EP0861310B1 - Procede et dispositif de craquage catalytique descendant mettant en oeuvre l'injection d'une charge sous un angle adequat sur un catalyseur conditionne - Google Patents

Procede et dispositif de craquage catalytique descendant mettant en oeuvre l'injection d'une charge sous un angle adequat sur un catalyseur conditionne Download PDF

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Publication number
EP0861310B1
EP0861310B1 EP97919105A EP97919105A EP0861310B1 EP 0861310 B1 EP0861310 B1 EP 0861310B1 EP 97919105 A EP97919105 A EP 97919105A EP 97919105 A EP97919105 A EP 97919105A EP 0861310 B1 EP0861310 B1 EP 0861310B1
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EP
European Patent Office
Prior art keywords
catalyst
zone
feed
injection
flow
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.)
Expired - Lifetime
Application number
EP97919105A
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German (de)
English (en)
French (fr)
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EP0861310A1 (fr
Inventor
Renaud Pontier
Régis Bonifay
Gérard Courteheuse
Mariano Del Pozo
Thierry Gauthier
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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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
    • 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
    • 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

Definitions

  • the invention relates to a process for catalytic cracking in a fluid bed (FCC) of a hydrocarbon charge in a reaction zone where the charge circulates from top to low (in English dropper).
  • FCC fluid bed
  • Patent application EP-A-0479645 describes a downflow reactor or dropper in which the load is supplied in a co-current direction the catalyst flow. This flows from a dense phase.
  • the area of dense phase catalyst can be a dense fluidized bed storage area located between the particle regenerator and the entrance to the droppers. In these conditions, the density of the gas-solid suspension can be controlled.
  • a another patent application EP-A-0663434 describes a dropper supplied with a catalyst from a conditioning zone of the fluidized bed catalyst which is connected to a coker catalyst regenerator. The packaging area includes elsewhere a gas disengagement zone.
  • US Pat. No. 4,919,898 describes the formation of a curtain falling from the catalyst from rectangular openings coming from a bed pressurized by steam. This bed therefore regulates the pressure difference between the enclosure containing the pressurized bed and a chamber for mixing the catalyst and the charge downstream of the bed. This patent further describes the injection of the charge in the direction of the valve forming the curtain.
  • US Patent 5,296,131 further describes a downwardly flowing catalyst curtain of annular shape.
  • the charge is injected downward at least in part through a radial opening under the seat of a valve type valve of frustoconical shape, pressed against the upper part of the reactor.
  • patent application EP-A-0 209 442 which describes the presence of a valve downstream of a first fluidization ring which disturbs the fluidization conditions until defluidization leading to obtaining a density corresponding to a bulk bed.
  • the object of the invention is to remedy the drawbacks of the prior art.
  • the invention relates to a catalytic cracking process in fluidized bed of an oil charge in lighter effluents in a cracked zone catalytic comprising a reaction zone or dropper in which introduces regenerated catalyst at an upper end called the injection zone coming from at least one regeneration zone, the catalyst is shaped by means of a shaping member having a restriction, it is brought into contact the catalyst with the charge, we form a mixture flowing down from catalyst and charge, and at least the majority of the charge is vaporized in said injection zone, we crack said charge to obtain lighter effluents, we separates effluent from spent catalyst in a separation zone at the end lower, the effluent is recovered and the spent catalyst is recycled in the regeneration, the process being characterized in that the catalyst is run off regenerated from the regeneration zone in a conditioning zone catalyst in a dense fluidized bed upstream of the injection zone comprising a gas disengagement zone, the speed of fluidization by a fluidizing gas being between 0.1 and 30 cm / s, a flow of catalyst flowing
  • the flow of catalyst flowing by gravity through the restriction with a variable or constant passage section is, as a general rule, between 200 and 20,000 kg / m 2 .s and preferably between 1,000 and 10,000 kg / m 2 .s, an excellent range of values between 4,000 and 6,000 kg / m 2 .s.
  • the charge can be injected by a plurality of injectors arranged all around the wall of the injection area at an angle less than or equal to 30 degrees from the horizontal and preferably at an angle of 5 to 25 degrees.
  • the injection angle ⁇ is determined so that the result of the vectors taking into account the momentum of the charge and the amount of movement of the catalyst is substantially horizontal, for example more or less ten degrees around the horizontal.
