CN1665586A - Method and equipment for separation of catalyst using cyclone in FCC process - Google Patents

Method and equipment for separation of catalyst using cyclone in FCC process Download PDF

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Publication number
CN1665586A
CN1665586A CN02829444.0A CN02829444A CN1665586A CN 1665586 A CN1665586 A CN 1665586A CN 02829444 A CN02829444 A CN 02829444A CN 1665586 A CN1665586 A CN 1665586A
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cyclone
eddy current
mixture
import
wall
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CN100421777C (en
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S·尼维德奇阿尔
D·N·麦尔斯
C·瑙恩海默
T·J·赫皮希
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Honeywell UOP LLC
Universal Oil Products Co
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Universal Oil Products Co
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
    • C10G31/10—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for with the aid of centrifugal force

Abstract

An apparatus and process for the separation of solids from gases in a mixture improves separation efficiency by imparting a swirl motion to the mixture in a first angular direction to centripetally separate the heavier solids from the lighter gases in conduit and orienting the inlet of the cyclone such that trajectory of the mixture is away from the center of the cyclone. The desired trajactory may be gained by imparting an opposite swirling angular direction to the mixture in a separation vessel with respecto to the cyclone or having the cyclone arranged tangentially with the vessel so that the cyclone and separation vessel share a common tangential sidewall. The apparatus and method incorporates a greater proportion of the mixture entering the cyclone into its vortex to further enhance separation between the solids and gases. Further separation efficiency is added by tangentially directing the mixture into the cyclone.

Description

In FCC technology, use the method and apparatus of cyclone separating catalyst
Background of invention
The present invention relates to the separation of particulate catalyst materials from gaseous material in FCC technology.
Being used for solid is known from the isolating cyclone method of gas, and this method is applied in hydrocarbon polymer usually and handles in the industry, wherein beaded catalyst contacts with gas reactant, thereby realize the chemical transformation of air-flow component, perhaps take place with particle that air-flow contacts in physical change.
FCC technology has been represented a kind of example of being familiar with of technology, and this process application air-flow contacts with the trickle shunting of granules of catalyst, produces gas and contacts with intergranular, and this method helps effectively beaded catalyst being separated from the product steam.Downstream filter method or additional tripping device must be removed the granules of catalyst that the FCC unit does not have recovery.The catalyzer that does not reclaim in the FCC technology shows dual loss.Catalyst changeout more, and this has brought and has improved material cost, and catalyst loss can cause the corrosion to upstream device.Therefore, in FCC technology, be very practical with particulate catalyst materials isolating method from gaseous fluid effectively.
The gaseous fluid discharge from FCC reaction tubes beginning beaded catalyst solid separates.The modal method of separating particles solid is entad to separate from air-flow.Knownly comprise entrained solid particulate gas tangential speed, force heavier solid particulate outwards and away from lighter gas, thereby upwards extract gas and collect solid downwards to centrifugal separator.
US-A-5584985 B1 discloses by making raw material and granules of catalyst enter separation vessel from riser tube, makes gas and beaded catalyst produce spiral motion by an arciform, tubulose eddy current arm, realizes the initial sharp separation from the reaction tubes ejecta.The eddy current of material, spiral motion have produced the initial separation of beaded catalyst from gas in separation vessel.Mixture still continues its vortex motion in the process that gas recovery pipe rises.Extract mixture at the effective terminal cyclone of gas recovery, with further separating particles catalyzer from gas.This equipment is called as UOP eddy current separation system (VSS SM).
Cyclone has a tangential entry usually in the outside of cylindrical vessel, cylindrical vessel forms the outer wall of cyclone.The internal surface acting in conjunction of cyclone import and outer wall, the spiral flow path or the eddy current of generation gas material and catalyzer in cyclone.The centripetal acceleration of eddy current outside makes granules of catalyst to the outer side shifting of bucket, and gas material enters the inside of eddy current and finally pass the top outlet and discharge.Heavier granules of catalyst is assembled on the sidewall of cyclone bucket, and finally drops down onto the cyclone bottom, discharge by outlet and dipleg pipe, thereby by the recirculation of FCC unit.
