EP0485259B1 - Verfahren und Einrichtung für Homogenisierung in ein röhrenformige Kohlenwasserstoff-Krackreaktor mit Wirbelbett von feste Teilchen, von das Gemisch von diese Teilchen und die zu behandeln Kohlenwasserstoffen - Google Patents

Verfahren und Einrichtung für Homogenisierung in ein röhrenformige Kohlenwasserstoff-Krackreaktor mit Wirbelbett von feste Teilchen, von das Gemisch von diese Teilchen und die zu behandeln Kohlenwasserstoffen Download PDF

Info

Publication number
EP0485259B1
EP0485259B1 EP91402913A EP91402913A EP0485259B1 EP 0485259 B1 EP0485259 B1 EP 0485259B1 EP 91402913 A EP91402913 A EP 91402913A EP 91402913 A EP91402913 A EP 91402913A EP 0485259 B1 EP0485259 B1 EP 0485259B1
Authority
EP
European Patent Office
Prior art keywords
reactor
particles
fluid
charge
treated
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
EP91402913A
Other languages
English (en)
French (fr)
Other versions
EP0485259A1 (de
Inventor
Vincent Demoulin
Marc Fersing
Thierry Patureaux
Denis Pontvianne
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.)
Total Marketing Services SA
Original Assignee
Total Raffinage Distribution SA
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 Total Raffinage Distribution SA filed Critical Total Raffinage Distribution SA
Priority to AT91402913T priority Critical patent/ATE97688T1/de
Publication of EP0485259A1 publication Critical patent/EP0485259A1/de
Application granted granted Critical
Publication of EP0485259B1 publication Critical patent/EP0485259B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

