JP2014508849A - 水素化分解及び流動接触分解を統合する分解システム及びプロセス - Google Patents
水素化分解及び流動接触分解を統合する分解システム及びプロセス Download PDFInfo
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- B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
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- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
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- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
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- C—CHEMISTRY; METALLURGY
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Abstract
【選択図】図1
Description
a.供給材料及び水素を、第1の水素化分解触媒を含有する第1の水素化分解反応帯に導入して、第1の反応帯溶出物を生成するステップ、
b.第1の反応帯流出物及び随意に追加の水素を、第2の水素化分解触媒を含有する第2の水素化分解反応帯に送って、第2の反応帯流出物を生成するステップ、
c.第2の反応帯溶出物を分留帯に送って、少なくとも低沸点留分及び高沸点留分、及び随意に1つ又は複数の中間留分を生成するステップ、
d.残油留分を、オレフィン及びガソリンの形成を促進し、オレフィン消費反応を最小限に抑える条件下で操業する流動接触分解反応及び分離帯に送るステップ、
e.流動接触分解反応及び分離帯からオレフィンを回収するステップ、
f.流動接触分解反応及び分離帯からガソリンを回収するステップ、
g.流動接触分解反応及び分離帯からの残留循環油の少なくとも部分を、第1及び/又は第2の水素化分解反応帯に運搬するステップを含む。
約300℃〜約500℃、ある実施形態では、約330℃から約475℃、及び更なる実施形態では、約330℃〜約450℃の反応温度、
約60kg/cm2〜約300kg/cm2、ある実施形態では約100kg/cm2〜約200kg/cm2、及び更なる実施形態では約130kg/cm2〜約180kg/cm2の水素分圧、
約0.1時間−1〜約10時間−1、ある実施形態では約0.25時間−1〜約5時間−1、及び更なる実施形態では0.5時間−1〜2時間−1の時間基準液空間速度(LHSV)、及び
1m3当たりの正規化m3で約500(Nm3/m3)〜約2500Nm3/m3、ある実施形態では約800Nm3/m3〜約2000Nm3/m3、及び更なる実施形態では約1000Nm3/m3〜約1500Nm3/m3の水素/油比。
約550℃〜約650℃、ある実施形態では、約580℃〜約630℃、及び更なる実施形態では約590℃〜約620℃の反応温度、
約1kg/cm2〜約20kg/cm2、ある実施形態では約1kg/cm2〜約10kg/cm2、更なる実施形態では約1kg/cm2〜約3kg/cm2の反応圧力、
約0.1秒〜約30秒間、ある実施形態では約0.1秒〜約10秒間、及び更なる実施形態では約0.2秒〜約0.7秒間の接触時間(反応器中で)、及び
約1:1〜約40:1、ある実施形態では約1:1〜約30:1、及び更なる実施形態では約10:1〜約30:1の触媒対供給材料比。
約480℃〜約650℃、ある実施形態では、約500℃〜約620℃、及び更なる実施形態では約500℃〜約600℃の反応温度、
約1kg/cm2〜約20kg/cm2、ある実施形態では約1kg/cm2〜約10kg/cm2、更なる実施形態では約1kg/cm2〜約3kg/cm2の反応圧力、
約0.7秒〜約10秒間、ある実施形態では約1秒〜約5秒間、更なる実施形態では約1秒〜約2秒間の接触時間(反応器中で)、及び
約1:1〜約15:1、ある実施形態では約1:1〜約10:1、更なる実施形態では約8:1〜約20:1の触媒対供給材料比。
