CN102676206B

CN102676206B - Gas/solid circulation mixing steam stripper and mixing and steam stripping method of solid particles

Info

Publication number: CN102676206B
Application number: CN201210152928.2A
Authority: CN
Inventors: 刘梦溪; 卢春喜; 王祝安; 范怡平
Original assignee: China University of Petroleum Beijing
Current assignee: China University of Petroleum Beijing
Priority date: 2012-05-16
Filing date: 2012-05-16
Publication date: 2014-04-09
Anticipated expiration: 2032-05-16
Also published as: CN102676206A

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 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, for the stripping of the solid particulate in the mixing and mix of two kinds of solid particulates (between regenerator and/or between spent agent) of differing temps between fluid catalytic cracking process riser tube and fluidized-bed.

Background technology

Fluid catalytic cracking is important crude oil secondary processing means, has huge economic benefit.Catalytic cracking reaction regeneration system rapidly is comprised of riser reactor, revivifier and line of pipes conventionally.Stock oil by nozzle atomization after, in riser reactor, contact with high-temperature regenerated catalyst, gasification, there is heat cracking reaction and catalyzed reaction, meanwhile there is condensation reaction and produce coke, coke is attached to catalyst surface and makes catalyst deactivation, the catalyzer of inactivation (spent agent) enters stripping stage after leg outlet is separated by gas-solid separation equipment, in stripping stage, spent agent entrained oil gas is replaced away by stripped vapor, then spent agent enters the revivifier regeneration of burning by pipeline to be generated, catalyzer after regeneration (regenerator) enters riser tube bottom by regeneration pipeline.The reaction product of catalytic cracking both object product likely, as gasoline, diesel oil, liquefied gas, also has and does not wish the byproduct that produces, as dry gas.

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

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

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

It is the patent of invention that 200710152287.X, name are called annular space air-lift gas-solid loop flow reactor that contriver also once proposed the patent No..This patent is introduced one catalyzer from solid particulate feed-pipe (being 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 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 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 object 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 after solid particulate mixed heat transfer.Therefore, in prior art, two kinds of solid particulates (between regenerator and/or between spent agent) of differing temps are difficult to the mixed heat transfer fully carrying out, and in prior art, also cannot when two kinds of solid particulates mix, carry out stripping.

Summary of the invention

The present invention aims to provide 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 to solve two kinds of solid particulates (between regenerator and/or between spent agent) of differing temps in fluid catalytic cracking process, simultaneously, the present invention has also solved prior art cannot carry out steam stripped problem when mixing, and makes the present invention also realize stripping completing when two kinds of solid particulates fully carry out mixed heat transfer.

For this reason, the invention provides a kind of gas-solid loop flow mixing stripper, fluid catalytic cracking process for reconstituted form mixes the first solid particulate and the second solid particulate of differing temps, and strip flue gas and the air that the first solid particulate and the second solid particulate are carried secretly, the first solid particulate can be low temperature catalyst or low temperature spent agent, the second solid particulate can be high temperature catalyst, and the temperature of the second solid particulate is higher than the temperature of the first solid particulate, described gas-solid loop flow mixing stripper comprises: have inner cylindrical shell 7, be arranged in the inside of described cylindrical shell and the guide shell 6 coaxially arranged with described cylindrical shell, the annular space gas distributor 3 of the bottom, annular space space between described cylindrical shell 7 and described guide shell 6, be arranged in described cylindrical shell and be positioned at the guide shell gas distributor 11 under annular space gas distributor 3, extend into the pneumatic outlet in described cylindrical shell 7 inside, described cylindrical shell 7 lower ends are connected with cone 2, be arranged on the blended solid particle outlet 1 of described cone 2 belows, be positioned at cone 2 bottoms and the loosening steam ring 12 in blended solid particle outlet 1 top, and be connected respectively to the first solid particulate admission passage and the second solid particulate admission passage in the inside of described cylindrical shell,

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

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

Further, described perforate is a plurality of long strip shapes holes, and the height of described perforate is less than or equal to 0.9 times of described guide shell 6 height, and the total area of described perforate is less than or equal to the lateral area of the guide shell 6 of 0.9 times; Or

Described perforate is a plurality of circular ports, and the radius of described perforate is less than or equal to 0.5 times of guide shell 6 height, and the total area of described perforate is less than or equal to the lateral area of the guide shell 6 of 0.9 times.

