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WO2003083014A1 - Procede et appareil fcc de regulation automatique du recyclage du catalyseur - Google Patents

Procede et appareil fcc de regulation automatique du recyclage du catalyseur Download PDF

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Publication number
WO2003083014A1
WO2003083014A1 PCT/US2002/009949 US0209949W WO03083014A1 WO 2003083014 A1 WO2003083014 A1 WO 2003083014A1 US 0209949 W US0209949 W US 0209949W WO 03083014 A1 WO03083014 A1 WO 03083014A1
Authority
WO
WIPO (PCT)
Prior art keywords
catalyst
conduit
regenerated
spent
regenerated catalyst
Prior art date
Application number
PCT/US2002/009949
Other languages
English (en)
Inventor
Neal E. Cammy
Ricardo Castillo
Original Assignee
Uop Llc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Uop Llc filed Critical Uop Llc
Priority to PCT/US2002/009949 priority Critical patent/WO2003083014A1/fr
Priority to AU2002303193A priority patent/AU2002303193A1/en
Publication of WO2003083014A1 publication Critical patent/WO2003083014A1/fr

Links

Classifications

    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
    • 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
    • B01J8/26—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
    • 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
    • C10G11/187—Controlling or regulating
    • 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
    • B01J2208/00008—Controlling the process
    • B01J2208/00548—Flow
    • 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
    • B01J2208/00008—Controlling the process
    • B01J2208/00654—Controlling the process by measures relating to the particulate material
    • B01J2208/00663—Concentration

