CN1926219A - Down-flow fluidization catalytic cracking device and method - Google Patents

Abstract

An apparatus for downflow fluid catalytic cracking is described, which comprise a regenerated catalyst riser carrying regenerated catalyst and a carrying fluid, those being directed through a crossover section to a distributor that will centrifuge gas and separate catalyst from carrying fluid, the catalyst being directed to a downflow reactor through a distributing basket provided with perforations. The upper part of the reactor is provided with feed injectors, which atomize the feed so that feed vaporization and feed and catalyst admixture is optimized. After the cracking reaction in downflow reactor, reaction products are separated and spent catalyst is directed to stripping and regeneration sections. The FCC process carried out in the apparatus is also described.

Description

Down-flow fluidization catalytic cracking device and method

Technical field

The present invention relates to down-flow fluidization catalytic cracking device and method, this device comprises the regenerated catalyst riser tube, is used for the sparger of described regenerated catalyst, downflow reactor and at the sharp separation element of collection container inside.More particularly, the present invention relates to the apparatus and method of the maximized down-flow fluidization catalytic cracking heavy feed stock of catalytic cracking and valuable product, it utilizes the regenerated catalyst sparger, and this design more is evenly distributed in the catalyzer that contacts with raw material in the reaction zone of downflow reactor.Except described sparger, this device is made as a whole other favourable feature that combines, and these features increase the performance of whole system and final downflow system FCC technology.

Background technology

FCC technology is known.In the more common FCC technology of using riser reactor, catalyzer and hydrocarbon feed upwards flow, and in the FCC technology of using downflow reactor, catalyzer and hydrocarbon feed flow downward.

In riser reactor, because the elevate a turnable ladder that the gasified raw material that rises causes causes solid upwards to flow.But the speed of hydrocarbon steam is lower than the center of close reactor near the wall place.Therefore, catalyzer is slower than moving at the center near reactor wall, thereby causes having at the wall place low resistance path of the hydrocarbon steam that rises on the regional and close center of relatively slowly moving of high catalyst density.Therefore, hydrocarbon steam is mainly by center flow, and catalyzer mainly is positioned near the wall.The gained flow pattern is called as nuclear-ring mode.

In addition, solid catalyst and hydrocarbon steam is upwards mobile relative with gravity in riser reactor, thereby causes rate of catalyst flow significantly to be slower than light hydrocarbon stream speed.Feed rate is that slippage factor is generally about 2-3 with the ratio of catalyst velocity.This causes the catalyzer back mixing, thereby causes the longer catalyzer residence time and undesirable secondary reaction occurs, for example crosses cracking.

Different with riser reactor, downflow reactor does not demonstrate big speed and density of catalyst difference between the center of reactor and wall.In addition because granules of catalyst do not have and the gravity reversal, in these reactors, catalyzer flow and the velocity contrast of hydrocarbon stream between moving less than riser reactor.The slippage factor of downflow reactor is generally about 1.

Therefore avoided back mixing greatly, catalyzer is evenly distributed in the middle of the whole reactor more, and catalyzer and effective duration of contact of raw material in downflow reactor are less than riser reactor.

United States Patent (USP) 5498326 has been instructed catalyst cracking method and relative unit, in two perpendicular and successive reaction zone cracking reaction takes place wherein, raw material is incorporated in first district, it circulates downwards from the top at this, at least a portion of products therefrom is introduced in second reaction zone then, and it circulates in up mode at this.It is believed that in downflow reactor separation is more difficult to be carried out owing to the high density at the reaction medium inner catalyst makes, if will need suitable efficient, then requires specially designed equipment.This is that above row mode carries out isolating reason after reaction.But the duration of contact that this layout is inferred between hydrocarbon steam and the catalyzer is long, and the consequent comes from the known disadvantage of long duration of contact, i.e. thermally splitting, coking etc.Therefore, the situation shown in Figure 2 of this patent shows after downflow reactor 27 internal reactions, inregion intermediate 34, between hydrocarbon steam and the catalyzer be reflected at separate hydrocarbons steam and catalyzer before continue for some time, wherein this separate design takes place in riser tube 35.Therefore, may damage and use the two advantage of dirty and riser reactor, and guarantee that the technical efficiency of the benefit of claiming is quite low.

The method of the short contacting time fluid catalytic cracking heavy oil feed with upflowing catalyzer and oily gasifier and downflow reactor is used in United States Patent (USP) 5468369 (' 369 patent) instruction.The slip of catalyzer make the upper reaches part can effectively mix and transformation efficiency limited, and in downflow reactor, under the situation of catalyst separating minimum, finish cracking.Catalyzer has the Y zeolite content of 25wt%, and total steam residence time was less than 5 seconds.The kind that this patent contains the short contact time reactions device is the detailed description of riser tube and downflow reactor.It is said, slide, therefore not nuclear-ring or similarly mobile formation, the admixture when wherein this keeps them fully and leaves mixing portion at the top in whole reactor owing in downflow reactor, exist hardly.Solid does not have migration, stall, diffusion or becomes piece.Owing to this reason, downflow reactor can not be induced suboptimum kinetics because of radially being separated.

Equally as described in what discuss in US ' 369 patents is the shortcoming of downflow reactor, be that initial catalyzer may be difficult to realize with mixing of oil, this is because in initial zone of action, and gravity plays the effect that reduces solid density, and these are different with the effect of noticing in riser tube.In any case the solid that enters tends to immediately landing downwards and can not reflux or circulation, this may improve initial heat and mass transfer with oil.Very stable and balance if the inlet of catalyzer and oil flows, then this effect is so unimportant.But the small amplitude oscillation of solid density never can really be stablized and be characterised in that usually to the fluidizing efflux of solids, no matter still move all like this in downflow reactor at riser tube.Therefore, in fact the gas-solid mixture in cracking case is made up of the pulse of rich catalyzer of alternative and poor catalyzer, and its variation is quite little.In riser tube, this pulse has influence seldom, and this is because the balance that the oil vapour faster than catalyzer of advancing passes the regional of high and low solid density and experiences catalyzer with the ratio of oil of suitable (on average).On the contrary, downflow reactor does not have the oily running gear from poor catalyst area to rich catalyst area, and vice versa.The oil that enters in the low solids density region will be retained in the density regions of whole reactor, because the too early inactivation of catalyzer causes finally carrying out thermally splitting.Oil in high-density region tended to cracking.Therefore, the product of the ratio of low catalyzer and oil and high catalyzer and the ratio of oil will never " on average " to the correct catalyzer and the product of the ratio of oil.As seeing subsequently in this manual, the present invention is by using the novel regenerated catalyst sparger that improves catalyzer and oily mixing efficiency, special-purpose feed injector and poor catalyzer mutually, thereby overcome this and other shortcoming of downflow reactor.