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

Definitions

  • Method and device for homogenization inside a tubular hydrocarbon cracking reactor with a bed of fluidized solid particles, of the mixture of these particles and of the hydrocarbon vapors to be treated.
  • the present invention relates to a process and a device for the homogenization, inside a tubular hydrocarbon cracking reactor with a bed of fluidized solid particles, of the mixture of these particles and of the hydrocarbon vapors to be treated.
  • the invention more particularly relates to a process and a device of this type applicable to catalytic cracking in the fluid state of hydrocarbon feeds, in a substantially vertical tubular reactor, operating in an ascending or descending fluidized bed.
  • the most commonly used process at present is the so-called fluid catalytic cracking process (in English, Fluid Catalytic Cracking, or FCC process).
  • FCC process Fluid Catalytic Cracking
  • other fluidized bed conversion methods have been developed, in particular thermal cracking or visbreaking methods.
  • EP-A- O 369 536 describes the injection of a hydrocarbon light liquid, sprayed in the form of droplets, in a cracking reactor, downstream of the injection zone of the hydrocarbon charge to be treated, so as to cause a quenching effect and to limit the temperature in the reaction zone to optimize the production of the desired products.
  • This injection of an auxiliary liquid has no effect on the distribution of the solid particles of catalyst inside the reactor.
  • the temperature distribution is not uniform over the entire section of the reaction zone downstream of the charge injectors. It is too hot at the periphery of the reactor, because the density of the grains is too high near the walls, which causes the overcracking of the charge, harms the desired liquid conversion and therefore promotes the production of dry gases. Conversely, when the pulverized charge comes into contact with a flow of insufficiently dense grains of catalyst in the central part of the reactor, the quantity of heat provided by these grains is insufficient to reach the temperature required for the desired reactions to take place, and a coking significant catalyst occurs, the catalyst then becoming inactive.
  • the present invention aims to remedy these drawbacks by proposing means capable of ensuring a homogeneous distribution of the hot solid particles, in particular catalyst particles, in a cracking reactor for hydrocarbons with a fluidized bed, upward or downward flow, downstream of the injection zone in the reactor of the hydrocarbon charge to be treated.
  • the invention also aims to standardize, throughout the reaction zone of such a fluidized bed cracking reactor, the contact between the hot catalyst particles and the hydrocarbon vapors.
  • the invention finally aims to standardize the speed of the fluids and to avoid any back-mixing downstream of the injection zone of the charge of hydrocarbons to be cracked in such a hydrocarbon cracking reactor.
  • the subject of the present invention is a process for homogenization, inside a tubular hydrocarbon cracking reactor with a bed of hot fluidized solid particles, of the mixture of these particles and of the hydrocarbon vapors with process, process in which the tubular reactor, which is arranged substantially vertically, is continuously supplied with a flow of hot solid particles, these particles, in the reactor, are given an upward or downward movement while maintaining them in a dilute fluidized bed, they are brought into contact with these particles at least one charge of hydrocarbons to be cracked, by injecting this charge into the diluted fluidized bed inside the reactor, the gaseous phase is separated, resulting from the contacting of the hydrocarbons with said particles and these particles, recovers the gas phase and the particles thus separated, said particles are optionally treated to reactivate them and they are recycled to the reactor supply, this process being characterized in that immediately downstream of the injection zone, in the reaction zone of the charge to be treated where at least 75% of the charge drops are vaporized, a fluid is injected in the gaseous state
  • the fluid in the gaseous state will be injected into the reactor at a plurality of locations distributed evenly on the internal wall thereof, either annularly or helically.
  • This fluid in the gaseous state may be injected into the reactor in a plane making with the axis of the reactor an angle between 30 and 150 °.
  • the gaseous fluid may also be introduced into the reactor substantially tangentially to the side wall of the reactor.
  • the fluid in the gaseous state may be hydrogen, an inert gas, a light hydrocarbon such as methane, ethane, propane, butane or pentane, a vaporized gasoline, or, preferably, water vapor.
