JP4557363B2 - Method and apparatus for raw material contact by an immediate catalyst separation system - Google Patents

Description

[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a method and an apparatus for immediate catalytic separation type feedstock contact in fluid catalytic cracking (FCC).
[0002]
[Prior art]
Fluidized solid technology, in which a stream containing at least partially liquid phase hydrocarbon compounds is contacted with fluidized solids in the contact zone and carbonaceous or other contaminants are deposited on the solids. There are many continuous circulation processes used. The solids are transported to another zone in the course of circulation, and the contaminants are removed in the regeneration section, or more specifically, in most cases, burned with a medium containing oxygen to at least one of the carbon deposits. Part is removed. Solids are sequentially removed from the reclaimed part and all or part of it is reintroduced into the contact zone.
[0003]
One of the more important processes of this nature is fluid catalytic cracking (FCC) to convert relatively high boiling hydrocarbons to lower hydrocarbons. The hydrocarbon feed is contacted with a particulate cracking catalyst that remains in a fluidized state under suitable conditions for converting hydrocarbons in one or more reaction zones.
[0004]
The processing of increasingly heavy feedstocks in FCC type processes and the tendency of these feedstocks to increase coke formation and the formation of undesirable products has led to new ways of contacting the feedstock with the catalyst. In recent years, there has been particular interest in methods of contacting the FCC catalyst for a very short time. In US Patent Application No. 4,985,136, the FCC feed is contacted with the falling curtain of the catalyst for a time of less than 1 second and then rapidly separated. This very short contact time improves the selectivity to gasoline and reduces the formation of coke and dry gas by using a highly active catalyst previously contacted with the feed for a relatively short period of time. These inventions particularly relate to highly active zeolite catalysts. Configurations for performing such raw material contact are known from US Patent Application No. 2,935,466, US Patent Application No. 4,435,272, US Patent Application No. 4,944,845, US Patent Application No. 5,296,131, and US Patent Application No. 5,462,652.
[0005]
The preferred injection system for such a short time contact system has received particular attention in the cited patent. The feed can be formed into a jet by a series of identical feed injection streams, or by expanded orifices that are in uniform contact with the catalyst stream flowing in a fused pattern. This raw material injection is configured such that the raw material is ejected to a relatively thin strip of catalyst that falls in a direction perpendicular to the flow of the jet.
[0006]
Apart from bringing the raw material and the catalyst into uniform contact, it is also necessary that the catalyst and hydrocarbon be well separated in a short contact time system. Such prior art typically directs the catalyst and gas mixture to a conduit that connects with a downstream separator. Thus, the contact between the hydrocarbon and the catalyst will flow into the separation device and will continue for a significant amount of time while present in the separation device.
[0007]
[Problems to be solved by the invention]
An object of the present invention is to further shorten the contact time between a catalyst and a hydrocarbon in an apparatus for bringing a relatively heavy hydrocarbon into contact with fluidized catalyst particles for a short time.
[0008]
[Means for Solving the Problems]
The present invention provides the feedstock by injecting the catalyst stream with the contacted steam into the free zone under dilute catalyst phase conditions and rapidly removing cracked steam from the upper portion of the dilute catalyst phase zone. It provides a rapid separation step from the catalyst stream. The combination of the horizontal injection of the dilute phase into the free vessel and the removal of the upper part of the steam immediately initiates the gravitational separation of the catalyst from the hydrocarbon vapor. This process stops a significant portion of the contact between the catalyst and the hydrocarbon immediately after the catalyst stream is injected into the free vessel. Contact between the feedstock and the catalyst is initiated at the same location as or close to the injection of the catalyst stream into the release vessel. In this way, this very short contact time can be controlled from a minimum time close to zero to a longer time. Unlike the prior art, the present invention requires that contact be maintained while the catalyst and hydrocarbon mixture is moving together vertically or horizontally toward the separation stage.
