WO1990011337A1 - Process and device for the injection of a hydrocarbon charge in a fluid catalytic cracking process - Google Patents

Process and device for the injection of a hydrocarbon charge in a fluid catalytic cracking process Download PDF

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Publication number
WO1990011337A1
WO1990011337A1 PCT/FR1990/000154 FR9000154W WO9011337A1 WO 1990011337 A1 WO1990011337 A1 WO 1990011337A1 FR 9000154 W FR9000154 W FR 9000154W WO 9011337 A1 WO9011337 A1 WO 9011337A1
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WO
WIPO (PCT)
Prior art keywords
axis
charge
opening
reaction zone
reactor
Prior art date
Application number
PCT/FR1990/000154
Other languages
French (fr)
Inventor
Alfred Beretta
Bernard Boute
Renaud Pontier
Jean-Louis Mauleon
Original Assignee
Institut Francais Du Petrole
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Publication date
Application filed by Institut Francais Du Petrole filed Critical Institut Francais Du Petrole
Priority to JP2504945A priority Critical patent/JPH06508159A/en
Publication of WO1990011337A1 publication Critical patent/WO1990011337A1/en

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1818—Feeding of the fluidising gas
    • B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B05—SPRAYING OR ATOMISING IN GENERAL; APPLYING FLUENT MATERIALS TO SURFACES, IN GENERAL
    • B05B—SPRAYING APPARATUS; ATOMISING APPARATUS; NOZZLES
    • B05B1/00—Nozzles, spray heads or other outlets, with or without auxiliary devices such as valves, heating means
    • B05B1/02—Nozzles, spray heads or other outlets, with or without auxiliary devices such as valves, heating means designed to produce a jet, spray, or other discharge of particular shape or nature, e.g. in single drops, or having an outlet of particular shape
    • B05B1/04—Nozzles, spray heads or other outlets, with or without auxiliary devices such as valves, heating means designed to produce a jet, spray, or other discharge of particular shape or nature, e.g. in single drops, or having an outlet of particular shape in flat form, e.g. fan-like, sheet-like
    • B05B1/048—Nozzles, spray heads or other outlets, with or without auxiliary devices such as valves, heating means designed to produce a jet, spray, or other discharge of particular shape or nature, e.g. in single drops, or having an outlet of particular shape in flat form, e.g. fan-like, sheet-like having a flow conduit with, immediately behind the outlet orifice, an elongated cross section, e.g. of oval or elliptic form, of which the major axis is perpendicular to the plane of the jet
    • 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 for catalytic cracking, in a fluidized bed, of a charge of hydrocarbons. It relates, more particularly, to a device for injecting or introducing the hydrocarbon charge into the reaction zone of an elevating reactor or "riser" in English.
  • It relates in particular to a catalytic cracking process in a fluidized bed (in English, Fluid Catalytic Cracking or FCC process) of hydrocarbon feed and / or petroleum residues having a Conradson carbon content and a relatively high metal content (for example fillers with a metal content of up to 100 ppm by weight or more and a Conradson carbon content of up to 10% by weight).
  • US-A-4097243 describes for example a charge injection system comprising a series of tubes arranged at the end of a cone allowing the distribution of the charge over all the grains of catalyst in motion.
  • a charge injection system comprising a series of tubes arranged at the end of a cone allowing the distribution of the charge over all the grains of catalyst in motion.
  • US-A-3812029 describes a particular injector for obtaining fine charge droplets; however, this injector does not allow a good distribution of the droplets, resulting in poor vaporization of the hydrocarbons and a excessive coking. In addition, when using heavy loads, this injector is often quickly clogged.
  • Patent application EP-A-220349 describes a particular injector, comprising a spiral, making it possible to obtain droplets with an average diameter of less than approximately (35x10 " 5 meter) 350 microns while at least partially avoiding contact of the charge with the walls of the reaction zone.
  • the formation of swirls of charge droplets near these injectors disturbs the flow of the catalyst grains and causes an increase in the phenomenon of back mixing (which is detrimental in English). the proper functioning of the process.
  • the object of the present invention is to overcome the drawbacks of the methods of injecting the hydrocarbon charge of the prior art, and to make it possible to obtain, in particular in the case of cracking of heavy charges, optimal contact, hydrocarbons with the catalyst grains due to atomization, homogeneous and instantaneous, in the form of fine droplets in the injection zone. Furthermore, the present invention makes it possible to obtain an excellent uniformity of the "C / O" ratio between the quantity, "C", of catalyst injected into the reaction zone and that, "0", of the feedstock to be treated introduced into said zone (that is to say to maintain the value of this ratio at any point of said zone).
  • the present invention relates to a process for catalytic cracking of a hydrocarbon feedstock in which the catalyst grains, in a fluidized bed, are brought into contact with said feedstock, in a reaction zone of elongated shape having an axis of symmetry, in the form of fine droplets with an average diameter of less than 3x10 ⁇ 4 m (meter), preferably less than 2x10 " 4 m and most often less than 10" 4 m, said charge being introduced in mixture with a fluid gaseous auxiliary in said reaction zone by means of at least one enclosure (or device) of venturi type, of axis substantially parallel to the axis of said reaction zone, comprising from upstream to downstream in the direction of displacement of the hydrocarbon charge, a first end comprising at least one means for introducing said auxiliary fluid and said hydrocarbon charge, said enclosure also comprising downstream of said first end (for example in the middle) a narrowing zone then a widening zone (convergent and divergent of the venturi type) and comprising at its other end
  • Figure 1 shows in section a schematic view of the lower part of a catalytic cracking reactor in a fluidized bed.
  • the fresh and / or regenerated catalyst arrives via the conduit (2) at the base of the reactor (1) and is placed in a fluidized bed by injection into the diffusers (3) of a gaseous fluid known as a fluidization fluid.
  • the charge to be cracked is introduced into the reaction zone by at least one device (5) of venturi type, with an axis substantially parallel to the axis of the reaction zone (4), into which it enters through one of the conduits ( 6) or (7) while the gaseous auxiliary fluid * used, to promote injection and spraying, enters through one of the conduits (7) or (6) different from that through which the charge penetrates.
  • enclosures or devices (5) at least two and more often at least three spaced, for example according to the schematic embodiment by FIG. 2, and the end of which, by which the charge enters the reaction zone, is usually located near the zone for introducing the catalyst and preferably substantially above.
  • FIG. 2 represents an arrangement corresponding to a preferred embodiment according to the present invention in which the devices or enclosures (5), of venturi type, are arranged on a support plate, preferably symmetrically, at one end of the zone reaction (4), for example at the bottom of said reaction zone (case of the elevating reactor), said support plate comprising then also at least two organs (3) for injecting a gas for fluidizing the grains of catalyst arriving via the conduit (2); or at the top of said reaction zone (case of the descending reactor, in English "dropper").
  • the top of the devices (5), venturi type is located near and substantially above the zone for introducing the catalyst grains. All the vertices of the devices (5) can be at the same level (case shown in FIG. 2) or at different levels.
  • FIG. 3 shows a schematic top view, according to the principle of embodiment of Figure 2, in which there are shown seven devices (5), which are distributed on a support plate so that the ends of these devices (5 ) opening into the reaction zone (4) are distributed symmetrically inside said reaction zone (4).
  • the openings (9) through which the charge enters the reaction zone (4) usually have a substantially rectangular, circular, elliptical or in the shape of a crown or of a crown sector.
  • the shape of the section of each opening (9) will preferably be chosen according to the position of the device (5) within the reaction zone.
  • each opening will preferably choose the shape of each opening according to the position of the device (5) in the reaction zone so that the jet of fine droplets obtained does not come into contact with the walls of the zone reaction and that this jet is well distributed over the greatest possible quantity of the moving solid.
  • the opening (9) of each of the devices (5) (6 in the case shown schematically in Figure 3) located near the wall of the reaction zone has a section substantially rectangular whose sides of the larger rectangle are preferably substantially perpendicular to one of the radii of the circular section of the reaction zone (these openings could also have a section in the form of a crown sector) and the opening (9) of the device (s) (5) located near the center of the reaction zone has an opening of substantially circular section (this or these openings could also have an elliptical or crown-shaped section).
  • the position of the devices (5) on the support plate is generally chosen as a function of the distribution of the grains of solid in motion, by example as in Figure 3 at the periphery where the grain density is maximum.
  • the six organs (3) for injecting a fluidizing gas are distributed on the support plate symmetrically. Also shown in Figure 3 reinforcing elements (8) connecting the devices (5) together.
  • the number of devices (5) is usually a function of the amount of charge to be introduced per unit of time and of the dimensions of the reaction zone; it is chosen so as to ensure the best uniformity of the "C / O" ratio as well as obtaining a distribution of the charge in the form of fine droplets over the entire solid in motion while avoiding contact of the charge with the walls.
  • the number of devices (5) is usually from 1 to 19, preferably at least 2 and for example from 3 to 13.
  • the number of devices for introducing the catalyst grain fluidization fluid is any, but must be chosen so as to ensure as perfect fluidization as possible of the catalyst grains; it is usually from 2 to 50, preferably from 2 to 26.
  • FIGS. 1 to 3 of these devices for introducing the fluidization fluid in the form of a tube should not be interpreted in a limiting manner; the skilled person is able to design other devices performing the same function, for example an annular device, without departing from the scope of the present invention. It is also possible to provide for an additional introduction of a lifting gas (in English "lift gas") for example at a level substantially above that of the introduction of the catalyst.
  • a lifting gas in English "lift gas”
  • FIGS. 4A and 4B show schematically a device (5), according to a preferred embodiment of the invention.