In addition, should be understood that, ' 369 patents do not realize the target of being claimed, this is because the upflowing internal mix shown in Fig. 2 of described patent partly has following shortcoming: i) by axial mode (this is a kind of out of date pattern) raw material is injected in 115, thereby ii) there is high catalyst content in the feed distribution of hint difference, on the other hand in reactor 100, enter at raw material between moment of reactor 100 and its gasification and exist at interval, therefore exist the huge coking may; Iii), consequently increase cumulative coke on the catalyzer on the other hand too much duration of contact between catalyzer and raw material that reactor 100 domestic demands are considered.

Usually, it is believed that in FCC technology two main DESIGNED FEATURE are in the mixing of raw material decanting point place catalyzer and oil, and the separating of hydrocarbon product and spent catalyst.

About catalyzer and oily mixing, below quote important prior art document.

About catalyzer and oily mixing, the present invention utilizes professional component, the theme of Brazilian patent application PIBR 0101433-1 (herein introducing fully as a reference), described element is the part of regenerated catalyst sparger of the present invention, Fig. 1 according to the application of described Brazil, described element consists essentially of: its diameter is less than the conduit (1) of downflow reactor diameter, the plate (3) of being furnished with equally distributed hole, described plate (3) constitute and to be mainly round shape, axially and vertically to be installed in the bottom of the inner collector/distributor catalyst container (2) of conduit (1).As seeing subsequently in this manual, described element realize up to just below the catalyst distribution optimized of downflow system reactive moieties aspect very useful.

But the element of instructing in PI BR 0101433-1 does not allow to handle the mixture of catalyzer and gas.Catalyzer only can fully distribute by porous plate, and for example the guiding valve of installing from the top of porous plate receives.This has limited this element can only be used for wherein preferably only existing the mobile situation of catalyzer below the regenerated catalyst guiding valve.

Opposite with the limitation of described element, the application can be used for from the catalyzer of riser tube and carries the fluidic mixture, separate suitably then and carry fluid and catalyzer, and in sparger abundant distribution catalyzer, the contact raw material is to make it gasification and cracking.

Catalyzer and oily blended are material gasification on the other hand.About this point, the present invention utilizes the downflow reactor device of the present invention (introducing by reference in its entirety at this) in another isolated plant, this device is as a kind of feed injector of being announced among the WO01/44406A1, described feed injector comprises: two concentric tubes, the atomizing fluids inner conduit of flowing through wherein, and the annular space that liquid raw materials flow forms via the internal surface of the outside surface of inner conduit and outer conduit; The atomization unit of the nozzle that having embarks on journey arranges, wherein delegation has and is connected to atomizing fluids with the central nozzle on the inner conduit, with be connected to supravasal two row or the multirow side nozzle more of external feed, wherein arrange the central nozzle and the side nozzle of atomization unit according to geometry, flow so that the energy of atomizing fluids changes into raw material fully by contact, this causes the atomizing fully of raw material; With the mixing section that the edge that passes through central nozzle forms, the size of wherein said mixing section can prevent formed oil droplet agglomeration.

Claimed feed injector is efficient syringe in WO01/444064A1.The similar effective syringe that is used in combination this feed injector or has herein a dirty technical characterictic that discloses has overcome downflow reactor because the exemplary shortcomings that low slippage factor causes, and described low slippage factor causes in effective duration of contact of mixing zone inner catalyst short.The quick material gasification of guaranteeing by this effective syringe allows cracking reaction to carry out in short duration of contact.

Two patents is second key character having considered in United States Patent (USP) 4514285 and the United States Patent (USP) 5582712 in FCC technology, i.e. the separating of product and spent catalyst after the cracking reaction.

Sharp separation hydrocarbon product and catalyzer are the inevitable outcomes of the short contacting time realized in downflow reactor, and this is that this moment, these benefits may be lost by oversize separating step because make a profit almost nonsensically from the benefit of downflow reactor.

United States Patent (USP) 4514285 has been instructed the catalyst separating method of separating spent catalyst and reactor product and separation regeneration catalyzer and stack gas.This separation method is called as the ballistic system in described patent, promptly wherein utilize momentum by the auxiliary granules of catalyst of gravity to carry out the system that catalyzer and reactor product or flue gas separate and do not need complex apparatus.The equipment that is proposed comprises that section area is towards the open ballistic disengaging zone of stripping zone, so allow catalyzer freely not fall in 20-30 times of scope of reaction zone section area and in its lower end with hindering under influence of gravity.Problem is that catalyzer is discharged into the possibility increase of inferring undesirable thermally splitting and char build-up in the separate part 15 of the container 16 with this high section area ratio.

In addition, the notion of United States Patent (USP) 4514285 does not provide the mixture of handling catalyzer and gas.Only may be by the porous plate catalyzer that fully distributes, the catalyzer that receives of the guiding valve of installing by the porous plate top for example.

United States Patent (USP) 5582712 also relates to fast separating process, and this method comprises that two steps of the spent catalyst that comes from downflow system FCC reactor and hydrocarbon product separate.Should be understood that, when having any unsettled operation in the reactor, use the cyclonic separator of the sealing of described US patent teaches to have problem, wherein said unsettled operation causes efficiency separator to reduce, so owing to the carrying secretly of gas phase with the catalyst suspension reaction causes undesirable cracking reaction excessively, and the heavy catalyst loss is in product fractionation system and utility appliance thereof.

In addition, United States Patent (USP) 5582712 does not have recognized the need to provide the external path of stripper gas.On the contrary, stripper gas is drawn with steam product by conduit.Because the conduit kind of instructing in described patent is the normal pneumatic outlet of cyclonic separator since below point out that this layout will make commercial FCC unit operate.

FCC commercial cyclonic separator is operated under the efficient of 99.995%+.This high efficient is for guaranteeing that unitary operability is even more important.Last in the delivery area, capacity are that the catalyzer of 30 tons of/minute solid particulate form of typical FCC unit circulation of 37000BPD is by the gas/solid separative element.Efficient is that 99.995% element means that daily loss is 2.2 tons to the solid order of magnitude of upstream device.If because of the efficient of any reason cyclonic separator descends slightly, for example drop to 99.985%, then catalyst loss can reach 6.5 tons.Except high catalyzer running cost, owing to equipment scaling, heat exchange capacitance loss, cause pump impaired because of corroding fast, thus cause this quantity can cause circulatory problems.

Therefore, under the external path situation of a small amount of gas (this is owing to pressure surge causes) of not considering stripper gas or escaping from cyclonic separator, may produce loss in efficiency based on the isolating element of cyclonic separator, even it is much higher to compare the embodiment that is quoted.Applicant's laboratory scale and commercial unit test have confirmed this judgement.

On the other hand, applicant's United States Patent (USP) 5569435 and in this reference teaches that all is incorporated herein by reference the separating catalyst particles and the system of reacted hydrocarbon, this system comprises by downwards by outlet with upwards directly leads to the uncovered cyclone separator element that the open no dipleg formula cyclonic separator of large volume separator vessel is formed by the annular space between the concentric pipe.The system that is proposed is applied on the FCC reactor upwards.In this application, described system is used in and carries out the spent catalyst and the sharp separation of reacted hydrocarbon in the downflow reactor.

