Abstract:
Apparatus and method are provided for separating and stripping suspensions comprising catalyst particles transported in vapors from the fluid catalytic cracking riser/reactor. Particles are disentrained from vapor in a vortex zone  112  of the primary cyclonic separator  100 . The disentrained particles enter a stripping zone  126 , wherein the particles are contacted with a stripping gas  136  to recover vapors entrained and adsorbed onto the catalyst. The stripping gas  136  enters stripping zone  126  via perforations in the wall of the cyclone  100 . The stripping gas  136  limits the residual catalytic conversion of hydrocarbon vapors and formation of delta-coke on the catalyst. Stripped catalyst is delivered from the cyclone stripping zone  126  via a dipleg  130  connected to a bottom of the cyclone  100 , and enters an FCC stripping vessel. Solids-lean stripping gas and vapors from the catalyst particles are blended with the carrier fluid and discharged from the cyclone.

Description:
BACKGROUND  
       [0001]     This invention relates to recovering particles from a fluid-particulate suspension in a cyclone separator, and subsequently stripping entrained fluid from the particles.  
         [0002]     Cyclonic separation involves separating a mixture of two or more phases, such as for example, suspensions of particulates in a carrier fluid, under a centrifugal force generated by centripetal motion. A cyclone separator, or cyclone, is a mechanical device to perform centrifugal separation of flowing mixed phases. Uses of cyclonic separation methods can include unit operations to purify a phase, to concentrate a phase, to terminate chemical and physical interactions between mixed phases, or combinations thereof.  
         [0003]     Cyclone separation is common in fluid catalytic cracking (FCC) technology where hydrocarbon vapors and particulate catalysts come into intimate contact. FCC processes, which employ catalyst fluidization and hydrocarbon atomization for conversion reactions, require rapid mixing and separation of fluid and solid phases to maintain control over product yields. Developments in cyclonic separation technology have driven FCC technology toward increased catalyst activities; conversely, increases in catalyst activity spur the need for development of higher cyclone efficiencies.  
         [0004]     Achieving high productivity from FCC systems requires methods for the regulation of contact times between the catalyst and the hydrocarbons. Controlling the contact times depends increasingly on rapid cyclonic separation, as contact time is the key to optimizing process yields. FCC systems are designed to operate using typical interphase contact times between 0.2 and 10 seconds, desirably between 1 and 4 seconds.  
         [0005]     In any cyclonic separation of a suspension, some residual carrier fluid will remain entrained with and adsorbed onto the particles, even after the particles have separated and settled out of the carrier fluid. Accordingly, because of high reaction rates in FCC applications, another important consideration of cyclonic separation is the displacement of the residual carrier fluid from the disentrained catalyst particles. This displacement will stop reactions between the catalyst and residual hydrocarbon fluids, helping to control conversion product profiles and to minimize “delta coking” on the catalyst.  
         [0006]     One method of displacing residual fluid from disentrained catalyst particles includes the introduction of a stripping gas, such as for example, air, steam, ammonia, flue gas, or similar gases, to diffuse the residual hydrocarbons away from the disentrained catalyst particles.  
         [0007]     U.S. Pat. No. 3,802,570 to Dehne discloses a cyclonic separation method to stabilize a vortex in a cyclone separator for improved phase separation through reduced re-entrainment of solids.  
         [0008]     U.S. Pat. Nos. 4,455,220 and 4,692,311 to Parker et al. disclose injecting air and ammonia via utility piping into an annulus below the cyclone, and diffusing the gases through a sintered, annular, stainless steel ring into the catalyst bed beneath a vortex stabilizer in the cyclone. The gases are injected at a rate of about 1 to 4 grams of gas per kilogram of catalyst separated in the cyclone.  
         [0009]     U.S. Pat. Nos. 4,502,947 and 4,741,883 to Haddad et al. disclose a method of closing a pathway of FCC-cracked hydrocarbon vapors wherein the catalyst suspended in the vapors exits the FCC riser-reactor and is conducted via an unsealed plenum through a succession of staged cyclone separators in series, wherein the cyclones are mounted in the FCC catalyst-stripping vessel. Stripping gas filling the stripping vessel blends with the suspension through an unsealed annular junction in the plenum, downstream of a first-stage riser cyclone.  
         [0010]     U.S. Pat. No. 4,778,488 to Koers discloses a cyclone separator for removing hot particles of shale, tar sand, or coal from a gas-borne suspension in a pyrolytic retorting process. A pipe manifold is inserted into the bottom section of the cyclone for introducing stripping gas into the dense bed of separated solids.  
         [0011]     U.S. Pat. No. 5,569,435 to Fusco et al. discloses an open-bottomed, diplegless, open-topped cyclone design for receiving a flow of suspended solids from the FCC riser. The design accommodates unsteady state FCC riser conditions, and is said to provide efficient separation of solids. Stripping gas is introduced into an upper section of an FCC catalyst-stripping vessel housing the cyclone. Up to 20 percent of the stripping gas enters the cyclone through the cyclone&#39;s open bottom, and the balance of the stripping gas enters an annular opening in the cyclone duct which discharges vapors from the top of the cyclone.  
