CN102649912A - Circulating method for cold regenerated catalyst and catalytic cracking reaction regenerating system - Google Patents

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 the fluid catalytic cracking process; Particularly; Relate to a kind of cold regenerated catalyst circulation means and catalytic cracking reaction regeneration system rapidly, be used for the stripping of the solid particulate in the mixing and mix of two kinds of catalyzer (between the regenerator and/or between the spent agent) of differing temps between fluid catalytic cracking process riser tube and the fluidized-bed.

Background technology

The catalytic cracking reaction regeneration system rapidly is made up of riser reactor, revivifier and line of pipes usually.Raw oil through nozzle atomization after; In riser reactor, contact, gasify, take place heat cracking reaction and catalyzed reaction with high-temperature regenerated catalyst; Condensation reaction meanwhile takes place and produce coke; Coke makes catalyst deactivation attached to catalyst surface, and the catalyzer of inactivation (spent agent) is separated the back in the riser tube outlet by gas-solid separation equipment and gets into stripping stage, and spent agent entrained oil gas is replaced away by stripped vapor in stripping stage; Spent agent gets into the revivifier regeneration of burning through pipeline to be generated then, and the catalyzer after the regeneration (regenerator) gets into bottom the riser tube through the regeneration pipeline.

Agent-oil ratio is the catalytic cracking most important control parameters, has reflected the mass flux ratio of catalyzer with oil.Under same processing condition, suitable bigger agent-oil ratio means that raw oil can touch more high activated catalyst, more in other words active site, thereby also have higher product yield and selectivity.But in actual production, the internal circulating load of catalyzer can not regulated at will because of receiving thermally equilibrated restriction.Increase the internal circulating load of regenerator and keep the total heat of bringing reactive system into constant, can only reduce the regenerator temperature.This often means the regeneration temperature that reduces revivifier in actual production, 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 can't take into account.For this reason, people have proposed various technology to address this problem.

At present, in the fluid catalytic cracking process, cold catalyst recirculation technology can be divided into following several types: (1) is directly mixed (patent 01144955.1 with cold spent agent with the high temperature regeneration agent in riser tube or in the pre lift zone; 201020608020.4); But, contain many spent agents in the mixed catalyzer, thereby activity is lower owing to there is not follow-up step for regeneration; Can reduce nozzle place activity of such catalysts like this, and then influence product yield.(2) do not carry out the mixing of hot and cold catalyzer; But regenerator is directly cooled off: on the regeneration circuit, heat collector is set, heat collector refrigerative catalyzer is introduced riser tube, but because the total heat that heat collector is taken away is a definite value; If guarantee certain from the temperature of the effusive refrigerative catalyzer of heat collector; Then can not satisfy the requirement of catalyst flow adjustment, in like manner, if guarantee certain from the flow of the effusive refrigerative catalyzer of heat collector; Then can not satisfy the requirement of catalyst temperature adjustment; So its catalyst flow is not an independent variable, be difficult to regulate (patent 99120517.0), and if build a heat collector again then flow process is complicated, the improvement project amount big, leave than large space (patent 200810146601.8) on the fluidisation difficulty of transportation, the circuit that needs to regenerate.(3) with the mixing tank (patent 99120529.4,200710054772,200510017751.5) of riser tube bottom pre lift zone as cold and hot regenerated catalyst.Though this technology is that regenerated catalyzer is mixed; Need not regenerated process like the required catalyzer of (1) kind situation; But high to the structural requirement of pre lift zone like this, cause the complex structure, cost of pre lift zone to increase, and in the pre lift zone mixing time and heat transfer time all very short; Even if cold and hot catalyzer can mix, there is not time enough to conduct heat yet.。

For example; Plant on the basis of mode above-mentioned (3); Prior art has following special patent to hot and cold catalyst mix device: the pre lift zone mixing tank that patent 200710054772.3 is adopted is the direct tube section of a diameter greater than riser tube; Direct tube section top links to each other with riser tube with a conical section, but any inner member is not adopted in pre lift zone inside.The pre lift zone internal mixer that patent 200510017751.5 adopts is provided with the steam gas sparger, but does not have other inner members.Can find out in the pre lift zone mixing tank that patent 200710054772.3 and patent 200510017751.5 adopted that all setting can not promote the blended inner member; Just rely on hot and cold catalyzer mixing naturally in fluidized-bed; Because catalyzer residence time in pre lift zone is very short; Thereby the catalyst mix effect is relatively poor, and because the flow of hot and cold catalyzer is generally different, is easy to cause the bias current in the 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 barrel inner sleeve is set, and each catalyst inlet pipe below is provided with the channel base plate under the screw.This patent can realize the particulate mixing preferably, but mobile comparatively complicacy, the resistance to flow of hot and cold catalyzer in pre lift zone is bigger, thereby influences mixed effect, and the channel base plate under the screw is difficult for installation, also easy deformation.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; Be arranged to the hydraucone of back taper with promoting the media outlet pipe; The pre lift zone outlet is provided with the baffling tube; The center that forms in the lifting process is rare to destroy, the nucleolus fluidal texture of Bian Binong, impels radially uniform distribution of granule density, but this patent exists catalyst mix, heat transfer time to lack, mix and the uneven 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, exists cold and hot catalyst mix, heat transfer time to lack, mix and the uneven problem of conducting heat to solve prior art.Simultaneously, the present invention has also solved prior art can't carry out steam stripped problem to two kinds of solid particulates simultaneously at blended, makes the present invention when two kinds of solid particulates of completion fully carry out mixed heat transfer, also realize stripping.

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

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

Gas-solid loop flow mixing stripper comprises: have inner chamber cylindrical shell 7, be arranged in the inner chamber of cylindrical shell and with the guide shell 6 of cylindrical shell coaxial arrangement, the annular space gas distributor 3 of the bottom, annular space space between cylindrical shell 7 and the guide shell 6, be arranged in cylindrical shell and be arranged in the guide shell gas distributor 11 under the guide shell 6, the pneumatic outlet that extend into cylindrical shell 7 inner chambers, cylindrical shell 7 lower ends and blended solid particle outlet 1 below cone 2 is connected, is arranged on cone 2, be arranged in cone 2 bottoms and be in the cone stripped vapor ring 12 above the blended solid particle outlet 1 and first kind of solid particulate admission passage and the second kind of solid particulate admission passage that is connected respectively to the inner chamber of cylindrical shell; First kind of solid particulate admission passage connects heat collector, and second kind of 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 the annular gas distributor and be positioned under the cylindrical shell 7 and be connected with the annular space space, and guide shell gas distributor 11 is positioned under the 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, and perforate 13 is communicated with the internal space of annular space space and guide shell 6, and perforate is a plurality of long strip shapes holes; The height of perforate is smaller or equal to 0.9 times of guide shell 6 height, and the total area of perforate is smaller or equal to the lateral area of 0.9 times guide shell 6; Perhaps perforate is a plurality of circular ports, and the radius of perforate is smaller or equal to 0.9 times of guide shell 6 height, and the total area of perforate is smaller or equal to the lateral area of 0.9 times guide shell 6.

