JP6262666B2 - 原油の直接処理のための水素処理、溶剤脱歴および蒸気熱分解統合プロセス - Google Patents
原油の直接処理のための水素処理、溶剤脱歴および蒸気熱分解統合プロセス Download PDFInfo
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- JP6262666B2 JP6262666B2 JP2014554903A JP2014554903A JP6262666B2 JP 6262666 B2 JP6262666 B2 JP 6262666B2 JP 2014554903 A JP2014554903 A JP 2014554903A JP 2014554903 A JP2014554903 A JP 2014554903A JP 6262666 B2 JP6262666 B2 JP 6262666B2
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- Thermal Sciences (AREA)
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Description
本出願は、2012年1月27日出願の米国特許仮出願第61/591,776号の利益を主張する。この開示は、参照によってその全体が本明細書に組み込まれる。
本発明は、原油の直接処理によりオレフィンや芳香族化合物などの石油化学製品を生産するための水素処理、溶剤脱歴および蒸気熱分解統合プロセスに関する。
BMCI=87552/VAPB+473.5*(sp.gr.)−456.8 (1)
式中、
VAPB=容積平均沸点(ランキン目盛)、
sp.gr.=供給原料の比重。
本発明は、添付図に言及しながら、以下でさらに詳細に説明される。
a.水素化脱金属触媒。HDM部の触媒は、通常、約140〜240m2/gの表面積のガンマアルミナ支持体に坦持される。この触媒は、例えば、1cm3/gを超える非常に高い気孔容積を持つとして最もよく表現される。孔径それ自体は、通常、主にマクロ多孔性である。これは、触媒表面上での金属および任意のドーパントの取り込み用の大きな容積を与えるのに必要である。典型的な例では、触媒表面上の活性金属は、Ni/Ni+Moの比率が0.15未満のニッケルおよびモリブデンの硫化物である。かなりのニッケルおよびバナジウムが除去の間に供給原料自体から沈着し、触媒として機能することが予想されるので、HDM触媒上のニッケルの濃度は、他の触媒より低い。使われるドーパントは、リン(例えば、米国特許公開第2005/0211603号を参照されたい。この特許は、参照によって本明細書に組み込まれる)、ホウ素、シリコンおよびハロゲンの内の1種または複数種であってよい。触媒は、アルミナ押出成形品またはアルミナビーズの形であってよい。特定の実施形態では、金属の取り込みがベッドの上部で30〜100%の範囲になるので、アルミナビーズを使って、反応装置中の触媒HDMベッドの取り出しを容易にする。
b.また、中間触媒を使って、HDMとHDS機能との間の移行を行わせることができる。それは中間金属充填材および孔径分布を有する。HDM/HDS反応装置中の触媒は実質的には押出成形品の形態のアルミナ支持体、任意選択で、VI族(例えば、モリブデンおよび/またはタングステン)の少なくとも1種の触媒金属、および/またはVIII族(例えば、ニッケルおよび/またはコバルト)の少なくとも1種の触媒金属から構成される。また、触媒は、任意選択で、ホウ素、リン、ハロゲンおよびシリコンから選択される少なくとも1種のドーパントを含む。物理学的性質には、約140〜200m2/gの表面積、少なくとも0.6cm3/gの気孔体積、およびメソポーラスであり、12〜50nmの範囲の気孔が含まれる。
c.HDS部の触媒は、HDM範囲のより高端側に近い、例えば、約180〜240m2/gの範囲の典型的表面積を備えたガンマアルミナベース支持材料を有するものを含んでもよい。この必要とされるHDSのより広い表面は、例えば、1cm3/gより小さい、比較的小さい気孔容積を生ずる。触媒は、モリブデンなどの少なくとも1種のVI族元素、およびニッケルなどの少なくとも1種のVIII族元素を含む。また、触媒は、ホウ素、リン、シリコンおよびハロゲンから選択される少なくとも1種のドーパントを含む。特定の実施形態では、コバルトを使って、比較的高いレベルの脱硫を行える。活性相用の金属充填材は、必要な活性がより高いので、より多くなり、その結果、モル比率Ni/Ni+Moは、0.1〜0.3の範囲であり、(Co+Ni)/Moモル比率は、0.25〜0.85の範囲である。
d.例えば、Appl.Catal.A General、204(2000)251、に記載のように、最終触媒(任意選択で、第2および第3触媒を置換してもよい)は、(水素化脱硫の一次機能よりは)供給原料の水素添加を行うように設計される。また、触媒はNiにより活性化されるであろうし、また、支持体は、大きな気孔のガンマアルミナとなろう。物理学的性質には、HDM範囲のより高端側に近い、例えば、180〜240m2/gの表面積が含まれる。この必要とされるHDSのより広い表面は、例えば、1cm3/gより小さい、比較的小さい気孔容積を生ずる。
本明細書記載の方法とシステムは、既知の蒸気熱分解プロセスに対し改善できる:
オレフィンおよび芳香族化合物などの石油化学製品の生産のための供給原料として原油の使用;
オレフィンの高収率のために、蒸気熱分解ゾーンへの供給原料の水素含量が富化される;
コークス前駆体は、最初の全原油からかなり除去され、これにより、ラジアンとコイル中でのコークス形成の低減が可能となる;