         [0012]     U.S. Pat. No. 5,869,008 to Dewitz discloses an open primary cyclone with the lower end of the cyclone inserted into the catalyst bed of the FCC stripping vessel enclosure. A piping manifold is installed within the open cyclone, beneath the surface of the cyclone&#39;s catalyst bed, for injecting stripping gas into the bed.  
       SUMMARY  
       [0013]     The present invention is a self-stripping method and apparatus for particulate separation from a flowing suspension of the particulates in a fluid carrier stream. Stripping is integrated with cyclonic separation to diffuse residual carrier fluid away from particulates as the particulates are disentrained from the suspension. The invention does not require an external source of stripping material, thereby reducing the overall mechanical complexity of the device. The invention can be advantageously employed in a process or system for which the stripping can improve process productivity, selectivity, retention of solids, or the like. In particular, this invention is suited for service in fluid catalytic cracking (FCC) and like processes. The invention facilitates FCC by advancing and accelerating the stripping of hydrocarbon vapors from FCC catalyst particles after the catalytic reactions are completed to the desired extent.  
         [0014]     In one embodiment the invention provides a particle stripping unit for separating particles in suspension with a carrier fluid with a self-stripping disengagement feature. The particle stripping unit includes a stripping vessel having a primary cyclone and an inlet to tangentally feed a particulate-fluid suspension to the primary cyclone. The unit has a cylindrical surface within the primary cyclone to separate a major fraction of the particulates from the suspension and form a central fluid vortex of reduced particulate content and includes a particulate discharge outlet into the stripping vessel from the primary cyclone. The stripping unit includes a plurality of openings in a wall of the primary cyclone for entry of stripping fluid into the primary cyclone from a dilute phase in the stripping vessel; and a fluid discharge line from the stripping vessel, in communication with the vortex of the primary cyclone and sealed against direct fluid entry from the dilute phase.  
         [0015]     The particle stripping unit can also include a stripping zone between the vortex and the particulate discharge outlet. The openings in the wall for entry of the stripping fluid can be located in the stripping zone. The self-stripping cyclone can include a thermal expansion joint in the fluid discharge line. The particle stripping unit can include a stabilizer between the vortex and the stripping zone forming an annular passage between the stabilizer and an interior surface of the cyclone for downward passage of particulates and upward passage of fluid. The inlet can be connected to a fluid catalytic cracking (FCC) riser to receive a suspension of solid catalyst particles in the vapor.  
         [0016]     The invention can include a method of operating the particle stripping unit. The method can include supplying the suspension to the inlet, passing particulates downwardly through a cross-sectional area of a lower portion of the stripping vessel comprising a vertical cylinder at an average flux rate of from 24 to 440 kg per square meter of cross-sectional area per second (5 to 90 lb/ft2s), introducing stripping fluid into the stripping zone openings at an average fluid velocity of from 9 to 90 meters per second (30 to 300 ft/s), and recovering stripped particles from the particulate discharge outlet. The method can further include a cyclone which can include a stabilizer between the vortex and the stripping zone forming an annular passage between the stabilizer and the interior surface of the cyclone for downward passage of particulates and upward passage of fluid. The method can include passing fluid up through the annular passage at a superficial velocity in a range of 0.1 to 5 meters per second (0.4 to 17 ft/s). The solids flux rate can be from 70 to 200 kg per square meter of cross-sectional area per second (14 to 40 lb/ft2s). The superficial fluid velocity in the annulus can be from 0.5 to 1.5 meters per second (1.7 to 5 ft/s), and the stripping fluid opening velocity can be from 37 to 60 meters per second (120 to 200 ft/s).  
         [0017]     In another embodiment the invention provides a method of operating the self-stripping cyclone described above. The method includes: (a) supplying the suspension to the inlet; (b) passing particulates downwardly through a cross-sectional area of a lower portion of the cyclone vessel comprising a vertical cylinder at an average flux rates from 24 to 440 kg per square meter per second (5 to 90 lb/ft2s); (c) introducing stripping fluid into the stripping zone openings at an average fluid velocity of from 9 to 90 meters per second (30 to 300 ft/s); and (d) recovering stripped particles from the particulate discharge outlet. The cyclone can include a stabilizer between the vortex and the stripping zone to form an annular passage between the stabilizer and an interior surface of the cyclone, and the operating method can include passing fluid upwardly through the annular passage at a superficial velocity of from 0.1 to 5 meters per second (0.4 to 17 ft/s). Desirably, the solids flux rate is from 70 to 200 kg per square meter of cross-sectional area per second (14 to 40 lb/ft2s), the annular superficial fluid velocity from 0.5 to 1.5 meters per second (1.7 to 5 ft/s), and the stripping fluid opening velocity from 37 to 60 meters per second (120 to 200 ft/s).  
