JP5166674B2 - 重炭化水素供給原料の水蒸気分解処理 - Google Patents
重炭化水素供給原料の水蒸気分解処理 Download PDFInfo
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Description
本発明は、比較的に不揮発性の炭化水素及び他の汚染物を包含する炭化水素の分解に関する。
水蒸気分解は、様々な炭化水素供給原料をオレフィンへ分解することに長らく用いられてきた。従来の水蒸気分解は、2つの主要な区画、即ち対流区画及び放射区画を有する炉を用いる。炭化水素供給原料は通常は炉の対流区画へ液体として入り(蒸気として入る軽供給原料は除く)、通常は、放射区画からの温排ガスとの間接接触により、或いは水蒸気との直接接触により加熱されて気化される。気化された供給原料と水蒸気との混合体は放射区画へ導入されて、ここで分解がなされる。結果的なオレフィンは、例えばクエンチングなどの更なる下流処理のために炉を離れる。
本発明は、重質炭化水素供給原料を加熱するための処理を与え、これは重質炭化水素を加熱し、重質炭化水素を液体と混合して混合体を形成し、その混合体をフラッシュさせて蒸気相及び液相を形成し、処理の少なくとも1つの選択された操作パラメータに従って重質炭化水素と混合された液体の量を変化させて、蒸気相を炉へ供給する。流体は液体炭化水素又は水とすることができる。
(a)重質炭化水素供給燃料を予熱して予熱重質炭化水素供給燃料を形成し、
(b)予熱重質炭化水素供給燃料を水と混合して水重質炭化水素混合体を形成し、
(c)一次希釈スチームを水重質炭化水素混合体へ射出して混合体ストリームを形成し、
(d)熱交換管列内の混合体ストリームを高温排ガスとの間接熱転移により加熱して高温混合体ストリームを形成し、
(e)高温混合体ストリームの温度を制御し、水の流量率及び一次希釈スチームの流量率を変化させることにより水蒸気の炭化水素に対する比を制御し、
(f)フラッシュドラム内の高温混合体ストリームをフラッシュし、蒸気相及び液相を形成して蒸気相を液相から分離し、
(g)蒸気相を炉の対流区画へ供給し、炉の輻射区画からの高温排ガスにより更に加熱して加熱蒸気相を形成し、
(h)加熱蒸気相を炉の輻射区画管へ供給し、ここで蒸気相内の炭化水素を熱的に分解して輻射熱に起因する生成物を形成する。
特に断らない限り、全てのパーセンテージ、割合、比その他は、重量部により記載する。特に断らない限り、組成又は成分に対する基準は、それ自身の組成又は成分、及び組成の混合物のような他の組成又は成分との組み合わせを含む。
本発明による大気パイプスチールボトム(atmospheric pipestill bottoms:APS)及び原油の処理を模擬する技術計算を導入した。添付の表1には、フラッシュドラムを有する商用型炉においてタピス(Tapis)APSボトム及びタピス原油を分解するための模擬結果を要約する。原油における非常に軽量の成分は、重質成分の部分的圧力を低減させる水蒸気のように働く。従って、公称950°F(510℃)切断点において、フラッシュドラムは大気中残留物のための温度よりも100°F(50℃)低い温度で作動する。
大気パイプスチール(APS)ボトム及び原油フラッシュドラムシュミレーションの概要
APSボトム 原油 図1の参照符号
対流供給速度 klb/hr(t/h) 126(57) 100(45) n/a
950°Fマイナス(510℃),wt% 70 93 n/a
多孔分散管の前の温度°F(℃) 400(205) 352(178) 4
多孔分散管水速度klb/hr(t/h) 12(5) 43(20) 14
一次希釈スチーム速度klb/h(t/h) 18(8) 8(4) 17
二次希釈スチーム速度klb/h(t/h) 17(8) 19(9) 18
過熱低減水速度klb/h(t/h) 6(3) 6(3) 26
フラッシュドラム温度°F(℃) 847(453) 750(400) 5
フラッシュドラム圧力 psig(kPag) 107(740) 101(694) 5
フラッシュドラムの蒸気化量wt% 74 93 5
輸送残留物klb/h(t/h) 33(15) 7(3) 22
例2
表2には、C4の2つの凝縮を有する残留物混合のためのフラッシュの性能の模擬を要約する。与えられたフラッシュ温度、圧力、及び水蒸気率において、残留物と混合されたC4の各パーセントは、フラッシュにおける残留物蒸気化を約1/4%増大させる。従って、供給するC4の添加は蒸気化される残留物からより多くの炭化水素をもたらす。