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

Further, described gas-solid loop flow mixing stripper also comprises: cover the end socket 8 at cylinder lumen described in described cylindrical shell upper end closed, wherein, the described pneumatic outlet extending in described cylindrical shell 7 inner chambers is the gas outlet tube 9 being arranged on end socket 8, and described guide shell 6 is and is arranged vertically with cylindrical shell 7.

Further, described the first solid particulate admission passage is the first solid particle inlet pipe 5, described the second solid particulate admission passage is the second solid particle inlet pipe 10, the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10 are connected to the both sides of described cylindrical shell 7 and are all communicated with described annular space space, and described blended solid particle outlet 1 can be connected with described pre lift zone;

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

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

Further, described the first solid particle inlet pipe 5 and described the second solid particle inlet pipe take level or Way in to be obliquely connected on described cylindrical shell 7, the Way in of described the first solid particle inlet pipe 5 and the axis angle of described cylindrical shell 7 are 20 °～90 °, and the Way in of described the second solid particle inlet pipe 10 and the axis angle of described cylindrical shell 7 are 20 °～90 °.

Further, described the first solid particle inlet pipe 5 and described the second solid particle inlet pipe 10 axis about described cylindrical shell 7 are symmetrical arranged, in described the first solid particle inlet pipe 5 and described the second solid particle inlet pipe 10, be respectively arranged with and carry airduct 4, the defeated wind direction of the conveying airduct in described the first solid particle inlet pipe 5 is identical with the Way in of described the first solid particle inlet pipe 5, the defeated wind direction of the conveying airduct in described the second solid particle inlet pipe 10 is identical with the Way in of described the second solid particle inlet pipe 10.

Further, described the first solid particle inlet pipe 5 and described the second solid particle inlet pipe 10 take level or oblique downward direction to be connected on described cylindrical shell 7, described the first solid particle inlet pipe 5 is 20 °～90 ° with the axis angle of described cylindrical shell 7, and described the second solid particle inlet pipe 10 is 20 °～90 ° with the axis angle of described cylindrical shell 7.

Further, mixing and the stripping process of described the first solid particulate and the second solid particulate complete by catalytic cracking reaction regeneration system rapidly, the mixing of described the first solid particulate and the second solid particulate mixes the first solid particulate and the second solid particulate of differing temps with stripping process, and strip flue gas that the first solid particulate and the second solid particulate carry secretly and the process of air, described catalytic cracking reaction regeneration system rapidly comprises: riser reactor, pre lift zone and revivifier, within described gas-solid loop flow mixing stripper is arranged on described revivifier, described cylindrical shell 7 is surrounded jointly by the inner side wall of revivifier and the arc of a side, the top of described cylindrical shell is uncovered, the inner chamber of described cylindrical shell is directly communicated with the inner chamber of described revivifier,

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

The present invention also provides a kind of mixing and gas stripping process of solid particulate, for fluid catalytic cracking process, mix the first solid particulate and the second solid particulate of differing temps, and strip flue gas and the air that the first solid particulate and the second solid particulate are carried secretly, the temperature of the second solid particulate is higher than the temperature of the first solid particulate, the mixing of described solid particulate and gas stripping process can complete by catalytic cracking reaction regeneration system rapidly, described catalytic cracking reaction regeneration system rapidly comprises: riser reactor, the pre lift zone being connected with riser reactor, revivifier and line of pipes, described revivifier is outside equipped with heat collector,

The mixing of described solid particulate adopts foregoing gas-solid loop flow mixing stripper with gas stripping process;

Mixing and the gas stripping process of described solid particulate comprise:

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

B, in heat exchange, strip flue gas and air that the first solid particulate and the second solid particulate are carried secretly.

The first solid particulate is low temperature catalyst or low temperature spent agent, the second solid particulate is high temperature catalyst, the temperature of the second solid particulate is low temperature catalyst or low temperature spent agent higher than a kind of solid particulate of temperature control of the first solid particulate, the second solid particulate is high temperature catalyst, and the temperature of the second solid particulate is higher than the temperature of the first solid particulate.

