EP0573316A1 - Verfahren und Einrichtung zur katalytischen Brechung in zwei aufeinanderfolgenden Reaktionszonen - Google Patents

Verfahren und Einrichtung zur katalytischen Brechung in zwei aufeinanderfolgenden Reaktionszonen Download PDF

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Publication number
EP0573316A1
EP0573316A1 EP93401080A EP93401080A EP0573316A1 EP 0573316 A1 EP0573316 A1 EP 0573316A1 EP 93401080 A EP93401080 A EP 93401080A EP 93401080 A EP93401080 A EP 93401080A EP 0573316 A1 EP0573316 A1 EP 0573316A1
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EP
European Patent Office
Prior art keywords
reactor
reaction
reaction zone
catalyst
zone
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EP93401080A
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English (en)
French (fr)
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EP0573316B1 (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 process and a device for the catalytic cracking of hydrocarbon charges.
  • catalytic cracking processes have been devised in which the reaction medium is operated in a downward flow.
  • the catalyst is then introduced into the upper part of the reaction zone and the atomized hydrocarbon charge is injected into the same part but into the downward flow of the catalyst (patent documents US-A-4,385,985 and EP-A.254,333).
  • 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 and then at least partially recycled to the cracking reactor.
  • the Applicant proposes a method and a device making it possible to use a cracking reactor comprising a reaction zone with downward flow followed by a reaction zone with upward flow, which makes it possible to combine the advantages of an efficient reaction and of separation solid / gas improved.
  • a cracking reactor comprising a reaction zone with downward flow followed by a reaction zone with upward flow, which makes it possible to combine the advantages of an efficient reaction and of separation solid / gas improved.
  • Such a device can also be installed on existing units with costs lower than those due to changes in direction of flow.
  • the subject of the invention is a method for cracking hydrocarbon charges, the cracking reaction taking place in the presence of catalyst in a entrained or fluidized bed, the catalyst particles being, after reaction, separated from the gas phase , regenerated and at least partly recycled, process in which the cracking reaction takes place in two successive substantially vertical reaction zones, the charge being introduced into the upper part of a first reaction zone, then at least part of the product obtained at the lower part of said first zone is introduced into a second reaction zone where it circulates in an ascending manner.
  • Figures 2 and 3 show devices associated with said method.
  • the catalyst (2) which comes in part at least from the catalyst regeneration reactor (3).
  • the particle flow rates of the catalyst between the reactor (3) and the first reaction zone (4) are adjusted by a pressure difference caused for 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, up to 20 m / s more generally up to 5 m / s.
  • the apparent density of the suspended catalyst is then approximately 50 to 600 kg / m3.
  • the charge (5) previously heated to temperatures between 100 and 250 ° C. is then introduced in 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 obtained often from known means of atomization.
  • the hydrocarbon feedstocks to be treated advantageously consist of heavy hydrocarbons, that is to say having final boiling points of the order of 400 ° C., such as gas oils under vacuum, but also oils more heavy such as crude oils and vacuum residues.
  • These fillers may, if necessary, have received a preliminary treatment, for example a hydrotreatment in the presence of a catalyst of the Co-Mo type.
  • Light fillers can also be treated, which have boiling points below 400 ° C.
  • the preferred fillers for the process according to the invention contain fractions normally boiling up to 700 ° C. and more, and which may contain high percentages of asphaltic products, the carbon content Conradson up to 4% and even beyond. These charges can optionally be mixed with lighter hydrocarbon fractions, such as LCO and HOO.
  • the charge Upon contact with the catalyst, the charge vaporizes. It is then entrained by the catalyst current with which it flows in downward co-current in this first reaction zone (4) where cracking takes place in part (the speed of the downward flow in the reactor varies and is most often between 0.5 to 50 m / s and preferably 0.5 to 10 m / s).
  • the product obtained at the lower part of said first reaction zone (4) is transferred, at least in part and preferably in whole, to the lower part of the second reaction zone (6) located in the reactor (7) with substantially axis vertical.
