EP0322276A1 - Verfahren und Einrichtung für das katalytische Kracken von schweren Einsätze, die eine zweite Wirbelschichtabstreifzone enthalten - Google Patents

Verfahren und Einrichtung für das katalytische Kracken von schweren Einsätze, die eine zweite Wirbelschichtabstreifzone enthalten Download PDF

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Publication number
EP0322276A1
EP0322276A1 EP88403159A EP88403159A EP0322276A1 EP 0322276 A1 EP0322276 A1 EP 0322276A1 EP 88403159 A EP88403159 A EP 88403159A EP 88403159 A EP88403159 A EP 88403159A EP 0322276 A1 EP0322276 A1 EP 0322276A1
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EP
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Prior art keywords
stripping
catalyst
zone
regeneration
gas
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EP88403159A
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English (en)
French (fr)
Inventor
Gérard Martin
Alain Feugier
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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

Definitions

  • the invention relates to a process and a device for catalytic cracking in a fluidized bed of hydrocarbon charges boiling above 400 ° C., comprising in particular an improvement in the stripping of the used catalyst.
  • the catalyst is kept in suspension in the vapors of hydrocarbons, and after having reached the desired product range with the lowering of the corresponding boiling points, the so-called used catalyst because of the deposit of coke which covers its surface, is separated from the hydrocarbon vapors, stripped, regenerated by combustion of the coke deposit, then again returned to the cracking zone.
  • the cracking reactor is generally in the form of an elongated substantially vertical tube.
  • the charges to be cracked are usually injected into the reaction zone after having been preheated to a temperature of between 80 and 400 ° C. This injection is carried out using one or more devices which spray and disperse the charge on the catalyst.
  • the pressure in the reaction zone is between 0.7 and 3.5 bar.
  • the regenerated catalyst is introduced into the zone of cracking at a temperature of the order of 600 to 950 ° C.
  • the quantity of catalyst injected is regulated by a valve located upstream of the reaction zone.
  • the grains of catalyst initially put into fluidization by appropriate injections of vapor, are then entrained by the hydrocarbon vapors towards the other end of the reactor where the charge opens into an enclosure where the separation of the cracked hydrocarbon vapors takes place.
  • the catalyst thus freed from most of the adsorbed hydrocarbons is then sent to one or more regenerators where its catalytic activity is restored by combustion of the coke which has deposited on the grains during the cracking step.
  • the thermal energy released by the combustion of coke is partly given up to the catalyst which heats up.
  • This amount of energy absorbed by the catalyst is then used in the reaction zone to vaporize and crack the charge: the catalyst acts as a coolant between the reactor where endothermic reactions take place and the regenerator or regenerators where reactions take place. exothermic.
  • the FCC process is implemented to ensure the thermal equilibrium of the unit.
  • the quantity of coke and of hydrocarbons present on the catalyst at the outlet of the stripping stage is therefore an essential variable of the process since it conditions all of the thermal levels of the unit.
  • such fillers which are difficult to vaporize are commonly encountered these days; however, poor spraying of the heaviest fractions generally leads to their deposition on the grains of catalyst despite steam stripping.
  • the resulting drawbacks are in particular a reduction in the yields of recoverable products, a release of energy during regeneration exceeding the needs of the unit and leading to final regeneration temperatures that are too high and therefore detrimental to the activity of the catalyst, increased production of fumes and greater air consumption resulting in oversizing of the regeneration unit, as well as high production of steam which is not always useful on site.
  • the stripping temperature is substantially the same as that of the reaction zone which itself depends on the conversion which it is desired to achieve for a given charge quality. Obtaining this conversion being the main element taken into consideration for the choice of the temperature of the cracking zone, stripping therefore appears to be an operation on which there are few means of action. At constant temperature, only an increase in the vapor flow rate or the residence time of the catalyst in the stripper currently makes it possible to improve the recovery yield of the absorbed hydrocarbons. In the current state of the art, and more particularly with heavy loads, the impact of a modification of these two operating parameters on the stripping efficiency therefore remains limited.
