CN102676206A

CN102676206A - Gas/solid circulation mixing steam stripper and mixing and steam stripping method of solid particles

Info

Publication number: CN102676206A
Application number: CN2012101529282A
Authority: CN
Inventors: 刘梦溪; 卢春喜; 王祝安; 范怡平
Original assignee: China University of Petroleum Beijing
Current assignee: China University of Petroleum Beijing
Priority date: 2012-05-16
Filing date: 2012-05-16
Publication date: 2012-09-19
Anticipated expiration: 2032-05-16
Also published as: CN102676206B

Abstract

The invention provides a gas/solid circulation mixing steam stripper and a mixing and steam stripping method of solid particles. The gas/solid circulation mixing steam stripper comprises a cylinder body (7) with an inner cavity, a flow guide cylinder (6), a ring-gap gas distributor (3), a gas distributor (11) of the flow guide cylinder, a gas outlet extending into the inside of the cylinder body (7), a cone (2) connected with the lower end of the cylinder body (7), a mixed solid particle outlet (1) arranged below the cone (2), a loose steam ring (12) which is positioned at the bottom of the cone (2) and is also positioned above the mixed solid particle outlet (1), a first solid particle inlet passage and a second solid particle inlet passage, wherein the first solid particle inlet passage and the second solid particle inlet passage are respectively connected to the inside of the cylinder body. The gas/solid circulation mixing steam stripper is adopted by the mixing and steam stripping method of the solid particles.

Description

The mixing of gas-solid loop flow mixing stripper and solid particulate and gas stripping process

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; The mixing and the gas stripping process that relate to a kind of gas-solid loop flow mixing stripper (belonging to a kind of mixing tank) and a kind of solid particulate are used for the stripping of the solid particulate in the mixing and mix of two kinds of solid particulates (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

FCC is important crude oil secondary processing means, has huge economic benefit.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.The reaction product of catalytic cracking existing desired purpose product is like gasoline, diesel oil, liquefied gas, also has not hope the sub product that produces, like dry gas.

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, can the serious regeneration effect that reduces catalyzer.Therefore, increase regenerator internal circulating load and a pair of contradiction that can't take into account of rising agent oil ratio.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 provides 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.

It is the patent of invention that 200710152287.X, name are called annular space air-lift gas-solid loop flow reactor that the contriver also once proposed the patent No..This patent is introduced one catalyzer from solid particulate feed-pipe (being the catalyst inlet pipe); Make this catalyzer stripping or carry out gas-solid reaction in annular space air-lift gas-solid loop flow reactor; Reduced the back-mixing between the annular space air-lift gas-solid loop flow reactor inner catalyst; But this patent is not carried out the mixing of hot and cold catalyzer, and catalyst flow is not an independent variable.The operation logic of this patent is only to consider contacting and mass transfer of a kind of solid particulate and gas, and implementing purpose is to carry out stripping, can not solve the problem of two kinds of solid particulate mixed heat transfers, can not solve two kinds of stripping problems behind the solid particulate mixed heat transfer.Therefore, in the prior art, two kinds of solid particulates (between the regenerator and/or between the spent agent) of differing temps are difficult to the mixed heat transfer that fully carries out, and in the prior art, also can't carry out stripping simultaneously at two kinds of solid particulate blended.

Summary of the invention

The present invention aims to provide the mixing and the gas stripping process of a kind of gas-solid loop flow mixing stripper and a kind of solid particulate; The problem that is difficult to fully carry out mixed heat transfer with the two kinds of solid particulates (between the regenerator and/or between the spent agent) that solve differing temps in the fluid catalytic cracking process; Simultaneously; The present invention has also solved prior art can't carry out steam stripped problem 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 provides a kind of gas-solid loop flow mixing stripper; 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 strips first kind of solid particulate and second kind of flue gas and air that solid particulate is carried secretly, and first kind of solid particulate can be low temperature catalyst or low temperature spent agent; 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; Said gas-solid loop flow mixing stripper comprises: have inner cylindrical shell 7; Be arranged in the inside of said cylindrical shell and with the guide shell 6 of said cylindrical shell coaxial arrangement; The annular space gas distributor 3 of the bottom, annular space space between said cylindrical shell 7 and said guide shell 6; Be arranged in said cylindrical shell and be positioned at the guide shell gas distributor 11 under the annular space gas distributor 3; Extend into the pneumatic outlet in said cylindrical shell 7 inside; Said cylindrical shell 7 lower ends are connected with cone 2; Be arranged on the blended solid particle outlet 1 of said cone 2 belows; Be positioned at loosening steam ring 12 cone 2 bottoms and that be in blended solid particle outlet 1 top; And be connected respectively to first kind of solid particulate admission passage and the second kind of solid particulate admission passage in the inside of said cylindrical shell;