Cyclone is installed in container need keep the gap between cyclone, think that the purpose of installation and maintenance provides enough passages.When in a container more cyclone being installed, the gap between cyclone becomes a prior Consideration.
Therefore, an object of the present invention is to improve in the FCC unit from steam separating particles solid efficient.Another object of the present invention is to use the VSS that has one or more cyclone SMFurther improve this separation efficiency in the FCC unit.Another object of the present invention is to guarantee enough gaps in container containing between cyclone.
The invention summary
Have been found that to adjust and start from separation vessel (VSS for example SM) the angle direction of vortex motion, thereby make its center can improve separation efficiency away from cyclone.This eddy current orientation can be opposite with the angle direction of vortex motion in the downstream cyclone in container for this reason.As long as cyclone import and separation vessel tangentially intersect feasible particle from separation vessel and enter cyclone along the track that is parallel to cyclone import medullary ray, even identically in the container also can reach identical purpose with the direction of eddy current in the cyclone.Work as VSS SMAnd cyclone import consistent with the vortex motion in the cyclone is not when tangentially receiving mixture, at the mixture that enters cyclone with mixture is produced between the outer wall internal surface of vortex motion can produce less contact.On the contrary, mixture trend contact cyclone center (it comprises the import of leading to gas outlet tube).Therefore, some enter the mixture of cyclone can discharge cyclone before it accepts vortex motion that outer wall produces, and was only to discharge cyclone under the further isolating situation of minimum degree at solid particulate from gaseous state smog.The fluid that comes out from container by guiding makes it be parallel to the outside direction of cyclone import medullary ray, and the cyclone outer wall is easier gave the mixture vortex motion before mixture contact cyclone center.Therefore, produce higher separation efficiency.In order to realize the common orientation of eddy current angle in container and the cyclone, the cyclone import need tangentially be connected with container, obtains the direction that desired mixture enters cyclone thereby make.When the vortex motion direction is opposite in cyclone and the separation vessel, with respect to separation vessel radially or the orientation of tangential cyclone can make mixture enter cyclone with desired direction.In order to make vortex motion reverse, VSS SMLocated an eddy current arm, made the opening of eddy current arm end be angle ground towards the cyclone inlet wall that is connected with the curved wall of cyclone.By this way, VSS SMThe direction that eddy current arm outlets direct mixture enters cyclone outer wall or the connected surface of cyclone import.By reverse vortex motion, the import of tangential tectonics cyclone and cyclone eddy current upstream one side and VSS SMEddy current and and cyclone downstream and VSS SMEddy current import opposite side can further be raised the efficiency.
Therefore, one embodiment of the present invention are the methods that are used for the fluid catalystic cracking of hydrocarbon material.This method enters reaction tubes with hydrocarbon material and solid catalyst particle transmission, thereby produces solid catalyst particle and gaseous state fluidic mixture.In separation vessel, make described granules of catalyst and gaseous fluid direction generation eddy current at an angle, thereby reduce the granules of catalyst concentration in the described mixture and improve gaseous fluid concentration.Container makes mixture pass the cyclone import from container and tangentially enters at least one cyclone, wherein has a upstream side and a downstream side the angle direction of cyclone import eddy current in container.According to the present invention, the eddy current of this angle direction is thrown into cyclone import with mixture with tangential direction, and the tangent line of the container that penetrates from the point of crossing between upstream cyclone import and the container is to be parallel to the cyclone import or to inject cyclone away from the direction at cyclone center like this.Can make the opposite or mixture of the angle direction of eddy current in mixture produces eddy current in cyclone angle direction and the container coexist in the cyclone mutually or in the container eddy current direction identical but mixture tangentially enters cyclone.