  • FIGS. 4A and 4B are a schematic view, in section, of the front and of the profile of a device (5) at 90 degrees from each other.
  • the load enters the device (5) through the pipe (6) whose axis is substantially parallel to the axis AA 'of said device (5) while the gaseous auxiliary fluid enters through the pipe (7) whose axis is substantially perpendicular to the axis of said device (5).
  • This mode of introduction of the charge and of the auxiliary fluid corresponds to the preferred mode of introduction according to the invention, however, it is possible to introduce the charge through the conduit (7) and the gaseous auxiliary fluid through the conduit (6).
  • the charge-auxiliary gas mixture which forms, preferably in the convergent of the venturi, acquires a very high speed at the level of the venturi neck, then is vaporized in the form of very fine charge droplets in the auxiliary gas at the opening (9) made in the end of said device (5).
  • the opening (9), formed in the thickness of the material forming the end of the device (5) usually has a shape such that the walls of this opening define, in at least one direction, a alpha angle of about 20 to 100 degrees, preferably about 40 to 90 degrees, the apex of which is directed upstream of the device (5).
  • this opening (9) will, for example, in the case of an opening of substantially circular section, have the shape of a truncated cone with an angle at the apex alpha.
  • the end of the device (5) has the shape of a spherical cap and the opening has a substantially rectangular section; the planes of the opening passing through the sides of the rectangle having the smallest dimension intersect at an alpha angle of 20 to 100 degrees and preferably 40 to 90 degrees and the planes passing through the sides of the rectangle having the largest dimension are substantially parallel.
  • FIG. 4B also schematically represents a view of the spherical cap and of the opening or slot (9) of rectangular section whose side of smaller dimension has a value T not shown in FIG. 4B, but visible in section in the figure 4A, and the side of larger dimension a value "Le” measured on the external part and a value "Li” measured on the internal part; the value "Li” usually being less than the value "Le”.
  • the conduit (6) for introducing the charge opens above the upper level of the conduit (7) for introducing the gaseous auxiliary fluid.
  • the conduit (6) opens near the beginning of the converging zone of the venturi and substantially below the latter.
  • the beta angle (FIG. 4A) of the convergent zone, or convergent, the venturi is usually 15 to 45 degrees, preferably 20 to 40 degrees
  • the delta angle ( Figure 4A) of the divergent, or divergent, area of the venturi is usually 2 to 20 degrees, preferably 3 to 12 degrees, the angle of the diverging point being always smaller than the angle of the converging point and preferably less than twice the angle of the converging point.
  • a member having an opening (9), defining a restriction of the section of said end, it means that said opening has usually one surface section (e.g. IxLe in the case of an opening (9) of rectangular section, as shown in figures 4A and 4B) less than ⁇ d 2/4, e.g. ⁇ d of 2/20 to ⁇ d 2/6 and preferably ⁇ d 2/12 to ⁇ d 2/8.
  • This member is represented in FIG.
  • the internal geometry of the injector is such that there is no offset between the wall of the venturi and that of the nozzle or of the member defining the section restriction; the external geometry can be of substantially identical shape (FIG. 4A) or substantially different (FIG. 5) from that of the internal geometry.
  • the opening (9) in Figures 3, 4A and 5 has been shown in a symmetrical position relative to the axis of the device (5).
  • This diagram is a representation of the preferred embodiment of the device (5). It is however possible, without departing from the scope of the present invention, to design an asymmetrical positioning of the opening (9) relative to the axis of the device (5).
  • each of them may have a different geometry from the others or a certain number will have a determined geometry and the other (s) another geometry or they can all be identical.
  • FIGS. 4A, 4B and 5 are only schematic representations of the device (5) according to the invention and should not be considered as limiting the invention to the mode of representation illustrated by these figures.
  • a person skilled in the art is able to design various forms for this device, for example a rectilinear zone at the neck may be present between the converging zone and the diverging zone of said device.
  • the use of the devices (5) according to the invention makes it possible to obtain very high load speeds. At the level of the venturi neck these speeds can even exceed the speed of sound. An excellent dispersion of the liquid charge in the gaseous auxiliary fluid is thus obtained.
  • the conditions are usually chosen so that the speed at the outlet of the devices (5) is from 10 to 600 m / s, preferably from 50 to 340 m / s. Since it is desirable to have rapid contact between the catalyst and the charge as soon as it leaves the devices (5), it is usually preferred to have high or even very high speeds of the charge, for example at least 100 m / s .
  • Another advantage of the use of the devices (5) is the possibility of obtaining a mist of very fine droplets whose average diameter is of the order of magnitude of the size of the catalyst grains, for example order of 65 microns (65x10 " ⁇ m) with a small dispersion around this value.
  • the size of the catalyst grains is usually from 10 to 120 microns (1 micron: 10" 6 m) with a high proportion of grains having a size about 65 microns.
  • the process of the present invention comprising the introduction of the hydrocarbon charge substantially in the direction of the catalyst grains makes it possible to limit, in particular with respect to the case of lateral injection, the collisions between the charge droplets and the grains catalyst resulting in better progressive vaporization and less coking.
  • the invention also relates to an apparatus or reactor (1), of elongated shape, substantially vertical comprising (see FIG. 2) an intake pipe (2) of solid particles and comprising at one of its ends and for example in its lower end a support plate (substantially perpendicular to the axis longitudinal of the reactor) through which are arranged means for introducing a fluidizing gas, for example pipes (3) substantially parallel to the axis of the elongated reactor, pipes through which said gas intended for introduction ensuring the fluidization of solid particles, said reactor further comprising means for introducing a hydrocarbon charge therein, characterized in that it comprises at least 1 device, and preferably at least 2 devices, venturi type, each device having the shape of a tube, each tube being arranged in the support plate, the axis of each tube being substantially parallel to the longitudinal axis of the reactor, each device comprising, from upstream to downstream in the direction of movement of the load, a) at one end a load inlet pipe whose axis is substantially perpendicular to the axis of the tube or
  • the reactor comprises a plurality of venturi-type devices distributed symmetrically on the plate support; the devices located at the periphery of said support plate comprise at one end an orifice for injecting the hydrocarbon charge, this orifice formed in a substantially spherical cap has an opening or slot of substantially rectangular section, the planes of the opening passing through the sides of the rectangle having the smallest dimension intersecting at an alpha angle (see FIG.
  • the industrial, dimensional and operational characteristics can usually be as follows: - height of the reaction zone: 5 to 40 meters
  • reaction zone 0.05 to 10 seconds, preferably less than 6 seconds and for example from 0.8 to 5 seconds.
  • auxiliary fluid used for spraying or atomizing the charge from 0.5 to 30% by weight relative to the weight of the charge to be cracked, preferably from 2 to 20% by weight.
  • the flow of catalyst grains into which the charge is introduced is usually a homogeneous flow of catalyst in the fluidized phase usually having a density of 15 to 800 kg / m 3 and preferably from 20 to 600 kg / m 3 -
  • the linear speed of this flow is advantageously from 0.01 to 30 m / s and preferably from 10 to 20 m / s.
  • the fluidization and the flow of catalyst grains are obtained by the introduction of a gaseous fluidization fluid which may be a hydrocarbon having for example from 1 to 5 carbon atoms in its molecule or a mixture of hydrocarbons.
  • This gaseous fluidization fluid can comprise up to 35% by volume of hydrogen and up to 10% by volume of water vapor.
  • This fluid can also be composed of 100% by volume of water vapor.
  • the conditions for injecting this gaseous fluid naturally vary depending on the size and weight of the catalyst grains.
  • the flow of catalyst grains is usually introduced at a temperature of 500 to 750 ° C. when the charge to be cracked is of the conventional type such as a diesel charge.
  • the temperature may advantageously be from 650 to 950 ° C. so as to ensure complete vaporization of the heaviest molecules, as well as their selective thermal cracking in the injection zone of the reactor.
  • each of the devices (5) is supplied separately by a determined amount of charge depending on its position.
  • This method makes it possible to take better account of the fact that the density of catalyst in a section of the reactor at a given level is not homogeneous and thus to introduce only the quantity of charge desired as a function of the quantity of catalyst present on the surface watered by the charge jet leaving a given device (5).
  • the quantity of catalyst in a given volume can vary over time, it is possible to provide a system for regulating the quantity of charge which is injected into each. devices (5) so as to adapt it to the quantity of catalyst reached by the jet of said device.
  • the gaseous auxiliary fluid used to promote atomization of the charge and introduced into the device (s) (5), is usually water vapor or a gaseous fluid relatively rich in hydrogen or hydrogenated compounds coming from the FCC unit (recycling) or other refinery units.
  • the catalysts which can be used in the process which is the subject of the present invention include cracking catalysts of the crystalline aluminosilicate type and certain types of silica-alumina, of silica-magnesia or of silica-zirconium, all having activities of relatively high cracking.
  • the crystalline aluminosilicates can be found in the natural state or be prepared by synthesis, according to techniques well known to those skilled in the art, They can be chosen from synthetic zeolites or clays, such as faujasite, some mordenites, montmonllonite, bridged clays, alumino-phosphates, or the like.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Combustion & Propulsion (AREA)
  • General Chemical & Material Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

Process and apparatus for catalytic cracking of a hydrocarbon charge in a fluid bed comprising the introduction of the charge mixed with a gaseous auxiliary fluid by means of at least one venturi-type device (5), whose axis is essentially parallel to the axis of the reaction region, said device (5) comprising at its first end means for introducing the filler and the auxiliary fluid and its other end an element comprising an opening, and defining a restriction in the section of said end, through which said mixture is fed into said reaction zone (4). The reactor (1) comprises means for introducing the catalyst and means (3) for introducing the fluid gas. The reactor preferably comprises a plurality of devices (5).

