JP4530502B2 - Method for producing aromatic polycarbonate - Google Patents

Description

【００１５】
（式中、Ｒ¹ 、Ｒ² 、Ｒ³ 、Ｒ⁴ は、各々独立に水素、炭素数１〜１０のアルキル基、炭素数１〜１０のアルコキシ基、環構成炭素数５〜１０のシクロアルキル基、環構成炭素数５〜１０の炭素環式芳香族基、炭素数６〜１０の炭素環式アラルキル基を表す。ｋは３〜１１の整数を表し、Ｒ⁵ 及びＲ⁶ は、各Ｘについて個々に選択され、お互いに独立に、水素または炭素数１〜６のアルキル基を表し、Ｘは炭素を表す。また、Ｒ¹ 、Ｒ² 、Ｒ³ 、Ｒ⁴ 、Ｒ⁵ 、Ｒ⁶ において、一つ以上の水素原子が反応に悪影響を及ぼさない範囲で他の置換基、例えばハロゲン原子、炭素数１〜１０のアルキル基、炭素数１〜１０のアルコキシ基、フェニル基、フェノキシ基、ビニル基、シアノ基、エステル基、アミド基、ニトロ基等によって置換されたものであっても良い。）
このような２価の芳香族基Ａｒとしては、例えば、下記化２に示されるものが挙げられる。
【００１６】
【化２】

【００１７】
（式中、Ｒ⁷ 、Ｒ⁸ は、各々独立に水素原子、ハロゲン原子、炭素数１〜１０のアルキル基、炭素数１〜１０のアルコキシ基、環構成炭素数５〜１０のシクロアルキル基またはフェニル基であって、ｍおよびｎは１〜４の整数で、ｍが２〜４の場合には各Ｒ⁷ はそれぞれ同一でも異なるものであってもよいし、ｎが２〜４の場合には各Ｒ⁸ はそれぞれ同一でも異なるものであってもよい。）
さらに、２価の芳香族基Ａｒは、−Ａｒ¹ −Ｚ−Ａｒ² −（式中、Ａｒ¹ 、Ａｒ² は前述の通りで、Ｚは単結合又は−Ｏ−、−ＣＯ−、−Ｓ−、−ＳＯ₂ −、−ＳＯ−、−ＣＯＯ−、−ＣＯＮ（Ｒ¹ ）−などの２価の基を表す。但し、Ｒ¹ は前述のとおりである。）で示されるものであっても良い。
このような２価の芳香族基Ａｒとしては、例えば、下記化３に示されるものが挙げられる。
【００１８】
【化３】

（式中、Ｒ⁷ 、Ｒ⁸ 、ｍおよびｎは、前述のとおりである。）
【００１９】
さらに、２価の芳香族基Ａｒの具体例としては、置換または非置換のフェニレン、置換または非置換のナフチレン、置換または非置換のピリジレン等が挙げられる。
本発明で用いられる芳香族ジヒドロキシ化合物は、単一種類でも２種類以上でもかまわない。芳香族ジヒドロキシ化合物の代表的な例としてはビスフェノールＡが挙げられる。
【００２０】
本発明で用いられるジアリールカーボネートは、下記化４に表される。
【化４】

（式中、Ａｒ³ 、Ａｒ⁴ はそれぞれ１価の芳香族基を表す。）
【００２１】
Ａｒ³ 及びＡｒ⁴ は、１価の炭素環式又は複素環式芳香族基を表すが、このＡｒ³ 、Ａｒ⁴ において、一つ以上の水素原子が、反応に悪影響を及ぼさない他の置換基、例えば、ハロゲン原子、炭素数１〜１０のアルキル基、炭素数１〜１０のアルコキシ基、フェニル基、フェノキシ基、ビニル基、シアノ基、エステル基、アミド基、ニトロ基などによって置換されたものであっても良い。Ａｒ³ とＡｒ⁴ は同じものであっても良いし、異なるものであっても良い。
１価の芳香族基Ａｒ³ 及びＡｒ⁴ の代表例としては、フェニル基、ナフチル基、ビフェニル基、ピリジル基を挙げることができる。これらは、上述の１種以上の置換基で置換されたものでも良い。
【００２２】
好ましいＡｒ³ 及びＡｒ⁴ としては、それぞれ例えば、下記化５に示されるものなどが挙げられる。
【化５】

