CN102649912B

CN102649912B - Circulating method for cold regenerated catalyst and catalytic cracking reaction regenerating system

Info

Publication number: CN102649912B
Application number: CN201210152931.4A
Authority: CN
Inventors: 刘梦溪; 卢春喜; 王祝安; 范怡平
Original assignee: China University of Petroleum Beijing
Current assignee: China University of Petroleum Beijing
Priority date: 2012-05-16
Filing date: 2012-05-16
Publication date: 2014-02-19
Anticipated expiration: 2032-05-16
Also published as: CN102649912A

Abstract

The invention provides a circulating method for a cold regenerated catalyst and a catalytic cracking reaction regenerating system. The catalytic cracking reaction regenerating system comprises a hoisting pipe reactor, a pre-hoisting section, a regenerator, a heater and a gas-solid annular flow mixing stripper, wherein the gas-solid annular flow mixing stripper is used for mixing a first solid grain and a second solid grain at different temperatures during a regenerating form fluid catalytic cracking process and stripping the smoke and air taken by the solid grains after being mixed; the first solid grain is a low-temperature catalyst or low-temperature to-be-generated agent; and the second solid grain is a high-temperature catalyst. The circulating method for the cold regenerated catalyst comprises the following steps of: mixing and exchanging heat of the first solid grain from the heater and the second solid grain from the regenerator in the gas-solid annular flow mixing stripper, and meanwhile, stripping the taken smoke and air, forming the mixed catalyst and then entering into the pre-hoisting section.

Description

Cold regenerated catalyst circulation means and catalytic cracking reaction regeneration system rapidly

Technical field

The present invention relates to petrochemical field, the refrigeration cycle technology and the stripping that relate to catalyzer in fluid catalytic cracking process, particularly, relate to a kind of cold regenerated catalyst circulation means and catalytic cracking reaction regeneration system rapidly, for the stripping of the solid particulate in the mixing and mix of two kinds of catalyzer (between regenerator and/or between spent agent) of differing temps between fluid catalytic cracking process riser tube and fluidized-bed.

Background technology

Catalytic cracking reaction regeneration system rapidly is comprised of riser reactor, revivifier and line of pipes conventionally.Stock oil by nozzle atomization after, in riser reactor, contact with high-temperature regenerated catalyst, gasification, there is heat cracking reaction and catalyzed reaction, meanwhile there is condensation reaction and produce coke, coke is attached to catalyst surface and makes catalyst deactivation, the catalyzer of inactivation (spent agent) enters stripping stage after leg outlet is separated by gas-solid separation equipment, in stripping stage, spent agent entrained oil gas is replaced away by stripped vapor, then spent agent enters the revivifier regeneration of burning by pipeline to be generated, catalyzer after regeneration (regenerator) enters riser tube bottom by regeneration pipeline.

Agent-oil ratio is the most important control parameter of catalytic cracking, has reflected catalyzer and oily mass flux ratio.Under same processing condition, suitable larger agent-oil ratio means that stock oil can touch more high activated catalyst, more active centre in other words, thereby also there is higher product yield and selectivity.But in actual production, the internal circulating load of catalyzer, because being subject to thermally equilibrated restriction, can not arbitrarily regulate.Increase the internal circulating load of regenerator and maintain that to bring the total heat of reactive system into constant, can only reduce regenerator temperature.This often means the regeneration temperature that reduces revivifier in actual production, and this can the serious regeneration effect that reduces catalyzer.Therefore, increasing regenerator internal circulating load and rising agent oil ratio is a pair of contradiction that cannot take into account.For this reason, people have proposed various technology to address this problem.

At present, in fluid catalytic cracking process, cold catalyst recirculation technology can be divided into following several types: (1) directly mixes (patent 01144955.1 by cold spent agent with high temperature regeneration agent in riser tube or in pre lift zone, 201020608020.4), but owing to there is no follow-up step for regeneration, in mixed catalyzer, contain many spent agents, thereby activity is lower, can reduce the activity of nozzle place catalyzer like this, and then affect product yield.(2) do not carry out cold, the mixing of thermocatalyst, but regenerator is directly cooling: on regeneration circuit, heat collector to be set, the catalyzer that heat collector is cooling is introduced to riser tube, but the total heat of taking away due to heat collector is definite value, if the temperature of the cooling catalyzer that assurance is flowed out from heat collector is certain, can not meet the requirement that catalyst flow is adjusted, in like manner, if the flow of the cooling catalyzer that assurance is flowed out from heat collector is certain, can not meet the requirement that catalyst temperature is adjusted, so its catalyst flow is not independent variable, be difficult to regulate (patent 99120517.0), if build a heat collector, flow process is complicated again, improvement project amount is large, fluidisation difficulty of transportation, need to regenerate on circuit and leave larger space (patent 200810146601.8).(3) mixing tank (patent 99120529.4,200710054772,200510017751.5) using riser tube bottom pre lift zone as cold and hot regenerated catalyst.Although being the catalyzer to having regenerated, this technology mixes, without as (1) process of planting the regeneration of the required catalyzer of situation, but high to the structural requirement of pre lift zone like this, cause complex structure, the cost of pre lift zone to increase, and pre lift zone in mixing time and the heat transfer time all very short, even if cold and hot catalyzer can mix, do not have time enough to conduct heat yet.

For example, above-mentioned (3), plant on the basis of mode, prior art has the following special patent for hot and cold catalyst mix device: the pre lift zone mixing tank that patent 200710054772.3 adopts is the direct tube section that a diameter is greater than riser tube, direct tube section top is connected with riser tube by a conical section, but pre lift zone inside does not adopt any inner member.The pre lift zone internal mixer that patent 200510017751.5 adopts is provided with steam gas sparger, but there is no other inner members.Can find out in the pre lift zone mixing tank that patent 200710054772.3 and patent 200510017751.5 adopt all less than arranging and can promote the inner member that mixes, just rely on hot and cold catalyzer naturally mixing in fluidized-bed, because catalyzer residence time in pre lift zone is very short, thereby catalyst mix effect is poor, and because the flow of hot and cold catalyzer is generally different, be easy to cause the bias current in riser tube.Patent 200720090003.4 is provided with hot and cold catalyst inlet at riser tube pre lift zone cylindrical shell different heights place, in inner barrel, inner sleeve is set, and each catalyst inlet pipe below arranges the channel base plate under screw.This patent can realize the mixing of particle preferably, but mobile comparatively complexity, the resistance to flow of hot and cold catalyzer in pre lift zone is larger, thereby affects mixed effect, and the channel base plate under screw is difficult for installation, also easily distortion.Patent 200810140821.X is provided with the thrust-augmenting nozzle of a level at each catalyst inlet place of pre lift zone, draft tube outlets and equipment axis are angled, lifting media outlet pipe is arranged to the hydraucone of back taper, pre lift zone outlet is provided with baffling cylinder, to destroy the dense nucleolus fluidal texture of Xi, limit, center wall forming in lifting process, impel granule density to be radially uniformly distributed, but this patent exist catalyst mix, heat transfer time shorter, mix and the inhomogeneous problem of conducting heat.

Summary of the invention

The present invention aims to provide a kind of catalytic cracking reaction regeneration system rapidly and cold regenerated catalyst circulation means, with solve prior art exist cold and hot catalyst mix, heat transfer time shorter, mix and the inhomogeneous problem of conducting heat.Meanwhile, the present invention has also solved prior art cannot carry out steam stripped problem to two kinds of solid particulates when mixing, and makes the present invention also realize stripping completing when two kinds of solid particulates fully carry out mixed heat transfer.

For this reason, the present invention proposes a kind of catalytic cracking reaction regeneration system rapidly, and catalytic cracking reaction regeneration system rapidly comprises: riser reactor, pre lift zone, revivifier and be arranged on the heat collector outside revivifier,

Catalytic cracking reaction regeneration system rapidly also comprises: be arranged on the gas-solid loop flow mixing stripper outside riser reactor and pre lift zone, gas-solid loop flow mixing stripper, the first solid particulate and the second solid particulate that for example, in can the fluid catalytic cracking process for reconstituted form, mix differing temps, and strip flue gas and the air that the first solid particulate and the second solid particulate are carried secretly, the first solid particulate can be low temperature catalyst or low temperature spent agent, the second solid particulate can be high temperature catalyst, the temperature of the second solid particulate is higher than the temperature of the first solid particulate,

Gas-solid loop flow mixing stripper comprises: the cylindrical shell 7 with inner chamber, be arranged in the inner chamber of cylindrical shell and the guide shell 6 coaxially arranged with cylindrical shell, the annular space gas distributor 3 of the bottom, annular space space between cylindrical shell 7 and guide shell 6, be arranged in cylindrical shell and be positioned at the guide shell gas distributor 11 under guide shell 6, extend into the pneumatic outlet in cylindrical shell 7 inner chambers, cylindrical shell 7 lower ends are connected with cone 2, be arranged on the blended solid particle outlet 1 of cone 2 belows, be positioned at cone 2 bottoms and the cone stripped vapor ring 12 in blended solid particle outlet 1 top, and be connected respectively to the first solid particulate admission passage and the second solid particulate admission passage in the inner chamber of cylindrical shell, the first solid particulate admission passage connects heat collector, the second solid particulate admission passage connects revivifier,

Wherein, the inner chamber of cylindrical shell comprises: the internal space of annular space space and guide shell 6, annular space gas distributor 3 is for annular gas distributor and be positioned under cylindrical shell 7 and with annular space space and be connected, and guide shell gas distributor 11 is positioned under guide shell 6 and with the internal space of guide shell 6 and is communicated with.