  • a light hydrocarbon such as methane, ethane, propane, butane or pentane
  • a vaporized gasoline or, preferably, water vapor.
  • the flow rate of injected fluid may represent between 0.005% and 1% by weight of the flow rate of solid grains in circulation.
  • the speed of the fluid in the gaseous state, at the outlet of the device for injecting this fluid will generally be between 1 and 100 m / s and preferably between 20 and 50 m / s.
  • the injection pressure of the gaseous fluid will naturally depend on this injection speed and the reactor operating conditions.
  • the injection temperature of this fluid has no significant influence on the temperature profile of the grains downstream of the charge injection zone, due to the low flow rate of fluid injected relative to the catalytic mass of the circulating fluidized bed.
  • the invention also relates to a homogenization device, inside a tubular hydrocarbon cracking reactor with a bed of hot fluidized solid particles, of the mixture of these particles and of the hydrocarbon vapors to be treated, this reactor being disposed substantially vertically and comprising means for continuously supplying a flow of hot solid particles, means for imparting an upward or downward motion to these particles in the reactor while maintaining them in a diluted fluidized bed, means for injection inside the reactor, into the diluted fluidized bed, of at least one charge of hydrocarbons, means for separating the gaseous phase resulting from the contacting of these hydrocarbons with said particles, means of separation and for recovering this gaseous phase and the solid particles, optionally means for treating the particles recovered for the reaction, and m means for recycling these particles to the reactor supply, this device being characterized in that it comprises, immediately downstream of the injection zone of the hydrocarbon charge, in at least one location on the internal face of the side wall of the reactor, a means for injecting a gaseous fluid into the reactor.
  • the means for injecting the fluid in the gaseous state will preferably be placed at a distance of between 0.5 and 6 times the radius of said reactor, downstream and from the charge injectors.
  • the means for injecting the fluid in the gaseous state may comprise a chamber connected to a source of gas under pressure, this chamber opening into the reactor through at least one orifice.
  • a chamber connected to a source of gas under pressure, this chamber opening into the reactor through at least one orifice.
  • several chambers will be provided and will open into the reactor through a plurality of orifices distributed regularly in an annular or helical manner relative to the axis of the reactor, these orifices preferably having the form of slots.
  • the means for injecting the gaseous fluid into the reactor may comprise at least one injector connected to a source of pressurized gas, the axis of this injector being substantially tangent to the side wall internal of the reactor.
  • the reactor will comprise several injectors distributed regularly around its axis and connected to a manifold, itself supplied by the source of gas under pressure. Due to the jets of gaseous fluid introduced tangentially by the injectors, in this embodiment of the invention, the solid particles adjacent to the internal face of the wall of the reactor will be brought, inside the latter, of a helical movement.
  • the regenerated catalyst is introduced at the base of the tubular reactor 1 by a line 2, at a flow rate determined by the opening or closing of a valve 3.
  • the grains of catalyst are then propelled towards the top of the reactor by injection, at the base of the latter, of a gaseous fluid coming from line 5; this injection is made using a fluid distributor or "diffuser" 4.
  • the charge to be cracked is introduced at a higher level by the line 7, using appropriate spraying devices 6, into the flow of catalyst grains.
  • the reactor 1 opens at its top into an enclosure 8 which is concentric here and in which, on the one hand, the separation between gaseous effluents and the grains of the catalyst takes place, thanks to the ballistic separator 9, and, d on the other hand, the stripping of the catalyst grains deactivated.
  • the reaction products are separated from any catalyst in a cyclonic system 10, which is housed in the upper part of the enclosure 8 and at the top of which is provided a line 11 for discharging the reaction effluents to the outside.
  • the grains of deactivated catalyst descend to the base of the enclosure 8, where the diffuser 13 supplies the fluidized bed with stripping gas (generally steam) through a line 12.
  • stripping gas generally steam
  • the regenerator 14 here comprises a single regeneration, where the grains of deactivated catalyst are introduced into the upper part of the fluidized bed 17, while the combustion fumes are discharged through line 18, after passing through a cyclone 19.