【００２３】
ジアリールカーボネートの代表的な例としては、下記化６に示される置換または非置換のジフェニルカーボネート類を挙げることができる。
【化６】

（式中、Ｒ⁹ 及びＲ¹⁰は、各々独立に水素原子、炭素数１〜１０のアルキル基、炭素数１〜１０のアルコキシ基、環構成炭素数５〜１０のシクロアルキル基又はフェニル基を示し、ｐ及びｑは１〜５の整数で、ｐが２以上の場合には、各Ｒ⁹ はそれぞれ異なるものであっても良いし、ｑが２以上の場合には、各Ｒ¹⁰は、それぞれ異なるものであっても良い。）
【００２４】
これらのジフェニルカーボネート類の中でも、非置換のジフェニルカーボネートや、ジトリルカーボネート、ジ−ｔ−ブチルフェニルカーボネートのような低級アルキル置換ジフェニルカーボネートなどの対称型ジアリールカーボネートが好ましいが、特にもっとも簡単な構造のジアリールカーボネートである非置換のジフェニルカーボネートが好適である。
これらのジアリールカーボネート類は単独で用いても良いし、２種以上を組み合わせて用いても良い。
【００２５】
本発明において、該ジアリールカーボネート中の水分含量は２００重量ｐｐｍ以下である。水分が２００重量ｐｐｍより多い場合は、製品芳香族ポリカーボネートのカラーが悪化し、かつ３８０℃以上の高温下で着色しやすくなり、分子量低下も大きくなる。この理由については明らかではないが、水分の存在によるジアリールカーボネートの分解とジアリールカーボネートの異性化反応等の組み合わせにより芳香族ポリカーボネートの高温下での安定性に悪影響を及ぼすものと推定している。該ジアリールカーボネート中の水分含量は、好ましくは１００重量ｐｐｍ以下、更に好ましくは５０重量ｐｐｍ以下である。また水分量の下限について特に限定はなく、０．０１重量ｐｐｍより水分量が少なくてもかまわないが、０．０１重量ｐｐｍより少なくしても芳香族ポリカーボネートの高温下での着色や分子量低下を改善させる効果は少ない。
ジアリールカーボネート中の水分含量を上記範囲にコントロールする方法としては、輸送や貯蔵中の吸湿を避ける方法や、吸湿して上記上限の２００重量ｐｐｍより高い水分量となった場合は、蒸留等による脱水操作を行った後に、芳香族ポリカーボネートの重合に使用する方法等が挙げられる。
【００２６】
本発明において、該ジアリールカーボネート中の銅含量は１重量ｐｐｍ以下である。銅含量が１重量ｐｐｍより多い場合は、製品芳香族ポリカーボネートのカラーが悪化し、かつ３８０℃以上の高温下で着色しやすくなり、分子量低下も大きくなる。
この理由については明らかではないが、銅の存在が芳香族ポリカーボネートの高温下での着色反応や分子量低下反応に触媒的に作用するものと推定される。該ジアリールカーボネート中の銅含量は、好ましくは０．５重量ｐｐｍ以下、更に好ましくは０．１重量ｐｐｍ以下である。また銅含量の下限について特に限定はなく、０．００１重量ｐｐｍより銅含量が少なくてもかまわないないが、０．００１重量ｐｐｍより銅含量を少なくしても芳香族ポリカーボネートの高温下での着色や分子量低下を改善させる効果は少ない。
【００２７】
銅含量を上記範囲にコントロールする方法としては、ジアリールカーボネートを製造する際、銅触媒を全く使用しないか、銅触媒を用いてジアリールカーボネートを製造した後、蒸留操作や洗浄操作等によって銅含量を減少させる方法等が挙げられる。ただし、銅触媒を全く使用しないでジアリールカーボネートを製造する場合は、製品ポリカーボネートの品質を悪化させる様な他の触媒成分がジアリールカーボネート中に含有されないことが好ましい。
【００２８】
本発明において、該ジアリールカーボネート中の（ｏ−フェノキシフェニル）（フェニル）カーボネート含量は１重量ｐｐｍ以下である。（ｏ−フェノキシフェニル）（フェニル）カーボネート含量が１重量ｐｐｍより多い場合は、製品芳香族ポリカーボネートのカラーが悪化し、かつ３８０℃以上の高温下で着色しやすくなる。
この理由についても明らかではないが、（ｏ−フェノキシフェニル）（フェニル）カーボネート自身、または（ｏ−フェノキシフェニル）（フェニル）カーボネートと芳香族ポリカーボネートとの反応物が高温で着色しやすいものと推定している。該ジアリールカーボネート中の（ｏ−フェノキシフェニル）（フェニル）カーボネート含量は、好ましくは０．５重量ｐｐｍ以下、更に好ましくは０．１重量ｐｐｍ以下である。また（ｏ−フェノキシフェニル）（フェニル）カーボネート含量の下限について特に限定はなく、０．０１重量ｐｐｍより（ｏ−フェノキシフェニル）（フェニル）カーボネート含量が少なくてもかまわないないが、０．０１重量ｐｐｍより（ｏ−フェノキシフェニル）（フェニル）カーボネート含量を少なくしても芳香族ポリカーボネートの高温下での着色を改善させる効果は少ない。
【００２９】
芳香族ジヒドロキシ化合物とジアリールカーボネートから芳香族ポリカーボネートを製造する際、ジアリールカーボネートを工業的に好ましくハンドリングするために、通常、ジアリールカーボネートは溶融状態で貯蔵された後に用いられる。本発明においては、該ジアリールカーボネートが、ステンレス製の容器で窒素雰囲気下に８０〜１９０℃の温度で溶融状態で貯蔵されたものであることが好ましい。貯蔵する容器がカーボンスチール製の場合には、（ｏ−フェノキシフェニル）（フェニル）カーボネートの生成量が多くなる場合がある。
【００３０】
ステンレスとは、ステンレス鋼便覧第１３〜２１頁（日刊工業新聞社発行、第５版）に定義、分類されるような通常クロムを１０〜３０重量％含む、マルテンサイト系、フェライト系、オーステナイト系、フェライト・オーステナイト系等のステンレス鋼や、上記ステンレス鋼便覧５４７頁の表に示されるようなＦｅ基超合金等があげられる。具体例としては、ＳＵＳ２０１、ＳＵＳ２０２、ＳＵＳ３０４、ＳＵＳ３０４Ｌ、ＳＵＳ３１６、ＳＵＳ３１６Ｌ、ＳＵＳ３４７、ＳＵＳ４０５、ＳＵＳ４３０、ＳＵＳ４０３、ＳＵＳ４１０、ＳＵＳ４３１、ＳＵＳ４４０Ｃ、ＳＵＳ６３０、インコロイ８００、インコロイ８０１、インコロイ８０２、インコロイ８０７、インコロイ９０１、ＬＣＮ１５５、Ｗ５４５、Ｖ５７、Ｗ５４５、Ｄ９７９、ＣＧ２７、Ｓ５９０等が挙げられる。好ましい具体例としてはＳＵＳ３０４、ＳＵＳ３０４Ｌ、ＳＵＳ３１６、ＳＵＳ３１６Ｌ等が挙げられ、特に好ましくはＳＵＳ３０４が挙げられる。
【００３１】
該ステンレス製の容器の内壁面の接液部は、フェノールで洗浄処理を施されたものであることが好ましい。フェノールで洗浄処理を施されたステンレス製の容器を用いた場合、特に（ｏ−フェノキシフェニル）（フェニル）カーボネートの生成量を少なくすることができる。この理由については明らかではないが、ステンレス表面の吸着酸素をフェノールで除去することにより、（ｏ−フェノキシフェニル）（フェニル）カーボネートの生成を妨げているものと推定される。
【００３２】
また、貯蔵は窒素雰囲気下とすることが好ましく、貯蔵容器に空気が混入すると（ｏ−フェノキシフェニル）（フェニル）カーボネートの生成量が多くなる。貯蔵温度は８０〜１９０℃の範囲であることが好ましく、１９０℃より高い場合は、（ｏ−フェノキシフェニル）（フェニル）カーボネートの生成量が多くなりやすい。８０℃より低い場合は、ジアリールカーボネートの種類によっては固化してしまうので好ましくない。より好ましい貯蔵温度範囲は８５〜１６０℃であり、更に好ましくは９０〜１４０℃である。
【００３３】
本発明において芳香族ポリカーボネートを製造する際、芳香族ジヒドロキシ化合物とジアリールカーボネートとの使用割合（仕込比率）は、用いられる芳香族ジヒドロキシ化合物とジアリールカーボネートの種類や、重合温度その他の重合条件によって異なるが、ジアリールカーボネートは芳香族ジヒドロキシ化合物１モルに対して、通常０．９〜２．５モル、好ましくは０．９５〜２．０モル、より好ましくは０．９８〜１．５モルの割合で用いられる。
本発明の方法で得られる芳香族ポリカーボネートの数平均分子量は、通常５０００〜１０００００の範囲であり、好ましくは５０００〜３００００の範囲である。
【００３４】
本発明の芳香族ポリカーボネートの製造法は、上記のような芳香族ジヒドロキシ化合物とジアリールカーボネートとから、触媒の存在もしくは不存在下で、減圧下および／または不活性ガスフロー下で加熱しながら溶融状態でエステル交換反応にて重縮合する方法であり、その重合器には特に制限はない。例えば、攪拌槽型反応器、薄膜反応器、遠心式薄膜蒸発反応器、表面更新型二軸混練反応器、二軸横型攪拌反応器、濡れ壁式反応器、自由落下させながら重合する多孔板型反応器、ワイヤーに沿わせて落下させながら重合するワイヤー付き多孔板型反応器等を用い、これらを単独もしくは組み合わせた重合器が用いられる。重合は、バッチ方式、連続方式のいずれも可能である。また、重合後、芳香族ポリカーボネートが溶融状態にある間に安定剤、添加剤等を添加するための装置として、押出機やポリマーミキサー等を重合器と組み合わせて用いることも好ましい方法である。これらの重合器の材質について特に制限はなく、通常ステンレススチールやニッケル、グラスライニング等から選ばれる。
【００３５】
本発明において、芳香族ジヒドロキシ化合物とジアリールカーボネートとを反応させて芳香族ポリカーボネートを製造するに当たり、反応の温度は、通常５０〜３５０℃、好ましくは１００〜３００℃の温度の範囲で選ばれる。
反応の進行にともなって、芳香族モノヒドロキシ化合物が生成してくるが、これを反応系外へ除去する事によって反応速度が高められる。従って、窒素、アルゴン、ヘリウム、二酸化炭素や低級炭化水素ガスなど反応に悪影響を及ぼさない不活性なガスを導入して、生成してくる該芳香族モノヒドロキシ化合物をこれらのガスに同伴させて除去する方法や、減圧下に反応を行う方法などが好ましく用いられる。好ましい反応圧力は、分子量によっても異なり、重合初期には１０ｍｍＨｇ〜常圧の範囲が好ましく、重合後期には、２０ｍｍＨｇ以下、特に１０ｍｍＨｇ以下が好ましく、２ｍｍＨｇ以下とすることが更に好ましい。
【００３６】
溶融重縮合反応は、触媒を加えずに実施することができるが、重合速度を高めるため、必要に応じて触媒の存在下で行われる。重合触媒としては、この分野で用いられているものであれば特に制限はないが、水酸化リチウム、水酸化ナトリウム、水酸化カリウム、水酸化カルシウムなどのアルカリ金属またはアルカリ土類金属の水酸化物類；水素化ホウ素ナトリウム、水素化ホウ素テトラメチルアンモニウムなどのホウ素の水素化物のアルカリ金属塩、アルカリ土類金属塩、第四級アンモニウム塩類；水素化リチウム、水素化ナトリウム、水素化カルシウムなどのアルカリ金属またはアルカリ土類金属の水素化合物類；
【００３７】
リチウムメトキシド、ナトリウムエトキシド、カルシウムメトキシドなどのアルカリ金属またはアルカリ土類金属のアルコキシド類；リチウムフェノキシド、ナトリウムフェノキシド、マグネシウムフェノキシド、ＬｉＯ−Ａｒ−ＯＬｉ、ＮａＯ−Ａｒ−ＯＮａ（Ａｒはアリール基）などのアルカリ金属またはアルカリ土類金属のアリーロキシド類；酢酸リチウム、酢酸カルシウム、安息香酸ナトリウムなどのアルカリ金属またはアルカリ土類金属の有機酸塩類；酸化亜鉛、酢酸亜鉛、亜鉛フェノキシドなどの亜鉛化合物類；酸化ホウ素、ホウ酸、ホウ酸ナトリウム、ホウ酸トリメチル、ホウ酸トリブチル、ホウ酸トリフェニル、（Ｒ¹ Ｒ² Ｒ³ Ｒ⁴ ）ＮＢ（Ｒ¹ Ｒ² Ｒ³ Ｒ⁴ ）で表されるアンモニウムボレート類、（Ｒ¹ Ｒ² Ｒ³ Ｒ⁴ ）ＰＢ（Ｒ¹ Ｒ² Ｒ³ Ｒ⁴ ）で表されるホスホニウムボレート類（Ｒ¹ 、Ｒ² 、Ｒ³ 、Ｒ⁴ は前記化１の説明通りである。）などのホウ素の化合物類；
【００３８】
酸化ケイ素、ケイ酸ナトリウム、テトラアルキルケイ素、テトラアリールケイ素、ジフェニル−エチル−エトキシケイ素などのケイ素の化合物類；酸化ゲルマニウム、四塩化ゲルマニウム、ゲルマニウムエトキシド、ゲルマニウムフェノキシドなどのゲルマニウムの化合物類；酸化スズ、ジアルキルスズオキシド、ジアルキルスズカルボキシレート、酢酸スズ、エチルスズトリブトキシドなどのアルコキシ基またはアリーロキシ基と結合したスズ化合物、有機スズ化合物などのスズの化合物類；酸化鉛、酢酸鉛、炭酸鉛、塩基性炭酸塩、鉛及び有機鉛のアルコキシドまたはアリーロキシドなどの鉛の化合物；第四級アンモニウム塩、第四級ホスホニウム塩、第四級アルソニウム塩などのオニウム化合物類；酸化アンチモン、酢酸アンチモンなどのアンチモンの化合物類；酢酸マンガン、炭酸マンガン、ホウ酸マンガンなどのマンガンの化合物類；酢酸ジルコニウム、酸化ジルコニウム、ジルコニウムのアルコキシド又はアリーロキシド、ジルコニウムアセチルアセトンなどのジルコニウムの化合物類などの触媒を挙げることができる。
【００３９】
触媒を用いる場合、これらの触媒は１種だけで用いても良いし、２種以上を組み合わせて用いても良い。また、これらの触媒の使用量は、原料の芳香族ジヒドロキシ化合物１００重量部に対して、通常１０^-8〜１重量部、好ましくは１０^-7〜１０^-1重量部の範囲で選ばれる。
【００４０】
【発明の実施の形態】
以下、本発明の実施の形態により本発明を更に詳細に説明する。
・水分：カールフィッシャー法により分析した。
・銅含量：ＩＣＰ（高周波誘導結合型プラズマ発光分析計；セイコー電子工業（株）製ＪＹ３８ＰII）を用いて分析した。
・（ｏ−フェノキシフェニル）（フェニル）カーボネート含量：ガスクロマトグラフ法により分析した。
・着色：試料１ｇを塩化メチレン７ｍｌに溶かした溶液を光路長１ｃｍのセルに入れ、分光光度計により４００ｎｍの吸光度を測定し、着色の指標とした。
【００４１】
・高温での着色のしやすさ：芳香族ポリカーボネートを窒素雰囲気下３８０℃で３０分間加熱し、加熱による上記４００ｎｍの吸光度の増大量で評価した。
・数平均分子量（Ｍｎ）：テトラヒドロフランを溶媒として用い、ゲルパーミエーションクロマトグラフィー（ＧＰＣ）｛カラム：ＴＳＫ−ＧＥＬ，東ソー（株）製｝法で測定し、標準単分散ポリスチレンを用いて得た下式による換算分子量較正曲線を用いて求めた。
Ｍ_PC＝０．３５９１Ｍ_PS ^1.0388
（式中、Ｍ_PCは芳香族ポリカーボネートの分子量、Ｍ_PSはポリスチレンの分子量を示す。）