Therefore, the teach literature of being quoted for the up-flow reactor of FCC technology and downflow reactor improved catalyzer and oil mix and separate spent catalyst/the method and the system of reacted hydrocarbon.But do not have document separately or in conjunction with other document description or hinted layout of the present invention: the regenerated catalyst riser tube, be furnished with catalyst distributor that porous plate allows best radially catalyst distribution, the feed injector of the raw material that allows to be gasified totally and be applicable to that the collection container inside being furnished with no dipleg formula cyclonic separator of downflow reactor system has the downflow reactor of sharp separation element, the application will describe also claimed this device and FCC technology.

Summary of the invention

In a broad sense, according to principle of the present invention, the device that carries out fluid catalytic cracking process in downflow reactor comprises:

A) regenerated catalyst riser tube, wherein the dilute phase of regenerated catalyst upwards arrives catalyst distributor by described regenerated catalyst riser tube;

B) is furnished with porous plate and being used for carries the fluidic autonomous channel of catalyzer in the regenerated catalyst riser tube regenerated catalyst sparger, described catalyst distributor links to each other with riser tube by cross section and then links to each other with downflow reactor by the catalyzer acceleration zone before the mixing zone, described sparger by the centrifugation catalyzer with carry fluid also distribute again catalyzer and carry fluid stream the two in described downflow reactor;

C) be furnished with feed injector at an upper portion thereof with gasified raw material and contact the downflow reactor of descending catalyzer, wherein the bottom of reactor links to each other with the sharp separation element of collection container inside;

D) comprise the collection container of flow velocity separative element, so that sharp separation spent catalyst and the appropriate hydrocarbon gas of having reacted.

Method of the present invention comprise with the regenerated catalyst logistics from carry fluid blended breeding blanket through riser tube and be directed in the catalyst distributor, wherein carry out centrifugal to carrying fluid and catalyzer, and uniform distribution catalyzer and guiding downwards, so that meet with raw material by the feed injector atomizing, wherein when the logistics of described regenerated catalyst provides heat, this raw material is gasified, make catalyzer and raw material at described downflow reactor internal reaction then, in the sharp separation element of collection container inside, separate spent catalyst and the hydrocarbon that has reacted then.

Therefore, the invention provides the device of FCC downflow system reaction, this device is in conjunction with the regenerated catalyst riser tube, described riser tube promotes dilute catalyst and upwards arrives catalyst distributor mutually, wherein combine with the feature of feed injector, the design of the described catalyst distributor that the catalyzer acceleration zone by appropriate designs connects allows best catalyzer to mix with oily.

The present invention also provides the device of FCC downflow system reaction, and this device allows fast and the hydrocarbon that easily separates spent catalyst and reacted, thereby further improves whole processing performance.

The present invention also is provided at low-cost apparatus of the present invention of installing in the existing FCC unit.

The present invention also is provided under the short contact time reaction condition, becomes valuable light hydrocarbon and gasoline fraction to keep the method for coking under acceptable level simultaneously the fluid catalytic cracking of high boiling point hydrocarbon ils under high yield.

Description of drawings

Accompanyingdrawing 1 is the synoptic diagram of apparatus of the present invention.

Accompanying drawing 2 is synoptic diagram of regenerated catalyst sparger of the present invention.

Accompanying drawing 3 is views of the employed feed injector of gasified raw material among the WO01/44406.

Fig. 4 shows the mixing zone that has feed injector.

Fig. 4 A is the synoptic diagram that has the mixing zone of feed injector.

Fig. 4 B is the top view that comprises the end of the plane of porous plate and feed injector.

Accompanying drawing 5 is at the inner sharp separation element of collection container of the present invention, and this is according to United States Patent (USP) 5569435 repackings.

Embodiment

Therefore the present invention relates to fluid catalytic cracking and contain apparatus and method at the hydrocarbon feed oil of 340-720 ℃ of following ebullient liquid hydrocarbon.

One aspect of the present invention is to use the device of downflow reactor catalytic cracking.

A second aspect of the present invention be to use FCC technology that device of the present invention carries out,

Use the device (representing with numeral 100 usually) of downflow reactor fluid catalytic cracking to comprise:

A) carry the regenerated catalyst riser tube 10 that the dilute phase regenerated catalyst upwards arrives regeneratedcatalyst sparger 30;

B) the regeneratedcatalyst sparger 30, it is furnished with thebasket 35 and by being used to carry the autonomous channel of carrying at least two pipelines of fluidic 33 of the catalyzer in the regenerated catalyst riser tube 10 of distributing, describedcatalyst distributor 30 links to each other with riser tube 10 bycross section 20, and link to each other withdownflow reactor 50 by thecatalyzer acceleration zone 37 before the mixing zone 40, describedsparger 30 is centrifugal to be carried fluid and catalyzer and distributes catalyzer in describeddownflow reactor 50;

C) has mixing zone 40 at an upper portion thereof to start thedownflow reactor 50 of catalytic cracking reaction, wherein said mixing zone 40 is furnished with feed injector 41, with the raw material that gasification will contact with regenerated catalyst in described mixing zone 40, the bottom ofreactor 50 links to each other with no dipleg formulacyclonic separator 61 by square-section pipeline 67;

D) is furnished with thecollection container 60 of sharp separation element, so that sharp separation spent catalyst and the appropriate hydrocarbon gas of having reacted.

Incollection container 60, the sharp separation element is furnished with: no dipleg formulacyclonic separator 61, with sharp separation crackene and particle mutually;Outlet conduit 66 is substantially free of the crackene logistics of granules of catalyst and arrives in the distillation system with outflow; With spentcatalyst conduit 65.

Now based on accompanying drawing the component parts of apparatus of the present invention is made following detailed description, these accompanying drawings should not be interpreted as limitation of the scope of the invention.

Fig. 1 has described the notion of device 100 of the present invention.

Therefore, the regenerated catalyst riser tube 10 of Shi Yonging is liquid stream (current) riser tube in this application, because it is to carry the fluidic conduit.

The riser tube 10 that should be pointed out that apparatus of the present invention is not used in and carries out any cracking reaction.On the contrary, it is used to be carried in the RS Regenerator Section dilute phase regenerated catalyst of (not illustrating in the drawings) of regenerating.

According to notion of the present invention, the statement in regenerated catalyst riser tube 10 " dilute phase regenerated catalyst " is meant that in described riser tube inner catalyst mass rate be 50-500kg/ (m²S), and average range be 150-300kg/ (m²S).

The RS Regenerator Section that can be used for the object of the invention is to belong to any commonly used section of any well-known catalysts regeneration techniques.