Definitions

  • This invention relates to a fluidized catalytic cracking (FCC) process and apparatus in which spent catalyst particles are sent to a regenerator before being sent back to a reaction zone while other catalyst particles are recycled back to the cracking zone without regeneration. Specifically, this invention relates to controlling the circulation rate of unregenerated, spent catalyst recycled back to the reaction zone.
  • FCC fluidized catalytic cracking
  • Catalytic cracking is accomplished by contacting hydrocarbons in a reaction zone with a catalyst composed of finely divided particulate material. As the cracking reaction proceeds, substantial amounts of coke are deposited on the catalyst. A high temperature regenerator within a regeneration zone operation burns coke from the catalyst. Coke-containing catalyst, referred to generally by those skilled in the art as spent catalyst, is continually removed from the reaction zone and replaced by essentially coke-free catalyst from the regeneration zone. Fluidization of the catalyst particles by various gaseous streams facilitates the transport of catalyst between the reaction zone and regeneration zone.
  • spent catalyst is typically sent from the base of the stripping vessel to the regenerator through a spent catalyst conduit.
  • Regenerated catalyst is passed from the regenerator vessel through a regenerated catalyst conduit to the base of the reaction zone.
  • the circulation rate of the spent catalyst through the spent catalyst conduit is maintained by a spent catalyst control valve, and the circulation rate of the catalyst through the regenerated catalyst conduit is maintained by a regenerated catalyst control valve.
  • Spent catalyst that will not undergo regeneration is recycled either from the separator vessel or, specifically, the stripping vessel to the base of the riser by a recycled catalyst conduit.
  • a recycled catalyst control valve regulates the recycled catalyst circulation rate.
  • the respective catalyst circulation rate through the spent catalyst control valve, the regenerated catalyst control valve and the recycled catalyst control valve is approximated using the density in the respective catalyst conduit, the differential pressure across the control valve and the position of the control valve relative to fully opened.
  • the spent catalyst control valve automatically controls the circulation rate of spent catalyst from the separator vessel to the regenerator to maintain a constant catalyst level in the separator.
  • the regenerated catalyst control valve to maintain a constant temperature of the separator vessel automatically controls the circulation rate of hot regenerated catalyst from the regenerator to the riser.
  • the controls that operate each of the spent catalyst and regenerated catalyst control valves also include a low differential pressure override.
  • the present invention relates to an apparatus for the fluidized catalytic cracking of hydrocarbons.
  • the apparatus comprises a reaction zone in which blended catalyst is contacted with a hydrocarbon feed.
  • a separator vessel receives effluent from the reaction zone and separates the effluent into a vapor product and spent catalyst.
  • a recycled catalyst conduit communicative with the separator vessel passes spent catalyst to the reaction zone.
  • the recycled catalyst conduit includes a recycled catalyst control valve for regulating spent catalyst circulation.
  • a regeneration zone removes carbon from the spent catalyst to provide regenerated catalyst.
  • a spent catalyst conduit communicative between the separator vessel and the regeneration zone passes spent catalyst to the regeneration zone.
  • a regenerated catalyst conduit communicative between the regeneration zone and the reaction zone passes regenerated catalyst from the regeneration zone to the reaction zone.
  • the regenerated catalyst is blended with the spent catalyst in the reaction zone to provide the blended catalyst.
  • a recycled catalyst controller sets a position of the recycled catalyst control valve dependent on whether a relationship between the circulation rate of spent catalyst through the recycled catalyst conduit and the circulation rate of regenerated catalyst through the regenerated catalyst conduit meets a preset condition.
  • FIGURE is an elevational schematic view showing an FCC unit in accordance with this invention.
  • the FIGURE shows a typical schematic arrangement of an FCC unit 2 arranged in accordance with this invention.
  • the description of this invention in the context of the specific process arrangement shown is not meant to limit it to the details disclosed therein.
  • the FCC unit 2 shown in the FIGURE consists of a reaction zone 4 comprising an elongate riser 6 and a separator vessel 8, and a regeneration zone 10 comprising a regenerator 12.
  • the arrangement circulates catalyst and contacts feed in the manner hereinafter described.
  • the catalyst that enters the riser 6 can include any of the well-known catalysts that are used in the art of fluidized catalytic cracking. These compositions include amorphous-clay type catalysts or high activity, crystalline alumina silica or zeolite containing catalysts.
  • FCC feedstocks suitable for processing by the method of this invention, include conventional FCC feeds and higher boiling or residual feeds.
  • the most common of the conventional feeds is a vacuum gas oil which is typically a hydrocarbon material having a boiling range of from 343° to 552°C (650° to 1025°F) and is prepared by vacuum fractionation of atmospheric residue.
  • Riser 6 is one type of conversion vessel that can be used in conjunction with this invention.
  • the riser type conversion vessel comprises a conduit for the pneumatic conveyance of the blended catalyst mixture and the feed stream.
  • the base of the riser 6 may include a blending vessel 14.
  • Feed is introduced into the riser 6 somewhere between inlet 28 and substantially upstream from an outlet 30.
  • the feed enters by nozzle 17 in the FIGURE, usually in a lower portion of the riser 6.
  • the feed will ordinarily have a temperature in a range of from 149° to 316°C (300° to 600°F). Additional amounts of feed may be added downstream of the initial feed point.
