 300 ° C !, you don't even need to be hot!
- the polymerization reaction proceeds at a relatively low temperature.
- Preferred reaction temperatures are between 100 and 290 ° C, more preferred between 150 and 270 ° C.
- an aromatic monohydroxy conjugate for example, phenol
- the reaction rate is increased by removing the product from the reaction system.
- an inert gas such as nitrogen, argon, helium, carbon dioxide, or a lower hydrocarbon gas which does not adversely affect the reaction is introduced into the polymerization apparatus, and the aromatic monohydric compound formed is produced.
- a method of removing substances by entraining these substances in these gases, a method of performing a reaction under reduced pressure, and the like are preferably used.
- a method using these in combination is also preferably used.
- the preferred reaction pressure in the polymerization zone in the present invention is determined by the aromatic polycarbonate to be produced. Forces that vary depending on the type, molecular weight, polymerization temperature, etc. of the acrylate.For example, when producing an aromatic polycarbonate from a molten prepolymer of bisphenol A and diphenol carbonate, if the number average molecular weight of the molten prepolymer is 5,000 or less, , 400-3, OOOPa range force S is preferable, and when the number average molecular weight force is 5,000-10,000, it is more preferably in the range of 50-500 Pa. When the number average molecular weight is 10,000 or more, it is preferably 300 Pa or less, and particularly preferably in the range of 20 to 250 Pa.
- a guide contact-flow type first polymerization device a guide contact flow-type second polymerization device, a guide contact flow-type third polymerization device, and a guide contact flow-type fourth polymerization device are used.
- the total external surface area of the guide having the power of each polymerization device is increased.
- the polymerization temperature may be the same in each polymerization apparatus, or may be increased in order. It is also possible to lower the polymerization pressure sequentially in each polymerization zone.
- a more preferred range is 1.5 ⁇ S1 / S2 ⁇ 15.
- each polymerization apparatus When two or more polymerization apparatuses are connected to perform polymerization, each polymerization apparatus is It is necessary that the supplied molten prevolumemer absorbs an inert gas.
- the inert gas absorption device is used as needed before supplying to the second polymerization device. It can be supplied to absorb a predetermined amount of inert gas.
- the molten prevolumemer which also discharges the power of the first polymerization unit, emits most of the inert gas absorbed in the first polymerization unit because of its relatively low viscosity.
- the type of inert gas supplied to the molten prepolymer discharged from the first polymerization device is the same as the type of inert gas absorbed by the molten prepolymer supplied to the first polymerization device. Good and different.
- the aromatic hydroxy compound produced by the force polymerization reaction which produces 1 ton or more of aromatic polycarbonate per hour, is discharged out of the system, so that it is more than 1 ton per hour.
- the raw material must be supplied to the polymerization equipment.
- the amount of the molten prepolymer to be supplied is a force that varies depending on the degree of polymerization and the degree of polymerization of the aromatic polycarbonate to be produced.
- the production amount of aromatic polycarbonate is 10 to 500 kgZhr higher per 1 ton Zhr, 1 01 ⁇ 1.5 tons Zhr range.
- the reaction for producing an aromatic polycarbonate from the aromatic dihydroxy conjugate and the diaryl carbonate can be carried out without adding a catalyst.
- a catalyst may be necessary. Done below.
- the catalyst is not particularly limited as long as it is used in this field.
- the catalyst examples include alkali metal and alkaline earth metal hydroxides such as lithium hydroxide, sodium hydroxide, potassium hydroxide, and calcium hydroxide; lithium aluminum hydride, Alkali metal salts, alkaline earth metal salts, quaternary ammonium salts of hydrides of boron and aluminum such as sodium borohydride and tetramethylammonium borohydride; lithium hydride, sodium hydride, hydrogen Alkali metal and alkaline earth metal hydrogen compounds such as calcium iodide; alkali metal and alkaline earth metal alkoxides such as lithium methoxide, sodium ethoxide and calcium methoxide; lithium Aliphatic oxides of alkali metals and alkaline earth metals such as phenoxide, sodium phenoxide, magnesium phenoxide, LiO—Ar—OLi, NaO—Ar—ONa (Ar is aryl group); lithium acetate, calcium acetate Organic acid salts of alkali metals and al
- Ammo-pamborate or phospho-pamborate represented by R 4 is as described above. ), Etc .; silicon compounds such as silicon oxide, sodium silicate, tetraalkyl silicon, tetraaryl silicon, diphenyl-ruethyl-ethoxy silicon, etc .; germanium oxide, germanium tetrachloride Compounds such as germanium, germanium ethoxide, and germanium phenoxide; Suzuki ligations bonded to alkoxy or aryloxy groups such as tin oxide, dialkyl tin oxide, dialkyl tin carboxylate, tin acetate, and ethyl ethyl tributoxide.