脱金属化油並びに軽質及び重質減圧軽油留分を含有する供給材料を、連続流動水素化分解ユニットで水素化分解した。供給材料混合物は、889.5kg/Lの密度、2.32W%の硫黄、886ppmwの窒素、12.1W%の水素、及び1.2W%の微小残留炭素を特徴としていた。初留点は、216℃;5W%、337℃;10W%、371℃;30W%、432℃;50W%、469℃;70W%、510℃、90W%、585℃;95W%、632℃であり、最終沸点は、721℃だった。シリカ−アルミナ系触媒を、第1の水素化分解反応帯で使用した。第1段階の操業条件は、以下の通りだった:水素分圧は115bar、温度は385℃、時間基準液空間速度は0.27時間−1、及び水素対油比は1263:1。第2段階の操業条件は、以下の通りだった:水素分圧は115bar、温度は370℃、時間基準液空間速度は0.80時間−1、及び水素対油比は1263:1。375℃超で沸騰する材料の全体的な転換率は、70W%だった。USYゼオライト触媒を、第2の水素化分解反応帯で使用した。
54 導管
56 導管
57 供給材料入口
58 第1の水素化分解反応帯
60 第1の水素化分解反応帯出口
62 導管
63 入口
64 第2の水素化分解反応帯
68 出口
69 入口
70 分留帯
72 出口
72a 頂塔ガスの部分
74 出口
76 出口
78 出口
79 流出口
82 FCC反応及び分離帯
84 水及びガス出口
86 オレフィン出口
88 ガソリン出口
90 軽質循環油出口
90 FCC反応及び分離帯出口
91 重質循環油出口
91 FCC反応及び分離帯出口
92 流出流動
94 導管
96 導管
97 導管
97 入口
98 供給材料入口
100 FCCユニット
110 反応器/分離器
114 反応帯
116 分離帯
118 再生帯
120 装入物
122 導管又はパイプ
124 導管又はパイプ
128 燃焼空気流動
130 導管
132 ストリッパ
134 流動ライン
200 FCCユニット
210 反応器/分離器
212 上昇管
214 反応帯
216 分離帯
218 再生容器
218 再生帯
220 導管
222 導管
224 導管
226 導管
228 導管
230 導管
Claims (31)
- 水素化分解及び流動接触分解を含む、300℃を超える沸点を有する炭化水素を含有する供給材料を変換するための統合型プロセスであって、
a.前記供給材料及び水素を、第1の水素化分解触媒を含有する第1の水素化分解反応帯に導入して、第1の反応帯溶出物を生成するステップ、
b.前記第1の反応帯流出物及び随意に追加の水素を、第2の水素化分解触媒を含有する第2の水素化分解反応帯に送って、第2の反応帯流出物を生成するステップ、
c.前記第2の反応帯溶出物を分留帯に送って、少なくとも低沸点留分及び高沸点留分、及び随意に1つ又は複数の中間留分を生成するステップ、
d.前記残油留分を、オレフィン及びガソリンの形成を促進し、オレフィン消費反応を最小限に抑える条件下で操業する流動接触分解反応及び分離帯に送るステップ、
e.前記流動接触分解反応及び分離帯からオレフィンを回収するステップ、
f.前記流動接触分解反応及び分離帯からガソリンを回収するステップ、
g.前記流動接触分解反応及び分離帯からの残留循環油の少なくとも部分を、前記第1及び/又は第2の水素化分解反応帯に運搬するステップを含むプロセス。 - ステップ(g)が、前記残留循環油の部分を、前記第2の水素化分解反応帯に運搬することを含む、請求項1に記載のプロセス。
- ステップ(g)が、前記残留循環油の部分を、前記第1の水素化分解反応帯に運搬することを含む、請求項1に記載のプロセス。
- 前記流動接触分解反応及び分離帯からガスを吐出することを更に含む、請求項1に記載のプロセス。
- 前記分留帯からナフサを回収することを更に含む、請求項1に記載のプロセス。
- 前記分留帯から中間留分を回収することを更に含む、請求項1に記載のプロセス。
- 前記分留帯からの前記残留物留分の部分が、前記プロセスから取り出される、請求項1に記載のプロセス。
- 前記流出する部分が、前記残油留分の約1V%〜約10V%である、請求項7に記載のプロセス。
- ステップ(d)が、追加供給材料を流動接触分解反応及び分離帯に導入することを更に含む、請求項1に記載のプロセス。
- 前記流動接触分解反応及び分離帯が、下降流反応器を含む、請求項1に記載のプロセス。
- 前記流動接触分解反応及び分離帯が、上昇流反応器を含む、請求項1に記載のプロセス。
- ステップ(d)が、流動分解塩基触媒としての前記流動分解触媒及び触媒添加剤を含む流動分解触媒混合物を運搬することを含む、請求項1に記載のプロセス。
- 前記流動分解塩基触媒が、前記流動分解触媒混合物全体の約60重量%〜約95重量%を占める、請求項12に記載のプロセス。
- 前記流動分解塩基触媒が、粘土及び無機多孔性酸化物からなる群から選択される、請求項12に記載のプロセス。