In another embodiment, the present invention is a kind of equipment that is used for the fluid catalystic cracking of hydrocarbon material.This equipment comprises a reaction tubes, and it is used to make hydrocarbon material to contact with solid catalyst particle, thereby produces solid catalyst particle and gaseous state fluidic mixture.Described reaction tubes has an eddy current outlet, and its outlet is configured to make solid catalyst particle and gaseous fluid to produce eddy current at first angle direction in separation vessel.The cyclone that is communicated with described eddy current outlet has eddy current and produces outer wall and cyclone import, and wherein eddy current generation outer wall makes solid catalyst particle and gaseous fluid produce eddy current with second angle direction, and the cyclone import tangentially extends through tangential wall from outer wall.The cyclone import intersects with container, thereby makes the first direction eddy current that mixture is injected cyclone with the direction that is parallel to or point to cyclone import tangential wall.Reaction tubes can have a bent tube form eddy current arm that is connected with reaction tubes, and this eddy current arm has a curved outer wall, and wherein the angle direction of eddy current arm is opposite with the angle direction of cyclone outer wall.
The accompanying drawing summary
Fig. 1 is the unitary cross sectional representation of FCC.
Fig. 2 is the cross-sectional view of Fig. 1 along the A-A intercepting.
Fig. 3 is the cross-sectional view of Fig. 1 along the B-B intercepting.
Fig. 4 is the partial view of Fig. 2, shows the flow trace of particulate material when vortex motion is identical.
Fig. 5 is Fig. 1 another cross-sectional view along the B-B intercepting.
Fig. 6 is the partial view of Fig. 2, shows the flow trace of granulated material when vortex motion is opposite.
Fig. 7 is Fig. 1 another cross-sectional view along the A-A intercepting.
Preferred implementation
Fig. 1 is the unitary synoptic diagram of FCC, and it is the basis of several embodiments as an illustration.A-A intercepting two selectable cross-sectional views, i.e. Fig. 2 and Fig. 7 from Fig. 1.In addition, from part B-B intercepting two selectable cross-sectional views, i.e. Fig. 4 and Fig. 6.This FCC unit is included in the separating device in the reaction vessel 10.In the typical FCC unit, the conduit of riser reactor 12 forms extend up through reaction vessel 10 than lower part.Pipe core or riser reactor 12 be vertical orientation in reaction vessel 10 preferably, and can extend up through the bottom of reaction vessel or extend downwards from the top of reaction vessel.Form with eddy current arm 14 stops riser reactor 12 in the eddy current exit in separation vessel 11.Eddy current arm 14 is curved tubes, and it has the axis of bending (referring to Fig. 4) that is parallel to riser reactor 12.Eddy current arm 14 also has an end that is connected with riser reactor 12 and another comprises the opening end of discharge outlet 16.Eddy current arm 14 is discharged the gaseous fluid mixture that comprises crackate and solid catalyst particle by discharge outlet 16.Gas and catalyzer have produced the eddy current spiral motion from the tangential discharge of discharge outlet 16 near the inwall of separation vessel 11.The centripetal acceleration relevant with spiral motion impels heavier granules of catalyst to the componental movement of separation vessel 11 than the outside.Assemble in the bottom of separation vessel 11 from the granules of catalyst that discharge outlet 16 is discharged, thereby form fine and close catalyst bed 17.Have than the easier change direction of the gas of solid catalyst particle less dense, and begin upwards spiral, gas finally passes an import 20 and enters gas recovery pipe 18.Pass the granules of catalyst that gas that import 20 enters gas recovery pipe 18 contains light weight usually.Import 20 is reclaimed from discharge outlet 16 expellant gas and the gas stripping gas of discharging from stripping section 27.The carrying capacity that enters granules of catalyst in the gas of gas recovery pipe 18 is often less than 16kg/m 3(1lb/ft 3), usually less than 2kg/m 3(0.1lb/ft 3).The vortex motion that is produced by eddy current arm 14 continues upward through gas recovery