JP2022528584A - エチレン又はプロピレンの生産を最大化する方法 - Google Patents
エチレン又はプロピレンの生産を最大化する方法 Download PDFInfo
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Abstract
Description
S1:原料を前処理してから混合器内で過熱蒸気と混合して、均一に混合した後に触媒クラッキング反応器に入れ、触媒の作用によって、原料を高温油気と廃残渣に変え、高温油気は予熱段とデスーパーヒーティング段とを含む二段式予洗塔による降温と不純物除去を経て、軽質、重質の二種類の留分油とガス生成物などの生成物を得る。
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表2
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Claims (10)
- エチレン又はプロピレンの生産を最大化する方法であって、前記方法は:
S1:原料を前処理してから混合器内で過熱蒸気と混合して、均一に混合した後に触媒クラッキング反応器に入れ、触媒の作用によって、原料を高温油気と廃残渣に変え、高温油気を二段式予洗塔による降温と不純物除去を経て、軽質、重質の二種類の留分油とガス生成物などの生成物を得るステップであって、前記二段式予洗塔は予熱段とデスーパーヒーティング段とを含むステップと、
S2:ステップS1における重質留分油に対し水素化反応操作を行い、軽質留分油中のオレフィン成分に対して再結合操作を行い、そのBTX成分を分離して生成物の一つとし、そのアルカン成分をスチームクラッキング装置に入れるステップと、
S3:ステップS2において得られた水素化及び再結合反応の生成物と、スチームクラッキング留分油とをステップS1の触媒クラッキング反応器に循環させて、触媒クラッキング反応器において再び選択的な触媒クラッキング反応を行うステップであって、循環総生成物量と新鮮な供給原材料との質量比は10~60:100であるステップと、
S4:ステップS1のガス生成物をスチームクラッキング装置に送り、メタン、エタン、エチレン、プロパンとプロピレンなどを集中的に分離し、エチレン、プロピレンを生成物として、エタン、プロパン及びその他のアルカンなどはスチームクラッキング装置に戻すステップと、
を含み、
以上の操作により、原料を最終的にメタン、エチレン、プロピレン、BTXなどの生成物に変換し、エチレンとプロピレンとを合わせた収率は原料の45~75m%、芳香族炭化水素BTXの収率は原料の15~30m%であり、残りのほとんどはメタンである
ことを特徴とする方法。
- 都市混合廃プラスチックを原料とする場合、前記前処理操作は:先ず、都市混合廃プラスチックを破砕、除鉄プロセスのうちの少なくとも一つの操作によって処理するステップと、そして、廃プラスチックを熱溶融釜に輸送し、過熱蒸気により前記熱溶融釜内の廃プラスチックを液化物に溶融して、前記熱溶融釜の底部に収集するステップであって、前記廃プラスチックを加熱して液化物に溶融する操作条件は、温度150~250℃、圧力0.01~0.5MPaであるステップと、最後に、廃プラスチック液化物を二段式予洗塔に送り、高温油気を熱源として予熱し、予熱された廃プラスチック液化物を原料として再び過熱蒸気と混合してから、触媒クラッキング反応器内に入れるステップと、を含む
ことを特徴とする請求項1に記載のエチレン又はプロピレンの生産を最大化する方法。
- 前記廃プラスチック液化物は予熱段とデスーパーヒーティング段を経てから、プレート毎に昇温し、塔釜に到達する際にその温度は250~320℃まで上がり、予熱された廃プラスチック液化物は、一部が混合器を通ってから触媒クラッキング反応器に入って触媒クラッキング反応を行われ、一部が熱溶融釜まで循環され戻される
ことを特徴とする請求項2に記載のエチレン又はプロピレンの生産を最大化する方法。
- 原油を原料とする場合、前記前処理操作は、電気脱塩、常圧分留及びブタン脱れき等のプロセスステップのうちの少なくとも1つの操作を含み、原油は常圧分留されてから、その抜頭油はスチームクラッキング装置に入ってエチレンを大量生産し、常圧第一ライン、常圧第二ラインは固定床水素化クラッキングプロセスを利用して航空ケロシンを生産でき、残りの常圧ボトム油は全て触媒クラッキング反応器に入る
ことを特徴とする請求項1に記載のエチレン又はプロピレンの生産を最大化する方法。
- 前記常圧ボトム油を触媒クラッキング反応器に導入する前に、ブタン脱れきプロセスを選択し、常圧ボトム油を改質することで、原油中の多くの重金属、アスファルテン、コロイド等の不純物を除去することが可能で、前記ブタン脱れき操作の温度は100~200℃、圧力は2.0~6.0MPaである
ことを特徴とする請求項4に記載のエチレン又はプロピレンの生産を最大化する方法。
- 前記前処理された原料は請求項2~5の何れか一項に記載の原料の何れか一つ、又は何れか二つ又は二つ以上の混合物から選択されたものである
ことを特徴とする請求項1に記載のエチレン又はプロピレンの生産を最大化する方法。
- 前記過熱蒸気はまた、他の過熱不活性媒体を選用してもよい
ことを特徴とする請求項1に記載のエチレン又はプロピレンの生産を最大化する方法。
- 前記二段式予洗塔の塔頂温度は100~200℃、圧力は0.05~0.30MPa、塔釜温度は250~320℃であり、デスーパーヒーティング段において、高温油気が過熱状態から飽和状態に冷却されると同時に、油気が帯びた粉塵は洗浄によって除去され、塔釜において重質留分油が得られ、塔頂油気が熱交換して冷却されてから三相分離器に入り、タンク底部から軽質留分油が出て、タンク頂部から不凝縮ガスなどの生成物が出る
ことを特徴とする請求項1に記載のエチレン又はプロピレンの生産を最大化する方法。
- 前記ステップS1において、前記触媒クラッキング反応器の操作条件は:反応温度300~600℃、反応圧力0.05~0.5MPa、触媒/油重量比6~12、空間速度0.1~30h-1であり、前記触媒クラッキング反応器内の触媒は分子篩触媒であり、前記分子篩触媒は、ZSM5、ZSM35、BETA、USY等の分子篩のいずれか一つ又はこれらの修飾物であり、前記触媒クラッキング反応器は、固定流動床又は循環流動床のうちの一つ、又はそれらの組み合わせを選用することができる
ことを特徴とする請求項1に記載のエチレン又はプロピレンの生産を最大化する方法。
- 前記ステップS2において、前記再結合反応はオリゴメリゼーション反応器において行われ、その操作条件は:反応温度40~200℃、反応圧力0.5~6.0MPa、空間速度0.1~6h-1である
ことを特徴とする請求項1に記載のエチレン又はプロピレンの生産を最大化する方法。
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