Further, the radial cross-section of guide shell 6 and cylindrical shell 7 is long-pending than being 0.2～0.8, the barrel of guide shell 6 is provided with perforate 13, perforate 13 is communicated with the internal space of annular space space and guide shell 6, perforate is a plurality of long strip shapes holes, the height of perforate is less than or equal to 0.9 times of guide shell 6 height, and the total area of perforate is less than or equal to the lateral area of the guide shell 6 of 0.9 times; Or perforate is a plurality of circular ports, the radius of perforate is less than or equal to 0.9 times of guide shell 6 height, and the total area of perforate is less than or equal to the lateral area of the guide shell 6 of 0.9 times.

Further, gas-solid loop flow mixing stripper is arranged on outside riser reactor, pre lift zone and revivifier; The first solid particulate admission passage is the first solid particle inlet pipe 5, the second solid particulate admission passage is the second solid particle inlet pipe 10, the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10 are connected to the both sides of cylindrical shell 7 and are all communicated with annular space space, and blended solid particle outlet 1 is connected with pre lift zone; Gas-solid loop flow mixing stripper also comprises: cover the end socket 8 at cylindrical shell upper end closed cylinder lumen, wherein, the pneumatic outlet extending in cylindrical shell 7 inner chambers is the gas outlet tube 9 being arranged on end socket 8, guide shell 6 be and be arranged vertically with cylindrical shell 7.

Further, within gas-solid loop flow mixing stripper is arranged on revivifier, cylindrical shell 7 is surrounded jointly by the inner side wall of revivifier and the arc of piece side, and the top of cylindrical shell is uncovered, and the inner chamber of cylindrical shell is directly communicated with the inner chamber of revivifier;

The first solid particulate admission passage is the first solid particle inlet pipe 5, the first solid particle inlet pipe 5 extend into the side direction of cylindrical shell 7 and is communicated with annular space space from the outside of revivifier, uncovered formation the second solid particulate admission passage at the inner chamber of revivifier and the top of cylindrical shell.

Further, the first solid particle inlet pipe 5 is connected with heat collector, and the second solid particle inlet pipe 10 is connected with revivifier.

Further, revivifier comprises: interconnective burning tank and two close phases, the first solid particle inlet pipe 5 is connected with heat collector, the second solid particle inlet pipe 10 and two close being connected.

Further, catalytic cracking reaction regeneration system rapidly comprises: a plurality of riser reactors, a plurality of pre lift zone, revivifier, a plurality of gas-solid loop flow mixing stripper and a line of pipes, on revivifier, be provided with one or more heat collectors, each pre lift zone is a corresponding riser reactor and the circulation mixing stripper of connecting one to one;

The second solid particle inlet pipe 10 is connected with revivifier, and the blended solid particle outlet of each circulation mixing stripper 1 is man-to-man to be respectively connected with a pre lift zone;

The first solid particle inlet pipe 5 of each circulation mixing stripper is connected on a heat collector jointly, or the first solid particle inlet pipe 5 of each circulation mixing stripper man-to-man being connected on a heat collector respectively.

Further, revivifier comprises: divide the first revivifier and the Second reactivator that are arranged, heat collector is connected with the first revivifier, the first solid particle inlet pipe 5 is connected with heat collector, the second solid particle inlet pipe 10 is connected with Second reactivator, and circulation mixing stripper is between the first revivifier and Second reactivator.

The present invention also provides a kind of cold regenerated catalyst circulation means, fluid catalytic cracking process for reconstituted form mixes the first solid particulate and the second solid particulate of differing temps, and strip flue gas and the air that the first solid particulate and the second solid particulate are carried secretly simultaneously, the first solid particulate is low temperature catalyst or low temperature half regenerator, the second solid particulate is high temperature catalyst, the temperature of the second solid particulate is higher than the temperature of the first solid particulate, cold regenerated catalyst circulation means completes by catalytic cracking reaction regeneration system rapidly, catalytic cracking reaction regeneration system rapidly comprises: riser reactor, the pre lift zone being connected with riser reactor, revivifier and line of pipes, revivifier is outside equipped with heat collector,

From the first solid particulate of heat collector, after also stripping as mixed heat transfer in gas-solid loop flow mixing stripper above flue gas and the air of carrying secretly simultaneously, forming mixed catalyst, enter pre lift zone with the second solid particulate from revivifier.

Further, gas-solid loop flow mixing stripper is arranged on outside riser reactor, pre lift zone and revivifier; By the first solid particulate and the second solid particulate level or be transported to obliquely in annular space space, what make annular space gas distributor 3 is greater than the tolerance of giving of guide shell gas distributor 11 to tolerance, make the first solid particulate and the second solid particulate in annular space for upwards flowing, in guide shell 6 for flowing downward;

A part of the second solid particulate from regeneration in-situ regeneration enters the cooling formation the first of heat collector solid particulate, and another part the second solid particulate flows out revivifier; The a part of the first solid particulate flowing out from heat collector returns to revivifier, and another part the first solid particulate flowing out from heat collector carries out mixed heat transfer and stripping with another part the second solid particulate flowing out from revivifier.

Further, gas-solid loop flow mixing stripper is arranged on outside riser reactor, pre lift zone and revivifier; By the first solid particulate and the second solid particulate level or oblique under be transported in annular space space, what make annular space gas distributor 3 is less than the tolerance of giving of guide shell gas distributor 11 to tolerance, make the first solid particulate and the second solid particulate in annular space space for flowing downward, in guide shell 6 for upwards flowing;

Further, within gas-solid loop flow mixing stripper is arranged on to revivifier, the top of cylindrical shell is uncovered, and the inner chamber of cylindrical shell is directly communicated with the inner chamber of revivifier;

The first solid particulate enters annular space space, the second solid particulate directly enters into the top of cylindrical shell 7 and the top of guide shell 6 from the inner chamber of revivifier, what make annular space gas distributor 3 is less than the tolerance of giving of guide shell gas distributor 11 to tolerance, make the first solid particulate and the second solid particulate in annular space space for flowing downward, in guide shell 6 for upwards flowing;

A part of the second solid particulate from regeneration in-situ regeneration enters the cooling formation the first of heat collector solid particulate, and another part the second solid particulate enters into the top of cylindrical shell 7 and the top of guide shell 6; The a part of the first solid particulate flowing out from heat collector returns to revivifier, another part the first solid particulate flowing out from heat collector with from entering into the second solid particulate at the top of cylindrical shell 7 and the top of guide shell 6, carry out mixed heat transfer and stripping.

Further, revivifier comprises: divide the first revivifier and the Second reactivator that are arranged, heat collector is connected with the first revivifier, reclaimable catalyst is introduced into the first revivifier, at the first revivifier, burn part defocused, a part is flowed out to enter Second reactivator and in Second reactivator, burn remaining Jiao by the first regenerator bottoms and forms the second solid particulate, another part out forms the first solid particulate from heat collector bottom, the second solid particulate is the catalyzer of the holomorphosis of high temperature, the first solid particulate is the catalyzer to be generated of low temperature, the catalyzer of the holomorphosis of the high temperature of being drawn by Second reactivator also strips with the catalyzer to be generated mixed heat transfer gas-solid loop flow mixing stripper of the low temperature of drawing from heat collector flue gas and the air of carrying secretly simultaneously.

By controlling air demand, what make guide shell gas distributor 11 gives the different to tolerance of tolerance and annular space gas distributor 3, in guide shell bottom, produce pressure difference, promote solid particulate (catalyzer) circulates between annular space and guide shell, when the first solid particulate and the second solid particulate enter into the inner chamber of cylindrical shell, the first solid particulate and the second solid particulate not only form respectively circulating separately between annular space and guide shell, completed stripping simultaneously, and flowing of the first solid particulate and flowing also to form mutually to intersect to mix in the inner chamber of cylindrical shell and having realized heat exchange of the second solid particulate, in a heat transfer process, the first solid particulate and the second solid particulate do not reach completely and mix after mixing, but form the cold of different sizes, hot solids particle (catalyzer) group, these are cold, hot solids particle (catalyzer) group is mingled with mutually, the process that enters annular space space by guide shell circulation be one by cold, hot solids particle (catalyzer) the group fragmentation newly assigned process of laying equal stress on, the process that is entered guide shell by annular space space is a process of again mixing.And then, on the guide shell of circulation mixing stripper, having hole, catalyzer not only mixes in the upper and lower of guide shell, and can mix through hole, thereby has efficient mixed effect.

Hot and cold solid particulate (catalyzer) the group fragmentation newly assigned process of laying equal stress on comprises: a, while entering annular space space from guide shell circulation, radially outwards the flow process of (scattering) of hot and cold solid particulate; By the perforate on guide shell, flow into guide shell with the hot and cold solid particulate in b, annular space, form the distribution of hot and cold solid particulate in annular space, during through perforate, a plurality of perforates on guide shell are carried out shearing, fragmentation repeatedly to hot and cold solid particulate (catalyzer) group.

The process that hot and cold solid particulate mixes again comprises: c, by annular space space, to enter guide shell be central authorities motions from guide shell edge to guide shell, realized mixed heat transfer; Pass in and out by the perforate on guide shell with d, hot and cold solid particulate, the process implementation of turnover mixed heat transfer.

So a plurality of perforates on guide shell have sufficient promoter action for the mixed heat transfer of two kinds of solid particulates.

