CN1237198A - 液体催化裂化室的反应器竖井 - Google Patents

液体催化裂化室的反应器竖井 Download PDF

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CN1237198A
CN1237198A CN97198345A CN97198345A CN1237198A CN 1237198 A CN1237198 A CN 1237198A CN 97198345 A CN97198345 A CN 97198345A CN 97198345 A CN97198345 A CN 97198345A CN 1237198 A CN1237198 A CN 1237198A
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vertical shaft
contact device
turbulent element
reactor
reactor vertical
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CN1122704C (zh
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许贝特斯·W·A·德赖斯
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Shell Internationale Research Maatschappij BV
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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
    • 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
    • B01J8/34—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 stationary packing material in the fluidised bed, e.g. bricks, wire rings, baffles
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • 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
    • 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
    • B01J8/1845—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised
    • 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
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00823—Mixing elements
    • B01J2208/00831—Stationary elements
    • B01J2208/0084—Stationary elements inside the bed, e.g. baffles

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)

Abstract

一种液体催化裂化室的反应器竖井(1),该反应器竖井具有一轴向通路(5),该通路在接受碳氢化合物进料和催化剂质点的进料口端与排出流出物和催化剂质点的出口端之间延伸;该反应器竖井设有多个接触装置(6,7,8),该接触装置在轴向通路中,沿轴向彼此相隔一段距离排列,其中,每个接触装置(6,7,8)包括一个具有一段弧形的扰流元件(10)。