pipe 18 with identical angle direction.Gas transfer after gas recovery pipe 18 will separate is gone into cyclone 22, and this cyclone is further isolated the granules of catalyst material in the gas from gas recovery pipe 18.Cyclone 22 portion within it produces vortex motion, thereby sets up one from gas delivery solid eddy current.There is not the product gas flow of granules of catalyst to pass vapor outlet port 24 comparatively speaking and outlet pipe 49 is discharged from cyclone 22.Product gas flow is passed outlet 25 and is discharged reaction vessel 10 then.The granules of catalyst that reclaims from cyclone 22 passes hopper 19 and dipleg 23 is discharged from the bottom of cyclone, and pass to reaction vessel 10 than lower part, form fine and close catalyst bed 28 in this outside at separation vessel 11.Catalyst solid in fine and close catalyst bed 28 passes window 26 and enters stripping section 27.Catalyst solid transmits downwards by stripping section 27.Gas is carried fluid, steam especially, pass at least one divider 29 enter stripping section 27 than lower part.Catalyzer continue downwards to move pass separation vessel 11 in, catalyzer with pass a series of gas and carry the gas of flow deflector 21 and put forward the fluidic counter current contact gas is discharged from catalyzer.Pass conduit 31 from the catalyzer of stripping section 27 and enter catalyst regenerator 37, this catalyst regenerator makes catalyzer contact with the high temperature oxygen-containing gas, thereby takes regenerated catalyst by the sedimentation of coke on oxide catalyst surface.After the regeneration, granules of catalyst passes the bottom that conduit 33 enters riser reactor 12, and the fluidizing gas of discharging from divider 35 is passed riser tube 12 with granules of catalyst pneumatic the transporting that make progress herein.When the mixture of catalyzer and carrier gases continues to move upward in riser tube 12, nozzle 40 sprays raw material in catalyzer, contacting of catalyzer and raw material makes material gasification, thereby produces extra gas, and these gases pass discharge outlet 16 with aforementioned manner and discharge.
Fig. 2 is by the cross-sectional view more detailed description cyclone 22 along the part A among Fig. 1-A intercepting.Each cyclone 22 comprises radially a cyclone import 30 and a tubbiness cavity 32.The vapor outlet port 24 that is configured in tubbiness cavity 32 centers is discharged from cyclone 22 for the product gas of the micro-particulate material of only carrying under one's arms outlet is provided.The same as the description of being correlated with Fig. 1, hopper 19 discharges particulate material to fine and close catalyst bed 28 from cyclone 22.Radially cyclone inlet 30 forms the tangential wall that this long straight sidewall provides cyclone to enter the mouth by long straight sidewall 34.Sidewall 34 preferably has continuous gradation section 34a, and it provides continuous bend to outer wall 38.One short straight sidewall 36 blocks curved outer wall 38 shrilly at sudden change section 36a place, and curved outer wall 38 forms the tubbiness cavity 32 of cyclone 22.Radially cyclone import 30 is radially led to cyclone 22 from gas recovery pipe 18.The radially essential characteristic of outlet of leading to cyclone from gas recovery pipe 18 is to leave gas recovery pipe 18 at it, and the transversely cutting radially center line " C " of cyclone inlet 30 runs through the cross-section center of gas recovery pipe 18 basically.In operational process, the mixture of gas and particulate material leaves the radially cyclone inlet 30 that gas recovery pipe 18 enters cyclone 22.Long straight sidewall 34 and curved outer wall 38 form a continuous surface, and it enters the mixture spiral motion of cyclone 22, thereby produces eddy current, and particulate material is separated from gas.
The bending direction of eddy current arm 114 as shown in Figure 3.Pass reactor riser 12 mixtures that rise, that comprise particulate material and air-flow and pass eddy current arm 114 and leave riser reactor 12, discharge from discharge outlet 16 spirals with the clockwise angle direction.When mixture leaves separation vessel 11, and when being conveyed through gas recovery pipe 18, mixture keeps the identical vortex motion of clockwise angle direction.