  • the catalyst grains are regenerated in a fluidized bed, by combustion of the coke and of the hydrocarbons still present on their surface or in their pores, by means of an injection of air or oxygen, by the diffuser 20, supplied by the line 21.
  • the catalyst grains thus brought to high temperature by the heat of combustion, return to the base of reactor 1 via line 2.
  • This brutal vaporization has the effect of throwing the catalyst grains towards the side wall of the reactor 1, and this results in an irregular distribution of the catalyst grains downstream of the injection zone of the hydrocarbon charge, with a risk of back mixing in the vicinity of the internal face of the wall 25 of the reactor 1.
  • a gas flow is injected into the reactor, immediately downstream of the devices 6 for spraying the hydrocarbon charge, capable of repelling the particles of catalyst in the direction of the axis of the reactor.
  • each of the chambers 26 are housed in the thickness of the wall 25 of the reactor 1.
  • These chambers 26 are connected by conduits 28 to a source of pressurized gas and each of them opens out through two slots 29 inside the reactor 1.
  • the eight slots 29 are distributed in an annular manner regularly around the axis of the reactor 1 .
  • the gas jets injected through the slits 29 are directed perpendicular to the wall 25 towards the interior of the reactor 1 and thus prevent the catalyst particles from accumulating in the vicinity of the wall 25, ensuring better contact between the vapors d hydrocarbons and catalyst particles.
  • water vapor can be used as a gas at a temperature of the order of 350 ° C. and an effective pressure of approximately 18 bars.
  • the reactor 31 comprises two systems for fluidizing the particles of regenerated catalyst recycled into the reactor by line 32.
  • a first diffuser 34 supplied by line 35, injects at the base of the reactor 31 , below the connection of line 32 to the reactor, a sufficient quantity of fluid to maintain dense fluidization ensuring homogenization of the grains in this zone.
  • a second diffuser 43 supplied by line 44 and disposed downstream of the connection of line 2 to the reactor, then makes it possible to inject the quantity of fluid necessary to create dilute fluidization conditions, with a constant flow of grains, which rise then in the reactor at an axial speed greater than 1.5 m / s and, preferably, between 2 and 10 m / s.
  • a system for injecting a gaseous fluid in the area immediately downstream of the devices 36 for spraying the hydrocarbon charge, there is provided a system for injecting a gaseous fluid, tangential to the wall of the reactor, at four points arranged symmetrically. in a plane perpendicular to the axis of the reactor.
  • Each of the injection tubes 46 is connected to a distributor 45 of the fluid, supplied by the line 47.
  • the tangential injections practiced simultaneously at several points of the reactor therefore allow the fluidized phase located in the vicinity of the reactor wall to be rotated. 3, with a rotational speed directly proportional to the quantity of fluid injected.
  • the gaseous fluid will preferably be of the same type as that used for the fluidization of the catalyst grains.
  • the angle between the injectors and the plane perpendicular to the axis of symmetry of the reactor will preferably be small, so as to minimize the amount of fluid to be injected to obtain the desired rotation.
  • these injectors must respect as much as possible the symmetry of revolution of the reactor, in order to obtain good homogeneity of the fluidized bed.
  • FIG. 6 finally illustrates the use of a homogenization device in accordance with the invention in a tubular reactor with dilute downward flow of catalyst particles.
  • the regenerated catalyst particles are introduced into the upper part of the reactor 51 via line 52 and flow there by gravity.
  • a valve 53 is provided to control the flow of catalyst.
  • a diffuser 55 supplied with gas by the line 54 first keeps the gas particles in a dense fluidized bed upstream of the valve 53. Downstream of this valve, the catalyst is maintained in the diluted fluidized phase by injection of a second gas in the reactor through the diffuser 58 supplied by the line 57.
  • the charge to be cracked is then introduced into the reactor 55 by sprayers 56 directed in the direction of the flow of the grains in the reactor and inclined relative to the axis thereof thereof by an angle of, for example, between 30 and 60 °.
  • a homogenization device Immediately downstream of these sprayers 56 is provided a homogenization device according to the invention of the same type as that of FIG. 5, that is to say comprising injectors 66, arranged tangentially to the reactor 51 and connected to a distributor 65, itself supplied with pressurized gas by a line 67.