  • a regenerated catalyst conduit 18 passes regenerated catalyst from the regenerator 12 into the blending vessel 14 at a circulation rate regulated by a control valve such as slide valve 20.
  • a recycled catalyst conduit 22 passes catalyst from separator vessel 8 at a circulation rate regulated by a control valve such as slide valve 24 into blending vessel 14. Fluidizing gas passed into blending vessel 14 by a nozzle 26 contacts the catalyst and maintains the catalyst in a fluidized state to mix the recycled catalyst and regenerated catalyst.
  • the regenerated catalyst will have a substantially higher temperature than the recycled catalyst.
  • Regenerated catalyst from the regenerated catalyst conduit 18 will usually have a temperature in a range from 593° to 760°C (1100° to 1400°F) and, more typically, in a range of from 649° to 760°C (1200° to 1400°F).
  • the temperature of the recycled catalyst will usually be in a range of from 482° to 621°C (900° to 1150°F).
  • the relative proportions of the recycled catalyst and regenerated catalyst will determine the temperature of the blended catalyst mixture that contacts the feed.
  • the blended catalyst mixture will usually range from 538° to 760°C (1000° to 1400°F) and, more preferably is in a range of from 566° to 677°C (1050° to 1250°F).
  • the ratio of recycled catalyst to regenerated catalyst entering the blending zone will be in a broad range of from 0.1 to 5 and more typically in a range of from 0.5 to 1.0.
  • the separator vessel 8 typically includes a stripping vessel 32.
  • the blended catalyst mixture and reacted feed vapors are then discharged from the end of riser 6 through an outlet 30 into the stripping vessel 32 of the separator vessel 8.
  • a swirl arm arrangement 31, provided at the end of riser 6 imparts a tangential velocity to the exiting catalyst and converted feed mixture to separate a product vapor stream from a collection of catalyst particles covered with substantial quantities of coke and generally referred to as "spent catalyst".
  • Direct conduit 37 passes a product vapor stream to a cyclone separator 34 in a primary chamber 39 of the separator vessel 8.
  • the cyclone separator 34 further removes catalyst particles from the product vapor stream to reduce particle concentrations to very low levels.
  • Product vapors comprising cracked hydrocarbons and some catalyst exit the top of separator vessel 8 through conduit 36 via plenum chamber 33.
  • Catalyst separated by cyclone separator 34 returns to the separator vessel 8 through dipleg conduits 35 into a dense catalyst bed (not shown).
  • Catalyst drops through the stripping vessel 32 that removes adsorbed hydrocarbons from the surface of the catalyst by counter-current contact with steam. Steam enters the stripping vessel 32 through at least one line 40.
  • Spent catalyst stripped of hydrocarbon vapor leave the bottom of stripping vessel 32 through a spent catalyst conduit 42 at a rate regulated by a control valve such as slide valve 46.
  • Spent catalyst for recycled to the base of the riser 6 may be withdrawn from the separator vessel 8 or even riser 6 after the spent catalyst has undergone a sufficient reduction in temperature.
  • Spent catalyst is most typically withdrawn downstream of the riser 6 and, more typically, from the stripping vessel 32.
  • the FIGURE depicts the withdrawal of spent catalyst from a lower portion of the stripping vessel 32.
  • a recycled catalyst conduit 22 transfers one portion of the spent catalyst exiting the separator vessel 8 back to the blending vessel 14 as recycled catalyst.
  • a spent catalyst conduit 42 transfers another portion of the spent catalyst to the regenerator 12 for the removal of coke in the regeneration zone 10.
  • spent catalyst transferred to the regenerator 12 via spent catalyst conduit 42 undergoes the typical combustion of coke from the surface of the catalyst particles by contact with an oxygen-containing gas.
  • the oxygen-containing gas enters the bottom of the regenerator 12 via an inlet 38 and passes through a dense fluidizing bed of catalyst (not shown). Flue gas consisting primarily of CO or CO2 passes upward from the dense bed into a dilute phase of regenerator 12.
  • a separator such as the cyclones 44 and 45, remove entrained catalyst particles from the rising flue gas before the flue gas exits the vessel through an outlet 48.
  • a level indicating controller (LIC) 50 receives a signal of the levels of the catalyst in the primary chamber 39 and in the stripping vessel 32 of the separator vessel 8.
  • the LIC 50 signals to a low signal selector (LSS) 52 a setting for the spent catalyst slide valve 46 relative to fully open to bring the respective levels in the separator vessel 8 and in the stripping vessel 32 to the desired preset levels.
  • a pressure differential transmitter (PDT) 53 senses and determines a differential pressure across spent catalyst slide valve 46 and signals a pressure differential to pressure differential indicating controller (PDIC) 54.
  • PDIC pressure differential indicating controller
  • the PDIC 54 signals a setting for the spent catalyst slide valve to the LSS 52.
  • a pressure differential transmitter (PDT) 61 senses and determines a pressure differential across the regenerated catalyst slide valve 20.
  • the PDT signals the pressure differential to the pressure differential indicating controller 64 (PDIC) which signals a setting to a low signal selector (LSS) 62.
  • a temperature indicating controller (TIC) 60 receives a temperature signal of the effluent gas from the separator vessel 8 in conduit 36, and signals a setting to the LSS 62 designed to open or close the slide valve 20 to effect the preset temperature desired in the separator vessel 8. If the differential pressure across the slide valve 20 is greater than an override setpoint, typically 0.14 kg/cm-2 (2 lbs/in ⁇ ), the LSS 62 will select and signal the slide valve 20 to adjust to the setting signaled from the
  • the LSS 62 will signal the lowest setting to the regenerated catalyst slide valve 20.
  • the regenerated catalyst conduit 18 and the recycled catalyst conduit 22 include instrumentation to determine the circulation rate through the respective slide valves 20 and 24. It should be understood that the determinations of the circulation rates are not precise, but they are sufficient for the purpose of controlling operation of the FCC unit 2.