[0009]
DETAILED DESCRIPTION OF THE INVENTION
Accordingly, one embodiment of the present invention is a method for fluidized catalytic cracking of hydrocarbon feedstock. In this method, catalyst particles and hydrocarbons are injected substantially horizontally from the injection point into the free zone. In the collection zone, the catalyst particles descending below the injection point are collected. The free zone between the injection point and the collection zone is at least 5 feet away, thus ensuring a fall zone for continuous separation of catalyst and hydrocarbon vapor. In that process, ascending steam and entrained catalyst particles are recovered from the upper part of the discharge zone and transferred to the inertial separation zone. The inertial separation zone separates the entrained catalyst from the rising gas and provides a separated vapor stream and a separated catalyst.
The process also recovers hydrocarbons from the bottom of the free zone and from the separated vapor stream.
[0010]
Typically, a jet of hydrocarbon-containing feed is injected into a fluidized bed of catalyst particles, located mainly upstream, upstream of the injection point, around the separation zone or outside the separation zone. In a particularly useful form of the invention, a vertical tube is used as the location for the distributor nozzle configuration that provides contact between the hydrocarbon-containing stream and the particulate falling layer. In general, injection of a jet of hydrocarbon-containing feed into a fluidized bed of catalyst particles takes place in a closed conduit, but injection takes place near the outlet of the conduit into a free vessel.
Due to the position of the distributor in the vertical tube, the fluid and solid mixture can be discharged directly from the distributor into the free container at an appropriate height for carrying out the present invention. This vertical pipe distributor configuration can fit in close to most vertical pipe joints.
[0011]
In an embodiment of the apparatus, the present invention is composed of a free container part, a catalyst and a raw material contact device in order to inject the raw material and the catalyst from the injection point into the free container part in a substantially horizontal direction. This raw material contacting device injects a hydrocarbon-containing raw material into a fluidized stream of catalyst and supplies the raw material and catalyst to the injection point. A collection vessel located just below the free vessel and located at least 5 feet below the point of injection collects a dense bed of catalyst from the free vessel. An inertial separation device located above the free vessel portion communicates directly with the upper portion of the free vessel portion and separates hydrocarbons from the catalyst particles rising with the hydrocarbons from the free vessel portion. The catalyst outlet formed by the inertia separator is separated from the inertia separator to recover hydrocarbons.
[0012]
The present invention can be used in combination with any type of particulate material. The substance may be inert in the presence of a specific fluid substance or may be reactive. A wide range of inert catalytic materials are suitable for use in the present invention. For example, a suitable inert material for the degradable distillation process includes alpha alumina. The FCC apparatus to which this method is applied can use any known catalyst used in the technical field of fluidized catalytic cracking. These compositions contain amorphous clay type catalysts which are largely replaced by highly active crystalline alumina silica or zeolite containing catalysts. Zeolite-containing catalysts are preferred over amorphous type catalysts in that they have a high activity inherent in them and high resistance to deactivation effects due to high temperatures and exposure to metals contained in most feedstocks. Zeolite is the most commonly used crystalline aluminosilicate and is usually dispersed in a porous inorganic support such as silica, alumina or zirconium. These catalyst compositions may contain 30% or more of zeolite. The zeolite catalyst used in the process according to the invention preferably contains zeolite corresponding to 25 to 80% by weight of the catalyst. Zeolites are also stabilized with rare earth elements and may contain 0.1 to 10 wt% rare earth elements.
[0013]
Although primarily intended for use in FCC units, the present invention is also useful for all processes where hydrocarbon containing streams and fluidized particle streams are contacted for a short time. Process types for which the present invention is useful include contact of catalyst with residual feed and cracking contact of high temperature inert or catalytic particles with high asphaltene containing feed. Liquid media suitable for the present invention include all liquid streams, at least a portion of which enters the distributor as a liquid and further evaporates upon contact with the particulate material. The raw materials for cracking contact include heat-resistant crude oil with a wide range of boiling points and high concentrations of metals and coke. For example, a typical crude oil has a boiling range of 116-815 ° C (240-1575 ° F) and more than half of the liquid volume boils above 1000 ° F. Suitable feedstocks for performing the FCC process with the method of the present invention include conventional feedstocks and high boiling feedstocks and residue feedstocks. The most common raw material in the past is a hydrocarbon substance having a boiling range of usually 343 to 552 ° C. (650 to 1050 ° F.), and a vacuum gas oil prepared by vacuum fractionation of an atmospheric residue. These fractions are generally low in coke precursors and heavy metals that can deactivate the catalyst. Heavy raw materials or residual raw materials having a boiling point of about 500 ° C. (930 ° F.) or higher and a high metal content are also frequently used in FCC apparatuses.