Further, gas-solid loop flow mixing stripper is arranged on outside riser reactor, pre lift zone and the revivifier; First kind of solid particulate admission passage is first kind of solid particle inlet pipe 5; Second kind of solid particulate admission passage is second kind of solid particle inlet pipe 10; First kind of solid particle inlet pipe 5 and second kind of solid particle inlet pipe 10 be connected to the both sides of cylindrical shell 7 and all with the annular space spatial communication, 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 that extend in cylindrical shell 7 inner chambers is the gas outlet tube 9 that is arranged on the end socket 8, guide shell 6 be vertical layout with cylindrical shell 7.

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

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

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

Further, revivifier comprises: interconnectively burn jar mutually closely with two, first kind of solid particle inlet pipe 5 is connected with heat collector, second kind of solid particle inlet pipe 10 and two close being connected.

Further; The 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; Revivifier is provided with one or more heat collectors, a corresponding one to one riser reactor and the circulation mixing stripper of connecting of each pre lift zone;

Second kind of 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 respectively to be connected with a pre lift zone;

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

Further; Revivifier comprises: divide first revivifier and second revivifier that are arranged; Heat collector is connected with first revivifier; First kind of solid particle inlet pipe 5 is connected with heat collector, and second kind of solid particle inlet pipe 10 is connected with second revivifier, and circulation mixing stripper is between first revivifier and second revivifier.

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

From first kind of solid particulate of heat collector with from second kind of solid particulate of revivifier mixed heat transfer and strip flue gas and the air of carrying secretly simultaneously in like the gas-solid loop flow mixing stripper of front, get into pre lift zone after forming mixed catalyst.

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

Second kind of solid particulate of a part behind the regeneration in-situ regeneration gets into first kind of solid particulate of heat collector cooling formation, and second kind of solid particulate of another part flows out revivifier; Return revivifier from the effusive a part of first kind of solid particulate of heat collector, carry out mixed heat transfer and stripping from first kind of solid particulate of the effusive another part of heat collector and second kind of solid particulate of effusive another part from revivifier.

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

Second kind of solid particulate of a part behind the regeneration in-situ regeneration gets into first kind of solid particulate of heat collector cooling formation, and second kind of solid particulate of another part flows out revivifier; Return revivifier from the effusive a part of first kind of solid particulate of heat collector, carry out mixed heat transfer and stripping from first kind of solid particulate of the effusive another part of heat collector and second kind of solid particulate of effusive another part from revivifier.

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

First kind of solid particulate gets into the annular space space; Second kind of 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 gives the give tolerance of tolerance less than guide shell gas distributor 11; Make win kind of solid particulate and second kind of solid particulate in the annular space space for flowing downward, in guide shell 6 for upwards flowing;

Second kind of solid particulate of a part behind the regeneration in-situ regeneration gets into first kind of solid particulate of heat collector cooling formation, and second kind of solid particulate of another part enters into the top of cylindrical shell 7 and the top of guide shell 6; Return revivifier from the effusive a part of first kind of solid particulate of heat collector, carry out mixed heat transfer and stripping from first kind of solid particulate of the effusive another part of heat collector and second kind of solid particulate from the top of the top that enters into cylindrical shell 7 and guide shell 6.

Further; Revivifier comprises: divide first revivifier and second revivifier that are arranged; Heat collector is connected with first revivifier; Reclaimable catalyst is introduced into first revivifier, and it is defocused to burn part at first revivifier, and a part is flowed out to get into second revivifier and in second revivifier, burn remaining Jiao by first regenerator bottoms and forms second kind of solid particulate; Another part comes out to form first kind of solid particulate from the heat collector bottom; Second kind of solid particulate is the catalyzer of pyritous holomorphosis, and first kind of solid particulate is cryogenic catalyzer to be generated, the catalyzer of the pyritous holomorphosis of being drawn by second revivifier and the catalyzer cryogenic to be generated of drawing from heat collector mixed heat transfer and strip flue gas and the air of carrying secretly simultaneously gas-solid loop flow mixing stripper.

Through the control air demand; What make guide shell gas distributor 11 gives the different to tolerance of tolerance and annular space gas distributor 3; Produce pressure difference in the guide shell bottom; Promote solid particulate (catalyzer) and between annular space and guide shell, circulate, when first kind of solid particulate and second kind of solid particulate enter into the inner chamber of cylindrical shell, first kind of solid particulate and second kind of solid particulate not only form circulating separately respectively between annular space and guide shell; Accomplished stripping simultaneously; And the flowing also in the inner chamber of cylindrical shell, to form to intersect each other to mix with flowing of second kind of solid particulate and realized heat exchange of first kind of solid particulate, in heat transfer process, do not reach completely after first kind of solid particulate and second kind of solid particulate mix and mix; But the hot and cold solid particulate (catalyzer) that forms different sizes is rolled into a ball; These hot and cold solid particulates (catalyzer) group is mingled with each other, by guide shell circulation get into annular space spatial process then be one with hot and cold solid particulate (catalyzer) the group fragmentation newly assigned process of laying equal stress on, the process that is got into guide shell by the annular space space then is a blended process again.And then, having the hole on the guide shell of circulation mixing stripper, catalyzer not only mixes in the upper and lower of guide shell, and can pass the hole and mix, thereby has mixed effect efficiently.

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

Hot and cold solid particulate blended process again comprises: c, by the annular space space get into guide shell be from the guide shell edge to the motion of guide shell central authorities, realized mixed heat transfer; Pass in and out through the perforate on the guide shell with d, hot and cold solid particulate, the process of turnover has realized mixed heat transfer.

So a plurality of perforates on the 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 needs 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 then needs: steam is diffused in the catalyzer micropore by the catalyzer outside surface by steam main diffusion to catalyzer outside surface, in micropore in the flue gas absorption that is at war with; The flue gas that displaces by catalyzer micropore internal diffusion to the catalyzer outside surface; Flue gas is diffused to 5 steps such as steam main body by the catalyzer outside surface, owing to go through a plurality of diffusion processes, the displacement of flue gas is very difficult in the catalyzer micropore; 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 fed 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) when mixed heat transfer is rolled into a ball broken and is redistributed; This makes the interior flue gas of catalyzer micropore come out more easily or the interior flue gas of catalyzer micropore contacts with steam more easily, and this has brought more opportunity for displacement of flue gas in the catalyzer micropore.