         [0018]     In a further embodiment, the invention provides an FCC unit including an FCC stripper vessel, a self-stripping primary cyclone disposed within the stripper vessel to separate catalyst from the FCC riser effluent and form a catalyst-lean stream of hydrocarbon vapors, and a catalyst stripping bed in a lower end of the FCC stripper. The vessel can include an inlet to the primary cyclone to tangentally supply the FCC riser effluent, a stripping fluid supply to the stripping bed, and a stripped catalyst outlet from the stripping bed through the lower end of the FCC stripper.  
         [0019]     In the FCC unit, the primary cyclone can include a cyclone vessel, a cylindrical surface centrally mounted in the primary cyclone to separate solids from the suspension and form a vapor vortex of reduced solids content, a sealed vapor outlet from the primary cyclone in communication with the vortex, a stripping zone between the vortex and a lower end of the primary cyclone, a solids discharge outlet from the stripping zone through the lower end of the primary cyclone, and a plurality of openings in a wall of the stripping zone for the entry of stripping fluid. The cyclone can also include a thermal expansion joint in the vapor outlet. The cyclone can also include a stabilizer below the vortex forming an annular passage between the stabilizer and an interior surface of the primary cyclone.  
         [0020]     The FCC unit can also include a secondary cyclone stage comprising at least one secondary cyclone downstream from the primary cyclone, wherein the at least one secondary cyclone can be connected in series with the primary cyclone by a sealed plenum including a thermal expansion joint in communication between a vapor outlet from the primary cyclone to a tangential inlet of the at least one secondary self-stripping cyclone. The FCC unit can have a catalyst regenerator that includes a stripped catalyst inlet to the regenerator connected to the solids discharge outlet of the FCC stripper, a distributor to introduce an oxygen-containing gas into the regenerator to regenerate the stripped catalyst, and an outlet from the regenerator to transfer regenerated catalyst from the regenerator to an inlet of the FCC riser.  
         [0021]     In a further embodiment, the invention provides a method of operating the FCC unit. The method can include the steps of: (a) supplying a vapor-solid suspension from an FCC riser to the inlet of the FCC unit described above; (b) passing solids downwardly through a cross-sectional area of a lower portion of the cyclone vessel comprising a vertical cylinder at an average flux rate of from 24 to 440 kg per square meter of cross-sectional area per second (5 to 90 lb/ft2s); (c) passing fluid upward through the cylinder at a superficial velocity of from 0.06 to 3 meters per second (0.2 to 10 ft/s); (d) introducing stripping fluid into the stripping zone wall openings at an average fluid velocity of from 9 to 90 meters per second (30 to 300 ft/s); and (e) recovering stripped particles from the solids discharge outlet. The cyclone vessel can include an annular passage, and the operating method can include passing fluid upwardly through the annular passage at a superficial velocity of from 0.1 to 5 meters per second (0.4 to 17 ft/s). The solids flux rate can be from 70 to 200 kg per square meter of cross-sectional area per second (14 to 40 lb/ft2s), the annular superficial fluid velocity can be from 0.5 to 1.5 meters per second (1.7 to 5 ft/s), and the stripping fluid opening velocity can be from 37 to 60 meters per second (120 to 200 ft/s). The stripping fluid supply can be selected from a source including steam, air, ammonia, a flue gas, or mixtures thereof.  
         [0022]     Another embodiment provides a method for stripping vapor from a suspension of particulates in a carrier gas. The method can include: (a) separating particulates from the suspension in an initial separation zone of a cyclone to form a particulate-rich stream with entrained vapor and a vapor stream lean in suspended matter; (b) introducing a stripping fluid through openings in an exterior wall of the cyclone into a stripping zone below the initial separation zone; (c) passing the particulate-rich stream from the separation zone, through the stripping zone in countercurrent contact with the stripping fluid to remove at least a portion of the entrained vapor, and into a dipleg in communication with the stripping zone; and (d) recovering stripped particulates from the dipleg. The stripping zone can be in fluid communication with the initial separation zone via an annular passage defined by an outside diameter of a vortex stabilizer and an interior wall of the cyclone between the separation and stripping zones.  
         [0023]     The invention can also include a retrofit embodiment providing a method of retrofitting an existing cyclone to a self-stripping cyclone. This embodiment is applicable to existing cyclones that are housed within a pressurized vessel to receive a vapor-solid suspension and separate the suspension into a solids-rich stream and a solids-lean stream, having a lower discharge to pass the particulates into the pressurized vessel, and are connected to a plenum in communication with an exterior of the pressurized vessel to recover the solids-lean stream. The retrofit can include installing a new cyclone bottom to an upper portion of the existing cyclone to provide a stripping zone in communication with the upper portion. The new cyclone bottom can include a dipleg to receive the solids rich stream from the stripping zone and a plurality of openings in a wall of the bottom to introduce stripping fluid into the stripping zone by differential pressure. When the plenum of the existing cyclone comprises an unsealed joint, the retrofit method can include replacing the unsealed joint with a sealed joint. If desired, the new cyclone bottom can include a vortex stabilizer defining an annular passage with an interior wall of the cyclone bottom. 
     
