KR101488854B1 - Apparatus and process for minimizing catalyst residence time in a reactor vessel - Google Patents

Abstract

The inventors have discovered a method of minimizing the time that the catalyst and gaseous product contact after exiting the discharge opening 22 of the reactor conduit 10. [ The reactor conduit is evacuated into a separation chamber (16) directly connected to the separator (32). The dip leg 34 of the separator is connected directly to the separation chamber or intermediate chamber 64 directly connected to the separation chamber. Thus, the catalyst never gets a chance to be incorporated into the large open volume of the reactor vessel. Consequently, the catalyst outside the separation chamber quickly returns to the separation chamber, minimizing the amount of time that the catalyst and gaseous product contact after being discharged from the reactor conduit.

Description

[0001] APPARATUS AND PROCESS FOR MINIMIZING CATALYST RESIDENCE TIME IN A REACTOR VESSEL [0002]

The present invention generally relates to a method for the rapid separation of solid particulates from gases. More particularly, the present invention relates to minimizing contact between the gaseous product and the catalyst particles after the reaction.

The fluidized catalytic cracking (FCC) process is the process of decomposing high molecular weight hydrocarbons into gasoline and LPG range hydrocarbons. The FCC process is carried out by contacting a hydrocarbon feedstock, such as vacuum gas oil, residual crude oil, or another source of relatively high boiling hydrocarbons, with a catalyst consisting of finely divided or particulate solid material in a long conduit. The feed is contacted with the fluidized bed catalyst particles to promote the cracking reaction and the coke is coated on the catalyst. The catalyst exiting the reaction zone is considered as "spent catalyst ", that is, partially deactivated by coating the catalyst with the coke. Typically, the spent catalyst is delivered to a stripper that removes hydrocarbons and gases adsorbed from the catalyst, and then to the regenerator to remove the coke by oxidation with oxygen containing gas. The regenerated catalyst returns to the reaction zone. Oxidizing the coke from the catalyst surface releases a large amount of heat, and some of the heat leaves the regenerator with the regenerated catalyst. The FCC process utilized herein, as well as its separation device, is described in detail in US 5,584,985 and US 4,792,437.

The spent catalyst still has catalytic activity. Prolonged contact between the spent catalyst and the cracked product may allow overspreading of the desired product and additional coke coating, thereby reducing the recovery of the desired product. Waste catalyst and gaseous products exiting the reactor conduit typically enter the reactor vessel of large volume and may remain in the vessel for a long time before separation, thereby allowing additional degradation to occur. A separation device at the exhaust end of the reactor conduit was used to quickly separate most of the catalyst and gaseous products.

US 4,397, 738 and US 4,482, 451 disclose an apparatus for rapidly separating a mixture of gaseous product and solid catalyst particles from a reactor conduit by tangentially discharging it into a reactor containment vessel. The centrifugal force generated by the tangential discharge of the gas containing the solid catalyst particles causes the heavy particles to move away from the light gas so that the gas is recovered from above and the solid is collected from below. The reactor containment vessel has a relatively large diameter and generally provides a first separation of solids from the gas. The first separation step in these devices is followed by a second separation which more fully separates the solid from the gas in a conventional cyclone separator, typically located in a reactor vessel.

Typically, the cyclone separator comprises a relatively small diameter cyclone having a tangential inlet on the outside of the cylindrical vessel forming the outer housing of the cyclone. The tangential inlet provides a tangential velocity to the entrained gas and the entrained gas to allow the solid to be collected downward and the light gas to be collected upward. The collected catalyst solids usually come down to the catalyst bed at the bottom of the reactor vessel via a dipleg.

The catalyst layer is typically fluidized to facilitate entry of the catalyst into the stripper vessel. The reactor vessel includes a large volume of void space through which the catalyst can be incorporated with the gaseous product. Contamination may occur when the catalyst is transferred between the separator ends, when they are transferred from the cyclone deep leg into the catalyst bed, and when fluidized in the catalyst bed. Typically, the reactor vessel is purged with an inert gas, such as steam, to prevent the gas product from floating with the catalyst particles incorporated in the reactor vessel. However, hydrocarbons are adsorbed to the catalyst particles incorporated in the inert gas, which can continue to react until the catalyst enters the stripping vessel. Finally, a significant percentage of hydrocarbons in the stripping vessel are desorbed and separated from the catalyst particles. Thus, the catalyst and gaseous products may be present together in the reaction vessel for a long period of time after the desired reaction is completed and the catalyst and gaseous product exits the reactor conduit.