Regenerated catalyst riser tube 10 allows than by adjusting under flow direction burden more low-cost device of the present invention being installed on the existing unit.

Regenerated catalyst is directed to the bottom of regenerated catalyst riser tube 10 from the regenerated catalyst standpipe (not shown), is carried fluid carry-over at this catalyzer.

The useful fluid that carries is a steam.

Another selection is to use water to substitute steam.Main influence in plan promoting FCC thermal equilibrium is so that revivifier is operated at a lower temperature and when increasing catalyst recirculation, it may be preferred selecting water.In this case, the water from regenerated catalyst reception heat is gasified at decanting point.

Other may be a naphtha stream to carry fluidic.As selecting water, when allowing to enter riser tube, naphtha stream is gasified, thereby serves as heat-eliminating medium.

Moreover method of the present invention comprises according to the availability in the gas compressor (not shown), uses fuel gas as the catalyst entrainment fluid.

Further replacement scheme is the availability according to natural gas stream in refinery, uses natural gas stream.

Being used in combination these logistics with each logistics of any consumption is possible equally.

The fluidisation ring that is positioned at regenerated catalyst riser tube 10 bottoms by use guarantees to carry the fluidic uniform distribution with the radial nozzles (not shown) that is positioned at the top (not shown).

Cross section 20 connects the upper end and the regeneratedcatalyst sparger 30 of regenerated catalyst riser tube 10.

Cross section 20 is round shape or preferred orthogonal part, and it shifts hanging down under the pressure reduction with catalyzer bottom thecatalyst distributor 30 inclinations-separating pipes of the angle that becomes to be enough to avoid undesirable salinization phenomenon with horizontal plane-guarantee.

In addition, thiscross section 20 links to each other withsparger 30, and its position makes catalyst stream enter described sparger along tangent position.

Therefore, the regenerated catalyst as dilute phase is directed in the regeneratedcatalyst sparger 30 throughcross section 20 by riser tube 10.

Fig. 2 shows the details drawing of regeneratedcatalyst sparger 30.

Regenerated catalyst sparger 30 comprises:

Regenerated catalyst and carry fluid and be directed into whereinchamber 31;

At least two are used for carryingfluidic pipeline 33 by regenerated catalyst;

Guiding is treated and the catalyzer that carries fluid separation enters theconical surface 34 of thedistribution basket 35 of being furnished withporous plate 32;

Be connected to thepiston 38 of the vertical sealing atsparger 30 tops, meet curve mode so that flow, limit this zone simultaneously so that catalyzer and carry fluidic speed and can increase, describedpiston 38 further the guiding catalyzer flow and by centrifugal auxiliary separating catalyst with carry fluid;

Thenozzle 36 of injected steam is so that the even and fluid catalyst beds of catalyst content on thebasket 35;

Catalyzer acceleration zone 37, it comprises tapered section and round shape part, thereby allows catalyzer is directed in the mixing zone 40.

Perhaps,sparger 30 utilizes thepiston 38 of sealing to distribute.

According to unitary size, the quantity ofpipeline 33 can change to several from two.Therefore, can use 2,4 ormore pipelines 33.

From regenerated catalyst riser tube 10 carry fluid and mixture of catalysts is directed in the regeneratedcatalyst sparger 30, at this centrifugal described mixture, separate and to carry fluid and catalyzer, then catalyzer is directed in the mixing zone 40.

Thereforedesign catalyst distributor 30 and finish dual role: centrifugal fluid-mixture of catalysts and the uniform distribution of carrying is fed to catalyzer in the mixing zone 40, thereby can realize perfect and instant the mixing of catalyzer and raw material, to guarantee/one second reaction very fast of number under the selective conditions of the best.

According to the present invention, regenerated catalyst enters regeneratedcatalyst sparger 30 by the tangent line pattern.

Speed when in addition, regenerated catalyst enters regeneratedcatalyst sparger 30 is important technical parameters.Minimum velocity remains under the 9.14m/s (30ft/s).Top speed should not surpass 20m/s (65ft/s).

Catalyst distributor 30 receives from the regenerated catalyst of regenerated catalyst riser tube 10 bycross section 20 and carries the fluidic mixture, thus by the centrifugation regenerated catalyst with carry fluid.

Flow throughconical surface 34 and being fed in thebasket 35 that distributes of regenerated catalyst, the described bottom that distributesbasket 35 is furnished withporous plate 32, carry thefluid pipeline 33 of flowing through simultaneously, and in the tapered section ofcatalyzer acceleration zone 37, belowbasket 35, mix in regenerated catalyst, and not to causing any interference by the describedbasket 35 even catalyst distribution that provided with low speed.Described low speed is 3-8m/s (10-25ft/s).

Therefore, when by the centrifugation catalyzer with carry the fluidic mixture, when catalyzer distributes in an ideal way by thebasket 35 that distributes then, in the tapered section ofcatalyzer acceleration zone 37, carry the fluidic low-momentum and be not enough to disturb the catalyst distribution that is obtained.

May damage catalyst stream to thebasket 35 that distributes for fear of thosepipelines 33 onconical surface 34, the shape of describedpipeline 33 is preferably the square-section that is connected on two semi-circular cross-section that are made of half pipeline, thereby cause oblong, rather than simple cylindrical in cross-section.

The cross section ofpipeline 33 can be so that the gas velocity in these pipelines be not more than 20m/s (65ft/s) and the mass velocity of the free space sufficient to guarantee catalyzer that flows at the catalyzer atconical surface 34 places preferably is not more than 500kg/ (m²S).

Optionally, help on thebasket 35 that distributes bynozzle 36 injecting steams and in fluid catalyst beds, make the content of catalyzer even.Part injecting steam (perhaps other the carries fluid)pipeline 33 of flowing through, and cross the distributebasket 35 and thecatalyzer acceleration zone 37 of flowing through with another part of catalyst mix.

Haveseveral nozzles 36 arounddistribution basket 35, the quantity of nozzle is the abundant desired quantity of fluidized catalyst on thebasket 35 that distributes.

The thin helical that the hole that is shaped as theporous plate 32 bybasket 35 of catalyzer/carry fluidic mixture (wherein catalyst distribution is in thecatalyzer acceleration zone 37 of catalyst distributor 30) forms, and descend bycatalyzer acceleration zone 37 40 (collection parts) towards the mixing zone by gravity.

The bore dia of porous plate 32 (wherein each hole is on every side with suitable hardened material) makes the mixing zone 40 below being positioned at realize that easily material jets are penetrated into the catalyzer helical, thereby the perfection of guaranteeing granules of catalyst and raw material contacts.

The OK range of the bore dia ofporous plate 32 is the 20-100 millimeter, more preferably the 40-80 millimeter.It is 250-750kg/ (m that total perforation field can make mass velocity (perhaps mass rate) scope of catalyzer²S), preferred 400-600kg/ (m²S).

