CN101400511A

CN101400511A - Stripping apparatus and process

Info

Publication number: CN101400511A
Application number: CNA2006800527210A
Authority: CN
Inventors: B·W·赫德里克
Original assignee: Universal Oil Products Co
Current assignee: Universal Oil Products Co
Priority date: 2006-02-13
Filing date: 2006-02-13
Publication date: 2009-04-01
Anticipated expiration: 2026-02-13
Also published as: WO2007094771A1; KR20080098052A; AU2006338298B2; CN101400511B; EP1984172A1; JP5388583B2; KR101279321B1; CA2642032A1; EP1984172A4; AU2006338298A1; CA2642032C; JP2009526632A

Abstract

A baffle-style stripping arrangement for an FCC process has downcomers (66) radially extending from a central axis in a stripping section (32). The baffles (35) may comprise radial sectors (58) with edges (58c, 58d) of adjacent sectors defining downcomers. Each sector may comprise a perforate section (60) and an imperforate section (62). The downcomer section of a superjacent baffle is aligned with the imperforate section of a subjacent baffle to assure horizontal movement of catalyst across the upper surface of the baffle.

Description

Stripper plant and method

Technical field

[0001] the present invention relates to the apparatus and method that catalyst contacts with hydrocarbon streamization.More specifically, the present invention relates to the hydrocarbon of carrying secretly in the catalyst and adsorbing is carried out steam stripped apparatus and method.

Background technology

[0002] have the multiple method that granular materials in small, broken bits is contacted with the charging that comprises hydrocarbon, wherein liquid is maintained at particle under the fluidized state, realizes that solid particle is transported to other stages of process.Fluid catalystic cracking (FCC) is a common examples of this method, and the hydrocarbon in the reaction zone is contacted with pellet type catalyst in small, broken bits.

[0003] the FCC process unit comprises reaction zone and catalyst regeneration zones.At reaction zone, charging and the temperature that remains on rising contact with fluidization solid particle in small, broken bits or catalyst under the suitable normal pressure.Charging and often contacting of catalyst occur in the riser, but also may occur in any feasible equipment, the contact arrangement of for example known short contacting time.Under the situation of riser, mainly be vertical conduit anabolic reaction position, the conduit effluent is emptied to jumbo container handling, and it can be reaction vessel or independent container.Catalyst and hydrocarbon finish substantially in riser that the required time of staying of cracking reaction has only several seconds or still less.Mobile steam/the catalyst stream that leaves riser can perhaps need not directly to enter into separation container through middle separator through the solid-steam separation equipment of riser to the container that is arranged in separation.When not having middle device, when mobile steam/catalyst stream left riser and enters separation container, a large amount of catalyst broke away from from liquid.One or more extra solids/vapor separation devices, cyclone separator always almost is usually located at the inner tip of big separation container.Product is separated from the part of the catalyst still carried secretly by steam flow by cyclone separator, and steam flow is by emitting in cyclone separator and the Disengagement zone.Spent catalyst drops to lower in separation container.

[0004] catalyst constantly circulates to reaction zone from the reaction zone to the renewing zone again.Therefore catalyst is distinguished the media that transmits heat as one from distinguishing to, and necessary catalytic activity is provided simultaneously.During the course can be with any FCC catalyst.Grain diameter is usually less than 100 microns.The catalyst of fetching from the renewing zone is called as " regeneration " catalyst.The catalyst that enters the renewing zone contacts with oxygen-containing gas, and for example air or oxygen-enriched air make the coke burning under this environment.The result has increased catalyst temperature, and a large amount of hot gas streams of removing in the renewing zone are called as flue gas stream.The operating temperature of renewing zone usually at 600 ℃ (1112 ℉) to 800 ℃ (1472 ℉).More operation informations about FCC reaction and renewing zone can be from US 4,541,922, and US 4,541,923, and US 4,431,749, and US4 obtains in 419,221 and US4,220,623.