- these catalysts may be used alone or in a combination of two or more.
- the amount of these catalysts, the aromatic dihydroxy I spoon compounds of the raw materials, usually 10 _1 ° to 1 wt%, preferably 10 9 to 10 _1 wt%, more preferably 10- 8 to : L0- 2 is in the range of weight 0/0.
- the polymerization catalyst used remains in the aromatic polycarbonate of the product, but these polymerization catalysts usually have many adverse effects on the physical properties of the polymer. Therefore, it is preferable to reduce the amount of the catalyst used as much as possible.
- the method of the present invention In this case, the polymerization can be carried out efficiently, so that the amount of the catalyst used can be reduced. This is also one of the advantages of the present invention that a high-quality aromatic polycarbonate can be produced.
- the material of the guide contact-flow polymerization apparatus and piping used in the present invention there is no particular limitation on the material of the guide contact-flow polymerization apparatus and piping used in the present invention.
- the surface of these materials may be subjected to various treatments such as plating, lining, passivation treatment, acid washing, phenol washing and the like as required.
- Particularly preferred are stainless steel, nickel, glass lining and the like.
- the aromatic polycarbonate produced by the method of the present invention has a repeating unit represented by the following formula.
- aromatic polycarbonate containing 85 mol% or more of the repeating units represented by the following formula in all the repeating units.
- the terminal group of the aromatic polycarbonate produced by the method of the present invention usually has a hydroxyl group or an aryl carbonate group represented by the following formula.
- Ar 5 is the same as Ar 3 and Ar 4 described above.
- the ratio of the hydroxy group to the aryl carbonate group is not particularly limited, but is usually in the range of 95: 5 to 5:95, preferably in the range of 90:10 to: LO: 90, and more preferably in the range of LO: 90.
- the range is from 80:20 to 20:80.
- aromatic polycarbonates in which the proportion of phenol carbonate groups in the terminal groups is at least 85 mol%.
- the aromatic polycarbonate produced by carrying out the method of the present invention includes a plurality of aromatic polycarbonate main chains, and the plurality of aromatic polycarbonate main chains as a whole have an ester bond and an ether bond. It may be partially branched by bonding to at least one side chain via one kind of hetero bond selected from the group consisting of bonding agents.
- the amount of the heterogeneous bond depends on a plurality of aromatic polycarbonate main chains.
- Against the carbonate bond is usually 0.005 to 2 mol%, preferably 0.01 to 1 Monore 0/0, a, more preferred, from 0.05 to 0.5 Monore 0/0 It is.
- Such a heterogeneous bond in such an amount improves flow characteristics during melt molding without deteriorating other polymer physical properties, and is therefore suitable for precision molding, and can be molded even at a relatively low temperature.
- a molded article having excellent performance can be manufactured. Molding cycle can be shortened It can also contribute to energy saving at the time.
- the aromatic polycarbonate produced by the method of the present invention hardly contains impurities, but contains at least one metal compound selected from the group consisting of alkali metal compounds and alkaline earth metal compounds. It is possible to produce an aromatic polycarbonate having an amount of 0.001 to lppm in terms of the total amount of alkali metal atoms and alkaline earth metal atoms. Preferably, this content is between 0.005 and 0.5 ppm, more preferably between 0.01 and 0.1 ppm.
- aromatic polycarbonates produced by the method of the present invention particularly preferred are a halogen-free high-purity aromatic dihydroxy conjugate and a halogen-free high-purity diaryl carbonate. It is produced by using the compound and usually has a halogen atom content of lOppb or less.
- the method of the present invention can produce an aromatic polycarbonate having a halogen atom content of 5 ppb or less, and more preferably an aromatic polycarbonate having a halogen atom content of 1 ppb or less. Is obtained.