Description

PROCEDE ET DISPOSITIF D'INJECTION DE LA CHARGE LOAD INJECTION METHOD AND DEVICE
^HYDROCARBURES DANS UN PROCEDE DE CRAQUAGE^ HYDROCARBONS IN A CRACKING PROCESS
CATALYTIQUE A L'ETAT FLUIDE La présente invention concerne un procédé de craquage catalytique, en lit fiuidisé, d'une charge d'hydrocarbures. Elle concerne, plus particulièrement, un dispositif d'injection ou d'introduction de la charge d'hydrocarbures dans la zone réactionnelle d'un réacteur élévateur ou "riser" en anglais.The present invention relates to a process for catalytic cracking, in a fluidized bed, of a charge of hydrocarbons. It relates, more particularly, to a device for injecting or introducing the hydrocarbon charge into the reaction zone of an elevating reactor or "riser" in English.
Elle concerne en particulier un procédé de craquage catalytique en lit fiuidisé (en anglais, Fluid Catalytic Cracking ou procédé FCC) de charge d'hydrocarbures et/ou de résidus pétroliers ayant une teneur en carbone Conradson et une teneur en métaux relativement importante (par exemple des charges ayant une teneur en métaux pouvant atteindre 100 ppm en poids ou plus et une teneur en carbone Conradson pouvant aller jusqu'à 10 % en poids).It relates in particular to a catalytic cracking process in a fluidized bed (in English, Fluid Catalytic Cracking or FCC process) of hydrocarbon feed and / or petroleum residues having a Conradson carbon content and a relatively high metal content (for example fillers with a metal content of up to 100 ppm by weight or more and a Conradson carbon content of up to 10% by weight).
Le craquage catalytique de charges d'hydrocarbures a connu et connaît encore un développement important dû au progrès de la technique et à celui des catalyseurs. Ce développement est lié en particulier à la demande de plus en plus importante en fractions légères en dépit de l'utilisation de plus en plus fréquente de charges lourdes d'hydrocarbures.The catalytic cracking of hydrocarbon feeds has known and still knows a significant development due to the progress of the technique and that of the catalysts. This development is linked in particular to the growing demand for light fractions despite the increasingly frequent use of heavy hydrocarbon charges.
Les développements récents en matière de craquage catalytique ont ainsi montré que des facteurs importants de la réaction de craquage sont la rapidité et l'uniformité de la mise efl contact de la charge avec les grains de catalyseur, et donc la qualité de l'atomisation et de la vaporisation de cette charge lors de son injection dans la zone réactionnelle.Recent developments in catalytic cracking have thus shown that important factors in the cracking reaction are the speed and uniformity of the contacting of the charge with the catalyst grains, and therefore the quality of the atomization and vaporization of this charge during its injection into the reaction zone.
Divers systèmes d'injection de la charge d'hydrocarbures dans la zone réactionnellle du réacteur de craquage catalytique ont été décrits dans l'art antérieur. Le brevet US-A-4097243 décrit par exemple un système d'injection de la charge comprenant une série de tubes disposés à l'extrémité d'un cône permettant la répartition de la charge sur la totalité des grains de catalyseur en mouvement. Un tel système présente cependant l'inconvénient de provoquer le contact d'une partie de la charge liquide avec les parois du réacteur ou avec les grains de catalyseur d'où une formation excessive et néfaste de coke. Le brevet US-A-3812029 décrit un iπjecteur particulier permettant d'obtenir de fines gouttelettes de charge ; cependant cet injecteur ne permet pas une bonne répartition des gouttelettes d'où une mauvaise vaporisation des hydrocarbures et un cokage excessif. De plus, lors de l'utilisation de charges lourdes, cet injecteur est souvent assez rapidement obstrué.Various systems for injecting the hydrocarbon feedstock into the reaction zone of the catalytic cracking reactor have been described in the prior art. US-A-4097243 describes for example a charge injection system comprising a series of tubes arranged at the end of a cone allowing the distribution of the charge over all the grains of catalyst in motion. However, such a system has the drawback of causing part of the liquid charge to come into contact with the walls of the reactor or with the catalyst grains, resulting in excessive and harmful formation of coke. US-A-3812029 describes a particular injector for obtaining fine charge droplets; however, this injector does not allow a good distribution of the droplets, resulting in poor vaporization of the hydrocarbons and a excessive coking. In addition, when using heavy loads, this injector is often quickly clogged.
La demande de brevet EP-A-220349 décrit un injecteur particulier, comprenant une spirale, permettant l'obtention de gouttelettes de diamètre moyen inférieur à environ (35x10"5 mètre) 350 microns tout en évitant au moins partiellement le contact de la charge avec les parois de la zone réactionnelle. Toutefois, la formation de tourbillons de gouttelettes de charge à proximité de ces injecteurs pertube l'écoulement des grains de catalyseur et entraîne une augmentation du phénomène de rétromélange (en anglais "back mixing") ce qui est préjudiciable au bon fonctionnement du procédé.Patent application EP-A-220349 describes a particular injector, comprising a spiral, making it possible to obtain droplets with an average diameter of less than approximately (35x10 " 5 meter) 350 microns while at least partially avoiding contact of the charge with the walls of the reaction zone. However, the formation of swirls of charge droplets near these injectors disturbs the flow of the catalyst grains and causes an increase in the phenomenon of back mixing (which is detrimental in English). the proper functioning of the process.
La présente invention a pour but de pallier les inconvénients des procédés d'injection de la charge d'hydrocarbures de l'art antérieur, et de permettre d'obtenir, en particulier dans le cas du craquage des charges lourdes, un contact optimal, des hydrocarbures avec les grains de catalyseur du fait d'une atomisation, homogène et instantanée, sous forme de fines gouttelettes dans la zone d'injection. Par ailleurs, la présente invention permet d'obtenir une excellente uniformité du rapport "C/O" entre la quantité, "C", de catalyseur injectée dans la zone réactionnelle et celle, "0", de la charge 'à traiter introduite dans ladite zone (c'est à dire de maintenir la valeur de ce rapport en tout point de ladite zone).The object of the present invention is to overcome the drawbacks of the methods of injecting the hydrocarbon charge of the prior art, and to make it possible to obtain, in particular in the case of cracking of heavy charges, optimal contact, hydrocarbons with the catalyst grains due to atomization, homogeneous and instantaneous, in the form of fine droplets in the injection zone. Furthermore, the present invention makes it possible to obtain an excellent uniformity of the "C / O" ratio between the quantity, "C", of catalyst injected into the reaction zone and that, "0", of the feedstock to be treated introduced into said zone (that is to say to maintain the value of this ratio at any point of said zone).
Elle permet également d'obtenir une répartition de la charge sous forme de fines gouttelettes de très faibles dimensions sur la totalité du solide en mouvement tout en évitant le contact de la charge avec les parois de la zone réactionnelle.It also makes it possible to obtain a distribution of the charge in the form of fine droplets of very small dimensions over the entire solid in motion while avoiding contact of the charge with the walls of the reaction zone.
De façon plus précise la présente invention concerne un procédé de craquage catalytique d'une charge d'hydrocarbures dans lequel les grains de catalyseur, en lit fiuidisé, sont mis en contact avec ladite charge, dans une zone réactionnelle de forme allongée ayant un axe de symétrie, à l'état de fines gouttelettes de diamètre moyen inférieur à 3x10~4 m (mètre), de préférence inférieur à 2x10"4 m et le plus souvent inférieur à 10"4 m, ladite charge étant introduite en mélange avec un fluide auxiliaire gazeux dans ladite zone réactionnelle par l'intermédiaire d'au moins une enceinte (ou dispositif) de type venturi, d'axe sensiblement parallèle à l'axe de ladite zone réactionnelle, comprenant d'amont en aval dans le sens du déplacement de la charge d'hydrocarbures, une première extrémité comprenant au moins un moyen d'introduction dudit fluide auxiliaire et de ladite charge d'hydrocarbures, ladite enceinte comprenant également en aval de ladite première extrémité (par exemple en son milieu) une zone de rétrécissement puis une zone d'élargissement (convergent et divergent du type venturi) et comprenant à son autre extrémité, c'est à dire à l'extrémité opposée, un orifice d'injection de la charge d'hydrocarbures dans la zone réactionnelle c'est à dire un organe comportant au moins une ouverture et définissant une restriction de la section de ladite extrémité, à travers laquelle ledit mélange est introduit dans ladite zone réactionnelle.More precisely, the present invention relates to a process for catalytic cracking of a hydrocarbon feedstock in which the catalyst grains, in a fluidized bed, are brought into contact with said feedstock, in a reaction zone of elongated shape having an axis of symmetry, in the form of fine droplets with an average diameter of less than 3x10 ~ 4 m (meter), preferably less than 2x10 " 4 m and most often less than 10" 4 m, said charge being introduced in mixture with a fluid gaseous auxiliary in said reaction zone by means of at least one enclosure (or device) of venturi type, of axis substantially parallel to the axis of said reaction zone, comprising from upstream to downstream in the direction of displacement of the hydrocarbon charge, a first end comprising at least one means for introducing said auxiliary fluid and said hydrocarbon charge, said enclosure also comprising downstream of said first end (for example in the middle) a narrowing zone then a widening zone (convergent and divergent of the venturi type) and comprising at its other end, that is to say at the opposite end, a orifice injection of the hydrocarbon feedstock into the reaction zone, that is to say a member comprising at least one opening and defining a restriction on the section of said end, through which said mixture is introduced into said reaction zone.