・高温での分子量低下のしやすさ：芳香族ポリカーボネートを窒素雰囲気下３８０℃で３０分間加熱し、加熱による数平均分子量の減少量で評価した。
【００４２】
【参考実施例１】
ジフェニルカーボネートをジメチルカーボネートとフェノールからジフェノキシ銅を触媒として製造した後、圧力１５９６Ｐａ、蒸留段数５、還流比３．２の条件で、塔頂から２段目の気相でサイドカットして蒸留精製し、ＳＵＳ３０４製の容器で、窒素雰囲気下、１１０℃、１００時間貯蔵した。貯蔵後のジフェニルカーボネート中の水分含量０．１重量ｐｐｍ、銅含量０．４重量ｐｐｍ、（ｏ−フェノキシフェニル）（フェニル）カーボネート含量０．１重量ｐｐｍであった。該ジフェニルカーボネートを用いて、図１に示すようなプロセスで芳香族ポリカーボネートを製造した。
【００４３】
撹拌槽型重合器３はバッチ的に運転し、貯槽１０以降は連続的に運転した。撹拌槽型重合器３（容量２００リットル）、１７（容量５０リットル）、２６（容量５０リットル）は、いずれも攪拌翼を備えている。横型二軸攪拌型重合器３５（容量３０リットル）は、Ｌ／Ｄ＝６で回転直径１４０ｍｍの二軸の攪拌羽根を有している。ワイヤ付多孔板型重合器４２は、孔径５ｍｍの孔を５０個有する多孔板４３を備えており、孔の中心から鉛直に１ｍｍ径のＳＵＳ３１６Ｌ製ワイヤ４４を重合器下部の液溜まで垂らしてあり、落下する高さは８ｍである。
【００４４】
撹拌槽型第１重合器３は、反応温度１８０℃、反応圧力常圧、シール窒素ガス流量１リットル／ｈｒの条件である。撹拌槽型第１重合器３に、充分に脱気したビスフェノールＡと上記ジフェニルカーボネート（対ビスフェノールＡモル比１．１０）を８０ｋｇと、水酸化ナトリウム７ｍｇを仕込み５ｈｒ溶融混合し、溶融した数平均分子量３５０の溶融ポリマーを全量圧送により、移送配管７から貯槽１０に移送した。
【００４５】
貯槽１０は、常圧、１８０℃に保たれている。貯槽１０に移送された溶融ポリマーは、プランジャーポンプ１４により１０ｋｇ／ｈｒで連続に攪拌槽型第２重合器１７に供給した。攪拌槽型第１重合器３では、貯槽１０の溶融ポリマーがなくなる前に上記と同様の方法で、数平均分子量３５０の溶融ポリマーを製造し、再び貯槽１０に移送する。この後、同様にして撹拌槽型第１重合器３でバッチ的に数平均分子量３５０の溶融ポリマーを製造し、貯槽１０に供給し続けた。攪拌槽型第２重合器１７は、反応温度２３５℃、反応圧力１００ｍｍＨｇの条件であり、溶融ポリマーの液容量が２０リットルに達したら、液容量２０リットルを一定に保つように攪拌槽型第３重合器２６に数平均分子量８５０の溶融ポリマーをギアポンプにより連続に供給した。
【００４６】
攪拌槽型第３重合器２６は、反応温度２４５℃、反応圧力６ｍｍＨｇの条件であり、溶融ポリマーの液容量が２０リットルに達したら、液容量２０リットルを一定に保つように横型二軸攪拌型重合器３５に数平均分子量２３００の溶融ポリマーをギアポンプにより連続に供給した。横型二軸攪拌型重合器３５では、反応温度２７０℃、反応圧力６７Ｐａの条件であり、溶融ポリマーの液容量が１０リットルに達したら、液容量１０リットルを一定に保つようにワイヤ付多孔板型重合器４２に数平均分子量６１００の溶融ポリマーをギアポンプにより供給した。ワイヤ付多孔板型重合器４２では、反応温度２６０℃、反応圧力５３Ｐａの条件であり、重合器下部の溶融ポリマーの液容量が２０リットルに達したら、液容量２０リットルを保つように、移送配管５０を経て抜き出し口５１より数平均分子量１００００、４００ｎｍの吸光度０．００２７のカラー良好な芳香族ポリカーボネートを抜き出した。
得られた芳香族ポリカーボネートを窒素雰囲気下３８０℃で３０分間加熱した後の吸光度の増大量は０．０００５、数平均分子量の低下量は３００であり、高温でも着色しにくく、分子量低下も起こしにくかった。
【００４７】
【参考実施例２】
貯蔵条件を１４５℃、３００時間とする他は参考実施例１と同様に製造、精製、貯蔵した水分含量０．１重量ｐｐｍ、銅含量０．４重量ｐｐｍ、（ｏ−フェノキシフェニル）（フェニル）カーボネート含量０．３重量ｐｐｍのジフェニルカーボネートを用いて、実施例１と同様に芳香族ポリカーボネートを製造し、数平均分子量１００００、４００ｎｍの吸光度０．００２９のカラー良好な芳香族ポリカーボネートを得た。得られた芳香族ポリカーボネートを窒素雰囲気下３８０℃で３０分間加熱した後の吸光度の増大量は０．０００６、数平均分子量の低下量は３００であり、高温でも着色しにくく、分子量低下も起こしにくかった。
【００４８】
【参考実施例３】
貯蔵条件を１６５℃、８００時間とする他は参考実施例１と同様に製造、精製、貯蔵した水分含量０．１重量ｐｐｍ、銅含量０．４重量ｐｐｍ、（ｏ−フェノキシフェニル）（フェニル）カーボネート含量０．５重量ｐｐｍのジフェニルカーボネートを用いて、実施例１と同様に芳香族ポリカーボネートを製造し、数平均分子量１００００、４００ｎｍの吸光度０．００３５のカラー良好な芳香族ポリカーボネートを得た。得られた芳香族ポリカーボネートを窒素雰囲気下３８０℃で３０分間加熱した後の吸光度の増大量は０．０００８、数平均分子量の低下量は５００であり、高温でも着色しにくく、分子量低下も起こしにくかった。
【００４９】
【実施例４】
内壁面をフェノール洗浄処理したＳＵＳ３０４製の容器に貯蔵する他は参考実施例３と同様に製造、精製、貯蔵した水分含量０．１重量ｐｐｍ、銅含量０．４重量ｐｐｍ、（ｏ−フェノキシフェニル）（フェニル）カーボネート含量０．２重量ｐｐｍのジフェニルカーボネートを用いて、実施例１と同様に芳香族ポリカーボネートを製造し、数平均分子量１００００、４００ｎｍの吸光度０．００２８のカラー良好な芳香族ポリカーボネートを得た。得られた芳香族ポリカーボネートを窒素雰囲気下３８０℃で３０分間加熱した後の吸光度の増大量は０．０００５、数平均分子量の低下量は３００であり、高温でも着色しにくく、分子量低下も起こしにくかった。
【００５０】
【参考実施例５】
蒸留段数を３、還流比を０．８とする他は参考実施例１と同様に製造、精製、貯蔵した水分含量２０重量ｐｐｍ、銅含量０．７重量ｐｐｍ、（ｏ−フェノキシフェニル）（フェニル）カーボネート含量０．１重量ｐｐｍのジフェニルカーボネートを用いて、実施例１と同様に芳香族ポリカーボネートを製造し、数平均分子量１００００、４００ｎｍの吸光度０．００３３のカラー良好な芳香族ポリカーボネートを得た。得られた芳香族ポリカーボネートを窒素雰囲気下３８０℃で３０分間加熱した後の吸光度の増大量は０．０００９、数平均分子量の低下量は７００であり、高温でも着色しにくく、分子量低下も起こしにくかった。
【００５１】
【参考実施例６】
蒸留段数を３、還流比を０．１とする他は参考実施例１と同様に製造、精製、貯蔵した、水分含量１５０重量ｐｐｍ、銅含量０．９重量ｐｐｍ、（ｏ−フェノキシフェニル）（フェニル）カーボネート含量０．１重量ｐｐｍのジフェニルカーボネートを用いて、実施例１と同様に芳香族ポリカーボネートを製造し、数平均分子量１００００、４００ｎｍの吸光度０．００３８のカラー良好な芳香族ポリカーボネートを得た。得られた芳香族ポリカーボネートを窒素雰囲気下３８０℃で３０分間加熱した後の吸光度の増大量は０．００１３、数平均分子量の低下量は９００であり、高温でも着色しにくく、分子量低下も起こしにくかった。
【００５２】
【参考実施例７】
酸素０．５容量％、窒素９９．５容量％の雰囲気下で貯蔵する他は、参考実施例１と同様に製造、精製、貯蔵した水分含量０．１重量ｐｐｍ、銅含量０．４重量ｐｐｍ、（ｏ−フェノキシフェニル）（フェニル）カーボネート含量０．９重量ｐｐｍのジフェニルカーボネートを用いて、実施例１と同様に芳香族ポリカーボネートを製造し、数平均分子量１００００、４００ｎｍの吸光度０．００４のわずかに着色した芳香族ポリカーボネートを得た。得られた芳香族ポリカーボネートを窒素雰囲気下３８０℃で３０分間加熱した後の吸光度の増大量は０．００２、数平均分子量の低下量は９００であり、高温で着色しにくく、分子量低下も起こしにくかった。
【００５３】
【比較例１】
蒸留精製しない他は参考実施例１と同様に製造、貯蔵した水分２５０重量ｐｐｍ、銅含量１．５重量ｐｐｍ、（ｏ−フェノキシフェニル）（フェニル）カーボネート含量０．１重量ｐｐｍのジフェニルカーボネートを用いて、実施例１と同様に芳香族ポリカーボネートを製造し、数平均分子量１００００、４００ｎｍの吸光度０．００４９の着色した芳香族ポリカーボネートを得た。得られた芳香族ポリカーボネートを窒素雰囲気下３８０℃で３０分間加熱した後の吸光度の増大量は０．００３７、数平均分子量の低下量は１５００であり、高温で着色しやすく、分子量低下も大きかった。
【００５４】
【比較例２】
酸素２容量％、窒素９８容量％の雰囲気下で貯蔵する他は、参考実施例１と同様に製造、精製、貯蔵した水分含量０．１重量ｐｐｍ、銅含量０．４重量ｐｐｍ、（ｏ−フェノキシフェニル）（フェニル）カーボネート含量１．２重量ｐｐｍのジフェニルカーボネートを用いて、実施例１と同様に芳香族ポリカーボネートを製造し、数平均分子量１００００、４００ｎｍの吸光度０．００５９の着色した芳香族ポリカーボネートを得た。得られた芳香族ポリカーボネートを窒素雰囲気下３８０℃で３０分間加熱した後の吸光度の増大量は０．００４４、数平均分子量の低下量は１４００であり、高温で着色し易く、分子量低下も大きかった。
【００５５】
【発明の効果】
本発明により、カラーが良好で、かつ３８０℃以上の高温でも着色が少なく、分子量低下も小さい高品質な芳香族ポリカーボネートを工業的に好ましい方法で製造することができる。
【図面の簡単な説明】
【図１】本発明の芳香族ポリカーボネートの製造プロセスの一例を示すフロー図である。
【符号の説明】
１：原料供給口
２、９、１９、２８、３６、４６：ベント口
３：攪拌槽型第１重合器
４、１８、２７、３９：攪拌軸
５、１１、２０、２９、４７：溶融ポリマー
６、１２、２１、３０、３７、４８：排出口
７、１３、１５、２４、３３、４０、５０：移送配管
８、１６、２５、３４、４１：供給口
１０：貯槽
１４、２３、３２、３８、４９：移送ポンプ
１７：攪拌槽型第２重合器
２２、３１、４５：ガス供給口
２６：攪拌槽型第３重合器
３５：横型二軸攪拌型重合器
４２：ワイヤ付多孔板型重合器
４３：多孔板
４４：ワイヤ
５１：製品排出口[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a method for producing an aromatic polycarbonate.
[0002]
[Prior art]
In recent years, aromatic polycarbonate has been widely used in many fields as engineering plastics excellent in heat resistance, impact resistance, transparency and the like. However, polycarbonates produced by the phosgene method that has been used in the past contain toxic phosgene during production, and contain residual methylene chloride that affects the thermal stability of the polycarbonate and mold corrosion during molding. In recent years, polycarbonate obtained by the transesterification method has been reviewed.
[0003]
Since transesterification polycarbonate generally has poor color, it has long been required to improve coloring. However, if the color at the time of polycarbonate production is good, it cannot be said that the quality as a molding material is satisfied. Among polycarbonates, aromatic polycarbonate is inferior in molding fluidity, so a good molding appearance is required. In applications as molding materials for injection molding and molding materials for molded products that require high transparency, they are generally molded at a higher temperature than ordinary resins. The use as a required molding material for precision molded products is expanding, and there has been a strong demand for aromatic polycarbonates that are less colored even when molded at high temperatures. In optical disc applications that require high cycle performance of molding, since molding is performed at a particularly high temperature, there are problems such as coloring of the resin at the time of molding interruption such as mold cleaning, or causing a decrease in molecular weight. .