And then; Catalyzer at guide shell with lower area circulating radially; Vapor bubbles to rising has very strong shearing action; Greatly reduce bubble diameter, make that the contact efficiency of steam-catalyzer is higher, vapor bubbles gets into more easily or, realized that catalyzer efficiently contacts with the long of live steam near the catalyzer micropore.Circulation mixing stripper of the present invention has not only been realized stripping in two kinds of solid particulate heat exchange; And owing to two kinds of solid particulates hot and cold solid particulate (catalyzer) when mixed heat transfer is rolled into a ball fragmentation and redistributed; This has brought more multimachine meeting for the displacement of flue gas in the catalyzer micropore; And every circulation primary just means live steam contact once, also makes the vapor bubbles that rises be sheared, and greatly reduces bubble diameter; Make vapor bubbles get into more easily or near the catalyzer micropore; So steam stripping efficiency is higher than the efficient of other strippers, for example, steam stripping efficiency is that 200710152287.X, name are called the annular space air-lift gas-solid loop flow reactor height than the patent No..Therefore, the present invention has also realized high efficiency stripping when two kinds of solid particulates of completion 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; Through catalyzer (spent agent or regenerator) in inside and outside the circulating of guide shell; And mixing repeatedly, reallocation, really realized the uniform 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 the background technology; The present invention can regulate control respectively to the temperature and the flow of cold catalyst inlet pipe 5 and thermocatalyst inlet tube 10; Both can obtain getting into the ideal temperature of pre lift zone; Can obtain competent flow again, setting range is very extensive, and the mixed catalyzer that guarantees temperature and flow simultaneously can be provided flexibly.In present catalytic cracking reaction regeneration system rapidly, the conditioned reaction temperature relies on and regulates catalyst flow, regulates the fuel oil preheating temperature and regulates the realization of raw oil flow, and wherein regulating catalyst flow is main means; But this method also has significant disadvantages; For example, can reduce temperature of reaction through reducing catalyst flow, but meanwhile; Participating in the catalyst for reaction amount is that agent-oil ratio has also descended 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, therefore can effectively solve this difficult problem.The agent-oil ratio of catalytic cracking at present generally between 6～8, from the angle of reaction, is being kept under the constant prerequisite of temperature of reaction; Further the rising agent oil ratio can effectively improve product yield and selectivity; But owing to receive the thermally equilibrated restriction of auto levelizer, further the rising agent oil ratio must cause temperature of reaction to raise, when the cold catalyst recirculation technology that the present invention proposes can be implemented in and improves the catalyst recirculation amount and be agent-oil ratio; Reduce catalyst temperature; Make device under the constant prerequisite of temperature of reaction, agent-oil ratio reaches 9～15 in the riser tube, thereby significantly improves the selectivity of product yield.

Description of drawings

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

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

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

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

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

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

Figure 10 is the structure according to first kind of catalytic cracking reaction regeneration system rapidly of the embodiment of the invention, wherein revivifier and settling vessel coaxial arrangement;

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 invention and the structure of the third catalytic cracking reaction regeneration system rapidly;

Figure 12 is the structure according to second kind of catalytic cracking reaction regeneration system rapidly of the embodiment of the invention, i.e. the reconstituted form of catalytic cracking is to burn jar-two close combined forms;

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

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

Below be the drawing reference numeral explanation:

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

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

9, gas outlet tube 10, thermocatalyst inlet tube (second kind of 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 of revivifier 61, two 63, burn jars 65, the 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, first revivifier 602, second revivifier

Embodiment

To understand in order technical characterictic of the present invention, purpose and effect being had more clearly, to contrast description of drawings embodiment of the present invention at present.

Extremely shown in Figure 14 like Figure 10; 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 outer heat collector 70 of 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 the pre lift zone; The fluid catalytic cracking process that gas-solid loop flow mixing stripper can be used for reconstituted form mixes first kind of solid particulate and second kind of solid particulate of differing temps; And strip first kind of solid particulate and second kind of flue gas and air that solid particulate is carried secretly; First kind of solid particulate is low temperature catalyst or low temperature half regenerator, and second kind of solid particulate is high temperature catalyst, and the temperature of second kind of solid particulate is higher than the temperature of first kind of solid particulate.The present invention is not limited to the FCC of reconstituted form, also can be used for the fluid catalytic cracking process of non-reconstituted form, not only can be used for the mixing stripping of catalyzer, also can be used for other solid particulates.

The characteristics of five kinds of catalytic cracking reaction regeneration system rapidlys among the present invention are: first kind of solid particulate admission passage connects heat collector; Second kind of solid particulate admission passage connects revivifier; Draw one cold regenerator (low temperature catalyst) from the heat collector bottom; Thermocatalyst (high temperature catalyst) gas-solid loop flow mixing stripper in long-time uniform mixing and the stripping next with revivifier; And be utilized in the further mixing of the interior mobile realization of regeneration pipeline and conduct heat, guaranteed the uniform mixing and the abundant heat transfer of hot and cold catalyzer fully.Wherein, two kinds of structure such as Fig. 1 that are arranged on the outer gas-solid loop flow mixing stripper of revivifier are extremely shown in Figure 9.Figure 11 shows the main TV structure of the third gas-solid loop flow mixing stripper.

To shown in Figure 5, gas-solid loop flow mixing stripper comprises like Fig. 1: have inner chamber cylindrical shell 7, be arranged in the inner chamber of cylindrical shell 7 and with the guide shell 6 of cylindrical shell 7 coaxial arrangement, the annular space gas distributor 3 of 67 bottoms, annular space space between cylindrical shell 7 and the guide shell 6, be arranged in cylindrical shell and be arranged in the guide shell gas distributor 11 under the annular space gas distributor 3, the pneumatic outlet that extend into cylindrical shell 7 inner chambers, cylindrical shell 7 be connected cone 2 below 11 from the guide shell gas distributor, be arranged on blended solid particle outlet 1 below the cone 2, be arranged in cone 2 bottoms and be in the cone stripped vapor ring 12 above the blended solid particle outlet 1 and first kind of solid particulate admission passage and the second kind of solid particulate admission passage that is connected respectively to the inner chamber of cylindrical shell.Cone 2 is a cone barrel, also has inner chamber and is communicated with the inner chamber of cylindrical shell 7.

Wherein, to shown in Figure 5, cylindrical shell 7 can be cylinder with guide shell 6 like Fig. 3, guide shell 6 all be up and down uncovered, make the internal space of guide shell 6 directly communicate, 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 the annular gas distributor through annular space gas distributor inlet tube 35; Annular space gas distributor 3 is positioned under the cylindrical shell 7 and with annular space space 67 and is connected; Usually, annular space gas distributor 3 is positioned at the vertical projection district in annular space space 67, through annular space gas distributor inlet tube 35 with to annular space space 67 air feed.Guide shell gas distributor 11 is positioned under the guide shell 6 and stretches out cylindrical shell 7 through guide shell gas distributor inlet tube 35.Guide shell gas distributor 11 is communicated with the internal space of guide shell 6, and usually, 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 feeds loosening wind, so that solid particulate suspends.Has been prior art about annular space gas distributor 3 with guide shell gas distributor 11; Can adopt the suitable construction of prior art; For example; Annular space gas distributor 3 is annular tube type gas distributor or tubular gas sparger or board-like gas distributor with guide shell gas distributor 11, and the percentage of open area of sparger is 0.5%～3.0%.

Fluidization steam vapor is fed 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.To shown in Figure 5, pneumatic outlet is a gas outlet tube 9 like Fig. 1.First kind of solid particulate admission passage and second kind of solid particulate admission passage are respectively cold catalyst inlet pipe 5 and thermocatalyst inlet tube 10, and all are connected with annular space space 67.

Further, to shown in Figure 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 like Fig. 5.Catalyzer not only mixes in the upper and lower of guide shell 6, and can pass the hole or groove mixes, thereby has mixed effect efficiently.Certainly, also can not be provided with perforate 13 on the guide shell 6, but such effective not as the mixed heat transfer that is provided with perforate 13.Perforate 13 on the same guide shell is a row or many rows, and adjacent two rows of openings or fluting are staggered arrangement or non-staggered arrangement, and adjacent two to arrange the width of groove equal or unequal with highly, the equal diameters of adjacent two rows of openings or unequal.For perforate is the width and height or unequal setting of staggered arrangement or adjacent two rows of openings, more helps thorough mixing.