US 4,220,623 discloses a reactor vessel for an FCC unit separated from a stripper vessel. The stripper exhaust line extends from the stripper vessel upwardly along the dip legs of the cyclone in the reactor vessel to a height above the dense layer in the reactor vessel. This arrangement aims at reducing the height of the reactor vessel. The reactor conduit is not directly connected to the cyclone separator in the reactor vessel.

US 4,946,656 discloses a reactor conduit which is connected directly to a first stage cyclone separator connected to a second stage cyclone separator by a gas conduit. The return conduit between the first stage cyclone separator and the second stage cyclone separator is opened to the reactor vessel. The dip legs of the first stage cyclone separator and the second stage cyclone separator descend into the stripper region through the truncated conical stripper cap. The periphery of the stripper cap is spaced from the inner sidewall of the reactor vessel by a maximum distance of 25% of the inner radius of the reactor vessel. The aeration conduit is passed from the stripper region to the conduit between the first stage cyclone separator and the second stage cyclone separator. The vapor flow rate required to prevent the gaseous product from being sent from the stripper area through the numerous openings in the stripper cap into the reactor vessel and to cause the gas product to flow upwardly through the aeration conduit to the recovery conduit will be very large.

The present inventors have found a way to minimize the time the catalyst and gaseous products contact after exiting the exit end of the reactor conduit of the FCC unit. The reactor conduit is discharged into a separation chamber connected directly to the separator. The dip leg of the separator is connected directly to the separation chamber or to the intermediate chamber directly connected to the separation chamber. Thus, the catalyst never enters the large open volume of the reactor vessel. As a result, the catalyst outside the separation chamber quickly returns to the separation chamber, minimizing the contact time after the catalyst and gaseous product are discharged from the reactor conduit. The reactor vessel may also be purged with an inert gas, such as steam, so that any gaseous product does not rise upwards in the reactor vessel.

It is therefore an object of the present invention to provide a method and apparatus for minimizing the contact time between solid catalyst particles and gaseous products after they exit the reactor conduits of the FCC unit.

Further details and embodiments of the invention will be apparent from the following detailed description of the invention.

1 is a schematic front view of an FCC unit deployed in accordance with the present invention.

Figure 2 is a schematic front view of an alternative FCC unit deployed in accordance with the present invention.

3 is an enlarged sectional view of Fig.

Figure 4 is a schematic front view of an alternative partial FCC unit deployed in accordance with the present invention.

5 is a schematic front view of an alternative partial FCC unit deployed in accordance with the present invention.

Figure 6 is a schematic front view of an alternative partial FCC unit deployed in accordance with the present invention.

7 is an enlarged sectional view of Fig.

The present invention can be used in an apparatus or method in which a solid and a gas must be separated. However, the FCC process always requires this separation and will be the most extensive application for the present invention. Accordingly, the present invention will be described by way of example in FCC application.

The FCC process, in which the present invention may be used, is a gas oil such as light vacuum diesel. Other petroleum derived feed streams to the FCC unit may include diesel boiling range mixtures of heavy hydrocarbons or hydrocarbons such as residual oil. In one embodiment, the feed stream has an initial boiling point above 230 ° C (446 ° F), often above 290 ° C (554 ° F), typically above 315 ° C (600 ° F) and above 566 ° C RTI ID = 0.0 > (1050 F). ≪ / RTI > The reaction zone of the FCC process is generally maintained at high temperature conditions, which may include temperatures of greater than 425 ° C (797 ° F). In one embodiment, the reaction zone has a temperature of 480 ° C to 590 ° C (896 ° F to 1094 ° F) and a pressure of less than 40 psig (69 to 517 kPa (ga) (10 to 75 psig), typically 275 kPa Lt; RTI ID = 0.0 > pressure. ≪ / RTI > The catalyst to oil ratio based on the weight of the catalyst and hydrocarbon feed entering the bottom of the riser is in the range of 20: 1 or less, but may typically range from 4: 1 to 10: 1. Although hydrogenation is known in the art, hydrogen is not normally added to the riser. In some cases, steam may be sent into the riser to effect catalytic fluidization and feed water dispersion. The average residence time of the catalyst in the riser may be less than 5 seconds. The catalyst types employed in the process may be selected from a variety of commercially available catalysts. Although a catalyst comprising a zeolitic material is preferred, a more elaborate amorphous catalyst can be used if desired.

