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WO2003053558A2 - Procede de regeneration d'un catalyseur use de craquage catalytique fluide - Google Patents

Procede de regeneration d'un catalyseur use de craquage catalytique fluide Download PDF

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Publication number
WO2003053558A2
WO2003053558A2 PCT/EP2002/014814 EP0214814W WO03053558A2 WO 2003053558 A2 WO2003053558 A2 WO 2003053558A2 EP 0214814 W EP0214814 W EP 0214814W WO 03053558 A2 WO03053558 A2 WO 03053558A2
Authority
WO
WIPO (PCT)
Prior art keywords
riser
lift gas
fluidized bed
inlet point
solids
Prior art date
Legal status (The legal status 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 status listed.)
Ceased
Application number
PCT/EP2002/014814
Other languages
English (en)
Other versions
WO2003053558A3 (fr
Inventor
Ye-Mon Chen
Hubertus Wilhelmus Albertus Dries
Rene Samson
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
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 Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Priority to AU2002363898A priority Critical patent/AU2002363898A1/en
Publication of WO2003053558A2 publication Critical patent/WO2003053558A2/fr
Anticipated expiration legal-status Critical
Publication of WO2003053558A3 publication Critical patent/WO2003053558A3/fr
Ceased legal-status Critical Current

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Classifications

    • 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
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/0025—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor by an ascending fluid
    • 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
    • B01J8/1818—Feeding of the fluidising gas
    • 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
    • C10G11/182—Regeneration
    • 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
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00752—Feeding
    • 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
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00761—Discharging
    • 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
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00769—Details of feeding or discharging
    • B01J2208/00778—Kinetic energy reducing devices in the flow channel
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00018—Construction aspects
    • B01J2219/00024—Revamping, retrofitting or modernisation of existing plants