Therefore, every through once circulation, hot and cold catalyzer just need to experience mixed once and reallocation.The flue gas of catalyst entrainment is present between the space of catalyzer and is adsorbed in the micropore of catalyzer, the interstitial flue gas of catalyzer is easier to displacement, but the flue gas of catalyzer micropore internal adsorption needs: steam by steam main diffusion to catalyzer outside surface, by catalyzer outside surface, diffused in catalyzer micropore, in micropore in the flue gas absorption that is at war with, the flue gas displacing by catalyzer micropore internal diffusion to catalyzer outside surface, flue gas is diffused to 5 steps such as steam main body by catalyzer outside surface, owing to going through a plurality of diffusion processes, in catalyzer micropore, the displacement of flue gas is very difficult, not only need high catalyzer-steam contact efficiency, and need long catalyzer-live steam duration of contact.The gas-solid loop flow mixing stripper kind that the present invention proposes, guide shell, annular space fluidization steam vapor are passed into by annular space gas distributor, guide shell gas distributor and loosening steam ring respectively, and the every circulation primary of solid particulate (catalyzer) just means with annular space gas distributor, guide shell gas distributor and the live steam of loosening steam ring of bottom and contacts once.

Secondly, because two kinds of solid particulates hot and cold solid particulate (catalyzer) group when the mixed heat transfer is broken and redistribute, this more easily comes out the interior flue gas of catalyzer micropore or the interior flue gas of catalyzer micropore more easily contacts with steam, and this has brought more chance to displacement of flue gas in catalyzer micropore.

And then, catalyzer at guide shell with lower area circulating radially, the vapor bubbles rising is had to very strong shearing action, greatly reduce bubble diameter, make the contact efficiency of steam-catalyzer higher, vapor bubbles more easily enters or approach catalyzer micropore, has realized the long high-efficient contact of catalyzer and live steam.Circulation mixing stripper of the present invention has not only been realized stripping in two kinds of solid particulate heat exchange, and because two kinds of solid particulates are cold when the mixed heat transfer, the fragmentation of hot solids particle (catalyzer) group is also redistributed, this has brought more multimachine meeting to the displacement of flue gas in catalyzer micropore, and every circulation primary just means live steam contact once, also make the vapor bubbles rising be sheared, greatly reduce bubble diameter, vapor bubbles is more easily entered or approach catalyzer micropore, so steam stripping efficiency is higher than the efficiency of other strippers, for example, steam stripping efficiency is 200710152287.X than the patent No., it is high that name is called annular space air-lift gas-solid loop flow reactor.Therefore, the present invention has also realized high efficiency stripping completing when two kinds of solid particulates fully carry out mixed heat transfer.

The gas-solid loop flow mixing stripper that the present invention proposes has utilized the theory of particle circulation cleverly; by catalyzer (spent agent or regenerator) in inside and outside the circulating of guide shell; and mixing repeatedly, reallocation, really realized the even mixing of hot and cold catalyzer, conducted heat and the temperature distribution of homogeneous for a long time.Especially with respect to the 2nd kind of mode of introducing in background technology, the present invention can regulate respectively control to the temperature of cold catalyst inlet pipe 5 and thermocatalyst inlet tube 10 and flow, both can obtain entering the ideal temperature of pre lift zone, can obtain sufficient flow again, setting range is very extensive, and the mixed catalyzer that simultaneously guarantees temperature and flow can be provided flexibly.In current catalytic cracking reaction regeneration system rapidly, regulate temperature of reaction to rely on and regulate catalyst flow, regulate fuel oil preheating temperature and regulate stock oil flow to realize, wherein regulating catalyst flow is Main Means, but this method also has obvious shortcoming, for example, can reduce temperature of reaction by reducing catalyst flow, but meanwhile, the catalytic amount that participates in reaction is that agent-oil ratio has also declined greatly, and this is unfavorable for the raising of product yield and optionally improves very much.Because cold catalyst recirculation technology provided by the invention can realize the adjusting respectively of temperature and flow, so can effectively solve this difficult problem.The agent-oil ratio of catalytic cracking is at present generally between 6～8, angle from reaction, maintaining under the constant prerequisite of temperature of reaction, further rising agent oil ratio can effectively improve product yield and selectivity, but owing to being subject to the thermally equilibrated restriction of auto levelizer, further rising agent oil ratio must cause temperature of reaction to raise, the cold catalyst recirculation technology that the present invention proposes can realize when raising catalyst recirculation amount is agent-oil ratio, reduce catalyst temperature, make device under the constant prerequisite of temperature of reaction, in riser tube, agent-oil ratio reaches 9～15, thereby significantly improve the selectivity of product yield.

Accompanying drawing explanation

Fig. 1 is according to the main TV structure schematic diagram of the first gas-solid loop flow mixing stripper of the embodiment of the present invention;

Fig. 2 is according to the main TV structure schematic diagram of the second gas-solid loop flow mixing stripper of the embodiment of the present invention;

Fig. 3 is the schematic diagram of annular space gas lifting type operator scheme for the first gas-solid loop flow mixing stripper of the embodiment of the present invention;

Fig. 4 is the schematic diagram of central gas lift-type operator scheme for the second gas-solid loop flow mixing stripper of the embodiment of the present invention;

Fig. 5 is that the first in Fig. 3 and the second gas-solid loop flow mixing stripper are along the sectional structure of A-A direction;

Fig. 6 is the first structure of guide shell; Fig. 7 is the second structure of guide shell; Fig. 8 is the third structure of guide shell; Fig. 9 is the 4th kind of structure of guide shell;

Figure 10 is that wherein revivifier and settling vessel are coaxially arranged according to the structure of the first catalytic cracking reaction regeneration system rapidly of the embodiment of the present invention;

Figure 11 is that i.e. gas-solid loop flow mixing stripper is arranged in internal regenerator according to the structure of the third gas-solid loop flow mixing stripper of the embodiment of the present invention and the structure of the third catalytic cracking reaction regeneration system rapidly;

Figure 12 is according to the structure of the second catalytic cracking reaction regeneration system rapidly of the embodiment of the present invention, i.e. the reconstituted form of catalytic cracking is the close combined forms of burning tank-bis-;

Figure 13 is according to the structure of the 4th of the embodiment of the present invention the kind of catalytic cracking reaction regeneration system rapidly, adopts the catalytic cracking form of two-stage riser;

Figure 14 is according to the structure of the 5th of the embodiment of the present invention the kind of catalytic cracking reaction regeneration system rapidly, adopts the catalytic cracking form of two-stage regeneration.

Be below drawing reference numeral explanation:

1, mixed catalyst particle outlet 2, cone 3, annular space gas distributor 4, conveying airduct

5, cold catalyst inlet pipe (the first solid particle inlet pipe) 6, guide shell 7, cylindrical shell 8, end socket

9, gas outlet tube 10, thermocatalyst inlet tube (the second solid particle inlet pipe)

11, guide shell gas distributor 12, cone stripped vapor ring 13, perforate 14, transfer lime (pipeline)

15a, transfer lime (pipeline) 16, transfer lime (pipeline) 16a, transfer lime (pipeline) 16b, transfer lime

35, annular space gas distributor inlet tube 115, guide shell gas distributor inlet tube

30, pre lift zone 40, riser reactor 50, regeneration pipeline

60, the close phase 63 of revivifier 61, two, burning tank 65, gas solid separation district

67, annular space space 70, heat collector 80, dilute phase pipe

90, settling vessel 100, gas-solid loop flow mixing stripper 200, gas-solid loop flow mixing stripper

300, gas-solid loop flow mixing stripper 601, the first revivifier 602, Second reactivator

Embodiment

For technical characterictic of the present invention, object and effect being had more clearly, understand, now contrast accompanying drawing explanation the specific embodiment of the present invention.

As shown in FIG. 10 to 14, the invention provides five kinds of catalytic cracking reaction regeneration system rapidlys, these catalytic cracking reaction regeneration system rapidlys include: riser reactor 40, pre lift zone 30, revivifier 60, and be arranged on the heat collector 70 outside revivifier 60, these catalytic cracking reaction regeneration system rapidlys also comprise: be arranged on the gas-solid loop flow mixing stripper outside riser reactor and pre lift zone, gas-solid loop flow mixing stripper mixes the first solid particulate and the second solid particulate of differing temps in can the fluid catalytic cracking process for reconstituted form, and strip flue gas and the air that the first solid particulate and the second solid particulate are carried secretly, the first solid particulate is low temperature catalyst or low temperature half regenerator, the second solid particulate is high temperature catalyst, the temperature of the second solid particulate is higher than the temperature of the first solid particulate.The present invention is not limited to the fluid catalytic cracking of reconstituted form, also can not only can be used for the mixing stripping of catalyzer for the fluid catalytic cracking process of non-renewable form, also can be used for other solid particulates.

The feature of five kinds of catalytic cracking reaction regeneration system rapidlys in the present invention is: the first solid particulate admission passage connects heat collector, the second solid particulate admission passage connects revivifier, from heat collector bottom, draw one cold regenerator (low temperature catalyst), the thermocatalyst (high temperature catalyst) coming with revivifier is long-time evenly mixing and stripping in gas-solid loop flow mixing stripper, and utilize the further mixing of mobile realization in regeneration pipeline and conduct heat, guaranteed the even mixing and abundant heat transfer of hot and cold catalyzer completely.Wherein, two kinds of structures that are arranged on the gas-solid loop flow mixing stripper outside revivifier as shown in Figures 1 to 9.Figure 11 shows the main TV structure of the third gas-solid loop flow mixing stripper.