La figure 1 représente en coupe une vue schématique de la partie inférieure d'un réacteur de craquage catalytique en lit fiuidisé. Le catalyseur frais et/ou régénéré arrive par le conduit (2) à la base du réacteur (1) et est mis en lit fiuidisé par injection dans les diffuseurs (3) d'un fluide gazeux dit fluide de fluidisation. La charge à craquer est introduite dans la zone réactionnelle par au moins un dispositif (5) de type venturi, d'axe sensiblement parallèle à l'axe de la zone réactionnelle (4), dans lequel elle pénètre par l'un des conduits (6) ou (7) tandis que le fluide auxiliaire gazeux* utilisé, pour favoriser l'injection et la pulvérisation, pénètre par l'un des conduits (7) ou (6) différent de celui par lequel pénètre la charge.Figure 1 shows in section a schematic view of the lower part of a catalytic cracking reactor in a fluidized bed. The fresh and / or regenerated catalyst arrives via the conduit (2) at the base of the reactor (1) and is placed in a fluidized bed by injection into the diffusers (3) of a gaseous fluid known as a fluidization fluid. The charge to be cracked is introduced into the reaction zone by at least one device (5) of venturi type, with an axis substantially parallel to the axis of the reaction zone (4), into which it enters through one of the conduits ( 6) or (7) while the gaseous auxiliary fluid * used, to promote injection and spraying, enters through one of the conduits (7) or (6) different from that through which the charge penetrates.
Pour assurer une répartition très uniforme de la charge atomisée dans la zone réactionnelle, il est préférable d'utiliser plusieurs enceintes ou dispositifs (5) (au moins deux et le plus souvent au moins trois) espacés, par exemple selon le mode de réalisation schématisé par la figure 2, et dont l'extrémité, par laquelle la charge entre dans la zone réactionnelle est habituellement située à proximité de la zone d'introduction du catalyseur et de préférence sensiblement au dessus.To ensure a very uniform distribution of the atomized charge in the reaction zone, it is preferable to use several enclosures or devices (5) (at least two and more often at least three) spaced, for example according to the schematic embodiment by FIG. 2, and the end of which, by which the charge enters the reaction zone, is usually located near the zone for introducing the catalyst and preferably substantially above.
La figure 2 représente un agencement correspondant à une forme préférée de réalisation selon la présente invention dans lequel les dispositifs ou enceintes (5), de type venturi, sont disposés sur une plaque support, de préférence de manière symétrique, à une extrémité de la zone réactionnelle (4), par exemple au bas de ladite zone réactionnelle (cas du réacteur élévateur), ladite plaque support comprenant alors également au moins deux organes (3) d'injection d'un gaz de fluidisation des grains de catalyseur arrivant par le conduit (2) ; ou en haut de ladite zone réactionnelle (cas du réacteur descendant, en anglais "dropper"). Selon l'agencement représenté sur la figure 2 le sommet des dispositifs (5), de type venturi, est situé à proximité et sensiblement au dessus de la zone d'introduction des grains de catalyseur. Tous les sommets des dispositifs (5) peuvent être au même niveau (cas représenté sur la figure 2) ou à des niveaux différents.FIG. 2 represents an arrangement corresponding to a preferred embodiment according to the present invention in which the devices or enclosures (5), of venturi type, are arranged on a support plate, preferably symmetrically, at one end of the zone reaction (4), for example at the bottom of said reaction zone (case of the elevating reactor), said support plate comprising then also at least two organs (3) for injecting a gas for fluidizing the grains of catalyst arriving via the conduit (2); or at the top of said reaction zone (case of the descending reactor, in English "dropper"). According to the arrangement shown in Figure 2 the top of the devices (5), venturi type, is located near and substantially above the zone for introducing the catalyst grains. All the vertices of the devices (5) can be at the same level (case shown in FIG. 2) or at different levels.
La figure 3 représente une vue schématique de dessus, selon le principe de réalisation de la figure 2, dans laquelle on a représenté sept dispositifs (5), qui sont répartis sur une plaque support de manière à ce que les extrémités de ces dispositifs (5) débouchant dans la zone réactionnelle (4) soient réparties symétriquement à l'intérieur de ladite zone réactionnelle (4). Les ouvertures (9) par lesquelles la charge pénètre dans la zone réactionnelle (4) ont habituellement une section sensiblement rectangulaire, circulaire, elliptique ou ayant la forme d'une couronne ou d'un secteur de couronne. La forme de la section de chaque ouverture (9) sera de préférence choisie en fonction de la position du dispositif (5) au sein de la zone réactionnelle. L'homme du métier choisira de préférence la forme de chaque ouverture en fonction de la position du dispositif (5) dans la zone réactionnelle de manière à ce que le jet de fines gouttelettes obtenu n'entre pas en contact avec les parois de la zone réactionnelle et à ce que ce jet soit bien réparti sur la plus grande quantité possible du solide en mouvement. Ainsi selon un mode préféré de réalisation représenté sur la figure 3 l'ouverture (9) de chacun des dispositifs (5) (6 dans le cas schématisé sur la figure 3) situés à proximité de la paroi de la zone réactionnelle a une section sensiblement rectangulaire dont les côtés du rectangle de plus grande dimension sont de préférence sensiblement perpendiculaires à l'un des rayons de la section circulaire de la zone réactionnelle (ces ouvertures pourraient également avoir une section en forme d'un secteur de couronne) et l'ouverture (9) du ou des dispositifs (5) situés à proximité du centre de la zone réactionnelle a une ouverture de section sensiblement circulaire (cette ou ces ouvertures pourraient également avoir une section elliptique ou en forme de couronne). La position des dispositifs (5) sur la plaque support est en général choisie en fonction de la répartition des grains de solide en mouvement, par exemple comme sur la figure 3 à la périphérie là où la densité de grains est maximum.3 shows a schematic top view, according to the principle of embodiment of Figure 2, in which there are shown seven devices (5), which are distributed on a support plate so that the ends of these devices (5 ) opening into the reaction zone (4) are distributed symmetrically inside said reaction zone (4). The openings (9) through which the charge enters the reaction zone (4) usually have a substantially rectangular, circular, elliptical or in the shape of a crown or of a crown sector. The shape of the section of each opening (9) will preferably be chosen according to the position of the device (5) within the reaction zone. Those skilled in the art will preferably choose the shape of each opening according to the position of the device (5) in the reaction zone so that the jet of fine droplets obtained does not come into contact with the walls of the zone reaction and that this jet is well distributed over the greatest possible quantity of the moving solid. Thus according to a preferred embodiment shown in Figure 3 the opening (9) of each of the devices (5) (6 in the case shown schematically in Figure 3) located near the wall of the reaction zone has a section substantially rectangular whose sides of the larger rectangle are preferably substantially perpendicular to one of the radii of the circular section of the reaction zone (these openings could also have a section in the form of a crown sector) and the opening (9) of the device (s) (5) located near the center of the reaction zone has an opening of substantially circular section (this or these openings could also have an elliptical or crown-shaped section). The position of the devices (5) on the support plate is generally chosen as a function of the distribution of the grains of solid in motion, by example as in Figure 3 at the periphery where the grain density is maximum.
Les six organes (3) d'injection d'un gaz de fluidisation sont répartis sur la plaque support de manière symétrique. On a représenté également sur la figure 3 des éléments de renfort (8) reliant les dispositifs (5) entre eux.The six organs (3) for injecting a fluidizing gas are distributed on the support plate symmetrically. Also shown in Figure 3 reinforcing elements (8) connecting the devices (5) together.
Dans le procédé de la présente invention le nombre de dispositifs (5) est habituellement fonction de la quantité de charge à introduire par unité de temps et des dimensions de la zone réactionnelle ; il est choisi de manière à assurer la meilleure uniformité du rapport "C/O" ainsi que l'obtention d'une répartition de la charge sous forme de fines gouttelettes sur la totalité du solide en mouvement tout en évitant le contact de la charge avec les parois.In the process of the present invention the number of devices (5) is usually a function of the amount of charge to be introduced per unit of time and of the dimensions of the reaction zone; it is chosen so as to ensure the best uniformity of the "C / O" ratio as well as obtaining a distribution of the charge in the form of fine droplets over the entire solid in motion while avoiding contact of the charge with the walls.
Le nombre des dispositifs (5) est habituellement de 1 à 19, de préférence d'au moins 2 et par exemple de 3 à 13. Le nombre de dispositifs d'introduction du fluide de fluidisation des grains de catalyseur est quelconque, mais doit être choisi de manière à assurer une fluidisation aussi parfaite que possible des grains de catalyseur ; il est habituellement de 2 à 50, de préférence de 2 à 26.The number of devices (5) is usually from 1 to 19, preferably at least 2 and for example from 3 to 13. The number of devices for introducing the catalyst grain fluidization fluid is any, but must be chosen so as to ensure as perfect fluidization as possible of the catalyst grains; it is usually from 2 to 50, preferably from 2 to 26.
La représentation sur les figures 1 à 3 de ces dispositifs d'introduction du fluide de fluidisation sous forme de tube ne doit pas être interprétée de manière limitative ; l'homme du métier est à même de concevoir d'autres dispositifs réalisant la même fonction, par exemple un dispositif annulaire, sans sortir du cadre de la présente invention. Il est également possible de prévoir une introduction supplémentaire d'un gaz élévateur (en anglais "lift gas") par exemple à un niveau sensiblement au dessus de celui de l'introduction du catalyseur.The representation in FIGS. 1 to 3 of these devices for introducing the fluidization fluid in the form of a tube should not be interpreted in a limiting manner; the skilled person is able to design other devices performing the same function, for example an annular device, without departing from the scope of the present invention. It is also possible to provide for an additional introduction of a lifting gas (in English "lift gas") for example at a level substantially above that of the introduction of the catalyst.