Preferably the catalyst regeneration zone operates at a pressure of 69 to 552 kPa (ga) (10 to 80 psig). The spent catalyst applied to the regeneration zone may contain 0.2 to 15 wt% coke. The coke is mainly composed of carbon and may contain sulfur and other elements as well as 3 to 12 wt% of hydrogen. Oxidation of coke will produce normal combustion products: water, carbon oxides, sulfur oxides and nitrous oxide. As known to those skilled in the art, the regeneration zone may take a variety of configurations, and the regeneration is performed in one or more stages.

1 is a schematic configuration of an FCC unit embodying the present invention. The FCC unit includes a long riser or reactor conduit 10. The high temperature catalyst is delivered to the lower section of the reactor conduit 10 and the fluidizing gas from the distributor 8 pneumatically transfers the catalyst particles upwardly through the reactor conduit 10. As the mixture of catalyst and carrier gas continues to rise through the reactor conduit 10, the nozzle 40 injects the hydrocarbon feed, possibly with steam, into the catalyst. Contact with the hot catalyst evaporates the hydrocarbons and further transports the gas and catalyst mixture through the reactor conduit 10 while at the same time decomposing the hydrocarbons into the desired lower boiling point product.

The reactor conduit 10 extends upwardly into the reactor vessel 12, as in a conventional FCC unit. The reactor conduit 10 preferably has a vertical orientation in the reactor vessel 12 and may extend upwardly through the bottom of the reactor vessel 12. The reactor vessel 12 includes a separation chamber 16 defined by an outer separation wall 24. The outer separating wall 24 of the separating chamber 16 has a section that can be partially cylindrical. The reactor conduit 10 terminates at the exit defined by the end of the vortex arm 14 in the separation chamber 16. Each of the vortex arms 14 may be a curved tube having an axis of curvature that may be parallel to the reactor conduit 10. Each vortical arm 14 has one open end communicatively connected to the reactor conduit 10 and another open end comprising a discharge opening. The vortex arm 14 discharges the gaseous fluid mixture comprising the decomposition products and the solid catalyst particles through the discharge opening 22. The tangential exhaust of the gas and catalyst from the discharge opening 22 creates a vortex spiral motion with respect to the cylindrical interior of the separation chamber 16. The centripetal acceleration coupled with the helical motive force causes the heavier catalyst particles to go to the outer portion of the separation chamber 16. The catalyst particles from the discharge openings 22 gather at the bottom of the separation chamber 16 to form a dense catalyst layer 38. Gas having a density lower than that of the solid catalyst particles changes direction more easily and starts upward spiral motion. The separation chamber 16 includes a gas return conduit 18 having an inlet 20 through which the spiraling gas eventually passes. The gas entering the gas return conduit 18 through the inlet 20 will usually contain a small amount of catalyst particles. The inlet 20 not only recovers gas from the discharge opening 22 but also recovers the stripping gas from the stripping section 28 which can be placed in the separation chamber 16 as described below. The content of catalyst particles in the gas entering the gas recovery conduit 18 are usually less than ^{16 kg / m 3 (1 lb} / ft 3) , and typically less than ^{3 kg / m 3 (0.2 lb} / ft 3). The gas recovery conduit 18 of the separation chamber 16 is connected to the inlet 30 of one or more cyclones 32 for further removal of the particulate catalyst material from the gas escaping from the gas recovery conduit 18 of the separation chamber 16. [ And an outlet 26 leading to the outlet 26. The separation chamber 16, the gas return conduit 18 and the cyclone 32 are all directly connected, which means that they are in fluid communication with each other and are sealed against substantial leakage. Thus, substantially all of the gases and solids exiting the separation chamber 16 enter the cyclone 32.