The periphery ofporous plate 32 must make its protuberance and the periphery of the end formation of the feed injector 41 that is positioned at 40 belows, mixing zone mate, shown in Fig. 4 B.

These standards can obtain the desired whole advantages of downflow mode, thereby guarantee to be better than thermally splitting and catalytic cracking mainly takes place and fully finish reaction.

Under the impossible situation of piston of theporous plate 32 of thebasket 35 that distributes, catalyzer flows out bypipeline 33, thereby with carrying fluid by the zone around described basket.The size of this zone and gas pipeline is enough to hold whole catalyst recirculation amounts.In the case, may need to prevent this situation by injecting fluidization steam vapors withbasket 35 nozzles that link to each other 36 that distribute.

Because regenerated catalyst distributes by regeneratedcatalyst sparger 30, therefore catalyzer is directed in the mixing zone 40, the feed injection position of thedownflow reactor 50 that described mixing zone 40 is Fig. 1, this reactor is furnished with feed injector 41, described feed injector is the element that atomized feed becomes hydrocarbon drop mist, and its mode is feasible to minimize the gasification time of raw material and optimize catalyzer and oily contacting.

Catalyzer begins to quicken incatalyzer acceleration zone 37 under action of gravity, wherein design describedcatalyzer acceleration zone 37, so that its length is enough to make catalyzer to reach the final velocity of abundant introducing catalyzer to the feed injector 41 raw materials mixed jets by being positioned at 40 places, mixing zone.Described speed can be 1.5-11m/s (5-35ft/s), more preferably 5-8m/s (15-25ft/s).

Regulate the diameter of the round shape part ofacceleration zone 37, to satisfy two conditions: with the descending speed of the fluidic speed of carrying near catalyzer of catalyzer, and the cross section of regulating described cylindrical portions may makes it identical with the cross section of thecatalyst basket 35 that distributes.

Described criteria classification is guaranteed the kinetic energy balancing and the restriction of 40 place's the bests in the mixing zone, described mixing zone 40 combines with the feed injector 41 of the following stated, guarantee unique and best downflow system reaction process, finish up to reaction so that required catalyzed reaction is occupied an leading position.

Fig. 3 shows feed injector 41.

Feed injector 41 is made up of the spray chamber of being furnished with theside nozzle 120 thatcentral nozzle 110 that atomizing fluids uses and liquid starting material use basically.Concentric tubes system transmission atomizing fluids and liquid starting material meet each other flowing of this atomizing fluids and liquid starting material in atomization unit.The positioned opposite of described center and side nozzle will cause the atomizing fully of raw material, promote simultaneously to interact with the best of descending catalyzer.Contact the gasification of promotion liquid starting material with the raw material of finer atomization and the regenerated catalyst of heat, this helps the unitary improvement in performance of FCC.

According to the diameter of downflow system reaction zone, the feed injector of variable number is installed.The quantity of described syringe is the function of reaction zone sectional area, wherein selects the quantity of syringe, so that cover the highest possible sectional area.According to the different heights level of downflow reactor, feed injector can be contained in the single stage or in a plurality of stages.Therefore, can use 2,4,6 or more described syringe.

According to the present invention, can with respect to the horizontal plane feed injector be installed with-30 ° to+30 ° angle.Preferably, with 0 ° to+30 ° angle or negative slightly angle mounting of syringe, and the raw material of atomizing injects with the direction relative with catalyst stream.

The mixing of liquid starting material and atomizing fluids takes place in spray chamber, and wherein the geometrical shape of spray chamber atomizes fully to raw material and plays an important role.

Although should be appreciated that according to the feed injector of describing this particular types to be specially adapted to purpose of the present invention, other efficient feed injector can be used in apparatus and method of the present invention equally.

Fig. 4 A shows the bottom ofsparger 30, and it has the basket ofdistribution 35,hole 32 and thecatalyzer acceleration zone 37 that contains feed injector 41 that links to each other with mixing zone 40, isreactor 50 afterwards.

Fig. 4 B is the top view that comprises the end of the plane of porous plate and feed injector, and wherein dotted line is a protuberance of representing the internal surface in the zone that is covered by the catalyzer helical of theporous plate 32 by thebasket 35 that distributes.

In Fig. 4 B, the definite zone that is covered by material jet of divergence angle β.Unique zone that shadow region 42 representatives are not covered by material jet.In this zone, only may find catalyzer.Determine the surface-area ofporous plate 32 and the sectional area of mixing zone 40, so that minimize shadow region 42.

In addition, to be inserted into the degree of depth in the mixing zone 40 are important parameters to feed injector 41.Therefore, if the wall of too close mixing zone 40, the end of feed injector 41 then will produce the zone that wherein only has raw material and do not have catalyzer.On the other hand, if the end of feed injector 41 far from the mixing zone 40 wall far away excessively, then shadow region 42 will be increased to and exceed desirable border.

Regenerated catalyst fromcatalyst distributor 30 contacts with raw material in the mixing zone 40 ofdownflow reactor 50, thereby provides required heat to come gasified raw material, makes raw material reach temperature of reaction and the heat absorption of desirable cracking reaction is provided.

The diameter of described mixing zone 40 should guarantee that range of gas velocity is 2-15m/s, preferred 5-10m/s.

Downflow reactor 50 is the pipelines that wherein carry out crackingreaction.Reactor 50 has the axle of perpendicular, and is furnished with the feed injector 41 that the introducing raw material is used on the top of reactor.The bottom ofdownflow reactor 50 links to each other with the no dipleg formulacyclonic separator 61 ofcollection container 60 inside by thepipeline 67 of discharging gained crackene and spent catalyst.

By aperture effect to the regenerated catalyst guiding valve, change the internal circulating load of catalyzer, control the temperature out of downflow reactor 50.In order to reach the desirable transform level of establishing in engineering project, this temperature should keep 450-700 ℃.Preferred temperature is 520-570 ℃.

Downflow reactor 50 is preferably operated under the pressure of 1.0-2.0bar.

That uses in regenerated catalyst riser tube 10 carries fluid and will assist hydrocarbon partial pressure and the catalyst temperature that reduces in thereactor 50, and this helps to reduce undesirable thermally splitting side reaction conversely.

The mixture of catalyzer, crackene, steam and the rare gas element carried secretly from the revivifier (not shown) is crossedwhole downflow reactor 50.

Catalyzer is preferably 0.5-5 second with the duration of contact of oil, more preferably 1-4 second and even more preferably 1.5-3 second.

Indownflow reactor 50, the mass velocity of catalyzer (perhaps mass rate) is 50-500kg/ (sm²), more preferably 100-350kg/ (sm²) and even more preferably 150-250kg/ (sm²).

Indownflow reactor 50, carry out after the cracking reaction, produce crackene and spent catalyst, they should be downflow reactor at the no dipleg formulacyclonic separator 61 of the sharp separation element ofcollection container 60 inside and separate in the system of the United States Patent (USP) 5569435 of reequiping.