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

Further, the barrel of said guide shell 6 is provided with the internal space of perforate 13, said perforate 13 connection said annular space spaces and guide shell 6.

Further, said perforate is a plurality of long strip shapes holes, and 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, and the radius of said perforate is smaller or equal to 0.5 times of 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.

Further, the radial cross-section of said guide shell 6 and said cylindrical shell 7 is long-pending than being 0.2～0.8.

Further; Said gas-solid loop flow mixing stripper also comprises: cover the end socket 8 at the said cylinder lumen of said cylindrical shell upper end closed; Wherein, The said pneumatic outlet that extend in said cylindrical shell 7 inner chambers is the gas outlet tube 9 that is arranged on the end socket 8, and described guide shell 6 is vertical layout with cylindrical shell 7.

Further; 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 can be connected with said pre lift zone;

Perhaps, first kind of solid particle inlet pipe 5 is connected the side direction of said cylindrical shell 7, and second kind of solid particle inlet pipe 10 is connected the top of said cylindrical shell 7, and said blended solid particle outlet 1 can be connected with said pre lift zone;

Perhaps, first kind of solid particle inlet pipe 5 is connected the top of said cylindrical shell 7, and second kind of solid particle inlet pipe 10 is connected the side direction of said cylindrical shell 7, and said blended solid particle outlet 1 can be connected with said pre lift zone.

Further; Said first kind of solid particle inlet pipe 5 takes level or Way in obliquely to be connected on the said cylindrical shell 7 with said second kind of solid particle inlet pipe; The axis angle of the Way in of said first kind of solid particle inlet pipe 5 and said cylindrical shell 7 is 20 °～90 °, and the axis angle of the Way in of said second kind of solid particle inlet pipe 10 and said cylindrical shell 7 is 20 °～90 °.

Further; Said first kind of solid particle inlet pipe 5 is symmetrical set with the axis of said second kind of solid particle inlet pipe 10 about said cylindrical shell 7; Be respectively arranged with in said first kind of solid particle inlet pipe 5 and the said second kind of solid particle inlet pipe 10 and carry airduct 4; The defeated wind direction of the conveying airduct in said first kind of solid particle inlet pipe 5 is identical with the Way in of said first kind of solid particle inlet pipe 5, and the defeated wind direction of the conveying airduct in said second kind of solid particle inlet pipe 10 is identical with the Way in of said second kind of solid particle inlet pipe 10.

Further; Said first kind of solid particle inlet pipe 5 takes level or oblique lower direction to be connected on the said cylindrical shell 7 with said second kind of solid particle inlet pipe 10; Said first kind of solid particle inlet pipe 5 is 20 °～90 ° with the axis angle of said cylindrical shell 7, and said second kind of solid particle inlet pipe 10 is 20 °～90 ° with the axis angle of said cylindrical shell 7.

Further; The mixing of said first kind of solid particulate and second kind of solid particulate and stripping process are accomplished through the catalytic cracking reaction regeneration system rapidly; The mixing of said first kind of solid particulate and second kind of solid particulate promptly mixes first kind of solid particulate and second kind of solid particulate of differing temps with stripping process; And strip the flue gas that first kind of solid particulate and second kind of solid particulate carry secretly and the process of air, and said catalytic cracking reaction regeneration system rapidly comprises: riser reactor, pre lift zone and revivifier, and 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; 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.