The cyclone 32 creates a vortex motion to form a vortex that separates the solid from the gas. The relatively gaseous product stream without catalyst particles exits the cyclone 32 into the fluid-tight plenum chamber 56 through the vapor discharge pipe 50. The gas product stream then exits the reactor vessel 12 through the outlet 25. Each cyclone 32 includes an upper cylindrical barrel 31 connected to an inlet 30. The barrel portion 31 is connected to the hopper portion 35 by the first conical portion 33. The hopper portion 35 leads to the second conical portion 37, which also extends to the deep leg 34. The catalyst solids recovered by the cyclone 32 escape through the bottom of the cyclone through the deep legs 34. The deep leg 34 includes a conduit which may have one or more sections. The deep leg 34 extends downwardly from the reactor vessel 12 and passes through the opening 36 in the outer separation wall 24 of the separation chamber 16. Thus, the deep leg 34 is directly connected to the separation chamber 16, which allows the deep leg 34 to leak out so that all solids and gases escaping substantially from the deep leg 34 enter into the separation chamber 16. [ Quot; seal " The dip leg 34 shown in Fig. 1 includes a diagonal portion extending into the separation chamber 16. Fig. It is not necessary, however, that other configurations of the deep legs 34 are included in the present invention, and that the deep legs 34 extend beyond the outer wall 24 of the separation chamber 16. A suitable device such as a slip joint or expansion joint may be used in the opening 36 to accommodate the differential thermal expansion between the deep leg 34 and the opening 36 at the outer wall 24 of the separation chamber 16. [ In addition, a suitable valve, such as a trickle valve, can be used at the outlet of the deep leg 34 to regulate the catalyst flow. If a slip joint is used between the dip leg 34 and the opening 36, an inert gas, such as steam, may be injected into the reactor vessel 12 by the distributor 42 to purgize the reactor, So that it can not escape. If an expansion joint is used in the opening 36, no purging will be necessary to prevent the gas or solid from escaping through the opening 36 by the expansion joint. However, injection of an inert gas may be required to purge other gaps between the piping in the reactor vessel 12. [

The deep leg 34 transfers the catalyst to the high density catalyst layer 38 in the separation chamber 16. The catalyst solids in the high-density catalyst layer 38 enter the stripping section 28, which can be placed in the separation chamber 16. The catalyst solids pass down and / or through a series of baffles 44 in the stripping section 28 downwardly. The stripping fluid, typically steam, enters the bottom of the stripping section 28 through at least one distributor 46. Through the baffle 44, the stripping fluid and the counter-current contact of the catalyst remove the gas product adsorbed to the catalyst as the catalyst continues to move downward through the stripping section 28. The stripped catalyst from the stripping section 28 can pass through the conduit 48 to the catalyst regenerator 52. In the regenerator, the coke coating is burned from the surface of the catalyst by contact with the oxygen-containing gas at elevated temperatures. Following regeneration, the regenerated catalyst particles are delivered back to the bottom of the reactor conduit 10 via conduit 54.

