JP6054366B2 - 統合型水素化分解及び流動接触分解システム及びプロセス - Google Patents
統合型水素化分解及び流動接触分解システム及びプロセス Download PDFInfo
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- JP6054366B2 JP6054366B2 JP2014501132A JP2014501132A JP6054366B2 JP 6054366 B2 JP6054366 B2 JP 6054366B2 JP 2014501132 A JP2014501132 A JP 2014501132A JP 2014501132 A JP2014501132 A JP 2014501132A JP 6054366 B2 JP6054366 B2 JP 6054366B2
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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
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G15/00—Cracking of hydrocarbon oils by electric means, electromagnetic or mechanical vibrations, by particle radiation or with gases superheated in electric arcs
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- 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
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/12—Silica and alumina
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- 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
- B01J29/084—Y-type faujasite
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- 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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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/80—Mixtures of different zeolites
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1048—Middle distillates
- C10G2300/1059—Gasoil having a boiling range of about 330 - 427 °C
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/301—Boiling range
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4081—Recycling aspects
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/20—C2-C4 olefins
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Physics & Mathematics (AREA)
- Electromagnetism (AREA)
- Mechanical Engineering (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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へ導入して、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、並びに随意に1つ又は複数の中間留分を生成するステップ、
c.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される流動接触分解反応及び分離帯に送るステップ、
d.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、
e.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、
f.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並びに水素を、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運搬して、第2段階流出物を生成するステップ、及び
g.第2段階流出物の少なくとも部分を、分留帯及び/又は第1の水素化分解反応帯へと再循環させるステップを含む。
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、水素化分解ユニットの第1段階で水素化分解した。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。
8 導管
10 導管
11 入口
12 第1の水素化分解反応帯
14 第1の水素化分解反応帯出口
15 入口
16 分留帯
18 出口
18a 頂塔ガスの部分
20 出口
22 出口
24 出口
26 導管
28 供給材料入口
32 FCC反応及び分離帯
34 水及びガス出口
36 オレフィン出口
38 ガソリン出口
40 軽質循環油出口
40 FCC反応及び分離帯出口
41 重質循環油出口
41 FCC反応及び分離帯出口
42 流出流動
43 導管
44 導管
45 入口
46 第2の水素化分解反応帯
47 第2の水素化分解反応帯出口
48 導管
49 流出口
50 導管
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 (27)
- 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、中間留分及び軽質オレフィン、プロピレン及びブチレンに変換するための統合型水素化分解及び流動接触分解プロセスであって、
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、並びに随意に1つ又は複数の中間留分を生成するステップ、
c.前記高沸点留分を流動接触分解反応及び分離帯に送り、前記流動接触分解反応及び分離帯が、オレフィン消費反応を最小限に抑える条件下で操業し、下降流構成である流動接触分解反応器を含み、580℃〜630℃の範囲の反応温度、10:1〜30:1の触媒対油比、並びに0.1秒〜1秒の触媒粒子及び前記高沸点留分間の接触時間で操業するステップ、
d.前記供給材料の容積に基づき、少なくとも10V%〜20V%の量の軽質オレフィン、プロピレン及びブチレンを、前記流動接触分解反応及び分離帯から回収するステップ、
e.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、
f.前記流動接触分解反応及び分離帯からの残りの循環油の少なくとも一部分並びに水素を、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運搬して、第2段階溶出物を生成するステップ、及び
g.前記第2段階溶出物の少なくとも一部分を、前記分留帯及び/又は前記第1の水素化分解反応帯に再循環させるステップを含み
前記統合型水素化分解及び流動接触分解プロセスは、前記第1及び第2の水素化分解反応帯のいずれか又は両方において水素化分解ユニットの変換率を変更することにより、所望の産物スレートに基づいて、柔軟性を提供するように操業され、前記水素化分解ユニットの変換率の変更は、
前記第1の又は第2の水素化分解反応帯において効率が低下した触媒で操業することにより、残油生産を促進し、流動接触分解反応器への供給材料の量を増加させ、それによりその産物オレフィン及び/又はガソリンの増加をもたらすこと、又は
比較的低いレベルの水素供給で操業することにより、水素の費用を低減し、流動接触分解反応器への供給材料の量を増加させ、それによりその産物オレフィン及び/又はガソリンの増加をもたらすこと