  • the temperature rise of the stripper by recycling partially or totally regenerated and hot catalyst can be much higher than in the case where the combustion gases are recycled as recommended in patent EP-A-184517 and WO 82/04061. Indeed, in the latter case, the ratio of mass flow rate of used catalyst to mass flow rate of smoke is such that one can hardly hope for temperature rises going beyond 15 to 20 ° C.
  • the hot catalyst reinjected near the diluted phase can come into contact with the light hydrocarbons present in the stripping enclosure and cause an overcracking detrimental to the overall performance of the unit.
  • the quantities of stripping vapor used are generally small so as to ensure a substantially piston flow of the catalyst, favorable to stripping and to the countercurrent training of light hydrocarbons. Under these conditions, the mixing of the hot catalyst from the regenerator with the used catalyst is not rapid and leads to hot spots which again favor the overcracking of the hydrocarbons desorbed in the dense phase.
  • This overcracking can also occur in the case of the process described in patent EP 137998, where a first stripping of the used catalyst is carried out in a separate stripping column in the presence of at least a portion of regenerated catalyst and of a gas. lift, which consists of cracking effluents.
  • Patent EP 187032 provides some remedies for the aforementioned drawbacks. It describes a cracking process in which the stripping operation is carried out in two stages. In the first stage, a conventional stripping is carried out with steam and at a temperature substantially equivalent to that prevailing in the reaction zone, and in the second stage, a more severe stripping is carried out at a higher temperature, after injecting hot catalyst from the regenerator.
  • the advantage of this process is that the second stripping is carried out so as to desorb the heavy hydrocarbons in a well individualized enclosure where it is easier to adjust the operating parameters (recycled flow rate, gas speed, etc.) without prejudice. for the rest of the vaporized hydrocarbon charge as could be the case with US patents 4,440,632 and 4,419,221.
  • a first object of the invention is therefore to propose a method and a device which make it possible to overcome the aforementioned drawbacks.
  • Another object of the invention is to facilitate the desorption of the hydrocarbons attached to the catalyst grains, in particular the heavy hydrocarbons with the aim of increasing the overall yield of the unit and limit the deposits of carbonaceous materials on the catalyst while strictly maintaining the thermal equilibrium of the installation.
  • the invention therefore relates to a catalytic cracking process in a fluid bed of a hydrocarbon charge boiling above 400 ° C.
  • This method comprises a step of bringing upward or downward flow into contact in an elongated tubular zone, under cracking conditions, of said charge and of the particles of a cracking catalyst, a step of separating the spent catalyst and the charge cracked in a first separation zone at the outlet of said tubular zone, a first stage of stripping of the used catalyst using a first stripping gas injected against the current of this catalyst, a first stage of separation of the catalyst mixture used and effluents resulting from the first stripping step, a second co-current stripping step delivering effluents from the second stripping, a step of regenerating said spent catalyst in at least one regeneration zone to form said hot regenerated catalyst, in conditions for combustion of the coke deposited thereon and a step of recycling at least part of the regenerated catalyst to the supply of said zone tubular.
  • the second stripping step is carried out in co-current and in a fluid bed, in a second stripping zone which is an elongated tubular zone, by introducing and mixing, upstream of the tubular zone and advantageously in the immediate vicinity of the end corresponding to the entry into said second tubular zone, at least part said catalyst regenerated and at a higher temperature with the spent catalyst resulting from the first stripping step and a stream of a second pressurized gas containing at least one stripping gas and a gas containing molecular oxygen, and separates effluents from said second stripping zone from the catalyst mixture thus stripped in a second separation zone downstream of this second stripping zone, said second stripping effluents are recovered and the catalyst mixture thus stripped is sent to said regeneration zone.
  • the regenerated catalyst is introduced in the immediate vicinity of the end, corresponding to the entry into the second tubular zone and preferably substantially above the arrival of the stripping gas, which has the advantage of promoting mixing. particles.