The present invention also provides a kind of mixing and gas stripping process of solid particulate; Be used for first kind of solid particulate and second kind of solid particulate that fluid catalytic cracking process mixes differing temps; And strip 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, and the mixing of said solid particulate and gas stripping process can be 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; Said revivifier is outside equipped with heat collector

The mixing of said solid particulate is adopted foregoing gas-solid loop flow mixing stripper with gas stripping process;

The mixing and the gas stripping process of said solid particulate comprise:

A, first kind of solid particulate and second kind of solid particulate are incorporated into respectively in the inside of said cylindrical shell, make first kind of solid particulate and second kind of solid particulate in cylindrical shell and guide shell, accomplish heat exchange;

B, in heat exchange, 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 spent agent; Second kind of solid particulate is high temperature catalyst; A kind of solid particulate of temperature control that the temperature of second kind of solid particulate is higher than first kind of solid particulate is low temperature catalyst or low temperature spent agent; 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.

Progressive ground; Steps A comprises: A1: with first kind of solid particulate and second kind of solid particulate level or be transported to obliquely in the said 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.

Further; Steps A comprises: A2: 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.

Further, steps A comprises:

A3: what make said guide shell gas distributor 11 gives the give tolerance of tolerance greater than said annular space gas distributor 3; Make win kind of solid particulate and second kind of solid particulate in said annular space for flowing downward; Mobile for upwards in said guide shell 6; First kind of solid particulate is transported in the said annular space space with level or direction obliquely, and second kind of solid particulate enters into said guide shell 6 from said guide shell 6 to the next top.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, its flow pattern or be solid particulate in annular space on mobile, in guide shell, flow downward; Perhaps be solid particulate in annular space on flow, in guide shell, flow downward.

Which kind of flow pattern no matter; Enter into the inner chamber of cylindrical shell when first kind of solid particulate and second kind of solid particulate; The solid particulate and second kind of solid particulate not only circulate between annular space and guide shell respectively; Accomplished stripping; 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 cold and hot 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.In the gas-solid loop flow mixing stripper 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.

And then; Along having realized mixing and reallocation repeatedly in the circulating of setting path, experimental study shows that hot and cold catalyzer is wanted circulation 6～15 times, and (promptly going through 6～15 mixing) just can be flowed out the mixing stripper to hot and cold catalyzer in circulation mixing stripper; Its residence time reaches 143 seconds; Considerably beyond the residence time of pre lift zone mixing tank, not only can realize mixing completely, and have the competent heat transfer time.

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.

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 Principle of Process figure of first kind of gas-solid loop flow mixing stripper according to the embodiment of the invention when adopting the annular space gas lifting type operator scheme;

Fig. 4 is the Principle of Process figure of second kind of gas-solid loop flow mixing stripper according to the embodiment of the invention when adopting central gas lift-type operator scheme;

Fig. 5 is 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;

The second kind gas-solid loop flow mixing stripper according to the embodiment of the invention of Figure 10 for adopting in the catalytic cracking reaction regeneration system rapidly;

Figure 11 is the structure according to the third gas-solid loop flow mixing stripper of the embodiment of the invention.

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, loosening steam ring 13, perforate 14, transfer lime 16, 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, revivifier 65, gas solid separation district 67, annular space space

70, heat collector 100, gas-solid loop flow mixing stripper 200, gas-solid loop flow mixing stripper

300, gas-solid loop flow mixing stripper

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.

The present invention provides a kind of gas-solid loop flow mixing stripper, and 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 mixed solid particulate is stripped flue gas and the air of carrying secretly.Certainly, the present invention also can be owing to the fluid catalytic cracking process of non-reconstituted form.With the fluid catalytic cracking process that is used for reconstituted form is example, and first kind of solid particulate is low temperature catalyst or low temperature spent agent, 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.Low temperature catalyst comprises after the regeneration and to be also referred to as cold catalyzer through (for example passing through heat collector) refrigerative catalyzer (cold regenerator) that high temperature catalyst comprises that the regeneration back without overcooled catalyzer, is also referred to as thermocatalyst (thermal regenerant).For example; The mixing of solid particulate of the present invention and gas stripping process are accomplished through the catalytic cracking reaction regeneration system rapidly; 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, said revivifier is outside equipped with heat collector.Heat collector (being also referred to as water cooler) the refrigerative regenerated catalyst of hanging oneself of first kind of solid particulate among the present invention, first kind of solid particulate among the present invention from through revivifier regeneration back without overcooled catalyzer.