[0004]
In other words, there has been a strong demand for aromatic polycarbonates that are less colored even at a high temperature of 380 ° C. or more and have a small molecular weight reduction.
When an aromatic polycarbonate is produced by polymerizing in an molten state from an aromatic dihydroxy compound and diaryl carbonate by a transesterification method, an application that specifies the abundance in a raw material of a specific compound from the viewpoint of improving the coloring of the product is Many have been made.
[0005]
For example, in JP-A-5-262872, the chlorine content based on chloroformate as an impurity contained in the carbonic acid diester is 30 ppm or less, and in JP-A-6-179744, phenyl salicylate, o- It contains substantially no phenoxybenzoic acid and phenyl o-phenoxybenzoate, JP-A-7-33866 uses a carbonic acid diaryl ester whose benzophenone derivative is 100 ppm or less, JP-A-7-62074, Use of a diaryl carbonate having an ester derivative of 100 ppm or less, JP-A-8-59815 uses diphenyl carbonate substantially free of phenyl o-methoxybenzoate and xanthone, European Patent (EP) In 0677545A1 discloses, salicylic acid derivatives, stannous ion, or the like using a carbonic acid diester without the one of methyl phenyl carbonate, defines the abundance of a particular compound in the diaryl carbonate.
[0006]
In JP-A-8-104747, the amount of the aromatic dihydroxy compound having a specific structure is from 10 ppm to 3 wt%. In JP-A-8-104748, a specific bisphenol A derivative, bisphenol is present. The use of bisphenol A having a total content of A isomer, chroman organic compound and trisphenol I of 100 ppm or more and 1000 ppm or less, in JP-A-11-310630, the content of chroman organic compound is 200 ppm or less, and The use of bisphenol A having an iron content of 0.1 ppm or less defines the abundance of a specific compound in the aromatic dihydroxy compound.
However, these inventions are not always sufficient for improving the color, and it has not been possible to provide an aromatic polycarbonate with little coloration and low molecular weight reduction even at a high temperature of 380 ° C. or higher.
[0007]
[Problems to be solved by the invention]
The object of the present invention is industrially preferable for producing a high-quality aromatic polycarbonate having a good color, little coloration even at a high temperature of 380 ° C. or more, and low molecular weight reduction when producing an aromatic polycarbonate by the melt polycondensation method. It is to provide a manufacturing method.
[0008]
[Means for Solving the Problems]
As a result of diligent investigations to solve the above problems, the present inventors achieved the object by controlling the specific component content in the diaryl carbonate to a specific range when producing the aromatic polycarbonate. I found what I could do and came to complete this invention.
[0009]
That is, the present invention
(1) In the method for producing an aromatic polycarbonate polymerized in a molten state from an aromatic dihydroxy compound and diaryl carbonate, the diaryl carbonate has (a) a moisture content of 200 ppm by weight or less, and (b) a copper content. 1 wt ppm or less, (c) (o-phenoxyphenyl) (phenyl) carbonate content is 1 wt ppm or less , and the wetted part of the inner wall surface is a stainless steel container that has been cleaned with phenol. A process for producing an aromatic polycarbonate, characterized in that it is a diaryl carbonate stored in a molten state at a temperature of 80 to 190 ° C. under an atmosphere ,
It is.
[0010]
When an aromatic polycarbonate is produced by a melt polymerization method, the raw material diaryl carbonate is usually not 100% pure, and various compounds derived from the production method of the diaryl carbonate or the storage method of the produced diaryl carbonate Contains. Diaryl carbonate is rarely used immediately after production, and is used after transportation and storage. Therefore, to clarify the influence of compounds mixed or generated during storage, industrial production of aromatic polycarbonate It is especially important to do.
[0011]
As a result of intensive studies by the present inventors, moisture mixed by moisture absorption, copper which is a catalyst component used when producing diaryl carbonate, and diaryl carbonate produced when stored in a molten state (o-phenoxyphenyl) ( By making the content of (phenyl) carbonate all below a specified value, the color of the aromatic polycarbonate that is a product is surprisingly improved, and the stability against coloring and molecular weight reduction at a high temperature of 380 ° C. or higher is achieved. It became clear that it was significantly improved.
[0012]
The present invention is described in detail below.
In the present invention, the aromatic dihydroxy compound is a compound represented by HO—Ar—OH (wherein Ar represents a divalent aromatic group).
The aromatic group Ar is preferably, for example, —Ar ¹ —Y—Ar ² — (wherein Ar ¹ and Ar ² are each independently a divalent carbocyclic or heterocyclic group having 5 to 70 carbon atoms. Represents a aromatic group, and Y represents a divalent substituted or unsubstituted alkane group having 1 to 30 carbon atoms.
[0013]
In the divalent aromatic groups Ar ¹ and Ar ² , one or more hydrogen atoms are other substituents that do not adversely influence the reaction, such as halogen atoms, alkyl groups having 1 to 10 carbon atoms, It may be substituted with 10 alkoxy groups, phenyl group, phenoxy group, vinyl group, cyano group, ester group, amide group, nitro group or the like.
Preferable specific examples of the heterocyclic aromatic group include aromatic groups having one or more ring-constituting nitrogen atoms, oxygen atoms or sulfur atoms.
The divalent aromatic groups Ar ¹ and Ar ² represent groups such as substituted or unsubstituted phenylene, substituted or unsubstituted biphenylene, substituted or unsubstituted pyridylene, and the like. The substituents here are as described above.
The divalent alkane group Y is, for example, an organic group represented by the following chemical formula 1.
[0014]
[Chemical 1]

