JP2009527615A - 環状反応器を変形させるための方法 - Google Patents
環状反応器を変形させるための方法 Download PDFInfo
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Abstract
【解決手段】既存の単一反応装置ラインに固体ポリマー製品をフラッシュ蒸気から分離するためのフラッシュタンクを設け、蒸気を少なくとも2つの分離カラムへ送ってその成分をモノマー、希釈剤およびコモノマーに分離する。
Description
下記文献には反応装置の不連続挙動を減らし、固形物濃度を増加させるための2つの方法が開示されている。
下記文献にも連続スラリーループ反応装置でポリマーを作る方法が開示されている。
従って、利用可能な空間に制限がある場合や、予算上の制約がある場合に、ダブルループ法の利点を得たいといニーズがある。
本発明のさらに他の目的は、単一反応装置ラインをダブル反応装置ラインに変えることによってビモダル樹脂を製造することにある。
本発明のさらに他の目的は、排出液を種々の成分に分離し、分離した各成分を反応装置の最適位置から個別に反応装置へ再噴射することにある。
これらの目的の少なくとも一つは本発明によって少なくとも部分的に達成される。
(1)既存の単一反応装置ラインの前に、この既存の反応装置より小型か、それと同じ寸法の他の単位反応装置ラインを加えるか、
(2)下記(a)〜(c):
(a)垂直沈殿レグ間の接続を再配置して2つの別々の反応装置ラインとし、第1の反応装置ラインは第2の反応装置ラインより小さくするか、それと同じ寸法にし、
(b)分離した新しい反応装置ラインにポンプを加え、
(c)第1の反応装置ラインから第2の反応装置ラインへ製品を連続的に移送する移送ラインを加える、
ことによって少なくとも6つの沈殿レグを有する既存の単一反応装置ラインをダブル反応装置ラインに変え、
上記の既存の単一反応装置ラインに固体ポリマー製品をフラッシュ蒸気から分離するためのフラッシュタンクを設け、この蒸気を少なくとも2つの分離カラムへ送ってその成分をモノマー、希釈剤およびコモノマーに分離する。
本発明は、希釈剤と未反応モノマーとから成る液体媒体中に懸濁した微粒子のポリマー固体のスラリーから成る流体を生じる任意の方法に適用できる。沈殿したポリマースラリーは所定のシーケンスパターンで開閉する吐出弁を介して少なくとも2つの沈澱レグから放出される。全ての沈殿レグの放出時間の合計は、同じ沈澱レグの2回の放出の間の時間の50%以上、好ましくは80%以上、さらに好ましくは95%以上である。最も好ましい実施例では全ての沈殿レグの放出時間の合計は同じ沈澱レグの2回の放出の間の時間の95%〜100%である。ここで、「放出時間の合計」とは各沈澱レグの吐出弁が開いている持続時間の合計を意味し、この合計は全ての沈澱レグで各沈澱レグが一回開口する場合の合計である。
本発明方法は反応装置から沈澱レグをシーケンシャルに開放することによって沈殿したポリマーのスラリーの流れを維持する階段を有する。
本発明のオレフィンポリマーの微粒子を製造する重合方法はポリマー化されるモノマーを含んだ希釈剤中でオレフィン、例えばC2〜C8オレフィンを触媒重合するもので、出発材料をループ反応器に供給し、ポリマー化したスラリーをループ反応器中で循環させ、形成されたポリマーをループ反応器から取り出す。本発明に適したモノマーの例としては分子中に2〜8の炭素原子を有するモノマー、例えばエチレン、プロピレン、ブチレン、ペンテン、ブタジエン、イソプレン、1-ヘキセンが挙げられるが、これらに限定されるものではない。
本発明の好ましい実施例では、本発明はイソブタン希釈剤中でエチレンを重合するに特に適している。適したエチレン重合法にはエチレンの単独重合、エチレンと高級1−オレフィンコモノマー、例えば1-ブテン、1−ペンテン、1-ヘキセン、1-オクテンまたは1-デセンとの共重合があるが、これに限定されるものではない。本発明の好ましい実施例でのコモノマは1-ヘキセンである。
(1)フラッシュタンクから出た気体を精製するための蒸留階段。この段階はモノマー、コモノマおよび希釈剤を分離するための少なくとも2つのカラムを含む。
(2)モノマー、好ましくはエチレンを分離、回収するの階段(エチレン回収ユニット)
(1)このカラムの底部から抜き出された製品は純粋な希釈剤であり、水素やモノマーは含まない。製品は冷却された後、サージタンク(V2)に貯蔵される。このサージタンク(V2)から乾燥後にポンプで反応装置へ送られる。触媒の希釈に適している。
(2)このカラムの頂部から出た流れは冷却水で凝縮され、減圧下で0℃近くの温度で希釈剤で冷却された熱交換器で凝縮される。モノマーを含む非凝縮製品、痕跡量のエタンおよび窒素は乾燥し、エチレン回収ユニットへ送られる。
ポリマー製品を第1の反応装置ラインから第2の反応装置ラインへ移すための移送システムを2つの反応装置ラインの間に配置しなければならない。移送システムは連続でも不連続でもよいが、不連続な場合には沈澱レグを備える。本発明の好ましいシステムは例えば下記文献に記載されている。
既存の反応装置ラインの前に反応装置ラインを追加
既存の反応装置ラインの特徴は書きのとおり:
反応装置の体積: 37m3
沈澱レグの数: 4
反応装置の直径: 500mm
ポリマー生産速度: 12トン/時
循環速度: 10.6 m/秒
エチレン濃度: 8重量%
温度: 92.5 ℃
循環ポンプパワー: 380kW。
反応装置の体積: 19m3
反応装置の直径: 500mm
ポリマーの生産速度: 5トン/時
循環速度: 10m/秒
エチレン濃度: 8重量%
温度: 92℃
固形物濃度: 40%。
最終的な反応装置システムは以下の特徴を有する:
全流量: 12トン/時
反応装置の固体濃度: 45%
沈澱レグ中の固体濃度: 54%
循環速度: 10m/秒。
Claims (8)
- 単一反応装置ラインをダブル反応装置ラインに変える方法であって、
(1)既存の単一反応装置ラインの前に、この既存の反応装置より小型か、同じ寸法の他の単位反応装置ラインを加えるか、
(2)下記(a)〜(c):
(a)垂直沈殿レグ間の接続を再配置して2つの別々の反応装置ラインとし、第1の反応装置ラインは第2の反応装置ラインより小さくするか、同じ寸法にし、
(b)分離した新しい反応装置ラインにポンプを加え、
(c)第1の反応装置ラインから第2の反応装置ラインへ製品を連続的に移送する移送ラインを加える、
ことによって少なくとも6つの沈殿レグを有する既存の単一反応装置ラインをダブル反応装置ラインに変え、
上記の既存の単一反応装置ラインには固体ポリマー製品をフラッシュ蒸気から分離するためのフラッシュタンクを設け、この蒸気を少なくとも2つの分離カラムへ送ってその成分をモノマー、希釈剤およびコモノマーに分離する、