[0005] in the reaction zone conversion of raw material by temperature, maintain activity of such catalysts in the reaction zone and quantity (be catalyst-oil plant than) control.The most frequently used adjusting method of temperature is to adjust catalyst flow to reaction zone from the renewing zone speed in the reaction zone, regulates catalyst-oil plant ratio simultaneously.In other words, if want to improve conversion ratio in the reaction zone, will increase catalyst flow to reaction zone from the renewing zone speed.This causes occurring more multi-catalyst in the oil of the relative equal volume of reaction zone.Because the temperature of renewing zone is apparently higher than the temperature of reaction zone under the normal operation, the catalyst ratio increase that flow to reaction zone from the renewing zone will cause reaction temperature to improve.

[0006] chemical composition of the charging in FCC apparatus and structure can influence the amount of coke that deposits on the catalyst in the reaction zone.Usually, ratio hydrocarbon in molecular weight, Conradson carbon value, heptane insolubles and the charging is big more, and the coke level of spent catalyst is high more.Bigger conversion ratio has also increased the coke level of spent catalyst.In addition, high-load in conjunction with nitrogen, for example derive from the oil of shale, can increase the coke level of spent catalyst.Handle heavier feedstocks, as oil (being commonly referred to reduced crude) at the bottom of the atmospheric tower of deasphalted oil or crude oil fractionating device, can cause increasing some or all these factors, and cause the increase of the coke level of spent catalyst.Used herein, term " spent catalyst " is in order to represent to be applied to reaction zone and will to be transferred to the renewing zone to eliminate the wherein catalyst of the coke of deposition.This term does not plan to represent that catalyst granules loses catalytic activity fully.Term " used catalyst " is identical with the implication of " spent catalyst ".

[0007] hydrocarbon vapour that great majority contact with catalyst in the reaction zone separates from solid particle by collision and/or centrifugation method in reaction zone.Yet the catalyst granules that uses in the FCC method has big surface area, and this is because in the particle a large amount of holes is arranged.Therefore, catalyst material remains on hydrocarbon on the inside and outside surface of hole when entering stripping zone and between each catalyst granules.Though the hydrocarbon quantity that each catalyst granules keeps is considerably less, normally used a large amount of catalyst and high catalyst cycle rate in the modern FCC process, the result is that a large amount of hydrocarbon and catalyst are removed from reaction zone.

[0008] therefore, common way was removed before spent catalyst enters the renewing zone or strip, hydrocarbons.It is high more to enter in the spent catalyst of regenerator hydrocarbon concentration, can increase the burning load of relative carbon, and cause higher regenerator temperature.Avoid unnecessary hydrocarbon burning to be even more important in heavily charging (the having higher molecular weight relatively) process, because be compared to light charging, handle the coke laydown that these charging meetings increase reacting middle catalyst, and improve the temperature of renewing zone.Improved stripping process produces lower regenerator temperature and the conversion ratio of Geng Gao.

[0009] method of the most frequently used stripping spent catalyst comprises by stripping gas, steam normally, and countercurrent direction is passed mobile catalyst.This steam stripping operation has effect in various degree, has removed the hydrocarbon vapour of carrying secretly and adsorbing from catalyst.At US4, disclose in 481,103 in simple open container catalyst is contacted with the stripping medium.

[0010] baffle plate by using perpendicular separation is so that catalyst passes through stackedly when it moves down in stripping apparatus and contacts with the stripping medium counter flow, and the efficient of stripping catalyst is improved.Moving horizontally catalyst has increased contacting of catalyst and stripping medium, and therefore stripping goes out more hydrocarbon in catalyst.Under this design, catalyst passes through the circuit of a series of baffle plates of different layers through complications.This design has increased contacting of catalyst and gas, wherein by there not being open horizontal path in the effective cross section of stripper plant substantially.The further example of FCC apparatus stripping apparatus appears at US2, and 440,620, US2,612,438, US3,894,932, US4 is in 414,100 and US4,364,905.These documents embody typical stripping container design, and it contains the stripping container, a series of outer baffles that catalyst inwardly are directed to the frusto-conical portion form of Internal baffle.Internal baffle is positioned at the center of circular cone or frustum of a cone, and the riser reactors of passing the stripping container by rising supports.Internal baffle moves on to outer baffle outside catalyst is turned to, and vice versa, moves horizontally with promotion.The stripping medium enters below low baffle plate, continues to rise to the back to back baffle plate of the next one from a baffle plate of bottom.The variation of baffle plate comprises as US2, describe in 994,659 behind baffle plate along adding the shirt rim, and US4, the multiple row baffle plate that uses at different baffle layers that shows among Fig. 3 of 500,423.A kind of variation of introducing the stripping medium is embodied in US2, and 541,801, enter some fluidizing gas in the position of many separation.US5,531,884 have shown a kind of improvement of baffle type stripping container, with one or more big vertical catheter combination in the baffle plate, produce the extra catalyst and the circulating path of gas in baffle plate.It also is known concentrating opening at the positive center of stripping baffles.