C4/残留物混合フラッシュ性能
純粋な残留物 混合1:残留物+C4 混合2:残留物+C4
対流供給のWt%残留物 100 94 89
C4のWt%残留物 0 6 11
バブル点°F 991 327 244
@112psig
フラッシュのWt%蒸気化残留物 65.0% 68.2% 70.8%
フラッシュの全Wt%蒸気化 65.0% 69.9% 74.0%
温度°F 819 819 819
フラッシュのWt%蒸気化残留物 70.0% 72.8% 75.1%
フラッシュの全Wt%蒸気化 70.0% 74.3% 77.8%
温度°F 835 835 835
フラッシュのWt%蒸気化残留物 75.0% 77.4% 79.4%
フラッシュの全Wt%蒸気化 75.0% 78.6% 81.7%
温度°F 855 855 855
Claims (27)
- 分解炉を用いて重質炭化水素供給原料の分解のための方法であって、
重質炭化水素を加熱して、この重質炭化水素を流体と混合して混合体を形成し、この混合体を気液分離して蒸気相と液相とを形成し、
前記混合体を気液分離する前に、前記重質炭化水素を一次希釈スチームと混合することを含むと共に、
前記分解炉は、輻射熱及び高温排ガスを与える輻射区画バーナーと、多段熱交換管列からなる対流区画とからなり、
前記流体は水であり、
前記方法は更に、
高温排ガスによる間接熱転移により熱交換管列内の混合体を加熱し、前記混合体の気液分離に先立って制御温度にして、前記制御温度と、水蒸気の炭化水素に対する比との両方は水の流量率及び一次希釈スチームの流量率を変化させることにより制御でき、
フラッシュドラム内で気液分離段階を実行して蒸気相と液相とを形成し、且つ蒸気相を液層から分離し、
前記蒸気相を前記分解炉の対流区画へ供給して、前記分解炉の輻射区画からの高温排ガスにより更に加熱して加熱蒸気相を形成し、
この加熱蒸気相を前記分解炉の輻射区間管へ供給し、前記蒸気相内の炭化水素が熱的に分解して、輻射熱に起因する生成物を形成することを含む方法。 - 請求項1に記載の方法において、前記重質炭化水素が、前記流体との混合の前に分解炉の対流区画において加熱される方法。
- 請求項1に記載の方法において、前記流体は液体炭化水素と水の少なくとも一方を含む方法。
- 請求項3に記載の方法において、前記流体が水である方法。
- 請求項1乃至4の何れか一項に記載の方法において、二次希釈スチームストリームが分解炉内で過熱されて、前記混合体が気液分離される前に前記混合体と混合される方法。
- 請求項1乃至5の何れか一項に記載の方法であって、前記蒸気相は分解炉内で分解される方法。
- 請求項1乃至6の何れか一項に記載の方法であって、前記重質炭化水素は、真空ガスオイル、重質ガスオイル、原油で汚染されたナフサ、大気残留物、重質残留物、C4/残留物混合体、ナフサ/残留物混合体及び原油のうちの少なくとも1つを含む方法。
- 請求項1乃至7の何れか一項に記載の方法であって、前記重質炭化水素は、少なくとも310℃(600°F)の公称最終沸点を有する方法。
- 請求項1乃至8の何れか一項に記載の方法であって、蒸気相が760℃(1400°F)より低いエンド沸点を有する方法。
- 請求項1乃至9の何れか一項に記載の方法であって、前記混合体が少なくとも1つのフラッシュドラムにおいて気液分離され、前記蒸気相が前記ドラムの上部部分から除去されて、前記液相が前記ドラムの下部分から除去される方法。
- 請求項1に記載の方法において、一次希釈スチームは、水が重質炭化水素供給原料と混合された後に混合体へ注入される方法。
- 請求項1又は11に記載の方法において、重質炭化水素供給原料が、水蒸気分解ガスオイル及び残留物、ガスオイル、加熱オイル、ジェット燃料、ディーゼル、 灯油、ガソリン、コーカーナフサ、水蒸気分解ナフサ、触媒分解ナフサ、水素化分解物、改質油、ラフィネート改質油、フィッシャー・トロップシュ液体、 フィッシャー・トロップシュガス、天然ガソリン、留出物、処女ナフサ、原油、大気パイプスチールボトム、ボトムを含む真空パイプスチールストリーム、広範 な沸点範囲のナフサ対ガスオイル凝縮体、精製所からの重非処女炭化水素ストリーム、真空ガスオイル、重ガスオイル、原油で汚染されたナフサ、大気残油、重残油、C4/残留物混合体、ナフサ残留物混合体のうちの一つ以上を含む方法。
- 請求項1,11又は12の何れか一項に記載の方法において、前記重質炭化水素供給原料は低硫黄蝋質残留物を含む方法。