Progressive ground, steps A comprises: A1: by the first solid particulate and the second solid particulate level or be transported to obliquely in described annular space space, what make described annular space gas distributor 3 is greater than the tolerance of giving of described guide shell gas distributor 11 to tolerance, make the first solid particulate and the second solid particulate in described annular space for upwards flowing, in described guide shell 6 for flowing downward.

Further, steps A comprises: A2: by the first solid particulate and the second solid particulate level or oblique under be transported in described annular space space, what make described annular space gas distributor 3 is less than the tolerance of giving of described guide shell gas distributor 11 to tolerance, make the first solid particulate and the second solid particulate in described annular space space for flowing downward, in described guide shell 6 for upwards flowing.

Further, steps A comprises:

A3: what make described guide shell gas distributor 11 is greater than the tolerance of giving of described annular space gas distributor 3 to tolerance, make the first solid particulate and the second solid particulate in described annular space for flowing downward, in described guide shell 6, for making progress, flow, the first solid particulate is transported in described annular space space with level or direction obliquely, and the second solid particulate enters into described guide shell 6 from described guide shell 6 to next top.By controlling air demand, what make guide shell gas distributor 11 gives the different to tolerance of tolerance and annular space gas distributor 3, in guide shell bottom, produce pressure difference, promote solid particulate (catalyzer) circulates between annular space and guide shell, its flow pattern or be solid particulate in annular space on flow, in guide shell, flow downward; Or be solid particulate in annular space on flow, in guide shell, flow downward.

Which kind of flow pattern no matter, when the first solid particulate and the second solid particulate enter into the inner chamber of cylindrical shell, the solid particulate and the second solid particulate not only circulate respectively between annular space and guide shell, completed stripping, and flowing of the first solid particulate and flowing also to form mutually to intersect to mix in the inner chamber of cylindrical shell and having realized heat exchange of the second solid particulate, in a heat transfer process, the first solid particulate and the second solid particulate do not reach completely and mix after mixing, but form the cold of different sizes, hot solids particle (catalyzer) group, these are cold, hot solids particle (catalyzer) group is mingled with mutually, the process that enters annular space space by guide shell circulation be one by cold, hot solids particle (catalyzer) the group fragmentation newly assigned process of laying equal stress on, the process that is entered guide shell by annular space space is a process of again mixing.And then, on the guide shell of circulation mixing stripper, having hole, catalyzer not only mixes in the upper and lower of guide shell, and can mix through hole, thereby has efficient mixed effect.

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

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

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

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

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

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

And then, hot and cold catalyzer has been realized mixing and reallocation repeatedly along circulating of setting path is middle in circulation mixing stripper, experimental study shows, hot and cold catalyzer is wanted circulation 6～15 times, and (going through 6～15 mixing) just can flow out mixing stripper, its residence time reaches 143 seconds, considerably beyond the residence time of pre lift zone mixing tank, not only can realize completely and mixing, and there is the sufficient heat transfer time.

The gas-solid loop flow mixing stripper that the present invention proposes has utilized the theory of particle circulation cleverly; by catalyzer (spent agent or regenerator) in inside and outside the circulating of guide shell; and mixing repeatedly, reallocation, really realized the even mixing of hot and cold catalyzer, conducted heat and the temperature distribution of homogeneous for a long time.Especially with respect to the 2nd kind of mode of introducing in background technology, the present invention can regulate respectively control to the temperature of cold catalyst inlet pipe 5 and thermocatalyst inlet tube 10 and flow, both can obtain entering the ideal temperature of pre lift zone, can obtain sufficient flow again, setting range is very extensive, and the mixed catalyzer that simultaneously guarantees temperature and flow can be provided flexibly.