Fig. 1 and Fig. 2 show the main TV structure of two kinds of gas-solid loop flow mixing strippers of the embodiment of the invention; Fig. 3 and Fig. 4 show the principle of work and the process of gas-solid loop flow mixing stripper; Fig. 5 shows the sectional structure of preceding two kinds of gas-solid loop flow mixing strippers, and Figure 11 shows the main TV structure of the third gas-solid loop flow mixing stripper.Introduce preceding two kinds of gas-solid loop flow mixing strippers below earlier.

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 said cylindrical shell 7 and with the guide shell 6 of said cylindrical shell 7 coaxial arrangement, the annular space gas distributor 3 of 67 bottoms, annular space space between said cylindrical shell 7 and the said guide shell 6, be arranged in said 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 said cylindrical shell 7 inner chambers, said cylindrical shell 7 lower ends and blended solid particle outlet 1 below cone 2 is connected, is arranged on said cone 2, be arranged in cone 2 bottoms and be in the loosening steam 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 inside of said 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, said cylindrical shell 7 can be cylinder with said 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 said cylindrical shell 7.The inner chamber of said cylindrical shell 7 comprises: the internal space of said annular space space 67 and said guide shell 6; Said 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 said guide shell 6 and with said 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.Said guide shell gas distributor 11 is positioned under the said 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 said guide shell 6, the vertical projection district that guide shell gas distributor 11 is positioned at said guide shell 6 through guide shell gas distributor inlet tube 35 with to annular space space 67 air feed.Loosening steam ring 12 is identical or similar with the structure of annular space gas distributor 3, and only the diameter of ring is less.Loosening steam ring 12 feeds loosening wind, and loosening wind is steam for example, 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 loosening steam 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 said guide shell 6 is provided with the internal space of perforate 13, said perforate 13 connections said annular space space 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 are staggered arrangement or non-staggered arrangement, the width of adjacent two rows of openings and highly equal or unequal, 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, said perforate 13 is a plurality of long strip shapes holes like Fig. 5, and 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, and the radius of said perforate is smaller or equal to 0.5 times of 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.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 said guide shell 6 and said 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; Extremely shown in Figure 4 like Fig. 1; Said gas-solid loop flow mixing stripper also comprises: cover the end socket 8 at the said cylinder lumen of said cylindrical shell upper end closed; Wherein, the said pneumatic outlet that extend in said cylindrical shell 7 inner chambers is the gas outlet tube 9 that is arranged on the end socket 8, and described guide shell 6 is 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.

Further, shown in figure 10, the gas-solid loop flow mixing stripper 200 among Fig. 2 can be accomplished 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.Shown in figure 10; Said fluid catalytic cracking process is accomplished through the catalytic cracking reaction regeneration system rapidly; Said catalytic cracking reaction regeneration system rapidly comprises: riser reactor 40, pre lift zone 30, revivifier 60, and said gas-solid loop flow mixing stripper 200 is arranged on outside riser reactor 40, pre lift zone 30 and the said revivifier 60; 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 connected with said pre lift zone.

Further; As shown in Figure 2; Said first kind of solid particle inlet pipe 5 takes level or oblique lower direction to be connected on the said cylindrical shell 7 with said second kind of solid particle inlet pipe 10; Said first kind of solid particle inlet pipe 5 is 20 °～90 ° with the axis angle γ of said cylindrical shell 7, and said second kind of solid particle inlet pipe 10 is 20 °～90 ° with the axis angle λ of said 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.Fluidization steam vapor is fed by annular space gas distributor, guide shell gas distributor and loosening steam 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.In the circulation mixing stripper is mixed catalyst, and temperature is lower, and it is also very low that the hot probability that collapses takes place catalyzer.