Definitions

  • the present invention is related to a process to supply solid particles to a fluidized bed via a substantially vertical riser which has an upper outlet opening in said fluidized bed and wherein the solid particles are transported upwards via the riser with a lift gas, which lift gas and solid particles, are contacted at the lower end of the substantially vertical riser.
  • the invention is especially directed to a process for improving distributions of both spent catalyst and , lift gas into a regenerator of a fluid catalytic cracking unit .
  • FCCU Fluid Catalytic Cracking Unit
  • a regenerator a riser reactor and a stripper
  • finely divided regenerated catalyst is drawn from the regenerator through the regenerator standpipe and contacts with a hydrocarbon feedstock in a lower portion of a reactor riser.
  • Hydrocarbon feedstock and steam enter the riser through feed nozzles.
  • the mixture of feed, steam and regenerated catalyst which has a temperature of from about 200 °C to about 700 °C, passes up through the riser reactor, converting the feed into lighter products while a coke layer deposits on the
  • the regenerated ca-talyst is then drawn from the regenerator fluidized bed through the regenerator standpipe and, in repetition of the previously mentioned cycle, contacts the feedstock in the reactor riser.
  • Catalyst regeneration is a critical step in FCCU operation. The success of the step depends on the contacting efficiency between the spent catalyst and oxygen-containing gas in the regenerator. While the operation of an FCCU with a single catalyst inlet opening was acceptable for many years, the potential benefit of improving catalyst distribution in the regenerator has become apparent more recently. An ideal condition for catalyst distribution is that the time for distribution and mixing of catalyst should be less than that for coke combustion. As the regenerator diameter increases, the radial mixing time of catalyst becomes longer. At the same time, as the regeneration temperature increases, the time required for combustion becomes shorter. Hence, the benefit of improving spent catalyst distribution is more significant for an FCCU comprising a regenerator vessel of large .diameter or in which regeneration is conducted at higher temperature.
  • Another important aspect of the spent catalyst distribution is to control afterburn, which is characterized by substantial temperature increase in the dilute phase of the regenerator above the fluidized bed. If the lift gas, most commonly air, coming along with the spent catalyst is not well distributed, gas will form large bubbles at the discharge of the spent catalyst distributor, rising quickly through the fluidized bed with little time for combustion, and releasing oxygen- rich gas into the dilute phase. This leads to afterburn and poor combustion efficiency of the transport gas in the fluidized bed.
  • EP-A-622116 discloses a device which distributes spent catalyst and lift gas by means of a central vertical spent catalyst riser terminated with a junction connecting to multiple, horizontal conveying conduits and discharging catalyst at the ends of the horizontal conduits to discrete distribution points.
  • the lower end of the riser will thus comprise a solids inlet and means to provide lift gas to position below and above said solids inlet.
  • the solids inlet is suitably connected to a solids supply conduit through which solids flow to the solids inlet mainly due to gravity. Because the solids are only significantly accelerated at a position above the solids inlet point a more evenly distributed flow of lift gas and solids throughout the riser is achieved. It has been found surprisingly that this more evenly flow through the whole length ' of the riser, which can range from 6 to 30 meters, would have such a major impact in the distribution of solids and gas in the fluidized bed in which gas and solids are dispersed into.
  • An even more evenly flow in the riser can be achieved when the on the interior surface of the riser one or more contacting devices are present. These devices will create turbulence and thus further promote an evenly flow of solids across the cross sectional area of the riser. Examples of such devices are the arc shaped mixing devices as disclosed in WO-A-9814533, the turbulence generating means as disclosed in US-A-5851380 or the venturi shaped contacting devices as disclosed in US-A-3353925.
  • the lift gas being provided at the second inlet point should be sufficient to maintain a dense fluidized bed at the position at which the solids enter the riser.
  • a dense fluidized bed is meant a bed having a preferred catalyst density of between 300 and 900 kg/m ⁇ and more preferably between 500 and 900 kg/m.3.
  • the superficial velocity of the' gas in the dense fluidized bed is preferably between 0,1 and 1 m/s for air as lift gas.
  • suitable means to supply lift gas at the second inlet position are conduits placed in the riser provided with upwardly directed gas discharge openings.
  • a sieve plate present in ' the cross sectional area of the riser below the catalyst inlet point through which lift gas is provided.
  • the conduit with openings may for example be an annular ring provided with upwardly directed gas discharge openings.
  • the amount of lift gas added at this first inlet point should be sufficient to create a dilute phase fluidized bed wherein gas and solids are transported upwards.
  • the more dilute phase fluidized bed which is present between the second and first inlet point, is meant a fluidized bed which is more dilute than the dense fluidized bed according to this invention.
  • the more dilute phase fluidized bed has a catalyst density of below 500 kg/m.3 and more preferably between 20 and 400 kg/m.3.
  • the superficial gas velocity in the more dilute phase fluidized bed is preferably between 1.5 and 20 m/s.
  • lift gas is added at said first inlet point at evenly distributed positions across the cross- sectional area of the dense fluidized bed.
  • suitable means to supply lift gas are conduits placed in the riser provided with upwardly directed gas discharge openings.
  • the conduit with openings may for example be an annular ring provided with upwardly directed gas discharge openings.
  • single point inlet devices having an upwardly directed gas discharge opening and optionally provided with a deflector cone may also be used.
  • the upper end of the substantially vertical riser will suitably be provided with means to distribute the solids and the lift gas in the dense fluidized bed.
  • means may for example be a device as described in the above referred to EP-A-622116 or similar devices comprising outwardly conveying conduits to distribute the solids.
  • a device found especially suitable is described in co-pending PCT application PCT/EP01/13624 and is incorporated herein by reference.
  • Such device comprises: a first disk surrounding the upper opening of the substantially vertical riser at the uppermost end of said riser, a second disk, spaced upwardly from, and rigidly connected to, said first disk, thereby forming a substantially open space therebetween; a deflection cone attached, at its base, to said second disk, said deflection cone pointing downward and being centred over the outlet of said conduit, said deflection cone adapted to direct said spent catalyst and said transfer gas in a substantially uniform, radially outward direction through said space formed between said first disk and said second disk, thereby providing a continuous circumferential discharge of said mixture of solids and lift gas from the outer circumference of said space formed between said first disk and said second disk into said fluidized bed in a substantially uniform radially outward direction.
  • the lift gas may be any gaseous medium and the choice will depend on the process in which the invention is applied.
  • the lift gas may be for example steam or nitrogen.
  • an oxygen containing gas suitably air or oxygen-enriched air is used.
  • the solids will be catalyst suitably be conventional FCC catalyst as for example described in "Fluid catalytic cracking: Science and Technology", Ed. Magee J.S., Mitchell M.M.Jr., 1993, Elsevier Science
  • Additives for example ZSM-5 or Zeolite Beta containing additives, to enhance propene selectivity may also be present.
  • FIG 1 shows the lower end of a FCCU regenerator vessel (1) comprising of a fluidized bed (2) of catalyst particles, an upper fluidized bed level (3) , means to add fluidizing gas (4), a catalyst discharge conduit (5) for discharge of regenerated catalyst particles and means to supply spent catalyst via a riser (6) .
  • Riser (6) is provided at its upper end with means (7) to evenly discharge catalyst and lift gas in the fluidized bed (2) . These means are thus located below upper bed level (3).
  • a solids inlet (8) is positioned between two means (9, 10) to add lift gas.
  • Figure 2 shows the lower end of the riser in more detail.
  • catalyst inlet opening (8) is connected to a catalyst standpipe (18) through which spent catalyst flows from a stripper (not shown) .
  • a gas ring (11) is provided as means (9) to add lift gas at the second inlet point to maintain a dense fluidized bed (12) .
  • a lift gas ring (13) is present as means (10) to supply lift gas at the first inlet point and create a dilute phase fluidized bed regime (14) above said position.
  • Figure 3 shows the cross-section AA' of reactor riser (6) including a preferred .embodiment of a gas ring (11) to supply lift gas.
  • This gas ring (11) is provided with a plurality of openings at the upper side.
  • the openings (15) are positioned such that gas will have an axial and radial velocity component. Part of the openings (15) will discharge the gas radially towards the riser (6) wall and part of the openings (16) will direct the gas radially towards the centre (17) of the reactor.
  • Figure 4 shows an embodiment wherein the first inlet point for lift gas is a single point inlet device.
  • Figure 4 shows features of Figure 2 and a vertical lift gas inlet conduit (19) extending from the bottom of the riser to a single point above the solids inlet -point (8). At the discharge opening of said conduit (19) a deflector cone (20) is present.