Fig. 2 shows an alternative embodiment of the invention shown in Fig. Fig. 3 shows an enlarged section of Fig. 2 and 3, the same reference numerals will be used to denote the same elements as in Fig. However, elements having different constructions in FIG. 1 and FIG. 2 will be denoted by the same reference numerals as in FIG. 1, but denoted by a prime symbol ('). Referring to FIG. 2, the deep leg 34 'of the cyclone 32' does not extend until it reaches the opening 36 'in the outer wall 24' of the separation chamber 16 '. However, the deep leg 34 'extends at least into the opening 62 in the intermediate separable separation wall 60 of the reactor vessel 12', and extends through the opening 62 in this embodiment. The intermediate separable separation wall 60 defines the intermediate chamber 64 together with the wall of the reactor vessel 12 'and the outer wall 24' of the separation chamber 16 '. Figure 3 shows this arrangement in detail. The intermediate separable separation wall 60 may be secured to the inner surface of the outer wall of the reactor vessel 12 'and the outer surface of the outer wall 24'. An expansion joint may be provided between the opening 62 in the intermediate separable separation wall 60 and the deep leg 34 '. This configuration will eliminate the need for purging to prevent gas escaping from the intermediate chamber 64 into the open volume within the reactor vessel 12 '. If a slip joint is provided between the opening 62 and the deep leg 34 'in the intermediate separable separation wall 60, purging of the inert gas is required to prevent gas from escaping through the opening 62 through the intermediate chamber 64 will be. The intermediate separable separation wall 60 can be made less durable than the walls of the outer wall 24 'or the reactor vessel 12'. If the pressure difference becomes severe, the intermediate separable separation wall 60 will break or rupture before the outer wall 24 'of the separation chamber 16' or the wall of the reactor vessel 12 'is broken, so that the separation chamber 16' ) Or the reactor vessel 12 '. However, the intermediate separable separation wall 60 is shown in FIGS. 2 and 3 as being fixed by welding or the like only to the outer surface of the outer wall 24 'of the separation chamber 16'. Alternatively, the intermediate separable separation wall 60 may be fixed only to the deep leg 34 'with respect to the opening 62 or only to the inner surface of the outer wall of the reactor vessel 12'. In this case, purging of the inert gas from the distributor 42 may be necessary to prevent the gas from escaping from the intermediate chamber 64. In the case of an interruption or failure that can promote a significant pressure difference between the separation chamber 16 'and the reactor vessel 12', the intermediate separable separation wall 60 is bent with respect to the fixed part, Can be. The intermediate separable separation wall 60 should have a small thickness compared to the walls of the outer wall 24 'and / or the reactor vessel 12' of the separation chamber 16 'to facilitate bending or tearing to relieve pressure do. In one embodiment, the intermediate separable separation wall 60 should be less than 1/8 of the wall thickness of the outer wall 24 'or the reactor vessel 12'. The edge of the intermediate separation wall 60, which is not secured to the abutment surface, defines a minimum gap of less than 25% of the reactor vessel 12 'radius. The gap between the edge of the intermediate separating wall 60 and the other wall where the separating wall is not secured reduces the load required to pump the vapor into the reactor vessel 12'and allows the gas product to escape from the reactor vessel 12 ' It must be wide enough to allow thermal expansion to prevent corrosion. Thus, the purging flow from the distributor 42 purges through this gap such that the vapor in the intermediate chamber 64 can not escape to the remainder of the reactor vessel 12 '. In one embodiment, the vapor in the intermediate chamber 64 can escape only through the opening 36 'in the outer wall 24' of the separation chamber 16 '. The opening 36 'allows such a high density catalyst layer 38 to be formed both inside and outside the outer wall 24' of the separation chamber 16 '. The dispenser 66 may dispense the fluidizing gas such as steam into the intermediate chamber 64 to facilitate introduction of the catalyst solids into the separation chamber 16 'through the opening 36'. An additional vent (not shown) is formed in the outer wall 24 'of the separation chamber 16' so that the vapor from the intermediate chamber 64, Into the separation chamber 16 '. Under such a configuration, an inert gas distributor 66 is further required. This vapor from the intermediate chamber 64 entering the separation chamber 16 'will mix with the stripping gas from the stripping section 28 rising through the separation chamber 16' The spent catalyst and the vapor product will rise through the gas return pipe 18 of the separation chamber 16'through the cyclone 32'and out the steam exhaust pipe 50 and the outlet 25. [ However, the gas product from the intermediate chamber 64 will not be allowed to mix in the reactor vessel 12 ', thereby reducing the residence time of the gas product exiting the discharge opening 22 from the reactor conduit 10 . The dip leg 34 'in Figures 2 and 3 is shown as having a counter-weighted flapper valve in that the bottom edge of the dip leg 34' is generally horizontal. Other configurations of dip leg outlets such as vertical or angled outlets may be applied. In this case, trickle valves or angled flapper valves may be appropriate, respectively. (Not shown) for pressure balance between the separation chamber 16 'and the reactor vessel 12' and / or the intermediate chamber 64 in the event of a failure can be provided to the separation chamber 16 ' May be provided in the conduit 18. The vent may include a piping structure in which one end is at a lower level in the reactor vessel 12 'or intermediate chamber 60 and the other end is in communication with the gas return conduit 18. Such a structure may be useful when a side stripper is employed.

