# US 8,785,565 B2 · Production method of polycarbonate, and polycarbonate pellet

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- Number: US 8,785,565 B2
- Document ID: US8785565B2
- Status: Granted
- Kind: B2
- Application number: 14/041,489
- Filed: 2013-09-30
- Published: 2014-01-30
- Granted: 2014-07-22
- Earliest claimed: 2011-03-31
- Assignees: Mitsubishi Chemical Corporation
- Applicants: Mitsubishi Chemical Corporation
- Inventors: Shingo Namiki; Yasuhiro Oda
- Web page: https://patentgrep.com/patent/US8785565B2

## CPC

- C08G 64/305: {and alcohols}
- C08G: MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS

## Abstract

The present invention relates to a method for producing a polycarbonate having excellent characteristics such as hue and mechanical properties with a stable quality and a high yield by solving a plurality of problems as those described above in producing a polycarbonate by using a specific dihydroxy compound exhibiting low thermal stability as compared with bisphenols and having a —CH2—O— structure. The polycarbonate obtained by polycondensation in the present invention is a polycarbonate having an appropriate viscosity despite decrease in the reaction temperature, providing for a color tone less susceptible to yellowing, and exhibiting excellent mechanical properties.

## Claims

### Claim 1

A method for producing a polycarbonate, the method comprising continuously feeding:
dihydroxy compounds containing a specific dihydroxy compound comprising a moiety represented by formula (1):
CH2—O (1);
a carbonic acid diester; and
a polymerization catalyst,
to a reactor and performing polycondensation to produce a polycarbonate,
wherein:
as the reactor, a plurality of reactors are connected at least in series;
an internal temperature of a penultimate reactor prior to a final polymerization reactor is from 200° C. to less than 230° C.; and
a melt viscosity of a reaction solution at an outlet of the penultimate reactor prior to the final polymerization reactor is from 100 to 1,000 Pa·s,
with the proviso that the moiety represented by formula (1) is not a part of —CH2—OH.

### Claim 2 (depends on 1)

The method according to claim 1, wherein the melt viscosity of the reaction solution at the outlet of the penultimate reactor prior to the final polymerization reactor is from 140 to 1,000 Pa·s.

### Claim 3 (depends on 1)

The method according to claim 1, wherein the internal temperature of a penultimate reactor prior to the final polymerization reactor is from 200° C. to less than 225° C.

### Claim 4 (depends on 1)

The method according to claim 1, wherein formula (2) is satisfied:
1.5≦Q/P≦2.5 (2),
wherein:
P represents a reduced viscosity of the reaction solution at the outlet of a penultimate reactor prior to the final polymerization reactor; and
Q represents a reduced viscosity of a reaction solution at the outlet of the final polymerization reactor.

### Claim 5 (depends on 1)

The method according to claim 1, wherein formula (3) is satisfied:
Y−X≦6 and at the same time, X≦5 (3),
wherein:
X (mol/ton) represents an amount of a double bond terminal structure in the reaction solution at the outlet of a penultimate reactor prior to the final polymerization reactor; and
Y (mol/ton) represents an amount of a double bond terminal structure in a reaction solution at the outlet of the final polymerization reactor.

### Claim 6 (depends on 1)

The method according to claim 1, wherein:
the final polymerization reactor is a horizontal stirring reactor having inside thereof a plurality of horizontal rotating shafts; and
the reaction conditions satisfy formula (4):
500≦ωμ≦20,000 (4),
wherein:
ω represents a rotation speed (rpm) of a stirring blade; and
μ represents a melt viscosity (Pa·s) of a reaction solution at the outlet of the horizontal reactor.

### Claim 7 (depends on 6)

The method according to claim 6, wherein the reaction conditions of the horizontal stirring reactor satisfy formula (5):
2≦V/A≦9 (5),
wherein:
V represents a volume (L) of the horizontal reactor; and
A represents a throughput (kg/hr) of a reaction solution.

### Claim 8 (depends on 1)

The method according to claim 1, wherein a melt viscosity of a reaction solution at the outlet of the final polymerization reactor is from 1,800 to 3,500 Pa·s.

### Claim 9 (depends on 1)

The method according to claim 1, wherein a temperature of a heating medium of the final polymerization reactor is from 210 to 260° C.

### Claim 10 (depends on 1)

The method according to claim 1, wherein a charge molar ratio of the carbonic acid diester to all dihydroxy compounds when charged into a first reactor is from 0.990 to 1.030.

### Claim 11 (depends on 1)

The method according to claim 1, wherein an amount of all hydroxy terminal groups in a reaction solution at the outlet of the final polymerization reactor is from 10 to 50 mol/ton.

### Claim 12 (depends on 1)

The method according to claim 1, wherein an amount of a monohydroxy compound in a reaction solution at the outlet of a penultimate reactor prior to the final polymerization reactor is from 1,000 ppm to 3 wt % and the amount of a monohydroxy compound in a reaction solution at the outlet of the final polymerization reactor is from 1 to 700 ppm.

### Claim 13 (depends on 1)

The method according to claim 1, wherein a pressure of the final polymerization reactor is from 10 Pa to 1 kPa.

### Claim 14 (depends on 1)

The method according to claim 1, wherein the polymerization catalyst is a compound comprising at least one metal belonging to Group 2 of the long-form periodic table and lithium.

### Claim 15 (depends on 1)

The method according to claim 1, wherein the specific dihydroxy compound is a compound having a cyclic ether structure.

### Claim 16 (depends on 15)

The method according to claim 15, wherein the specific dihydroxy compound is a compound represented by formula (6):

### Claim 17 (depends on 1)

The method according to claim 1, further comprising filtering the polycarbonate obtained by the polycondensation by feeding the polycarbonate in the molten state without being solidified to a filter.

### Claim 18 (depends on 1)

The method according to claim 1, further comprising ejecting the polycarbonate obtained by the polycondensation or a resin obtained by filtering the polycarbonate through a filter, into a strand from a die head and after cooling, pelletizing the strand with a cutter.

### Claim 19 (depends on 18)

A polycarbonate pellet produced by the method according to claim 18.

### Claim 20 (depends on 19)

The polycarbonate pellet according to claim 19, wherein a number of extraneous matters of 20 μm or more is 1,000 pieces/m2 or less.