Fig. 4 shows the situation that the particulate material 50 of radially discharging gas recovery pipe 18 enters cyclone 22.For simplicity, Fig. 4 only shows a cyclone.Has the vortex motion that the eddy current arm 14 of bending direction as shown in Figure 3 makes the mixture that comprises particulate material 50 produce clockwise angle direction " D " in gas recovery pipe 18.The bending direction of eddy current arm 14 has been determined the angle direction from import to outlet.The vortex motion that straight sidewall 34, transition 34a and curved outer wall 38 make the mixture in the cyclone 22 produce clockwise angle direction " E ".When each eddy current arm 114 has the bending direction identical with cyclone 22, the same with prior art, the clockwise angle direction " D " that they produce in gas recovery pipe 18 and cyclone 22 and the vortex motion of " E ".Therefore, the particulate material 50 that enters cyclone has the trend near vapor outlet port 24, thereby rather than produces desired vortex motion along the internal surface of curved outer wall 38.Therefore, should believe that some particulate materials 50 before the isolating eddy current are discharged particulate material 50 entering by vapor outlet port 24 from gas, therefore reduce gas and the isolating efficient of particulate material.
Tangent line J among Fig. 4 shows the direction of not expecting of mixture flow in the prior art more fully.The tangential ejaculation of the wall of container of the gas recovery pipe 18 that tangent line J begins along the joining L place at sidewall 34 and conduit 18.With respect to the direction of eddy current in the conduit 18, sidewall 34 becomes the upstream side of cyclone import 30.The described structure of Fig. 4 is launched and vapor outlet port 24 corresponding to tangent line J to the center of cyclone 22.
In order to reach purpose of the present invention, Fig. 4 also shows wall of container 34 to 34 ' adjustment.Mobile sidewall 34 34 ' makes point of crossing, upstream L move to a L ' to the position, and wall 34 ' has formed from the tangent line of point of crossing L ' like this, though and do not illustrate, the mobile of import 30 gives the cyclone import 30 1 medullary rays that are parallel to line 34 '.Therefore, the along the line 34 ' tangent line of drawing is not to penetrate to the center of cyclone 22, but is parallel to the medullary ray of cyclone import, and such mixture track that enters then is parallel to the cyclone import.
Direction by eddy current in the container inverted also can reach purpose of the present invention.Fig. 5 shows the bending direction of the eddy current arm 14 of one embodiment of the present invention, and this direction is opposite with the direction of eddy current arm shown in Figure 4, and opposite with the bending direction of cyclone 22.Identical Reference numeral is represented identical parts among Fig. 3 and Fig. 5.Discharge outlet 16 among discharge outlet 16 among Fig. 5 and Fig. 3 is oppositely relative.Therefore the bending direction of eddy current arm 14 is opposite with the bending direction of cyclone 22.Fig. 5 shows four eddy current arms 14.Can use more or less eddy current arm.
Fig. 6 has illustrated the interaction between gas recovery pipe 18 and 22 opposite eddy current angle directions of cyclone.The mixture that discharge outlet 16 is discharged in the eddy current arm 14 of Fig. 5 can be with counterclockwise angle direction " F " eddy current.When mixture rose in gas recovery pipe 18, mixture can continue with the counter clockwise direction vortex motion.But the vortex motion meeting in the cyclone 22 is as shown in Figure 2 carried out with clockwise angle direction " E ".When the mixture that comprises particulate material 50 enters the radially cyclone import 30 of cyclone 22, the moment of momentum sidewall 34 of mixture rather than the center of tubbiness cavity 32.Therefore, the vortex motion that long straight sidewall 34 and curved outer wall 38 can make more mixture produce clockwise angle direction " E " therefore can make more mixture integrate with the eddy current of separating particles material 50 from gas.Heavier particulate material 50 produces eddy current on the curved outer wall 38 of cyclone 22, they finally drop to hopper 19 herein, enters dipleg 23, and finally enters fine and close catalyst bed 28.Eddy current arm 14 make mixture produce eddy current and cyclone with counterclockwise angle direction to make mixture produce eddy current in a clockwise direction be not limiting factor, and the inverse relationship of the vortex motion angle direction that eddy current arm 14 and cyclone 22 are produced is an effective way of avoiding particle to contact with the cyclone centre portions.
