EP0573316B1 - Verfahren und Einrichtung zum katalytischen Kracken in zwei aufeinanderfolgenden Reaktionszonen - Google Patents

Verfahren und Einrichtung zum katalytischen Kracken in zwei aufeinanderfolgenden Reaktionszonen Download PDF

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Publication number
EP0573316B1
EP0573316B1 EP93401080A EP93401080A EP0573316B1 EP 0573316 B1 EP0573316 B1 EP 0573316B1 EP 93401080 A EP93401080 A EP 93401080A EP 93401080 A EP93401080 A EP 93401080A EP 0573316 B1 EP0573316 B1 EP 0573316B1
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Prior art keywords
reactor
process according
load
catalyst
reaction
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English (en)
French (fr)
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EP0573316A1 (de
Inventor
Pierre Galtier
Sigismond Franckowiak
Renaud Pontier
Régis Bonifay
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
    • 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
    • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
    • C10G51/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only
    • C10G51/026—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only only catalytic cracking steps
    • 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 present invention relates to a method and a device for cracking catalytic of hydrocarbon charges.
  • reaction product is then subjected to separation, for example in a cyclone, so as to obtain, on the one hand, a gaseous hydrocarbon phase and, on the other hand, the catalyst.
  • the catalyst is regenerated then at least in part recycled to the cracking reactor.
  • the applicant proposes a method and a device for using a cracking reactor having a downflow reaction zone followed by an upward flow reaction zone, which allows to cumulate the advantages of an efficient reaction and a solid / gas separation improved.
  • a device can also be installed on the units existing with lower costs than those due to changes in direction of the flow.
  • the subject of the invention is a process for cracking hydrocarbon feedstocks, the cracking reaction taking place in the presence of entrained or fluidized bed catalyst, the catalyst particles being, after reaction, separated from the gas phase, regenerated and at least in part recycled, process in which the cracking reaction takes place in two zones substantially vertical successive reactions, the charge being introduced at the upper part of a first reaction zone, then a part at less of the product obtained at the bottom of said first zone is introduced into a second reaction zone where it circulates so ascending.
  • Figures 2 and 3 show devices associated with said method.
  • the particle flow rates of the catalyst between the reactor (3) and the first zone reaction (4) are adjusted by a pressure difference caused by example in a valve, or any other suitable means.
  • the catalyst enters with a speed greater than 0.5 m / s and generally greater than 1 m / s, being able to go up to 20 m / s more generally up to 5 m / s.
  • the apparent density of the suspended catalyst is then about 50 to 600 kg / m 3 .
  • the load (5) previously heated to temperatures between 100 and 250 ° C. is then introduced into contact with the hot catalyst in a fluidized bed, in the form of fine droplets with a diameter generally between 20 and 300 ⁇ m (micrometers), most often obtained from known means atomization.
  • the hydrocarbon charges to be treated are advantageously made up heavy hydrocarbons, i.e. with final boiling points around 700 ° C, such as vacuum gas oils, but also more heavy such as crude oils and vacuum residues. These charges may, if applicable, have received prior treatment, for example a hydrotreating in the presence of a Co-Mo type catalyst. Light loads can also be processed, which have lower boiling points at 400 ° C.
  • the preferred fillers for the process according to the invention contain fractions normally boiling up to 700 ° C and above, and may contain high percentages of asphalt products, Conradson carbon content up to 4% and even beyond. These charges may possibly be mixed with lighter hydrocarbon cuts, such as LCOs and HCO.
  • the charge Upon contact with the catalyst, the charge vaporizes. She is then trained by the catalyst current with which it flows in downward cocurrent in this first reaction zone (4) where the cracking takes place in part (the speed of the downflow in the reactor varies and is the most often between 0.5 to 50 m / s and preferably 0.5 to 10 m / s).
  • the product obtained at the bottom of said first reaction zone (4) is transferred, at least in part and preferably in whole, to the lower part the second reaction zone (6) located in the axis reactor (7) substantially vertical.