  • the method according to the invention has the advantage of facilitating better desorption of the hydrocarbons in the second stripping stage, in particular thanks to the introduction of a certain quantity of gas containing molecular oxygen. It follows that the residual deposits of carbonaceous materials before entering the regenerator are limited to strictly maintaining the thermal equilibrium of the unit without leading to unacceptable temperatures and water vapor pressures in the regenerator. for the activity and the service life of the catalyst. Even when the charge treated is heavy, it makes it possible to regenerate the catalyst in a single step, which translates into investment savings.
  • Another advantage of the invention is that the use of a gas containing molecular oxygen in the stripping gas causes in part the combustion of a fraction of the released hydrocarbons containing hydrogen and a release of heat allowing to maintain a given temperature, while limiting the flow of hot catalyst from the regenerator. This results in simplification and lower cost of installation.
  • Another advantage of the invention is that the stripping in the second stage is carried out in a fluidized bed, diluted, therefore without diffusion limitation linked to the hydrodynamics of the gas-particle flow. of catalyst.
  • the catalyst grains are well individualized within a large volume of gas, so that the partial pressure of hydrocarbons outside the grain is low or all at least much weaker than that prevailing in the dense phase of a fluidized bed (generally called emulsion phase by specialists).
  • the sliding speed of the grain relative to the surrounding gas is much greater than in the case of a dense fluidized bed. As a result, the resistance to transfer to the outer surface of the grain is low.
  • Another advantage of the invention is that the heating of the used catalyst with hot catalyst from the regenerator is carried out in an enclosure separate from the first stripping zone and makes it possible to avoid any contact of the hot catalyst with light hydrocarbons and eliminates therefore any risk of overcracking of these light hydrocarbons.
  • Another advantage of the invention relates to the mixing of the used catalyst from the first stripping stage with the hot catalyst of the regenerator.
  • This mixture is produced in a fluid bed, therefore in a much more turbulent medium than the dense fluidized bed, and therefore it is more intimate and faster.
  • This almost instantaneous mixture makes it possible to homogenize the temperatures of the two grain populations very quickly and contributes to significantly improving the efficiency of stripping.
  • Another advantage of the invention is that the reinjection of hot catalyst at the base of the second stripper makes it possible to rapidly initiate the oxidation of the hydrocarbons. This reinjection also makes it possible to stabilize the combustion in the elevator, even during the transient phases when fluctuations in the flow rate of used catalyst are observed.
  • Another advantage of the process is that the catalyst after this second stripping is freed from most of the hydrogen initially contained in the coke so that it is possible in most cases to regenerate the catalyst in a single step, even if the temperature is higher than 700 ° C., since the water vapor content of the regeneration effluents is low and therefore does not risk excessively accelerating the aging of the catalyst.
  • the invention allows a significant reduction in the sulfur contents in the regeneration effluents, since the heavy hydrocarbons rich in sulfur have been overwhelmingly desorbed from the catalyst grains in this second stripping zone.
  • the regeneration zone is withdrawn and a mass of regenerated catalyst, generally representing from 5 to 100% by mass, advantageously from 10 to 50%, is recycled into the second tubular stripping zone. mass and preferably between 20 and 40% of the mass of spent catalyst coming from the first stripping stage situated at the end of the cracking reaction zone.
  • the temperature of the regenerated catalyst may be approximately at least 80 ° C higher than the temperature of the spent catalyst at the outlet of the first stripping stage and at most approximately 400 ° C, without however exceeding 700 ° C, which would cause rapid catalyst deactivation.
  • the hot regenerated catalyst recycled in the second stripping stage can be cleaned beforehand of at least part of the combustion fumes in the connection line leading to the stripping column, preferably by stripping using a fluid (for example, inert gases or water vapor).
  • a fluid for example, inert gases or water vapor.
  • the so-called regenerated catalyst recycled in the second stripping stage can come from one or other of the compartments when the regenerator is multi-stage. It can be taken during regeneration in the last compartment, that is to say the one where the regeneration ends and which operates at the highest temperature when it is desired to minimize the recycling rate. But it can also be taken during regeneration in a lower regeneration stage operating at a lower temperature and where the catalyst is partially rid of the deposited coke, if it is feared a catalytic over-cracking or a significant thermal cracking of the hydrocarbons released during of this second stripping step.