In Fig. 1, the collection container that comprises no dipleg formulacyclonic separator 61 is represented withnumeral 60.

Fig. 5 showscollection container 60 and inside thereof.

The design of no dipleg formulacyclonic separator 61 allows catalyzer and crackene sharp separation, so that avoid product to cross cracking after reaction zone, minimizes the hydrocarbon amount that is entrained in the stripping zone simultaneously.

The enrichment suspensoid of the lightweight crackene on describeddownflow reactor 50 bottoms dischargings is rich in spent catalyst particles and is adsorbed on catalyzer also is directed to it square-section pipeline 67 that links to each other withdownflow reactor 50, thereby causes that sharp separation gas phase and particle are mutually in no dipleg formulacyclonic separator 61.

No dipleg formulacyclonic separator 61arrival outlet conduits 66 are left in the crackene logistics that is substantially free of granules of catalyst, describedoutlet conduit 66 receives directly from no dipleg formulacyclonic separator 61 and from the described logistics of theconduit 68 that places no dipleg formulacyclonic separator 61 tops, arrives the distillation system (not shown) then.

Collect incollection container 60 bottoms by all catalyzer that no dipleg formulacyclonic separator 61 is separated,fluid injection member 64 keeps catalyzer at describedcontainer 60 bottom uniform distribution simultaneously.

By the fluid ofinjection member 63 purgings from steam supply, thus the stagnation parts of purgingcollection container 60.

Alternatively,element 64 can at first remove the entraining hydrocarbon (stripping) from spent catalyst.

Spent catalyst conduit 65 is carried spent catalyst to additional stripping zone or in the revivifier (not shown).

Implementing replacement scheme of the present invention is when needs, emits the particle and the suspensoid of reaction mixture by thelower part outlet 62 of no dipleg formula cyclonic separator 61.This can improve the collection effciency of solid in collection container 60.Stoping gas stream fromcontainer 60 to enter in processcyclonic separator 61 in, prevent carrying secretly again of granules of catalyst, this is a big problem in the uncovered cyclonic separator of processing.

Account for the discharging hydrocarbon of the effluent 3-20% that reaches distillation system, flow out the top of no dipleg formulacyclonic separator 61 or pass throughconduit 68 fromcollection container 60 with stripping fluid and purge fluid.

In described no dipleg formulacyclonic separator 61, the catalyzer greater than 99% separates with appropriate hydrocarbon gas, and isolating catalyzer leavescyclonic separator 61 and is deposited on the bottom ofcontainer 60 by exporting 62.Gas leavessharp separation container 60 byoutlet conduit 66, and describedoutlet conduit 66 is by the divided gas flow that leavescyclonic separator 61 and the gas feed of carrying byconduit 68.

Device 100 of the present invention can use with the sharp separation system of other prior art, therefore the invention is not restricted to the sharp separation system of collection container shown in Figure 5 60 inside.

The sharp separation that carries out incollection container 60 avoids hydrocarbon to cross cracking.In case the hydrocarbon gas is mutually separated with catalyzer mutually, then gas phase is directed in the product distillation system (not shown), and spent catalyst is directed in the stripping container (not shown).

The spent catalyst that reclaims coke (coke is the result of catalyzed reaction) that is deposited onsharp separation container 60 bottoms is directed in the stripping tower (not shown), and described stripping tower contacts with residual appropriate hydrocarbon gas in the displacement catalyst pore volume granules of catalyst with stripping gas.

By recovering activity of such catalysts at revivifier internal combustion coke.The regeneration of catalyzer takes place under low vapor partial pressure, and this is owing to low hydrogen richness in the coke that comes from the sharp separation element causes.Regenerator bed is being operated under the temperature of 600-750 ℃ (preferred 670-720 ℃) and under the pressure at 1.0-2.5bar.The catalyst particles that first section cyclonic separator by revivifier and second section cyclonic separator of revivifier reclaim turns back in the catalyst bed.

The combustion gases that generate by coke burning rise in the whole fluidized-bed of revivifier, are directed in the inside of dilute phase and revivifier or the outside cabin and from that and arrive the guiding valve of the combustion gases of hierarchy of control pressure.

Therefore, more than the Consideration proof listed in this manual the invention provides the low-cost downflow reactor system of installing in existing FCC unit, this method is unknown in the prior art.

The FCC technology of carrying out in described device relates generally to heavy feed stock.The density d of the heavy vacuum gas oil that exemplifies_20/4Be 0.9386 and Lan Shi carbon residue RCR be 0.38wt%.Final boiling point is higher than 500 ℃.

Ratio at catalyzer and oil is this technology of operation under the 3-15 then, and this ratio is 6-10 more preferably, still 7.0-9.0 more preferably.

The service temperature of raw material changes to 400 ℃ from 200 ℃.Preferred operating restraint is 310-350 ℃.Therefore, according to WO01/44406, the raw material under 320 ℃ is introduced in thedownflow reactor 50 by one group of feed injector 41.At themixing section 101 that is positioned at dispersingnozzle 120 lower ends, dispersive raw material like this is atomized into size by dispersion steam and is lower than 200 microns drop, is expelled in thedownflow reactor 50 as fine spraying from described dispersingnozzle 120 raw materials.The nebulization efficiency that should be pointed out that raw material is a particularly important in the downflow reactor system, and this is because different with upper reaches system or riser tube, does not have catalyst recirculation in downflow reactor.

The temperature that regenerated catalyst is incorporated in the regenerated catalyst standpipe (not shown) is 600-750 ℃, more preferably 670-720 ℃.Therefore, catalyzer is introduced in the regenerated catalyst standpipe, wherein comes the flow of control catalyst by the guiding valve (not shown).Guiding valve drives under temperature of reaction control, and wherein said temperature is measured at select location place, the lower end ofdownflow reactor 50.

Should be pointed out that FCC technology of the present invention mainly utilizes riser reactor.Therefore, any improvement in the FCC technology of using downflow reactor all should be compared with the riser tube technology of standard.This is that the present invention uses the reason of standard as a comparison case from the result of riser cracking reaction.On the other hand there is not known downflow reactor operation commercial unit.

Therefore, according to following embodiment, by comparing with productive rate from typical FCC riser tube, thereby set forth advantage of the present invention, wherein these embodiment should not be interpreted as limitation of the present invention.

Embodiment

Raw material is made up of 80% heavy gas oil and 20% vacuum resid.Listed the principal character of raw material in the following table 1.