Accompanying drawing explanation

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

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

Fig. 3 is the Principle of Process figure while adopting annular space gas lifting type operator scheme according to the first gas-solid loop flow mixing stripper of the embodiment of the present invention;

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

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

Fig. 6 is the first structure of guide shell;

Fig. 7 is the second structure of guide shell;

Fig. 8 is the third structure of guide shell;

Fig. 9 is the 4th kind of structure of guide shell;

Figure 10 be in catalytic cracking reaction regeneration system rapidly, adopt according to the second gas-solid loop flow mixing stripper of the embodiment of the present invention;

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

Drawing reference numeral explanation:

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

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

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

11, guide shell gas distributor 12, 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

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

The invention provides a kind of gas-solid loop flow mixing stripper, for the fluid catalytic cracking process of reconstituted form, mix the first solid particulate and the second solid particulate of differing temps, and mixed solid particulate is stripped to flue gas and the air of carrying secretly.Certainly, the present invention also can be due to the fluid catalytic cracking process of non-renewable form.Fluid catalytic cracking process for reconstituted form is example, and the first solid particulate is low temperature catalyst or low temperature spent agent, and the second solid particulate is high temperature catalyst, and the temperature of the second solid particulate is higher than the temperature of the first solid particulate.Low temperature catalyst for example comprises after regeneration, through (passing through heat collector) cooling catalyzer (cold regenerator), and also referred to as cold catalyzer, high temperature catalyst comprises after regeneration without overcooled catalyzer, also referred to as thermocatalyst (thermal regenerant).For example, the mixing of solid particulate of the present invention and gas stripping process complete by catalytic cracking reaction regeneration system rapidly, described catalytic cracking reaction regeneration system rapidly comprises: riser reactor, the pre lift zone being connected with riser reactor, revivifier and line of pipes, described revivifier is outside equipped with heat collector.The first solid particulate in the present invention cooling regenerated catalyst of heat collector (also referred to as water cooler) of hanging oneself, the first solid particulate in the present invention from after revivifier regeneration 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 present invention, Fig. 3 and Fig. 4 show principle of work and the process of gas-solid loop flow mixing stripper, Fig. 5 shows the sectional structure of first two gas-solid loop flow mixing stripper, and Figure 11 shows the main TV structure of the third gas-solid loop flow mixing stripper.First introduce first two gas-solid loop flow mixing stripper below.

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

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

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

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

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

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

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

Further, as shown in figure 10, the gas-solid loop flow mixing stripper 200 in Fig. 2 can complete separately mixing and the steam stripped function of catalyzer, with alleviate upstream and downstream operation burden and and upstream and downstream operation cooperatively interact.As shown in figure 10, described fluid catalytic cracking process completes by catalytic cracking reaction regeneration system rapidly, described catalytic cracking reaction regeneration system rapidly comprises: riser reactor 40, pre lift zone 30, revivifier 60, and described gas-solid loop flow mixing stripper 200 is arranged on outside riser reactor 40, pre lift zone 30 and described revivifier 60; Described the first solid particulate admission passage is the first solid particle inlet pipe 5, described the second solid particulate admission passage is the second solid particle inlet pipe 10, the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10 are connected to the both sides of described cylindrical shell 7 and are all communicated with described annular space space, and described blended solid particle outlet 1 is connected with described pre lift zone.

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

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

Progressive ground, as shown in Figure 1, described the first solid particle inlet pipe 5 and described the second solid particle inlet pipe 10 take level or Way in to be obliquely connected on described cylindrical shell 7, the Way in of described the first solid particle inlet pipe 5 and the axis angle of described cylindrical shell 7 are 20 °～90 °, and the Way in of described the second solid particle inlet pipe 10 and the axis angle of described cylindrical shell 7 are 20 °～90 °.In Figure 10, adopted the gas-solid loop flow mixing stripper in Fig. 2, certainly, gas-solid loop flow mixing stripper in Fig. 1 also can be applied in the catalytic cracking reaction regeneration system rapidly shown in Figure 10, but will take level or Way in to be obliquely connected on described cylindrical shell 7 described the first solid particle inlet pipe 5 and described the second solid particle inlet pipe 10.

