JP6668507B2 - 重合体の連続製造装置及び連続製造方法 - Google Patents
重合体の連続製造装置及び連続製造方法 Download PDFInfo
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- HNJBEVLQSNELDL-UHFFFAOYSA-N pyrrolidin-2-one Chemical compound O=C1CCCN1 HNJBEVLQSNELDL-UHFFFAOYSA-N 0.000 description 1
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- IGLNJRXAVVLDKE-UHFFFAOYSA-N rubidium atom Chemical compound [Rb] IGLNJRXAVVLDKE-UHFFFAOYSA-N 0.000 description 1
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- LXOXXUIVMOYGST-UHFFFAOYSA-M rubidium(1+);sulfanide Chemical compound [SH-].[Rb+] LXOXXUIVMOYGST-UHFFFAOYSA-M 0.000 description 1
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- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 description 1
- GNCGTEQGBYYYBX-UHFFFAOYSA-M sodium;4-methylbenzoate Chemical compound [Na+].CC1=CC=C(C([O-])=O)C=C1 GNCGTEQGBYYYBX-UHFFFAOYSA-M 0.000 description 1
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- 239000007858 starting material Substances 0.000 description 1
- 150000003460 sulfonic acids Chemical class 0.000 description 1
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Images
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Description
図1は、本発明に係る重合体連続製造装置の一実施形態(以下、「実施形態1」という。)を示す部分断面図である。以下、図1に基づき、実施形態1の構成を説明する。
図3は、本発明に係る重合体連続製造装置の別の実施形態(以下、「実施形態2」という。)を示す部分断面図である。以下、図3に基づき、実施形態2の構成及び動作を説明する。図3において、隔壁を跨ぐ右向きの点線矢印は、反応混合物の移動方向を示す。また、左向きの実線矢印は、不活性ガスの移動方向を示す。また、破線の矢印は、蒸発成分の移動方向を示す。
図4は、本発明に係る重合体連続製造装置の別の実施形態(以下、「実施形態3」という。)を示す部分断面図である。以下、図4に基づき、実施形態3の構成及び動作を説明する。
本発明の第1の態様によれば、重合体の連続製造装置であって、前記装置は、複数の反応槽を収容する収容室を備え、前記収容室には、少なくとも溶媒及びモノマーが供給され、少なくとも1つの反応槽において、前記溶媒中で前記モノマーの重合反応を行うことにより反応混合物が形成され、前記反応槽は、前記収容室における気相部を介して互いに連通し、前記反応槽は、順次接続され、前記反応混合物は、各反応槽に順次移動し、前記収容室は、少なくとも1組の隣接する反応槽の境界又はその近傍において、気相部の横断面積を狭めるバッフルを備え、前記バッフルは、前記反応混合物の移動方向の上流側に位置する反応槽から、当該バッフルを挟んで前記移動方向の下流側に隣接する反応槽内に、前記気相部を介して気体が移動するのを防ぐバッフルであることを特徴とする連続製造装置が提供される。
ポリマーの重量平均分子量(Mw)は、株式会社センシュー科学製の高温ゲルパーミエーションクロマトグラフ(GPC)SSC−7101を用いて、以下の条件で測定した。重量平均分子量はポリスチレン換算値として算出した。