Observe particle once more along tangent line mobile track.Fig. 5 shows from the tangent line M of conduit 18 tangential emissions, and this tangent line is initial from a N, and sidewall 36 (being the upstream wall of cyclone import 30 now) intersects with conduit 18 herein.The end of tangent line M points to the outside of import 30, in the face of sidewall 34 and away from the center of cyclone 22.Therefore the end of tangent line M is away from the center of cyclone 22.
Fig. 7 has described another embodiment of the invention, it provides the tangential basically outlet from gas recovery pipe 18 to cyclone, and the vortex motion of the clockwise direction " H " that wherein produces in the vortex motion of the counterclockwise angle direction of mixture " F " and the cyclone in gas recovery pipe 18 is opposite.Fig. 7 regards Fig. 1 another cross section along A-A as.The Reference numeral of each element that the respective element structure with among Fig. 2 of being correlated with import among Fig. 7 is different is that the Reference numeral among Fig. 2 is added 200.Other components identical is still used identical Reference numeral among Fig. 2 and Fig. 7.Corresponding Fig. 1 is shown in Figure 5 along the cross section of B-B with embodiment shown in Figure 7.The vortex motion that eddy current arm 14 makes the mixture that contains particulate material 50 of discharge from riser reactor 12 produce counterclockwise angle direction " F ".When mixture during upward movement, is proceeded the vortex motion of this counterclockwise angle direction " F " in gas recovery pipe 18.Mixture passes cyclone import 230 and discharges gas recovery pipe 18, and wherein cyclone import 230 is tangent with gas recovery pipe 18 basically.Mixture enters each cyclone 22 by tangential cyclone import 230, and cyclone import 230 is formed by long straight sidewall 234 and short straight sidewall 236.Tangent with the cross-sectional profiles of gas recovery pipe 18 basically with the line " I " of short straight sidewall 236 coplanes or conllinear.Short straight sidewall 236 can be arranged on the inside a little position of tangent line, is beneficial to it is welded on the gas recovery pipe 18.This arrangement allows more cyclone 22 is installed in reaction vessel 10, and has bigger gap between each cyclone 22.Long straight sidewall 234 is successive, and has continuous gradation section 234a and a curved outer wall 238 that has formed the tubbiness cavity 232 of cyclone 22.Short straight sidewall 236 has a sharp-pointed section 236a from curved outer wall 238 sudden changes.Pass hopper 19 than those mixtures that enter cyclone 22 and discharge downwards, upwards discharge and pass vapor outlet port 24 than those mixtures that enter cyclone 22 with bigger gaseous state fluid concentrations with larger particle material 50 concentration.Long straight sidewall 234 and curved outer wall 238 make the mixture that enters cyclone 22 produce vortex motion jointly, thereby set up particulate material 50 isolating eddy current from gas.In this embodiment, the vortex motion of the counterclockwise angle direction " F " that is produced by eddy current arm 14 from riser reactor 12 is reverse with the vortex motion of the clockwise angle direction " H " of cyclone 22 generations.Therefore, passing pneumatic outlet 24 together with gas then with respect to its center that at first contacts cyclone 22 discharges from cyclone, particulate material 50 in the mixture easier at first long straight sidewall 234 of contact and/or curved outer wall 238 suffer the vortex motion of eddy current then.Therefore, suffer vortex motion because more most mixture is easier compared with trend cyclone center, so in separation, realized higher efficient.This arrangement by with the direction of the change cyclone of having admitted in the past 22 rather than the direction of eddy current arm 114, the vortex motion of opposite angles direction in gas recovery pipe 18 and the cyclone 22 also is provided.