  • the used catalyst from the first stripping stage and the regenerated catalyst from the regenerator are brought into contact with a gas generally containing approximately 0.1 to 30% by mass of oxygen, advantageously from 1 to 10%, and preferably from 2 to 5%, the balance to 100% can be water vapor, nitrogen, hydrogen, light hydrocarbons such as methane, ethane, propane or a mixture of these different gases.
  • a gas generally containing approximately 0.1 to 30% by mass of oxygen, advantageously from 1 to 10%, and preferably from 2 to 5%, the balance to 100% can be water vapor, nitrogen, hydrogen, light hydrocarbons such as methane, ethane, propane or a mixture of these different gases.
  • a gas generally containing approximately 0.1 to 30% by mass of oxygen, advantageously from 1 to 10%, and preferably from 2 to 5%, the balance to 100% can be water vapor, nitrogen, hydrogen, light hydrocarbons such as methane, ethane, propane or a mixture of these different gases.
  • water vapor and molecular oxygen are used.
  • the molecular oxygen content is determined in order to carry out the oxidation of the hydrogen released by the second stripping as well as of a minority part of the desorbed hydrocarbons.
  • the flow rate of gas injected at the base of the tubular stripping zone by means for example of a gas distributor is adjusted so that the surface speed of the gas in this zone is in generally between approximately 1 and 20 meters per second, and more advantageously between 2 and 10 meters per second, which makes it possible to obtain a entrained bed, to maximize the speed of sliding between the grains of catalyst and said gas of stripping and of ensuring contact times of the catalyst grains with the stripping gas of between 1 and 30 seconds.
  • the temperature rise of the catalyst in the second stripping zone relative to the first stripping zone due to the recycling of the hot regenerated catalyst on the one hand and to the partial oxidation of a fraction of the hydrocarbons desorbed from the catalyst, is generally between approximately 10 and 200 ° C. and is preferably between 50 and 100 ° C.
  • the stripping effluents are separated from the catalyst by means of devices which can, for example, be similar to those used at the outlet of the cracking reaction zone.
  • These effluents which contain inter alia the released hydrocarbons, the products of partial combustion and the stripping water vapor, can be directed like the cracking effluents towards a fractionation tower or any other point of use justified by the quality of said effluents.
  • the catalyst, freed from these effluents, is directed to the regenerator downstream.
  • the fillers which can be used boil above the range of gasolines and diesel oils, that is to say in general above about 400 ° C.
  • fillers those having initial boiling points of the order of 400 ° C., such as gas oils under vacuum, but also oils heavier hydrocarbons, such as crude and / or de-essential oils, and residues from atmospheric distillation or vacuum distillation.
  • These fillers may have received a preliminary treatment such as, for example, a hydrotreatment in the presence, for example, of cobalt-molybdenum type catalysts.
  • the preferred fillers of the invention will be those containing fractions normally boiling between 400 and 700 ° C and above, which may contain high percentages of asphaltenic products and have a Conradson carbon content of up to 10% and beyond.
  • the catalysts which can be used in the devices described above include cracking catalysts of the crystalline aluminosilicate type, certain types of silica-aluminas, of silica-magnesia, of silica-zirconium, all having relatively high cracking activities, such as example those described in US Patent 4,405,445.
  • the invention also relates to a catalytic cracking device in particular for implementing the process. It comprises an elongated tubular enclosure 1, means 4 for injecting pressure under pressure of said charge disposed at one end of said enclosure, means for supplying particles 2 of a cracking catalyst towards said end of said enclosure, first means 6 for separating the cracked charge from the spent catalyst particles at the other end of said enclosure 1 situated in a separation enclosure 5 disposed at the concentric end of the enclosure, a first means of stripping 8 of said spent catalyst by a first stripping gas in said separation enclosure 5, at least one regeneration unit 21 of said spent catalyst by combustion of the coke deposited on it, and means for recycling 27 of at least part of the regenerated catalyst towards said supply means 2.