    
     BRIEF DESCRIPTION OF THE DRAWINGS  
       [0024]      FIG. 1  is simplified perspective drawing of a self-stripping cyclone for separating particles from a fluid suspension according to an embodiment of the invention.  
         [0025]      FIG. 2  is a cross-sectional view of the cyclone of  FIG. 1  as seen along the lines  2 - 2 .  
         [0026]      FIG. 3  is a cross-sectional view of the cyclone of  FIG. 1  as seen along the lines  3 - 3 .  
         [0027]      FIG. 4  is a schematic diagram of staged cyclones in series according to an embodiment of the present invention.  
         [0028]      FIG. 5  is a schematic of a self-stripping riser cyclone integrated into a fluid catalytic cracking stripper unit according to an embodiment of the invention.  
         [0029]      FIG. 6  is a schematic of a self-stripping riser cyclone integrated into a fluid catalytic cracking unit according to another embodiment of the invention.  
         [0030]      FIG. 7  is a schematic of a self-stripping riser cyclone integrated into a fluid catalytic cracking unit according to a further embodiment of the invention.  
         [0031]      FIG. 8  is a simplified perspective drawing of an existing open cyclone being modified to a self-stripping cyclone according to an embodiment of the invention.  
         [0032]      FIG. 9  is a simplified perspective drawing of an existing closed cyclone being modified to a self-stripping cyclone according to another embodiment of the invention.  
         [0033]      FIG. 10  is a simplified cross-sectional view of the experimental self-stripping cyclone featuring a 20.3 cm (8 in.) stripping section.  
         [0034]      FIG. 11  is a simplified cross-sectional view of the experimental self-stripping cyclone featuring a 30.5 cm ( 12  in.) stripping section.  
         [0035]      FIG. 12  is a graph showing the effect of upward cyclone stripping steam velocity on stripping efficiency.  
         [0036]      FIG. 13  is a graph showing the effect of inlet loading on cyclone catalyst collection efficiency. 
     