Figure 4 is another alternative embodiment of the present invention shown in Figure 1. The elements of Figure 4 having a different configuration from the corresponding elements in Figures 1-3 will be denoted by the double prime symbol ("). The outer separation wall 24" of the separation chamber 16 " Quot; extends about the periphery 36 " In one embodiment, the deep leg 34 "of the cyclone 32" includes an oblique portion and extends into the opening 36 "to deliver gas and solids from the separation chamber 16" The vent portion 72 in the deep leg 34 " is located in the vicinity of the deep leg 34 "from the distributor 42. The vent portion 72 of the deep leg 34 "Quot; function to vent purge gas into the separation chamber 16 "through the opening 34" and aperture 36 ". The embodiment of FIG. Consider sealing the periphery of the leg 34 ". Thus, the deep leg 34 " has vent holes 72 to purgate the outlet of the deep leg and relieve pressure when the device fails. In this embodiment, the deep leg 34 " But has a slip joint to allow for differential thermal expansion. Quot ;, the purge gas will flow through the slip joint to prevent the gas product from escaping into the reactor vessel 12 ". Alternatively, the dip leg 34 " may be completely sealed against fluid communication with the reactor vessel 12 " In this alternative, the distributor 42 and the vent opening 72 may be omitted. In addition, the deep leg 34 " may be provided with a trickle valve < RTI ID = 0.0 & Which may be omitted or another type of discharge valve for the deep leg may be used. The cylindrical extension 70 is defined by the upper and lower walls and the outer cylindrical separating wall 74 connecting the cylindrical separating wall 74 extending to the outer wall 24 "of the separating chamber 16 ".

Figure 5 is an alternative embodiment to an extended separation chamber. Reference numerals in Fig. 5 representing elements having a configuration different from any of Figs. 1 to 4 are indicated by triple prime symbols ('' '). In the embodiment of FIG. 5, the separation chamber 16 '' 'is expanded and separated into an extension 70' '' surrounding the separation chamber 16 '' '. In one embodiment, an annular separation wall 74 '' 'extends diagonally from the outer wall 24' '' of the separation chamber 16 '' 'to engage the shell of the reactor vessel 12' '' Defines an extension 70 '' '. The deep leg 34 '' 'of the cyclone 32' '' has an opening 36 '' 'in the enlarged separation wall 74' '' of the outer wall 24 '' 'of the separation chamber 16' '). Accordingly, the deep leg 34 '' 'omits the oblique portion. In one embodiment, the deep leg is sealed to the separation wall 74 '' 'extended with the expansion joint such that steam from outside the extension 70' '' is removed through the deep leg 34 '' ' And does not flow in or out through the separating wall 74 '' '. Under these conditions, the purge gas from the distributor can be omitted. Alternatively, in another embodiment, although not shown in FIG. 5, it may be desirable to have a distributor of purge gas so that the deep leg 34 '' 'is coupled to the separating wall 74' '' by a slip joint, A vent may be provided at any point in the outer wall 24 '' 'of the separation chamber 16' '' or the gas return conduit 18 to enable the purge gas to pass therethrough. The deep leg 34 '' 'is shown without a discharge valve and extends through an extended separation wall 74' ''. However, a suitable discharge valve can be provided and the deep leg 34 '' 'can be configured not to extend beyond the extended separation wall 74' ''.