Les figures 4A et 4B représentent schématiquemeπt un dispositif (5), selon un mode de réalisation préféré de l'invention. Les figures 4A et 4B sont une vue schématique, en coupe, de face et de profil d'un dispositif (5) à 90 degrés d'angle l'une de l'autre. Sur les figures 4A et 4B, la charge pénètre dans le dispositif (5) par le conduit (6) dont l'axe est sensiblement parallèle à l'axe AA' dudit dispositif (5) tandis que le fluide auxiliaire gazeux pénètre par le conduit (7) dont l'axe est sensiblement perpendiculaire à l'axe dudit dispositif (5). Ce mode d'introduction de la charge et du fluide auxiliaire correspond au mode d'introduction préféré selon l'invention, cependant il est possible d'introduire la charge par le conduit (7) et le fluide auxiliaire gazeux par le conduit (6).Figures 4A and 4B show schematically a device (5), according to a preferred embodiment of the invention. FIGS. 4A and 4B are a schematic view, in section, of the front and of the profile of a device (5) at 90 degrees from each other. In FIGS. 4A and 4B, the load enters the device (5) through the pipe (6) whose axis is substantially parallel to the axis AA 'of said device (5) while the gaseous auxiliary fluid enters through the pipe (7) whose axis is substantially perpendicular to the axis of said device (5). This mode of introduction of the charge and of the auxiliary fluid corresponds to the preferred mode of introduction according to the invention, however, it is possible to introduce the charge through the conduit (7) and the gaseous auxiliary fluid through the conduit (6).
Le mélange charge-fluide auxiliaire gazeux qui se forme, de préférence dans le convergent du venturi, acquiert une vitesse très élevée au niveau du col du venturi, puis est vaporisé sous forme de très fines gouttelettes de charge dans le fluide auxiliaire gazeux au niveau de l'ouverture (9) pratiquée dans l'extrémité dudit dispositif (5). Selon un mode préféré de réalisation l'ouverture (9), pratiquée dans l'épaisseur du matériau formant l'extrémité du dispositif (5), a habituellement une forme telle que les parois de cette ouverture définissent, suivant au moins une direction, un angle alpha d'environ 20 à 100 degrés, de préférence d'environ 40 à 90 degrés, dont le sommet est dirigé vers l'amont du dispositif (5). De façon plus précise cette ouverture (9) aura par exemple, dans le cas d'une ouverture de section sensiblement circulaire, la forme d'un cône tronqué d'angle au sommet alpha. Selon le mode de réalisation schématisé sur les figures 4A et 4B, l'extrémité du dispositif (5) a la forme d'une calotte sphérique et l'ouverture a une section sensiblement rectangulaire ; les plans de l'ouverture passant par les côtés du rectangle ayant la plus petite dimension se coupent suivant un angle alpha de 20 à 100 degrés et de préférence de 40 à 90 degrés et les plans passant par les côtés du rectangle ayant la plus graYide dimension sont sensiblement parallèles.The charge-auxiliary gas mixture which forms, preferably in the convergent of the venturi, acquires a very high speed at the level of the venturi neck, then is vaporized in the form of very fine charge droplets in the auxiliary gas at the opening (9) made in the end of said device (5). According to a preferred embodiment the opening (9), formed in the thickness of the material forming the end of the device (5), usually has a shape such that the walls of this opening define, in at least one direction, a alpha angle of about 20 to 100 degrees, preferably about 40 to 90 degrees, the apex of which is directed upstream of the device (5). More precisely, this opening (9) will, for example, in the case of an opening of substantially circular section, have the shape of a truncated cone with an angle at the apex alpha. According to the embodiment shown diagrammatically in FIGS. 4A and 4B, the end of the device (5) has the shape of a spherical cap and the opening has a substantially rectangular section; the planes of the opening passing through the sides of the rectangle having the smallest dimension intersect at an alpha angle of 20 to 100 degrees and preferably 40 to 90 degrees and the planes passing through the sides of the rectangle having the largest dimension are substantially parallel.
La figure 4B représente également schématiquement une vue de la calotte sphérique et de l'ouverture ou fente (9) de section rectangulaire dont le côté de plus petite dimension a une valeur T non représenté sur la figure 4B, mais visible en coupe sur la figure 4A, et le côté de plus grande dimension une valeur "Le" mesurée sur la partie externe et une valeur "Li" mesurée sur la partie interne ; la valeur "Li" étant habituellement inférieure à la valeur "Le".FIG. 4B also schematically represents a view of the spherical cap and of the opening or slot (9) of rectangular section whose side of smaller dimension has a value T not shown in FIG. 4B, but visible in section in the figure 4A, and the side of larger dimension a value "Le" measured on the external part and a value "Li" measured on the internal part; the value "Li" usually being less than the value "Le".
Dans la forme de réalisation préférée du dispositif (5) représenté sur les figures 4A et 4B le conduit (6) d'introduction de la charge débouche au dessus du niveau supérieur du conduit (7) d'introduction du fluide auxiliaire gazeux. De préférence le conduit (6) débouche à proximité du début de la zone convergente du venturi et sensiblement en dessous de celle-ci. L'angle bêta ( figure 4A ) de la zone convergente, ou convergent, du venturi est habituellement de 15 à 45 degrés, de préférence de 20 à 40 degrés et l'angle delta ( figure 4A ) de la zone divergente, ou divergent, du venturi est habituellement de 2 à 20 degrés, de préférence de 3 à 12 degrés, l'angle du divergent étant toujours plus petit que l'angle du convergent et de préférence inférieur à 2 fois l'angle du convergent.In the preferred embodiment of the device (5) shown in Figures 4A and 4B the conduit (6) for introducing the charge opens above the upper level of the conduit (7) for introducing the gaseous auxiliary fluid. Preferably the conduit (6) opens near the beginning of the converging zone of the venturi and substantially below the latter. The beta angle (FIG. 4A) of the convergent zone, or convergent, the venturi is usually 15 to 45 degrees, preferably 20 to 40 degrees, and the delta angle (Figure 4A) of the divergent, or divergent, area of the venturi is usually 2 to 20 degrees, preferably 3 to 12 degrees, the angle of the diverging point being always smaller than the angle of the converging point and preferably less than twice the angle of the converging point.
A l'extrémité du divergent dont le diamètre dans sa partie la plus large est appelé "d" (voir figure 4A), se trouve un organe, ayant une ouverture (9), définissant une restriction de la section de ladite extrémité, c'est à dire que ladite ouverture présente habituellement une section de surface (par exemple IxLe dans le cas d'une ouverture (9), de section rectangulaire, telle que représentée sur les figures 4A et 4B) inférieure à πd2/4, par exemple de πd2/20 à πd2/6 et de préférence de πd2/12 à πd2/8. Cet organe est représenté sur la figure 4A comme étant la continuité du venturi ; on peut également envisager un embout (10) ayant la forme désirée qui vient se fixer, par exemple se visser, sur l'extrémité du venturi, et de même à l'autre extrémité du venturi on peut envisager la fixation des moyens d'introduction (11) de la charge et du fluide auxiliaire gazeux comme cela est représenté sur la figure 5. Il est dans tous les cas 'préférable que la géométrie interne de l'injecteur soit telle qu'il n'y ait pas de décrochement entre la paroi du venturi et celle de l'embout ou de l'organe définissant la restriction de section ; la géométrie externe pouvant être de forme sensiblement identique (figure 4A) ou sensiblement différente (figure 5) de celle de la géométrie interne.At the end of the diverging part, the diameter of which in its widest part is called "d" (see FIG. 4A), there is a member, having an opening (9), defining a restriction of the section of said end, it means that said opening has usually one surface section (e.g. IxLe in the case of an opening (9) of rectangular section, as shown in figures 4A and 4B) less than πd 2/4, e.g. πd of 2/20 to πd 2/6 and preferably πd 2/12 to πd 2/8. This member is represented in FIG. 4A as being the continuity of the venturi; we can also consider a nozzle (10) having the desired shape which is fixed, for example screwing, on the end of the venturi, and similarly at the other end of the venturi we can consider fixing the introduction means (11) of the charge and of the gaseous auxiliary fluid as shown in FIG. 5. It is in any case ' preferable that the internal geometry of the injector is such that there is no offset between the wall of the venturi and that of the nozzle or of the member defining the section restriction; the external geometry can be of substantially identical shape (FIG. 4A) or substantially different (FIG. 5) from that of the internal geometry.
L'ouverture (9) sur les figures 3, 4A et 5 a été représentée dans une position symétrique par rapport à l'axe du dispositif (5). Cette schématisation est une représentation de la forme préférée de réalisation du dispositif (5). Il est cependant possible, sans sortir du cadre de la présente invention, de concevoir un positionnement non symétrique de l'ouverture (9) par rapport à l'axe du dispositif (5). Dans une forme préférée de réalisation comportant plusieurs enceintes (ou dispositifs) (5), chacun d'entre eux pourra avoir une géométrie différente des autres ou un certain nombre auront une géométrie déterminée et le ou les autres une autre géométrie ou ils pourront être tous identiques.The opening (9) in Figures 3, 4A and 5 has been shown in a symmetrical position relative to the axis of the device (5). This diagram is a representation of the preferred embodiment of the device (5). It is however possible, without departing from the scope of the present invention, to design an asymmetrical positioning of the opening (9) relative to the axis of the device (5). In a preferred embodiment comprising several enclosures (or devices) (5), each of them may have a different geometry from the others or a certain number will have a determined geometry and the other (s) another geometry or they can all be identical.