Further, to shown in Figure 9, perforate 13 is a plurality of long strip shapes holes like Fig. 5, and the height of perforate is smaller or equal to 0.9 times of guide shell 6 height, and the total area of perforate is smaller or equal to the lateral area of 0.9 times guide shell 6; Perhaps perforate is a plurality of circular ports, and the radius of perforate is smaller or equal to 0.5 times of guide shell 6 height, and the total area of perforate is smaller or equal to the lateral area of 0.9 times guide shell 6.The corresponding first kind of solid particulate of size of perforate and the size of second kind of 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 annular space spatial useful range, and can guarantee that also annular space space and guide shell 6 form the round-robin space, circulated to form reasonably.

Further; To shown in Figure 4, gas-solid loop flow mixing stripper also comprises: cover the end socket 8 at cylindrical shell upper end closed cylinder lumen, wherein like Fig. 1; The pneumatic outlet that extend in cylindrical shell 7 inner chambers is the gas outlet tube 9 that is arranged on the end socket 8, guide shell 6 be vertical layout with cylindrical shell 7.This gas-solid loop flow mixing stripper that has end socket 8 can be accomplished first kind of solid particulate and the second kind of solid particulate that mixes differing temps individually; And mixed solid particulate stripped flue gas and the air of carrying secretly; Be implemented in mixing and the steam stripped function of accomplishing catalyzer in the device, reduced the load of follow-up system pneumatic press, and; Very high in the conventional regeneration agent flue gas stripping device owing to the regenerator temperature; With very easily produce that heat collapses and hydrothermal deactivation after water stripping steam contacts, very big to catalyst impairment, but be mixed catalyzer in the mixing stripper that the present invention proposes; Temperature is lower, mixes rear catalyst generation heat and collapses with the probability of hydrothermal deactivation very low.

Top description has reflected the substruction of two kinds of gas-solid loop flow mixing strippers of Fig. 1 and Fig. 2; Two kinds of gas-solid loop flow mixing stripper key distinctions of Fig. 1 and Fig. 2 are that the direction that is provided with of first kind of solid particle inlet pipe 5 and second kind of solid particle inlet pipe 10 is respectively obliquely or oblique lower 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, can adopt the annular space gas lifting type operator scheme for the gas-solid loop flow mixing stripper 100 among Fig. 1, the gas-solid loop flow mixing stripper 200 among Fig. 2 can adopt central gas lift-type operator scheme.It is mobile for upwards in guide shell 6 that central gas lift-type operator scheme refers to granules of catalyst (solid particulate); At guide shell 6 with mix in the annular space of 7 of stripper cylindrical shells and flow downward; The 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 give tolerance greater than annular space gas distributor 3 give tolerance (being meant flow) time; Gas-solid loop flow mixing stripper (also abbreviating circulation mixing stripper as) is operated with central gas lift-type circulating current system; When annular space gas distributor 3 give tolerance greater than guide shell gas distributor 11 give tolerance the time, circulation mixing stripper is operated with the annular space gas lifting type circulating current system.

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

Existing is the example explanation with the annular space gas lifting type operator scheme:

As shown in Figure 3; Annular space gas distributor 3 give the give tolerance of tolerance greater than guide shell gas distributor 11; Cause the guide shell bottom to produce pressure difference; Promote catalyzer and between annular space and guide shell, circulate, its flow pattern be catalyzer annular space space 67 in on flow, the catalyzer that in guide shell, flows downward is during via cold catalyst inlet pipe 5, thermocatalyst inlet tube 10 entering annular space spaces 67; Have 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 gets in the annular space space 67 obliquely.After hot and cold catalyzer got into annular space space 67, the catalyst mix that in annular space, rises also upwards flowed, and got into to be positioned at the gas solid separation district 65 on the 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, and the catalyzer of solid particulate has been realized separating with fluidizing agent or steam, no longer continues to rise; The catalyzer of solid particulate changes flow direction; Become macro-flow radially, because hot and cold catalyzer gets in the annular space space 67 from both sides respectively, hot and cold catalyzer goes in the same direction; Mix fully; Get in the guide shell then and flow downward, the cone 2 that the sub-fraction catalyzer gets into the bottom in the following space of guide shell also flows out circulation mixing stripper, and is 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, circulate again so most of catalyzer is sent into annular space space 67 by guide shell gas distributor 11 and annular space gas distributor 3, have only the sub-fraction catalyzer gets into the bottom through the edge cone 2 or sub-fraction catalyzer still less to get into 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 to mix, but form the hot and cold catalyzer group of different sizes, these hot and cold catalyzer groups are mingled with each other; The process that gets into annular space space 67 by guide shell circulation then be one with 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 needs experience mixed once and reallocation.Above-mentioned concrete flow process is following:

Cold catalyzer shows as filled arrows C when just having got into annular space space 67 with obliquely direction and since catalyzer annular space space 67 in on mobile, filled arrows C is divided into filled arrows C1 and C2; Filled arrows C1 continue annular space space 67 in on mobile; Because guide shell 6 has perforate 13, the perforate 13 that a part of C2 of filled arrows C passes guide shell 6 gets in the guide shell 6, and in guide shell 6, flows downward; The top entering that filled arrows C1 is raised to annular space space 67 is positioned at the gas solid separation district 65 on the guide shell; No longer continue to rise, the catalyzer of solid particulate changes flow direction, becomes macro-flow radially; Form filled arrows C3, in the downward then or oblique guide shell 6 of entering down.

Meanwhile, thermocatalyst shows as filled arrows d when just having got into annular space space 67 with obliquely direction and since catalyzer annular space space 67 in on mobile; Filled arrows d is divided into filled arrows d1 and d2; Filled arrows d1 continue annular space space 67 in on flow because guide shell 6 has perforate 13, a part of d2 of filled arrows d passes in the perforate 13 entering guide shells 6 inherent guide shells 6 of guide shell 6 and flows downward; The top entering that filled arrows d1 is raised to annular space space 67 is positioned at the gas solid separation district 65 on the guide shell; No longer continue to rise, the catalyzer of solid particulate changes flow direction, becomes macro-flow radially; Form filled arrows d3, in the downward then or oblique guide shell 6 of entering down.

In gas solid separation district 65, promptly in the above space of guide shell, filled arrows C3 and filled arrows d3 be macro-flow radially all; Mixed heat transfer takes place, form filled arrows Cd, filled arrows Cd flows downward in guide shell 6 then; During this period, heat exchange also takes place in filled arrows Cd and filled arrows C2 and filled arrows d2, after filled arrows Cd drops to the bottom of guide shell 6; The part catalyzer in the following space of guide shell, for example, filled arrows Cd2 gets into the cone 2 of bottom and flows out circulation mixing stripper; Most of catalyzer is seen then circulation entering annular space space 67 of filled arrows Cd1, circulates once more; In cone, form filled arrows Cd3 through recycling, 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 the circulation.Above-mentioned filled arrows is represented each granules of catalyst group, and when hot and cold catalyzer was rolled into a ball heat exchange, annular space gas distributor 3, guide shell gas distributor 11 and cone stripped vapor ring 12 fed fluidized wind, fluidized wind and loosening wind respectively.Fluidized wind and loosening wind can be steam.The every circulation primary of catalyzer just means with the bottom live steam and contacts once, so steam stripping efficiency is also very high.Test the result factually; For the catalyzer that gets into guide shell 6 and annular space space 67,, add the effect of annular space gas distributor 3 and guide shell gas distributor 11 and loosening steam ring 12 owing to got into sleeve shaped and guide shell 6 with holes; Catalyzer generally will be through 6～15 circulations; Promptly 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.