[0015]
(Wherein R ¹ , R 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 10 carbon atoms, or a cycloalkyl having 5 to 10 ring carbon atoms. Group, a C5-C10 carbocyclic aromatic group, a C6-C10 carbocyclic aralkyl group, k represents an integer of 3 to 11, and R ⁵ and R ⁶ represent each X Independently selected from each other, each independently represents hydrogen or an alkyl group having 1 to 6 carbon atoms, X represents carbon, and R ¹ , R ² , R ³ , R ⁴ , R ⁵ , R ⁶ In the range where one or more hydrogen atoms do not adversely affect the reaction, for example, a halogen atom, an alkyl group having 1 to 10 carbon atoms, an alkoxy group having 1 to 10 carbon atoms, a phenyl group, a phenoxy group, vinyl Substituted by a group, cyano group, ester group, amide group, nitro group, etc. It may be.)
Examples of such a divalent aromatic group Ar include those shown in Chemical Formula 2 below.
[0016]
[Chemical 2]

[0017]
(Wherein R ⁷ and R ⁸ are each independently a hydrogen atom, a halogen atom, an alkyl group having 1 to 10 carbon atoms, an alkoxy group having 1 to 10 carbon atoms, a cycloalkyl group having 5 to 10 ring carbon atoms, or A phenyl group, m and n are integers of 1 to 4, and 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.)
Furthermore, the divalent aromatic group Ar is —Ar ¹ —Z—Ar ² — (wherein Ar ¹ and Ar ² are as defined above, Z is a single bond or —O—, —CO—, —S Represents a divalent group such as —, —SO ₂ —, —SO—, —COO—, —CON (R ¹ ) —, where R ¹ is as defined above. Also good.
Examples of such a divalent aromatic group Ar include those shown in Chemical Formula 3 below.
[0018]
[Chemical 3]

(Wherein R ⁷ , R ⁸ , m and n are as described above.)
[0019]
Furthermore, specific examples of the divalent aromatic group Ar include substituted or unsubstituted phenylene, substituted or unsubstituted naphthylene, substituted or unsubstituted pyridylene, and the like.
The aromatic dihydroxy compound used in the present invention may be a single type or two or more types. A typical example of the aromatic dihydroxy compound is bisphenol A.
[0020]
The diaryl carbonate used in the present invention is represented by the following chemical formula 4.
[Formula 4]

(In the formula, Ar ³ and Ar ⁴ each represent a monovalent aromatic group.)
[0021]
Ar ³ and Ar ⁴ represent a monovalent carbocyclic or heterocyclic aromatic group, and in Ar ³ and Ar ⁴ , one or more hydrogen atoms are other substituents that do not adversely influence the reaction. Substituted with, for example, a halogen atom, an alkyl group having 1 to 10 carbon atoms, 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, or a nitro group It may be. 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 as described above.
[0022]
Preferable examples of Ar ³ and Ar ⁴ include those shown in the following chemical formula 5, for example.
[Chemical formula 5]

[0023]
Representative examples of diaryl carbonates include substituted or unsubstituted diphenyl carbonates represented by the following chemical formula (6).
[Chemical 6]