  • the invention also provides adapted devices described below (U-shaped tubes, inclined ).
  • the reaction medium flows into the second reaction zone so ascending, with speeds generally greater than 2 m / s and capable of going up to 50 m / s, and preferably between 10 and 30 m / s.
  • This fluid can be one or more naphtha generally a liquid with a boiling point lower than that of the feed, which allows the calories to be removed from the reaction zone.
  • a hydrocarbon phase (8).
  • the amount of hydrocarbon phase introduced relative to the amount of charge introduced into the first reaction zone represents 0 to 50% by weight, and preferably 5 to 30%.
  • the hydrocarbon phase can consist of part of the charge to treat. It can also be a light load, i.e. a load of boiling point below 400 ° C, and most often around 180 ° C at about 380 ° C.
  • the product obtained at the top of the reaction zone (6) is transferred to a solid / gas separation means (9) to obtain, on the one hand, the gas phase (10) containing the cracked products, and on the other hand the catalyst.
  • the separated catalyst particles are transferred to at least one regeneration reactor (3), where the coke is burned in a conventional manner, then a at least part of the particles is recycled to the first reaction zone.
  • Another object of the invention is a device for carrying out the method of catalytic cracking of hydrocarbon feed according to the process object of the invention.
  • the device is described from Figures 2 and 3.
  • Said device comprises a first reactor (20) with a substantially vertical axis provided with means (21) for introducing the catalyst into the upper part of the reactor, of means (24) for the introduction of the atomized charge to be treated in the upper part of the reactor, said means (24) being located below means (21), and said reactor also being provided with an opening arranged at the bottom of the reactor and along its axis, for the evacuation of the product obtained, said device further comprising a second axis reactor (28) substantially vertical, provided at its lower part with an opening for the introduction of the product obtained at the bottom of the first reactor (20) and provided at its upper part with a pipe (29) for the evacuation of the product obtained after treatment in the second reactor, said device also comprising at least one pipe (30) connecting the parts lower of the first and second reactors.
  • It includes the two successive reactors (20) and (28) with a substantially axis vertical, the lower parts of which are connected by a pipe (30).
  • the catalyst is introduced by means (21) generally consisting of a pipe (22) provided with a slide valve (23) arranged on the axis of the reactor.
  • the charge to be treated is introduced, in atomized form, by means (24), generally constituted by a pipe (25) provided with a means of atomization (26).
  • This pipe opens below the opening through which introduced the catalyst, so as to introduce the charge into the catalyst downward movement.
  • the product obtained at the lower part (27) of the first reactor is transferred by line (30) to the second reactor.
  • the pipe (30) - or the pipes if necessary - must allow a rapid transfer and with a low deposit of solid catalyst.
  • FIG. 3 represents a pipe (30) inclined towards the second reactor, the transfer takes place by training.
  • This configuration is particularly interesting because it approaches the current configuration of the catalytic cracking, the charge being injected in the most recent recent processes generally in (32) and / or in (42).
  • the parts (20) and (30) are then not reaction zones and play a role purely functional in the transport of the catalyst. It is possible to maintain in place in the part (30) one or more means (42) of injection-atomization of the hydrocarbon charge, which makes it possible to inject possibly a fraction of hydrocarbons to be converted in the part ascending.
  • Said means (42) can be constituted simply by a pipe provided with injection means and arranged for example in the lower part of the second reactor (line (42) and / or (32) shown in FIG. 3) or proximity to this part.
  • said means are constituted by vents (34) arranged on the pipe (30) so that the direction of the injection follows the movement of the catalyst (injection substantially tangential). This embodiment makes it possible to significantly reduce the deposits.
  • the device can also include, at the bottom of the second reactor (28) or nearby, a pipe (33) for the introduction of a fluid training.
  • This fluid may for example be a hydrocarbon preferably liquid or gaseous, water or an inert gas such as for example nitrogen.