[0011] baffle plate of the stripping container of FCC apparatus is usually from the horizontal by 45.The baffle plate that tilts guarantees that catalyst drops to next stage from tower tray in the stripping container, can guarantee moving of horizontal direction simultaneously.Yet each takies considerable height owing to the tower tray that tilts, and has just limited the number of trays that can install in the stripping container of certain altitude.Number of trays is many more in the stripping container, and overall performance is just good more.On the other hand, the slope of baffle plate is established a little bit smaller, can be made catalyst accumulate in the baffle plate top, unless the fluidisation on the baffle plate strengthens, this may need to increase the flow of stripping medium.US2002/0008052A1 discloses a kind of stripping baffles of abundant fluidisation.

[0012] US5,910,240 disclose the frustum of a cone stripping baffles, comprise that the catalyst that blade is set to rotatablely move to give decline rotatablely moves.US5,549,814 disclose a kind of stripping container that comprises radially-protruding inverted U lattice from interior riser.The eyelet of " U " type shank can allow the stripping medium pass through.

[0013] WO 91/00899 discloses a kind of stripping container that the horizontal tray of perforation is arranged.Fluidization in the stripping container makes catalyst can only drop to another from a tower tray by the part of the downspout of tower tray (downcomer) separately substantially.Catalyst material has formed dense bed at the top surface of each tower tray, does not have catalyst to spill from the hole of tower tray substantially.This document has also been told about the use deflecting plates, and deflecting plates is on the downspout of the central vertical alignment of ring-type tower tray and the column plate that contains wire netting or bar row.US2001/0027938A1 has also told about horizontal baffle.

Summary of the invention

[0014] has been found that now and provide from the baffle plate center or the radially-protruding downspout of inner conduit, produce generally horizontal movement at the catalyst of the direction at the several angles of baffle surface to stripping container with baffle plate.Therefore, catalyst disperses in each baffle surface level, provides with the more of stripping medium that rises to contact.

[0015] in one embodiment, the present invention includes the device of strip, hydrocarbons from granular materials.Device comprises that a stripping container and at least one stripping container define is used for receiving the particle that comprises hydrocarbon and the stripping liquid extracted out from the stripping container and the mouth of steam stripped hydrocarbon.In at least a portion of stripping container, a plurality of stripping baffles are vertically separated.One comprises at least three downspouts that radially extend from the vertical center of stripping container in a plurality of baffle plates.The a plurality of perforates that are scattered here and there of at least a portion on the surface of a stripping baffles.At least a liquid inlet is transported to stripping liquid below the stripping baffles, with strip, hydrocarbons from particle.Device comprises that at least one particle outlet is used for reclaiming steam stripped particle from stripping baffles.

[0016] in another embodiment, conduit extends through the stripping container, downspout from described catheter drive to extension.

[0017] in further embodiment, the present invention includes a kind of from particle the method for strip, hydrocarbons.This method comprises the container of the particle that contains hydrocarbon being sent into the stripping baffles that contains a plurality of perpendicular separations.One comprises the downspout that radially extends from the stripping container center in a plurality of baffle plates.Downspout is by relative uneven side restriction.The a plurality of perforates that are scattered here and there of at least a portion on the surface of a stripping baffles.This method further comprises stripping liquid is transported to below the stripping baffles, with strip, hydrocarbons from particle.Reclaim stripping liquid and steam stripped hydrocarbon from container, collect steam stripped catalyst from container.

[0018] therefore, the objective of the invention is to improve the steam stripping efficiency of Flapper type stripping container.

[0019] another object of the present invention embodies in embodiment and the details specific embodiment below.

Description of drawings

[0020] Fig. 1 is the front view schematic diagram of FCC reactor of the present invention.

[0021] Fig. 2 is the amplification fragmentary, perspective view of stripping section of the present invention among Fig. 1.

