Mitsubishi Chemical Corporation

Takehito Nagao

Shingo Namiki

Masanori Yamamoto

Masashi Yokogi

The present invention is a method for producing a polycarbonate resin, comprising performing polycondensation through a transesterification reaction by using a catalyst and using a dihydroxy compound and a carbonic acid diester as raw material monomers, and feeding the produced polycarbonate resin to an extruder, wherein the dihydroxy compound contains at least a dihydroxy compound having a moiety represented by formula (1) in a part of the structure, the dihydroxy compound having a moiety represented by formula (1) contains a compound having a cyclic ether structure, and the temperature at the time of feeding the polycarbonate resin to the extruder is from 180&#xb0; C. to less than 250&#xb0; C., with the proviso excluding the case where the moiety represented by formula (1) is a part of &#x2014;CH&#x2014;O&#x2014;HCH&#x2014;O&#x2003;&#x2003;(1).

Production method of polycarbonate resin

The present invention is a production method of a polycarbonate resin, including a step of performing melt polycondensation by continuously feeding a dihydroxy compound (A) having a predetermined moiety in a part of the structure and a carbonic acid diester each in a liquid state to a reactor, wherein the residence time from liquefaction of the dihydroxy compound to its feeding to a reactor is from 0.1 to 10 hours.

A method for producing a polycarbonate, comprises: continuously feeding a dihydroxy compound having a portion represented by &#x2014;(&#x2014;CH&#x2014;O&#x2014;)&#x2014; in a part of a structure thereof and a carbonic acid diester; and continuously performing polycondensation to produce a polycarbonate, wherein the method satisfies all of the conditions: (A) at least two reactor vessels connected in series are used; (B) a reaction solution reacted in a first reactor of the first vessel is continuously fed to a reactor of the second vessel; (C) the first reactor is equipped with a reflux condenser; and (D) a reflux ratio in the first reactor is from 0.01 to 10 based on a distillate volume.

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Fukuoka, Japan

Takehito Nagao