Claims (18)

  1. Verfahren zum Kracken von Kohlenwasserstoffchargen in Kontakt mit dem Katalysator im Schleppbett oder fluidisierten Bett, wobei die Katalysatorpartikel nach Reaktion von der gasförmigen Phase getrennt, regeneriert und wenigstens zum Teil recycliert werden, wobei das Verfahren sich dadurch auszeichnet, daß die Krackreaktion in zwei aufeinanderfolgenden im wesentlichen vertikalen Reaktionszonen abläuft, die Charge von oben nach unten aus der ersten Zone fließt und dann wenigstens ein Teil des aus dieser ersten Zone stammenden Produktes in eine zweite Reaktionszone eingeführt wird, wo es im Aufstrom zirkuliert.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Gesamtheit das aus der ersten Zone stammenden Produktes in die zweite Reaktionszone eingeführt wird.
  3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß die in die absteigende Reaktionszone eintretende Charge aus schweren Kohlenwasserstoffen gebildet wird.
  4. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß die in die absteigende Reaktionszone eintretende Charge durch leichte Kohlenwasserstoffe mit einem Siedepunkt unter 400°C gebildet wird.
  5. Verfahren nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, daß eine kohlenwasserstoffhaltige Phase in das in die zweite Reaktionszone eintretende Reaktionsmedium eingeführt wird.
  6. Verfahren nach Anspruch 5, dadurch gekennzeichnet, daß die kohlenwasserstoffhaltige Phase identisch mit der zu behandelnden Charge ist.
  7. Verfahren nach Anspruch 5, dadurch gekennzeichnet, daß die kohlenwasserstoffhaltige Phase eine leichte Phase mit einem Siedepunkt unterhalb 400°C ist.
  8. Verfahren nach Anspruch 7, dadurch gekennzeichnet, daß die kohlenwasserstoffhaltige Phase eine leichte Phase mit einem Siedepunkt zwischen 180 und 380°C ist.
  9. Verfahren nach einem der Ansprüche 5 bis 8, dadurch gekennzeichnet, daß die Menge an eingeführter kohlenwasserstoffhaltiger Phase 0 bis 50% des Volumens der in die erste Reaktionszone eingeführten Charge ausmacht.
  10. Verfahren nach Anspruch 9, dadurch gekennzeichnet, daß diese Menge von 5 bis 30 Vol.-% der Charge geht.
  11. Verfahren nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, daß ein Mitreißefluid im unteren Teil der zweiten Reaktionszone eingeführt wird.
  12. Verfahren nach einem der Ansprüche 1 bis 11, dadurch gekennzeichnet, daß die absteigende Strömung des Katalysators und der mitgerissenen Charge mit einer Geschwindigkeit von 0,5-50m/s und die aufsteigende Strömung des Reaktionsmedium mit einer Geschwindigkeit von 2-50m/s stattfindet.
  13. Verfahren nach einem der Ansprüche 1 bis 12, dadurch gekennzeichnet, daß die absteigende Strömung des Katalysators und der mitgerissenen Charge mit einer Geschwindigkeit von 0,5-10m/s stattfindet.
  14. Verfahren nach einem der Ansprüche 1 bis 13, dadurch gekennzeichnet, daß die aufsteigende Strömung des Reaktionsmediums mit einer Geschwindigkeit von 10-30m/s stattfindet.
  15. Vorrichtung zum katalytischen Kracken kohlenwasserstoffhaltiger Chargen mit einem ersten Reaktor (20) von einer im wesentlichen vertikalen Achse, die mit Mitteln (21) zum Einführen des Katalysators im oberen Teil des Reaktors, mit Mitteln (24) zum Einführen der zerstäubten Charge im oberen Teil des Reaktors versehen ist und unterhalb des Mittels (21) angeordnet ist, wobei dieser Reaktor (20) ebenfalls mit einer Öffnung zum Abzug des erhaltenen Produktes versehen und im unteren Teil des Reaktors gemäß seiner Achse angeordnet ist, wobei diese Vorrichtung sich dadurch auszeichnet, daß sie im übrigen einen zweiten Reaktor (28) von im wesentlichen vertikaler Achse umfaßt, der an seinem unteren Teil mit einer öffnung zum Einführen des im unteren Teil des ersten Reaktors (20) erhaltenen Produktes und an seinem oberen Teil mit einer Leitung (29) zum Abziehen des bei Austritt aus der Behandlung in diesem zweiten Reaktor erhaltenen Produktes versehen ist, wobei diese ersten und zweiten Reaktoren (20) und (28) in ihrem unteren Teil über wenigstens eine Leitung (30) verbunden sind.
  16. Vorrichtung nach Anspruch 15, dadurch gekennzeichnet, daß sie Mittel (32) und/oder (42) zum Einführen einer kohlenwasserstoffhaltigen Phase in das Reaktionsmedium des zweiten Reaktors umfaßt.
  17. Vorrichtung nach Anspruch 16, dadurch gekennzeichnet, daß die Mittel zum Einführen einer kohlenwasserstoffhaltigen Phase durch wenigstens eine Leitung (32) gebildet sind, die im unteren Teil des zweiten Reaktors angeordnet ist.
  18. Vorrichtung nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, daß sie Mittel (33) zum Einführen eines Schleppfluids am unteren Teil des zweiten Reaktors (28) umfaßt.
EP93401080A 1992-05-07 1993-04-26 Verfahren und Einrichtung zum katalytischen Kracken in zwei aufeinanderfolgenden Reaktionszonen Expired - Lifetime EP0573316B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9205714A FR2690922B1 (fr) 1992-05-07 1992-05-07 Procede et dispositif de craquage catalytique dans deux zones reactionnelles successives.
FR9205714 1992-05-07