[0014]
When used in catalytic operations, deposited metal and coke inactivate the catalyst by blocking the active site of the catalyst. To overcome this inactivation effect, coke can be removed to the desired extent by regeneration.
[0015]
Embodiments of the present invention will be described with reference to the drawings. FIG. 1 shows an FCC device arranged according to the present invention. The FCC apparatus shown in FIG. 1 is constituted by a reaction tower 10 including a free container section 11, a collection container section 14, and a separator 13. The separator 13 includes a separation container portion 12 and a riser 15. With this configuration, the catalyst and the raw material are circulated in the manner described below.
[0016]
For reaction zone operation, freshly regenerated catalyst, spent catalyst, or a mixture thereof enters the reaction tower through a nozzle 16 that is normally in communication with the end of the regenerated catalyst vertical tube. The feed is injected into the vertical tube nozzle through a feed injection nozzle 17 in contact with the catalyst, and preferably through a contactor described below. The feedstock and catalyst particles enter the free vessel portion 11 from the injection point 18 after or simultaneously with the contact between the feedstock and the hydrocarbon.
[0017]
Due to the contact between the catalyst and the raw material, a concentrated stream of the catalyst flowing into the free container portion 11 along a substantially horizontal flow path is formed. As used herein, a substantially horizontal flow path means a flow path having at least a major horizontal component. The main direction of the catalyst stream as it enters the free vessel mainly determines the trajectory into which the feed and hydrocarbon streams flow. Thus, the hydrocarbon stream, as shown at A in FIG. 1, is 60 ° to ensure that the catalyst moment moves so that the mixture of catalyst and hydrocarbon crosses the free vessel section 11 in a substantially horizontal direction. It is directed into the separation vessel at an angle of less than that. Discharging from the liberation point in a substantially horizontal direction facilitates rapid separation of the vapor hydrocarbon stream from relatively heavy catalyst particles. In order to perform rapid separation, a vertical space is also required so as not to restrict the path of the gas rising upward through the free vessel 11. For this purpose, the free container part has a substantial opening 19 above the injection point and, perhaps more importantly, a substantial opening 20 below the injection point. Yes. Opening 20 is defined as the diluted catalyst density region indicated by dimension B in FIG. The dimension B is at least 1.5 m at a minimum and more generally in the range of 2 to 3.6 m. The diluted phase state means that the catalyst is 300 kg / m ^Three Less than density, more typically 150 kg / m ^Three Less than density. The catalyst density in the open portions 19 and 20 changes as the raw material and catalyst contact point is approached. Normally, the density of open parts is 80kg / m on average ^Three Typically, the average catalyst density is 48.4kg / m ^Three Is less than. Catalyst from the openings 19 and 20 collects in a dense bed 22 in the collection zone 14. The high-density phase state means that the apparent bulk density of the catalyst is 240 to 800 kg / m ^Three It is characterized by being in the range. Thus, the dense bed in collection zone 22 typically has at least 240 kg / m of catalyst particles. ^Three , More preferably 730kg / m ^Three It is held at the above bulk density. The portion of distance B on the liberation zone 11 can also function as a descending zone where the catalyst separates from the ascending gas and descends.
[0018]
The collection zone 14 is entrained from the catalyst entering this zone and can serve as a stripping zone for recovering the adsorbed hydrocarbons. Stripping gas enters collection zone 14 through nozzle 23 and distributor 24. Dispersed stripping gas such as water vapor rises upward through the catalyst. A series of grids 25 redistribute the stripping medium and the stripped hydrocarbons as they move upward through the bed 22. Nozzle 26 draws the stripped catalyst for regeneration in a regeneration vessel (not shown) and / or recirculates to nozzle 16 to recontact the catalyst and feedstock. By selectively adding a regenerated catalyst that is heated to the bed 22, stripping can be facilitated by raising the temperature within the stripping zone. The heated catalyst can enter the stripping zone above the bed interface 21 through the nozzle 27. Alternatively, if there is a minimum free length between the injection point 18 and the bed level 21 ', the high density phase catalyst should be maintained on the entry point of the regenerated catalyst through the nozzle 27. An extended bed portion 22 'having a higher catalyst interface 21' may be provided.