  • the invention also provides suitable devices described below (U-shaped tubes, inclined ).
  • the reaction medium flows in the second reaction zone in an ascending manner, with speeds generally greater than 2 m / s and which can range up to 50 m / s, and preferably between 10 and 30 m / s.
  • a drive fluid at the lower part of the second reactor (or near this part, which is equivalent).
  • This fluid can be a naphtha or more 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 from 0 to 50% by weight, and preferably from 5 to 30%.
  • the hydrocarbon phase can consist of part of the charge to be treated. It can also be a light charge, that is to say a boiling point charge of less than 400 ° C, and most often from about 180 ° C to about 380 ° C.
  • the product obtained at the upper part 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 at least part of the particles is recycled to the first reaction zone.
  • the volume content of catalyst in the mixture entering the separator (9) can be reduced from 1.5 times to 2.0 times at least, by suitably injecting, for example, from 20 to 40% by weight of light hydrocarbons (8 ) with respect to the feed introduced in (5), with respect to the catalyst content of the mixture entering the separator if the latter was positioned at the bottom of the first reaction enclosure (1). This provides better separation efficiency.
  • Another object of the invention is a device for carrying out the process for catalytic cracking of a hydrocarbon feedstock according to the method which is the subject 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 the introduction of the catalyst into the upper part of the reactor, means (24) for the introduction of the charge to be treated atomized in the part upper part of the reactor, said means (24) being located below the means (21), and said reactor also being provided with an opening disposed at the lower part of the reactor and along its axis, for the evacuation of the product obtained, said device further comprising a second reactor (28) of substantially vertical axis, provided at its lower part with an opening for the introduction of the product obtained at the lower part of the first reactor (20) and provided at its upper part with '' a pipe (29) for the evacuation of the product obtained at the end of the treatment in the second reactor, said device also comprising at least one pipe (30) connecting the lower parts of the first and second reactor s.
  • It comprises the two successive reactors (20) and (28) of substantially vertical axis, the lower parts of which are connected by a pipe (30).
  • the catalyst is introduced by means (21) generally constituted by 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 an atomization means (26).
  • This pipe opens below the opening through which the catalyst is introduced, so as to introduce the charge into the downward moving catalyst.
  • the product obtained at the lower part (27) of the first reactor is transferred via line (30) to the second reactor.
  • Line (30) - or lines if necessary - must allow rapid transfer and with a low deposit of solid catalyst.
  • the bent shape shown in FIG. 2 is perfectly suitable, there is then a U-shaped device. The curvature and the spacing between the two reactors are then calculated so that the transfer is carried out properly under the conditions of the process.
  • FIG. 3 represents a pipe (30) inclined towards the second reactor, the transfer takes place by entrainment.
  • This configuration is particularly interesting because it is close to the current configuration of catalytic cracking processes, the charge being injected in recent processes most generally in (32) and / or (42).
  • the parts (20) and (30) are then not reaction zones and play a purely functional role in the transport of the catalyst. It is possible to keep in place in the part (28) one or more means (42) of injection-atomization of the hydrocarbon charge, which optionally makes it possible to inject a fraction of hydrocarbons to be converted into the ascending part. .
  • 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 (pipe (42) and / or (32) shown in FIG. 3) or near this part .
  • said means are constituted by aerators (34) arranged on the pipe (30) so that the direction of injection follows the movement of the catalyst (substantially tangential injection). This embodiment makes it possible to significantly reduce deposits.
  • the device can also include, at or near the bottom of the second reactor (28), a pipe (33) for the introduction of a fluid drive.
  • This fluid can be for example a hydrocarbon preferably liquid or gaseous, water or an inert gas such as for example nitrogen.