Progressive ground; As shown in Figure 1; Said first kind of solid particle inlet pipe 5 takes level or Way in obliquely to be connected on the said cylindrical shell 7 with said second kind of solid particle inlet pipe 10; The axis angle of the Way in of said first kind of solid particle inlet pipe 5 and said cylindrical shell 7 is 20 °～90 °, and the axis angle of the Way in of said second kind of solid particle inlet pipe 10 and said cylindrical shell 7 is 20 °～90 °.Adopted the gas-solid loop flow mixing stripper among Fig. 2 among Figure 10; Certainly; Gas-solid loop flow mixing stripper 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 said cylindrical shell 7 with said second kind of solid particle inlet pipe 10 said first kind of solid particle inlet pipe 5.

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

Top description has reflected the substruction of Fig. 1 and the described two kinds of gas-solid loop flow mixing strippers of Fig. 2; The described 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 said second kind of solid particle inlet pipe 10 is respectively obliquely or oblique lower direction; Making win kind of solid particulate and second kind of solid particulate all is to get into obliquely in the annular space space 67, or all is that oblique lower direction gets in the annular space space 67.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.

Below in conjunction with Fig. 3, be example with the gas-solid loop flow mixing stripper among Fig. 1, the working process and the principle of gas-solid loop flow mixing stripper is described:

Gas-solid loop flow mixing stripping utensil among Fig. 1 has end socket 8 and gas outlet tube 9; Said first kind of solid particle inlet pipe 5 taked level or Way in obliquely to be connected to the both sides of said cylindrical shell 7 with said second kind of solid particle inlet pipe 10 and is communicated with annular space space 67; The axis angle α of the Way in of said first kind of solid particle inlet pipe 5 and said cylindrical shell 7 is 20 °～90 °, the axis angle of the Way in of said second kind of solid particle inlet pipe 10 and said 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 mobile, in guide shell, flow downward.Catalyzer has level or speed obliquely via cold catalyst inlet pipe 5, when thermocatalyst inlet tube 10 gets into annular space spaces 67, 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 separation district 65 horizontal directions is greater than guide shell or annular space district, so also reduction greatly of gas velocity, the catalyzer of solid particulate has been realized separating with fluidizing agent or steam; No longer continue to rise; The catalyzer of solid particulate changes flow direction, becomes 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; As shown in Figure 5; Cone 2 is shunk gradually, and guide shell gas distributor 11 and annular space gas distributor 3 are arranged at the top of cone 2, circulates again so most of catalyzer is sent into annular space space 67 by guide shell gas distributor 11 and annular space gas distributor 3; The cone 2 of having only the sub-fraction catalyzer to get into the bottom through the edge, perhaps still less sub-fraction catalyzer gets into the cone 2 of bottom and flows 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; In the following space of guide shell part catalyzer for example, the cone 2 that filled arrows Cd2 gets into the bottom also flows out circulation mixing stripper, most of catalyzer; See then circulation entering annular space space 67 of filled arrows Cd1, circulate again, 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 loosening steam ring 12 fed fluidization steam vapor, fluidization steam vapor and loosening wind respectively.Fluidization steam vapor 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, adopt gas-solid loop flow mixing stripper 200 shown in Figure 2 to carry out the operation of central gas lift-type, 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, i.e. the filled arrows C20 perforate 13 of passing guide shell 6 gets in the guide shells 6 inherent guide shells 6 to last mobile formation filled arrows C40; The top entering that filled arrows C40 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.

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 C d10 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 loosening steam ring 12 fed fluidization steam vapor, fluidization steam vapor and loosening wind respectively.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, catalyzer generally will promptly mix and reallocate for 6～15 times and could flow out circulation mixing stripper through 6～15 circulations, and the catalyzer residence time reaches 143 seconds, so mixed effect is very good.