ことを特徴とする方法。 - 第1の反応装置ラインが第2の反応装置ラインより小さな能力を有する請求項1に記載の方法。
- 既存の反応装置ラインの接続セグメントABとCDとをすることを無くし、接続ADおよびBCを設けることによって6つの沈殿レグを有する単一反応装置ラインをダブル反応装置ラインへ変える請求項1または2に記載の方法。
- 第2の反応装置ライン上に配置したバイパスラインと接続した移送ラインを介して、第1の反応装置ラインを出たポリマー製品を第2の反応装置ラインへ送る請求項1〜3のいずれか一項に記載の方法。
- 請求項1〜4のいずれか一項に記載の方法によって得られるダブル反応装置システム。
- 分離された流体製品がモノマー、希釈剤およびコモノマーであり、これらの流体製品を反応装置ラインへ再循環し、モノマーは両方の反応装置ラインで循環ポンプの下流に循環させ、希釈剤は両方の反応装置ラインで循環ポンプの上流に循環させ、必要な場合にはコモノマーを一方の反応装置にのみ循環ポンプの下流へ循環させる、請求項5に記載のダブル反応装置システムの使用。
- モノマーがエチレンであり、コモノマーがヘキセンであり、希釈剤がイソブタンである請求項6に記載の使用。
- 請求項6のダブル反応装置システムのビモダルな(双峰)ポリエチレンの製造での使用。
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EP06110380A EP1825910A1 (en) | 2006-02-24 | 2006-02-24 | Method for transforming a loop reactor |
EP06110380.0 | 2006-02-24 | ||
PCT/EP2007/051659 WO2007096380A1 (en) | 2006-02-24 | 2007-02-21 | Method for transforming a loop reactor |
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EP (2) | EP1825910A1 (ja) |
JP (1) | JP5220621B2 (ja) |
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DK (1) | DK1933976T3 (ja) |
EA (1) | EA014515B1 (ja) |
ES (1) | ES2327794T3 (ja) |
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JP2021520441A (ja) * | 2018-06-21 | 2021-08-19 | バーゼル・ポリオレフィン・ゲーエムベーハー | 反応器カスケードにおけるエチレンコポリマーを製造するための懸濁プロセス |
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EP1825910A1 (en) * | 2006-02-24 | 2007-08-29 | Total Petrochemicals Research Feluy | Method for transforming a loop reactor |
US8871886B1 (en) | 2013-05-03 | 2014-10-28 | Chevron Phillips Chemical Company Lp | Polymerization product pressures in olefin polymerization |
US8344078B2 (en) | 2010-05-21 | 2013-01-01 | Chevron Phillips Chemical Company Lp | Continuous take off technique and pressure control of polymerization reactors |
ES2399346T3 (es) * | 2010-07-30 | 2013-03-27 | Total Research & Technology Feluy | Procedimiento de preparación de poliolefinas |
US9238698B2 (en) | 2012-10-31 | 2016-01-19 | Chevron Phillips Chemical Company Lp | Pressure management for slurry polymerization |
US20140140894A1 (en) | 2012-11-20 | 2014-05-22 | Chevron Phillips Chemical Company, Lp | Polyolefin production with multiple polymerization reactors |
US9096694B1 (en) * | 2014-01-20 | 2015-08-04 | Chevron Phillips Chemical Company Lp | Monomer/diluent recovery |
EP4372016A1 (en) * | 2022-11-18 | 2024-05-22 | Basell Poliolefine Italia S.r.l. | Olefin polymerization process comprising the use of an antistatic composition |
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HU230794B1 (hu) | 2018-05-28 |
DE602007001226D1 (de) | 2009-07-16 |
EP1933976B1 (en) | 2009-06-03 |
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EA014515B1 (ru) | 2010-12-30 |
HUP0800389A3 (en) | 2012-09-28 |
CN101378832B (zh) | 2011-12-28 |
EP1825910A1 (en) | 2007-08-29 |
US20110166302A1 (en) | 2011-07-07 |
CN101378832A (zh) | 2009-03-04 |
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