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

Description has above reflected the basic structure of two kinds of gas-solid loop flow mixing strippers described in Fig. 1 and Fig. 2, the setting party that two kinds of gas-solid loop flow mixing stripper key distinctions described in Fig. 1 and Fig. 2 are the first solid particle inlet pipe 5 and described the second solid particle inlet pipe 10 is to being respectively obliquely or oblique downward direction, making the first solid particulate and the second solid particulate is all to enter obliquely in annular space space 67, or is all that oblique downward direction enters in 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, for the gas-solid loop flow mixing stripper 100 in Fig. 1, can adopt annular space gas lifting type operator scheme, the gas-solid loop flow mixing stripper 200 in Fig. 2 can adopt central gas lift-type operator scheme.Central gas lift-type operator scheme refers to granules of catalyst (solid particulate) and for making progress, flows in guide shell 6, at guide shell 6 with mix in the annular space of 7 of stripper cylindrical shells and flow downward, annular space gas lifting type operator scheme refer to granules of catalyst in annular space for upwards flowing, in guide shell 6 for flowing downward.When guide shell gas distributor 11 to tolerance be greater than annular space gas distributor 3 give tolerance (referring to flow) time, gas-solid loop flow mixing stripper (also referred to as circulation mixing stripper) operates with central gas lift-type circulating current system, when annular space gas distributor 3 to tolerance be greater than guide shell gas distributor 11 give tolerance time, circulation mixing stripper operates with annular space gas lifting type circulating current system.

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

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

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

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

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

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

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

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

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

As shown in Figure 4, adopt the gas-solid loop flow mixing stripper 200 shown in Fig. 2 to carry out the operation of central gas lift-type, cold catalyzer shows as filled arrows C while just having entered annular space space 67 with the direction under oblique, because catalyzer under central gas lift-type operator scheme flows downward in annular space, in guide shell on flow, filled arrows C is divided into filled arrows C10 and C20, filled arrows C10 flows downward in annular space space 67, to change into behind the bottom in annular space space 67 guide shell 6 interior on flow and form filled arrows C30, because guide shell 6 has perforate 13, a part for cold catalyzer, it is interior to upper mobile formation filled arrows C40 that to be filled arrows C20 enter the inherent guide shell 6 of guide shell 6 through the perforate 13 of guide shell 6, the top that filled arrows C40 is raised to annular space space 67 enters the gas solid separation district 65 being positioned on guide shell, no longer continue to rise, the catalyzer of solid particulate changes flow direction, become macro-flow radially.

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

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

Above-mentioned filled arrows represents each granules of catalyst group, and when hot and cold catalyzer is rolled into a ball heat exchange, annular space gas distributor 3, guide shell gas distributor 11 and loosening steam ring 12 pass into respectively fluidization steam vapor, fluidization steam vapor and loosening wind.Loosening wind can be steam.The every circulation primary of catalyzer just means with bottom live steam and contacts once, so steam stripping efficiency is also very high.According to experimental result, catalyzer generally will 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.

Above the mode of operation of the gas-solid loop flow mixing stripper 100 shown in Fig. 1 is described, the gas-solid loop flow mixing stripper shown in Fig. 1 can adopt annular space gas lifting type operator scheme.For the gas-solid loop flow mixing stripper 200 shown in Fig. 2, can adopt central gas lift-type operator scheme.For the gas-solid loop flow mixing stripper shown in Fig. 2, except adopting the first solid particle inlet pipe 5 and the second solid particle inlet pipe 10 to be connected to the mode of the both sides of described cylindrical shell 7, can also make the first solid particle inlet pipe 5 be connected to the side direction of described cylindrical shell 7, the second solid particle inlet pipe 10 is connected to the top of described cylindrical shell 7, and described blended solid particle outlet 1 is connected with described pre lift zone; Or the first solid particle inlet pipe 5 is connected to the top of described cylindrical shell 7, the second solid particle inlet pipe 10 is connected to the side direction of described cylindrical shell 7, and described blended solid particle outlet 1 is connected with described pre lift zone.