溶媒: 1−クロロナフタレン、
温度: 210℃、
検出器: UV検出器(360nm)、
サンプル注入量: 200μl(濃度:0.05質量%)、
流速: 0.7ml/分、
標準ポリスチレン: 616,000、113,000、26,000、8,200、及び600の5種類の標準ポリスチレン。
ポリマーの重量平均分子量(Mw)は、日本分光製のゲルパーミエーションクロマトグラフ(GPC)EXTREMAを用いて、以下の条件で測定した。重量平均分子量はポリスチレン換算値として算出した。
溶媒: LiBr0.01M NMP溶液
温度: 40℃
検出器: RI検出器
サンプル注入量: 100μl(濃度:1mg/1ml)、
流速: 1.0ml/分、
標準ポリスチレン: 427,000、96,400、37,900、17,400、及び5,560の5種類の標準ポリスチレン。
収容室が5枚の隔壁により仕切られて形成された6個の反応槽を有し、反応混合物の上流から第5番目の反応槽と第6番目の反応槽との間の隔壁の直上の気相部にバッフルを備える以外は、図4に示すのと同様の重合体連続製造装置を用いた。この重合体連続装置において、収容室は、内径108mm×長さ300mmの寸法を有するTi製反応装置であり、隔壁は半円形であり、バッフルは、図5(a)に示されるようなドーナツ型半円形(外径108mm、内径16mm)であった。また、第5番目の反応槽と第6番目の反応槽との境界において、境界部の横断総面積から、隔壁、バッフル及び撹拌軸の横断面積を引いた面積、すなわち、気体が通過し得る開口部Xの横断総面積は2cm2であった。
気相部にドーナツ型半円形のバッフルを有しない他は実施例1と同様の装置を用いて、実施例と同様の条件でPPSの連続製造を実施した。
収容室が5枚の隔壁により仕切られて形成された6個の反応槽を有し、反応混合物の上流から第5番目の反応槽と第6番目の反応槽との間の隔壁の直上の気相部にバッフルを備える以外は、図4に示すのと同様の重合体連続製造装置を用いた。この重合体連続装置において、収容室は、内径108mm×長さ300mmの寸法を有するTi製反応装置であり、隔壁は半円形であり、バッフルは、図5(a)に示されるようなドーナツ型半円形(外径108mm、内径16mm)であった。また、第5番目の反応槽と第6番目の反応槽との境界において、境界部の横断総面積から、隔壁、バッフル及び撹拌軸の横断面積を引いた面積、すなわち、気体が通過し得る開口部Xの横断総面積は2cm2であった。
実施例2で使用した連続製造装置に、N−メチル−2−ピロリドン(NMP)950gを仕込んだ後、窒素ガスを上流側から第5番目の隔壁の下流側より0.1NL/minの流量で流しながら、収容室2の底部に設置した外部ヒーターにより上流側から1番目の隔壁と2番目の隔壁で区切られた部分、すなわち上流側から第2番目の反応槽の温度1を200℃、上流側から第4番目の反応槽の温度2を210℃、上流側から第6番目の反応槽の温度3を210℃に保持した。定常状態において、上流側から第1番目の反応槽の温度4は180℃、上流側から第5番目の反応槽の温度5は215℃であった。上流から第5番目の反応槽までは温度が順次上昇するが、第6番目の反応槽は第5番目の反応槽よりも温度が低下する条件であった。
実施例2で使用した連続製造装置に、N−メチル−2−ピロリドン(NMP)950gを仕込んだ後、窒素ガスを上流側から第5番目の隔壁の下流側より0.1NL/minの流量で流しながら、収容室の底部に設置した外部ヒーターにより上流側から1番目の隔壁と2番目の隔壁で区切られた部分、すなわち上流側から第2番目の反応槽の温度1を220℃、上流側から第5番目の反応槽の温度2を260℃、上流側から第6番目の反応槽の温度3を250℃に保持した。定常状態において、上流側から第1番目の反応槽の温度4は190℃、上流側から第4番目の反応槽の温度5は250℃であった。上流から第5番目の反応槽までは温度が順次上昇するが、第6番目の反応槽は温度が低下する条件であった。
PEEK0.1gおよび4−クロロフェノール10mLをオイルバスで180℃、20分間、加熱および撹拌して溶解させた。室温になるまで冷却したのち、該溶液3mLをo−ジクロロベンゼン7mLで希釈した。
35℃においてウベローデ粘度計で測定した。
溶媒の粘度(η0)を、オストワルド型粘度管を用いて測定した。調整した溶液の粘度(η)と溶媒の粘度(η0)から、比粘性率((η−η0)/η0)を求め、この比粘性率を、溶液の濃度(0.3g/dL)で割ることにより、還元粘度(dL/g)を求めた。