Figure 6 shows another embodiment of the present invention. Fig. 7 shows a partially enlarged view of Fig. In Figs. 6 and 7, reference numerals denoting elements having a different configuration from the corresponding elements of Figs. 1 to 5 are denoted by a quadruple prime ('' ''). In this embodiment, the separation chamber 16 '' '' has a receiving tube 78 extending from the outer wall 24 '' '' of the separation chamber 16 '' ''. The deep leg 34 '' '' of the cyclone 32 '' '' extends through the opening 36 '' '' in the separation wall 74 '' '' of the receiving tube 78. The containment tube 78 together define an extension 70 " '" that receives the lower portion of the deep leg 34 "' ". A slip joint is provided in the opening 36 '' '' to permit differential thermal expansion between the deep leg 34 '' '' and the separation wall 74 '' '' of the receiving tube 78. Therefore, the purge gas from the distributor 42 in the reactor vessel 12 " '" is drawn to the inside diameter of the opening 36' '' 'of the separating wall 74' (Not shown). The flow rate of the purge gas from the distributor 42 is such that the purge gas can enter the expansion portion 70 " '' through the opening 36 " '' So that the entrained catalyst and gas can not escape through opening 36 " ''. Alternatively, the deep leg 34 '' '' may be connected to the receiving tube 78 by an expansion joint that eliminates the need for purging the inert gas. In another alternative, the extension 70 " 'includes a single annular portion that includes a plurality of apertures 36 "' " surrounding all or a portion of the separation chamber 16 " .

Claims (10)

An apparatus for separating solid particles from a stream comprising a mixture of hydrocarbon gas and solid catalyst particles, A long reactor conduit (10) in which the hydrocarbon feed contacts the catalyst particles to produce a gaseous product, the long reactor conduit comprising an outlet opening (22); Wherein the outlet 26 of the separation chamber 16 is connected to an inlet 30 of the cyclone separator 32 and a separation chamber 16 for receiving the outlet opening 22 of the reactor conduit, ); And A reactor vessel 12 for receiving a cyclone separator 32 having a gas product outlet 50 and a catalyst dip leg 34, Wherein the deep leg extends into openings (36, 62) in a separation wall (24, 60, 74) separating the volume of the reactor vessel from the volume of the separation chamber, ) Or the separating wall is a wall of the separating chamber (16). 2. The solid particle separation apparatus of claim 1, comprising a distributor (42) in the reactor vessel for distributing a purge gas into the reactor vessel. 3. The apparatus of claim 1, wherein the deep leg extends to an intermediate chamber (64) between the separation wall (60) and the separation chamber, wherein an opening (36 ') is provided between the intermediate chamber and the separation chamber Solid particle separator. 2. The solid particle separation apparatus of claim 1, wherein the separation chamber comprises a stripping section (28). The apparatus of claim 1, wherein the separation chamber includes a return conduit (18) leading to an inlet (30) of the cyclone separator. 2. The solid particle separation apparatus of claim 1, wherein the deep leg (34) comprises a plurality of sections. The apparatus of claim 1, wherein the outlet opening (22) of the reactor conduit (10) is at an end of the vortex tube (14). A method of contacting a hydrocarbon feed with solid catalyst particles and separating the solid catalyst particles from a gaseous product stream comprising a mixture of hydrocarbon gas and solid catalyst particles, Contacting the hydrocarbon feed with the solid catalyst particles in a reactor conduit (10); Passing the hydrocarbon gas product and the solid catalyst particles through the reactor conduit to the separation chamber (16); Separating the hydrocarbon gas product from the solid catalyst particles in the separation chamber; Sending all of the hydrocarbon gas products separated from the solid catalyst particles to a separator 32; Further separating the hydrocarbon gas product from the solid catalyst particles in the separator; Transferring the solid catalyst particles through openings (36, 62) in walls (24, 60, 74) separating the volume of the reactor vessel (12) from the volume of the separation chamber; And Preventing the solid catalyst particles from entering the volume of the reactor vessel ≪ / RTI > 9. The method of claim 8, wherein the solid catalyst particles are transferred directly from the separator to the separation chamber. 9. The method of claim 8, wherein the solid catalyst particles are delivered from the separator to the intermediate chamber (64) and the gaseous products and solid catalyst particles pass between the intermediate chamber and the separation chamber.

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