    
     DETAILED DESCRIPTION  
       [0037]     Detailed embodiments of the present invention are disclosed herein. However, it is understood that the disclosed embodiments are merely exemplary of the invention, which can be embodied in various forms. Specific structural and functional details disclosed herein are not intended to be limiting, but are merely illustrations that can be modified within the scope of the attached claims.  
         [0038]     The present invention can be used in a process requiring particulate disentrainment from carrier fluids in a flowing suspension, particularly in systems with a need to quickly heat or cool the separated particles, or to strip the separated particulates of residually entrained carrier fluids. The present invention can accommodate a variety of different applications involving various fluid and particulate phases, fluid mechanics, separation and stripping rates, and contact times.  
         [0039]     With reference to the drawings, wherein like numerals refer to like parts, the embodiment seen in  FIGS. 1-3  shows a self-stripping cyclone  100  for separating catalyst particles from hydrocarbon vapor suspension  102  from a fluid catalytic cracking (FCC) riser. The self-stripping cyclone  100  can include a cyclone vessel  104 , a tangential inlet  106  connected to the riser (not shown), and an inner cylindrical surface  108  to separate catalyst solids  110  and form a vapor vortex  112  of reduced solids content. A sealed vapor outlet plenum  114  at the upper end  116  of the cyclone vessel  104  can communicate with the vortex  112  via a vortex tube  117 . In high-temperature applications such as fluid catalytic cracking, the outlet plenum can typically include a thermal expansion joint  144  to absorb structural strains imposed by thermal expansion of components and piping.  
         [0040]     A conventional stabilizer  118  below the vortex  112  can be used to form an annular passage  120  between the stabilizer  118  and an interior surface of the cyclone vessel  104 . A stripping zone  126  below the stabilizer  118  in the lower end  128  of the cyclone vessel  104  can be in communication with a solids discharge dipleg  130 . A plurality of openings  132  can be provided in a perforated wall  134  of the stripping zone  126  for the entry of stripping gas  136 . A lower portion of the stripping zone  126  can comprise a settling bed (not shown) of the catalyst solids  110  into the dipleg  130 .  
         [0041]     In the operation of the self-stripping cyclone, the fluid/particulate suspension  102  enters the cyclone vessel  104  tangentially and swirls circumferentially against the cylindrical surface of the vessel, forming the vortex  112 . Suspended particulates  110  are immediately driven outward towards the wall  108  by centrifugal force as the gas phase of decreasing particulate loading forms the vortex  112 . From the vortex  112 , the solids-lean vapor  140  can exit via the vortex tube  117  to the plenum  114 .  
         [0042]     Disentrained particulates  110  rapidly concentrate at the vessel wall and pass downward as indicated by flow arrow  122  through the annular passage  120  and stripping zone  126  and into the dipleg  130 . Due to a differential pressure between the exterior and the interior of the cyclone vessel  104 , stripping gas  136  enters the stripping zone  126  through the openings  132  in the wall  134  and passes upwardly as indicated by flow arrow  124  through the annular passage  120  into the vortex  112 . The process vapor is thus quickly diffused away from the particulates  110  into the stripping gas  136  in the stripping zone  126  and/or annular passage  120 . The stripping gas  136  can be air, steam, ammonia, flue gas, or a mixture thereof. In applications other than FCC systems, the stripping fluid can desirably be chosen to be compatible with the particulates to be stripped and the process fluids to be removed from the particulates.  
         [0043]      FIG. 4  shows a two-stage embodiment that can include the primary stripping cyclone  100  connected to the tangential inlet  106  to receive effluent  102  from the FCC riser  146 , as in  FIG. 1 , and a secondary cyclone  148  connected at the tangential inlet  150  to the primary cyclone plenum  114  to receive the solids-lean vapor  140  from the primary cyclone  100 . The secondary cyclone  148  can include a solids discharge dipleg  154  and a vapor discharge plenum  158 . Further cyclone stages can be configured in a like manner for series and/or parallel flow, as is well known in the industry.  