  • the circulation rate is determined by a formulation of the density of the recycled catalyst stream, the position of the respective slide valve relative to fully open as indicated by the setting thereof and the differential pressure across the respective slide valve.
  • the instrumentation for determining the circulation rate of regenerated catalyst through the regenerated catalyst slide valve 20 includes the following. Density in the regenerated catalyst conduit 18 is determined by density indicator (Dl) 65 which factors readings from a pressure differential transmitter (PDT) 63 with connections placed at different heights along the regenerated catalyst conduit 18 upstream of the regenerated catalyst slide valve 20. The pressure differential across the slide valve 20 is determined by a signal from a pressure differential transmitter (PDT) 61 with connections placed upstream and downstream of the slide valve 20. The PDT 61 signals the pressure differential to a pressure differential indicating controller (PDIC) 64.
  • Dl density indicator
  • PDT pressure differential transmitter
  • PDIC pressure differential indicating controller
  • the Dl 65 signals a density value
  • the PDIC 64 signals a pressure differential value
  • the actuator 21 signals a value for the setting of the slide valve 20 all to a flow computer (FY) 69.
  • the FY 69 determines the flow rate of the regenerated catalyst based on the density, pressure differential and valve setting signals received and transmits the regenerated catalyst circulation rate to the a flow indicator (FI) 66.
  • the FI 66 signals the determined regenerated catalyst circulation rate to a flow fraction computer (FFY) 70.
  • the instrumentation for determining the circulation rate of spent catalyst through the recycled catalyst slide valve 24 includes the following. Density in the recycled catalyst conduit 22 is determined by density indicator (Dl) 73 which factors readings from a pressure differential transmitter (PDT) 71 with connections placed at different heights along the recycled catalyst conduit 22 upstream of the recycled catalyst slide valve 24. The pressure differential across the slide valve 24 is determined by a signal from a pressure differential transmitter (PDT) 77 with connections placed upstream and downstream of the slide valve 24. The PDT 77 signals the pressure differential to a pressure differential indicating controller (PDIC) 78.
  • Dl density indicator
  • PDT pressure differential transmitter
  • PDIC pressure differential indicating controller
  • the Dl 73 signals a density value
  • the PDIC 78 signals a pressure differential value
  • the actuator 25 signals a value for the setting of the slide valve 24 all to a flow computer (FY) 67.
  • the FY 67 determines the flow rate of the recycled catalyst based on the density, pressure differential and valve setting signals received and transmits the recycled catalyst circulation rate to the a flow indicator (FI) 68.
  • the FI 68 signals the determined recycled catalyst circulation rate to the FFY 70.
  • the spent catalyst conduit 42 may include similar instrumentation for determination of the spent catalyst circulation rate but it is not necessary for purposes of the invention.
  • the FFY 70 determines a process variable based on a relationship between the circulation rate of spent catalyst through the recycled catalyst conduit 22 and the circulation rate of regenerated catalyst through the regenerated catalyst conduit 18. It is preferred that this relationship be a ratio of a sum of the regenerated catalyst circulation rate and the spent catalyst circulation rate to the regenerated catalyst circulation rate:
  • the FFY 70 determines the process variable and signals an outputted process variable to a flow fraction indicating controller (FFIC) 72 which compares the process variable to a preset value. If there is a difference between the actual process variable and the preset value, then the FFIC 72 signals to a low signal selector (LSS) 74 a setting to which the slide valve 24 should be positioned to return the process variable to the preset value.
  • LSS 74 also receives output settings for the slide valve 24 from a temperature indicating controller (TIC) 76 that monitors the temperature of the regeneration zone 10 and the pressure differential indicating controller (PDIC) 78 that monitors the differential pressure across the slide valve 24.
  • TIC temperature indicating controller
  • PDIC pressure differential indicating controller
  • the TIC 76 and the PDIC 78 are overrides, they will typically only signal settings of 100% open to the LSS 74. Hence, the setting signaled by the FFIC 72 will typically control the setting of the slide valve 24. However, if the regenerator temperature exceeds the predetermined override setpoint, typically 732°C (1350°F) or the differential pressure across the slide valve 24 is less than or equal to the override setpoint, typically 0.14 kg/cm ⁇ (2 lbs/in ⁇ ), the respective indicating controller will signal a setting of the position of the slide valve 24 which is less than 100% fully open. Again, this LSS 74 will select the lowest setting and output that lowest setting to the actuator 25 for slide valve 24.
  • the slide valve 24 may be controlled automatically based on a relationship between the circulation rate of the recycled catalyst and the regenerated catalyst.
  • the LSS 74, and the TIC 76 and PDIC 78 overrides enhance the control of the slide valve 24 but are not necessary features.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention porte sur un procédé et appareil mélangeant le catalyseur épuisé et le catalyseur régénéré avant qu'ils n'entrent en contact avec l'apport dans la zone de réaction. Le débit de circulation du catalyseur épuisé est automatiquement régulée en fonction de celui du catalyseur régénéré.
PCT/US2002/009949 2002-03-27 2002-03-27 Procede et appareil fcc de regulation automatique du recyclage du catalyseur WO2003083014A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
PCT/US2002/009949 WO2003083014A1 (fr) 2002-03-27 2002-03-27 Procede et appareil fcc de regulation automatique du recyclage du catalyseur
AU2002303193A AU2002303193A1 (en) 2002-03-27 2002-03-27 Fcc process and apparatus with automatic catalyst recycle control