Be the example explanation with central gas lift-type operator scheme more below:

Guide shell gas distributor 11 give tolerance greater than annular space gas distributor 3 give tolerance the 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 when just having got into annular space space 67 with the direction under oblique because catalyzer flows downward in annular space under the central gas lift-type operator scheme, 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, change into behind the bottom in annular space space 67 in guide shell 6 on flow and form filled arrows C30 because guide shell 6 has perforate 13; The part of cold catalyzer; Be that perforate 13 that filled arrows C20 passes guide shell 6 gets in the guide shells 6 inherent guide shells 6 to last mobile formation filled arrows C40, the top that filled arrows C40 is raised to annular space space 67 gets into and is positioned at the gas solid separation district 65 on the guide shell, no longer continues to rise; The catalyzer of solid particulate changes flow direction, becomes macro-flow radially.

Thermocatalyst shows as filled arrows d when just having got into annular space space 67 with the direction under oblique because catalyzer flows downward in annular space under the central gas lift-type operator scheme, 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, change into behind the bottom in annular space space 67 in guide shell 6 on flow and form filled arrows d30 because guide shell 6 has perforate 13; The part of cold catalyzer; Be that perforate 13 that filled arrows d20 passes guide shell 6 gets in the guide shells 6 inherent guide shells 6 to last mobile formation filled arrows d40, the top that filled arrows d40 is raised to annular space space 67 gets into and is positioned at the gas solid separation district 65 on the guide shell, no longer continues to rise; The catalyzer of solid particulate changes flow direction, becomes 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 gets into cone 2, forms filled arrows Cd10, and a part of solid particulate flows above guide shell 6 under the circulation effect of guide shell 6 and forms filled arrows Cd20.In the gas solid separation district 65 that is positioned on the guide shell, filled arrows C40 and filled arrows d40 meet intermingling; Form filled arrows Cd30, in repeatedly circulating, filled arrows Cd30 flows downward in annular space space 67 respectively; And meet with filled arrows C10 and filled arrows d10 respectively, the intermingling heat exchange forms filled arrows Cd50 and filled arrows Cd40; The part of filled arrows Cd50 and filled arrows Cd40 continues circulation; Upwards get into guide shell, another part of filled arrows Cd50 and filled arrows Cd40 then gets into cone 2 downwards, forms filled arrows Cd60 and filled arrows Cd70 respectively; And with filled arrows Cd10 mixed heat transfer, flow out mixed catalyst particle outlet 2 then.

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

Figure 10 is the structure according to first kind of catalytic cracking reaction regeneration system rapidly of the embodiment of the invention, wherein revivifier and settling vessel 90 coaxial arrangement.First kind of catalytic cracking reaction regeneration system rapidly shown in figure 10 can adopt the gas-solid loop flow mixing stripper 100 among Fig. 1; Also can adopt the gas-solid loop flow mixing stripper 200 among Fig. 2; All can accomplish the mixing and the steam stripped function of catalyzer separately, with the burden that alleviates the upstream and downstream operation and and the upstream and downstream operation cooperatively interact.Two kinds of gas-solid loop flow mixing stripper key distinctions of Fig. 1 and Fig. 2 are that the direction that is provided with of first kind of solid particle inlet pipe 5 and second kind of solid particle inlet pipe 10 is respectively obliquely or oblique lower direction, and other structures are basic identical.

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

Further; As shown in Figure 2; First kind of solid particle inlet pipe 5 and second kind of solid particle inlet pipe 10 take level or oblique lower direction to be connected on the cylindrical shell 7; First kind of solid particle inlet pipe 5 is 20 °～90 ° with the axis angle γ of cylindrical shell 7, and second kind of 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, need not to carry the auxiliary of airduct 4.

The place that gas-solid loop flow mixing stripper 200 is arranged near revivifier 60 regenerator outlets, gas-solid loop flow mixing stripper 200 is connected through transfer lime (thermocatalyst pipe) 16 with revivifier 60, is connected through transfer lime pipeline (14) with revivifier heat collector 70.Draw one high-temperature regenerated catalyst by revivifier 60 and get into gas-solid loop flow mixing stripper (be called for short and mix stripper) 200 via thermocatalyst pipe 16; Draw one cold regenerated catalyst by revivifier heat collector 60 bottoms and get into the mixing stripper via pipeline 14; Cold catalyst flow is by the guiding valve control that is arranged on the pipeline 14, and the thermocatalyst flow is by the guiding valve control that is arranged on the pipeline 16.Fluidization steam vapor is fed by annular space gas distributor, guide shell gas distributor and cone stripped vapor ring respectively, and is drained into the dilute phase pipe by the gas outlet tube 9 at top and enters the revivifier dilute phase again.Cold and hot catalyzer mixes in mixing stripper, draw by mixing the stripper bottom after the heat transfer, stripping, gets into pre lift zones 30 backs via regeneration pipeline (regenerator sloped tube) 50 and gets into riser reactors 40.The regeneration pipeline is made up of multistage standpipe, inclined tube usually, and mixed catalyst can repeatedly turn to when in the regenerator pipeline, flowing, and has also further promoted the mixing between catalyzer.The residence time long-range far surpassed in the pre lift zone blended residence time of catalyzer in technical scale circulation mixing stripper.

Adopted the gas-solid loop flow mixing stripper among Fig. 2 among Figure 10; Certainly; Gas-solid loop flow mixing stripper 100 among 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 obliquely to be connected on the cylindrical shell 7 first kind of solid particle inlet pipe 5 and second kind of solid particle inlet pipe 10.For example, the axis angle α of the Way in of first kind of solid particle inlet pipe 5 and cylindrical shell 7 is 20 °～90 °, and the axis angle β of the Way in of second kind of solid particle inlet pipe 10 and cylindrical shell 7 is 20 °～90 °.The concrete principle of work of the gas-solid loop flow mixing stripper 100 among Fig. 1 can be with reference to the description of figure 3.

Further, as shown in Figure 1, first kind of solid particle inlet pipe 5 and second kind of solid particle inlet pipe 10 are symmetrical set about the axis of cylindrical shell 7, and such first kind of solid particulate and second kind of solid particulate mix more even.Be respectively arranged with conveying airduct 4 in first kind of solid particle inlet pipe 5 and second kind of solid particle inlet pipe 10; The defeated wind direction of the conveying airduct in first kind of solid particle inlet pipe 5 is identical with the Way in of first kind of solid particle inlet pipe 5, and the defeated wind direction of the conveying airduct in second kind of solid particle inlet pipe 10 is identical with the Way in of second kind of solid particle inlet pipe 10.Through carry airduct 4 can first kind of solid particle inlet pipe 5 and second kind of solid particle inlet pipe 10 be level or the situation of arranging obliquely under make two kinds of solid particulates can overcome gravity influence enter into annular space space 67 according to the direction obliquely that designs.