- the method of the present invention enables long-term stable and efficient production of an aromatic polycarbonate having no variation in molecular weight, because of the use of a molten prepolymer which absorbs a specific amount of an inert gas. It is clear from the examples that this is because the use of the above polymerization apparatus is combined.
- GPC Gel permeation chromatography
- M 0.391M image (Where M is the molecular weight of the aromatic polycarbonate, and M is the molecular weight of the polystyrene
- hetero bond The amount of at least one hetero bond selected from the group consisting of ester bond and ether bond (hereinafter, simply referred to as "hetero bond”) was measured by the method described in WO 97Z32916.
- Alkali metal Z The content of alkaline earth metal was measured by the ICP method.
- An aromatic polycarbonate was produced using an apparatus in which a guide contact falling inert gas absorption device and a guide contact falling type polymerization device as shown in Fig. 2 were connected in series.
- the material of the inert gas absorption device and the polymerization device is stainless steel, except for the molten prepolymer discharge pump 8 and the aromatic polycarbonate discharge pump 8.
- An inert gas supply port 9 is provided at a lower portion of the inert gas absorption zone 5, and a vent port 6 is provided at an upper portion, but the vent port 6 is usually closed.
- the outside of the inert gas absorber is a jacket, which is heated by a heating medium. From the discharge pump 8 of the inert gas absorption device, through the supply port 1 of the polymerization device, the molten prevolumemer that has absorbed the inert gas supplied to the molten prepolymer supply zone is distributed by the distribution plate 2 to each guide 4 of the polymerization reaction zone 5. Evenly distributed.
- An inert gas supply port 9 is provided at the lower part of the polymerization apparatus, and a vacuum vent port 6 is provided at the upper part.
- the outside of the polymerization vessel is a jacket, which is heated by a heating medium.
- the molten pre-bolymer of aromatic polycarbonate (number average molecular weight M is 3,800) maintained at 260 ° C manufactured from bisphenol ⁇ and diphenol carbonate (bisphenol A molar ratio to 1.05) , Supplied from the supply port 1 of the inert gas absorption device by the supply pump
- Zone 3 was fed continuously.
- the molten prevolimer which was continuously supplied to the inert gas absorption zone 5 through the perforated plate 2 in the inert gas absorption device, was absorbed along the guide 4 while absorbing the inert gas.
- the inert gas absorption zone 5 supplies nitrogen gas from the inert gas supply port 9 and is maintained at 200, OOOPa.
- the lower force of the guide 4 is also inert.
- the amount of the molten pre-bolimer (containing 0.05 Nl of nitrogen per 1 kg of the molten prepolymer) that has fallen into the tapered lower part 11 of the casing of the inert gas absorbing device becomes almost constant at the bottom.
- the liquid was continuously withdrawn by the discharge pump 8 and continuously supplied to the supply zone 3 through the supply port 1 of the polymerization apparatus as it was.
- the nitrogen-absorbed molten pre-polymer which was continuously supplied to the polymerization reaction zone 5 through the distribution plate 2 in the polymerization apparatus, flowed down along the guide 4, and the polymerization reaction proceeded.
- the polymerization reaction zone is maintained at 60 Pa through the vacuum vent 6.
- the produced aromatic polycarbonate dropped from the lower part of the guide 4 to the tapered lower part 11 of the casing of the polymerization apparatus so that the amount at the bottom is almost constant.
- the liquid was continuously extracted from the outlet 7 at a flow rate of 5.2 tons Zhr by a discharge pump 8.
- the number average molecular weight Mn of the aromatic polycarbonate extracted from 12 was 11, 000, 10, 980, 11 000, 10, 980, 11 000, 11 000, 10, 980, 11 000, which was stable.
- a very high molecular weight polymer mass (usually having a diameter of 1 mm or less, which can be visually confirmed by the difference in refractive index from other parts) Did not exist.
- the content of the alkali metal and the Z or alkaline earth metal compound in the aromatic polycarbonate thus produced is 0.04 to 0.05 ppm in terms of these metal elements,
- the content of halogen atoms (chlorine atoms) was less than lppb.
- the content of the heterogeneous bond was 0.12 to 0.15 mol%.
