CN1214857C - Circulating fluidized bed reactor for ultrafine and sticky particles - Google Patents
Circulating fluidized bed reactor for ultrafine and sticky particles Download PDFInfo
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- CN1214857C CN1214857C CN 02131273 CN02131273A CN1214857C CN 1214857 C CN1214857 C CN 1214857C CN 02131273 CN02131273 CN 02131273 CN 02131273 A CN02131273 A CN 02131273A CN 1214857 C CN1214857 C CN 1214857C
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Abstract
The present invention relates to a circulating fluidized bed reactor for ultra-fine and sticky particles. The present invention comprises a lifting pipe, an ultra-fine particle catching system and a material returning system, wherein the material returning system is provided with a V-shaped valve and a dipleg; the upper part of the lifting pipe is connected with the ultra-fine particle catching system; the lower part of the ultra-fine particle catching system is connected with the material returning system; the dipleg is connected with the lifting pipe by the V-shaped valve; a suspending inner component is placed in the lifting pipe; the tapered angle of the tapered dipleg is from 5 to 60 degrees; the V-shaped valve is a V-shaped pneumatic material transferring valve; the bottom of the tapered dipleg is provided with a fluidizing gas inlet and a gas distributing plate; the V-shaped pneumatic material transferring valve is provided with an auxiliary gas inlet of the V-shaped valve and an auxiliary gas distributing plate of the V-shaped valve; the reactor can normally fluidize ultra-fine and sticky particles; the phenomenon that the particles adhere to a wall in the lifting pipe is thoroughly eliminated; a crushing-agglomeration process of a fluidizing gather group is strengthened; the mixing among the particles is strengthened; the heat transfer and the mass transfer between the gather group and a main body and in the gather group are improved; the present invention has the advantages of easy amplification, simple operation, stable operation, energy conservation and no later-period material separation.
Description
Technical field
The invention belongs to gas-solid phase reactor, particularly a kind of circulating fluid bed reactor that is applicable to ultra-fine and sticky particle gas-solid phase reaction and particle processing.
Background technology
Fluidization ultra-fine and sticky particle has important effect in many industrial process, a most typical application is exactly a fluidized catalytic reaction, such as the chlorination of hydrocarbon, the ozone oxidation of ultra-fine carbon black etc.Fluidization ultra-fine and sticky particle also has important effect in many physics contact processes, such as heat transmission, solid mixing, drying, absorption and parsing, heat treatment, material modification (as starch conversion) etc.For the bigger particle of particle diameter,, be easy to realize comparatively desirable fluid effect such as the category-A particle.Yet when particle diameter hour, between the particle mutual adhesion will take place and coalesce together, thereby had a strong impact on the fluidizability of these materials.We claim that these particles that show the mutual sticking property of particle are sticky particle.Most ultra-fine grains such as calcium carbonate superfine powder, superfine titanium white etc. all belong to sticky particle, but non-ultra-fine sticky particle is also arranged.The adhesiveness intensity that different ultra-fine grains are showed also has very big difference, some ultra-fine grain has very strong adhesiveness, such as unmodified calcium carbonate superfine powder etc., and the other ultra-fine grain has relative good mobility simultaneously, such as superfine silicon carbide etc.
Yet, in general, because active force between the stronger particle that ultra-fine grain has, when carrying out the fluidization operation for it, be easy to generate channel, save improper fluidisation phenomenons such as gushing, gather group even dead bed, greatly reduce the gas-solid contacting efficiency, limited the application of ultra-fine grain fluid bed in industry.
According to the difference of fluidized bed process state, fluid bed can be divided into classical bubbling fluidized bed and recirculating fluidized bed.Classical bubbling fluidized bed is meant that the particle that is fluidized rests in the fluid bed main reactor, and recirculating fluidized bed is meant and is fluidized particle along with fluidizing gas is taken out of after the main reactor, in the middle of revert system is sent back to main reactor once more, move in circles, reach a kind of dynamic balance.