[0022] Fig. 3 is the sectional view of 3-3 part among Fig. 2.

The specific embodiment

[0023] at first look at the more details of the FCC method that the present invention may use, the typical feed of FCC apparatus is a gas oil, as light or vacuum gas oil (VGO).Other petroleum-derived feed streams of FCC apparatus can comprise hydrocarbon or the heavier hydrocarbon such as the mixture of reduced crude oil of diesel boiling range.The boiling point of the charging of being made up of hydrocarbon mixture preferably more than 230 ℃ (446 ℉), more preferably more than 290 ℃ (554 ℉), measure with suitable ASTM method by boiling point.Usually will handle heavily charging for example the FCC type device of atmospheric depressurized crude oil be called residue crude product cracking unit or slag oil crack unit.Method and apparatus of the present invention can be used for FCC or residue cracking operation.For simplicity, the other parts of specification are only mentioned the FCC method.

[0024] reaction zone of FCC method, it is called as " riser " owing to being extensive use of vertical tube-shaped catheter or pipeline, remains under the hot conditions, and general temperature is higher than 425 ℃ (797 ℉).Preferably, reaction zone remains under the cracking conditions, and temperature is at 480 ℃ to 590 ℃ (896 ℉ are to 1094 ℉), and pressure arrives 500kPa (9.4 to 72.5psia) 65, but preferably less than 275kPa (39.9psia).Catalyst is to the ratio of oil, based on the catalyst that enters the riser bottom and the weight of hydrocarbon, can be high to 20:1 but preferably at 4:1 between the 10:1.Hydrogen can not join riser usually, is prior art though add hydrogen.Sometimes, steam can be sent into riser.The mean residence time of catalyst is preferably less than 5 seconds in the riser.Catalyst in the process can be selected various industrial available catalyst for use.Catalyst preferably comprises the material based on zeolite, but if desired also can be with old-fashioned amorphous catalyst.

[0025] catalyst regeneration zones preferably is operated under 35 to 500kPa (5.1 to 72.5psia) pressure.The spent catalyst that enters the renewing zone can contain the coke of 0.2 to 15 weight %.The main carbon containing of coke also can contain the hydrogen of 3 to 12 weight %, and sulphur and other element.The oxidation meeting of coke produces common combustion product: water, oxycarbide, oxysulfide and nitrogen oxide.As well known to those skilled in the art, can there be various configurations the renewing zone, regenerates in one or more stages.Further possible variation is possible, finishes regeneration because can use in the renewing zone with dilute phase or the thick fluidized catalyst that exists mutually.Term " dilute phase " is meant that catalyst/gas mixture density is less than 300kg/m ³(18.7lb/ft ³).Similarly, term " thick phase " is meant that catalyst/gas mixture density is more than or equal to 300kg/m ³(18.7lb/ft ³).Typical dilute phase operating condition generally includes catalyst/gas mixture density 15 to 150kg/m ³(0.9 to 9.4lb/ft ³).

[0026] shown FCC apparatus among Fig. 1 with coaxial riser and stripping container.Regenerator vertical tube 16 is exported with the speed under the control of guiding valve 11 catalyst from regenerator 10.Fluidizing agent in the nozzle 17 makes catalyst upwards by riser 14 with relative high density, injects charging in the stream of a plurality of feed injection nozzles 15 (only having shown) at catalyst granules.Consequent mixture continues upwards by riser 14, tangentially emits gas and mixture of catalysts up to pair of separated arm 21 from the top 19 of riser 14, passes mouthfuls 29 and enters separation container 23, realizes that gas separates from catalyst.Transport catheter 22 comprises steam stripped hydrocarbon, stripping medium and the catalyst of carrying secretly with hydrocarbon vapour, is transported to the one or more cyclone separators 24 in the separation container 12, and spent catalyst is separated from hydrocarbon vapor stream.Collecting chamber 25 in the separation container 12 is collected cyclone separator 24 isolated hydrocarbon vapours, enters the fractionation zone (not shown) at last by outlet nozzle 20.Dipping tube 18 is released to separation container 12 low sections in collection space 31 with the catalyst in the cyclone separator 24, at last catalyst and absorption or the hydrocarbon carried secretly is passed the mouth 37 that the wall 39 of separation container 23 limits and enters stripping part 32.Separation container 23 isolated catalyst directly enter stripping part 32.Because separation container 23 comprises stripping part 32, also can be called the stripping container.Stripping part 32 comprises that baffle plate 35 is to promote contacting and mixing of stripping gas and catalyst.Baffle plate shown in the figure is a level, but also can be other shape, for example conical butt.Stripping gas is by 33,34 parts that enter the lower of stripping part 32 that enter the

mouth.Inlet

33,34 can be supplied with stripping gas one or more distributor (not shown)s, thus around baffle plate 35 distributing gas.Spent catalyst passes reactor conduit 36 and leaves stripping part 32 and enter regenerator 10.