As shown in Figures 1 to 5, gas-solid loop flow mixing stripper comprises: the cylindrical shell 7 with inner chamber, be arranged in the inner chamber of cylindrical shell 7 and the guide shell 6 coaxially arranged with cylindrical shell 7, the annular space gas distributor 3 of 67 bottoms, annular space space between cylindrical shell 7 and guide shell 6, be arranged in cylindrical shell and be positioned at the guide shell gas distributor 11 under annular space gas distributor 3, extend into the pneumatic outlet in cylindrical shell 7 inner chambers, cylindrical shell 7 connects cone 2 below 11 from guide shell gas distributor, be arranged on the blended solid particle outlet 1 of cone 2 belows, be positioned at cone 2 bottoms and the cone stripped vapor ring 12 in blended solid particle outlet 1 top, and be connected respectively to the first solid particulate admission passage and the second solid particulate admission passage in the inner chamber of cylindrical shell.Cone 2 is cone barrel, also has inner chamber and is communicated with the inner chamber of cylindrical shell 7.

Wherein, as shown in Figures 3 to 5, cylindrical shell 7 can be cylinder with guide shell 6, guide shell 6 be all uncovered up and down, the internal space of guide shell 6 is directly communicated, so that the circulation of formation catalyst stream with the inner chamber of cylindrical shell 7.The inner chamber of cylindrical shell 7 comprises: the internal space of annular space space 67 and guide shell 6, annular space gas distributor 3 stretches out cylindrical shell 7 for annular gas distributor by annular space gas distributor inlet tube 35, annular space gas distributor 3 is positioned under cylindrical shell 7 and with annular space space 67 and is connected, conventionally, annular space gas distributor 3 is positioned at the vertical projection district in annular space space 67, by annular space gas distributor inlet tube 35 with to annular space space 67 air feed.Guide shell gas distributor 11 is positioned under guide shell 6 and stretches out cylindrical shell 7 by guide shell gas distributor inlet tube 35.Guide shell gas distributor 11 is communicated with the internal space of guide shell 6, and conventionally, the vertical projection district that guide shell gas distributor 11 is positioned at guide shell 6 passes through guide shell gas distributor inlet tube 35 with to annular space space 67 air feed.Cone stripped vapor ring 12 is identical or similar with the structure of annular space gas distributor 3, and only the diameter of ring is less.Cone stripped vapor ring 12 passes into loosening wind, so that solid particulate suspends.About annular space gas distributor 3 and guide shell gas distributor 11, be prior art, can adopt the suitable construction of prior art, for example, annular space gas distributor 3 and guide shell gas distributor 11 are annular tube type gas distributor or tubular gas sparger or board-like gas distributor, and the percentage of open area of sparger is 0.5%～3.0%.

Fluidization steam vapor is passed into by annular space gas distributor 3, guide shell gas distributor 11 and cone stripped vapor ring 12 respectively, and is discharged by the pneumatic outlet at top.As shown in Figures 1 to 5, pneumatic outlet is gas outlet tube 9.The first solid particulate admission passage and the second solid particulate admission passage are respectively cold catalyst inlet pipe 5 and thermocatalyst inlet tube 10, and are all connected with annular space space 67.

Further, as shown in Figures 5 to 9, the barrel of guide shell 6 is provided with the internal space of perforate 13, perforate 13 connection annular space spaces 67 and guide shell 6.Catalyzer not only mixes in the upper and lower of guide shell 6, and can mix through hole or groove, thereby has efficient mixed effect.Certainly, on guide shell 6, also can not be provided with perforate 13, but like this not as being provided with mixed heat transfer effective of perforate 13.Perforate 13 on same guide shell is a row or multi-row, and adjacent two rows of openings or fluting are staggered arrangement or non-staggered arrangement, and adjacent two arrange the width of groove and highly equal or unequal, the equal diameters of adjacent two rows of openings or unequal.For perforate, be width and height or the unequal setting of staggered arrangement or adjacent two rows of openings, be more conducive to abundant mixing.

Further, as shown in Figures 5 to 9, perforate 13 is a plurality of long strip shapes holes, and the height of perforate is less than or equal to 0.9 times of guide shell 6 height, and the total area of perforate is less than or equal to the lateral area of the guide shell 6 of 0.9 times; Or perforate is a plurality of circular ports, the radius of perforate is less than or equal to 0.5 times of guide shell 6 height, and the total area of perforate is less than or equal to the lateral area of the guide shell 6 of 0.9 times.The corresponding the first solid particulate of size of perforate and the size of the second solid particulate.

Further, the radial cross-section of guide shell 6 and cylindrical shell 7 is long-pending than being 0.2～0.8.Like this, both can guarantee the useful range in annular space space, also can guarantee that annular space space and guide shell 6 form the space of circulation, circulate to form reasonably.

Further, as shown in Figures 1 to 4, gas-solid loop flow mixing stripper also comprises: cover the end socket 8 at cylindrical shell upper end closed cylinder lumen, wherein, the pneumatic outlet extending in cylindrical shell 7 inner chambers is the gas outlet tube 9 being arranged on end socket 8, guide shell 6 be and be arranged vertically with cylindrical shell 7.This gas-solid loop flow mixing stripper with end socket 8 can complete the first solid particulate and the second solid particulate that mixes differing temps individually, and mixed solid particulate is stripped to flue gas and the air of carrying secretly, realization completes mixing and the steam stripped function of catalyzer in a device, reduced the load of follow-up system pneumatic press, and, conventional regeneration agent flue gas stripping device is interior because regenerator temperature is very high, after contacting with water stripping steam, very easily produce that heat collapses and hydrothermal deactivation, very big to catalyst impairment, but be mixed catalyzer in the mixing stripper that the present invention proposes, temperature is lower, mixing rear catalyst generation heat collapses with the probability of hydrothermal deactivation very low.

Description has above reflected the basic structure of two kinds of gas-solid loop flow mixing strippers of Fig. 1 and Fig. 2, the setting party that two kinds of gas-solid loop flow mixing stripper key distinctions of Fig. 1 and Fig. 2 are the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10 is to being respectively obliquely or oblique downward direction, and other structures are basic identical.Gas-solid loop flow mixing stripper of the present invention can have central gas lift-type and two kinds of operator schemes of annular space gas lifting type.Wherein, for the gas-solid loop flow mixing stripper 100 in Fig. 1, can adopt annular space gas lifting type operator scheme, the gas-solid loop flow mixing stripper 200 in Fig. 2 can adopt central gas lift-type operator scheme.Central gas lift-type operator scheme refers to granules of catalyst (solid particulate) and for making progress, flows in guide shell 6, at guide shell 6 with mix in the annular space of 7 of stripper cylindrical shells and flow downward, annular space gas lifting type operator scheme refer to granules of catalyst in annular space for upwards flowing, in guide shell 6 for flowing downward.When guide shell gas distributor 11 to tolerance be greater than annular space gas distributor 3 give tolerance (referring to flow) time, gas-solid loop flow mixing stripper (also referred to as circulation mixing stripper) operates with central gas lift-type circulating current system, when annular space gas distributor 3 to tolerance be greater than guide shell gas distributor 11 give tolerance time, circulation mixing stripper operates with annular space gas lifting type circulating current system.

Gas-solid loop flow mixing stripping utensil in Fig. 1 has end socket 8 and gas outlet tube 9, the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10 take level or Way in are obliquely connected to the both sides of cylindrical shell 7 and are communicated with annular space space 67, the Way in of the first solid particle inlet pipe 5 and the axis angle α of cylindrical shell 7 are 20 °～90 °, the Way in of the second solid particle inlet pipe 10 and the axis angle of cylindrical shell 7 and be 20 °～90 °.

Now take annular space gas lifting type operator scheme as example explanation:

As shown in Figure 3, annular space gas distributor 3 to tolerance, be greater than the tolerance of giving of guide shell gas distributor 11, cause guide shell bottom to produce pressure difference, promote catalyzer circulates between annular space and guide shell, its flow pattern be catalyzer annular space space 67 interior on flow, when the catalyzer that flows downward in guide shell enters annular space space 67 via cold catalyst inlet pipe 5, thermocatalyst inlet tube 10, there is level or speed obliquely, thereby can not hinder flowing of annular space space 67 inner catalysts.According to the fluidized state of pipe inner catalyst, the inlet tube root of hot and cold catalyzer can be provided with carries airduct 4 so that hot and cold catalyzer enters in annular space space 67 obliquely.Cold, thermocatalyst enters behind annular space space 67, with the catalyst mix rising in annular space and together with upwards flow, enter the gas solid separation district 65 being positioned on guide shell, because the cross-sectional area of gas-solid separator 65 horizontal directions is greater than guide shell or annular space district, therefore gas velocity also reduces greatly, the catalyzer of solid particulate has been realized separated with fluidizing agent or steam, no longer continue to rise, the catalyzer of solid particulate changes flow direction, become macro-flow radially, due to cold, thermocatalyst enters in annular space space 67 from both sides respectively, cold, thermocatalyst goes in the same direction, mix fully, then enter in guide shell and flow downward, at the following space of guide shell sub-fraction catalyzer, enter the cone 2 of bottom and flow out circulation mixing stripper, as shown in Figure 5, cone 2 is shunk gradually, guide shell gas distributor 11 and annular space gas distributor 3 are arranged at the top of cone 2, so most of catalyzer diversed cylinder gas distributor 11 and annular space gas distributor 3 are sent into annular space space 67 and are circulated again, the cone 2 or the sub-fraction catalyzer still less that only have sub-fraction catalyzer to enter bottom by edge enter the cone 2 of bottom and flow out circulation mixing stripper from the bottom of guide shell 6.Catalyzer is after gas solid separation district 65 is mixed, do not reach completely and mix, but form the hot and cold catalyzer group of different sizes, these hot and cold catalyzer are rolled into a ball and are mutually mingled with, the process that enters annular space space 67 by guide shell circulation be one by the hot and cold catalyzer group fragmentation newly assigned process of laying equal stress on, therefore, every through once circulation, hot and cold catalyzer just need to experience mixed once and reallocation.Above-mentioned concrete flow process is as follows:

Cold catalyzer shows as filled arrows C while just having entered annular space space 67 with direction obliquely, due to catalyzer annular space space 67 interior on flow, filled arrows C is divided into filled arrows C1 and C2, filled arrows C1 continue annular space space 67 interior on flow, because guide shell 6 has perforate 13, a part of C2 of filled arrows C enters in guide shell 6 through the perforate 13 of guide shell 6, and flow downward in guide shell 6, the top that filled arrows C1 is raised to annular space space 67 enters the gas solid separation district 65 being positioned on guide shell, no longer continue to rise, the catalyzer of solid particulate changes flow direction, become macro-flow radially, form filled arrows C3, then downward or oblique under enter in guide shell 6.