- Example 3 was continuously supplied. Polymerization was carried out in the same manner as in Example 1 except that the pressure in the polymerization reaction zone 5 was maintained at 90 Pa to produce an aromatic polycarbonate. The produced aromatic polycarbonate was continuously extracted from the outlet 7 at a flow rate of 6.5 tons Zhr.
- the number-average molecular weight Mn of the aromatic polycarbonate discharged by 12 forces was 7,700, 7,700, 7,72,0,720, 7,700, 7,700, 7,700, and 7,720, respectively.
- the content of the alkali metal and the Z or alkaline earth metal compound in the aromatic polycarbonate thus produced is 0.03 to 0.04 ppm in terms of these metal elements,
- the content of halogen atoms (chlorine atoms) was less than lppb.
- the content of the heterogeneous bond was 0.08 to 0.1 mol%.
- two inert gas absorbing devices (first inert gas absorbing device, second inert gas absorbing device) and two guide contact-flow-type polymerization devices (first polymerization device, second polymerization device)
- the polymerization apparatus was used to produce an aromatic polycarbonate using a polymerization apparatus in which a first inert gas absorption device, a first polymerization device, a second inert gas absorption device, and a second polymerization device were arranged in this order.
- the material of the inert gas absorption device and the polymerization device is stainless steel, except for the molten pre-polymer discharge pump 8 and the aromatic polycarbonate discharge pump 8.
- the first inert gas absorbing device is almost the same as the inert gas absorbing device of Example 1 except that the diameter of the hole of the distribution plate is about 0.2 cm.
- Feed zone 3 was continuously fed.
- the molten prevolimer which was continuously supplied to the inert gas absorbing zone 5 through the perforated plate 2 of the first inert gas absorbing device, was absorbed along the guide 4 while absorbing the inert gas.
- the inert gas absorption zone of the first inert gas absorption device is supplied with nitrogen gas from the inert gas supply port 9 and maintained at 180, OOOPa.
- the lower force of guide 4 is also the taper type of the casing of the first inert gas absorber.
- the molten pre-bolimer (which contains 0.04 N liters of nitrogen per kg of the molten pre-bolimer) that has fallen into the lower part 11 is continuously withdrawn by the discharge pump 8 so that the amount at the bottom becomes substantially constant, and is discharged as it is into the first part. It was continuously supplied to supply zone 3 via supply port 1 of the polymerization apparatus.
- the polymerization reaction zone of the first polymerization apparatus is maintained at a pressure of 600 Pa through a vacuum vent 6.
- the inert gas absorption zone 5 is formed.
- the molten prevolumer supplied continuously was absorbed along the guide 4 while absorbing the inert gas.
- the inert gas absorption zone of the second inert gas absorption device is supplied with nitrogen gas from the inert gas supply port 9 and is maintained at 200, OOOPa.
- the molten pre-volimer (containing 0.05 N liter of nitrogen per kg of the molten pre-volimer) dropped from the lower part of the guide 4 to the tapered lower part 11 of the first inert gas absorber casing so that the amount at the bottom is almost constant.
- the mixture was continuously discharged at a constant rate by a discharge pump 8 and continuously supplied to the supply zone 3 through the supply port 1 of the second polymerization apparatus.
- the polymerization reaction proceeded while the molten prepolymer was continuously supplied to the polymerization reaction zone 5 through the distribution plate 2 in the second polymerization apparatus and flowed down along the guide 4.
- the polymerization reaction zone of the second polymerization apparatus is maintained at a pressure of 70 Pa through the vacuum vent 6.
- the produced aromatic polycarbonate which has fallen from the lower part of the guide 4 to the tapered lower part 11 of the casing of the second polymerization apparatus, is discharged from the discharge port 7 to 7 tons by the discharge pump 8 so that the amount at the bottom is substantially constant. At a constant flow rate.
- the number average molecular weight Mn of the aromatic polycarbonate extracted from the outlet 12 was 11,530, 11,530, and 11, respectively.
- 500, 11, 500, 11, 510, 11, 500, 11, 520, 11, 510 were stable.
- no very high molecular weight polymer lump (which could be visually confirmed by the difference in refractive index from other parts) was found o.