         [0044]      FIG. 5  shows an embodiment of the invention with a primary self-stripping cyclone integrated in an FCC stripper unit  166 . The FCC stripping vessel  168  can house the primary self-stripping cyclone  100  and a plurality of secondary cyclones  148  above a catalyst bed  170 . The FCC riser  146  can be connected to the tangential inlet  106  of the primary cyclone  100 , and stripping gas can be supplied via a conventional distributor  172  near the bottom of the bed  170  above the stripped catalyst discharge dipleg  176 . In this embodiment a sealed discharge plenum  114  from the first-stage cyclone  100  can connect dual tangential inlets  150  to a pair of secondary cyclones  148  configured for parallel flow operation.  
         [0045]     In operation, effluent from the FCC riser  146  flows into the cyclones  100 ,  148 . Fresh stripping gas is introduced at the distributor  172 , percolating upward through the bed  170  to maintain a pressure in the vessel  168  that is greater than the interior pressures in the cyclones  100 ,  148 . The stripping gas flows through the perforated walls  134  of the cyclone  100  (see  FIGS. 1-4 ) to achieve self-stripping as described above. Disentrained catalyst is initially stripped in the stripping zone and annular passage of the cyclone  100 , and then the stripped catalyst is discharged through the dipleg  130  to the bed  170 . Additional catalyst disentrained from the secondary cyclones  148  is discharged to the bed  170  via the diplegs  154 . The cyclone diplegs  130 ,  154  can be sealed in the catalyst bed or can regulate catalyst flow with trickle valves (not shown). Stripping is completed to remove residual hydrocarbons from the catalyst in the bed  170 . A blend of process vapor and stripping gas lean in suspended solids can be recovered from overhead outlet  156 .  
         [0046]      FIG. 6  shows an embodiment of an FCC unit  180 , wherein the stripper unit  166  of  FIG. 5  can be positioned directly over a conventional regenerator  182 . Stripped catalyst can enter the regenerator  182  via the dipleg  176  and the conventional standpipe  184 . An oxygen-containing gas can be introduced via the distributor  186 , and the off-gas can be removed in a manner well known in the industry. Regenerated catalyst can be recirculated to the riser  146  via the transfer line  188  along with a fresh feed stream  190 . Diplegs  130 ,  154  can be sealed in the catalyst bed or alternatively can include with trickle valves (not shown).  
         [0047]      FIG. 7  shows an alternate embodiment of an FCC unit  192  wherein the regenerator  182 A can be offset from the stripper unit  166 A, and the stripper unit can be positioned vertically over the riser  146 , with the riser  146  passing through the stripping bed  170  of unit  166 A. The stripped catalyst can be supplied to the regenerator  182 A via the transfer line  176 A. The FCC unit  192  can be otherwise similar to the unit  180  shown in  FIG. 6 . Additionally, diplegs  130 ,  154  can be sealed in the catalyst bed, or alternatively can include trickle valves (not shown).  
         [0048]     The present invention can be used in a new facility, or it can be implemented as a retrofit in an existing cyclone separator.  FIG. 8  shows the conversion of an existing FCC stripper primary cyclone  210  having an open cyclone design housed within an FCC stripping vessel (not shown). The open cyclone  210  can have a cylindrical wall  212  with an open bottom end  214  and a closed top  216 . The existing cyclone can have a tangential inlet  218 , vortex tube  222 , and discharge plenum  224 . The disentrained catalyst can fall through the open bottom directly into the catalyst bed in the stripper vessel  240 . The cyclone  210  can be equipped with an unsealed junction  228  to allow for entry of the stripping gas and to allow for differential thermal expansion of the plenum  224 .  
         [0049]     To retrofit the existing cyclone  210 , an add-on lower cyclone body portion  240 , as shown in a lower half of  FIG. 8 , can be attached to the bottom  214  of the cyclone  210  by welding the lower ends A-A of cyclone  210  and the upper end B-B of add-on  240  together. If necessary, the existing wall  212  can be cut at the appropriate height to accommodate the add-on cyclone bottom  240 . The dipleg (not shown) can extend an appropriate length into the catalyst stripping bed, which may be higher or lower than the catalyst bed in the operation of the pre-existing cyclone  210 . Similarly, the unsealed junction  228  can be cut out at the lines C-C and replaced with a new thermal expansion joint  260  that can be welded at the lines D-D. The new thermal expansion joint  260  can be sealed to prevent fluid entry or exit along the plenum  224 .  