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/US2002/009949 WO2003083014A1 (fr) 2002-03-27 2002-03-27 Procede et appareil fcc de regulation automatique du recyclage du catalyseur

Publications (1)

Publication Number Publication Date
WO2003083014A1 true WO2003083014A1 (fr) 2003-10-09

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WO (1) WO2003083014A1 (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7002052B2 (en) 2000-02-02 2006-02-21 Dow Global Technologies Inc. Integrated process for producing an alkenyl-substituted aromatic compound
WO2010072733A1 (fr) * 2008-12-22 2010-07-01 Shell Internationale Research Maatschappij B.V. Appareil à retour de catalyseur et processus de réaction d'un apport
WO2013173164A1 (fr) * 2012-05-18 2013-11-21 Uop Llc Procédé de mélange de catalyseur et régénérateur associé
WO2014003891A1 (fr) * 2012-06-29 2014-01-03 Uop Llc Appareil de mélange de deux courants de catalyseur ayant un élément inséré à ouvertures alignées
US8653317B2 (en) 2009-03-19 2014-02-18 Dow Global Technologies Llc Dehydrogenation process and catalyst
US9624142B2 (en) 2004-02-09 2017-04-18 Dow Global Technologies Llc Process for the preparation of hydrogenated hydrocarbon compounds
WO2024118459A1 (fr) * 2022-11-29 2024-06-06 Dow Global Technologies Llc Procédés de déshydrogénation d'hydrocarbures utilisant de multiples entrées de catalyseur

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2965454A (en) * 1957-04-30 1960-12-20 Phillips Petroleum Co Fluidized conversion and stripping apparatus
US5451313A (en) * 1993-09-24 1995-09-19 Uop FCC feed contacting with catalyst recycle reactor
US5965012A (en) * 1997-12-05 1999-10-12 Uop Llc FCC process with short primary contacting and controlled secondary contacting
US6010620A (en) * 1997-11-11 2000-01-04 Uop Llc Distribution apparatus and method for short time contact of hydrocarbon compounds with particles
US6143253A (en) * 1997-11-17 2000-11-07 Uop Llc Standpipe distributor for short time contact of hydrocarbon compounds with particles

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2965454A (en) * 1957-04-30 1960-12-20 Phillips Petroleum Co Fluidized conversion and stripping apparatus
US5451313A (en) * 1993-09-24 1995-09-19 Uop FCC feed contacting with catalyst recycle reactor
US6010620A (en) * 1997-11-11 2000-01-04 Uop Llc Distribution apparatus and method for short time contact of hydrocarbon compounds with particles
US6143253A (en) * 1997-11-17 2000-11-07 Uop Llc Standpipe distributor for short time contact of hydrocarbon compounds with particles
US5965012A (en) * 1997-12-05 1999-10-12 Uop Llc FCC process with short primary contacting and controlled secondary contacting
US6183699B1 (en) * 1997-12-05 2001-02-06 Uop Llc FCC apparatus with short primary contacting and controlled secondary contacting

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7002052B2 (en) 2000-02-02 2006-02-21 Dow Global Technologies Inc. Integrated process for producing an alkenyl-substituted aromatic compound
US9624142B2 (en) 2004-02-09 2017-04-18 Dow Global Technologies Llc Process for the preparation of hydrogenated hydrocarbon compounds
WO2010072733A1 (fr) * 2008-12-22 2010-07-01 Shell Internationale Research Maatschappij B.V. Appareil à retour de catalyseur et processus de réaction d'un apport
US8653317B2 (en) 2009-03-19 2014-02-18 Dow Global Technologies Llc Dehydrogenation process and catalyst
WO2013173164A1 (fr) * 2012-05-18 2013-11-21 Uop Llc Procédé de mélange de catalyseur et régénérateur associé
WO2014003891A1 (fr) * 2012-06-29 2014-01-03 Uop Llc Appareil de mélange de deux courants de catalyseur ayant un élément inséré à ouvertures alignées
US8871151B2 (en) 2012-06-29 2014-10-28 Uop Llc Apparatus for mixing two streams of catalyst with an insert having aligned openings
WO2024118459A1 (fr) * 2022-11-29 2024-06-06 Dow Global Technologies Llc Procédés de déshydrogénation d'hydrocarbures utilisant de multiples entrées de catalyseur

Also Published As

Publication number Publication date
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