- the content of the alkali metal and the Z or alkaline earth metal compound in the aromatic polycarbonate thus produced is 0.03 to 0.05 ppm in terms of these metal elements,
- the content of halogen atoms (chlorine atoms) was less than lppb.
- the content of the heterogeneous bond was 0.11 to 0.16 mol%.
Description
Claims
Priority Applications (10)
Application Number | Priority Date | Filing Date | Title |
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BRPI0510102-6A BRPI0510102A (pt) | 2004-06-14 | 2005-06-14 | método para produzir eficientemente um policarbonato aromático e policarbonato aromático produzido por meio de tal método |
AT05751169T ATE498644T1 (de) | 2004-06-14 | 2005-06-14 | Verfahren zur effizienten herstellung von aromatischem polycarbonat |
JP2006514605A JP4181601B2 (ja) | 2004-06-14 | 2005-06-14 | 芳香族ポリカーボネートを効率的に製造する方法 |
US10/592,690 US7528213B2 (en) | 2004-06-14 | 2005-06-14 | Method for efficiently producing an aromatic polycarbonate |
AU2005252556A AU2005252556B2 (en) | 2004-06-14 | 2005-06-14 | Process for efficiently producing aromatic polycarbonate |
CN2005800128678A CN1946762B (zh) | 2004-06-14 | 2005-06-14 | 有效生产芳族聚碳酸酯的方法 |
EA200601808A EA011093B1 (ru) | 2004-06-14 | 2005-06-14 | Способ эффективного получения ароматического поликарбоната |
DE602005026382T DE602005026382D1 (de) | 2004-06-14 | 2005-06-14 | Verfahren zur effizienten herstellung von aromatischem polycarbonat |
CA002560015A CA2560015A1 (en) | 2004-06-14 | 2005-06-14 | Method for efficiently producing an aromatic polycarbonate |
EP05751169A EP1760107B1 (en) | 2004-06-14 | 2005-06-14 | Process for efficiently producing aromatic polycarbonate |
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JP2004-176205 | 2004-06-14 | ||
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US (1) | US7528213B2 (ja) |
EP (1) | EP1760107B1 (ja) |
JP (1) | JP4181601B2 (ja) |
KR (1) | KR100813451B1 (ja) |
CN (1) | CN1946762B (ja) |
AT (1) | ATE498644T1 (ja) |
AU (1) | AU2005252556B2 (ja) |
BR (1) | BRPI0510102A (ja) |
CA (1) | CA2560015A1 (ja) |
DE (1) | DE602005026382D1 (ja) |
EA (1) | EA011093B1 (ja) |
WO (1) | WO2005121211A1 (ja) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
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EP1760109A1 (en) * | 2004-06-14 | 2007-03-07 | Asahi Kasei Chemicals Corporation | Improved process for producing aromatic polycarbonate |
WO2008065776A1 (fr) * | 2006-11-27 | 2008-06-05 | Asahi Kasei Chemicals Corporation | Procédé de fabrication industrielle de polycarbonate aromatique haute qualité |
WO2008065874A1 (fr) * | 2006-11-28 | 2008-06-05 | Asahi Kasei Chemicals Corporation | Procédé de fabrication d'un polycarbonate aromatique de qualité élevée à l'échelle industrielle |
WO2022202130A1 (ja) * | 2021-03-26 | 2022-09-29 | 旭化成株式会社 | ポリカーボネートの製造装置の組み立て方法、及びポリカーボネートの製造装置 |
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EP2428266B1 (en) | 2010-09-10 | 2013-07-10 | Princo Middle East FZE | Process for preparation of high viscosity polymeric materials |
US9321884B2 (en) | 2010-10-29 | 2016-04-26 | Asahi Kasei Chemicals Corporation | Process for producing polycondensation polymer, and polymerizer |