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)

Claims (13)

  1. Verfahren zum Homogenisieren im Inneren eines rohrförmigen Reaktors zum Kracken von Kohlenwasserstoffen mit einer Wirbelschicht heißer Feststoffteilchen, und zwar zum Homogenisieren des Gemisches der Teilchen und der zu behandelnden Kohlenwasserstoffdämpfe, wobei der im wesentlichen vertikal angeordnete rohrförmige Reaktor kontinuierlich mit einem Strom heißer Feststoffteilchen gespeist wird, den Teilchen im Reaktor eine steigende oder fallende Bewegung vermittelt wird, wobei sie in verdünnter Wirbelschicht gehalten werden, mindestens eine Charge zu krackender Kohlenwasserstoffe mit den Teilchen in Berührung gebracht wird, indem die Charge in die verdünnte Wirbelschicht im Inneren des Reaktors eingespritzt wird, die sich aus dem Inberührungbringen der Kohlenwasserstoffe mit den Teilchen ergebende Gasphase und die Teilchen getrennt werden, die Gasphase und die Teilchen, welche so getrennt wurden, gewonnen werden, die Teilchen gegebenenfalls behandelt werden, um sie zu reaktivieren, und sie wieder zur Speisung des Reaktors verwendet werden, dadurch gekennzeichnet, daß unmittelbar stromabwärts von der Einspritzzone in die Reaktionszone der zu behandelnden Charge, wo mindestens 75 % der Chargentropfen verdampft sind, ein Strömungsmittel im gasförmigen Zustand in den Reaktor eingeblasen wird, und zwar an mindestens einer Stelle der Innenseite seiner Seitenwand.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das Strömungsmittel Im gasförmigen Zustand an mehreren Stellen in den Reaktor eingeblasen wird, welche gleichmäßig auf der Innenwand desselben verteilt sind, und zwar ringförmig oder schraubenförmig.
  3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß das Strömungsmittel im gasförmigen Zustand in einer Ebene in den Reaktor eingeblasen wird, welche mit dessen Achse einen Winkel zwischen 30 und 150° einschließt.
  4. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß das Strömungsmittel im gasförmigen Zustand im wesentlichen tangential zur Seitenwand des Reaktors in denselben eingeblasen wird.
  5. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekenneichnet, daß das Strömungsmittel im gasförmigen Zustand aus der Gruppe ausgewählt wird, welche Wasserstoff, die inerten Gase, wie Stickstoff, die leichten Kohlenwasserstoffe mit I bis 5 Kohlenstoffatomen, die verdampften Kraftstoffe und Wasserdampf umfaßt.
  6. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekenneichnet, daß das Strömungsmittel im gasförmigen Zustand mit einem Durchsatz in den Reaktor eingeblasen wird, welcher zwischen 0,005 und 1 % des Gewichts des Durchsatzes zirkulierender Feststoffkörner ausmacht.
  7. Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekenneichnet, daß das Strömungsmittel im gasförmigen Zustand mit einer Geschwindigkeit in den Reaktor eingeblasen wird, welche zwischen 1 und 100 m/s, vorzugsweise zwischen 20 und 50 m/s, liegt.
  8. Vorrichtung zum Homogenisieren im Inneren eines rohrförmigen Reaktors zum Kracken von Kohlenwasserstoffen mit einer Wirbelschicht heißer Feststoffteilchen, und zwar zum Homogenisieren des Gemisches der Teilchen und der zu behandelnden Kohlenwasserstoffdämpfe, wobei der Reaktor (1, 31, 51) im wesentlichen vertikal angeordnet ist und Mittel (2, 32, 52) zum kontinuierlichen Einspeisen eines Stromes heißer Feststoffteilchen, Mittel (4; 35, 43; 55, 58), um den Teilchen im Reaktor eine steigende oder fallende Bewegung zu vermitteln, wobei sie in verdünnter Wirbelschicht gehalten werden, Mittel (6, 36, 56) zum Einspritzen mindestens einer Kohlenwasserstoffcharge in die verdünnte Wirbelschicht im Inneren des Reaktors, Mittel (8, 9, 10) zum Trennen der sich aus dem Inberührungbringen der Kohlenwasserstoffe mit den Teilchen ergebenden Gasphase, Mittel zum Trennen und zum Gewinnen der Gasphase und der Feststoffteilchen, gegebenenfalls Mittel (14) zur Behandlung der gewonnenen Teilchen, um Sie zu reaktivieren, und Mittel zur neuerlichen Einspeisung der Teilchen in den Reaktor aufweist, dadurch gekenneichnet, daß unmittelbar stromabwärts von der Einspritzzone der Kohlenwasserstoffcharge an mindestens einer Stelle der Innenseite der Seitenwand (25) des Reaktors ein Mittel (26, 29; 46; 66) zum Einblasen eines gasförmigen Strömungsmittels in den Reaktor vorgesehen ist.
  9. Vorrichtung nach Anspruch 8, dadurch gekennzeichnet, daß die Mittel zum Einblasen des Strömungsmittels im gasförmigen Zustand in einem Abstand stromabwärts von den Chargeninjektoren angeordnet sind, welcher zwischen dem 0,5- und dern 6-fachen des Reaktorradius liegt.
  10. Vorrichtung nach Anspruch 8 oder 9, dadurch gekenneichnet, daß die Mittel zum Einblasen des gasförmigen Strömungsmittels eine Kammer (26) aufweisen, welche in der Dicke der Wand (25) des Reaktors ausgebildet und mit einer Druckgasquelle verbunden ist, wobei die Kammer (26) mit mindestens einer Öffnung (29) in den Reaktor (1) mündet.
  11. Vorrichtung nach Anspruch 10, dadurch gekennzeichnet, daß mehrere Kammern (26) und Öffnungen (29) vorgesehen sind, welche gleichmäßig um die Achse des Reaktors herum verteilt sind, und zwar ringförmig oder schraubenförmig, wobei die Öffnungen vorzugsweise schlitzförmig ausgebildet sind.
  12. Vorrichtung nach Anspruch 8, dadurch gekenneichnet, daß die Mittel zum Einblasen des gasförmigen Strömungsmittels in den Reaktor (31, 51) mindestens einen Injektor (46, 66) aufweisen, welcher mit einer Druckgasquelle verbunden ist und dessen Achse sich im wesentlichen tangen- tial zur inneren Seitenwand des Reaktors sowie senkrecht zu dessen Achse erstreckt.
  13. Vorrichtung nach Anspruch 12, dadurch gekennzeichnet, daß mehrere Injektoren (46, 66) vorgesehen sind, welche gleichmäßig um die Achse des Reaktors (31, 51) herum verteilt und mit einem von der Druck- gasquelle gespeisten Sammler (45, 65) verbunden sind.
EP91402913A 1990-11-08 1991-10-30 Verfahren und Einrichtung für Homogenisierung in ein röhrenformige Kohlenwasserstoff-Krackreaktor mit Wirbelbett von feste Teilchen, von das Gemisch von diese Teilchen und die zu behandeln Kohlenwasserstoffen Expired - Lifetime EP0485259B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT91402913T ATE97688T1 (de) 1990-11-08 1991-10-30 Verfahren und einrichtung fuer homogenisierung in ein roehrenformige kohlenwasserstoff-krackreaktor mit wirbelbett von feste teilchen, von das gemisch von diese teilchen und die zu behandeln kohlenwasserstoffen.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9013874 1990-11-08
FR9013874A FR2669037A1 (fr) 1990-11-08 1990-11-08 Procede et dispositif d'homogeneisation, a l'interieur d'un reacteur tubulaire de craquage d'hydrocarbures a lit de particules solides fluidisees, du melange de ces particules et des vapeurs d'hydrocarbures a traiter.