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

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

Gas-solid loop flow mixing stripper (be called for short circulation mixings stripper or mixing stripper) 200 is put in the place near the regenerator outlet of revivifier 60; Circulation mixing stripper 200 is connected through transfer lime (thermocatalyst pipe) 16 with revivifier 60, is connected through transfer lime (also being called for short pipeline) 14 with revivifier heat collector 70.Draw one high-temperature regenerated catalyst (second kind of solid particulate) by revivifier and get into gas-solid loop flow mixing stripper 200 via thermocatalyst pipe 16, another part flows out revivifier; Draw one cold regenerated catalyst (first kind of solid particulate) by outer heat collector 70 bottoms of revivifier and get into the mixing stripper via pipeline 14; Another part cold regenerated catalyst returns revivifier; In order to regulate the temperature of revivifier, cold catalyst flow is by the guiding valve control that is arranged on the pipeline 14.Fluidization steam vapor is fed by annular space gas distributor 3, guide shell gas distributor 11 and cone stripped vapor ring respectively, and enters the 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 in mixing stripper, draw by mixing the stripper bottom after the heat transfer, stripping, via regeneration pipeline 50 (for example be regenerator sloped tube) entering riser reactor 40.Mix the temperature of rear catalyst and control, perhaps pass through the temperature control of regulating regenerator temperature and/or flowing out the heat collector catalyzer according to the high temperature regeneration agent flux that flows out revivifier and the ratio of the low-temp recovery agent flux that flows out heat collector.First kind of solid particulate (low-temp recovery agent) and the mixed temperature of second kind of solid particulate (high temperature regeneration agent) are controlled with the ratio of the flow of the first kind of solid particulate that flows out heat collector according to the flow of the second kind of solid particulate that flows out revivifier; For example; The flow of hot and cold catalyzer all can be through the control of the guiding valve on the hot and cold catalyst transport (pipeline); Perhaps through regulating regenerator temperature and/or flowing out the temperature control of first kind of solid of heat collector, first kind of solid particulate and second kind of mixed temperature of solid particulate are 550 ℃～680 ℃.

Because the regenerator pipeline is made up of multistage standpipe, inclined tube usually in the actual production, mixed catalyst can repeatedly turn to when in the regenerator pipeline, flowing, and has also further promoted the mixing between catalyzer.

Figure 12 is the structure according to second kind of catalytic cracking reaction regeneration system rapidly of the embodiment of the invention, i.e. the reconstituted form of catalytic cracking is to burn jar-two close combined forms.Something in common with embodiment Figure 10 this embodiment is seldom narrated, and the key distinction has: burn jar outlet and be dilute phase pipe or macropore grid distributor.Be the catalyzer of holomorphosis for the catalyzer that guarantees entering circulation mixing stripper; The thermocatalyst of heat collector is introduced by two close phases 61; A cooling back part is returned and is burnt jar 63, and a part gets into circulation mixing stripper, and the thermocatalyst of circulation mixing stripper is introduced by two close phases 61; After hot and cold catalyzer mixes in circulation mixing stripper; Get into riser tube via the regenerator pipeline, wherein, the flow of hot and cold catalyzer all can be through the control of the guiding valve on the hot and cold catalyst transport (pipeline).About the gas-solid loop flow mixing stripper that Figure 12 adopted; Can adopt the gas-solid loop flow mixing stripper 100 among Fig. 1; Also can adopt the gas-solid loop flow mixing stripper 200 among Fig. 2; Operating method can adopt like preceding employing central gas lift-type and annular space gas lifting type accordingly, and concrete principle of work and catalyst recirculation mode can be with reference to the catalytic cracking reaction regeneration system rapidlys of Figure 10.

Figure 13 is the structure according to the 4th kind of catalytic cracking reaction regeneration system rapidly of the embodiment of the invention, promptly adopts the catalytic cracking form of two-stage riser.Something in common with embodiment Figure 10 this embodiment is seldom narrated; The key distinction has: revivifier 60 is provided with a heat collector 70; A low temperature catalyst part of coming out in heat collector 70 bottoms is returned revivifier 60; Another part low temperature catalyst is introduced two circulation mixing strippers 200 via transfer lime 14, and cold catalytic amount is by the guiding valve control that is arranged on the catalyst tube transfer lime 14.Thermocatalyst is by drawing in the revivifier 60; Get into respectively in the circulation mixing stripper via catalyst tube transfer lime 16a or 16b; And with cold catalyst mix; Wherein, the flow of hot and cold catalyzer all can be through the control of the guiding valve on the hot and cold catalyst transport (pipeline), and circulation mixing stripper outlet at bottom links to each other with two riser tubes.This embodiment is arranged comparatively flexible, can control the catalyst recirculation amount of each riser tube 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 among Fig. 1; Also can adopt the gas-solid loop flow mixing stripper 200 among Fig. 2; Operating method can adopt like preceding employing central gas lift-type and annular space gas lifting type accordingly, and concrete principle of work and catalyst recirculation mode can be with reference to the catalytic cracking reaction regeneration system rapidlys of Figure 10.

Figure 14 is the structure according to the 5th kind of catalytic cracking reaction regeneration system rapidly of the embodiment of the invention, promptly adopts the catalytic cracking form of two-stage regeneration.Something in common with embodiment Figure 10 this embodiment is seldom narrated; The key distinction has: revivifier comprises: divide first revivifier 601 and second revivifier 602 that are arranged; Heat collector 70 is connected with first revivifier 601; Reclaimable catalyst is introduced into first revivifier 601; Burn part Jiao at first revivifier 601 and become half regenerator; A part is flowed out to get into second revivifier 602 and in second revivifier, burn remaining Jiao by first revivifier, 601 bottoms and forms second kind of solid particulate, and another part comes out to form first kind of solid particulate from the heat collector bottom, and second kind of solid particulate is the catalyzer of pyritous holomorphosis; First kind of solid particulate is cryogenic half regenerated catalyst; The catalyzer of the pyritous holomorphosis of being drawn by second revivifier and cryogenic half regenerated catalyst of drawing from heat collector mixed heat transfer and strip flue gas and the air of carrying secretly simultaneously gas-solid loop flow mixing stripper 200, wherein, the flow of hot and cold catalyzer all can be through the control of the guiding valve on the hot and cold catalyst transport (pipeline).The advantage of this embodiment is, all leaves bigger space between general two revivifiers, so embodiment 4 installations, more or less freely when constructing.

Further, 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 preceding two kinds key distinction: gas-solid loop flow mixing stripper 300 is not arranged on outside riser reactor 40, pre lift zone 30 and the revivifier 60, but gas-solid loop flow mixing stripper 300 is arranged within the revivifier 60.The top of the cylindrical shell 7 of gas-solid loop flow mixing stripper 300 is not provided with end socket 8 and gas outlet tube 9; The inner chamber of revivifier 60 directly is communicated with the top of cylindrical shell 7; Cold catalyzer is introduced by first kind of solid particle inlet pipe; First kind of solid particle inlet pipe extend into from the outside of revivifier cylindrical shell 7 side direction and with the annular space spatial communication, heat (regeneration) catalyzer directly enters into guide shell 6 from cylindrical shell 7 by cylindrical shell 7 tops, thereby need not to be provided with thermocatalyst inlet tube 10.Elswhere, 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 among Fig. 1 and Fig. 2.