Publications (2)

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EP0573316A1 EP0573316A1 (de) 1993-12-08
EP0573316B1 true EP0573316B1 (de) 1998-07-22

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US (1) US5498326A (de)
EP (1) EP0573316B1 (de)
JP (1) JP3345690B2 (de)
KR (1) KR100251425B1 (de)
CA (1) CA2095794C (de)
DE (1) DE69319800T2 (de)
ES (1) ES2120487T3 (de)
FR (1) FR2690922B1 (de)

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Publication number Priority date Publication date Assignee Title
US6299759B1 (en) 1998-02-13 2001-10-09 Mobil Oil Corporation Hydroprocessing reactor and process with gas and liquid quench
FR2785907B1 (fr) * 1998-11-13 2001-01-05 Inst Francais Du Petrole Procede et dispositif de craquage catalytique comprenant des reacteurs a ecoulements descendant et ascendant
US6339181B1 (en) 1999-11-09 2002-01-15 Exxonmobil Chemical Patents, Inc. Multiple feed process for the production of propylene
FR2811327B1 (fr) 2000-07-05 2002-10-25 Total Raffinage Distribution Procede et dispositif de craquage d'hydrocarbures mettant en oeuvre deux chambres reactionnelles successives
BR0309560B1 (pt) 2002-04-26 2013-06-18 reator de craqueamento catalÍtico de fluxo descendente e sua aplicaÇço
US7087154B2 (en) * 2002-12-30 2006-08-08 Petroleo Brasileiro S.A. - Petrobras Apparatus and process for downflow fluid catalytic cracking
US8435401B2 (en) 2009-01-06 2013-05-07 Process Innovators, Inc. Fluidized catalytic cracker with active stripper and methods using same
RU2705236C1 (ru) * 2018-12-24 2019-11-06 Армен Каренович Мартиросян Виброакустическое устройство для реализации коронарной эндартерэктомии

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Publication number Priority date Publication date Assignee Title
US2307879A (en) * 1941-07-12 1943-01-12 Standard Oil Dev Co Catalytic conversion process
NL99020C (de) * 1954-06-28
US3607730A (en) * 1968-04-05 1971-09-21 Pullman Inc Apparatus and method for conversion of hydrocarbons
US3826738A (en) * 1972-03-23 1974-07-30 F Zenz Folded transfer line reactor
US4385985A (en) * 1981-04-14 1983-05-31 Mobil Oil Corporation FCC Reactor with a downflow reactor riser
FR2626284B1 (fr) * 1988-01-26 1990-06-08 Total France Appareil pour le craquage catalytique en lit fluidise d'une charge d'hydrocarbures
WO1989007010A1 (en) * 1988-01-29 1989-08-10 Thacker Milton P Low profile fluid catalytic cracking apparatus and method

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Publication number Publication date
DE69319800D1 (de) 1998-08-27
DE69319800T2 (de) 1998-11-26
KR100251425B1 (ko) 2000-04-15
FR2690922A1 (fr) 1993-11-12
KR930023442A (ko) 1993-12-18
JPH0633073A (ja) 1994-02-08
US5498326A (en) 1996-03-12
JP3345690B2 (ja) 2002-11-18
EP0573316A1 (de) 1993-12-08
FR2690922B1 (fr) 1994-07-22
CA2095794A1 (fr) 1993-11-08
ES2120487T3 (es) 1998-11-01
CA2095794C (fr) 2003-10-07

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