Les figures 4A, 4B et 5 ne sont que des représentations schématiques du dispositif (5) selon l'invention et ne doivent pas être considérées comme limitant l'invention au mode de représentation illustré par ces figures. En particulier l'homme du métier est à même de concevoir diverses formes pour ce dispositif, par exemple une zone rectiligne au col peut être présente entre la zone convergente et la zone divergente dudit dispositif. L'utilisation des dispositifs (5) selon l'invention permet d'obtenir des vitesses de la charge très élevées. Au niveau du col du venturi ces vitesses peuvent même dépasser la vitesse du son. On obtient ainsi une excellente dispersion de la charge liquide dans le fluide auxiliaire gazeux. Les conditions sont habituellement choisies de manière à ce que la vitesse à la sortie des dispositifs (5) soit de 10 à 600 m/s, de préférence de 50 à 340 m/s. Etant donné qu'il est souhaitable d'avoir un contact rapide entre le catalyseur et la charge dès la sortie des dispositifs (5) on préfère habituellement avoir des vitesses élevées ou même très élevées de la charge, par exemple au moins 100 m/s. Un autre avantage de l'utilisation des dispositifs (5) est la possibilité d'obtention d'un brouillard de très fines gouttelettes dont le diamètre moyen est de l'ordre de grandeur de la taille des grains de catalyseur, par exemple de l'ordre de 65 microns (65x10"^ m) avec une faible dispersion autour de cette valeur. La taille des grains de catalyseur est habituellement de 10 à 120 microns (1 micron : 10"6 m ) avec une forte proportion de grains ayant une taille d'environ 65 microns.FIGS. 4A, 4B and 5 are only schematic representations of the device (5) according to the invention and should not be considered as limiting the invention to the mode of representation illustrated by these figures. In particular, a person skilled in the art is able to design various forms for this device, for example a rectilinear zone at the neck may be present between the converging zone and the diverging zone of said device. The use of the devices (5) according to the invention makes it possible to obtain very high load speeds. At the level of the venturi neck these speeds can even exceed the speed of sound. An excellent dispersion of the liquid charge in the gaseous auxiliary fluid is thus obtained. The conditions are usually chosen so that the speed at the outlet of the devices (5) is from 10 to 600 m / s, preferably from 50 to 340 m / s. Since it is desirable to have rapid contact between the catalyst and the charge as soon as it leaves the devices (5), it is usually preferred to have high or even very high speeds of the charge, for example at least 100 m / s . Another advantage of the use of the devices (5) is the possibility of obtaining a mist of very fine droplets whose average diameter is of the order of magnitude of the size of the catalyst grains, for example order of 65 microns (65x10 " ^ m) with a small dispersion around this value. The size of the catalyst grains is usually from 10 to 120 microns (1 micron: 10" 6 m) with a high proportion of grains having a size about 65 microns.
Le procédé de la présente invention comprenant l'introduction de la charge d'hydrocarbures sensiblement suivant la direction des grains de catalyseur permet de limiter, en particulier par rapport au cas d'une injection latérale, les collisions entre les gouttelettes de charge et les grains de catalyseur d'où une meilleure vaporisation progressive et un cokage moins important.The process of the present invention comprising the introduction of the hydrocarbon charge substantially in the direction of the catalyst grains makes it possible to limit, in particular with respect to the case of lateral injection, the collisions between the charge droplets and the grains catalyst resulting in better progressive vaporization and less coking.
L'invention concerne également un appareil ou réacteur (1), de forme allongée, sensiblement vertical comportant (voir figure 2) une conduite d'admission (2) de particules solides et comportant à l'une de ses extrémités et par exemple en son extrémité inférieure une plaque support (sensiblement perpendiculaire à l'axe longitudinal du réacteur) à travers laquelle sont agencés des moyens d'introduction d'un gaz de fluidisation, par exemple des tubulures (3) sensiblement parallèles à l'axe du réacteur allongé, tubulures à travers lesquelles on introduit dans le réacteur ledit gaz destiné à assurer la fluidisation des particules solides, ledit réacteur comportant en outre des moyens d'introduction d'une charge d'hydrocarbures en son sein, caractérisé en ce qu'il comporte au moins 1 dispositif, et de préférence au moins 2 dispositifs, de type venturi, chaque dispositif ayant la forme d'un tube, chaque tube étant aménagé dans la plaque support, l'axe de chaque tube étant sensiblement parallèle à l'axe longitudinal du réacteur, chaque dispositif comportant, d'amont en aval dans le sens du déplacement de la charge, a) à une extrémité une conduite d'entrée de la charge dont l'axe est sensiblement perpendiculaire à l'axe du tube ou dont l'axe est sensiblement confondu avec l'axe du tube (forme de réalisation préférée) et une conduite d'entrée d'un fluide auxiliaire dont l'axe est sensiblement confondu avec l'axe du tube ou dont l'axe est sensiblement perpendiculaire à l'axe du tube (forme de réalisation préférée) (les deux conduites d'entrée de la charge et du fluide auxiliaire étant ainsi sensiblement perpendiculaires), b) un convergent et un divergent, l'angle du convergent du venturi étant compris entre 15 et 45 degrés, l'angle du divergent du venturi étant compris entre 2 et 20 degrés, l'angle du divergent étant toujours plus petit que (inférieur à) l'angle du convergent et c) à l'autre extrémité un orifice d'injection de la charge dans le réacteur, cet orifice comportant une calotte sensiblement sphérique comportant une ouverture de section sensiblement rectangulaire, circulaire, elliptique ou ayant la forme d'une couronne ou d'un secteur de couronne, ladite ouverture ayant de préférence une forme telle que ses parois définissent, suivant au moins une direction, un angle alpha (voir figure 4B) compris entre 20 et 100 degrés, la surface de ladite ouverture étant inférieure à πd2/4 où "d" est le diamètre du divergent dans sa partie la plus large (voir figure 4A).The invention also relates to an apparatus or reactor (1), of elongated shape, substantially vertical comprising (see FIG. 2) an intake pipe (2) of solid particles and comprising at one of its ends and for example in its lower end a support plate (substantially perpendicular to the axis longitudinal of the reactor) through which are arranged means for introducing a fluidizing gas, for example pipes (3) substantially parallel to the axis of the elongated reactor, pipes through which said gas intended for introduction ensuring the fluidization of solid particles, said reactor further comprising means for introducing a hydrocarbon charge therein, characterized in that it comprises at least 1 device, and preferably at least 2 devices, venturi type, each device having the shape of a tube, each tube being arranged in the support plate, the axis of each tube being substantially parallel to the longitudinal axis of the reactor, each device comprising, from upstream to downstream in the direction of movement of the load, a) at one end a load inlet pipe whose axis is substantially perpendicular to the axis of the tube or whose axis is substantially coincident with the axis d u tube (preferred embodiment) and an auxiliary fluid inlet pipe whose axis is substantially coincident with the axis of the tube or whose axis is substantially perpendicular to the axis of the tube (embodiment preferred) (the two inlet lines for the charge and the auxiliary fluid thus being substantially perpendicular), b) a convergent and a diverging, the angle of the converging of the venturi being between 15 and 45 degrees, the angle of the diverging of the venturi being between 2 and 20 degrees, the angle of the diverging point being always smaller than (less than) the angle of the converging point and c) at the other end an orifice for injecting the charge into the reactor, this orifice comprising a substantially spherical cap comprising an opening of substantially rectangular, circular, elliptical section or having the shape of a crown or of a crown sector, said opening preferably having a shape such that its walls define According to at least one direction, an angle alpha (see FIG 4B) of between 20 and 100 degrees, the surface of said opening being less than πd 2/4 where "d" is the diameter of the diverging part in its widest part ( see Figure 4A).
Dans une forme préférée de réalisation de l'invention le réacteur comprend une pluralité de dispositifs de type venturi répartis symétriquement sur la plaque support ; les dispositifs situés à la périphérie de ladite plaque support comportent à une extrémité un orifice d'injection de la charge d'hydrocarbures, cet orifice ménagé dans une calotte sensiblement sphérique a une ouverture ou fente de section sensiblement rectangulaire, les plans de l'ouverture passant par les côtés du rectangle ayant la plus petite dimension se coupant suivant un angle alpha (voir figure 4B) compris entre 20 et 100 degrés, les plans passant par les côtés du rectangle ayant la plus grande dimension étant sensiblement parallèles et les dispositifs situés à proximité du centre de ladite plaque support comportent à une extrémité un orifice d'injection de la charge d'hydrocarbures, cet orifice ménagé dans une calotte sensiblement sphérique a une ouverture de préférence circulaire, elliptique ou ayant la forme d'une couronne.In a preferred embodiment of the invention the reactor comprises a plurality of venturi-type devices distributed symmetrically on the plate support; the devices located at the periphery of said support plate comprise at one end an orifice for injecting the hydrocarbon charge, this orifice formed in a substantially spherical cap has an opening or slot of substantially rectangular section, the planes of the opening passing through the sides of the rectangle having the smallest dimension intersecting at an alpha angle (see FIG. 4B) of between 20 and 100 degrees, the planes passing through the sides of the rectangle having the largest dimension being substantially parallel and the devices located at near the center of said support plate have at one end an orifice for injecting the hydrocarbon charge, this orifice formed in a substantially spherical cap has an opening preferably circular, elliptical or having the shape of a crown.