Description

液体催化裂化室的反应器竖井
本发明涉及一种液体催化裂化室的反应器竖井。这种反应器竖井具有一轴向通路，该通路在接受碳氢化合物进料和催化剂质点的进料口端与排出流出物(effluent)和催化剂质点的出口端之间延伸。
除反应器竖井外，液体催化裂化室可包括反应器罐，反应器竖井的出口通入其中；和再生罐。当正常运行时，再生的催化剂质点和碳氢化合物进料从反应器竖井的进料口供给。在竖井中进料被蒸发，形成催化剂质点在气态进料中的混合体弥散状态。在反应器竖井中，进料发生催化裂化，从而获得一种进料的气态混合物和产品。由于进料气态混合体与产品的混合物沿竖井反应器变化，这种混合体将被看作是“流出物”。催化剂质点在气态流出物中的弥散物，在摄氏500至540度温度或高于此温度时留在反应器竖井中。弥散物进入反应器罐的一个分离器系统，在这里，气态流出物从催化剂质点中分离。气态流出物从反应器罐的上端被除去，而催化剂质点则从反应器罐的下端排出，在这里，催化剂质点被剥离。被剥离的催化剂质点进入再生罐，在这里，当裂化物在高温熔化，焦炭沉积催化剂质点上，以获得氧化产品和再生的催化剂。氧化产品从再生罐的上端除去，而再生催化剂得以重用。
在反应器竖井中，气体的平均线速度在10至30m/s范围内，而催化剂质点的平均线速度高达25m/s。催化剂质点本质上将与气态反应混合体同步移动，不过最好在气体与质点之间存在小的滑动。
由于裂化反应发生在催化剂质点，在气态流出物与催化剂质点之间的良好接触，本质上达到发生转变的足够程度。
为了改善催化剂质点与气态流出物间的接触，美国专利No.3353925建议在反应器竖井设置多个接触装置，该装置在反应器竖井轴向通路上，沿轴向彼此相隔一段距离排列。已知的接触装置包括一环形扰流元件。其必然结果是，在接触装置处的通路直径小于竖井轴向通路的直径。这样，环形扰流元件贯穿入通路愈深(指环形扰流元件的内径愈小---译注)，通路的直径(从而通路的面积)变得愈小。这对于接触装置内的压力降有一种不利的影响，因为，通路的面积愈小，压力降变得更大。
本申请人现在考虑一种接触装置，该装置具有较大的贯穿深度，但在接触装置内的压力降可维持在可以接受的水平。
为此目的，根据本发明的液体催化裂化室的反应器竖井，具有一轴向通路，该通路在接受碳氢化合物进料和催化剂质点的进料口端与排出流出物和催化剂质点的出口端之间延伸，并设有多个接触装置，该接触装置在轴向通路中，沿轴向彼此相隔一段距离排列，其中每个接触装置包括一个具有一段弧形的扰流元件。
本发明的扰流元件的优点，在于其可以容易地设置在现有反应器竖井的轴向通路中。
下面，参看附图，通过例子对本发明给予详细说明。
图1示出了根据本发明的反应器竖井纵剖面的原理图；和
图2示出了图1的Ⅱ-Ⅱ剖面。
参看图1和图2。反应器竖井用数字1表示。为清楚起见，反应器竖井1的壁2上的任何镶衬均未示出。此外，因为液体催化裂化室是众所周知的，催化裂化室的其余部分就不示出。
一般立式反应器竖井1具有一轴向通路5，该通路在接受碳氢化合物进料和催化剂质点的进料口端(未示出)与排出流出物和催化剂质点的出口端(未示出)之间延伸。
反应器竖井1设有多个接触装置6、7和8。该接触装置6、7和8在轴向通路5中，沿轴向彼此相隔一段距离排列。每个接触装置6、7和8包括一平板扰流元件10，该扰流元件具有一弧段外形和矩形剖面。平板扰流元件10的贯穿深度为弧段拱高12。平板扰流元件10可用任何已知的方法连接在反应器竖井的壁上。
可以看出，接触元件7只有一个平板扰流元件10，而每一接触元件6和8包括一对相互面对放置的平板扰流元件10。扰流元件的合适数量不大于4。接触装置的轴向间距要求不严格，通常不应大于轴向通路5的直径。
当正常运行时，催化剂质点在气态流出物中的弥散物，通过轴向通路5，弥散物流被平板扰流元件10扰动，从而使催化剂质点与气态流出物获得有效的混合。
图2中用虚线所示的圆15，表示根据现有技术的环形平板扰流元件的内圆周，该扰流元件具有与本发明之平板扰流元件相同的贯穿深度。很清楚，为现有技术的接触装置所固有的通路面积(相当于圆15所包容的面积)大大小于根据本发明接触装置所固有的的通路面积。因此，对于相同的贯穿深度，根据本发明的接触装置比现有技术的接触装置所带来的压力降小得多。
用虚线所示的圆16表示根据现有技术另一个环形扰流元件的内圆周。圆16的直径是这样选择的，该扰流元件所形成的通路面积(相当于圆16所包容的面积)，与根据本发明的接触装置所固有的面积相同。很清楚，现有技术的环形平板扰流元件所具有的贯穿深度，大大小于本发明的平板扰流元件的贯穿深度。
相邻接触装置的平板扰流元件可以直接放置在另一个之上。不过，一个接触装置的平板扰流元件合适的排列方式，是安排成与相邻接触装置的平板扰流元件交错排列，如图所示，相邻接触装置的平板扰流元件安排成彼此垂直。此角度并不需要是90度，可以是任何锐角。
此外，平板扰流元件还可以包括一种向内的唇边凸起。
如图所示，平板扰流元件10的中心平面20，设置成垂直于反应器竖井1的纵向中心轴线21。在另一个实施例中，扰流元件可以安排成相对于反应器竖井1的纵向中心轴线21是倾斜的。例如，中心平面与纵向中心轴线的夹角为5度至20度。
本发明的平板扰流元件，如参考附图所讨论的那样，具有矩形剖面。除此之外，该剖面可以是三角形，其中，每一剖面的三角形顶点均位于一直线上。

Claims (4)