Meanwhile, thermocatalyst shows as filled arrows d while just having entered annular space space 67 with direction obliquely, due to catalyzer annular space space 67 interior on flow, filled arrows d is divided into filled arrows d1 and d2, filled arrows d1 continue annular space space 67 interior on flow, because guide shell 6 has perforate 13, a part of d2 of filled arrows d enters in the inherent guide shell 6 of guide shell 6 and flows downward through the perforate 13 of guide shell 6, the top that filled arrows d1 is raised to annular space space 67 enters the gas solid separation district 65 being positioned on guide shell, no longer continue to rise, the catalyzer of solid particulate changes flow direction, become macro-flow radially, form filled arrows d3, then downward or oblique under enter in guide shell 6.

In gas solid separation district 65, be in space more than guide shell, filled arrows C3 and filled arrows d3 be macro-flow radially all, there is mixed heat transfer, form filled arrows Cd, then filled arrows Cd flows downward in guide shell 6, during this period, also there is heat exchange in filled arrows Cd and filled arrows C2 and filled arrows d2, filled arrows Cd drops to behind the bottom of guide shell 6, at the following space of guide shell part catalyzer, for example, filled arrows Cd2 enters the cone 2 of bottom and flows out circulation mixing stripper, most of catalyzer, see filled arrows Cd1 circulation enter annular space space 67, again circulate, through recirculation, in cone, form filled arrows Cd3, filled arrows Cd3 also can carry out mixed heat transfer with filled arrows Cd2, then through repeatedly flowing out mixed catalyst particle outlet 2 after circulation.Above-mentioned filled arrows represents each granules of catalyst group, and when hot and cold catalyzer is rolled into a ball heat exchange, annular space gas distributor 3, guide shell gas distributor 11 and cone stripped vapor ring 12 pass into respectively fluidized wind, fluidized wind and loosening wind.Fluidized wind and loosening wind can be steam.The every circulation primary of catalyzer just means with bottom live steam and contacts once, so steam stripping efficiency is also very high.According to experimental result, for the catalyzer that enters guide shell 6 and annular space space 67, owing to having entered sleeve shaped and guide shell 6 with holes, add the effect of annular space gas distributor 3 and guide shell gas distributor 11 and loosening steam ring 12, catalyzer generally will be through 6～15 circulations, mix and reallocate for 6～15 times and could flow out circulation mixing stripper, the catalyzer residence time reaches 143 seconds, so mixed effect is very good.

Central gas lift-type operator scheme take below as example explanation again:

Guide shell gas distributor 11 to tolerance be greater than annular space gas distributor 3 give tolerance time, circulation mixings stripper is with the operation of central gas lift-type circulating current system, its flow pattern is that catalyzer flows downward in annular space, in guide shell on mobile.

As shown in Figure 4, cold catalyzer shows as filled arrows C while just having entered annular space space 67 with the direction under oblique, because catalyzer under central gas lift-type operator scheme flows downward in annular space, in guide shell on flow, filled arrows C is divided into filled arrows C10 and C20, filled arrows C10 flows downward in annular space space 67, to change into behind the bottom in annular space space 67 guide shell 6 interior on flow and form filled arrows C30, because guide shell 6 has perforate 13, the part of cold catalyzer, it is interior to upper mobile formation filled arrows C40 that to be filled arrows C20 enter the inherent guide shell 6 of guide shell 6 through the perforate 13 of guide shell 6, the top that filled arrows C40 is raised to annular space space 67 enters the gas solid separation district 65 being positioned on guide shell, no longer continue to rise, the catalyzer of solid particulate changes flow direction, become macro-flow radially.

Thermocatalyst shows as filled arrows d while just having entered annular space space 67 with the direction under oblique, because catalyzer under central gas lift-type operator scheme flows downward in annular space, in guide shell on flow, filled arrows d is divided into filled arrows d10 and d20, filled arrows d10 flows downward in annular space space 67, to change into behind the bottom in annular space space 67 guide shell 6 interior on flow and form filled arrows d30, because guide shell 6 has perforate 13, a part for cold catalyzer, it is interior to upper mobile formation filled arrows d40 that to be filled arrows d20 enter the inherent guide shell 6 of guide shell 6 through the perforate 13 of guide shell 6, the top that filled arrows d40 is raised to annular space space 67 enters the gas solid separation district 65 being positioned on guide shell, no longer continue to rise, the catalyzer of solid particulate changes flow direction, become macro-flow radially.

Wherein, in 67 bottoms, annular space space, filled arrows C30 mixes with filled arrows d30, a mixed solid particulate part flows downward and enters cone 2, form filled arrows Cd10, a part of solid particulate forms filled arrows Cd20 to flowing above guide shell 6 under the circulation effect of guide shell 6.In the gas solid separation district 65 being positioned on guide shell, filled arrows C40 and filled arrows d40 meet, mix mutually, form filled arrows Cd30, in repeatedly circulating, filled arrows Cd30 flows downward respectively in annular space space 67, and meet with filled arrows C10 and filled arrows d10 respectively, mutual mixed heat transfer, form filled arrows Cd50 and filled arrows Cd40, a part of filled arrows Cd50 and filled arrows Cd40 continues circulation, upwards enter guide shell, another part of filled arrows Cd50 and filled arrows Cd40 enters cone 2 downwards, form respectively filled arrows Cd60 and filled arrows Cd70, and with filled arrows Cd10 mixed heat transfer, then flow out mixed catalyst particle outlet 2.

Above-mentioned filled arrows represents each granules of catalyst group, and when hot and cold catalyzer is rolled into a ball heat exchange, annular space gas distributor 3, guide shell gas distributor 11 and cone stripped vapor ring 12 pass into respectively fluidized wind, fluidized wind and loosening wind.Fluidized wind and loosening wind can be steam.The every circulation primary of catalyzer just means with bottom live steam and contacts once, so steam stripping efficiency is also very high.For the gas-solid loop flow mixing stripper shown in Fig. 2, except adopting the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10 to be connected to the mode of the both sides of cylindrical shell 7, can also make the first solid particle inlet pipe 5 be connected to the side direction of cylindrical shell 7, the second solid particle inlet pipe 10 is connected to the top of cylindrical shell 7, and blended solid particle outlet 1 is connected with pre lift zone; Or the first solid particle inlet pipe 5 is connected to the top of cylindrical shell 7, the second solid particle inlet pipe 10 is connected to the side direction of cylindrical shell 7, and blended solid particle outlet 1 is connected with pre lift zone.

Figure 10 is that wherein revivifier and settling vessel 90 are coaxially arranged according to the structure of the first catalytic cracking reaction regeneration system rapidly of the embodiment of the present invention.The first catalytic cracking reaction regeneration system rapidly as shown in figure 10 can adopt the gas-solid loop flow mixing stripper 100 in Fig. 1, also can adopt the gas-solid loop flow mixing stripper 200 in Fig. 2, all can complete separately mixing and the steam stripped function of catalyzer, with alleviate upstream and downstream operation burden and and upstream and downstream operation cooperatively interact.The setting party that two kinds of gas-solid loop flow mixing stripper key distinctions of Fig. 1 and Fig. 2 are the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10 is to being respectively obliquely or oblique downward direction, and other structures are basic identical.

As shown in figure 10, the gas-solid loop flow mixing stripper 200 of take in employing Fig. 2 is example, catalytic cracking reaction regeneration system rapidly comprises: riser reactor 40, pre lift zone 30, revivifier 60, and gas-solid loop flow mixing stripper 200 is arranged on outside riser reactor 40, pre lift zone 30 and revivifier 60; The first solid particulate admission passage is the first solid particle inlet pipe 5, the second solid particulate admission passage is the second solid particle inlet pipe 10, the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10 are connected to the both sides of cylindrical shell 7 and are all communicated with annular space space, and blended solid particle outlet 1 is connected with pre lift zone.

Further, as shown in Figure 2, the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10 take level or oblique downward direction to be connected on cylindrical shell 7, the first solid particle inlet pipe 5 is 20 °～90 ° with the axis angle γ of cylindrical shell 7, and the second solid particle inlet pipe 10 is 20 °～90 ° with the axis angle λ of cylindrical shell 7.This mode has been utilized the self gravitation of solid particulate, directly enters into annular space space 67, without carrying the auxiliary of airduct 4.