また、金属、硫黄および窒素化合物などのさらなる不純物も、出発供給原料から著しく除去され、最終生成物の後処理の必要性がなくなる。
Claims (7)
- 原油を直接処理してオレフィンおよび芳香族石油化学製品を生産するための水素処理、溶剤脱歴および蒸気熱分解統合プロセスであって、
a.低減された混入物含量、増加したパラフィン度、低下した鉱山局相関インデックス、および増加した米国石油協会比重度を有する還元水素化処理流出物を生成するのに効果的な条件下で動作する水素化処理ゾーンに前記原油を装填するステップ、
b.脱アスファルトおよび脱金属油流ならびに底部アスファルト相を生産するのに効果的な量の溶剤と共に前記水素化処理流出物を溶剤脱歴ゾーンに装填するステップ、
c.蒸気の存在下で前記脱アスファルトおよび脱金属油流を熱分解して混合生成物流を生成するステップであって、
ここに、
前記脱アスファルトおよび脱金属油流は蒸気熱分解ゾーンの対流部で加熱され;
前記加熱された脱アスファルトおよび脱金属油流は、
流入流混合物の受け入れ用の断面S1の入口、前記入口に第1の端部で連結された曲線形導管および前記曲線形導管の第2の端部に連結された連結要素を有する予備回転要素、
前記連結要素の前記曲線形導管および前記サイクロン型部を通じて前記予備回転要素に接合された入口と、前記サイクロン型部の上端に配置され、気相が通過する上昇管部とを有する制御されたサイクロン型部、および
液体が通過する液体収集器/沈降部
を含む気液分離装置を使って気相と液相に分離され;
ここに前記気相は蒸気熱分解ゾーンの熱分解部に送られ;および液相は排出され;
d.前記熱分解された混合生成物流を分離するステップ、
e.ステップ(d)で回収された水素を精製し、それをステップ(a)で再利用するステップ、
f.前記分離された混合生成物流からオレフィンおよび芳香族化合物を回収するステップ、および
g.前記分離された混合生成物流から熱分解燃料油を回収するステップ、
を含む、前記統合プロセス。 - ステップ(d)が、
前記熱分解混合生成物流を複数の圧縮段階で圧縮するステップ、
前記圧縮された熱分解混合生成物流を苛性処理して、硫化水素および二酸化炭素の含量が低減した熱分解混合生成物流を生成するステップ、
硫化水素および二酸化炭素の含量が低減した前記熱分解混合生成物流を圧縮するステップ、
硫化水素および二酸化炭素の含量が低減した前記圧縮された熱分解混合生成物流を脱水するステップ、
硫化水素および二酸化炭素の含量が低減した前記脱水された圧縮熱分解混合生成物流から水素を回収するステップ、および
硫化水素および二酸化炭素の含量が低減した前記脱水された圧縮熱分解混合生成物流の残部から、ステップ(f)のようにオレフィンおよび芳香族化合物を得てかつ、ステップ(g)のように熱分解燃料油を得るステップ
を含み、さらに
ステップ(e)が、
硫化水素および二酸化炭素の含量が低減した前記脱水された圧縮熱分解混合生成物流から回収された水素を、前記水素化処理ゾーンで再利用するために精製するステップを含む、請求項1に記載の統合プロセス。 - 硫化水素および二酸化炭素の含量が低減した前記脱水された圧縮熱分解混合生成物流から水素を回収するステップが、前記熱分解ステップのバーナーおよび/またはヒーター用の燃料として使用するために別にメタンを回収するステップをさらに含む、請求項2に記載の統合プロセス。
- 前記熱分解ステップが、蒸気熱分解ゾーンの対流部で脱アスファルトおよび脱金属油流を加熱するステップ、前記加熱された脱アスファルトおよび脱金属油を蒸気留分および液体留分に分離するステップ、前記蒸気留分を蒸気熱分解ゾーンの熱分解部に送るステップ、および前記液体留分を排出するステップを含み、前記排出された液体留分がステップ(g)で回収された熱分解燃料油とブレンドされる、請求項1に記載の統合プロセス。
- 前記水素化処理流出物を高圧分離器中で分離し、洗浄して追加の水素源として前記水素化処理ゾーンに再利用するガス部分、および液体部分を回収するステップ、および
前記高圧分離器からの前記液体部分を低圧分離器中でガス部分および液体部分に分離するステップであって、前記低圧分離器からの前記液体部分が、ステップ(b)で処理された前記水素化処理流出物であり、前記低圧分離器からの前記ガス部分が、ステップ(c)における熱分解後で、ステップ(d)の分離前に前記混合生成物流と組み合わされる前記ステップ
をさらに含む請求項1に記載の統合プロセス。 - ステップ(b)が、
前記原油を補充用溶剤および任意選択で新しい溶剤と混合し、混合物を生成するステップ、
前記混合物を一次脱アスファルトおよび脱金属油相ならびに一次アスファルト相が形成される一次沈降タンクに移すステップ、
前記一次脱アスファルトおよび脱金属油相を二次脱アスファルトおよび脱金属油相ならびに二次アスファルト相が形成される二次沈降タンクに移すステップ、
前記二次アスファルト相を前記一次沈降タンクに再利用し、追加の脱アスファルトおよび脱金属油を回収するステップ、
前記二次脱アスファルトおよび脱金属油相を脱アスファルトおよび脱金属油分離ゾーンに送り、再利用溶剤流、ならびに実質的に溶剤不含の脱アスファルトおよび脱金属油流を得るステップ、
追加の再利用溶剤流および底部アスファルト相のフラッシュ分離のために、前記一次アスファルト相を分離器に送るステップ、
を含み、
前記実質的に溶剤不含脱アスファルトおよび脱金属油流が、ステップ(c)における熱分解への供給原料である、
請求項1に記載の統合プロセス。 - 前記底部アスファルト相が、ステップ(g)で回収された熱分解燃料油とブレンドされる、請求項6に記載の統合プロセス。
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