At present, for the research of the fluid mapper process of ultra-fine grain and use the classical bubbling fluidized beds that great majority concentrate on ultra-fine grain, and taked various measures to strengthen the fluid mapper process of ultra-fine grain.These measures roughly comprise:
1, external force field method
The external force field method refers to adopt oscillator field, sound field and magnetic field etc. to add the fluidization quality that the sticky particle fluid bed is improved in the field of force.Mori S (the Sino-Japan fluidization meeting in second boundary collection, 1988, P.75) point out that most of sticky particles can realize normal fluidization under the vibration of certain frequency.Chirone R, massimilla L, Russo S (Bubble-FreeFluidization of a cohesive powder in an acoustic field, Chemical Engineering Science, 1993,48 (1): 41～52) with sound field sticky particle has been realized being similar to the fluidisation of category-A material.The Zhu Qingshan of Chemical Industry ﹠ Metallrygy Research Office of CAS has studied externally-applied magnetic field for the influence that improves sticky particle fluidization quality at its Master's thesis in 1994 " improvement of C class goods fluid quality under the effect of magnetic field ".But there is the shortcoming of a maximum in these based on the method that adds the field of force is exactly that the industry that is difficult to the equipment of realizing is amplified.Such as adding oscillator field, make reactor be in vibrational state, no matter be that pipeline connects, or equipment life etc., problem was to be difficult to fundamentally overcome.Externally-applied magnetic field, the same existence amplified difficulty, unsuitable high-temperature operation, shortcoming such as power consumption is also very huge simultaneously.For the sound field fluidisation, this is merely able to be suitable for very small-scale application especially.
2, intrinsic method
Improve the fluidization quality of sticky particle by the character of adjusting particle itself.The researcher of Chinese patent ZL97111769.1, U.S. Pat 4591334, US4743431 and Japan Patent JP62106214 reduces adhesiveness between sticky particle by the component of adding other in sticky particle, improves the flowability of sticky particle.The disadvantage of these class methods is to add man-hour being used for solid phase, must increase complicated particle separation and purifying procedure.
3, bed structure method.
The bed structure rule is improved the fluidization quality of sticky particle by fluid bed being designed, adopts methods such as inner member, as Chinese patent CN1198962A, U.S. Pat 5067252.Venkatesh, R.D., J.Chaouki, etal. is in (1996). " Fluidization of cryogels in a conical column. " Powder Technology 89 (3): disclose a kind of NiO/Al that the conical bed fluidisation is used that is used among the 179-186
2O
3Aeroge.At present these class methods can play a role for the fluidization quality of improving the lower ultra-fine grain of adhesiveness, yet for the ultra-fine grain of high-adhesiveness, effect is unsatisfactory.
4, additive method
(a) high pressure fluid bed improves fluidization quality by the density that improves fluid; Rotating fluidized bed is used for overcoming adhesion in the particle by rotating produce overweight at a high speed, thereby improves fluidization quality.Yet these methods face the device structure that high pressure and rotation at a high speed bring and the difficulty of operating aspect.
(b) Yunyi Liu, Kiyoshi Sato, Tsutomu Tashimo and Kunio Kato, at " Proceeding ofthe Tenth Engineering Foundation Conference on Fluidization " (Beijing, China, May 20-25,2001, Kwauk, Jinghai Li and Wen-Ching Yang (eds.), pp.517-524) disclose Productionof ultrafine calcium carbonate powders by multiphase reaction in powder-particle spoutedbed, it is to produce calcium carbonate superfine powder with the spouted bed of fine powder one particle, is a kind of special application.
Along with people go deep into gradually to the understanding of ultra-fine and sticky particle fluid mapper process, begun recirculating fluidized bed research gradually to ultra-fine and sticky particle.Li Hongzhong Hongzhong Li, Legros, R., Breeton, C.M.H., et al discloses Hydrodynamic behavior of AerogelPowders in high-velocity fluidized beds in " Powder Technology " [(1990) 60:121], realized the recirculating fluidized bed operation to aeroge.The Hong Ruoyu of Chemical Industry ﹠ Metallrygy Research Office of CAS discloses " the fluidised research of superfine powder in interior circulation and the external circulation fluidized bed " in its thesis for the doctorate in 1996, this research has been carried out preliminary research to the circulating fluidization of sticky particle.
Compare with classical bubbling fluidized bed, recirculating fluidized bed has following advantage:
1, can realize continued operation, particularly can realize for the continuity operation of catalyst granules material reaction with regeneration.
2, the particle diameter of Shi Yonging is wider, from tens microns to several millimeters.And the poly-group of the particle of ultra-fine viscosity typically has a diameter from tens microns.