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

As shown in figure 11, described gas-solid loop flow mixing stripper 300 is for example positioned at regenerator and takes out exit within being arranged on described revivifier 60, is positioned at thermocatalyst exit.Described cylindrical shell 7 is surrounded jointly by the inner side wall of revivifier 60 and the arc of a side, the top of described cylindrical shell 7 is uncovered, the inner chamber of described cylindrical shell is directly communicated with the inner chamber of described revivifier 60, described the first solid particulate admission passage is the first solid particle inlet pipe, described the first solid particle inlet pipe extend into the side direction of described cylindrical shell 7 and is communicated with described annular space space, the described the second solid particulate of the uncovered formation admission passage at the inner chamber of described revivifier and the top of described cylindrical shell from the outside of described revivifier.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 fluidizing agent or steam used by 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), when site layout project space is not or during insufficient height, is placed on internal regenerator by circulation mixing stripper, can save large quantity space; (2) do not need catalyst recycle line to transform, thereby install and overhaul very simply, the operation of device is also very simple; (3) circulation mixing stripper is placed on to internal regenerator, not only do not increase the resistance to flow of regeneration circuit, because extract mouth out at regenerator, be provided with circulation mixing stripper on the contrary, played the effect of flooding stream bucket that is similar to, increase regenerator pressure accumulation, increased the mobile impellent of regenerator.(4) described cylindrical shell 7 is surrounded jointly by the inner side wall of revivifier 60 and the arc of a side, and like this, the inner side wall utilization ratio of revivifier 60 provides, and has simplified the making of circulation mixing stripper, has saved material, has reduced cost.Although circulation mixing stripper is arranged on after internal regenerator, can occupy the space of partial regeneration device, but the maximization gradually along with device, more than the diameter of catalytic cracking regenerator can reach 10m, circulation mixing stripper has only occupied very little a part of space, and the regeneration effect of revivifier is not had to impact substantially.

The present invention also provides a kind of mixing and gas stripping process of solid particulate, the mixing of described solid particulate and gas stripping process complete by catalytic cracking reaction regeneration system rapidly, described catalytic cracking reaction regeneration system rapidly comprises: riser reactor, the pre lift zone being connected with riser reactor, revivifier and line of pipes, described revivifier is outside equipped with heat collector

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

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

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

Further, as shown in Figure 3, steps A comprises: A1: by the first solid particulate and the second solid particulate level or be transported to obliquely in described annular space space, what make described annular space gas distributor 3 is greater than the tolerance of giving of described guide shell gas distributor 11 to tolerance, make the first solid particulate and the second solid particulate in described annular space for upwards flowing, in described guide shell 6 for flowing downward.

Further, as shown in figure 10, steps A comprises: A2: by the first solid particulate and the second solid particulate level or oblique under be transported in described annular space space, what make described annular space gas distributor 3 is less than the tolerance of giving of described guide shell gas distributor 11 to tolerance, make the first solid particulate and the second solid particulate in described annular space space for flowing downward, in described guide shell 6 for upwards flowing.

Within gas-solid loop flow mixing stripper 300 is arranged on revivifier 60.The top of the cylindrical shell 7 of gas-solid loop flow mixing stripper 300 does not arrange end socket 8 and gas outlet tube 9, the inside of described revivifier 60 is directly communicated with the top of described cylindrical shell 7, cold catalyzer is introduced by the first solid particle inlet pipe, described the first solid particle inlet pipe extend into the side direction of described cylindrical shell 7 and is communicated with described annular space space from the outside of described revivifier, heat (regeneration) catalyzer directly enters cylindrical shell 7 by cylindrical shell 7 tops, thereby without thermocatalyst inlet tube 10 is set.Elsewhere, for example the structure of cylindrical shell 7, guide shell 6, annular space gas distributor 3, guide shell gas distributor 11 and loosening steam ring 12 still can adopt the structure in Fig. 1 and Fig. 2.

Further, as shown in figure 11, steps A comprises: A3: the first solid particulate (cold catalyzer) with level or oblique under direction be transported in described annular space space, the second solid particulate directly enters into described cylindrical shell 7 and described guide shell 6 from described cylindrical shell 7 and the top of described guide shell 6, within described gas-solid loop flow mixing stripper is arranged on described revivifier 60, for example be positioned at regenerator and take out exit, be positioned at thermocatalyst exit.Described cylindrical shell 7 is surrounded jointly by the inner side wall of revivifier 60 and the arc of a side, the top of described cylindrical shell 7 is uncovered, the internal direct of the inside of described cylindrical shell and described revivifier 60 is logical in succession, described the first solid particulate admission passage is the first solid particle inlet pipe, described the first solid particle inlet pipe extend into the side direction of described cylindrical shell 7 and is communicated with described annular space space, the described the second solid particulate of the uncovered formation admission passage at the inside of described revivifier and the top of described cylindrical shell from the outside of described revivifier.This gas-solid loop flow mixing stripper 300 can adopt central gas lift-type operator scheme.