Figure 11 has also illustrated structure and the mode of operation according to the catalytic cracking reaction regeneration system rapidly of the embodiment of the invention.Further, gas-solid loop flow mixing stripper 300 cylindrical shells 7 are surrounded by inboard wall and a lateral arc of revivifier jointly, reduce cost of manufacture like this, make full use of the inboard 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 the revivifier 60 is applicable to conventional single revivifier.Circulation mixing stripper is arranged on internal regenerator regenerator extraction mouth, and mixed catalyzer gets into circulation mixing stripper bottom, bottom regeneration pipeline 50 entering riser tubes.

The inner chamber that fluidizing agent that this gas-solid loop flow mixing stripper 300 that end socket 8 and gas outlet tube 9 be not set is used with annular space gas distributor 3, guide shell gas distributor 11 and cone stripped vapor ring 12 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; First kind of 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; The central gas lift-type operator scheme of introducing according to the front circulates; Promptly solid particulate flows direction for upwards in guide shell 6, and in the annular space space, the mobile direction of solid particulate is downward.

The advantage of this embodiment is: (1) during not enough or insufficient height, is placed on internal regenerator with circulation mixing stripper when on-the-spot arrangement space, can save big quantity space; (2) need not transform catalyst recycle line, thereby install and overhaul very simply, the operation of device is also very simple; (3) circulation mixing stripper is placed on internal regenerator; Not only increase the resistance to flow of regeneration circuit, be provided with circulation mixing stripper because extract mouth out on the contrary, played the effect of flooding the stream bucket that is similar at regenerator; Increase the regenerator pressure accumulation, increased regenerator mobile impellent.Maximization gradually along with device; The diameter of catalytic cracking regenerator can reach more than the 10m; 300 of gas-solid loop flow mixing strippers have occupied very little a part of space (cross-sectional area accounts for that the 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 influence basically.

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

(1) the catalyzer heat collector that utilizes present conventional catalytic cracking all to be equipped with; Draw one cold regenerator from the heat collector bottom; Thermocatalyst mixing tank in the long-time uniform mixing next with revivifier; And be utilized in the further mixing of the interior mobile realization of regeneration pipeline and conduct heat, guaranteed the uniform mixing and the abundant heat transfer of hot and cold catalyzer fully.The present invention only need be provided with one separately and mix stripper; And got final product 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 of little; The change amount of getting up to work is little; Need not to change on a large scale catalyst cracker, shorten the scrap build time, reduce and change cost.

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

(3) the regenerator pipeline is made up of multistage standpipe, inclined tube usually in the actual production, and mixed catalyst can repeatedly turn to when in the regenerator pipeline, flowing, and 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 the catalyzer, reduce the load of follow-up system pneumatic press.

(6) very high in the conventional regeneration agent flue gas stripping device owing to the regenerator temperature; Heat collapses and hydrothermal deactivation with very easily producing after water stripping steam contacts; Very big to catalyst impairment; But in the gas-solid loop flow mixing stripper (abbreviating circulation mixing stripper as) that the present invention proposes is mixed catalyzer, and temperature is lower, and catalyzer heat takes place 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 owing to two kinds of solid particulates hot and cold solid particulate (catalyzer) when mixed heat transfer is rolled into a ball fragmentation and redistributed; This has brought more multimachine meeting for the displacement of flue gas in the catalyzer micropore; And every circulation primary just means live steam contact once, also makes the vapor bubbles that rises be sheared, and greatly reduces bubble diameter; Make vapor bubbles get into more easily or near the catalyzer micropore, so steam stripping efficiency is higher than the efficient of other strippers.

(8) the present invention can regulate control respectively to the temperature and the flow of cold catalyst inlet pipe 5 and thermocatalyst inlet tube 10; Both can obtain getting into the ideal temperature of pre lift zone; Can obtain competent flow again; Setting range is very extensive, and the mixed catalyzer that guarantees temperature and flow simultaneously can be provided flexibly.

The above is merely the schematic embodiment of the present invention, is not in order to limit scope of the present invention.For each integral part of the present invention can make up under the condition of not conflicting each other, any those skilled in the art, equivalent variations of under the prerequisite that does not break away from design of the present invention and principle, having done and modification all should belong to the scope that the present invention protects.

Claims (15)

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

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

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

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

2. catalytic cracking reaction regeneration system rapidly as claimed in claim 1; It is characterized in that; Said guide shell (6) is 0.2～0.8 with the horizontal direction cross-sectional area ratio of said cylindrical shell (7); The barrel of said guide shell (6) is provided with perforate (13), and said perforate (13) is communicated with the internal space of said annular space space and guide shell (6), and said perforate is a plurality of long strip shapes holes; The height of said perforate is smaller or equal to 0.9 times of said guide shell (6) height, and the total area of said perforate is smaller or equal to the lateral area of 0.9 times guide shell 6; Perhaps said perforate is a plurality of circular ports; The radius of said perforate is smaller or equal to 0.5 times of guide shell (6) height; The total area of said perforate is smaller or equal to the lateral area of 0.9 times guide shell 6, and gas-solid loop flow mixing stripper bottom links to each other with pre lift zone or riser reactor bottom.

3. catalytic cracking reaction regeneration system rapidly according to claim 1 or claim 2 is characterized in that said gas-solid loop flow mixing stripper is arranged on outside riser reactor, pre lift zone and the said revivifier; Said first kind of solid particulate admission passage is first kind of solid particle inlet pipe (5); Said second kind of solid particulate admission passage is second kind of solid particle inlet pipe (10); First kind of solid particle inlet pipe (5) and second kind of solid particle inlet pipe (10) be connected to the both sides of said cylindrical shell (7) and all with said annular space spatial communication, said blended solid particle outlet (1) is with said pre lift zone or directly be connected with riser reactor; Said cylindrical shell (7) upper end is internally connected with end socket (8); Wherein, The said pneumatic outlet that extend in said cylindrical shell (7) inner chamber also comprises for the said gas-solid loop flow mixing of gas outlet tube (9) stripper that is arranged on the end socket (8): end socket (8) and gas outlet tube (9), described guide shell (6) is vertical layout with cylindrical shell (7).

4. catalytic cracking reaction regeneration system rapidly according to claim 1 or claim 2; It is characterized in that; Said gas-solid loop flow mixing stripper is arranged within the said revivifier; Said cylindrical shell (7) is surrounded by inboard wall and a lateral arc of revivifier jointly, and the top of said cylindrical shell is uncovered, and the inner chamber of said cylindrical shell directly is communicated with the inner chamber of said revivifier;

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

5. like the said catalytic cracking reaction regeneration system rapidly of claim 3, it is characterized in that said first kind of solid particle inlet pipe (5) is connected with heat collector, said second kind of solid particle inlet pipe (10) is connected with said revivifier.

6. like the said catalytic cracking reaction regeneration system rapidly of claim 3; It is characterized in that; Said revivifier comprises: interconnectively burn jar mutually closely with two, said first kind of solid particle inlet pipe (5) is connected with heat collector, said second kind of solid particle inlet pipe (10) and said two close being connected.