[0019]
It is also possible to separate stripped hydrocarbons recovered from the bottom of the bed 22 through a baffle not shown. Separation of stripped hydrocarbons can provide different product streams for downstream separation and recovery. By increasing the contact time of hydrocarbons entering the collection zone, the characteristics of cracked hydrocarbons recovered from this zone can be fundamentally changed. By individually collecting the streams from the stripping zone, the product stream isolated from the upper portion of the release vessel 11 can be more easily collected alone.
[0020]
However, the stripping medium and stripped hydrocarbons usually rise inside the free vessel 11 and combine with the free hydrocarbons coming from the nozzle 16 along with the catalyst stream. As the gas and jetted catalyst ascend inside the free zone 19, the transitional portion of the truncated cone 28 reduces the area of the flow stream, and as it enters the riser riser 15, the velocity of those gases increases. The state in the liberation zone 19, the truncated cone 28 and the riser 15 is often referred to as a rapid fluidization state, in which the upward catalyst transfer rate is in the range of 6-18 m / sec and the density range is 65 550kg / m ^Three Range.
[0021]
Ascending hydrocarbons and all additional entrained catalyst enter the inertial separator with each pair of arms 29 having an opening 30 that rises and is tangentially directed. The arm 29 provides inertial separation by centripetal acceleration of relatively heavy catalyst particles, thereby quickly removing most of the catalyst from the vaporized hydrocarbon. The fact that the opening is directed tangentially for centripetal or cyclonic separation does not mean that other inertial separation devices such as using ballistic separation from vaporized hydrocarbons are excluded. The cracked hydrocarbon containing a trace amount of catalyst leaves the separator 13 through the outlet 31.
[0022]
In many cases, the hydrocarbon vapor from the outlet 31 is further subjected to a separation process in order to recover a trace amount of catalyst particles contained therein. Usually, in the cyclone type separation device, secondary recovery of the residual catalyst particles is performed. The catalyst particles recovered from the additional separation device can be returned to the collection zone 14 via the nozzle 32. After performing additional catalyst recovery, the product is usually transferred to a separation zone (not shown) to remove light gases and heavy hydrocarbons from the product.
[0023]
Catalyst recovered from inertial separator 13 is collected in bed 33 for return to bed 22 inside collection zone 14. The catalyst can be sent from the bed 33 through one or more internal or external vertical tubes 34 to the collection zone 14. FIG. 1 shows the configuration of an internal vertical tube 34 for refluxing the catalyst from a bed 33 that is isolated from the open portions 19 and 20 of the free zone 11. The bottom 35 of the vertical pipe 34 is usually disposed below the floor 22. Placing the bottom 35 of the vertical tube below the floor 22 is to prevent the reverse flow of the stripped vapor to the separated vapor that is recovered through the vertical tube to the head of the separation zone 13.
[0024]
The internal vertical tube 34 is configured such that the injected hydrocarbon and catalyst particles can leave a clear trajectory when entering the free zone 11 from the injection point 18. As more clearly shown in FIG. 2, the space between the inner conduits is increased in the region of the nozzle 16 to provide a spacing equal to the dimension C between the conduits 34. Preferably, the dimension C is at least equal to the diameter of the nozzle 16. With this layout, the injected hydrocarbon and catalyst particles will have a well-defined trajectory extending at least to the center of the free zone 11 as indicated by dimension T.