The advantage of this method has: (1), when site layout project space is not or during insufficient height, is placed on internal regenerator by circulation mixing stripper, can save large quantity space; (2) do not need catalyst recycle line to transform, thereby install and overhaul very simply, the operation of device is also very simple; (3) circulation mixing stripper is placed on to internal regenerator, not only do not increase the resistance to flow of regeneration circuit, because extract mouth out at regenerator, be provided with circulation mixing stripper on the contrary, played the effect of flooding stream bucket that is similar to, increase regenerator pressure accumulation, increased the mobile impellent of regenerator.(4) described cylindrical shell 7 is surrounded jointly by the inner side wall of revivifier 60 and the arc of a side, and like this, the inner side 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 obvious advantage and useful effect:

(1) hot and cold catalyzer has been realized mixing and reallocation repeatedly along circulating of setting path is middle in circulation mixing stripper, considerably beyond the residence time of pre lift zone mixing tank, not only can realize completely and mixing, and there is the sufficient heat transfer time, more better than the mixed effect of pre lift zone.(2) on the guide shell of circulation mixing stripper, have hole or groove, catalyzer not only mixes in the upper and lower of guide shell, and can mix through hole or groove, thereby has efficient mixed effect; (3) when fluidizing medium adopts steam, can effectively strip the flue gas of carrying secretly in catalyzer, reduce the load of follow-up system pneumatic press.(4) conventional regeneration agent flue gas stripping device is interior because regenerator temperature is very high, after contacting with water stripping steam, very easily produce that heat collapses and hydrothermal deactivation, very big to catalyst impairment, but be mixed catalyzer in the mixing stripper that the present invention proposes, temperature is lower, and catalyzer heat occurs and 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 because two kinds of solid particulates hot and cold solid particulate (catalyzer) group when the mixed heat transfer is broken and redistribute; this has brought more multimachine meeting to the displacement of flue gas in catalyzer micropore; and every circulation primary just means live steam contact once; also make the vapor bubbles rising be sheared; greatly reduce bubble diameter; vapor bubbles is more easily entered or approach catalyzer micropore, so steam stripping efficiency is higher than the efficiency of other strippers.

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

Claims

1. a gas-solid loop flow mixing stripper, it is characterized in that, described gas-solid loop flow mixing stripper mixes the first solid particulate and the second solid particulate of differing temps for fluid catalytic cracking process, and stripping flue gas and the air that the first solid particulate and the second solid particulate are carried secretly, the temperature of the second solid particulate is higher than the temperature of the first solid particulate;

Described gas-solid loop flow mixing stripper comprises: the cylindrical shell (7) with inner chamber, be arranged in the inner chamber of described cylindrical shell (7) and the guide shell (6) coaxially arranged with described cylindrical shell (7), be positioned at the annular space gas distributor (3) of the bottom, annular space space between described cylindrical shell (7) and described guide shell (6), be arranged in described cylindrical shell (7) and be positioned at the guide shell gas distributor (11) under guide shell (6), extend into the pneumatic outlet in described cylindrical shell (7) inner chamber, described cylindrical shell (7) lower end is connected with cone (2), be arranged on the blended solid particle outlet (1) of described cone (2) below, be positioned at cone (2) bottom the loosening steam ring (12) in blended solid particle outlet (1) top, and the first solid particle inlet pipe (5) and the second solid particle inlet pipe (10) that are connected respectively to the inside of described cylindrical shell (7),

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

The barrel of described guide shell (6) is provided with the internal space that perforate (13), described perforate (13) are communicated with described annular space space and guide shell (6);

Described perforate is a plurality of long strip shapes holes, and the height of described perforate is less than or equal to 0.9 times of described guide shell (6) height, and the total area of described perforate is less than or equal to the lateral area of the guide shell (6) of 0.9 times; Or

Described perforate is a plurality of circular ports, and the radius of described perforate is less than or equal to 0.5 times of guide shell (6) height, and the total area of described perforate is less than or equal to the lateral area of the guide shell (6) of 0.9 times.