Gas-solid loop flow mixing stripper 200 is arranged on the place near revivifier 60 regenerator outlets, gas-solid loop flow mixing stripper 200 is connected by transfer lime (thermocatalyst pipe) 16 with revivifier 60, is connected by transfer lime pipeline (14) with revivifier heat collector 70.By revivifier 60, draw one high-temperature regenerated catalyst and enter gas-solid loop flow mixing stripper (be called for short and mix stripper) 200 via thermocatalyst pipe 16, by revivifier heat collector 60 bottoms, draw one cold regenerated catalyst and enter mixing stripper via pipeline 14, cold catalyst flow is controlled by the guiding valve being arranged on pipeline 14, and thermocatalyst flow is controlled by the guiding valve being arranged on pipeline 16.Fluidization steam vapor is passed into by annular space gas distributor, guide shell gas distributor and cone stripped vapor ring respectively, and by the gas outlet tube 9 at top, is drained into dilute phase pipe and enters revivifier dilute phase again.Cold and hot catalyzer mixes within mixing stripper, by mixing stripper bottom, draw after heat transfer, stripping, enters riser reactor 40 after entering pre lift zone 30 via regeneration pipeline (regenerator sloped tube) 50.Regeneration pipeline is comprised of multistage standpipe, inclined tube conventionally, and mixed catalyst can repeatedly turn to while flowing in regenerator pipeline, has also further promoted the mixing between catalyzer.The residence time of catalyzer in technical scale circulation mixing stripper is long considerably beyond the residence time of mixing at pre lift zone.

In Figure 10, adopted the gas-solid loop flow mixing stripper in Fig. 2, certainly, gas-solid loop flow mixing stripper 100 in Fig. 1 also can be applied in the catalytic cracking reaction regeneration system rapidly shown in Figure 10, but will take level or Way in to be obliquely connected on cylindrical shell 7 the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10.For example, the Way in of the first solid particle inlet pipe 5 and the axis angle α of cylindrical shell 7 are 20 °～90 °, and the Way in of the second solid particle inlet pipe 10 and the axis angle β of cylindrical shell 7 are 20 °～90 °.The specific works principle of the gas-solid loop flow mixing stripper 100 in Fig. 1 can be with reference to the description of figure 3.

Further, as shown in Figure 1, the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10 are symmetrical arranged about the axis of cylindrical shell 7, and the first solid particulate and the second solid particulate mix more even like this.In the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10, be respectively arranged with and carry airduct 4, the defeated wind direction of the conveying airduct in the first solid particle inlet pipe 5 is identical with the Way in of the first solid particle inlet pipe 5, and the defeated wind direction of the conveying airduct in the second solid particle inlet pipe 10 is identical with the Way in of the second solid particle inlet pipe 10.By the impact of carrying airduct 4 to make two kinds of solid particulates can overcome gravity, according to the direction obliquely of design, enter into annular space space 67 in the situation that the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10 are level or arrange obliquely.

Certainly, the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10 are symmetrical arranged just a preferred embodiment of the present invention about the axis of cylindrical shell 7, the first solid particle inlet pipe 5 of the present invention and the second solid particle inlet pipe 10 are not that axis about cylindrical shell 7 is symmetrical arranged yet, for example, the first solid particle inlet pipe 5 and the asymmetric both sides that are arranged on cylindrical shell 7 of the second solid particle inlet pipe 10, or, the first solid particle inlet pipe 5 is connected to the side direction of cylindrical shell 7, the second solid particle inlet pipe 10 is connected to the top of cylindrical shell 7, blended solid particle outlet 1 is connected with pre lift zone, or the first solid particle inlet pipe 5 is connected to the top of cylindrical shell 7, the second solid particle inlet pipe 10 is connected to the side direction of cylindrical shell 7, and blended solid particle outlet 1 is connected with pre lift zone.Like this, can, according to actual equipment layout situation, the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10 be connected on cylindrical shell 7 flexibly.

The mode of operation of the catalytic cracking reaction regeneration system rapidly in Figure 10 is once described below, i.e. the cold regenerated catalyst circulation means of this catalytic cracking reaction regeneration system rapidly:

Gas-solid loop flow mixing stripper (be called for short circulation mixing stripper or mix stripper) 200 is put the place at the regenerator outlet near revivifier 60, circulation mixing stripper 200 is connected by transfer lime (thermocatalyst pipe) 16 with revivifier 60, is connected by transfer lime (being also called for short pipeline) 14 with revivifier heat collector 70.By revivifier, draw one high-temperature regenerated catalyst (the second solid particulate) and enter gas-solid loop flow mixing stripper 200 via thermocatalyst pipe 16, another part flows out revivifier; By heat collector 70 bottoms outside revivifier, draw one cold regenerated catalyst (the first solid particulate) and enter mixing stripper via pipeline 14, another part cold regenerated catalyst returns to revivifier, in order to regulate the temperature of revivifier, cold catalyst flow is controlled by the guiding valve being arranged on pipeline 14.Fluidization steam vapor is passed into by annular space gas distributor 3, guide shell gas distributor 11 and cone stripped vapor ring respectively, and enters revivifier dilute phase by the dilute phase pipe 80 (dilute phase pipe 80 is communicated with gas outlet tube 9) at top.Cold and hot catalyzer mixes within mixing stripper, by mixing stripper bottom, draw after heat transfer, stripping, for example, via regeneration pipeline 50 (being regenerator sloped tube), enters riser reactor 40.The temperature of mixing rear catalyst is controlled according to the ratio that flows out the high temperature regeneration agent flux of revivifier and the low-temp recovery agent flux of outflow heat collector, or by regulating the temperature of regenerator temperature and/or outflow heat collector catalyzer to control.The first solid particulate (low-temp recovery agent) and the mixed temperature of the second solid particulate (high temperature regeneration agent) are controlled according to the ratio that flows out the flow of the second solid particulate of revivifier and the flow of the first solid particulate of outflow heat collector; for example; the flow of hot and cold catalyzer all can be controlled by the guiding valve on hot and cold catalyst transport (pipeline); or by the temperature that regulates regenerator temperature and/or flow out the first solid of heat collector, control, the first solid particulate and the mixed temperature of the second solid particulate are 550 ℃～680 ℃.

Because regenerator pipeline in actual production is comprised of multistage standpipe, inclined tube conventionally, mixed catalyst can repeatedly turn to while flowing in regenerator pipeline, has also further promoted the mixing between catalyzer.

Figure 12 is according to the structure of the second catalytic cracking reaction regeneration system rapidly of the embodiment of the present invention, i.e. the reconstituted form of catalytic cracking is the close combined forms of burning tank-bis-.This embodiment seldom narrate with the something in common of embodiment Figure 10, the key distinction has: burning tank outlet is dilute phase pipe or macropore grid distributor.For guaranteeing to enter the catalyzer of circulation mixing stripper, be the catalyzer of holomorphosis, the thermocatalyst of heat collector is introduced by two close phases 61, cooling rear portion is returned to burning tank 63, a part enters circulation mixing stripper, the thermocatalyst of circulation mixing stripper is introduced by two close phases 61, after hot and cold catalyzer mixes in circulation mixing stripper, via regenerator pipeline, enter riser tube, wherein, the flow of hot and cold catalyzer all can be controlled by the guiding valve on hot and cold catalyst transport (pipeline).The gas-solid loop flow mixing stripper adopting about Figure 12, can adopt the gas-solid loop flow mixing stripper 100 in Fig. 1, also can adopt the gas-solid loop flow mixing stripper 200 in Fig. 2, operating method can adopt accordingly as front employing central gas lift-type and annular space gas lifting type, and specific works principle and catalyst recirculation mode can be with reference to the catalytic cracking reaction regeneration system rapidlys of Figure 10.

Figure 13 is according to the structure of the 4th of the embodiment of the present invention the kind of catalytic cracking reaction regeneration system rapidly, adopts the catalytic cracking form of two-stage riser.This embodiment seldom narrate with the something in common of embodiment Figure 10, the key distinction has: revivifier 60 is provided with a heat collector 70, a heat collector 70 bottoms low temperature catalyst part is out returned to revivifier 60, another part low temperature catalyst is introduced two circulation mixing strippers 200 via transfer lime 14, and cold catalytic amount is controlled by the guiding valve being arranged on catalyst tube transfer lime 14.Thermocatalyst is by drawing in revivifier 60, via catalyst tube transfer lime 16a or 16b, enter respectively in a circulation mixing stripper, and with cold catalyst mix, wherein, the flow of hot and cold catalyzer all can be controlled by the guiding valve on hot and cold catalyst transport (pipeline), and circulation mixing stripper outlet at bottom is connected with two riser tubes.This embodiment is arranged comparatively flexible, can to the catalyst recirculation amount of each riser tube, control according to processing requirement.Certainly, this embodiment is not limited to two catalytic cracking reaction regeneration system rapidlys that also can be used for many riser tubes.The 4th kind of catalytic cracking reaction regeneration system rapidly can adopt the gas-solid loop flow mixing stripper 100 in Fig. 1, also can adopt the gas-solid loop flow mixing stripper 200 in Fig. 2, operating method can adopt accordingly as front employing central gas lift-type and annular space gas lifting type, and specific works principle and catalyst recirculation mode can be with reference to the catalytic cracking reaction regeneration system rapidlys of Figure 10.