Publications (2)

Publication Number Publication Date
EP0485259A1 EP0485259A1 (de) 1992-05-13
EP0485259B1 true EP0485259B1 (de) 1993-11-24

Family

ID=9401986

Family Applications (1)

Application Number Title Priority Date Filing Date
EP91402913A Expired - Lifetime EP0485259B1 (de) 1990-11-08 1991-10-30 Verfahren und Einrichtung für Homogenisierung in ein röhrenformige Kohlenwasserstoff-Krackreaktor mit Wirbelbett von feste Teilchen, von das Gemisch von diese Teilchen und die zu behandeln Kohlenwasserstoffen

Country Status (8)

Country Link
US (1) US5338438A (de)
EP (1) EP0485259B1 (de)
JP (1) JP2996791B2 (de)
AT (1) ATE97688T1 (de)
DE (1) DE69100683T2 (de)
ES (1) ES2060332T3 (de)
FR (1) FR2669037A1 (de)
ZA (1) ZA918891B (de)

Families Citing this family (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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.
US5851380A (en) * 1996-08-01 1998-12-22 Phillips Petroleum Company Process and apparatus for fluidized catalytic cracking of a hydrocarbon feed
CN1243609C (zh) * 1997-03-14 2006-03-01 日石三菱株式会社 一种混合装置
FR2770225B1 (fr) * 1997-10-24 2000-01-07 Total Raffinage Distribution Procede et dispositif de vaporisation selective des charges d'hydrocarbures en craquage catalytique
US6042717A (en) * 1997-12-05 2000-03-28 Uop Llc Horizontal FCC feed injection process
FR2791354B1 (fr) 1999-03-25 2003-06-13 Inst Francais Du Petrole Procede de conversion de fractions lourdes petrolieres comprenant une etape d'hydroconversion en lits bouillonnants et une etape d'hydrotraitement
US6613290B1 (en) 2000-07-14 2003-09-02 Exxonmobil Research And Engineering Company System for fluidized catalytic cracking of hydrocarbon molecules
US20110058989A1 (en) * 2009-09-09 2011-03-10 Uop Llc Apparatus for contacting hydrocarbon feed and catalyst
US8691081B2 (en) * 2009-09-09 2014-04-08 Uop Llc Process for contacting hydrocarbon feed and catalyst
CN103827262B (zh) 2011-07-29 2015-12-23 沙特***石油公司 用于流化催化裂化方法的富氢原料
FR2981659B1 (fr) 2011-10-20 2013-11-01 Ifp Energies Now Procede de conversion de charges petrolieres comprenant une etape d'hydroconversion en lit bouillonnant et une etape d'hydrotraitement en lit fixe pour la production de fiouls a basse teneur en soufre
FR2983866B1 (fr) 2011-12-07 2015-01-16 Ifp Energies Now Procede d'hydroconversion de charges petrolieres en lits fixes pour la production de fiouls a basse teneur en soufre
FR2999600B1 (fr) 2012-12-18 2015-11-13 IFP Energies Nouvelles Procede de raffinage d'une charge hydrocarbonee lourde mettant en oeuvre un desasphaltage selectif
FR3000097B1 (fr) 2012-12-20 2014-12-26 Ifp Energies Now Procede integre de traitement de charges petrolieres pour la production de fiouls a basse teneur en soufre
FR3000098B1 (fr) 2012-12-20 2014-12-26 IFP Energies Nouvelles Procede avec separation de traitement de charges petrolieres pour la production de fiouls a basse teneur en soufre
US8936761B1 (en) * 2013-08-21 2015-01-20 Uop Llc Apparatuses and risers for reacting feedstock in the presence of catalyst and methods for fabricating risers
US9073030B2 (en) * 2013-08-21 2015-07-07 Uop Llc Apparatuses and risers for reacting feedstock in the presence of catalyst and methods for installing baffles in risers