         [0050]      FIG. 9  illustrates the retrofit of an existing closed cyclone  270  having a cyclone vessel  212 , closed bottom section  274 , closed top  276 , tangential inlet  278 , vortex tube  282 , and unsealed, annular junction  284  connected to the plenum  286 . The existing bottom section  274  can be modified by providing perforations (not shown) as needed in one or more walls. Desirably, the bottom section  274  can be cut at E-E and replaced with the new bottom section  240  as described in reference to  FIG. 8 . The junction  284  can be replaced by removing the plenum  286  defined by lines H-H and installing the expansion joint  260  at D-D. The modified cyclone can receive the stripping gas through the new bottom section  240 . If necessary, a replacement vortex tube  282  can also be installed to accommodate the additional flow volume from the stripping gas.  
         [0051]     In the various configurations and applications of the embodiments described above, a stripping gas can flow through perforations in a lower end of the self-stripping cyclone, as shown for example, in  FIG. 1  as  132 . At steady-state conditions, pressure in the stripping vessel housing the self-stripping cyclone will be higher than the pressure inside the cyclone. The stripping vessel can provide a source of lean stripping gas, and the lower pressure in the cyclone can draw the stripping gas into the cyclone. In FCC applications, the self-stripping cyclone can be operated with downward passage of disentrained particulates in the primary self-stripping cyclone vessel at an average flux from 24 to 440 kg/m2s (5 to 90 lbm/ft2s), desirably from 50 to 290 kg/m2s (10 to 60 lbm/ft2s), and even more desirably from 70 to 200 kg/m2s (14 to 40 lbm/ft2s). The stripping gas and recovered process fluid can flow up through an annular passage into the vortex zone at superficial gas velocities from 0.1 to 5 m/s (0.4 to 17 ft/s), desirably from 0.2 to 2 m/s (0.7 to 7 ft/s), and even more desirably in the range of 0.5 to 1.5 m/s (1.7 to 5 ft/s). The perforations in the lower cyclone wall can be uniformly sized to provide an average stripping gas velocity through the openings of between 9 and 90 m/s (30 and 300 ft/s), more desirably between 27 and 73 m/s (90 and 240 ft/s), and even more desirably between 37 and 60 m/s (120 and 200 ft/s).  
         [0000]     Cold Flow Modeling  
         [0052]     Both stripping efficiency and separation efficiency of the self-stripping cyclone were tested via cold flow modeling. Two different self-stripping cyclone units were utilized for experimental purposes. As shown in  FIGS. 10 and 11 , each experimental cyclone had separation sections with 30.5 cm (12 in.) upper barrels. The first test unit, shown in  FIG. 10 , had a 20.3 cm (8 in.) stripping section  126  with a conical transition  302  between the 30.5 cm ( 12  in.) separation section  100  and the 20.3 cm (8 in.) stripping section  126 . The first test unit had a 10.2 cm (4 in.) dipleg wherein the outlet was submerged below the solids level.  
         [0053]     The second testing unit, shown in  FIG. 11 , had a 30.5 cm (12 in.) stripping section and a 30.5 cm (12 in.) separation section, without any conical transition. In addition, the unit included a 15.2 cm (6 in.) unsealed dipleg with a trickle valve  127 , and an outlet located above the solids level.  
         [0054]     The diplegs of the first and second testing units emptied into a 61 cm (24 in.) stripper vessel, which was connected to a 30.5 cm (12 in.) stand pipe. Dimensions for the two experimental testing units are given in Table 1. A list of the physical and operational differences between the experimental cyclones is given in Table 2.  
                             TABLE 1                           Dimensions of Experimental Self-Stripping Cyclone Units            Cyclone configuration                       Riser pipe (146)   15.2 cm (6 in.)   15.2 cm (6 in.)       Cyclone, separation section (100)   30.5 cm (12 in.)   30.5 cm (12 in.)       Cyclone stripping section (126)   20.3 cm (8 in.)   30.5 cm (12 in.)       Primary cyclone dipleg (130)   10.2 cm (4 in.)   15.2 cm (6 in.)       Standpipe (304)   30.5 cm (12 in.)   30.5 cm (12 in.)       Stripping vessel (306)     61 cm (24 in.)     61 cm (24 in.)                  
 