Dans le procédé de la présente invention les caractéristiques, dimensionnelies et opératoires, industrielles peuvent être habituellement les suivantes: - hauteur de la zone réactionnelle : 5 à 40 mètresIn the process of the present invention, the industrial, dimensional and operational characteristics can usually be as follows: - height of the reaction zone: 5 to 40 meters
- température d'introduction de la charge à craquer : 60 à 450 °C, de préférence 70 à 400 °C- introduction temperature of the charge to be cracked: 60 to 450 ° C, preferably 70 to 400 ° C
- débit d'alimentation de la colonne en catalyseur : 3 à 50 tonnes par minute- feed rate of the column of catalyst: 3 to 50 tonnes per minute
- temps de séjour de la charge dans la colonne (zone réactionnelle) 0,05 à 10 secondes, de préférence moins de 6 secondes et par exemple de 0,8 à 5 secondes.- residence time of the charge in the column (reaction zone) 0.05 to 10 seconds, preferably less than 6 seconds and for example from 0.8 to 5 seconds.
- quantité de fluide auxiliaire utilisé pour la pulvérisation ou atomisatioπ de la charge de 0,5 à 30 % en poids par rapport au poids de la charge à craquer, de préférence de 2 à 20 % en poids.- amount of auxiliary fluid used for spraying or atomizing the charge from 0.5 to 30% by weight relative to the weight of the charge to be cracked, preferably from 2 to 20% by weight.
Le flux de grains de catalyseur dans lequel la charge est introduite est habituellemnt un flux homogène de catalyseur en phase fluidisée ayant habituellement une densité de 15 à 800 kg/m3 et de préférence de 20 à 600 kg/m3- La vitesse linéaire de ce flux est avantageusement de 0,01 à 30 m/s et de préférence de 10 à 20 m/s- La fluidisation et le flux de grains de catalyseur sont obtenus par l'introduction d'un fluide gazeux de fluidisation qui pourra être un hydrocarbure ayant par exemple de 1 à 5 atomes de carbone dans sa molécule ou un mélange d'hydrocarbures. Ce fluide gazeux de fluidisation peut comprendre jusqu'à 35 % en volume d'hydrogène et jusqu'à 10 % en volume de vapeur d'eau. Ce fluide peut aussi être composé de 100 % en volume de vapeur d'eau.The flow of catalyst grains into which the charge is introduced is usually a homogeneous flow of catalyst in the fluidized phase usually having a density of 15 to 800 kg / m 3 and preferably from 20 to 600 kg / m 3 - The linear speed of this flow is advantageously from 0.01 to 30 m / s and preferably from 10 to 20 m / s. The fluidization and the flow of catalyst grains are obtained by the introduction of a gaseous fluidization fluid which may be a hydrocarbon having for example from 1 to 5 carbon atoms in its molecule or a mixture of hydrocarbons. This gaseous fluidization fluid can comprise up to 35% by volume of hydrogen and up to 10% by volume of water vapor. This fluid can also be composed of 100% by volume of water vapor.
Les conditions d'injection de ce fluide gazeux varient bien entendu en fonction de la taille et du poids des grains de catalyseur.The conditions for injecting this gaseous fluid naturally vary depending on the size and weight of the catalyst grains.
Le flux de grains de catalyseur est habituellement introduit à une température de 500 à 750 °C lorsque la charge à craquer est du type classique telle qu'une charge de gas-oil. Cependant avec des charges dites lourdes, c'est à dire des charges contenant par exemple plus de 10 % de leur volume composé d'hydrocarbures de point d'ébullition supérieur à 550 °C, la température pourra avantageusement être de 650 à 950 °C de façon à assurer la vaporisation complète des molécules les plus lourdes, ainsi que leur craquage thermique sélectif dans la zone d'injection au réacteur.The flow of catalyst grains is usually introduced at a temperature of 500 to 750 ° C. when the charge to be cracked is of the conventional type such as a diesel charge. However with so-called heavy fillers, that is to say fillers containing for example more than 10% of their volume composed of hydrocarbons with a boiling point higher than 550 ° C., the temperature may advantageously be from 650 to 950 ° C. so as to ensure complete vaporization of the heaviest molecules, as well as their selective thermal cracking in the injection zone of the reactor.
Les études effectuées par la demanderesse ont montré que lors de l'utilisation d'injecteurs de forme tubulaire, à sortie libre, comme décrit dans l'art antérieur, seule une très faible quantité de catalyseur est atteinte par le jet directionnel obtenu. Au contraire l'utilisation d'injecteur ayant la forme des dispositifs décrits dans la présente demande permet d'obtenir de fines gouttelettes ayant une direction privilégiée imposée par les caractéristiques de l'ouverture et recouvrant une plus grande surface de catalyseur. Ces études ont également montré qu'il est préférable d'utiliser plusieurs dispositifs (5) de manière à mieux répartir la quantité de charge et de fluide auxiliaire gazeux sur chacun d'eux en fonction de leur positionnement dans la zone réactionnelle.The studies carried out by the applicant have shown that when using injectors of tubular shape, with free outlet, as described in the prior art, only a very small amount of catalyst is reached by the directional jet obtained. On the contrary, the use of an injector having the form of the devices described in the present application makes it possible to obtain fine droplets having a preferred direction imposed by the characteristics of the opening and covering a larger surface of catalyst. These studies have also shown that it is preferable to use several devices (5) so as to better distribute the quantity of charge and of gaseous auxiliary fluid on each of them according to their positioning in the reaction zone.
Ainsi dans une forme préférée de réalisation chacun des dispositifs (5) est alimenté séparément par une quantité déterminée de charge en fonction de sa position. Cette méthode permet de mieux tenir compte du fait que la densité de catalyseur dans une section du réacteur à un niveau donné n'est pas homogène et ainsi de n'introduire que la quantité de charge souhaitée en fonction de la quantité de catalyseur présente sur la surface arrosée par le jet de charge sortant d'un dispositif (5) donné. La quantité de catalyseur dans un volume donné pouvant varier au cours du temps il est possible de prévoir un système de régulation de la quantité de charge que l'on injecte dans chacun des dispositifs (5) de manière à l'adapter à la quantité de catalyseur atteinte par le jet dudit dispositif.Thus in a preferred embodiment each of the devices (5) is supplied separately by a determined amount of charge depending on its position. This method makes it possible to take better account of the fact that the density of catalyst in a section of the reactor at a given level is not homogeneous and thus to introduce only the quantity of charge desired as a function of the quantity of catalyst present on the surface watered by the charge jet leaving a given device (5). As the quantity of catalyst in a given volume can vary over time, it is possible to provide a system for regulating the quantity of charge which is injected into each. devices (5) so as to adapt it to the quantity of catalyst reached by the jet of said device.
Le fluide auxiliaire gazeux, utilisé pour favoriser l'atomisation de la charge et introduit dans le ou les dispositifs (5), est habituellement de la vapeur d'eau ou un fluide gazeux relativement riche en hydrogène ou en composés hydrogénés en provenance de l'unité de FCC (recyclage) ou d'autres unités de la raffinerie.The gaseous auxiliary fluid, used to promote atomization of the charge and introduced into the device (s) (5), is usually water vapor or a gaseous fluid relatively rich in hydrogen or hydrogenated compounds coming from the FCC unit (recycling) or other refinery units.
Enfin, les catalyseurs utilisables dans le procédé faisant l'objet de la présente invention comprennent les catalyseurs de craquage de type alumino-siiicates cristallins et certains types de silice-alumine, de silice-magnésie ou de silice-zirconium, tous ayant des activités de craquage relativement élevées. Les alumino-siiicates cristallins peuvent se trouver à l'état naturel ou être préparés par synthèse, selon des techniques bien connues de l'homme du métier, lis peuvent être choisis parmi les zéoiithes de synthèse ou les argiles, telles que la faujasite, certaines mordénites, la montmonllonite, les argiles pontées, les alumino-phosphates, ou similaires. Finally, the catalysts which can be used in the process which is the subject of the present invention include cracking catalysts of the crystalline aluminosilicate type and certain types of silica-alumina, of silica-magnesia or of silica-zirconium, all having activities of relatively high cracking. The crystalline aluminosilicates can be found in the natural state or be prepared by synthesis, according to techniques well known to those skilled in the art, They can be chosen from synthetic zeolites or clays, such as faujasite, some mordenites, montmonllonite, bridged clays, alumino-phosphates, or the like.

Claims

REVENDICATIONS
1 - Procédé de craquage catalytique d'une charge d'hydrocarbures en lit fiuidisé dans lequel les grains de catalyseur en lit fiuidisé sont mis en contact avec ladite charge laquelle se présente sous forme de fines gouttelettes de diamètre moyen inférieur à 3x10"4 m dans une zone réactionnelle de forme allongée ayant un axe de symétrie caractérisé en ce que ladite charge est introduite en mélange avec un fluide auxiliaire gazeux dans ladite zone réactionnelle par l'intermédiaire d'au moins une enceinte de type venturi, d'axe sensiblement parallèle à l'axe de ladite zone réactionnelle, comprenant d'amont en aval dans le sens du déplacement de la charge d'hydrocarbures,1 - Process for catalytic cracking of a charge of hydrocarbons in a fluidized bed in which the grains of catalyst in a fluidized bed are brought into contact with said charge which is in the form of fine droplets with an average diameter of less than 3 × 10 −4 m in a reaction zone of elongated shape having an axis of symmetry characterized in that said charge is introduced as a mixture with a gaseous auxiliary fluid into said reaction zone by means of at least one enclosure of venturi type, of axis substantially parallel to the axis of said reaction zone, comprising from upstream to downstream in the direction of displacement of the hydrocarbon charge,
- (a) à une première extrémité au moins un moyen d'introduction dudit fluide auxiliaire et de ladite charge d'hydrocarbures,- (a) at a first end at least one means for introducing said auxiliary fluid and said hydrocarbon charge,
- (b) en aval de ladite première extrémité une zone de rétrécissement puis une zone d'élargissement et- (b) downstream of said first end a narrowing zone then a widening zone and
- (c) comprenant à son autre extrémité un organe comportant au moins une ouverture et définissant une restriction de la section de ladite extrémité, à travers laquelle ledit mélange est introduit dans ladite zone réactionnelle.- (c) comprising at its other end a member comprising at least one opening and defining a restriction on the section of said end, through which said mixture is introduced into said reaction zone.