Figure 14 is according to the structure of the 5th of the embodiment of the present invention the kind of catalytic cracking reaction regeneration system rapidly, adopts the catalytic cracking form of two-stage regeneration.This embodiment seldom narrate with the something in common of embodiment Figure 10, the key distinction has: revivifier comprises: divide the first revivifier 601 and the Second reactivator 602 that are arranged, heat collector 70 is connected with the first revivifier 601, reclaimable catalyst is introduced into the first revivifier 601, at the first revivifier 601, burn part Jiao and become half regenerator, a part is flowed out to enter Second reactivator 602 and in Second reactivator, burn remaining Jiao by the first revivifier 601 bottoms and forms the second solid particulate, another part out forms the first solid particulate from heat collector bottom, the second solid particulate is the catalyzer of the holomorphosis of high temperature, the first solid particulate is half regenerated catalyst of low temperature, the catalyzer of the holomorphosis of the high temperature of being drawn by Second reactivator also strips with half regenerated catalyst mixed heat transfer gas-solid loop flow mixing stripper 200 of the low temperature of drawing from heat collector flue gas and the air of carrying secretly simultaneously, wherein, cold, the flow of thermocatalyst all can be by cold, guiding valve on thermocatalyst transfer lime (pipeline) is controlled.The advantage of this embodiment is, between general two revivifiers, all leaves larger space, thus embodiment 4 is installed, comparatively easy during construction.

Further, as shown in figure 11, the present invention also proposes the third gas-solid loop flow mixing stripper 300.This gas-solid loop flow mixing stripper 300 is with the key distinction of first two: gas-solid loop flow mixing stripper 300 is not arranged on outside riser reactor 40, pre lift zone 30 and revivifier 60, but within gas-solid loop flow mixing stripper 300 is arranged on revivifier 60.The top of the cylindrical shell 7 of gas-solid loop flow mixing stripper 300 does not arrange end socket 8 and gas outlet tube 9, the inner chamber of revivifier 60 is directly communicated with the top of cylindrical shell 7, cold catalyzer is introduced by the first solid particle inlet pipe, the first solid particle inlet pipe extend into the side direction of cylindrical shell 7 and is communicated with annular space space from the outside of revivifier, heat (regeneration) catalyzer directly enters into guide shell 6 from cylindrical shell 7 by cylindrical shell 7 tops, thereby without thermocatalyst inlet tube 10 is set.Elsewhere, for example the structure of cylindrical shell 7, guide shell 6, annular space gas distributor 3, guide shell gas distributor 11 and cone stripped vapor ring 12 still can adopt the structure in Fig. 1 and Fig. 2.

Figure 11 has also illustrated according to structure and the mode of operation of the catalytic cracking reaction regeneration system rapidly of the embodiment of the present invention.Further, gas-solid loop flow mixing stripper 300 cylindrical shells 7 are surrounded jointly by the inner side wall of revivifier and the arc of a side, reduce like this cost of manufacture, make full use of the inner side wall of original revivifier.This gas-solid loop flow mixing stripper 300 is arranged on the pattern that catalytic cracking reaction regeneration system rapidly within revivifier 60 is applicable to conventional single revivifier.Circulation mixing stripper is arranged on internal regenerator regenerator and extracts mouth out, and mixed catalyzer enters circulation mixing stripper bottom, via regeneration pipeline 50, enters riser tube bottom.

This gas-solid loop flow mixing stripper 300 that end socket 8 and gas outlet tube 9 are not set is by annular space gas distributor 3, the inner chamber that the fluidizing agent that guide shell gas distributor 11 and cone stripped vapor ring 12 are used or steam enter revivifier 60, this gas-solid loop flow mixing stripper 300 can adopt central gas lift-type operator scheme, heat (regeneration) catalyzer directly enters into guide shell 6 from cylindrical shell 7 by cylindrical shell 7 tops, the first solid particle inlet pipe 5 extend into the side direction of cylindrical shell 7 and enters into annular space space 67 from the outside of revivifier, according to the central gas lift-type operator scheme of introducing above, circulate, in guide shell 6, solid particulate flow direction is upwards, in annular space space, solid particulate flow direction is downward.

The advantage of this embodiment is: (1), when site layout project space is not or during insufficient height, is placed on internal regenerator by circulation mixing stripper, can save large quantity space; (2) do not need catalyst recycle line to transform, thereby install and overhaul very simply, the operation of device is also very simple; (3) circulation mixing stripper is placed on to internal regenerator, not only do not increase the resistance to flow of regeneration circuit, because extract mouth out at regenerator, be provided with circulation mixing stripper on the contrary, played the effect of flooding stream bucket that is similar to, increase regenerator pressure accumulation, increased the mobile impellent of regenerator.Maximization gradually along with device, more than the diameter of catalytic cracking regenerator can reach 10m, 300 of gas-solid loop flow mixing strippers have occupied very little a part of space (cross-sectional area accounts for that revivifier cross-sectional area is no more than 5%, volume be no more than 2.5%), and the regeneration effect of revivifier is not had to impact substantially.

The present invention compared with prior art has obvious advantage and useful effect:

(1) the catalyzer heat collector that utilizes current conventional catalytic cracking to be all equipped with, from heat collector bottom, draw one cold regenerator, the thermocatalyst coming with revivifier evenly mixes for a long time in mixing tank, and utilize the further mixing of mobile realization in regeneration pipeline and conduct heat, guaranteed the even mixing and abundant heat transfer of hot and cold catalyzer completely.The present invention only need to arrange separately one and mix stripper, and by heat collector to the catalyst line that mixes stripper, and the long-pending relative riser reactor of gas-solid loop flow mixing stripping body, pre lift zone and revivifier are all very little, take up an area little, the change amount of getting up to work is little, without the extensive catalyst cracker of changing, shorten the scrap build time, reduce and change cost.

(2) on the guide shell of circulation mixing stripper, have hole or groove, catalyzer not only mixes in the upper and lower of guide shell, and can mix through hole or groove, thereby has efficient mixed effect;

(3) in actual production, regenerator pipeline is comprised of multistage standpipe, inclined tube conventionally, and mixed catalyst can repeatedly turn to while flowing in regenerator pipeline, has also further promoted mixing and heat transfer between catalyzer.

(4) residence time of mixed catalyst before mixing stripper, regenerator pipeline and pre lift zone, riser tube nozzle amounts to and reaches several minutes, fully guaranteed the heat transfer time of hot and cold catalyzer.

(5) when fluidizing medium adopts steam, can effectively strip the flue gas of carrying secretly in catalyzer, reduce the load of follow-up system pneumatic press.

(6) conventional regeneration agent flue gas stripping device is interior because regenerator temperature is very high, after contacting with water stripping steam, very easily produce that heat collapses and hydrothermal deactivation, very big to catalyst impairment, but be mixed catalyzer in the gas-solid loop flow mixing stripper (referred to as circulation mixing stripper) that the present invention proposes, temperature is lower, and catalyzer heat occurs and collapses with the probability of hydrothermal deactivation very low.

(7) circulation mixing stripper of the present invention has not only been realized stripping in two kinds of solid particulate heat exchange; and because two kinds of solid particulates hot and cold solid particulate (catalyzer) group when the mixed heat transfer is broken and redistribute; this has brought more multimachine meeting to the displacement of flue gas in catalyzer micropore; and every circulation primary just means live steam contact once; also make the vapor bubbles rising be sheared; greatly reduce bubble diameter; vapor bubbles is more easily entered or approach catalyzer micropore, so steam stripping efficiency is higher than the efficiency of other strippers.

(8) the present invention can regulate respectively control to the temperature of cold catalyst inlet pipe 5 and thermocatalyst inlet tube 10 and flow, both can obtain entering the ideal temperature of pre lift zone, can obtain sufficient flow again, setting range is very extensive, and the mixed catalyzer that simultaneously guarantees temperature and flow can be provided flexibly.

The foregoing is only the schematic embodiment of the present invention, not in order to limit scope of the present invention.For each integral part of the present invention can mutually combine under the condition of not conflicting, any those skilled in the art, not departing from equivalent variations and the modification of having done under the prerequisite of design of the present invention and principle, all should belong to the scope of protection of the invention.

Claims

1. a catalytic cracking reaction regeneration system rapidly, described catalytic cracking reaction regeneration system rapidly comprises: riser reactor, pre lift zone, revivifier and be arranged on the heat collector outside described revivifier, it is characterized in that,

Described catalytic cracking reaction regeneration system rapidly also comprises: be arranged on the gas-solid loop flow mixing stripper outside riser reactor and pre lift zone, described gas-solid loop flow mixing stripper mixes the first solid particulate and the second solid particulate of differing temps for fluid catalytic cracking process, and stripping flue gas and the air that the first solid particulate and the second solid particulate are carried secretly, the temperature of the second solid particulate is higher than the temperature of the first solid particulate;

Described gas-solid loop flow mixing stripper comprises: the cylindrical shell (7) with inner chamber, be arranged in the inner chamber of described cylindrical shell and the guide shell (6) coaxially arranged with described cylindrical shell, be positioned at the annular space gas distributor (3) of the bottom, annular space space between described cylindrical shell (7) and described guide shell (6), be arranged in described cylindrical shell and be positioned at the guide shell gas distributor (11) under described guide shell (6), extend into the pneumatic outlet in described cylindrical shell (7) inner chamber, described cylindrical shell (7) lower end is connected with cone (2), be arranged on the blended solid particle outlet (1) of described cone (2) below, be positioned at cone (2) bottom and the cone stripped vapor ring (12) in blended solid particle outlet (1) top, and be connected respectively to the first solid particulate admission passage and the second solid particulate admission passage in the inner chamber of described cylindrical shell, the first solid particulate admission passage connects described heat collector, the second solid particulate admission passage connects described revivifier,

Wherein, the inner chamber of described cylindrical shell (7) comprising: the internal space of described annular space space and described guide shell (6), described annular space gas distributor (3) is that the perforate of annular tube type gas distributor and annular space gas distributor (3) is connected with described annular space space, and described guide shell gas distributor (11) is positioned under described guide shell (6) and the perforate of guide shell gas distributor (11) is communicated with the internal space of described guide shell (6);

Described guide shell (6) is 0.2～0.8 with the horizontal direction cross-sectional area ratio of described cylindrical shell (7), the barrel of described guide shell (6) is provided with perforate (13), described perforate (13) is communicated with the internal space of described annular space space and guide shell (6), described perforate is a plurality of long strip shapes holes, the height of described perforate is less than or equal to 0.9 times of described guide shell (6) height, and the total area of described perforate is less than or equal to the lateral area of the guide shell 6 of 0.9 times; Or described perforate is a plurality of circular ports, the radius of described perforate is less than or equal to 0.5 times of guide shell (6) height, the total area of described perforate is less than or equal to the lateral area of the guide shell 6 of 0.9 times, and gas-solid loop flow mixing stripper bottom is connected with pre lift zone or riser reactor bottom.