Family Cites Families (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2906695A (en) * 1956-08-07 1959-09-29 Exxon Research Engineering Co High temperature short time hydrocarbon conversion process
US2901420A (en) * 1956-12-24 1959-08-25 Shell Dev Process of separating catalyst particles from hydrocarbon vapors
US4036779A (en) * 1976-10-20 1977-07-19 Mobil Oil Corporation Method of regenerating catalyst in a swirl type regenerator containing a dilute phase baffle
US4534851A (en) * 1983-06-02 1985-08-13 Exxon Research And Engineering Co. Feed injection method to prevent coking on the walls of transfer line reactors
US4753780A (en) * 1983-09-26 1988-06-28 Phillips Petroleum Company Atomizing feed for cracking unit
US4479870A (en) * 1984-02-29 1984-10-30 Jop Inc. Use of lift gas in an FCC reactor riser
US4615992A (en) * 1985-04-02 1986-10-07 Air Products And Chemicals, Inc. Catalyst regeneration process with improved catalyst distribution in a fluidized bed
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
CA1327177C (en) * 1988-11-18 1994-02-22 Alan R. Goelzer Process for selectively maximizing product production in fluidized catalytic cracking of hydrocarbons
US4994424A (en) * 1989-11-06 1991-02-19 Mobil Oil Corporation Catalytic cracking process with improved flow in swirl regenerator
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.

Also Published As

Publication number Publication date
ATE97688T1 (de) 1993-12-15
US5338438A (en) 1994-08-16
FR2669037A1 (fr) 1992-05-15
DE69100683D1 (de) 1994-01-05
FR2669037B1 (de) 1993-02-26
ZA918891B (en) 1993-03-31
JPH05186780A (ja) 1993-07-27
JP2996791B2 (ja) 2000-01-11
EP0485259A1 (de) 1992-05-13
ES2060332T3 (es) 1994-11-16
DE69100683T2 (de) 1994-06-16