Table 1

D20/4	0.9386
		P.C.R.(wt％)	0.38
Sulphur (wt%)	0.575
		Pitch (wt%)	0.1
Total nitrogen (ppm)	3211
		Basic nitrogen (ppm)	961
Aniline point (℃)	80.8
		Viscosity under 40 ℃ (cSt)	268.4
Viscosity under 100 ℃ (cSt)	14.57
		ASTM D 1160 distillates a little under 760mmHg, ℃
IBP	334.5
		5％	387.1
10％	398.3
		20％	423.2
30％	440.6
		40％	455.6
50％	471.3
		60％	490.4
70％	512.4
		Metal (ppm)
Ni	＜1
		V	＜1

Under above-described total reaction conditions, in device of the present invention, carry out cracking reaction.

From the pilot scale unit, obtain the two productive rate of riser tube technology tower and tower of the present invention, wherein under homogeneity coking (iso-coke) condition, compare.

Listed reaction yield in the following table 2.

Table 2

Productive rate based on raw material	The riser tube technology	The present invention
				wt％	wt％
Fuel gas	3.6	3.5
			LPG (comprising propylene)	20.3	21.0
Gasoline, C5-220℃	47.5	52.6
			LCO	12.1	9.6
Decanted oil	8.0	4.8
			Coke	8.5	8.5
Amount to	100.0	100.0
			Propylene	7.0	9.0
Transformation efficiency	79.9	85.6

Therefore, the present invention causes the high yield of valuable product such as propylene, LPG and gasoline, and the productive rate that keeps coke simultaneously is in rational numerical.

When comparing with the typical results that obtains according to the riser tube technology of prior art, the FCC technology of carrying out in device of the present invention obtains very excellent results.

Claims (55)

1. fluid catalytic cracking contains the device at the hydrocarbon feed oil of 340-720 ℃ of following ebullient liquid hydrocarbon, and wherein said device comprises:

(a) regenerated catalyst riser tube, it carries the dilute phase regenerated catalyst upwards to the regenerated catalyst sparger;

(b) regenerated catalyst sparger, it is furnished with the basket and by carrying the autonomous channel that the fluid user carries the catalyzer in the described regenerated catalyst riser tube of distributing, described catalyst distributor links to each other by cross section with described riser tube, with link to each other with downflow reactor by the catalyzer acceleration zone before the mixing zone, described sparger make carry fluid and catalyzer is centrifugal and the distribution catalyzer in described downflow reactor;

(c) downflow reactor, has the mixing zone at an upper portion thereof to start catalytic cracking reaction, wherein said mixing zone is furnished with the raw material that feed injector will contact with regenerated catalyst with gasification in described mixing zone, the bottom of described reactor links to each other with no dipleg formula cyclonic separator by the square-section pipeline;

(d) is furnished with the collection container of sharp separation element, so that sharp separation spent catalyst and the appropriate hydrocarbon gas of having reacted.

2. the device of claim 1, wherein said cross section is to tilt towards described catalyst distributor with horizontal plane is angled.

3. claim 1 or 2 device, wherein catalyst stream enters in the described sparger along tangent position.

4. claim 1,2 or 3 device, the described feed injector that wherein is installed in the described mixing zone of downflow reactor comprises the atomization unit of being furnished with the central nozzle that is used for atomizing fluids and being used for the side nozzle of liquid starting material, wherein arrange described nozzle, to cause that raw material atomizes fully, promote interaction simultaneously with hot descending catalyst optimization.

5. each device of aforementioned claim, the quantity of wherein said feed injector is the function of the sectional area of described mixing zone, wherein select the quantity of feed injector, so that cover the highest possible sectional area, described feed injector was accommodated in single stage or a plurality of stage.

6. each device of aforementioned claim, wherein said feed injector can with respect to the horizontal plane be installed with-30 ° to+30 ° angle, and atomized feed is injected along the direction relative with catalyst stream.

7. each device of aforementioned claim, wherein said feed injector tilts to install with 0 ° to+30 ° angle, and atomized feed is injected along the direction relative with catalyst stream.

8. each device of aforementioned claim, wherein feed injector is any feed injector efficiently.

9. each device of aforementioned claim, the surface-area of the porous plate of wherein relevant with the divergence angle β of material jet distribution catalyzer minimizes the zone that wherein only has catalyzer.

10. each device of aforementioned claim wherein below the distribution basket in the tapered section of described catalyzer acceleration zone, carries fluid and mixes in regenerated catalyst with the low speed of 3-8m/s (10-25ft/s).

11. each device of aforementioned claim, it is 2-15m/s that the diameter of wherein said mixing zone should guarantee to carry fluidic speed.

12. it is 5-10m/s that the device of claim 11, the diameter of wherein said mixing zone should guarantee to carry fluidic speed.

13. each device of aforementioned claim, wherein collection container comprises the duct orientation of the square-section that links to each other with the no dipleg formula cyclonic separator that is symmetrically located at described downflow reactor exit with described downflow reactor, so that separate catalyzer and appropriate hydrocarbon gas greater than 99% in described no dipleg formula cyclonic separator.

14. a regenerated catalyst sparger that is used for being included in the downflow reactor of heavy hydrocarbon streams fluidized catalytic cracking unit, wherein said catalyst distributor comprises:

A) from the regenerated catalyst riser tube to wherein guiding regenerated catalyst and carrying the fluidic chamber;

B) at least two are used for carrying the fluidic pipeline by regenerated catalyst;

C) will be directed to the conical surface of the distribution basket of being furnished with porous plate with the catalyzer that carries fluid separation;

D) be connected to the piston of the vertical sealing at described sparger top, meet curve mode so that flow;

E) be used to inject logistics to assist the nozzle that on the described basket that distributes, forms even catalyst content and fluid catalyst beds;

F) comprise the catalyzer acceleration zone of tapered section and round shape part, thereby catalyzer be directed to catalyzer and raw material therein in the mixing zone of blended downflow reactor,

And described sparger makes catalyst entrainment fluid and catalyzer centrifugal, and catalyzer is directed in the described mixing zone, the catalyst entrainment fluid described pipeline of flowing through simultaneously, and mixed in catalyzer with low speed below described distributions basket.

15. the regenerated catalyst sparger of claim 14, wherein said sparger also can utilize the piston of described vertical sealing to distribute.

16. the regenerated catalyst sparger of claim 14 or 15, wherein said pipeline be shaped as prolate shape.

17. the maximum gas velocity in claim 14,15 or 16 the regenerated catalyst sparger, wherein said pipeline is 20m/s (65ft/s), the biggest quality speed of catalyzer is 500kg/ (m simultaneously²S).

18. each regenerated catalyst sparger of claim 14-17, the bore dia of wherein said porous plate is 20-100mm.

19. the regenerated catalyst sparger of claim 18, the bore dia of wherein said porous plate are 40-80mm.

20. each regenerated catalyst sparger of claim 14-19, wherein the catalyst quality speed by punched areas is 250-750kg/ (m²S).

21. the regenerated catalyst sparger of claim 20, wherein the catalyst quality speed by punched areas is 400-600kg/ (m²S).

22. the periphery that each regenerated catalyst sparger of claim 14-21, the periphery of wherein said porous plate form the end of its protuberance and the feed injector that is positioned at the mixing zone, below is complementary.