  • this device comprises an elongated tubular stripping column 13 disposed between said first stripping means 8 and said regeneration unit 21, means for supplying pressure 15 with a second gas comprising at least one stripping gas and a gas containing molecular oxygen, preferably at the inlet of said stripping column 13, means 14 for supplying at least particles of catalyst and regenerated part connected on the one hand to the regeneration unit 21 and on the other hand, preferably, at the inlet of said stripping column 13, means 11 for supplying used catalyst connected to the first stripping means 8 and to the stripping column 13, preferably at its inlet, said supply means 14, 15 being adapted to inject the second gas and the particles of regenerated catalyst into said stripping column, under pressure, in a fluid bed and cocurrently with the flow of the particles of used catalyst coming from the first stripping means 8 and a second separation enclosure 16 for the mixture of stripped catalyst from the effluents of the second stripping connected to the outlet of said tubular column 13 and to said regenerator 21.
  • the tubular column generally has a length to diameter ratio L / D of between 10 and 300 and advantageously between 25 and 100.
  • the diameter of the tube is determined so that there is a gas velocity sufficient to entrain the grains of catalyst, this taking into account the total gas flow rate necessary for carrying out the second stripping.
  • FIG. 1 illustrates the device according to the invention with an ascending cracking enclosure (riser) and an ascending stripping column.
  • This equipment includes: a vertical tubular enclosure 1 supplied at its base with hot regenerated catalyst by means 2, themselves supplied by line 27 from the regenerator 21, with fluidization vapor and pre-training of the catalyst by line 3 and with hydrocarbon feedstock by line 4. a separation enclosure 5 situated at the upper end of the tubular enclosure 1 and concentric therewith and in which the separation of the cracking effluents and of a first stripping described below takes place , used catalyst thanks to an inertial separator 6 placed just above the riser outlet and to one or more levels of cyclones 7 located in the upper part of the enclosure 5, and on the other hand, a first stripping at the vapor of said used catalyst in the lower part 8 of the enclosure 5.
  • the stripping vapor is supplied by the line 8a and the lower part 8 of the enclosure 5 is internally provided with baffles 9 which favor the flow against stream of spent catalyst and said stripping vapor.
  • the hydrocarbon vapors leave the unit via line 10 and are directed to the fractionation tower.
  • This connection line is equipped with a valve 12 for controlling the flow rate of catalyst which is controlled by the level of catalyst in enclosure 5.
  • a vertical elongated tubular column 13 where the second stripping of the used catalyst takes place in a driven bed.
  • This column is supplied at its base, co-current with the flow, with catalyst used by the line 11, with regenerated catalyst hot by the supply means 14 and with gas containing at least steam and molecular oxygen via line 15.
  • Known type injectors are regularly placed around the column. an enclosure 16 for separation at the outlet of the column 13 and concentric therewith, where the effluents from the second stripping of the catalyst mixture are separated. The separation is carried out by means of an inertial separator 17 in the immediate vicinity of the column outlet 13 and of one or more levels of cyclones 18 separating the stripped particles from the effluents.
  • the stripped catalyst is sent to the regenerator 21 via line 20 which communicates with the base of the enclosure 16.
  • a regeneration unit 21 preferably located concentrically with the column 13 and supplied with used catalyst by the line 20 and with gas containing molecular oxygen by the distributor 22, located at the bottom of the unit, itself being supplied by line 23.
  • the regeneration effluents are dedusted by the cyclone level (s) 24 advantageously arranged outside the unit 21 and leave the installation by line 25.
  • the regenerated catalyst is extracted from the regenerator by line 26 which feeds thanks to supply means 14 for the second stripping column.
  • Line 26, of reduced diameter is equipped with a valve 28 for adjusting the catalyst flow rate controlled by the temperature prevailing in the second stripping column 13.
  • Means for recycling 27 of the regenerated catalyst connected to the regenerator 21 also supply the cracking enclosure 1 thanks to the supply means 2 and to a valve 29 for adjusting the catalyst flow rate controlled at the desired temperature at the upper end of the cracking enclosure 1.
  • Figure 2 illustrates the case where the tubular cracking enclosure operates in dropper. There are all the elements of Figure 1, excluding the riser 1 and the inertial separator 6 which have given way to the dropper 30.
  • connection line 20 ensures the transfer of the stripped catalytic particles from the second separation enclosure 16 to the first regenerator where s' performs the first regeneration.
  • the catalyst is then completely regenerated in a second regenerator.
  • the regenerated catalyst could come from one or other of the regenerators as it was said above, the transfer line 26 can be connected either to the first or to the second regenerator to supply the stripping column 13 while the line 27 leaves the second regenerator to supply the tubular cracking enclosure 1.