(In the formula, R ⁹ and R ¹⁰ each independently represent a hydrogen atom, an alkyl group having 1 to 10 carbon atoms, an alkoxy group having 1 to 10 carbon atoms, a cycloalkyl group having 5 to 10 ring carbon atoms, or a phenyl group. P and q are integers of 1 to 5, and when p is 2 or more, each R ⁹ may be different, and when q is 2 or more, each R ¹⁰ is Each may be different.)
[0024]
Among these diphenyl carbonates, preferred are symmetric diaryl carbonates such as unsubstituted diphenyl carbonate, lower alkyl-substituted diphenyl carbonates such as ditolyl carbonate and di-t-butylphenyl carbonate, and the most simple structure. Unsubstituted diphenyl carbonate which is a diaryl carbonate is preferred.
These diaryl carbonates may be used alone or in combination of two or more.
[0025]
In the present invention, the water content in the diaryl carbonate is 200 ppm by weight or less. When the water content is higher than 200 ppm by weight, the color of the product aromatic polycarbonate is deteriorated, and it becomes easy to be colored at a high temperature of 380 ° C. or higher, and the molecular weight is greatly reduced. Although the reason for this is not clear, it is presumed that the stability of aromatic polycarbonate at high temperatures is adversely affected by a combination of decomposition of diaryl carbonate due to the presence of moisture and isomerization reaction of diaryl carbonate. The water content in the diaryl carbonate is preferably 100 ppm by weight or less, more preferably 50 ppm by weight or less. The lower limit of the amount of water is not particularly limited, and the amount of water may be less than 0.01 ppm by weight. However, even if the amount is less than 0.01 ppm by weight, the aromatic polycarbonate may be colored or lowered in molecular weight at high temperatures. There is little improvement effect.
As a method for controlling the water content in the diaryl carbonate within the above range, a method for avoiding moisture absorption during transportation or storage, or when moisture content is higher than the upper limit of 200 ppm by weight, dehydration by distillation or the like. Examples of the method used for the polymerization of the aromatic polycarbonate after the operation are given.
[0026]
In the present invention, the copper content in the diaryl carbonate is 1 ppm by weight or less. When the copper content is more than 1 ppm by weight, the color of the product aromatic polycarbonate is deteriorated, and it becomes easy to be colored at a high temperature of 380 ° C. or higher, and the molecular weight is greatly lowered.
The reason for this is not clear, but it is presumed that the presence of copper acts catalytically on the coloring reaction and molecular weight reduction reaction of aromatic polycarbonate at high temperatures. The copper content in the diaryl carbonate is preferably 0.5 ppm by weight or less, more preferably 0.1 ppm by weight or less. The lower limit of the copper content is not particularly limited, and the copper content may be less than 0.001 ppm by weight. However, the aromatic polycarbonate may be colored at a high temperature even if the copper content is less than 0.001 ppm by weight. And the effect of improving molecular weight reduction is small.
[0027]
As a method for controlling the copper content within the above range, when producing diaryl carbonate, the copper content is reduced by distillation operation, washing operation, etc. either after using copper catalyst or after producing diaryl carbonate using copper catalyst. And the like. However, when the diaryl carbonate is produced without using any copper catalyst, it is preferable that no other catalyst component that deteriorates the quality of the product polycarbonate is contained in the diaryl carbonate.
[0028]
In the present invention, the (o-phenoxyphenyl) (phenyl) carbonate content in the diaryl carbonate is 1 ppm by weight or less. When the content of (o-phenoxyphenyl) (phenyl) carbonate is more than 1 ppm by weight, the color of the product aromatic polycarbonate is deteriorated and it is easy to be colored at a high temperature of 380 ° C. or higher.
The reason for this is not clear, but (o-phenoxyphenyl) (phenyl) carbonate itself or a reaction product of (o-phenoxyphenyl) (phenyl) carbonate and aromatic polycarbonate is presumed to be easily colored at high temperature. ing. The (o-phenoxyphenyl) (phenyl) carbonate content in the diaryl carbonate is preferably 0.5 ppm by weight or less, more preferably 0.1 ppm by weight or less. The lower limit of the (o-phenoxyphenyl) (phenyl) carbonate content is not particularly limited, and the (o-phenoxyphenyl) (phenyl) carbonate content may be less than 0.01 ppm by weight. Even if the content of (o-phenoxyphenyl) (phenyl) carbonate is less than ppm, the effect of improving the coloration of the aromatic polycarbonate at high temperature is small.
[0029]
In producing an aromatic polycarbonate from an aromatic dihydroxy compound and a diaryl carbonate, the diaryl carbonate is usually used after being stored in a molten state in order to handle the diaryl carbonate industrially preferably. In the present invention, the diaryl carbonate is preferably stored in a molten state at a temperature of 80 to 190 ° C. in a nitrogen atmosphere in a stainless steel container. When the container to store is carbon steel, the production amount of (o-phenoxyphenyl) (phenyl) carbonate may increase.
[0030]
Stainless steel is a martensitic, ferritic, and austenitic material containing 10 to 30% by weight of normal chromium as defined and classified in stainless steel handbook pages 13 to 21 (published by Nikkan Kogyo Shimbun, 5th edition). Examples thereof include stainless steels such as ferrite and austenite, and Fe-based superalloys as shown in the table on page 547 of the stainless steel manual. Specific examples include SUS201, SUS202, SUS304, SUS304L, SUS316, SUS316L, SUS347, SUS405, SUS430, SUS403, SUS410, SUS431, SUS440C, SUS630, Incoloy 800, Incoloy 801, Incoloy 802, Incoloy 807, Incoloy 807, Incoloy 807, W545, V57, W545, D979, CG27, S590, etc. are mentioned. Preferable specific examples include SUS304, SUS304L, SUS316, SUS316L and the like, and particularly preferably SUS304.
[0031]
The wetted part of the inner wall surface of the stainless steel container is preferably one that has been washed with phenol. When a stainless steel container that has been washed with phenol is used, the amount of (o-phenoxyphenyl) (phenyl) carbonate produced can be reduced. The reason for this is not clear, but it is presumed that the formation of (o-phenoxyphenyl) (phenyl) carbonate is prevented by removing the adsorbed oxygen on the stainless steel surface with phenol.
[0032]
Moreover, it is preferable to store in a nitrogen atmosphere, and when air is mixed into the storage container, the amount of (o-phenoxyphenyl) (phenyl) carbonate produced increases. The storage temperature is preferably in the range of 80 to 190 ° C. When the storage temperature is higher than 190 ° C, the amount of (o-phenoxyphenyl) (phenyl) carbonate produced tends to increase. When it is lower than 80 ° C., it is not preferable because it solidifies depending on the kind of diaryl carbonate. A more preferable storage temperature range is 85 to 160 ° C, and further preferably 90 to 140 ° C.
[0033]
When the aromatic polycarbonate is produced in the present invention, the use ratio (preparation ratio) of the aromatic dihydroxy compound and diaryl carbonate varies depending on the type of the aromatic dihydroxy compound and diaryl carbonate used, the polymerization temperature, and other polymerization conditions. The diaryl carbonate is usually used in a proportion of 0.9 to 2.5 mol, preferably 0.95 to 2.0 mol, more preferably 0.98 to 1.5 mol, relative to 1 mol of the aromatic dihydroxy compound. It is done.
The number average molecular weight of the aromatic polycarbonate obtained by the method of the present invention is usually in the range of 5,000 to 100,000, preferably 5,000 to 30,000.
[0034]
The process for producing an aromatic polycarbonate of the present invention comprises the above-mentioned aromatic dihydroxy compound and diaryl carbonate in a molten state with heating in a vacuum and / or an inert gas flow in the presence or absence of a catalyst. In this method, polycondensation is performed by transesterification, and the polymerization vessel is not particularly limited. For example, stirring tank type reactor, thin film reactor, centrifugal thin film evaporation reactor, surface renewal type biaxial kneading reactor, biaxial horizontal type stirring reactor, wet wall type reactor, perforated plate type that polymerizes while freely falling A reactor, a perforated plate reactor with a wire that is polymerized while being dropped along a wire, or the like, and a polymerization vessel in which these are used alone or in combination are used. The polymerization can be performed either batchwise or continuously. Moreover, it is also a preferable method to use an extruder, a polymer mixer, etc. in combination with a polymerizer as an apparatus for adding stabilizers, additives and the like while the aromatic polycarbonate is in a molten state after polymerization. There are no particular restrictions on the material of these polymerization vessels, and it is usually selected from stainless steel, nickel, glass lining and the like.
[0035]