[0025]
The construction of the inertia separator 13 and the manner of refluxing the catalyst to the collection zone 14 can be accomplished in a variety of different ways. FIG. 3 illustrates the use of a downwardly extending conduit 36 and separation side plate 40 to increase the amount of catalyst recovered from the inertial separator and returned to the dense bed 22 "through the external vertical tube 38. 3 is operated in a manner similar to that described in connection with Fig. 1. The main difference is that the steam moves up in the free vessel 11 '. Introducing additional changes in the direction of the steam when doing and further separating the catalyst particles from the hydrocarbon gas before the mixture leaves the separation zone 13 '. The hydrocarbons entering the free vessel portion 11 'from the point 18' are further separated from incoming catalyst particles as they flow towards the opening 39 that receives the inertially separated hydrocarbon gas. 39 functions as a separator inlet, where catalyst particles and hydrocarbons are injected at 18 points. Facing the separation zone facing the side to be ejected through, with such a configuration, the hydrocarbons exit the separation zone on the side opposite to where the catalyst particles and hydrocarbons are injected.
[0026]
Hydrocarbon and entrained catalyst from the intake 39 continues to move upward through the riser 15 '. The arm 29 'again discharges the catalyst and jet catalyst particles in the tangential direction through the opening 30'. The side plate 40 moves upward to provide a restricted opening 41 for the recovered gas that enters the second portion 42 of the separator 13 '. The recovered hydrocarbon leaves the separation zone 13 'again from the nozzle 31' together with the residual catalyst.
[0027]
External vertical tube 38 recovers catalyst from bed 33 'which recovers catalyst from inertial separator 13'. The conduit 38 bypasses the liberation zone 11 'and feeds the catalyst into the catalyst bed 22' of the collection zone 14 '. The outer vertical tube 38 'keeps the liberation zone 11' fully open to separate the vaporized hydrocarbons from the catalyst stream.
[0028]
The opening in the liberation zone may be further sectioned to limit hydrocarbon separation from the catalyst particle stream. As shown in FIG. 4, a pair of baffles 43 can be placed in the central portion 44 of the free zone 11 'near the catalyst conduit 16' that discharges the mixture of catalyst particles and feedstock. The liberation zone 11 'may be further modified to provide a conduit for refluxing catalyst particles located outside the region 44'. The catalyst conduit 46 may be arranged in a fan shape outside the baffle 43.
[0029]
In the method and apparatus according to the present invention, the feed may first be contacted with a regenerated catalyst, a carbonized catalyst, or a mixture of the two. This process can be used in any regeneration format to remove coke. Coke removal, which usually operates to completely remove coke from the catalyst, is commonly referred to as “complete regeneration”. Complete regeneration is the removal of coke from the catalyst to a level of less than 0.2 wt%, preferably less than 0.1 wt%, more preferably less than 0.05 wt%.
[0030]
The regenerated catalyst has a much higher temperature than the carbonized catalyst. Usually, the regenerated catalyst entering the regeneration conduit 16 is in the temperature range of 590-760 ° C, more typically the temperature is in the range of 650-760 ° C. Once the catalyst mixture is in contact with the feedstock, the catalyst accumulates coke on the catalyst particles and cools. The temperature of the carbonization catalyst is usually in the range of 480-620 ° C., but the temperature varies depending on the source.
[0031]
A preferred vertical tube and feed injection scheme for the present invention is shown in FIG. FIG. 5 shows a contact device 115 that breaks the raw material into a stream of fine droplets. A flange 111 at the end of the conduit 17 normally holds the contact device 115 inside the conduit 17. The stream produced by the contact device 115 provides a linear array of catalysts in contact with the catalyst descending curtain formed by the outlet 114 of the chute 113.
[0032]
When the raw material is brought into contact with the catalyst, rapid evaporation occurs, and the catalyst is discharged into the separation vessel at a high speed. Heavy hydrocarbons are decomposed into light hydrocarbons by contact between the raw material and the catalyst, and coke is produced at most catalytic active sites on the catalyst. When the catalyst curtain descending in the vertical direction and the raw material contact in the lateral direction, an effective trajectory to the free vessel of the catalyst and raw material mixture is formed. In order to achieve rapid contact between the feed and the catalyst particles, the feed is preferably brought into lateral contact with the curtain of descending catalyst. The expression “contacting in the lateral direction” means that the feed does not flow parallel to the direction of the falling curtain of the catalyst. After injecting the hydrocarbon jet, it is usually less than 1.5 m, preferably less than 0.3 m, through the conduit 17 before being injected into the free zone from the injection point.