[0027] regeneration gas, for example compressed air enters regenerator 10 by conduit 30.Air sparger 28 is at the cross section dispersion air of regenerator 10, at this air contact spent catalyst.Coke is removed from catalyst by the burning of carrying out with oxygen from air sparger 28.Combustion by-products and unreacting gas composition rise, and enter the inlet of

cyclone separator

26 and 27 by regenerator 10 with the catalyst of carrying secretly.The gas of catalyst-free is collected in inner room 38 relatively, and it is communicated with the gas vent 40 of removing the inefficacy regeneration gas from regenerator 10.

Cyclone separator

26,27 isolated catalyst fall from discharge legs (discharge leg) 42,43, get back to the bed 44 of regenerator 10 lowers.

[0028] Fig. 2 shows the amplification fragmentary, perspective view of stripping part 32 among Fig. 1.Fig. 2 partly is excluded or opens so that stripping part 32 of the present invention to be described fully.Spent catalyst passes the upper end 23a of separation container 23 or the mouth 37 of collection space 31 enters stripping part 32.Steam stripped hydrocarbon and stripping medium leave from the top of separation container 23.Each baffle plate 35 in the stripping part 32 is supported by cantilevered support structure 50.Cantilevered support structure 50 can comprise excircle band 52 and inner periphery band 54.Excircle band 52 is connected on the inner periphery band 54 to extension rod or the spoke 56 that excircle band 52 stretches out from inner periphery band 54.The two ends of each spoke 56 are fixed on excircle band 52 and the inner periphery band 54.Excircle band 52 is connected to the wall 39 of the separation container 23 that comprises stripping part 32, and perhaps inner periphery band 54 is connected to the wall 13 of the riser 14 of the remainder that extends through stripping part 32 and separation container 23.Do not comprise internal riser in the stripping part 32 in one embodiment, spoke can resemble and extend through excircle band 52 diameter, and each spoke 56 has only an end to be fixed on the excircle band 52.The other end of spoke 56 and wall 39 have at interval.This embodiment can avoid using necessity of inner periphery band 54.

[0029] each baffle plate 35 comprises the part that several have punch block 60 and imperforate section 62.Punch block 60 is made up of the circular open of plate that contains grid or groove.In one embodiment, the opening of baffle plate is big to allowing catalyst granules pass.Imperforate section 62 can be the part of plate that comprises the baffle part 58 of atresia on it, perhaps can comprise the imperforate plate on the punch block 60 of baffle part 58.Each limit of baffle part 58 can comprise downward skirt-type wall 64.In one embodiment, all contiguous baffle part 58 are at interval in the distance of unanimity, and the adjacent edge of contiguous baffle part 58 has been decided downspout and downspout part 66.Contiguous baffle plate 35 is with the height setting of alternating direction along stripping part 32.Therefore, the downspout part 66 of top baffle plate 35 is vertically alignd with the imperforate section 62 of top baffle plate 35.With 62 alignment of downspout part 66 and imperforate section and the design that will be close to downspout part 66 skews of baffle plate 35, guaranteed that catalyst passes baffle plate 35 surfaces, particularly baffle part 58 moves horizontally.Although catalyst falls from the opening of the punch block 60 of each baffle part 58, most of catalyst fall from downspout part 66.Therefore, stoped catalyst to pass directly without moving horizontally that all baffle-panels are vertical to be fallen with the porous plate of downspout part 66 vertical alignments of top baffle plate 35.

[0030] in one embodiment, the height that separates between adjacent trays is 31 to 76cm (12 to 30 inches).In another embodiment, the height that separates between adjacent trays is at 61cm (24 inches), but also more preferably difference in height is reduced to 46cm (18 inches) thus in stripping part 32, pack more baffle plates into.If like that, then need nine baffle plates 35 in all baffle plates 35 image patterns 2.