Mode of operation to gas-solid loop flow mixing stripper 100 shown in Figure 1 is described above, and gas-solid loop flow mixing stripper shown in Figure 1 can adopt the annular space gas lifting type operator scheme.For gas-solid loop flow mixing stripper 200 shown in Figure 2, can adopt central gas lift-type operator scheme.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 said cylindrical shell 7; Can also make first kind of solid particle inlet pipe 5 be connected the side direction of said cylindrical shell 7; Second kind of solid particle inlet pipe 10 is connected the top of said cylindrical shell 7, and said blended solid particle outlet 1 is connected with said pre lift zone; Perhaps first kind of solid particle inlet pipe 5 is connected the top of said cylindrical shell 7, and second kind of solid particle inlet pipe 10 is connected the side direction of said cylindrical shell 7, and said blended solid particle outlet 1 is connected with said pre lift zone.

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 said revivifier 60 directly is communicated with the top of said cylindrical shell 7; Cold catalyzer is introduced by first kind of solid particle inlet pipe; Said first kind of solid particle inlet pipe extend into from the outside of said revivifier said cylindrical shell 7 side direction and with said annular space spatial communication, heat (regeneration) catalyzer directly gets into 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 loosening steam ring 12 still can adopt the structure among Fig. 1 and Fig. 2.

Shown in figure 11, said gas-solid loop flow mixing stripper 300 is arranged within the said revivifier 60, for example is positioned at regenerator and takes out the exit, promptly is positioned at the thermocatalyst exit.Said cylindrical shell 7 is surrounded by inboard wall and a lateral arc of revivifier 60 jointly; The top of said cylindrical shell 7 is uncovered; The inner chamber of said cylindrical shell directly is communicated with the inner chamber of said revivifier 60; Said first kind of solid particulate admission passage is first kind of solid particle inlet pipe; Said first kind of solid particle inlet pipe 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.This gas-solid loop flow mixing stripper 300 that end socket 8 and gas outlet tube 9 are not set is discharged annular space gas distributor 3, guide shell gas distributor 11 and loosening steam ring 12 used fluidizing agent or steam through the inner chamber of revivifier 60, and this gas-solid loop flow mixing stripper 300 can adopt central gas lift-type operator scheme.

The advantage of this built-in gas-solid loop flow mixing stripper 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.(4) said cylindrical shell 7 is surrounded by inboard wall and a lateral arc of revivifier 60 jointly, and like this, the inboard wall utilization ratio of revivifier 60 provides, and has simplified the making of circulation mixing stripper, has saved material, has reduced cost.Though after circulation mixing stripper is arranged on internal regenerator; Can occupy the space of partial regeneration device; But maximization gradually along with device; The diameter of catalytic cracking regenerator can reach more than the 10m, and circulation mixing stripper has only occupied very little a part of space, and the regeneration effect of revivifier is not had influence basically.

The present invention also provides a kind of mixing and gas stripping process of solid particulate; The mixing of said solid particulate and gas stripping process are accomplished through the catalytic cracking reaction regeneration system rapidly; 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; Said revivifier is outside equipped with heat collector

Like Fig. 3, Fig. 4, Figure 10 and shown in Figure 11, the mixing and the gas stripping process of said solid particulate comprise:

A, first kind of solid particulate and second kind of solid particulate are incorporated into respectively in the inside of said cylindrical shell 7, make first kind of solid particulate and second kind of solid particulate in cylindrical shell and guide shell, accomplish heat exchange;

The present invention has also realized high efficiency stripping when two kinds of solid particulates of completion fully carry out mixed heat transfer.

Further; As shown in Figure 3; Steps A comprises: A1: with first kind of solid particulate and second kind of solid particulate level or be transported to obliquely in the said 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.

Further; Shown in figure 10; Steps A comprises: A2: 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, mobile for making progress said guide shell 6 in.

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 inside of said revivifier 60 directly is communicated with the top of said cylindrical shell 7; Cold catalyzer is introduced by first kind of solid particle inlet pipe; Said first kind of solid particle inlet pipe extend into from the outside of said revivifier said cylindrical shell 7 side direction and with said annular space spatial communication, heat (regeneration) catalyzer directly gets into 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 loosening steam ring 12 still can adopt the structure among Fig. 1 and Fig. 2.