2. catalytic cracking reaction regeneration system rapidly as claimed in claim 1, is characterized in that, described gas-solid loop flow mixing stripper is arranged on outside riser reactor, pre lift zone and described revivifier; Described the first solid particulate admission passage is the first solid particle inlet pipe (5), described the second solid particulate admission passage is the second solid particle inlet pipe (10), the first solid particle inlet pipe (5) and the second solid particle inlet pipe (10) are connected to the both sides of described cylindrical shell (7) and are all communicated with described annular space space, and described blended solid particle outlet (1) is with described pre lift zone or be directly connected with riser reactor; Described cylindrical shell (7) upper end is internally connected with end socket (8), wherein, the described pneumatic outlet extending in described cylindrical shell (7) inner chamber is that the described gas-solid loop flow mixing of gas outlet tube (9) stripper being arranged on end socket (8) also comprises: end socket (8) and gas outlet tube (9), described guide shell (6) is and is arranged vertically with cylindrical shell (7).

3. catalytic cracking reaction regeneration system rapidly as claimed in claim 1, it is characterized in that, within described gas-solid loop flow mixing stripper is arranged on described revivifier, described cylindrical shell (7) is surrounded jointly by the inner side wall of revivifier and the arc of a side, the top of described cylindrical shell is uncovered, and the inner chamber of described cylindrical shell is directly communicated with the inner chamber of described revivifier;

Described the first solid particulate admission passage is the first solid particle inlet pipe (5), described the first solid particle inlet pipe (5) extend into the side direction of described cylindrical shell (7) and is communicated with described annular space space, the described the second solid particulate of the uncovered formation admission passage at the inner chamber of described revivifier and the top of described cylindrical shell from the outside of described revivifier.

4. catalytic cracking reaction regeneration system rapidly as claimed in claim 2, is characterized in that, described the first solid particle inlet pipe (5) is connected with heat collector, and described the second solid particle inlet pipe (10) is connected with described revivifier.

5. catalytic cracking reaction regeneration system rapidly as claimed in claim 2, it is characterized in that, described revivifier comprises: interconnective burning tank and two close phases, described the first solid particle inlet pipe (5) is connected with heat collector, described the second solid particle inlet pipe (10) and described two close being connected.

6. catalytic cracking reaction regeneration system rapidly as claimed in claim 2, it is characterized in that, described catalytic cracking reaction regeneration system rapidly comprises: a plurality of described riser reactors, a plurality of described pre lift zones, a described revivifier, a plurality of described gas-solid loop flow mixing strippers, and line of pipes, on described revivifier, be provided with one or more heat collectors, each pre lift zone is a corresponding riser reactor and the described gas-solid loop flow mixing stripper of connecting one to one, described the second solid particle inlet pipe (10) is connected with described revivifier, described in each, the blended solid particle outlet (1) of circulation mixing stripper is man-to-man is respectively connected with a pre lift zone,

Described in each, the first solid particle inlet pipe (5) of circulation mixing stripper is connected on a heat collector jointly, or the first solid particle inlet pipe (5) man-to-man being connected on a heat collector respectively of circulation mixing stripper described in each.

7. catalytic cracking reaction regeneration system rapidly as claimed in claim 2, it is characterized in that, described revivifier comprises: divide the first revivifier and the Second reactivator that are arranged, described heat collector is connected with the first revivifier, described the first solid particle inlet pipe (5) is connected with described heat collector, described the second solid particle inlet pipe (10) is connected with described Second reactivator, and described circulation mixing stripper is between the first revivifier and Second reactivator.

8. a cold regenerated catalyst circulation means, fluid catalytic cracking process for reconstituted form mixes the first solid particulate and the second solid particulate of differing temps, and strip flue gas and the air that the first solid particulate and the second solid particulate are carried secretly simultaneously, the first solid particulate is low temperature catalyst or low temperature half regenerator, the second solid particulate is high temperature catalyst, the temperature of the second solid particulate is higher than the temperature of the first solid particulate, described cold regenerated catalyst circulation means completes by catalytic cracking reaction regeneration system rapidly, described catalytic cracking reaction regeneration system rapidly comprises: riser reactor, the pre lift zone being connected with riser reactor, revivifier and line of pipes, described revivifier is outside equipped with heat collector, it is characterized in that,

From the first solid particulate of described heat collector, also strip with the second solid particulate mixed heat transfer in gas-solid loop flow mixing stripper as claimed in claim 1 from described revivifier flue gas and the air of carrying secretly simultaneously, after formation mixed catalyst, enter described pre lift zone.

9. cold regenerated catalyst circulation means as claimed in claim 8, is characterized in that, described gas-solid loop flow mixing stripper is arranged on outside riser reactor, pre lift zone and described revivifier; By the first solid particulate and the second solid particulate level or be transported to obliquely in annular space space, what make described annular space gas distributor (3) is greater than the tolerance of giving of described guide shell gas distributor (11) to tolerance, make the first solid particulate and the second solid particulate in described annular space for upwards flowing, in described guide shell (6) for flowing downward;

A part of the second solid particulate from described regeneration in-situ regeneration enters the cooling formation the first of heat collector solid particulate, and another part the second solid particulate flows out revivifier; The a part of the first solid particulate flowing out from described heat collector returns to revivifier, and another part the first solid particulate flowing out from described heat collector carries out mixed heat transfer and stripping with the described another part the second solid particulate flowing out from revivifier.

10. cold regenerated catalyst circulation means as claimed in claim 8, is characterized in that, described gas-solid loop flow mixing stripper is arranged on outside riser reactor, pre lift zone and described revivifier; By the first solid particulate and the second solid particulate level or oblique under be transported in described annular space space, what make described annular space gas distributor (3) is less than the tolerance of giving of described guide shell gas distributor (11) to tolerance, make the first solid particulate and the second solid particulate in described annular space space for flowing downward, in described guide shell (6) for upwards flowing;

11. cold regenerated catalyst circulation meanss as claimed in claim 8, is characterized in that, within described gas-solid loop flow mixing stripper is arranged on to described revivifier, the top of described cylindrical shell is uncovered, and the inner chamber of described cylindrical shell is directly communicated with the inner chamber of described revivifier;

Described the first solid particulate level or oblique under enter described annular space space, the second solid particulate directly enters into the top of cylindrical shell (7) and the top of guide shell (6) from the inner chamber of described revivifier, what make described annular space gas distributor (3) is less than the tolerance of giving of described guide shell gas distributor (11) to tolerance, make the first solid particulate and the second solid particulate in described annular space space for flowing downward, in described guide shell (6) for upwards flowing;

A part of the second solid particulate from described regeneration in-situ regeneration enters the cooling formation the first of heat collector solid particulate, and another part the second solid particulate enters into the top of cylindrical shell (7) and the top of guide shell (6); The a part of the first solid particulate flowing out from described heat collector returns to revivifier, another part the first solid particulate flowing out from described heat collector with from entering into the second solid particulate at the top of cylindrical shell (7) and the top of guide shell (6), carry out mixed heat transfer and stripping.

12. cold regenerated catalyst circulation meanss as claimed in claim 8, it is characterized in that, described revivifier comprises: divide the first revivifier and the Second reactivator that are arranged, described heat collector is connected with the first revivifier, reclaimable catalyst is introduced into the first revivifier, at the first revivifier, burn burnt half regenerated catalyst that forms of part, a part is flowed out by the first regenerator bottoms, enter Second reactivator and in Second reactivator, burn remaining burnt the second solid particulate that forms, another part out forms the first solid particulate from heat collector bottom, the catalyzer of the holomorphosis that described the second solid particulate is high temperature, half regenerated catalyst that described the first solid particulate is low temperature, the catalyzer of the holomorphosis of the high temperature of being drawn by Second reactivator also strips with half regenerated catalyst mixed heat transfer described gas-solid loop flow mixing stripper of the low temperature of drawing from heat collector flue gas and the air of carrying secretly simultaneously.

13. cold regenerated catalyst circulation meanss as claimed in claim 8; it is characterized in that; the first solid particulate and the mixed temperature of the second solid particulate are controlled according to the ratio that flows out the flow of the second solid particulate of revivifier and the flow of the first solid particulate of outflow heat collector; or by the temperature that regulates regenerator temperature and/or flow out the first solid of heat collector, control, the first solid particulate and the mixed temperature of the second solid particulate are 550 ℃～680 ℃.

14. cold regenerated catalyst circulation meanss as claimed in claim 8, it is characterized in that, the temperature of reaction of riser reactor is according to the internal circulating load of mixed the first solid particulate and the second solid particulate, or the temperature of mixed the first solid particulate and the second solid particulate or stock oil flow or the adjusting of fuel oil preheating temperature.