7. like the said catalytic cracking reaction regeneration system rapidly of claim 3; It is characterized in that; Said catalytic cracking reaction regeneration system rapidly comprises: a plurality of said riser reactors, a plurality of said pre lift zone, said revivifier, a plurality of said gas-solid loop flow mixing stripper and a line of pipes; Said revivifier is provided with one or more heat collectors; A corresponding one to one riser reactor and the said gas-solid loop flow mixing stripper of connecting of each pre lift zone, said second kind of solid particle inlet pipe (10) is connected with said revivifier, and the blended solid particle outlet (1) of each said circulation mixing stripper is man-to-man respectively to be connected with a pre lift zone;

First kind of solid particle inlet pipe (5) of each said circulation mixing stripper is connected on the heat collector jointly, or first kind of solid particle inlet pipe (5) of each said circulation mixing stripper is man-to-man respectively is connected on the heat collector.

8. like the said catalytic cracking reaction regeneration system rapidly of claim 3; It is characterized in that; Said revivifier comprises: divide first revivifier and second revivifier that are arranged, said heat collector is connected with first revivifier, and said first kind of solid particle inlet pipe (5) is connected with said heat collector; Said second kind of solid particle inlet pipe (10) is connected with said second revivifier, and said circulation mixing stripper is between first revivifier and second revivifier.

9. cold regenerated catalyst circulation means; The fluid catalytic cracking process that is used for reconstituted form mixes first kind of solid particulate and second kind of solid particulate of differing temps; And strip first kind of solid particulate and second kind of flue gas and air that solid particulate is carried secretly simultaneously, and first kind of solid particulate is low temperature catalyst or low temperature half regenerator, second kind of solid particulate is high temperature catalyst; The temperature of second kind of solid particulate is higher than the temperature of first kind of solid particulate; Said cold regenerated catalyst circulation means is accomplished through the catalytic cracking reaction regeneration system rapidly, and said catalytic cracking reaction regeneration system rapidly comprises: riser reactor, the pre lift zone that is connected with riser reactor, revivifier and line of pipes, and said revivifier is outside equipped with heat collector; It is characterized in that

From first kind of solid particulate of said heat collector with from second kind of solid particulate of said revivifier mixed heat transfer and strip flue gas and the air of carrying secretly simultaneously in like each described gas-solid loop flow mixing stripper in the claim 1 to 2, get into said pre lift zone after forming mixed catalyst.

10. like the said cold regenerated catalyst circulation means of claim 9, it is characterized in that, said gas-solid loop flow mixing stripper is arranged on outside riser reactor, pre lift zone and the said revivifier; With first kind of solid particulate and second kind of solid particulate level or be transported to obliquely in the annular space space; What make said annular space gas distributor (3) gives the give tolerance of tolerance greater than said guide shell gas distributor (11); Make win kind of solid particulate and second kind of solid particulate in said annular space for upwards flowing, in said guide shell (6) for flowing downward;

Second kind of solid particulate of a part behind said regeneration in-situ regeneration gets into first kind of solid particulate of heat collector cooling formation, and second kind of solid particulate of another part flows out revivifier; Return revivifier from the effusive a part of first kind of solid particulate of said heat collector, carry out mixed heat transfer and stripping from first kind of solid particulate of the effusive another part of said heat collector and second kind of solid particulate of effusive said another part from revivifier.

11. like the said cold regenerated catalyst circulation means of claim 9, it is characterized in that, said gas-solid loop flow mixing stripper be arranged on outside riser reactor, pre lift zone and the said revivifier; With first kind of solid particulate and second kind of solid particulate level or oblique under be transported in the said annular space space; What make said annular space gas distributor (3) gives the give tolerance of tolerance less than said guide shell gas distributor (11); Make win kind of solid particulate and second kind of solid particulate in said annular space space for flowing downward, in said guide shell (6) for upwards flowing;

Second kind of solid particulate of a part behind said regeneration in-situ regeneration gets into first kind of solid particulate of heat collector cooling formation, and second kind of solid particulate of another part flows out revivifier; Return revivifier from the effusive a part of first kind of solid particulate of said heat collector, carry out mixed heat transfer and stripping from first kind of solid particulate of the effusive another part of said heat collector and second kind of solid particulate of effusive said another part from revivifier.

12., it is characterized in that said gas-solid loop flow mixing stripper is arranged within the said revivifier, and the top of said cylindrical shell is uncovered like the said cold regenerated catalyst circulation means of claim 9, the inner chamber of said cylindrical shell directly is communicated with the inner chamber of said revivifier;

Said first kind of solid particulate level or the oblique said annular space space that gets into down; Second kind of solid particulate directly enters into the top of cylindrical shell (7) and the top of guide shell (6) from the inner chamber of said revivifier; What make said annular space gas distributor (3) gives the give tolerance of tolerance less than said guide shell gas distributor (11); Make win kind of solid particulate and second kind of solid particulate in said annular space space for flowing downward, in said guide shell (6) for upwards flowing;

Second kind of solid particulate of a part behind said regeneration in-situ regeneration gets into first kind of solid particulate of heat collector cooling formation, and second kind of solid particulate of another part enters into the top of cylindrical shell (7) and the top of guide shell (6); Return revivifier from the effusive a part of first kind of solid particulate of said heat collector, carry out mixed heat transfer and stripping from first kind of solid particulate of the effusive another part of said heat collector and second kind of solid particulate from the top of the top that enters into cylindrical shell (7) and guide shell (6).

13. like the said cold regenerated catalyst circulation means of claim 9; It is characterized in that; Said revivifier comprises: divide first revivifier and second revivifier that are arranged; Said heat collector is connected with first revivifier; Reclaimable catalyst is introduced into first revivifier, burns burnt half regenerated catalyst that forms of part at first revivifier, and a part is flowed out, gets into second revivifier and in second revivifier, burnt remaining Jiao by first regenerator bottoms and forms second kind of solid particulate; Another part comes out to form first kind of solid particulate from the heat collector bottom; Said second kind of catalyzer that solid particulate is pyritous holomorphosis, said first kind of solid particulate is cryogenic half regenerated catalyst, the catalyzer of the pyritous holomorphosis of being drawn by second revivifier and cryogenic half regenerated catalyst of drawing from heat collector mixed heat transfer and strip flue gas and the air of carrying secretly simultaneously said gas-solid loop flow mixing stripper.

14. like the said cold regenerated catalyst circulation means of claim 9; It is characterized in that; First kind of solid particulate and second kind of mixed temperature of solid particulate are controlled with the ratio of the flow of the first kind of solid particulate that flows out heat collector according to the flow of the second kind of solid particulate that flows out revivifier; Perhaps through regulating regenerator temperature and/or flowing out the temperature control of first kind of solid of heat collector, first kind of solid particulate and second kind of mixed temperature of solid particulate are 550 ℃～680 ℃.

15. like the said cold regenerated catalyst circulation means of claim 9; It is characterized in that; The temperature of reaction of riser reactor is according to the internal circulating load of mixed first kind of solid particulate and second kind of solid particulate, or the temperature of mixed first kind of solid particulate and second kind of solid particulate or raw oil flow or fuel oil preheating temperature regulation.

Images