  • the catalyst mass ratio on load in the injection area can be between 5 and 20, preferably between 10 and 18.
  • the speed of the gravity-flowing catalyst by the restriction can be from 0.1 to 20 m / s and advantageously from 0.5 to 5 m / s, while the speed atomized charge droplets is usually between 50 and 100 m / s and preferably 70 to 90 m / s.
  • the flow rate of catalyst in the injection zone can be adjusted by means of a valve with variable opening which can be that according to the first variant, or a valve with variable opening arranged on the introduction line of the regenerated catalyst and from the regenerator to the conditioning area.
  • This valve is also slaved to a temperature sensor at the output of the dropper.
  • the catalyst conditioning zone can have a catalyst gas disengagement zone above the level dense fluidized bed, between a third and a half of the total height of the conditioning area.
  • the injection zone of the reaction zone is generally sized to receive a given mass of catalyst such as the residence time in this zone is usually between 0.02 s and 0.5 s and preferably between 0.03 s and 0.1 s.
  • the catalyst can be one of those known to those skilled in the art, for example those cited in US Patent 5,296,131.
  • the member for introducing the hydrocarbon charge can be any member well known to those skilled in the art allowing the introduction of a hydrocarbon charge, preferably in the form of droplets preferably having a mean diameter. less than 5x10 -4 meter (m) and advantageously less than 1x10 -4 (m). It is preferable that the hydrocarbon charge is introduced so as to form fine droplets distributed homogeneously at the level of the introduction zone.
  • An auxiliary fluid called atomization promoting the production of fine droplets can also be introduced with the hydrocarbon charge.
  • This auxiliary fluid will usually be a gas such as steam, or a gas relatively rich in hydrogen or hydrogenated compounds from other units of the refinery.
  • the atomization is generally carried out outside the reaction zone.
  • injectors are usually arranged at the periphery of the injection area, under the catalyst shaping member and their end is located in at minus a plane substantially perpendicular to the axis of the injection zone or of the dropper.
  • the distance of these injectors, counted from the theoretical impact points of the jets load on the axis of the injection zone (or reaction zone), at the point lowest of the catalyst forming member is at most equal to 2 times the diameter of the injection area.
  • this distance can be 0.5 to 1 times the diameter of the zone injection.
  • the invention also relates to a catalytic cracking unit with a descending reactor. or dropper to catalytically crack a hydrocarbon charge in the presence of a cracking catalyst and to produce an effluent of light products and coked cracking catalyst.
  • Unit includes organ with restriction for the shaping of the catalyst upstream of the dropper, a supply of charge communicating with an injection chamber at the top of the dropper and bringing the charge into contact with the shaped catalyst, a effluent separation enclosure for the coked catalyst at the bottom of the dropper and at least one coke catalyst regeneration enclosure communicating with the separation enclosure and a catalyst supply line regenerated connecting the regeneration enclosure to the catalyst shaping member, said unit being characterized in that it comprises an enclosure of conditioning of the regenerated catalyst in a dense fluidized bed connected between the regenerator and the catalyst shaping member, said enclosure comprising fluidization means and having a catalyst disengagement zone from the gas, of suitable volume at the top of said enclosure, which communicates by a pressure equalization line with the upper part of the containment regeneration, and in that
  • a device 1 for catalytic cracking in a known fluidized bed known in itself essentially comprises a dropper (descending reactor) 13 supplied with its upper part by catalyst conditioned in an enclosure of conditioning 2.
  • This enclosure is supplied with catalyst by a line 3 oblique, coming from a regeneration zone which in this case contains two regenerators 4 and 17 in fluidized bed, superimposed.
  • the dropper is fed in its upper part by a load introduced by injectors 12 and vaporized in contact with the hot regenerated catalyst (approximately 780 ° C).
  • the effluents are separated from the catalyst in a stripper 14 known per se, discharged by a line 15 while the catalyst once stripped by water vapor by example and containing coke is recycled in the first regenerator 17 by a recycling line 16.
  • the catalyst partially regenerated, in the presence of a gas containing oxygen is raised in the second regenerator 4 by a lift 25, where it undergoes a second combustion in the presence of an oxygen-containing gas.
  • cyclones or means of fluidization in the separator or regenerators which are well known to those skilled in the art, and which do not are not shown in the figure for the sake of simplification.