Example I
Fluid Mechanics Computation (CFD) simulation of FLUENT program has been used in execution, studies the separation efficiency under three set conditions.Supposition is under three set conditions below: minimum catalyst size is 40 microns, and gas density is 2.75kg/m 3, gas velocity is 0.02c.p., and the mixture speed of discharging each eddy current arm is 20.8m/sec, and pressure is 299kPa, and temperature is 549 ℃.
First set condition relates to a kind of model, and wherein the radially cyclone import 30 to cyclone 22 is provided with respect to gas recovery pipe 18 as shown in Figure 2, and eddy current arm 114 is for being provided with as shown in Figure 3.The key of this model is, the angle direction of the eddy current that is produced by the eddy current arm is identical with the angle direction of the eddy current of cyclone 22 generations shown in Figure 4.The CFD simulation shows that in this model, the mixture that enters cyclone 21% is redirected to the center of cyclone, rather than the periphery that is redirected to cyclone embodies loss in efficiency with further divided gas flow and solid.
Second set condition has identical with aforementioned model as shown in Figure 2 cyclone structure.But, the direction of eddy current arm 14 as shown in Figure 5, thereby make the angle direction of the vortex motion that produces by eddy current arm 14 opposite with the angle direction of the vortex motion that is produced by cyclone 22 as shown in Figure 6.This simulation shows, enters in the mixture of cyclone to have only 10% to be redirected to the center of the cyclone that vapor outlet port is set, and can not be redirected to eddy current further to separate.
Example II
Simulate a reaction vessel with five cyclones.The import of cyclone comprises a longwell and a short straight sidewall, and wherein longwell has the transition section towards the curved outer wall of determining the cyclone bucket, and short straight sidewall has sharp-pointed section towards the sudden change of curved outer wall.Long straight sidewall is set to gas recovery pipe tangent basically, and gas recovery pipe transfers to cyclone with mixture from riser reactor.By the eddy current the cyclone, the cyclone import is longer, is 45.7cm (18 inches) for fear of the mixture that enters cyclone from bypass.Each cyclone only is 10.7cm (4.2 inches) in the gap of its maximum separation distance.
In another model, except the length of short straight sidewall only for 32.0cm (12.6 inches) and be set to as shown in Figure 7 with gas recovery pipe tangent basically and aforementioned model similarly five cyclones are fit in the reaction vessel.Therefore, in second model in the bending direction of cyclone and first model the bending direction of cyclone opposite.But in second model, each cyclone is 45.7cm (18 inches) in the gap of its maximum separation distance.Therefore, reverse by the direction that makes cyclone, the gap between each cyclone has nearly improved 300%.Therefore, thus second model except the bending direction that makes cyclone with the opposite raising of the bending direction separation efficiency of the eddy current arm in reaction tubes exit, also improved the handiness that the given number cyclone is installed in reaction vessel.
First set condition relates to a kind of model, and wherein the radially cyclone import 30 to cyclone 22 is provided with respect to gas recovery pipe 18 as shown in Figure 2, and eddy current arm 114 is provided with as shown in Figure 3.This model shows a kind of situation, i.e. the eddy current of the equal angular direction that eddy current arm generation and cyclone 22 are as shown in Figure 4 produced, and cyclone import sidewall is by numeral 34 expressions.CFD simulation shows that in this model, the mixture that enters cyclone 21% is redirected to the cyclone center, thereby rather than be redirected to the cyclone periphery to participate in eddy current further divided gas flow and solid, embody loss in efficiency.
Second set condition has identical with aforementioned model as shown in Figure 2 cyclone structure.But eddy current arm 14 is directed as shown in Figure 5, and the angle direction of the vortex motion that is produced by eddy current arm 14 is opposite with the angle direction of as shown in Figure 6 cyclone 22 vortex motion that produces like this.Simulation shows that the mixture that enters cyclone has only 10% to be redirected to the cyclone center that vapor outlet port is set, and can not be redirected to eddy current further to separate.