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

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

4. gas-solid loop flow mixing stripper as claimed any one in claims 1 to 3, is characterized in that,

Described the first solid particulate admission passage is the first solid particle inlet pipe (5), described the second solid particulate admission passage is the second solid particle inlet pipe (10), and the first solid particle inlet pipe (5) and the second solid particle inlet pipe (10) are connected to the both sides of described cylindrical shell (7) and are all communicated with described annular space space;

Or the first solid particle inlet pipe (5) is connected to the side direction of described cylindrical shell (7), the second solid particle inlet pipe (10) is connected to the top of described cylindrical shell (7);

Or the first solid particle inlet pipe (5) is connected to the top of described cylindrical shell (7), the second solid particle inlet pipe (10) is connected to the side direction of described cylindrical shell (7).

5. gas-solid loop flow mixing stripper as claimed in claim 4, it is characterized in that, described the first solid particle inlet pipe (5) and described the second solid particle inlet pipe take level or Way in to be obliquely connected on described cylindrical shell (7), the axis angle of the Way in of described the first solid particle inlet pipe (5) and described cylindrical shell (7) is 20 °～90 °, and the axis angle of the Way in of described the second solid particle inlet pipe (10) and described cylindrical shell (7) is 20 °～90 °; Or

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

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

7. the gas-solid loop flow mixing stripper as described in any one in claim 1 to 2, is characterized in that,

Mixing and the stripping process of described the first solid particulate and the second solid particulate complete by catalytic cracking reaction regeneration system rapidly, described catalytic cracking reaction regeneration system rapidly comprises: riser reactor, pre lift zone and revivifier, within described gas-solid loop flow mixing stripper is arranged on described revivifier, described cylindrical shell (7) is surrounded jointly by the inner side wall of revivifier and the arc of a side, the top of described cylindrical shell is uncovered, the inner chamber of described cylindrical shell is directly communicated with the inner chamber of described revivifier

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

8. the mixing of a solid particulate and gas stripping process, for fluid catalytic cracking process, mix the first solid particulate and the second solid particulate of differing temps, and strip flue gas and the air that the first solid particulate and the second solid particulate are carried secretly, the temperature of the second solid particulate is higher than the temperature of the first solid particulate, it is characterized in that

The mixing of described solid particulate adopts the gas-solid loop flow mixing stripper as described in any one in claim 1 to 2 with gas stripping process;

Mixing and the gas stripping process of described solid particulate comprise:

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

9. the mixing of solid particulate as claimed in claim 8 and gas stripping process, it is characterized in that, the first solid particulate is low temperature catalyst or low temperature spent agent, and the second solid particulate is high temperature catalyst, the temperature of the second solid particulate is higher than the temperature of the first solid particulate, and steps A comprises:

A1: what make described annular space gas distributor (3) is greater than the tolerance of giving of described guide shell gas distributor (11) to tolerance, the first solid particulate and the second solid particulate are flowed for making progress in described annular space, in described guide shell (6) for flowing downward, by the first solid particulate and the second solid particulate level or be transported to obliquely in described annular space space.

10. the mixing of solid particulate as claimed in claim 8 and gas stripping process, is characterized in that, the first solid particulate is low temperature catalyst or low temperature spent agent, and the second solid particulate is high temperature catalyst, and steps A comprises:

A2: what make described annular space gas distributor (3) is less than the tolerance of giving of described guide shell gas distributor (11) to tolerance, make the first solid particulate and the second solid particulate in described annular space space for flowing downward, in described guide shell (6) for upwards flowing, by the first solid particulate and the second solid particulate level or oblique under be transported in described annular space space.

The mixing of 11. solid particulates as claimed in claim 8 and gas stripping process, it is characterized in that, the first solid particulate is low temperature catalyst or low temperature spent agent, and the second solid particulate is high temperature catalyst, the temperature of the second solid particulate is higher than the temperature of the first solid particulate, and steps A comprises:

A3: what make described guide shell gas distributor (11) is greater than the tolerance of giving of described annular space gas distributor (3) to tolerance, make the first solid particulate and the second solid particulate in described annular space for flowing downward, in described guide shell (6), for making progress, flow, the first solid particulate is transported in described annular space space with level or direction obliquely, and the second solid particulate enters into described guide shell (6) downwards from the top of described guide shell (6).