  • the regenerated and hot catalyst from the second zone of regeneration in dense fluidized phase is introduced by gravity through line 3 inclined in the packaging enclosure 2 in a dense fluidized bed upstream of the dropper 13.
  • a fluidization ring 5 supplies a fluidization gas 5a which may be steam, the lower part of the enclosure for conditioning the catalyst at a speed of 10 cm / s.
  • the catalyst then has a density, for example between 550 and 800 kg / m 3 and typically 600 kg / m 3 .
  • the catalyst conditioning chamber 2 is dimensioned so as to present in its upper part a zone 8 for disengagement of the gas from the catalyst, located above the arrival of line 3 and of height between the third and a quarter of the total height of the conditioning enclosure.
  • Line 9 pressure balancing connects the disengagement zone to the upper part of the second regenerator.
  • level 7 of the fluidized bed in the second controlled regenerator by a level probe 23 and controlled by a regulator 24 to the air flow of rise (lift) of the catalyst corresponds substantially to that 6 of the fluidized bed in the conditioning enclosure.
  • the device Downstream of the conditioning enclosure 2, the device comprises an injection chamber 10 of diameter at least equal to that of the dropper, at the inlet of which a flow control valve 11 or shaping valve of a curtain of falling catalyst lets escape, by its annular section of opening or restriction, a catalyst flow of about 800 kg / m 2 .s.
  • This valve can have a fixed central part or insert which determines with the wall from the injection zone, the cross section of the catalyst flow determined in combination with another flow control valve 19 on the intake line catalyst 3.
  • the curtain shaping valve can comprise a movable central part connected to a rod, according to patent FR 2631857, this rod being protected from the catalyst by a sheath containing a sweeping gas. Said movable central part of the valve determines with its seat a section of adequate annular passage for a given flow rate of catalyst delivered by the valve 19 and therefore an appropriate flow.
  • the injection chamber generally has a larger diameter than that of the restriction (the largest diameter of the annular curtain of catalyst formed) so that the charge injector tips do not intercept the catalyst curtain.
  • the charge after being atomized outside the device, is injected by a plurality of injectors 12 disposed at the periphery, on a plane substantially perpendicular to the axis of the dropper and whose jet of charge droplets is directed towards said axis at an injection angle close to 25 degrees of angle under the valve 11, against the current of the curtain falling from the catalyst, which allows it to break.
  • the distance of the injectors, counted from the theoretical impact points of the jets load on the axis of the injection chamber (or of the dropper), at the lowest point of the shaping member of the catalyst curtain is at most equal to 2 times the diameter of the injection enclosure and preferably between 0.5 and 1 times that diameter.
  • This distance of the injectors relative to the valve 11 prevents on the one hand the erosion of the valve and on the other hand the recirculation zones above the injectors, the catalyst and / or charge.
  • This dropper can have a diameter smaller than that of the enclosure injection.
  • the cracked effluents are collected after stripping with steam using the line 15 and the catalyst is recycled to the first regenerator 17.
  • the flow control valve 19 is generally controlled by a line 22 to a temperature measurement 20 given by a probe 21 arranged at the lower end of the dropper.
  • the unit is generally started by closing the flow restriction 11 variable or by closing an all or nothing valve not shown in the figure, placed for example below the member 11, when the latter, with a fixed central part, determines a constant passage section of catalyst.
  • the part of the catalyst shaping member opposite the load injected can have a concave shape and thus determine an area of containment for the vaporization thereof capable of improving the selectivity of the cracking reaction.
  • the distance along the axis of the charge injectors from the insert (most bottom) is 0.5 times the diameter of the injection chamber.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Catalysts (AREA)
EP97919105A 1996-09-18 1997-09-16 Procede et dispositif de craquage catalytique descendant mettant en oeuvre l'injection d'une charge sous un angle adequat sur un catalyseur conditionne Expired - Lifetime EP0861310B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR9611379A FR2753454B1 (fr) 1996-09-18 1996-09-18 Procede et dispositif de craquage catalytique descendant mettant en oeuvre l'injection d'une charge sous un angle adequat sur un catalyseur conditionne
FR9611379 1996-09-18
PCT/FR1997/001630 WO1998012280A1 (fr) 1996-09-18 1997-09-16 Procede et dispositif de craquage catalytique descendant mettant en oeuvre l'injection d'une charge sous un angle adequat sur un catalyseur conditionne

