JP2018533477A - 溶媒回収装置および溶媒回収方法 - Google Patents
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Abstract
【解決手段】本出願は溶媒回収装置および溶媒回収方法に関するもので、本出願に係る溶媒回収装置および方法は合成ゴムの製造工程においてスチーム使用量を節減することができ、凝縮機を介して捨てられる廃熱を回収することによってエネルギー使用量を節減することができる。
【選択図】図2
Description
図2に例示された通り、水供給タンク10から水供給ライン121を通じて供給される水とスチーム供給ライン131を通じて供給されるスチームをスチーム混合器71で混合して脱去装置22に供給した。前記脱去装置22で高分子と分離された溶媒は回収されて溶媒流入ライン201を通じて第1蒸留塔31に流入させた。前記第1蒸留塔31の塔底領域から流出する第1塔底流れ301は、第1再沸器311を通じて再加熱して第1蒸留塔31に還流させた。第1蒸留塔31から流出する溶媒は、第1流出ライン321を通じて第2蒸留塔41に流入させた。前記第2蒸留塔41の塔底領域から流出する第2塔底流れ421は、第2再沸器411で加熱して第2蒸留塔41に還流させた。
図3に例示された通り、水の供給流れ122の一部612を熱交換器62で第2蒸留塔42の塔頂領域から流出する塔頂流れ402の一部452と熱交換させた後、水流出ライン602を通じて水供給ライン122に供給し、前記塔頂流れ402の一部442を第1再沸器312に流入させて前記第1蒸留塔32の第1塔底流れ302と熱交換させたことを除いては、実施例1と同じ装置を使った。
図1で例示された通り、第2蒸留塔40の塔頂領域から流出する塔頂流れ400を凝縮機55を通じて凝縮した後、第1蒸留塔30または第2蒸留塔40に流入させ、凝縮機50に供給された冷却水からの廃熱は廃棄したことを除いては、実施例1と同じ装置を使った。
Claims (16)
- 水供給タンクおよび高分子成分と溶媒を含む混合物から前記高分子成分と前記溶媒を分離し得る脱去装置を含む溶媒分離部;前記溶媒分離部で回収された溶媒を精製し得る精製部であって、互いに連結されており、それぞれ再沸器と凝縮機を有する第1蒸留塔と第2蒸留塔を含む精製部;および配管システムを含み、
前記配管システムは、前記水供給タンクからの水を前記混合物と混合した後に前記脱去装置に導入できるように形成された第1ライン;
前記溶媒分離部から回収された溶媒を前記第1蒸留塔に導入できるように形成された第2ライン;および
前記第1蒸留塔で精製された溶媒を前記第2蒸留塔に導入できるように形成された第3ラインを含み、
前記配管システムは、前記混合物と混合する前の水と前記第2蒸留塔の塔頂生成物を熱交換させることができるように設置された第1熱交換ライン
または前記第1蒸留塔の再沸器と前記第2蒸留塔の塔頂生成物を熱交換させることができるように設置された第2熱交換ラインをさらに含む、溶媒回収装置。 - 第1熱交換ラインには熱交換器および第2蒸留塔の凝縮機が設置されており、前記熱交換器および第2蒸留塔の凝縮機は第2蒸留塔の塔頂生成物が前記熱交換器で水と熱交換された後に前記第2凝縮機に導入されるように前記第1熱交換ラインに設置されている、請求項1に記載の溶媒回収装置。
- 第2熱交換ラインには第1蒸留塔の再沸器および第2蒸留塔の凝縮機が設置されており、前記第1蒸留塔の再沸器および第2蒸留塔の凝縮機は第2蒸留塔の塔頂生成物が前記第1蒸留塔の再沸器を経た後に前記第2凝縮機を経ることができるように前記第2熱交換ラインに設置されている、請求項1に記載の溶媒回収装置。
- 第1ラインにスチームを供給できるように設置されたスチーム供給ラインをさらに含む、請求項1に記載の溶媒回収装置。
- 配管システムは第1および第2熱交換ラインを含み、前記第1および第2熱交換ラインは、第2蒸留塔の塔頂生成物の一部が溶媒回収部の水と熱交換された後に第2蒸留塔の凝縮機を経て第2蒸留塔に還流され、前記第2蒸留塔の塔頂生成物の他の一部が第1蒸留塔の再沸器および前記第2蒸留塔の凝縮機を順に経た後に前記第2蒸留塔に還流するように形成されている、請求項1に記載の溶媒回収装置。
- 請求項1に記載された溶媒回収装置を用いて溶媒を回収する方法であって、
高分子成分と溶媒を含む混合物を水供給タンクからの水と混合した後に脱去装置に導入する工程を含む溶媒回収段階;および溶媒回収段階で回収された溶媒を第1および第2蒸留塔で精製する溶媒精製段階を含むものの、