Similar Documents

Publication Publication Date Title
EP0485259B1 (de) Verfahren und Einrichtung für Homogenisierung in ein röhrenformige Kohlenwasserstoff-Krackreaktor mit Wirbelbett von feste Teilchen, von das Gemisch von diese Teilchen und die zu behandeln Kohlenwasserstoffen
EP0208609B2 (de) Verfahren und Einrichtung für das katalytische Kracken von Kohlenwasserstoffen mit Kontrolle der Reaktionstemperatur
EP0191695B1 (de) Verfahren und Einrichtung für die Injektion von Katalysator in ein katalytisches Wirbelschichtkrackverfahren, insbesondere von schweren Einsätzen
EP0323297B1 (de) Wirbelschichtverfahren zur Kohlenwasserstoffumwandlung
FR2667609A1 (fr) Procede et dispositif de craquage catalytique en lit fluide a courant descendant.
EP0184517B1 (de) Verfahren und Anlagen für das katalytische Kracken von Kohlenwasserstoffeinsätzen
FR2654435A1 (fr) 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.
EP0960929B1 (de) Verfahren und Vorrichtung zur Einführung von Katalysatorteilchen in einem katalytischen Wirbelschichtspaltungsreaktor
EP0226483B1 (de) Verfahren und Vorrichtung für die katalytische Spaltung eines mit wenig aktiven Festteilchen vorbehandelten Kohlenwasserstoffeinsatzes
EP0489726B1 (de) Verfahren und einrichtung zum dampfkracken von kohlenwasserstoffen in der wirbelschichtphase
EP0874880B1 (de) Fluidkatalytisch krackverfahren und -einrichtung fur kohlenwasserstoffeinsätze
EP0861310B1 (de) Methode und vorrichtung zum katalytischen craken mit fluss in abwärtsrichtung durch einspritzung vom ausgangsstoff in einem gezielten winkel auf den konditionierten katalysator
FR2877671A1 (fr) Dispositif et procede pour le craquage catalytique de deux charges distinctes d'hydrocarbures
EP0291408B1 (de) Dampfspaltungsverfahren in einer Wirbelschicht-Reaktionszone
FR2610638A1 (fr) Perfectionnements aux procedes et dispositifs pour le craquage catalytique de charges d'hydrocarbures
CA2250342A1 (fr) Procede et dispositif de vaporisation selective des charges d'hydrocarbures en craquage catalytique
EP0536054B1 (de) Verbesserungen an Vorrichtungen für das katalytische Wirbelschichtkracken von Kohlenwasserstoffeinsätzen
FR2605643A1 (fr) Procede et dispositif pour le craquage catalytique en lit fluidise d'une charge d'hydrocarbures
FR2624877A1 (fr) Procede et dispositif pour le craquage catalytique de charges lourdes comportant un second strippage en lit fluide
WO1991003527A1 (fr) Procede et dispositif de vapocraquage d'hydrocarbures en phase fluidisee
FR2599376A1 (fr) Procede et appareil de craquage catalytique d'une charge hydrocarbonee soumise a un pretraitement par des particules de solides peu actives

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE CH DE DK ES GB GR IT LI LU NL SE

17P Request for examination filed

Effective date: 19920807

17Q First examination report despatched

Effective date: 19921127

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

ITF It: translation for a ep patent filed

Owner name: BARZANO' E ZANARDO MILA

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE CH DE DK ES GB GR IT LI LU NL SE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Effective date: 19931124

Ref country code: NL

Effective date: 19931124

Ref country code: DK

Effective date: 19931124

Ref country code: AT

Effective date: 19931124

REF Corresponds to:

Ref document number: 97688

Country of ref document: AT

Date of ref document: 19931215

Kind code of ref document: T

REF Corresponds to:

Ref document number: 69100683

Country of ref document: DE

Date of ref document: 19940105

REG Reference to a national code

Ref country code: GR

Ref legal event code: FG4A

Free format text: 3009907

GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)

Effective date: 19940222

NLV1 Nl: lapsed or annulled due to failure to fulfill the requirements of art. 29p and 29m of the patents act
PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 19941031

Ref country code: LI

Effective date: 19941031

Ref country code: CH

Effective date: 19941031

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2060332

Country of ref document: ES

Kind code of ref document: T3

26N No opposition filed
REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 20010924

Year of fee payment: 11

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GR

Payment date: 20010927

Year of fee payment: 11

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20011004

Year of fee payment: 11

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 20011010

Year of fee payment: 11

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: ES

Payment date: 20011024

Year of fee payment: 11

REG Reference to a national code

Ref country code: GB

Ref legal event code: IF02

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20021030

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: ES

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20021031

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20021031

BERE Be: lapsed

Owner name: S.A. *TOTAL RAFFINAGE DISTRIBUTION

Effective date: 20021031

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20030501

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20030506

GBPC Gb: european patent ceased through non-payment of renewal fee
REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20031112

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED.

Effective date: 20051030