[0031] Fig. 3 is a sectional view of taking from 3-3 among Fig. 2.Fig. 3 shows riser 14 and eight baffle part 58 that constitute baffle plate 35.Each baffle part 58 has internal circle 58a, outer circumferential edge 58b and longitudinal edge 58c, 58d.Internal circle 58a is supported on the top sides 54a of inner periphery band 54, and outer circumferential edge 58b is supported on the top sides 52a of excircle band 52.The arc that internal circle 58a defines is shorter than the arc that outer circumferential edge 58b defines.Imperforate section 62 covers spoke 56, and it is shown in the shade, supports the band of circumference separately 52,54 that is not connected to

wall

39,13 separately.The relative longitudinal edge 58c, the 58d that close on baffle part 58 clamp downspout part 66.Therefore, in one embodiment punch block 60 between downspout part 66.In addition, in one embodiment, imperforate section 62 is between two punch blocks 60 and two downspout parts 66.Skirt wall 64 can be from longitudinal edge 58c, the 58d of each baffle part 58 but is only launched downwards between inner periphery band 54 and excircle band 52.In one embodiment, each baffle part 58, each imperforate section 62 and/or each downspout part 66 are from the center radiation shape extension of stripping part 32.In one embodiment, the relative edge of each baffle part 58, each imperforate section 62 and each downspout part 66 are more more close on the direction at the center of stripping part 32 in the outer rim of nonparallel stripping part 32 than them.

[0032] fall when the downspout part 66 of catalyst from top baffle plate 35, its bump imperforate section 62 is also scattered to downspout part 66 at a certain angle and flatly.Have eight each between two downspout parts 66, exist in the embodiment of baffle part of imperforate section 62, catalyst falls and horizontal dispersion from top baffle plate 35, generally to the direction of 16 angles.

[0033] punch block 60 can comprise the many openings that bore on the plate.In one embodiment of the invention, baffle openings distributes on the entire area of the punch block 60 of baffle plate 35.The spacing of perforation can be designed as wide band and the regional any way that elimination does not comprise the drive access of fluidizing agent on the punch block 60.The distribution in favourable hole can be described as comprising the greatest circle zone of at least one opening among the present invention.Usually, any 0.09m at least ²(1ft ²) circle zone preferably in this zone, have the part that comprises at least one or a plurality of openings.The round zone that is not impaled the hole centering on preferably is no more than 0.05m ²(0.5ft ²).According to this standard, the size of the minimum in the zone must comprise an eyelet to promote sufficient fluidisation.

[0034] in one embodiment, the grid 68 of the opening 70 of qualification can be contained in punch block 60 as shown in Figure 3.Grid 68 can comprise the intersection grid that crosses each other by the elongation band of each elongation band major opposing side.In another embodiment, grid 68 can comprise the elongation band that a row and a series of bars parallel or the composition pattern that are supported on elongation band top extend in parallel.Those skilled in the art know a lot of methods of making punch block 60.Yet in one embodiment, the opening of punch block 60 will be greatly to allowing a large amount of catalyst pass therefrom.This is easy to finish in the punch block 60 that comprises grid 68.Term " a large amount of catalyst " is meant that the catalyst of at least 20 weight % falls from the opening 70 of each baffle plate 35.It is estimated that nearly the catalyst of the 60 weight % opening that passes each baffle plate 35 of the grid 68 that comprises punch block 60 falls usually.The remainder of catalyst falls by the downspout part 66 of each baffle plate 35.In one embodiment, at least 35% zone comprises greatly to allowing catalyst granules and stripping medium by the simultaneously little opening that forms air pocket below reducing baffle plate 35 in the punch block 60.In one embodiment, the stripping medium is not subjected to remarkable resistance upwards to pass through opening mutually.Like this, can be by the stripping medium velocity of opening greater than 0.15m/s (0.5ft/s).Opening size in 1.0 to 1.3cm (0.375 to 0.5 inch) scope is suitable.In addition, steam/kg catalyst (0.5 to 3.0 pound of steam per pounds catalyst) steam ratio of the vapor (steam) velocity of 0.015 to 0.6m/s (0.05 to 2ft/s) and 0.5 to 3.0 kilogram is suitable among the present invention.