CN102675619B (zh) * | 2011-12-05 | 2013-06-12 | 陕西延长石油(集团)有限责任公司 | 一种采用熔融酯交换法生产芳香族聚碳酸酯的聚合反应装置 |
EA032233B1 (ru) * | 2014-03-19 | 2019-04-30 | Асахи Касеи Кабусики Кайся | Поликонденсационный полимер и установка для его получения |
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- 2005-06-14 JP JP2006514605A patent/JP4181601B2/ja active Active
- 2005-06-14 WO PCT/JP2005/010854 patent/WO2005121211A1/ja not_active Application Discontinuation
- 2005-06-14 BR BRPI0510102-6A patent/BRPI0510102A/pt not_active IP Right Cessation
- 2005-06-14 AU AU2005252556A patent/AU2005252556B2/en not_active Ceased
- 2005-06-14 US US10/592,690 patent/US7528213B2/en active Active
- 2005-06-14 AT AT05751169T patent/ATE498644T1/de not_active IP Right Cessation
- 2005-06-14 EA EA200601808A patent/EA011093B1/ru not_active IP Right Cessation
- 2005-06-14 KR KR1020067022878A patent/KR100813451B1/ko active IP Right Grant
- 2005-06-14 EP EP05751169A patent/EP1760107B1/en active Active
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Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
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EP1760109A1 (en) * | 2004-06-14 | 2007-03-07 | Asahi Kasei Chemicals Corporation | Improved process for producing aromatic polycarbonate |
EP1760109A4 (en) * | 2004-06-14 | 2010-11-03 | Asahi Kasei Chemicals Corp | IMPROVED PROCESS FOR PRODUCING AROMATIC POLYCARBONATE |
WO2008065776A1 (fr) * | 2006-11-27 | 2008-06-05 | Asahi Kasei Chemicals Corporation | Procédé de fabrication industrielle de polycarbonate aromatique haute qualité |
JP5320071B2 (ja) * | 2006-11-27 | 2013-10-23 | 旭化成ケミカルズ株式会社 | 高品質芳香族ポリカーボネートの工業的製造法 |
WO2008065874A1 (fr) * | 2006-11-28 | 2008-06-05 | Asahi Kasei Chemicals Corporation | Procédé de fabrication d'un polycarbonate aromatique de qualité élevée à l'échelle industrielle |
JP5344927B2 (ja) * | 2006-11-28 | 2013-11-20 | 旭化成ケミカルズ株式会社 | 高品質芳香族ポリカーボネートを工業的規模で製造する方法 |
WO2022202130A1 (ja) * | 2021-03-26 | 2022-09-29 | 旭化成株式会社 | ポリカーボネートの製造装置の組み立て方法、及びポリカーボネートの製造装置 |
JP2022150566A (ja) * | 2021-03-26 | 2022-10-07 | 旭化成株式会社 | ポリカーボネートの製造装置の組み立て方法、及びポリカーボネートの製造装置 |
KR20220144412A (ko) * | 2021-03-26 | 2022-10-26 | 아사히 가세이 가부시키가이샤 | 폴리카르보네이트의 제조 장치의 조립 방법 및 폴리카르보네이트의 제조 장치 |
KR102503433B1 (ko) | 2021-03-26 | 2023-02-24 | 아사히 가세이 가부시키가이샤 | 폴리카르보네이트의 제조 장치의 조립 방법 및 폴리카르보네이트의 제조 장치 |
JP7258069B2 (ja) | 2021-03-26 | 2023-04-14 | 旭化成株式会社 | ポリカーボネートの製造装置の組み立て方法、及びポリカーボネートの製造装置 |
Also Published As
Publication number | Publication date |
---|---|
KR100813451B1 (ko) | 2008-03-13 |
EA011093B1 (ru) | 2008-12-30 |
BRPI0510102A (pt) | 2007-09-25 |
JPWO2005121211A1 (ja) | 2008-04-10 |
AU2005252556A1 (en) | 2005-12-22 |
AU2005252556B2 (en) | 2007-11-01 |
US20080234444A1 (en) | 2008-09-25 |
CN1946762B (zh) | 2011-01-19 |
DE602005026382D1 (de) | 2011-03-31 |
JP4181601B2 (ja) | 2008-11-19 |
EA200601808A1 (ru) | 2007-02-27 |
EP1760107B1 (en) | 2011-02-16 |
CN1946762A (zh) | 2007-04-11 |
CA2560015A1 (en) | 2005-12-22 |
KR20070036040A (ko) | 2007-04-02 |
EP1760107A4 (en) | 2009-09-16 |
ATE498644T1 (de) | 2011-03-15 |
EP1760107A1 (en) | 2007-03-07 |
US7528213B2 (en) | 2009-05-05 |
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