1．一种液体催化裂化室的反应器竖井，该反应器竖井具有一轴向通路，该通路在接受碳氢化合物进料和催化剂质点的进料口端与排出流出物和催化剂质点的出口端之间延伸；该反应器竖井设有多个接触装置，该接触装置在轴向通路中，沿轴向彼此相隔一段距离排列，其中，每个接触装置包括一个具有一段弧形的扰流元件。
2．如权利要求1所述的反应器竖井，其中，每个接触装置包括一对相面对放置的扰流元件。
3．如权利要求1或2所述的反应器竖井，其中，接触装置的扰流元件相对于相邻接触装置的扰流元件设置成交错排列。
4．如权利要求1至3其中之一所述的反应器竖井，其中，扰流元件还包括一种向内的唇边凸起。
CN97198345A 1996-09-30 1997-09-29 液体催化裂化室的反应器竖井 Expired - Fee Related CN1122704C (zh)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP96202726A EP0832956A1 (en) 1996-09-30 1996-09-30 Reactor riser of a fluidized-bed catalytic cracking plant
EP96202726.4 1996-09-30

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CN1237198A true CN1237198A (zh) 1999-12-01
CN1122704C CN1122704C (zh) 2003-10-01

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EP (2) EP0832956A1 (zh)
JP (1) JP3948755B2 (zh)
CN (1) CN1122704C (zh)
AR (1) AR009100A1 (zh)
AT (1) ATE192479T1 (zh)
AU (1) AU711645B2 (zh)
BR (1) BR9712122A (zh)
CA (1) CA2265604C (zh)
DE (1) DE69701891T2 (zh)
ES (1) ES2148945T3 (zh)
GR (1) GR3034019T3 (zh)
WO (1) WO1998014533A1 (zh)
ZA (1) ZA978642B (zh)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2024078905A1 (fr) * 2022-10-13 2024-04-18 IFP Energies Nouvelles Réacteur à lit fluidisé à co-courant gaz-solide descendant à écoulement homogène

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6613290B1 (en) 2000-07-14 2003-09-02 Exxonmobil Research And Engineering Company System for fluidized catalytic cracking of hydrocarbon molecules
EP2367621B1 (en) 2008-12-22 2015-08-05 Shell Internationale Research Maatschappij B.V. Process and reactor system for the preparation of an olefinic product
FR3064197B1 (fr) * 2017-03-24 2019-03-22 Total Raffinage Chimie Dispositif d'injection de charge ameliore pour une unite fcc.
FR3064196B1 (fr) * 2017-03-24 2021-10-15 Total Raffinage Chimie Dispositif d'injection de charge d'une unite fcc a perte de charge limitee.

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Publication number Priority date Publication date Assignee Title
US2763516A (en) * 1951-10-01 1956-09-18 Phillips Petroleum Co Conveying of fluidized mass of particles and apparatus therefor
NL293037A (zh) * 1962-05-23

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2024078905A1 (fr) * 2022-10-13 2024-04-18 IFP Energies Nouvelles Réacteur à lit fluidisé à co-courant gaz-solide descendant à écoulement homogène
FR3140776A1 (fr) * 2022-10-13 2024-04-19 IFP Energies Nouvelles Réacteur à lit fluidisé à co-courant gaz-solide descendant à écoulement homogène.

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CA2265604A1 (en) 1998-04-09
ZA978642B (en) 1998-03-26
BR9712122A (pt) 1999-08-31
AU4780297A (en) 1998-04-24
EP0832956A1 (en) 1998-04-01
CN1122704C (zh) 2003-10-01
EP0931121A1 (en) 1999-07-28
AU711645B2 (en) 1999-10-21
JP2001501245A (ja) 2001-01-30
DE69701891T2 (de) 2000-10-05
DE69701891D1 (de) 2000-06-08
EP0931121B1 (en) 2000-05-03
AR009100A1 (es) 2000-03-08
CA2265604C (en) 2006-10-31
JP3948755B2 (ja) 2007-07-25
ATE192479T1 (de) 2000-05-15
ES2148945T3 (es) 2000-10-16
GR3034019T3 (en) 2000-11-30
WO1998014533A1 (en) 1998-04-09

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