の1つまたは複数によるものであり、前記第1の又は第2の水素化分解反応帯における前記操業条件は、1m3当たりの正規化m3で500(Nm 3 /m 3 )〜2500Nm3/m3の水素/油比を含む、プロセス。 - 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、中間留分及び軽質オレフィン、プロピレン及びブチレンに変換するための統合型水素化分解及び流動接触分解プロセスであって、
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、
c.前記高沸点留分を流動接触分解反応及び分離帯に送り、前記流動接触分解反応及び分離帯が、オレフィン消費反応を最小限に抑える条件下で操業し、上昇流構成である流動接触分解反応器を含み、500℃〜620℃の範囲の反応温度、8:1〜20:1の触媒対油比、並びに1秒〜2秒の触媒粒子及び前記高沸点留分間の接触時間で操業するステップ、
d.前記初期供給材料の容積に基づき、少なくとも10V%〜20V%の量の軽質オレフィン、プロピレン及びブチレンを、前記流動接触分解反応及び分離帯から回収するステップ、
e.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、
f.前記流動接触分解反応及び分離帯からの残りの循環油の少なくとも一部分及び水素を、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運搬して、第2段階溶出物を生成するステップ、及び
g.前記第2段階溶出物の少なくとも一部分を、前記分留帯及び/又は前記第1の水素化分解反応帯に再循環させるステップを含み
前記統合型プロセスは、前記第1及び第2の水素化分解反応帯のいずれか又は両方において水素化分解ユニットの変換率を変更することにより、所望の産物スレートに基づいて、柔軟性を提供するように操業され、前記水素化分解ユニットの変換率の変更は、
前記第1の又は第2の水素化分解反応帯において効率が低下した触媒で操業することにより、残油生産を促進し、流動接触分解反応器への供給材料の量を増加させ、それによりその産物オレフィン及び/又はガソリンの増加をもたらすこと、又は
比較的低いレベルの水素供給で操業することにより、水素の費用を低減し、流動接触分解反応器への供給材料の量を増加させ、それによりその産物オレフィン及び/又はガソリンの増加をもたらすこと
の1つまたは複数によるものであり、前記第1の又は第2の水素化分解反応帯における操業条件は、1m3当たりの正規化m3で500(Nm 3 /m 3 )〜2500Nm3/m3の水素/油比を含む、プロセス。 - ステップ(g)が、前記第2段階溶出物の部分を、前記分留帯に運搬することを含む、請求項1又は2に記載のプロセス。
- ステップ(g)が、前記第2段階溶出物の部分を、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又は2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又は2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又は2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又は2に記載のプロセス。
- 前記分留帯からの前記高沸点留分の部分が取り出される、請求項1又は2に記載のプロセス。
- 前記取り出される部分が、前記高沸点留分の1V%〜10V%である、請求項8に記載のプロセス。
- ステップ(c)が、追加供給材料を前記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又は2に記載のプロセス。
- ステップ(c)が、流動分解塩基触媒としての前記流動分解触媒を含む流動分解触媒混合物、及び触媒添加剤を運搬することを含む、請求項1又は2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60重量%〜95重量%を占める、請求項11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11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12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11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15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15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15に記載のプロセス。
- 前記液体分解触媒混合物が、5重量%〜40重量%の前記触媒添加剤を含む、請求項15に記載のプロセス。
- 前記触媒添加剤が、20重量%から70重量%の形状選択的ゼオライトを含む、請求項15に記載のプロセス。
- 前記触媒添加剤が、30重量%から60重量%の形状選択的ゼオライトを含む、請求項15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
少なくとも1つの循環油出口を含む、
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;
前記流動接触分解反応及び分離帯の循環油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
前記分留帯の前記入口と液体連通している第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;
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つの流量計と;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含み
前記コントローラにより指示される前記調節は、
前記第1の又は第2の水素化分解反応帯において効率が低下した触媒で操業することにより、残油生産を促進し、流動接触分解反応器への供給材料の量を増加させ、それによりその産物オレフィン及び/又はガソリンの増加をもたらすこと;又は
比較的低いレベルの水素供給で操業することにより、水素の費用を低減し、流動接触分解反応器への供給材料の量を増加させ、それによりその産物オレフィン及び/又はガソリンの増加をもたらすこと
の1つまたは複数によるものであり、前記第1の又は第2の水素化分解反応帯における操業条件は、300℃〜500℃の反応温度、60Kg/cm2〜300Kg/cm2の水素分圧、0.1h-1〜10h-1の時間基準液空間速度(LHSV)、及び1m3当たりの正規化m3で500(Nm 3 /m 3 )〜2500Nm3/m3の水素/油比を含む、装置。 - 前記第2段階溶出物出口が、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22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22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22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22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22に記載の装置。
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US9101853B2 (en) | 2015-08-11 |
US20120241358A1 (en) | 2012-09-27 |
EP2688983A4 (en) | 2014-11-19 |
US20130343956A1 (en) | 2013-12-26 |
KR20140030163A (ko) | 2014-03-11 |
EP2688983A1 (en) | 2014-01-29 |
CN103429708B (zh) | 2016-03-09 |
KR101895645B1 (ko) | 2018-09-05 |
CN103429708A (zh) | 2013-12-04 |
US10232285B2 (en) | 2019-03-19 |
WO2012128975A1 (en) | 2012-09-27 |
JP2014512428A (ja) | 2014-05-22 |
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