Further; Shown in figure 11; Steps A comprises: A3: first kind of solid particulate (cold catalyzer) with level or oblique under direction be transported in the said annular space space, second kind of solid particulate directly enters into said cylindrical shell 7 and said guide shell 6 from the top of said cylindrical shell 7 and said guide shell 6, said gas-solid loop flow mixing stripper is arranged within the said revivifier 60; For example be positioned at regenerator and take out the exit, promptly be positioned at the thermocatalyst exit.Said cylindrical shell 7 is surrounded by inboard wall and a lateral arc of revivifier 60 jointly; The top of said cylindrical shell 7 is uncovered; The inside of said cylindrical shell directly is communicated with the inside of said revivifier 60; Said first kind of solid particulate admission passage is first kind of solid particle inlet pipe; Said first kind of solid particle inlet pipe 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 inside of said revivifier and the top of said cylindrical shell.This gas-solid loop flow mixing stripper 300 can adopt central gas lift-type operator scheme.

The advantage of this method has: (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.(4) said cylindrical shell 7 is surrounded by inboard wall and a lateral arc of revivifier 60 jointly, and like this, the inboard wall utilization ratio of revivifier 60 improves, and has simplified the making of circulation mixing stripper, has saved material, has reduced cost.

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

(1) hot and cold catalyzer in circulation mixing stripper along having realized mixing and reallocation repeatedly in the circulating of setting path; Considerably beyond the residence time of pre lift zone mixing tank; Not only can realize mixing completely; And have the competent heat transfer time, more better than the mixed effect of pre lift zone.(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) 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.(4) 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 mixing stripper 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.(5) 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.

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

1. gas-solid loop flow mixing stripper; It is characterized in that; 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: the cylindrical shell (7) with inner chamber; Be arranged in the inner chamber of said cylindrical shell (7) and with the guide shell (6) of said cylindrical shell (7) coaxial arrangement; Be positioned at the annular space gas distributor (3) of the bottom, annular space space between said cylindrical shell (7) and the said guide shell (6); Be arranged in said cylindrical shell (7) and be positioned at the guide shell gas distributor (11) under the guide shell (6); Extend into the pneumatic outlet in said cylindrical shell (7) inner chamber; Said cylindrical shell (7) lower end is connected with cone (2); Be arranged on the blended solid particle outlet (1) of said cone (2) below; Be positioned at cone (2) bottom and be in the loosening steam ring (12) of blended solid particle outlet (1) top; And the first kind of solid particle inlet pipe (5) and the second kind of solid particle inlet pipe (10) that are connected respectively to the inside of said cylindrical shell (7);

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. gas-solid loop flow mixing stripper as claimed in claim 1 is characterized in that, the barrel of said guide shell (6) is provided with the internal space of perforate (13), said perforate (13) connection said annular space space and guide shell (6);

Said perforate is a plurality of long strip shapes holes, and 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, and the radius of said perforate is smaller or equal to 0.5 times of 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.

3. gas-solid loop flow mixing stripper as claimed in claim 1 is characterized in that, the radial cross-section of said guide shell (6) and said cylindrical shell (7) is long-pending than being 0.2～0.8.

4. gas-solid loop flow mixing stripper as claimed in claim 1; It is characterized in that; Said cylindrical shell (7) upper end is internally connected with end socket (8), and wherein, the gas outlet tube (9) that is arranged on the end socket (8) is the pneumatic outlet in cylindrical shell (7) inner chamber; Said gas-solid loop flow mixing stripper also comprises: end socket (8) and gas outlet tube (9), described guide shell (6) is vertical layout with cylindrical shell (7).

5. like each described gas-solid loop flow mixing stripper in the claim 1 to 4, it is characterized in that,

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 said cylindrical shell (7) both sides and all with said annular space spatial communication;

Perhaps, first kind of solid particle inlet pipe (5) is connected the side direction of said cylindrical shell (7), and second kind of solid particle inlet pipe (10) is connected the top of said cylindrical shell (7);

Perhaps, first kind of solid particle inlet pipe (5) is connected the top of said cylindrical shell (7), and second kind of solid particle inlet pipe (10) is connected the side direction of said cylindrical shell (7).