- 請求項1乃至13の何れか一項に記載の方法において、前記重質炭化水素の60乃至80%は600℃(1100°F)よりも下で沸騰する方法。
- 請求項1乃至14の何れか一項に記載の方法において、流体との混合に先立つ前記重質炭化水素の温度は、150℃から260℃(300°F乃至500°F)である方法。
- 請求項1乃至15の何れか一項に記載の方法において、前記制御温度は、310℃から510℃(600°F乃至950°F)である方法。
- 請求項1乃至16の何れか一項に記載の方法において、前記重質炭化水素供給原料は、少なくとも310℃(600°F)の公称最小沸点を有する方法。
- 請求項1乃至16の何れか一項に記載の方法において、前記重質炭化水素供給原料が、前記対流区画における上部熱交換管列において加熱される方法。
- 請求項1乃至18の何れか一項に記載の方法において、前記フラッシュドラムの圧力は40psiaと200psiaとの間で操作される方法。
- 請求項1乃至19の何れか一項に記載の方法において、混合体ストリームの50乃至90%は、前記フラッシュドラム内に形成された蒸気相にある方法。
- 請求項1乃至20の何れか一項に記載の方法において、一次希釈スチームが前記対流区画における熱交換管列において加熱される方法。
- 請求項1乃至21の何れか一項に記載の方法において、前記加熱混合体ストリームを二次希釈スチームと混合することを更に含む方法。
- 請求項22に記載の方法において、二次希釈スチームが過熱される方法。
- 請求項22又は23に記載の方法において、二次希釈スチームが、前記対流区画における熱交換管列において加熱される方法。
- 請求項1乃至24の何れか一項に記載の方法において、前記蒸気相を前記フラッシュドラムから遠心分離機へ移送して、この蒸気相を前記分解炉の対流区画へ供給する前に、液体に随伴する微量成分を除去する方法。
- 請求項1乃至25の何れか一項に記載の方法において、前記フラッシュドラム内に見出される蒸気相は、前記分解炉の対流区画へ供給される前に、バイパススチームと混合される方法。
- 請求項1乃至26の何れか一項に記載の方法において、前記加熱蒸気相温度が430℃から650℃(800°Fから1200°F)である方法。
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US10/188,901 | 2002-07-03 | ||
US10/188,901 US7090765B2 (en) | 2002-07-03 | 2002-07-03 | Process for cracking hydrocarbon feed with water substitution |
US10/188,461 | 2002-07-03 | ||
US10/188,461 US7138047B2 (en) | 2002-07-03 | 2002-07-03 | Process for steam cracking heavy hydrocarbon feedstocks |
US10/189,618 US7097758B2 (en) | 2002-07-03 | 2002-07-03 | Converting mist flow to annular flow in thermal cracking application |
US10/189,618 | 2002-07-03 | ||
PCT/US2003/020378 WO2004005433A1 (en) | 2002-07-03 | 2003-06-27 | Process for steam cracking heavy hydrocarbon feedstocks |
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JP2004519667A Expired - Fee Related JP4403071B2 (ja) | 2002-07-03 | 2003-06-27 | 熱分解法におけるミスト流の環状流への変換 |
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JP2004519668A Expired - Fee Related JP4387301B2 (ja) | 2002-07-03 | 2003-06-27 | 水置換による炭化水素原料分解処理 |
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