In the present invention, in producing an aromatic polycarbonate by reacting an aromatic dihydroxy compound and diaryl carbonate, the reaction temperature is usually selected in the range of 50 to 350 ° C, preferably 100 to 300 ° C.
As the reaction proceeds, an aromatic monohydroxy compound is produced, and the reaction rate can be increased by removing this from the reaction system. Therefore, an inert gas that does not adversely influence the reaction, such as nitrogen, argon, helium, carbon dioxide, and lower hydrocarbon gas, is introduced, and the generated aromatic monohydroxy compound is accompanied by these gases and removed. And a method of reacting under reduced pressure are preferably used. The preferable reaction pressure varies depending on the molecular weight, and is preferably in the range of 10 mmHg to normal pressure in the initial stage of polymerization.
[0036]
The melt polycondensation reaction can be carried out without adding a catalyst, but is carried out in the presence of a catalyst as necessary in order to increase the polymerization rate. The polymerization catalyst is not particularly limited as long as it is used in this field, but alkali metal or alkaline earth metal hydroxides such as lithium hydroxide, sodium hydroxide, potassium hydroxide, and calcium hydroxide. Alkali metal salts, alkaline earth metal salts, quaternary ammonium salts of boron hydrides such as sodium borohydride and tetramethylammonium borohydride; alkalis such as lithium hydride, sodium hydride and calcium hydride Metal or alkaline earth metal hydrides;
[0037]
Alkali metal or alkaline earth metal alkoxides such as lithium methoxide, sodium ethoxide, calcium methoxide; lithium phenoxide, sodium phenoxide, magnesium phenoxide, LiO-Ar-OLi, NaO-Ar-ONa (Ar is an aryl group) Alkali metal or alkaline earth metal aryloxides such as: Lithium acetate, calcium acetate, organic acid salts of alkaline earth metals such as sodium benzoate; Zinc compounds such as zinc oxide, zinc acetate, zinc phenoxide; Boron oxide, boric acid, sodium borate, trimethyl borate, tributyl borate, triphenyl borate, ammonium borate represented by (R ¹ R ² R ³ R ⁴ ) NB (R ¹ R ² R ³ R ⁴ ) ^{s, (R 1 R 2 R 3} R 4) P ^{(R 1 R 2 R 3 R} 4) phosphonium borates represented by ^{(. R 1, R 2,} R 3, R 4 is an explanatory as the Formula 1) compounds of boron and the like;
[0038]
Silicon compounds such as silicon oxide, sodium silicate, tetraalkyl silicon, tetraaryl silicon, diphenyl-ethyl-ethoxy silicon; germanium compounds such as germanium oxide, germanium tetrachloride, germanium ethoxide, germanium phenoxide; tin oxide , Dialkyltin oxide, dialkyltin carboxylate, tin compounds such as tin compounds bonded with alkoxy groups or aryloxy groups such as tin acetate and ethyltin tributoxide, organotin compounds; lead oxide, lead acetate, lead carbonate, base Lead compounds such as alkaline carbonates, lead and organic lead alkoxides or aryloxides; onium compounds such as quaternary ammonium salts, quaternary phosphonium salts, quaternary arsonium salts; antimony oxide, antimony acetate Antimony compounds; manganese compounds such as manganese acetate, manganese carbonate, manganese borate; and catalysts such as zirconium acetate, zirconium oxide, zirconium alkoxides or aryloxides, zirconium compounds such as zirconium acetylacetone. .
[0039]
When using a catalyst, these catalysts may be used alone or in combination of two or more. The amount of these catalysts used is usually selected in the range of 10 ^-8 to 1 part by weight, preferably 10 ^-7 to 10 ^-1 part by weight, based on 100 parts by weight of the starting aromatic dihydroxy compound.
[0040]
DETAILED DESCRIPTION OF THE INVENTION
Hereinafter, the present invention will be described in more detail with reference to embodiments of the present invention.
Moisture: analyzed by Karl Fischer method.
Copper content: analyzed using ICP (high frequency inductively coupled plasma emission analyzer; JY38PII manufactured by Seiko Electronics Co., Ltd.).
-(O-phenoxyphenyl) (phenyl) carbonate content: analyzed by gas chromatography.
Coloring: A solution obtained by dissolving 1 g of a sample in 7 ml of methylene chloride was placed in a cell having an optical path length of 1 cm, and the absorbance at 400 nm was measured with a spectrophotometer to obtain a coloring index.
[0041]
Easiness of coloring at high temperature: An aromatic polycarbonate was heated at 380 ° C. for 30 minutes in a nitrogen atmosphere, and evaluated by the increase in absorbance at 400 nm due to heating.
Number average molecular weight (Mn): measured by gel permeation chromatography (GPC) {column: TSK-GEL, manufactured by Tosoh Corporation} using tetrahydrofuran as a solvent, and obtained using standard monodisperse polystyrene It calculated | required using the conversion molecular weight calibration curve by a type | formula.
M _PC = 0.3591M _PS ^1.0388
(Wherein, M _PC molecular weight of the aromatic polycarbonate, M _PS represents the molecular weight of the polystyrene.)
Ease of molecular weight reduction at high temperature: Aromatic polycarbonate was heated at 380 ° C. for 30 minutes in a nitrogen atmosphere, and the number average molecular weight decreased by heating was evaluated.
[0042]
[ Reference Example 1 ]
After diphenyl carbonate is produced from dimethyl carbonate and phenol using diphenoxy copper as a catalyst, it is distilled and purified by side-cutting in the second gas phase from the top of the column under conditions of pressure 1596 Pa, number of distillation stages 5 and reflux ratio 3.2. And stored in a SUS304 container at 110 ° C. for 100 hours under a nitrogen atmosphere. The water content in the diphenyl carbonate after storage was 0.1 ppm by weight, the copper content was 0.4 ppm by weight, and the (o-phenoxyphenyl) (phenyl) carbonate content was 0.1 ppm by weight. Using the diphenyl carbonate, an aromatic polycarbonate was produced by a process as shown in FIG.
[0043]
The stirred tank type polymerizer 3 was operated batchwise, and the storage tank 10 and subsequent tanks were operated continuously. All of the stirring tank type polymerizers 3 (capacity 200 liters), 17 (capacity 50 liters) and 26 (capacity 50 liters) are provided with stirring blades. The horizontal biaxial stirring type polymerizer 35 (capacity 30 liters) has biaxial stirring blades with L / D = 6 and a rotating diameter of 140 mm. The perforated plate type polymerizer 42 with a wire is provided with a perforated plate 43 having 50 holes with a diameter of 5 mm, and a SUS316L wire 44 with a diameter of 1 mm is vertically suspended from the center of the hole to a liquid reservoir at the bottom of the polymerizer. The falling height is 8 m.
[0044]
The stirring tank type first polymerization vessel 3 is under the conditions of a reaction temperature of 180 ° C., a reaction pressure and a normal pressure, and a seal nitrogen gas flow rate of 1 liter / hr. The stirred tank type first polymerization vessel 3 was charged with 80 kg of sufficiently degassed bisphenol A and diphenyl carbonate (molar ratio of bisphenol A 1.10) and 7 mg of sodium hydroxide, melted and mixed for 5 hours, and melted number average The molten polymer having a molecular weight of 350 was transferred from the transfer pipe 7 to the storage tank 10 by pumping the whole amount.
[0045]
The storage tank 10 is maintained at normal pressure and 180 ° C. The molten polymer transferred to the storage tank 10 was continuously supplied to the stirring tank type second polymerization device 17 by the plunger pump 14 at 10 kg / hr. In the stirring tank type first polymerization vessel 3, a molten polymer having a number average molecular weight of 350 is produced by the same method as described above before the molten polymer in the storage tank 10 runs out, and is transferred to the storage tank 10 again. Thereafter, in the same manner, a molten polymer having a number average molecular weight of 350 was batch-produced in the stirred tank type first polymerization vessel 3 and continuously supplied to the storage tank 10. The stirring tank type second polymerization vessel 17 is under the conditions of a reaction temperature of 235 ° C. and a reaction pressure of 100 mmHg. When the liquid volume of the molten polymer reaches 20 liters, the stirring tank type second polymerization vessel 17 is maintained so as to keep the liquid volume of 20 liters constant. A molten polymer having a number average molecular weight of 850 was continuously fed to the polymerization vessel 26 by a gear pump.
[0046]
The stirring tank type third polymerization vessel 26 is under the conditions of a reaction temperature of 245 ° C. and a reaction pressure of 6 mmHg. When the liquid volume of the molten polymer reaches 20 liters, a horizontal biaxial stirring type is used to keep the liquid volume of 20 liters constant. A molten polymer having a number average molecular weight of 2300 was continuously supplied to the polymerization vessel 35 by a gear pump. In the horizontal biaxial agitation type polymerizer 35, the reaction temperature is 270 ° C. and the reaction pressure is 67 Pa. When the liquid volume of the molten polymer reaches 10 liters, the perforated plate type with wire is used to keep the liquid volume 10 liters constant. A melt polymer having a number average molecular weight of 6100 was supplied to the polymerization vessel 42 by a gear pump. In the perforated plate polymerizer 42 with wire, the reaction temperature is 260 ° C. and the reaction pressure is 53 Pa. When the liquid volume of the molten polymer in the lower part of the polymerizer reaches 20 liters, the transfer pipe is maintained so as to keep the liquid volume 20 liters. After 50, an aromatic polycarbonate having a number average molecular weight of 10,000 and a light absorbency of 0.0027 at 400 nm was extracted from the extraction port 51.