2 収容室
3、3a、3b、3c 隔壁
4 気相部
5、5a、5b 側壁
6 供給ライン
7 送気ライン
8 排気ライン
9、9a、9b、9c バッフル
10a、10b、10c 反応混合物
11 反応混合物回収ライン
12 送気部
13 回転駆動装置
14 脱水部
15 溶媒回収ライン
16 蒸気回収ライン
17 気液分離部
18 気体回収ライン
19、24 反応原料分離回収部
20 廃ガスライン
21、26 反応原料再供給ライン
22、27 反応原料再供給部
23 液体回収ライン
25 廃水ライン
28 撹拌軸
29a、29b、29c 撹拌翼
30a、30b 沈殿物
100、200、300 重合体連続製造装置
Claims (9)
- 脱塩重縮合により得られる重合体の連続製造装置であって、
前記装置は、複数の反応槽を収容する収容室を備え、
前記収容室には、少なくとも溶媒及びモノマーが供給され、
少なくとも1つの反応槽において、前記溶媒中で前記モノマーの重合反応を行うことにより反応混合物が形成され、
前記反応槽は、前記収容室における気相部を介して互いに連通し、
前記反応槽は、順次接続され、前記反応混合物は、各反応槽に順次移動し、
前記収容室は、少なくとも1組の隣接する反応槽の境界又はその近傍において、気相部の横断面積を狭めるバッフルを備え、
前記バッフルは、前記反応混合物の移動方向の上流側に位置する反応槽から、当該バッフルを挟んで前記移動方向の下流側に隣接する反応槽内に、前記気相部を介して気体が移動するのを防ぐバッフルであることを特徴とする連続製造装置。 - 隣接する前記反応槽同士は、隔壁によって隔てられ、
前記バッフルは、少なくとも1つの前記隔壁に対向する位置又はその近傍の壁面に設けられている、請求項1に記載の連続製造装置。 - 前記収容室における気相部と連通し、前記反応混合物の移動方向の下流側から上流側に向けて、前記気相部に不活性ガスを送り込む送気ラインと、
前記不活性ガスを排出する排気ラインと、
を更に備える請求項1又は2に記載の連続製造装置。 - 調温可能な温度制御装置を、前記反応槽のうち少なくとも二つの反応槽にさらに備える、請求項1〜3のいずれか1項に記載の連続製造装置。
- 重合体の連続製造装置を用いた、重合体の脱塩重縮合による連続製造方法であって、
前記連続製造装置は、複数の反応槽を収容する収容室を備え、前記反応槽は順次接続され且つ前記収容室における気相部を介して互いに連通し、前記収容室は少なくとも1組の隣接する反応槽の境界又はその近傍において気相部の横断面積を狭めるバッフルを備え、前記バッフルは、反応混合物の移動方向の上流側に位置する反応槽から、当該バッフルを挟んで前記移動方向の下流側に隣接する反応槽内に、前記気相部を介して気体が移動するのを防ぐバッフルであり、
前記連続製造装置内の前記収容室に、溶媒及びモノマーを供給する工程と、
少なくとも1つの反応槽において、前記溶媒中で前記モノマーの重合反応を行うことにより前記反応混合物を形成する工程と、
前記収容室内の水の少なくとも一部を、前記収容室における気相部を介して前記収容室から除去する工程と、
各反応槽に、前記反応混合物を順次移動させる工程と、
を同時並行して行う重合体の連続製造方法。 - 前記反応混合物の移動方向の下流側から上流側に向けて、前記気相部に不活性ガスを送り込む工程を更に同時並行して行う請求項5に記載の連続製造方法。
- 前記重合体は、硫黄、窒素及び酸素からなる群より選択される少なくとも1種のヘテロ原子を含む芳香族重合体である、請求項5又は6に記載の連続製造方法。
- 前記重合体が、芳香族ポリチオエーテルおよび芳香族ポリエーテルから選ばれる、請求項7に記載の連続製造方法。
- 前記芳香族ポリチオエーテルがポリアリーレンスルフィドであり、前記芳香族ポリエーテルが、芳香族ポリスルホン、ポリアリールエーテルケトンおよびポリエーテルニトリルから選ばれる、請求項8に記載の連続製造方法。
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CN109923153A (zh) | 2019-06-21 |
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EP3514197A4 (en) | 2019-11-13 |
CN109923153B (zh) | 2021-08-24 |
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