- 前記流動分解塩基触媒が、0.5g/ml〜1.0g/mlのバルク密度、50ミクロン〜90ミクロンの平均粒径、50m2/g〜350m2/gの表面積、及び0.05ml/g〜0.5ml/gの細孔容積を有する、請求項14に記載のプロセス。
- 前記触媒添加剤が、形状選択的ゼオライトを含む、請求項12に記載のプロセス。
- 前記形状選択的ゼオライトが、Y型ゼオライトの平均細孔径よりも小さい平均細孔径により特徴付けられる、請求項16に記載のプロセス。
- 前記形状選択的ゼオライトが、ZSM−5ゼオライト、ゼオライトオメガ、SAPO−5ゼオライト、SAPO−11ゼオライト、SAPO−34ゼオライト、ペンタシル型アルミノケイ酸塩、及び前記形状選択的ゼオライトの少なくとも1つを含む組み合わせからなる群から選択される、請求項16に記載のプロセス。
- 前記形状選択的ゼオライトが、0.5g/ml〜1.0g/mlのバルク密度、50ミクロン〜90ミクロンの平均粒径、10m2/g〜200m2/gの表面積、及び0.01ml/g〜0.3ml/gの細孔容積を有する、請求項16に記載のプロセス。
- 前記流動分解触媒混合物が、約5重量%〜約40重量%の前記触媒添加剤を含む、請求項16に記載のプロセス。
- 前記触媒添加剤が、約20重量%から約70重量%の形状選択的ゼオライトを含む、請求項16に記載のプロセス。
- 前記触媒添加剤が、約30重量%から約60重量%の形状選択的ゼオライトを含む、請求項16に記載のプロセス。
- 統合型分解装置であって、
供給材料の供給源及び水素の供給源と液体連通している供給材料入口、及び
第1の反応帯出口を含み、
第1の水素化分解触媒を含有する、
第1の水素化分解反応帯と;
前記第1の水素化分解反応帯の第1の反応帯出口及び水素ガスの供給源と液体連通している少なくとも1つの入口、及び
第2の反応帯出口を含み、
第2の水素化分解触媒を含有する、
第2の水素化分解反応帯と;
前記第2の反応帯出口と液体連通している入口、
頂塔ガス出口、
残油出口、及び
随意に1つ又は複数の中間留分出口を含む
分留帯と;
前記分留帯の前記残油出口と液体連通している少なくとも1つの入口、
オレフィン出口、
ガソリン出口、及び
前記第2の水素化分解反応帯の前記入口と液体連通している、
少なくとも1つの循環油出口とを含む、
オレフィン及びガソリンの形成を促進し、オレフィン消費反応を最小限に抑える条件下で操業する流動接触分解反応及び分離帯と;
を含む装置。 - 前記少なくとも1つの循環油出口が、前記第1の水素化分解反応帯の前記供給材料入口とも液体連通している、請求項23に記載の装置。
- 前記分留帯の前記残油出口と液体連通している流出出口を更に含む、請求項23に記載の装置。
- 前記流動接触分解反応及び分離帯の前記入口が、前記分留帯の前記残油出口とは異なる供給材料の供給源と液体連通している、請求項23に記載の装置。
- 前記流動接触分解反応及び分離帯が、下降流反応器を含む、請求項23に記載の装置。
- 前記流動接触分解反応及び分離帯が、上昇流反応器を含む、請求項23に記載の装置。
- 生産量を測定するために前記出口の1つに構築及び配置されている少なくとも1つの流量計、及び
前記測定された生産量に基づいて調節の実施を指示するようにプログラムされている、前記流量計と電子的に通信するコントローラを更に含む、請求項23に記載の装置。 - 前記測定された生産量が、前記オレフィン出口での流速である、請求項29に記載の装置。
- 前記調節が、前記第1の水素化分解反応帯又は前記第2の水素化分解反応帯での変換効率を変更する、請求項29に記載の装置。
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EP2688982A1 (en) | 2014-01-29 |
US20130343957A1 (en) | 2013-12-26 |
US20120241359A1 (en) | 2012-09-27 |
US9101854B2 (en) | 2015-08-11 |
US10207196B2 (en) | 2019-02-19 |
CN103429709B (zh) | 2016-04-13 |
KR20140025400A (ko) | 2014-03-04 |
CN103429709A (zh) | 2013-12-04 |
KR101895644B1 (ko) | 2018-09-05 |
EP2688982A4 (en) | 2014-11-19 |
WO2012128973A1 (en) | 2012-09-27 |
JP6054365B2 (ja) | 2016-12-27 |
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