2 - Procédé selon la revendication 1 dans lequel l'enceinte de type venturi comprend un organe comportant une ouverture de section sensiblement rectangulaire, circulaire, elliptique ou ayant la forme d'une couronne ou d'un secteur de couronne.2 - Method according to claim 1 wherein the venturi type enclosure comprises a member having an opening of substantially rectangular, circular, elliptical section or having the shape of a crown or of a crown sector.
3 - Procédé selon la revendication 1 ou 2 dans lequel l'ouverture a une forme telle que les parois de cette ouverture définissent, suivant au moins une direction, un angle alpha d'environ 20 à 100 degrés.3 - Process according to claim 1 or 2 wherein the opening has a shape such that the walls of this opening define, in at least one direction, an angle alpha of about 20 to 100 degrees.
4 - Procédé selon l'une des revendications 1 à 3 comportant l'utilisation d'au moins deux enceintes de type venturi, disposées de manière à ce que les extrémités de ces enceintes débouchant dans la zone réactionnelle soient réparties symétriquement à l'intérieur de ladite zone réactionnelle. 5 - Procédé selon l'une des revendications 1 à 4 dans lequel les dispositifs (5) situés à proximité de la paroi de la zone réactionnelle ont une ouverture (9) de section sensiblement rectangulaire ou en forme de secteur de couronne et le ou les dispositifs (5) situés à proximité du centre de la zone réactionnelle ont une ouverture (9) de section sensiblement circulaire, elliptique ou en forme de couronne.4 - Method according to one of claims 1 to 3 comprising the use of at least two venturi-type enclosures, arranged so that the ends of these enclosures opening into the reaction zone are distributed symmetrically inside said reaction zone. 5 - Method according to one of claims 1 to 4 wherein the devices (5) located near the wall of the reaction zone have an opening (9) of substantially rectangular section or in the form of a crown sector and the or the devices (5) located near the center of the reaction zone have an opening (9) of substantially circular, elliptical or crown-shaped section.
6 - Procédé selon l'une des revendications 1 à 5 dans lequel la charge d'hydrocarbures est introduite dans le ou les enceintes de type venturi par un conduit dont l'axe est sensiblement parallèle à l'axe de ladite enceinte et le fluide auxiliaire par un conduit dont l'axe est sensiblement perpendiculaire à l'axe de la dite enceinte.6 - Method according to one of claims 1 to 5 wherein the hydrocarbon charge is introduced into the venturi type enclosure (s) by a conduit whose axis is substantially parallel to the axis of said enclosure and the auxiliary fluid by a conduit whose axis is substantially perpendicular to the axis of said enclosure.
7 - Procédé selon l'une des revendications 1 à 6 dans lequel la charge d'hydrocarbures et le fluide auxiliaire sont introduits à l'aide d'au moins trois enceintes de type venturi disposées de manière symétrique sur une plaque support disposée au bas de la zone réactionnelle, ladite plaque support comprenant également au moins deux organes d'injection d'un gaz de fluidisation des grains de catalyseur, le sommet desdits dispositifs de type venturi étant situé au dessus de la zone d'introduction des grains de catalyseur.7 - Method according to one of claims 1 to 6 wherein the hydrocarbon charge and the auxiliary fluid are introduced using at least three venturi type chambers arranged symmetrically on a support plate disposed at the bottom of the reaction zone, said support plate also comprising at least two members for injecting a gas for fluidizing the catalyst grains, the top of said venturi type devices being located above the zone for introducing the catalyst grains.
8 - Réacteur (1), de forme allongée, sensiblement vertical comportant (voir figure 2) une conduite d'admission (2) de particules solides et comportant à l'une de ses extrémités une plaque support (sensiblement perpendiculaire à l'axe longitudinal du réacteur) à travers laquelle sont agencés des moyens d'introduction d'un gaz de fluidisation, moyens à travers lesquels on introduit dans le réacteur ledit gaz destiné à assurer la fluidisation des particules solides, ledit réacteur comportant en outre des moyens d'introduction d'une charge d'hydrocarbures en son sein, caractérisé en ce qu'il comporte au moins 1 dispositif de type venturi ayant la forme d'un tube, ledit tube étant aménagé dans la plaque support, l'axe dudit tube étant sensiblement parallèle à l'axe longitudinal du réacteur, chaque dispositif comportant, d'amont en aval dans le sens du déplacement de la charge, a) à une extrémité une conduite d'entrée de la charge dont l'axe est sensiblement confondu avec l'axe du tube ou dont l'axe est sensiblement perpendiculaire à l'axe du tube et une conduite d'entrée d'un fluide auxiliaire dont l'axe est sensiblement perpendiculaire à l'axe du tube ou dont l'axe est sensiblement confondu avec l'axe du tube (les deux conduites d'entrée de la charge et du fluide auxiliaire étant ainsi sensiblement perpendiculaire), b) un convergent et un divergent, l'angle du convergent du venturi étant compris entre 15 et 45 degrés, l'angle du divergent du venturi étant compris entre 2 et 20 degrés, l'angle du divergent étant toujours plus petit que l'angle du convergent et c) à l'autre extrémité un orifice d'injection de la charge dans le réacteur, cet orifice comportant une calotte sensiblement sphérique comportant une ouverture de section sensiblement rectangulaire, circulaire, elliptique ou ayant la forme d'une couronne ou d'un secteur de couronne, ladite ouverture ayant de préférence une forme telle que ses parois définissent, suivant au moins une direction, un angle alpha (voir figure 4B) compris entre 20 et 100 degrés, la surface de ladite ouverture étant inférieure à πd2/4 où "d" est le diamètre du divergent dans sa partie la plus large (voir figure 4A). 8 - Reactor (1), of elongated shape, substantially vertical comprising (see FIG. 2) an intake pipe (2) of solid particles and comprising at one of its ends a support plate (substantially perpendicular to the longitudinal axis of the reactor) through which are arranged means for introducing a fluidizing gas, means through which said gas intended to ensure the fluidization of solid particles is introduced into the reactor, said reactor further comprising means for introducing of a hydrocarbon charge therein, characterized in that it comprises at least 1 venturi type device having the form of a tube, said tube being arranged in the support plate, the axis of said tube being substantially parallel at the longitudinal axis of the reactor, each device comprising, from upstream to downstream in the direction of displacement of the load, a) at one end a feed inlet pipe whose axis is substantially coincident with the axis of the tube or whose axis is substantially perpendicular to the axis of the tube and an auxiliary fluid inlet pipe whose axis is substantially perpendicular to the axis of the tube or whose axis is substantially coincident with the axis of the tube (the two inlet pipes for the load and the auxiliary fluid thus being substantially perpendicular), b) a convergent and a diverging point, the angle of the converging point of the venturi being between 15 and 45 degrees, the angle of the diverging point of the venturi being between 2 and 20 degrees, the angle of the diverging point being always smaller than the angle of the converging point and c) at the other end an orifice for injecting the charge into the reactor, this orifice comprising a substantially spherical cap having an opening of substantially rectangular, circular, elliptical section or having the shape of a crown or of a crown sector, said opening preferably having a shape such that its walls define, su ivant at least one direction, an angle alpha (see FIG 4B) of between 20 and 100 degrees, the surface of said opening being less than πd 2/4 where "d" is the diameter of the diverging part in its widest part (see Figure 4A).
PCT/FR1990/000154 1989-03-24 1990-03-07 Process and device for the injection of a hydrocarbon charge in a fluid catalytic cracking process WO1990011337A1 (en)

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FR8904046A FR2644795B1 (en) 1989-03-24 1989-03-24 METHOD AND DEVICE FOR INJECTING THE HYDROCARBON LOAD IN A FLUID CATALYTIC CRACKING PROCESS

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EP0546739A2 (en) * 1991-12-13 1993-06-16 Mobil Oil Corporation Heavy hydrocarbon feed atomization
US5289976A (en) * 1991-12-13 1994-03-01 Mobil Oil Corporation Heavy hydrocarbon feed atomization
US6645437B1 (en) 1995-11-10 2003-11-11 Institut Francais Du Petrole Device for injecting a hydrocarbon charge
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EP0454416A3 (en) * 1990-04-27 1991-11-13 Exxon Research And Engineering Company Feed injector for catalytic cracking unit
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CN115672196A (en) * 2021-07-23 2023-02-03 中国石油天然气股份有限公司 Stirring type small-particle catalyst filling equipment

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ZA902253B (en) 1990-11-28
FR2644795B1 (en) 1993-12-17
JPH06508159A (en) 1994-09-14
FR2644795A1 (en) 1990-09-28

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