[0035] in one embodiment, imperforate section 62 can comprise the shield at 60 tops, punch block that are supported on baffle plate 35.The shield that comprises imperforate section 62 can be fixed to punch block 60.Shield can be supported on punch block 60 in the level land, can comprise the inclined-plane guiding catalyst and the discharging on one or two top.

[0036] in one embodiment, the cross section of stripping part 32 and each baffle plate 35 are divided into the baffle part 58 that eight areas equate.Each baffle part 58 can comprise 36 ° the part open baffle district that contains perforation and

imperforate section

60,62, and 9 ° of wide-open downspout parts 66.In one embodiment, imperforate section 62 constitutes 9 ° of each baffle part 58, and punch block 60 constitutes 27 ° of each baffle part 58.

[0037] in another embodiment, replace by spoke 56 supporting baffle, the interior outer rim of skirt wall 64 can be respectively fixed to excircle band 52 and inner periphery band 54.Be respectively fixed to the wall 13 and the wall 39 of riser 14 after excircle band 52 or the inner periphery band 54.In another embodiment, baffle plate can design in not comprising the stripping container of internal riser 14.Other supporting construction also is acceptable.

[0038] in one embodiment, baffle plate is made of the steel alloy that can bear the hot conditions in the reaction zone.These steel are often corroded, and baffle plate can benefit to limit opening from using plug-in unit and nozzle, and the etching condition that the catalyst circulation that strides across the baffle plate top is caused tolerance is provided.In addition, thus baffle plate often covers one deck refractory material provides additional corrosion resistance.The details of anti abrasive nozzle and refractory lining is that the technical staff in particle transport field is known.

Claims

1, a kind of from granular materials the device of strip, hydrocarbons, described device comprises:

Stripping container (32);

At least one mouthful (29,37) that the stripping container limits is used to receive the particle of hydrocarbonaceous, and extracts stripping liquid and steam stripped hydrocarbon from the stripping container out;

A plurality of stripping baffles (35) of perpendicular separation at least a portion of stripping container, one in described a plurality of stripping baffles comprises at least three downspouts that radially extend from the vertical centre of described stripping container (66);

Be distributed in a plurality of openings at least a portion (60) on one surface in the described stripping baffles; Be used for stripping liquid is delivered at least one liquid inlet (33,34) of one below of described stripping baffles, with strip, hydrocarbons from granular materials; With

Be used to retrieve at least one particle outlet (36) at the steam stripped particle of stripping baffles.

2, the described device of claim 1, its feature further be, (58c 58d) clamps by nonparallel, relative side in described at least three downspouts one.

3, claim 1 or 2 described devices, its feature are that further described one in the described stripping baffles is level.

4, the described device of claim 1,2 or 3, its feature are that further a described baffle plate further comprises imperforate section (62) and punch block (60), and described punch block comprises described a plurality of opening.

5, claim 1,2,3 or 4 described devices, its feature is that further described imperforate section is arranged between two described downspouts.

6, claim 1,2,3,4 or 5 described devices, its feature is that further described punch block is arranged between described downspout and the described imperforate section.

7, claim 1,2,3,4,5 or 6 described devices, its feature is that further conduit (14) extends through described stripping container, a described stripping baffles is at least indirectly by described conduit support.

8, claim 1,2,3,4,5,6,7 or 8 described devices, its feature is that further described stripping baffles comprises grid.

9, a kind of being used for from the method for granular materials strip, hydrocarbons, described method comprises:

The particle of hydrocarbonaceous is sent into container (32), described container comprises the stripping baffles (35) of a plurality of perpendicular separations, one in the wherein said baffle plate comprises the downspout (66) that radially extends from described stripping container center, described downspout is by nonparallel, relative side (58c, 58d) clamp at least a portion district (60) on described one surface in the described stripping baffles a plurality of openings that distribute;

Stripping liquid is delivered to described one below in the described stripping baffles, with strip, hydrocarbons from granular materials;

From described container, reclaim stripping liquid and steam stripped hydrocarbon; And

From described container, collect stripped catalyst.

10, the described method of claim 9 is characterized in that, a described baffle plate comprises at least three described downspouts.