Claims (10)

1, a kind of method that is used for the fluidized-bed hydrocracking of hydrocarbon material comprises:
Hydrocarbon material and solid catalyst particle transmission are entered reaction tubes, thereby produce solid catalyst particle and gaseous state fluidic mixture;
In separation vessel, make described granules of catalyst and gaseous fluid direction generation eddy current at an angle, thereby reduce the granules of catalyst concentration in the described mixture, improve gaseous fluid concentration; With
Make mixture pass the cyclone import and tangentially enter at least one cyclone, wherein have a upstream inlet wall and a downstream inlet wall the angle direction of cyclone import eddy current in container from this container,
It is characterized in that the eddy current of this angle direction is launched into cyclone import with mixture with tangential direction, the tangent line of the container that penetrates from the point of crossing between upstream inlet wall and the container is to inject cyclone away from the cyclone center position like this.
2, the method for claim 1 is characterized in that tangent line penetrates along a line that is parallel to cyclone import medullary ray.
3, the method for claim 1 is characterized in that cyclone tangentially receives the mixture that enters the cyclone import from separation vessel.
4,, it is characterized in that the angle direction of eddy current in the separation vessel is opposite with the angle direction of eddy current in the cyclone as any one described method among the claim 1-3.
5, as any one described method among the claim 1-3, it is characterized in that described mixture passes the eddy current arm and discharges from described reaction tubes, thus the eddy current of described generation first angle direction.
6, as any one described method among the claim 1-3, it is characterized in that described mixture is transferred to described container from reaction tubes, described container comprises the gas recovery pipe that directly is communicated with described cyclone.
7, a kind of equipment that is used for the fluidized-bed hydrocracking of hydrocarbon material comprises:
A reaction tubes, be used to make hydrocarbon material to contact with solid catalyst particle, thereby produce solid catalyst particle and gaseous state fluidic mixture, described reaction tubes has an eddy current outlet, and this outlet is configured to make solid catalyst particle and gaseous fluid to produce eddy current at first angle direction;
A separation vessel is used to receive the mixture of discharging from reaction tubes, and keeps the eddy current of this mixture at first angle direction; With
A cyclone that is communicated with described eddy current outlet, described cyclone has an eddy current and produces an outer wall and a cyclone import, wherein eddy current generation outer wall makes solid catalyst particle and gaseous fluid produce eddy current with second angle direction, the cyclone import tangentially extends into the wall of tangential extension from outer wall
It is characterized in that the cyclone import intersects with separation vessel, the first direction eddy current is injected cyclone with mixture with the direction that is parallel to cyclone import tangential wall like this.
8, equipment as claimed in claim 7, it is characterized in that, the eddy current outlet comprises a tubulose eddy current arm, tubulose eddy current arm has an end that is connected with reaction tubes and at the opening of opposite end, described eddy current arm is around the axis bending that is parallel to described reaction tubes, and described cyclone has a curved outer wall; The angle direction of wherein said eddy current brachiocylloosis is opposite with the bending direction of cyclone outer wall.
9,, it is characterized in that the eddy current outlet is arranged in separation vessel as claim 7 or 8 described equipment.
10,, it is characterized in that cyclone import and separation vessel tangentially intersect as claim 7 or 8 described equipment.
CNB028294440A 2002-08-08 2002-08-08 Method and equipment for separation of catalyst using cyclone in FCC process Expired - Fee Related CN100421777C (en)

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PCT/US2002/025396 WO2004014538A1 (en) 2002-08-08 2002-08-08 Process and apparatus for the separation of the catalyst using a cyclone in a fcc process

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WO2012103790A1 (en) * 2011-02-01 2012-08-09 中国科学院工程热物理研究所 Large-scale circulating fluidized bed boiler

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EP1525048A1 (en) 2005-04-27
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AU2002327435A1 (en) 2004-02-25
CA2493684A1 (en) 2004-02-19

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