配管システムを通じて前記第2蒸留塔の塔頂生成物を前記混合物と混合する前の水または前記第1蒸留塔の再沸器と熱交換させる段階を遂行する、溶媒回収方法。 - 水または再沸器と熱交換される前の塔頂生成物の温度Tiが110〜160℃の範囲内にある、請求項7に記載の溶媒回収方法。
- 塔頂生成物と熱交換された後の水または再沸器の流出流れの温度Taが90〜140℃の範囲内にある、請求項7に記載の溶媒回収方法。
- 第1蒸留塔の再沸器に導入される前の第2蒸留塔の塔頂生成物の温度Tiが130〜160℃の範囲内にある、請求項10に記載の溶媒回収方法。
- 配管システムを通じて前記第2蒸留塔の塔頂生成物の一部を前記混合物と混合する前の水と熱交換させ、前記第2蒸留塔の塔頂生成物の他の一部を前記第1蒸留塔の再沸器と熱交換させる段階を遂行する、請求項6に記載の溶媒回収方法。
- 水と熱交換される第2蒸留塔の塔頂生成物の流量Aと第1蒸留塔の再沸器と熱交換される第2蒸留塔の塔頂生成物の流量Bの比率が0.40〜0.65である、請求項12に記載の溶媒回収方法。
- 第1蒸留塔の塔頂運転温度は95〜105℃の範囲内であり、塔底運転温度は125〜140℃の範囲内である、請求項6に記載の溶媒回収方法。
- 第2蒸留塔の塔頂運転温度は110〜160℃の範囲内であり、塔底運転温度は120〜165℃の範囲内である、請求項6に記載の溶媒回収方法。
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KR102347112B1 (ko) * | 2021-08-11 | 2022-01-05 | 주식회사 다산바이오 | 카다놀제조시스템 및 이를 이용한 카다놀제조방법 |
JP7488414B2 (ja) | 2021-11-17 | 2024-05-21 | エルジー・ケム・リミテッド | 廃水精製方法 |
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KR102106806B1 (ko) | 2018-02-09 | 2020-05-06 | 주식회사 엘지화학 | 공액디엔계 중합체 제조방법 및 공액디엔계 중합체 제조장치 |
CN108273282B (zh) * | 2018-02-28 | 2023-11-10 | 重庆云天化天聚新材料有限公司 | 三聚甲醛合成蒸馏塔汽相低位热回收系统及其回收方法 |
WO2020091391A1 (ko) | 2018-11-01 | 2020-05-07 | 주식회사 엘지화학 | 유기용매 함유 혼합용액으로부터 유기용매의 분리방법 |
KR102520447B1 (ko) * | 2018-11-22 | 2023-04-10 | 주식회사 엘지화학 | 용매 회수 방법 및 용매 회수 장치 |
KR102383417B1 (ko) | 2018-12-10 | 2022-04-07 | 주식회사 엘지화학 | 에틸렌 올리고머화 반응 생성물의 분리방법 |
KR102474740B1 (ko) * | 2018-12-18 | 2022-12-05 | 주식회사 엘지화학 | 아미드계 화합물의 회수 방법 |
EP3971221A4 (en) * | 2020-07-22 | 2022-09-07 | Lg Chem, Ltd. | METHOD AND DEVICE FOR RECOVERING A SOLVENT |
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JP6615995B2 (ja) | 2019-12-04 |
KR20170141872A (ko) | 2017-12-27 |
US20180319949A1 (en) | 2018-11-08 |
US10703875B2 (en) | 2020-07-07 |
EP3473668A1 (en) | 2019-04-24 |
WO2017217708A1 (ko) | 2017-12-21 |
CN108368288A (zh) | 2018-08-03 |
EP3473668A4 (en) | 2019-04-24 |
EP3473668B1 (en) | 2020-03-18 |
KR102089414B1 (ko) | 2020-03-16 |
CN108368288B (zh) | 2021-03-26 |
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