Publications (2)

Publication Number Publication Date
EP0861310A1 EP0861310A1 (fr) 1998-09-02
EP0861310B1 true EP0861310B1 (fr) 2001-12-12

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EP97919105A Expired - Lifetime EP0861310B1 (fr) 1996-09-18 1997-09-16 Procede et dispositif de craquage catalytique descendant mettant en oeuvre l'injection d'une charge sous un angle adequat sur un catalyseur conditionne

Country Status (13)

Country Link
US (1) US6099720A (es)
EP (1) EP0861310B1 (es)
JP (1) JP4281026B2 (es)
KR (1) KR100493753B1 (es)
CN (1) CN1134528C (es)
AT (1) ATE210712T1 (es)
CA (1) CA2236296C (es)
DE (1) DE69709050T2 (es)
ES (1) ES2169860T3 (es)
FR (1) FR2753454B1 (es)
ID (1) ID18268A (es)
MX (1) MX9803790A (es)
WO (1) WO1998012280A1 (es)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2385094A1 (fr) 2010-05-06 2011-11-09 IFP Energies nouvelles Procédé de craquage catalytique avec recycle d'une coupe oléfinique prélevée en amont de la section de séparation des gaz afin de maximiser la production de propylène

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BR0101433B1 (pt) * 2001-04-10 2011-02-22 método e dispositivo de entrada multi-funcional para reator tubular de fluxo descendente.
EP1392796A2 (en) * 2001-06-08 2004-03-03 Albemarle Netherlands B.V. Process for fluid catalytic cracking----------------------------
US7087154B2 (en) * 2002-12-30 2006-08-08 Petroleo Brasileiro S.A. - Petrobras Apparatus and process for downflow fluid catalytic cracking
CN1332742C (zh) * 2004-05-14 2007-08-22 中国石油化工股份有限公司 催化裂化装置催化剂/助剂补充方法
US20080011644A1 (en) * 2006-07-13 2008-01-17 Dean Christopher F Ancillary cracking of heavy oils in conjuction with FCC unit operations
US20080011645A1 (en) * 2006-07-13 2008-01-17 Dean Christopher F Ancillary cracking of paraffinic naphtha in conjuction with FCC unit operations
US7758817B2 (en) * 2006-08-09 2010-07-20 Uop Llc Device for contacting high contaminated feedstocks with catalyst in an FCC unit
WO2009147512A2 (en) * 2008-06-04 2009-12-10 Inbicon A/S Devices and methods for discharging pretreated biomass from higher to lower pressure regions
CN103814114B (zh) 2011-07-27 2018-04-24 沙特阿拉伯石油公司 在下流式反应器中流化催化裂化链烷烃族石脑油
JP5823911B2 (ja) * 2012-04-27 2015-11-25 Ｊｘ日鉱日石エネルギー株式会社 流動接触分解装置における原料と触媒を混合する混合装置
CN108726507B (zh) * 2017-04-21 2020-11-13 山东大展纳米材料有限公司 一种单级连续化制备碳纳米管的装置及方法
CN117654409A (zh) * 2023-11-03 2024-03-08 佛山市瑞重机械设备有限公司 一种纳米气相二氧化硅表面改性生产装置及其生产方法

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JPS624784A (ja) * 1985-07-16 1987-01-10 コンパニ−・フランセ−ズ・ド・ラフイナ−ジユ 炭化水素仕込物の接触クラツキングのための方法および装置の改良
US4919898A (en) * 1987-08-11 1990-04-24 Stone & Webster Engineering Corp. Particulate solids cracking apparatus
US4985136A (en) * 1987-11-05 1991-01-15 Bartholic David B Ultra-short contact time fluidized catalytic cracking process
FR2631857B1 (fr) * 1988-05-24 1990-09-14 Inst Francais Du Petrole Reacteur a lit fluidise entraine comprenant un moyen de regulation du flux de particules solides et son utilisation dans un procede de craquage catalytique
FR2667609B1 (fr) * 1990-10-03 1993-07-16 Inst Francais Du Petrole Procede et dispositif de craquage catalytique en lit fluide a courant descendant.
FR2683743B1 (fr) * 1991-11-14 1994-02-11 Institut Francais Petrole Procede et dispositif d'echange thermique de particules solides pour double regeneration en craquage catalytique.
US5296131A (en) * 1992-12-02 1994-03-22 Mobil Oil Corporation Process for short contact time cracking
FR2715163B1 (fr) * 1994-01-18 1996-04-05 Total Raffinage Distribution Procédé de craquage catalytique en lit fluidisé d'une charge d'hydrocarbures, notamment d'une charge à forte teneur en composés azotés basiques.

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2385094A1 (fr) 2010-05-06 2011-11-09 IFP Energies nouvelles Procédé de craquage catalytique avec recycle d'une coupe oléfinique prélevée en amont de la section de séparation des gaz afin de maximiser la production de propylène

Also Published As

Publication number Publication date
WO1998012280A1 (fr) 1998-03-26
JP2001503080A (ja) 2001-03-06
JP4281026B2 (ja) 2009-06-17
KR19990067633A (ko) 1999-08-25
CA2236296C (fr) 2007-01-16
ES2169860T3 (es) 2002-07-16
DE69709050T2 (de) 2002-05-02
DE69709050D1 (de) 2002-01-24
ATE210712T1 (de) 2001-12-15
KR100493753B1 (ko) 2005-09-02
FR2753454B1 (fr) 1999-06-04
MX9803790A (es) 1998-09-30
EP0861310A1 (fr) 1998-09-02
ID18268A (id) 1998-03-19
FR2753454A1 (fr) 1998-03-20
CN1134528C (zh) 2004-01-14
CN1208432A (zh) 1999-02-17
CA2236296A1 (fr) 1998-03-26
US6099720A (en) 2000-08-08

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