[0033]
As shown in FIGS. 5 and 6, the chute 113 is fixed to the inside of the conduit 116, and the opening 114 has a shape surrounded by a straight line. This chute usually has a width equal to or greater than about half the width of the conduit 16. Exhausted catalyst enters conduit 16 from a control valve, generally a slip valve (not shown). This control valve controls the flow rate of the catalyst entering the chute 113. The discharge rate of the catalyst from the take-out port 114 can be controlled by adding a stream upstream of the chute 113.
[0034]
The contactor 115 creates a spray pattern that can be merged with the shape of the descending curtain. When the descending curtain has a linear shape as shown, the raw material injector typically produces a horizontal pattern of atomized liquid. Thus, in a preferred configuration, the feed is discharged substantially laterally with respect to the falling curtain of the catalyst. The expression substantially lateral contact is used when the contactor 115 is at an angle of at least 30 °, preferably at least 45 ° between the main directions of injecting the feed into the catalyst layer or descending curtain. ing. Preferably, the feed flows perpendicularly to and contacts the downward curtain of the moving catalyst. When in contact with the falling curtain of the catalyst, the feed is generally at a speed of 0.3 m / sec or more and the temperature is in the range of 150 ° C to 320 ° C.
[0035]
The nozzle of the contact device 115 is sized to produce a jet with a flow velocity from the opening in the range of 9 to 120 m / sec, and preferably 30 to 90 m / sec. In accordance with FCC general practice standards, the raw material exits the nozzle opening of the contact device as a jet.
[0036]
Dispersion of the raw material into fine droplets is promoted by giving sufficient energy to the liquid. In some instances, the present invention may be practiced with some degree of gas dilution, such as steam, added to the feed before being discharged through the outlet. Adding gaseous substances helps to atomize the ingredients. Usually, a minimum amount of gaseous material corresponding to about 0.2% by weight of the liquid gas mixture is mixed with the liquid before being discharged through the nozzle.
Usually, when steam is added, the amount is 5% by weight of the liquid gas mixture or less. For most liquids, atomization creates droplets in the size range 50-750 microns.
[0037]
FIG. 7 shows a linear array of nozzles 123 that extend across the front surface of the contactor 115. The nozzle 123 is oriented such that a mixture of fluid atomized in a linear flow pattern from a nozzle arranged in a more central direction is directly ejected from the contactor 115. These nozzles 123 arranged on the outer side of the array can be set at an angle that allows the atomized liquid to be directed onto a wider pattern and maintain a uniform and even gap between the jets. The nozzle 123 can be angle-adjusted in this manner to accommodate any length and configuration of catalyst flow pattern or catalyst dispersion.
[0038]
【The invention's effect】
The process of the present invention stops a significant portion of the contact between the catalyst and hydrocarbon immediately after the catalyst stream is injected into the free vessel, and the contact between the feed and the catalyst is injected into the free vessel of the catalyst stream. The contact time between the raw material and the catalyst can be controlled from a minimum time close to zero to a longer time.
[Brief description of the drawings]
FIG. 1 is a schematic diagram of an FCC device incorporating the short-term contact time device of the present invention.
FIG. 2 is a schematic view of a cross section taken along line 2-2 of FIG.
FIG. 3 is a schematic diagram of an FCC device incorporating another short contact time device of the present invention.
4 is a schematic view of a section taken along line 4-4 of FIG.
FIG. 5 is a cross-sectional view of a vertical conduit portion including a contact device used in the present invention.
6 is a cross-sectional view taken along line 6-6 of FIG.
7 is a front view of the raw material distributor of line 7-7 in FIG. 5. FIG.