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  • 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)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
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)

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

Family

ID=9429682

Family Applications (1)

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EP93401080A Expired - Lifetime EP0573316B1 (de) 1992-05-07 1993-04-26 Verfahren und Einrichtung zum katalytischen Kracken in zwei aufeinanderfolgenden Reaktionszonen

Country Status (8)

Country Link
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)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2785907A1 (fr) * 1998-11-13 2000-05-19 Inst Francais Du Petrole Procede et dispositif de craquage catalytique comprenant des reacteurs a ecoulements descendant et ascendant
EP1170355A1 (de) * 2000-07-05 2002-01-09 Total Raffinage Distribution S.A. Verfahren und Einrichtung zum Cracken von Kohlenwasserstoffen in zwei aufeinanderfolgenden Reaktionstufen
US7153478B2 (en) 2002-04-26 2006-12-26 China Petroleum & Chemical Corporation Downflow catalytic cracking reactor and its application

Families Citing this family (5)

* Cited by examiner, † Cited by third party
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
US6339181B1 (en) * 1999-11-09 2002-01-15 Exxonmobil Chemical Patents, Inc. Multiple feed process for the production of propylene
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

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE539185A (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
EP0326478A1 (de) * 1988-01-26 1989-08-02 Société Anonyme dite: COMPAGNIE DE RAFFINAGE ET DE DISTRIBUTION TOTAL FRANCE Einrichtung für die katalytische Wirbelschichtspaltung eines Kohlenwasserstoffeinsatzes

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2307879A (en) * 1941-07-12 1943-01-12 Standard Oil Dev Co Catalytic conversion process
DE3885622T2 (de) * 1988-01-29 1994-04-28 John M Limburg Verfahren zum kracken mit flüssigen katalysator und vorrichtung dafür mit geringem querschnitt.

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE539185A (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
EP0326478A1 (de) * 1988-01-26 1989-08-02 Société Anonyme dite: COMPAGNIE DE RAFFINAGE ET DE DISTRIBUTION TOTAL FRANCE Einrichtung für die katalytische Wirbelschichtspaltung eines Kohlenwasserstoffeinsatzes

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2785907A1 (fr) * 1998-11-13 2000-05-19 Inst Francais Du Petrole Procede et dispositif de craquage catalytique comprenant des reacteurs a ecoulements descendant et ascendant
WO2000029508A1 (fr) * 1998-11-13 2000-05-25 Institut Francais Du Petrole Procede et dispositif de craquage catalytique comprenant des reacteurs a ecoulements descendant et ascendant
US6641715B1 (en) 1998-11-13 2003-11-04 Institut Francais Du Petrole Method and device for catalytic cracking comprising reactors with descending and ascending flows
EP1170355A1 (de) * 2000-07-05 2002-01-09 Total Raffinage Distribution S.A. Verfahren und Einrichtung zum Cracken von Kohlenwasserstoffen in zwei aufeinanderfolgenden Reaktionstufen
FR2811327A1 (fr) * 2000-07-05 2002-01-11 Total Raffinage Distribution Procede et dispositif de craquage d'hydrocarbures mettant en oeuvre deux chambres reactionnelles successives
US6767451B2 (en) 2000-07-05 2004-07-27 Total Raffinage Distribution S.A. Procedure and device for cracking of hydrocarbons using two successive reaction chambers
US7544333B2 (en) 2000-07-05 2009-06-09 Total Raffinage Distribution S.A. Device for cracking of hydrocarbons using two successive reaction chambers
US7153478B2 (en) 2002-04-26 2006-12-26 China Petroleum & Chemical Corporation Downflow catalytic cracking reactor and its application

Also Published As

Publication number Publication date
US5498326A (en) 1996-03-12
CA2095794A1 (fr) 1993-11-08
EP0573316B1 (de) 1998-07-22
CA2095794C (fr) 2003-10-07
DE69319800T2 (de) 1998-11-26
KR930023442A (ko) 1993-12-18
FR2690922B1 (fr) 1994-07-22
KR100251425B1 (ko) 2000-04-15
JP3345690B2 (ja) 2002-11-18
JPH0633073A (ja) 1994-02-08
ES2120487T3 (es) 1998-11-01
FR2690922A1 (fr) 1993-11-12
DE69319800D1 (de) 1998-08-27

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