After the aromatic polycarbonate obtained is heated at 380 ° C. for 30 minutes in a nitrogen atmosphere, the amount of increase in absorbance is 0.0005, the amount of decrease in number average molecular weight is 300, it is difficult to color even at high temperatures, and the molecular weight is unlikely to decrease. It was.
[0047]
[ Reference Example 2 ]
Manufactured, purified and stored in the same manner as in Reference Example 1 except that the storage conditions were 145 ° C. and 300 hours, the water content was 0.1 wt ppm, the copper content was 0.4 wt ppm, (o-phenoxyphenyl) (phenyl) Using diphenyl carbonate having a carbonate content of 0.3 ppm by weight, an aromatic polycarbonate was produced in the same manner as in Example 1 to obtain an aromatic polycarbonate having a number average molecular weight of 10000, a 400 nm absorbance of 0.0029 and good color. After the aromatic polycarbonate obtained is heated at 380 ° C. for 30 minutes in a nitrogen atmosphere, the amount of increase in absorbance is 0.0006, the amount of decrease in number average molecular weight is 300, and it is difficult to color even at high temperatures and the molecular weight is not easily lowered. It was.
[0048]
[ Reference Example 3 ]
Manufactured, purified and stored in the same manner as in Example 1 except that the storage conditions were 165 ° C. and 800 hours, the water content was 0.1 wt ppm, the copper content was 0.4 wt ppm, (o-phenoxyphenyl) (phenyl) Using diphenyl carbonate having a carbonate content of 0.5 ppm by weight, an aromatic polycarbonate was produced in the same manner as in Example 1 to obtain an aromatic polycarbonate having a number average molecular weight of 10,000 and a 400 nm absorbance of 0.0035 and good color. After the aromatic polycarbonate obtained is heated at 380 ° C. for 30 minutes in a nitrogen atmosphere, the increase in absorbance is 0.0008, the decrease in number average molecular weight is 500, it is difficult to color even at high temperatures, and the molecular weight is unlikely to decrease. It was.
[0049]
[Example 4]
A water content of 0.1 wt ppm, a copper content of 0.4 wt ppm, (o-phenoxyphenyl) produced, purified, and stored in the same manner as in Reference Example 3 except that the inner wall surface was stored in a SUS304 container that had been phenol-cleaned. ) (Phenyl) carbonate Using diphenyl carbonate having a content of 0.2 ppm by weight, an aromatic polycarbonate was produced in the same manner as in Example 1, and an aromatic polycarbonate having a number average molecular weight of 10,000, 400 nm and an absorbance of 0.0028 was obtained. Obtained. After the aromatic polycarbonate obtained is heated at 380 ° C. for 30 minutes in a nitrogen atmosphere, the amount of increase in absorbance is 0.0005, the amount of decrease in number average molecular weight is 300, it is difficult to color even at high temperatures, and the molecular weight is unlikely to decrease. It was.
[0050]
[ Reference Example 5 ]
A water content of 20 ppm by weight, a copper content of 0.7 ppm by weight, (o-phenoxyphenyl) (phenyl) produced, purified and stored in the same manner as in Reference Example 1 except that the number of distillation stages was 3 and the reflux ratio was 0.8. A) An aromatic polycarbonate was produced in the same manner as in Example 1 by using diphenyl carbonate having a carbonate content of 0.1 ppm by weight to obtain an aromatic polycarbonate having a number average molecular weight of 10000 and a 400 nm absorbance of 0.0033 and good color. The amount of increase in absorbance after heating the obtained aromatic polycarbonate at 380 ° C. for 30 minutes in a nitrogen atmosphere is 0.0009, the amount of decrease in number average molecular weight is 700, it is difficult to color even at high temperatures, and it is difficult to cause a decrease in molecular weight. It was.
[0051]
[ Reference Example 6 ]
Manufactured, purified and stored in the same manner as in Reference Example 1 except that the number of distillation stages was 3 and the reflux ratio was 0.1, the water content was 150 ppm by weight, the copper content was 0.9 ppm by weight, (o-phenoxyphenyl) ( An aromatic polycarbonate was produced in the same manner as in Example 1 by using diphenyl carbonate having a phenyl) carbonate content of 0.1 ppm by weight to obtain an aromatic polycarbonate having a number average molecular weight of 10000, a 400 nm absorbance of 0.0038, and good color. . The amount of increase in absorbance after heating the obtained aromatic polycarbonate at 380 ° C. for 30 minutes in a nitrogen atmosphere is 0.0013, the amount of decrease in number average molecular weight is 900, and it is difficult to color even at high temperatures, and it is difficult to cause a decrease in molecular weight. It was.
[0052]
[ Reference Example 7 ]
Except for storing in an atmosphere of 0.5 volume% oxygen and 99.5 volume% nitrogen, the water content produced, purified and stored in the same manner as in Reference Example 1 was 0.1 ppm by weight, and the copper content was 0.4 ppm by weight. , (O-phenoxyphenyl) (phenyl) carbonate Using diphenyl carbonate having a content of 0.9 ppm by weight, an aromatic polycarbonate was produced in the same manner as in Example 1. The number average molecular weight was 10,000, and the absorbance at 400 nm was a slight 0.004. A colored aromatic polycarbonate was obtained. After the aromatic polycarbonate obtained is heated at 380 ° C. for 30 minutes in a nitrogen atmosphere, the amount of increase in absorbance is 0.002, the amount of decrease in number average molecular weight is 900, it is difficult to color at high temperatures, and the molecular weight is unlikely to decrease. It was.
[0053]
[Comparative Example 1]
Except for not purifying by distillation, diphenyl carbonate having a water content of 250 ppm by weight, copper content of 1.5 ppm by weight, and (o-phenoxyphenyl) (phenyl) carbonate content of 0.1 ppm by weight was prepared and stored in the same manner as in Reference Example 1. Then, an aromatic polycarbonate was produced in the same manner as in Example 1 to obtain a colored aromatic polycarbonate having a number average molecular weight of 10,000 and an absorbance of 0.0049 at 400 nm. The amount of increase in absorbance after heating the obtained aromatic polycarbonate at 380 ° C. for 30 minutes in a nitrogen atmosphere was 0.0037, the amount of decrease in number average molecular weight was 1500, and it was easy to color at high temperatures, and the decrease in molecular weight was also large. .
[0054]
[Comparative Example 2]
Oxygen 2 volume%, in addition to stored under an atmosphere of 98 volume% nitrogen, prepared as in Reference Example 1, purification, storage and moisture content 0.1 wt ppm, copper content 0.4 wt ppm, (o- Aromatic polycarbonate was produced in the same manner as in Example 1 using diphenyl carbonate having a phenoxyphenyl) (phenyl) carbonate content of 1.2 ppm by weight, and a colored aromatic polycarbonate having a number average molecular weight of 10,000 and a absorbance of 0.0059 at 400 nm. Got. After the aromatic polycarbonate obtained was heated at 380 ° C. for 30 minutes in a nitrogen atmosphere, the increase in absorbance was 0.0044, the decrease in number average molecular weight was 1400, and it was easily colored at high temperatures, and the decrease in molecular weight was also large. .
[0055]
【The invention's effect】
According to the present invention, a high-quality aromatic polycarbonate having a good color, little coloring even at a high temperature of 380 ° C. or more, and a small molecular weight reduction can be produced by an industrially preferable method.
[Brief description of the drawings]
FIG. 1 is a flow diagram showing an example of a process for producing an aromatic polycarbonate of the present invention.
[Explanation of symbols]
1: Raw material supply port 2, 9, 19, 28, 36, 46: Vent port 3: Stirring tank type first polymerization device 4, 18, 27, 39: Stirring shaft 5, 11, 20, 29, 47: Molten polymer 6, 12, 21, 30, 37, 48: discharge port 7, 13, 15, 24, 33, 40, 50: transfer pipe 8, 16, 25, 34, 41: supply port 10: storage tanks 14, 23, 32 38, 49: Transfer pump 17: Stirring tank type second polymerization device 22, 31, 45: Gas supply port 26: Stirring tank type third polymerization device 35: Horizontal biaxial stirring polymerization device 42: Perforated plate type with wire Polymerizer 43: Perforated plate 44: Wire 51: Product outlet

Claims (1)

In the method for producing an aromatic polycarbonate polymerized in a molten state from an aromatic dihydroxy compound and diaryl carbonate, the diaryl carbonate has (a) a moisture content of 200 ppm by weight or less, and (b) a copper content of 1 ppm by weight. (C) (o-phenoxyphenyl) (phenyl) carbonate content is 1 ppm by weight or less , and the wetted part of the inner wall surface is a stainless steel container that has been subjected to a cleaning treatment with phenol. A method for producing an aromatic polycarbonate, which is a diaryl carbonate stored in a molten state at a temperature of 80 to 190 ° C.

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