23. each regenerated catalyst sparger of claim 14-22 wherein in the tapered section of described catalyzer acceleration zone, carries fluid low speed with 3-8m/s (10-25ft/s) below the basket that distributes and mixes in regenerated catalyst.

24. each regenerated catalyst sparger of claim 14-23, wherein design described catalyzer acceleration zone, catalyzer is incorporated into final velocity by the feed injector raw materials mixed jet that is positioned at the mixing zone, below so that the length in described district is enough to make catalyzer to reach.

25. the regenerated catalyst sparger of claim 24, wherein said final velocity are 1.5-11m/s (5-35ft/s).

26. the regenerated catalyst sparger of claim 25, wherein said final velocity are 5-8m/s (15-25ft/s).

27. each regenerated catalyst sparger of claim 14-26 is wherein regulated the diameter of the described round shape part of acceleration zone, so that close with the descending speed of carrying fluidic speed and catalyzer of catalyzer.

28. each regenerated catalyst sparger of claim 14-27 is wherein regulated the diameter of the described round shape part of acceleration zone, so that the cross section of regulating described round shape part is identical with the cross section that distributes basket.

29. fluid catalytic cracking contains the method at the hydrocarbon feed oil of 340-720 ℃ of following ebullient liquid hydrocarbon under the situation that does not add any hydrogen, wherein said method comprises the steps:

A) provide the regenerated catalyst riser tube, by regenerated catalyst sparger, downflow reactor that cross section links to each other with described riser tube, this downflow reactor comprises mixing zone, feed injector and is furnished with the collection container of sharp separation element;

B) under 600-750 ℃, regenerated catalyst is incorporated into the bottom of described regenerated catalyst riser tube, wherein catalyzer is carried fluid carry-over and upwards enters the described cross section that links to each other with described sparger as dilute phase, catalyzer and carry the fluidic dilute phase and enter described sparger by the tangent line pattern;

C) in described catalyst distributor, carry out centrifugal, carry fluid and catalyzer with separation, and uniform distribution waits to be fed to the catalyzer of the mixing zone of described downflow reactor, flow through the downwards conical surface of the described basket that distributes of catalyzer, the bottom of the wherein said basket that distributes is porose, below described distribution basket, carry fluid gas coming through pipeline and mix in catalyzer with low speed simultaneously, described catalyzer quickens in acceleration zone under influence of gravity;

D) under 200-400 ℃ by in the former described mixing zone of expecting described downflow reactor of feed injector injected hydrocarbon, so that atomize hydrocarbon feed fully, so the raw material of atomizing as fine spraying then with the descending catalyst reaction of spirally from described distributions basket, the suspensoid that described reaction obtains being rich in spent catalyst particles and is adsorbed on the light hydrocarbon cracked product on the catalyzer, described suspensoid is discharged into the sharp separation element of described collection container from described downflow reactor bottom;

E) sharp separation crackene product and granules of catalyst be mutually in described sharp separation element.

30. the method for claim 29, wherein to carry fluid be steam, water, petroleum naphtha, Sweet natural gas and fuel gas to regenerated catalyst.

31. the method for claim 29 or 30, what wherein be used to carry catalyzer in the regenerated catalyst riser tube carries auxiliary hydrocarbon partial pressure and the catalyst temperature that reduces in the downflow reactor of fluid, therefore reduces the thermally splitting side reaction.

32. claim 29,30 or 31 method, wherein the mass rate in regenerated catalyst riser tube inner catalyst dilute phase is 50-500kg/ (m²S).

33. the method for claim 32, wherein the mass rate in regenerated catalyst riser tube inner catalyst dilute phase is 150-300kg/ (m²S).

34. each method of claim 29-33, the minimum velocity when wherein regenerated catalyst enters described regenerated catalyst sparger is 9.14m/s (30ft/s).

35. each method of claim 29-34, the top speed when wherein regenerated catalyst enters described regenerated catalyst sparger is 20m/s (65ft/s).

36. each method of claim 29-35, wherein the final catalyst velocity in acceleration zone is 1.5-11m/s (5-35ft/s).

37. the method for claim 36, wherein the final catalyst velocity in acceleration zone is 5-8m/s (15-25ft/s).

38. each method of claim 29-37, wherein carrying fluidic speed in described mixing zone is 2-15m/s.

39. the method for claim 38, wherein carrying fluidic speed in described mixing zone is 5-10m/s.

40. each method of claim 29-39, wherein the mass velocity at described downflow reactor inner catalyst is 50-500kg/ (m²S).

41. the method for claim 40, wherein the mass velocity at described downflow reactor inner catalyst is 100-350kg/ (m²S).

42. the method for claim 41, wherein the mass velocity at described downflow reactor inner catalyst is 150-250kg/ (m²S).

43. each method of claim 29-42, wherein said downflow reactor is operated under the pressure of 1.0-2.0bar.

44. each method of claim 29-43, wherein cracking reaction takes place in second at 1-4.

45. the method for claim 44, wherein cracking reaction takes place in second at 1.5-3.

46. each method of claim 29-45, wherein catalyzer is 3-15 with the ratio of oil.

47. the method for claim 46, wherein catalyzer is 6-10 with the ratio of oil.

48. the method for claim 47, wherein catalyzer is 7-9 with the ratio of oil.

49. each method of claim 29-48, the temperature out of wherein said downflow reactor is 450-700 ℃.

50. the method for claim 49, the temperature out of wherein said downflow reactor are 520-570 ℃.

51. each method of claim 29-50, wherein in the described no dipleg formula cyclonic separator of collection container inside, catalyzer greater than 99% separates with appropriate hydrocarbon gas, isolating catalyzer leave cyclonic separator by outlet and be deposited on the bottom of described collection container, appropriate hydrocarbon gas is left described no dipleg formula cyclonic separator by outlet conduit simultaneously, and described outlet conduit is by the gas separated of leaving described cyclonic separator and the gas feed of carrying by the conduit that is inserted in the described outlet conduit.

52. each method of claim 29-51 wherein in order to reach higher solid collection efficient in described collection container, is emitted the suspensoid of particle and the mixture that reacted by the lower part outlet of described no dipleg formula cyclonic separator.

53. each method of claim 29-52, the sharp separation element that wherein is used to separate spent catalyst and the appropriate hydrocarbon gas of having reacted is the sharp separation element of any prior art.

54. each device of claim 1-13, the quantity of wherein said feed injector is the function of the sectional area of described mixing zone, wherein select the quantity of feed injector, so that cover the highest possible sectional area, described feed injector was accommodated in single stage or a plurality of stage.

55. each method of claim 29-53, what wherein be used to carry catalyzer in the regenerated catalyst riser tube carries auxiliary hydrocarbon partial pressure and the catalyst temperature that reduces in the downflow reactor of fluid, therefore reduces the thermally splitting side reaction.

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