Landscapes

  • 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)

Abstract

Cette invention concerne un procédé consistant à introduire des particules solides dans un lit fluidisé par une colonne montante sensiblement verticale qui comporte une ouverture d'évacuation supérieure débouchant dans le lit fluidisé, les particules solides étant transportées vers le haut dans la colonne montante au moyen d'un gaz de sustentation, lequel gaz de sustentation et les particules solides sont mis en contact au niveau de l'extrémité inférieure de la colonne montante sensiblement verticale, cette mise en contact étant effectuée selon un procédé consistant à introduire les particules solides dans la colonne montante par une entrée de solides située au niveau de l'extrémité inférieure de la colonne montante, une partie du gaz de sustentation étant introduite dans la colonne montante par une première entrée située au-dessus de l'entrée de solides et une partie du gaz de sustentation étant introduite dans la colonne montante par une deuxième entrée située en dessous de l'entrée de solides de sorte que dans la colonne montante se trouvent d'une part un lit fluidisé dense en dessous de la première entrée de gaz de sustentation et d'autre part un lit fluidisé plus dilué au-dessus de la première entrée de gaz de sustentation.
PCT/EP2002/014814 2001-12-21 2002-12-16 Procede de regeneration d'un catalyseur use de craquage catalytique fluide Ceased WO2003053558A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU2002363898A AU2002363898A1 (en) 2001-12-21 2002-12-16 Process to regenerate fcc spent catalyst

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US34483701P 2001-12-21 2001-12-21
US60/344,837 2001-12-21

Publications (2)

Publication Number Publication Date
WO2003053558A2 true WO2003053558A2 (fr) 2003-07-03
WO2003053558A3 WO2003053558A3 (fr) 2007-12-06

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PCT/EP2002/014814 Ceased WO2003053558A2 (fr) 2001-12-21 2002-12-16 Procede de regeneration d'un catalyseur use de craquage catalytique fluide

Country Status (2)

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AU (1) AU2002363898A1 (fr)
WO (1) WO2003053558A2 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8728302B2 (en) 2010-06-25 2014-05-20 Exxonmobil Research And Engineering Company Spent catalyst riser distributor

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3844973A (en) * 1972-05-30 1974-10-29 Universal Oil Prod Co Fluidized catalyst regeneration by oxidation in a dense phase bed and a dilute phase transport riser
US3893812A (en) * 1972-05-30 1975-07-08 Universal Oil Prod Co Regeneration apparatus with external regenerated-catalyst recycle means
US3970587A (en) * 1973-07-18 1976-07-20 Mobil Oil Corporation Combustion regeneration of hydrocarbon conversion catalyst with recycle of high temperature regenerated catalyst
CA1055915A (fr) * 1974-06-17 1979-06-05 Hartley Owen Methode et systeme de regeneration de catalyseurs fluidisables
GB1528432A (en) * 1976-05-07 1978-10-11 Texaco Development Corp Fluidized cracking catalyst regeneration process and apparatus
US4340566A (en) * 1979-12-07 1982-07-20 Uop Inc. Catalyst regeneration apparatus
FR2576906B1 (fr) * 1985-02-07 1987-09-25 Raffinage Cie Francaise Procede et dispositif d'injection de catalyseur dans un procede de craquage catalytique a l'etat fluide, notamment de charges lourdes
FR2654435B1 (fr) * 1989-11-10 1992-03-13 Total France Procede et dispositif de mise en contact d'une charge d'hydrocarbures avec des particules solides chaudes, dans un reacteur tubulaire a lit fluidise ascendant.
FI104247B1 (fi) * 1997-02-26 1999-12-15 Imatran Voima Oy Sovitelma tasaisen kaasuvirran muodostamiseksi raemaisten kiinteiden materiaalien leijuttamiseen tai kuljetukseen

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8728302B2 (en) 2010-06-25 2014-05-20 Exxonmobil Research And Engineering Company Spent catalyst riser distributor

Also Published As

Publication number Publication date
WO2003053558A3 (fr) 2007-12-06
AU2002363898A1 (en) 2003-07-09
AU2002363898A8 (en) 2008-02-28

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