[Explanation of symbols]
16, 17 Closed conduit
18 Injection point
19 Opening area
20 Free zone
22 Collection zone
27, 39 intake
29 Inertial separator
31 Outlet
34 conduit
114,115 contactor

Claims (10)

In the method of fluid catalytic cracking of hydrocarbon-containing raw materials,
a) Around the free zone (20) or in the free zone (20) in the catalyst particle free vessel, which has a catalyst particle collection zone (22) on the lower side and a free zone (20) for the catalyst particles on the upper side. Injecting a jet of hydrocarbon-containing raw material from an injection point (18) arranged outside, mainly in a transverse direction toward the fluidized bed of catalyst particles upstream of the injection point;
b) injection point the catalyst particles and hydrocarbons free zone (20) from (18), comprising the steps of injecting horizontally, opening the top and bottom of the free zone (20) is injection point (18) (19) An injection step characterized in that the average catalyst density is lower than 80 kg / m ³ ;
c) Collecting catalyst particles descending in the collection zone (22) below the injection point (18) and at least a descent distance (B) between the injection point (18) and the collection zone (22). Maintaining in the release zone at .5 m, wherein the collection zone has a catalyst density of at least 240 kg / m ³ ;
d) the vapor and entrained catalyst particles rises from the open portion disposed in the upper (19) of the injection point (18) was collected, and the pre-Symbol ascending vapor and entrained catalyst particles to an inertial separation zone (29) Transferring and separating the entrained catalyst from the rising steam to provide separated steam and separated catalyst ; and e) recovering hydrocarbons from the bottom of the liberation zone (20) and the separated steam stream. and,
Including methods.   The process according to claim 1, wherein the hydrocarbons recovered from the lower part of the liberation zone (20) flow upwards to the inertial separator (29) and are recovered as part of the separated vapor stream.   The process according to claim 1, wherein the catalyst separated in the common stripping zone (22) is collected together with the descending catalyst.   The process according to claim 1, wherein the separated catalyst is recovered at the top of the liberation zone (20), isolated from the rising steam and flowing downwards towards the collection zone (22). Injection of the jet of hydrocarbon-containing feedstock to the catalyst particles fluidized layer is performed in a closed conduit (16, 17) within the catalyst particles after injection of the jet of hydrocarbon-containing feedstock injection point a conduit interior from (18) 3. The method according to claim 2, wherein the free zone is injected before flowing over 1.5 m. Regenerated catalyst stream regenerated catalyst inlet (27) through the injection point (18) below the free zone (20) or enters the collection zone (22), wherein the drop of the catalyst is pre-Symbol regenerated catalyst inlet (27 2. The process according to claim 1, which is carried out in a descending zone (22) extending below.   The rising steam and entrained catalyst enter the inertial separator (29) through a separator inlet (39) having an opening facing the free zone (20) facing the side on which the catalyst particles and hydrocarbons are injected. Item 2. The method according to Item 1. An apparatus for rapidly contacting a granular catalyst with a hydrocarbon-containing feedstock,
A catalyst particle release vessel ( 11 ) having a catalyst particle collection zone (22) on the lower side and a catalyst particle release zone (20) on the upper side ;
In a catalyst and raw material contactor for injecting hydrocarbon-containing raw material into a fluidized bed of catalyst particles and injecting catalyst particles and raw material horizontally into the free vessel part (11) from the injection point (18) From the injection point (18) disposed around the free zone (20) in the free vessel or outside the free zone (20), the jet of the contained raw material is directed to the fluidized bed of catalyst particles upstream from the injection point. Catalyst and feedstock contactors (114, 115) characterized by being injected mainly in the transverse direction ;
A collection vessel portion (14) located adjacent to the free vessel portion and at least 1.5 m below the injection point (18) for collecting a concentrated layer of catalyst ;
In order to separate the hydrocarbons from the catalyst particles increases with hydrocarbons from the free container portion (11), is disposed above the free container portion (11), through further upper part and communicating directly free container portion (11) An inertial separator (29) , and
Catalyst outlet for collecting the separated hydrocarbons from the previous SL inertial separator (31),
Including the device. A plurality of conduits (34) extend vertically through the free vessel section ( 11 ) and take a trajectory such that hydrocarbons and catalyst particles entering the free zone (20) from the injection point (18) enter the center of the free zone. 9. The apparatus of claim 8 , wherein the plurality of conduits are spaced apart.   9. The inertia separator (29) forms a horizontally protruding intake (39) that opens to the free zone (20) side facing the side from which catalyst particles and hydrocarbons are poured. The device described.

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