         [0055]    
       
         
               
             
               
               
             
           
               
                 TABLE 2 
               
             
             
               
                   
               
               
                   
               
               
                 Differences in Self-Stripping Cyclone Configurations 
               
             
          
           
               
                   Fig. 10  Configuration 
                   Fig. 11  Configuration 
               
               
                   
               
               
                 Transition cone between the 
                 Cyclone barrel and stripping section 
               
               
                 30.5 cm (12 in.) cyclone barrel and 
                 have the same diameter 
               
               
                 the 20.3 cm (8 in.) stripping 
               
               
                 section 
               
               
                 Flat transition from bottom of 
                 Conical transition from bottom of 
               
               
                 stripping section to dipleg 
                 stripping section to dipleg 
               
               
                 Stripping grid holes located in 
                 Stripping grid holes located in conical 
               
               
                 horizontal transition 
                 transition 
               
               
                 Dipleg diameter is 10.2 cm (4 in.) 
                 Dipleg diameter is 15.2 cm (6 in.) 
               
               
                 without a trickle valve 
                 with trickle valve 127 
               
               
                 Dipleg submerged in operation 
                 Dipleg not submerged 
               
               
                 Vortex stabilizer located below 
                 Vortex stabilizer located at flange 
               
               
                 transition cone 
                 below cyclone barrel 
               
               
                   
               
             
          
         
       
     
         [0056]     The experimental equipment consisted of a primary self-stripping cyclone  100 , a stripping vessel  126 , two secondary cyclones  150 , a riser  146 , a lateral transition  106 , standpipes  304 , a bag house, a dry air source, FCC catalyst reserves and a supply of tracer gas (such as, for example, helium or carbon dioxide). Instrumentation for monitoring flow and pressure were used in conjunction with an analyzer for measurement of tracer gas concentrations.  
         [0057]     During testing, catalyst was cycled through the system in a closed loop. The catalyst was stored in a bottom hopper of a bag house, and upon initiation, was introduced into the system through an eductor attached to the bottom of the hopper. Air was used for eduction and fluidization of the catalyst in the adjoining lateral section and riser. To evaluate the stripping efficiency of the primary self-stripping cyclone, a tracer gas was injected (as a step change) into the air/catalyst mixture before entering the cyclone. A tracer gas preferentially adsorbed by the FCC catalyst was selected. Upon exiting the riser  146 , fluidized catalyst entered the primary self-stripping cyclone  100  where the initial gas-solid separation was performed. The separated gas, lean in solid particles, exited through the overhead line  114  in the cyclone  100 . A T-junction in the overhead line split the flow into equal volumes for further separation in the secondary cyclones  150 .  
         [0058]     The remaining solids in the primary self-stripping cyclone were supplied to the stripping section  126  of the cyclone  100 . A stripping medium was introduced into the cyclone through a series of orifices in the transition  132  to the dipleg  130 , and used to remove the adsorbed gas from the catalyst particles. After the catalyst was stripped, it underwent further stripping in the stripper, was fluidized, and returned to the test loop at the lateral transition section. Gas supplied to the secondary cyclones  150  was further separated as the remaining gas-lean solids were removed and supplied to the stripping vessel  306  via the secondary cyclone dipleg  154 . The solids-lean gas from the secondary cyclones exited the top of the cyclone and was sent to the bag house. Any remaining particulates were removed from the gas in the bag house and vented.  
         [0059]     To determine stripping efficiency of the primary self-stripping cyclone, three independent variables were identified and tested: cyclone inlet velocity, catalyst circulation rate and stripping section upward velocity. For each variable, a range of data points were selected to provide a representative model of the effect of each variable on the dependent variables. Measurement of cyclone separation efficiency was based on a mass balance of the FCC catalyst, and cyclone stripping efficiency on a mass balance of the tracer gas.  
         [0060]     During testing, the following experimental conditions were employed with respect to independent variables described above. Catalyst circulation rates were maintained at 318 kg/min (700 lb/min), 250 kg/min (550 lb/min), or 136 kg/min (300 lb/min). Cyclone inlet velocity was maintained at 12.2 m/s (40 ft/s), 10.7 m/s (35 ft/s), or 8.5 m/s (28 ft/s). Stripper upward velocity was maintained at 0.2 m/s (0.7 ft/s), 0.18 m/s (0.6 ft/s), 0.15 m/s (0.5 ft/s), 0.12 m/s (0.4 ft/s), or 0.09 m/s (0.3 ft/s).  
         [0061]     Results demonstrated that the primary self-stripping cyclone had high stripping efficiency, while the addition of the stripping functionality to the cyclone had a minimal negative effect on separation efficiency.  FIG. 12  shows that stripping efficiencies of greater than 99.5% were achieved, including at low stripping steam velocities in the cyclone, i.e. 8.5 m/s (28 ft/s). Additionally,  FIG. 13  shows that separation efficiencies of greater than 93% were achieved for the primary self-stripping cyclone. Separation efficiency was greatest at low inlet velocity where greater than 99% separation was achieved.  
         [0062]     The invention is described above with reference to non-limiting examples provided for illustrative purposes only. The metes and bounds of the invention are not to be limited by the foregoing disclosure, which is illustrative only, but should be determined in accordance with the full scope and spirit of the appended claims. Various modifications and changes will become apparent to the skilled artisan in view thereof. It is intended that all such changes and modifications are within the scope and spirit of the appended claims and shall be embraced thereby.