6. gas-solid loop flow mixing stripper as claimed in claim 5; It is characterized in that; Said first kind of solid particle inlet pipe (5) and said second kind of solid particle inlet pipe take level or Way in obliquely to be connected on the said cylindrical shell (7); The axis angle of the Way in of said first kind of solid particle inlet pipe (5) and said cylindrical shell (7) is 20 °～90 °, and the axis angle of the Way in of said second kind of solid particle inlet pipe (10) and said cylindrical shell (7) is 20 °～90 °; Perhaps

Said first kind of solid particle inlet pipe (5) and said second kind of solid particle inlet pipe (10) take level or oblique lower direction to be connected on the said cylindrical shell (7); Said first kind of solid particle inlet pipe (5) is 20 °～90 ° with the axis angle of said cylindrical shell (7), and said second kind of solid particle inlet pipe (10) is 20 °～90 ° with the axis angle of cylindrical shell (7).

7. gas-solid loop flow mixing stripper as claimed in claim 6; It is characterized in that; The said first solid kind particle inlet tube (5) and said second kind of solid particle inlet pipe (10) are symmetrical set about the axis of said cylindrical shell (7); Be respectively arranged with in said first kind of solid particle inlet pipe (5) and the said second kind of solid particle inlet pipe (10) and carry airduct (4); The defeated wind direction of the conveying airduct in said first kind of solid particle inlet pipe (5) is identical with the Way in of said first kind of solid particle inlet pipe (5), and the defeated wind direction of the conveying airduct in said second kind of solid particle inlet pipe (10) is identical with the Way in of said second kind of solid particle inlet pipe (10).

8. like each described gas-solid loop flow mixing stripper in the claim 1 to 3, it is characterized in that,

The mixing of said first kind of solid particulate and second kind of solid particulate and stripping process are accomplished through the catalytic cracking reaction regeneration system rapidly; Said catalytic cracking reaction regeneration system rapidly comprises: riser reactor, pre lift zone and revivifier; 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; 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.

9. the mixing of a solid particulate and gas stripping process; Be used for first kind of solid particulate and second kind of solid particulate that fluid catalytic cracking process mixes differing temps; And strip 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, it is characterized in that

The mixing of said solid particulate is adopted like each described gas-solid loop flow mixing stripper in the claim 1 to 3 with gas stripping process;

The mixing and the gas stripping process of said solid particulate comprise:

A, first kind of solid particulate and second kind of solid particulate are incorporated into respectively in the inner chamber of said cylindrical shell (7), make first kind of solid particulate and second kind of solid particulate in cylindrical shell and guide shell, accomplish heat exchange;

10. the mixing of solid particulate as claimed in claim 9 and gas stripping process; It is characterized in that first kind of solid particulate is low temperature catalyst or low temperature spent agent, 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; First kind of solid particulate is low temperature catalyst or low temperature spent agent, and second kind of solid particulate is high temperature catalyst, and steps A comprises:

A1: 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, with first kind of solid particulate and second kind of solid particulate level or be transported to obliquely in the said annular space space.

11. the mixing of solid particulate as claimed in claim 9 and gas stripping process is characterized in that, first kind of solid particulate is low temperature catalyst or low temperature spent agent, and second kind of solid particulate is high temperature catalyst, and steps A comprises:

A2: 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, with first kind of solid particulate and second kind of solid particulate level or oblique under be transported in the said annular space space.

12. the mixing of solid particulate as claimed in claim 9 and gas stripping process; It is characterized in that first kind of solid particulate is low temperature catalyst or low temperature spent agent, 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; First kind of solid particulate is low temperature catalyst or low temperature spent agent, and second kind of solid particulate is high temperature catalyst, and steps A comprises:

A3: what make said guide shell gas distributor (11) gives the give tolerance of tolerance greater than said annular space gas distributor (3); Make win kind of solid particulate and second kind of solid particulate in said annular space for flowing downward; Mobile for upwards in said guide shell (6); First kind of solid particulate is transported in the said annular space space with level or direction obliquely, and second kind of solid particulate enters into said guide shell (6) downwards from the top of said guide shell (6).