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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)
  • Catalysts (AREA)
EP88403159A 1987-12-22 1988-12-13 Verfahren und Einrichtung für das katalytische Kracken von schweren Einsätze, die eine zweite Wirbelschichtabstreifzone enthalten Withdrawn EP0322276A1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8717989 1987-12-22
FR8717989A FR2624877B1 (fr) 1987-12-22 1987-12-22 Procede et dispositif pour le craquage catalytique de charges lourdes comportant un second strippage en lit fluide

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EP0322276A1 true EP0322276A1 (de) 1989-06-28

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EP88403159A Withdrawn EP0322276A1 (de) 1987-12-22 1988-12-13 Verfahren und Einrichtung für das katalytische Kracken von schweren Einsätze, die eine zweite Wirbelschichtabstreifzone enthalten

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1998046700A1 (en) * 1997-04-11 1998-10-22 Shell Internationale Research Maatschappij B.V. Fluidized-bed catalytic cracking process
WO2003089546A1 (en) * 2002-04-18 2003-10-30 Uop Llc Process and apparatus for upgrading fcc product with additional reactor with catalyst recycle

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0023402A1 (de) * 1979-07-18 1981-02-04 Exxon Research And Engineering Company Katalytisches Wirbelschicht-Krackverfahren mit verminderter Temperatur und Zusammenstellungsgradiente in der verdünnten Phase im Regenerator
WO1982004061A1 (en) * 1981-05-13 1982-11-25 Mckay William E Jr Stripping hydrocarbons from catalyst with combustion gases
EP0137998A2 (de) * 1983-09-16 1985-04-24 Ashland Oil, Inc. Belüftetes Steigrohr für die Strippung von gebrauchten Katalysatoren
EP0184517A1 (de) * 1984-12-07 1986-06-11 Compagnie De Raffinage Et De Distribution Total France Verfahren und Anlagen für das katalytische Kracken von Kohlenwasserstoffeinsätzen

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0023402A1 (de) * 1979-07-18 1981-02-04 Exxon Research And Engineering Company Katalytisches Wirbelschicht-Krackverfahren mit verminderter Temperatur und Zusammenstellungsgradiente in der verdünnten Phase im Regenerator
WO1982004061A1 (en) * 1981-05-13 1982-11-25 Mckay William E Jr Stripping hydrocarbons from catalyst with combustion gases
EP0137998A2 (de) * 1983-09-16 1985-04-24 Ashland Oil, Inc. Belüftetes Steigrohr für die Strippung von gebrauchten Katalysatoren
EP0184517A1 (de) * 1984-12-07 1986-06-11 Compagnie De Raffinage Et De Distribution Total France Verfahren und Anlagen für das katalytische Kracken von Kohlenwasserstoffeinsätzen

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1998046700A1 (en) * 1997-04-11 1998-10-22 Shell Internationale Research Maatschappij B.V. Fluidized-bed catalytic cracking process
WO2003089546A1 (en) * 2002-04-18 2003-10-30 Uop Llc Process and apparatus for upgrading fcc product with additional reactor with catalyst recycle
US6866771B2 (en) 2002-04-18 2005-03-15 Uop Llc Process and apparatus for upgrading FCC product with additional reactor with catalyst recycle

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Publication number Publication date
FR2624877B1 (fr) 1992-01-10
FR2624877A1 (fr) 1989-06-23

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Effective date: 19910115