3, there is the fine powder entrainment problem in classical bubbling fluidization bed bioreactor.That is to say that always some fine powder can be entrained with reactor by gas.When improving gas velocity, carry secretly just even more seriously, cause the loss of material in particular for improving fluidization quality.U.S. Pat 6269778, US6214065 adopt circulation fluidized bed, greatly reduce the loss of fine granular materials.U.S. Pat 4793292, US4869207 adopt a vertical tube filter that the fine grained that comes out from the circulation fluidized bed riser is separated from gas, are transmitted back to riser then.U.S. Pat 4548797 has been mentioned and a kind of fine grained has been separated and be transmitted back to method in the fluid bed riser from the gas that the recirculating fluidized bed riser comes out, fundamentally overcome the problem that material is carried secretly, therefore have operating gas speed more widely, the engineering that helps reactor is amplified.But these designs noted earlier, use ultra-fine and sticky particle when being operated granule materials, can not avoid the phenomenon such as sticking wall, obstruction, bridge formation of sticky particle, sticky particle can not flow freely in send-back system, and obviously the method that these patents provided is inapplicable for the high particle of adhesiveness.
4, the interior gas velocity height of riser in the recirculating fluidized bed, generally greater than the sinking speed of particle (or poly-group), speed difference is big between gas-solid, and the poly-group of formed fluidization is easy to be broken.Poly-group in the high-speed motion collides each other and between the wall mutually, the broken and reunion again of easy generation, and the surface of solids often obtains renewal etc.
5, mix fiercely between particle, the poly-group of fluidization is broken easily, so the poly-group of fluidization and the main body mass transfer between mutually and heat transfer are well; Poly-group is good with main body mass transfer mutually and heat transfer, helps inner heat transfer and the diabatic process of poly-group, the inside of fluidizing reactor, and concentration gradient and thermograde are all less.
6, the gas velocity height in the recirculating fluidized bed riser is operated in the fast bed state.Fast bed is the state of operating under the gas velocity between common bubbling fluidized bed and the strength conveying, does not have the bubble in the bubbling fluidized bed, does not have channel, and gas does not leave fluid bed with the short circuit form.During fluidisation, viscosity is strong between particle, channel often occurs in the bubbling bed for ultra-fine grain, and dead bed or joint gush, and in fast bed, these phenomenons no longer occur.
7, the particle disposal ability on the unit cross-sectional area is big, is applicable to large-scale production.
9, the gas velocity adjustable range is wide, and operating flexibility is big, is easy to implementation procedure and amplifies and the application of different processes.
The loopback of material system of recirculating fluidized bed is an important component part in the circulating fluidized bed system.Its effect be loopback of material that the material trapping system by recirculating fluidized bed is captured to the riser bottom, keep the continuity of recirculating fluidized bed work.Simultaneously, the loopback of material system of recirculating fluidized bed also must provide the ability of enough confining gas, makes fluidizing gas in the riser not return string and enters in the dipleg, guarantees the steady operation of circulating fluidized bed system.
Distinguish from the angle of the driving force of carrying particle, the loopback of material system of recirculating fluidized bed can be divided into mechanical send-back system and pneumatic send-back system.As a rule, pneumatic send-back system operation is more reliable and stable, simple in structure, and sealing property is better, is more suitable for engineering and uses.
Existing pneumatic send-back system, its primary structure form comprise have V-shaped valve, L type valve and the isostructural returning charge dipleg of J type valve.Other have described a kind of method that is built in material envelope in the recirculating fluidized bed as U.S. Pat 5242662, and U.S. Pat 4955295 has been described the material return system material sealing property method of another kind of raising circulation fluidized bed.The dipleg of L type valve, J type valve arrangement all can not satisfy the needs of sticky particle loopback, forms easily to stop up, build bridge.Promotion gas in the valve can not effectively promote movement of particles, passes through with the short circuit form usually, and consequently particle flow difficulties in valve is unsuitable for the loopback of sticky particle material.
Classical fluidization dipleg with V-shaped valve structure, can be used for the conveying of the less ultra-fine grain of adhesiveness, but for the strong ultra-fine grain of adhesiveness, as unmodified calcium carbonate superfine powder, then there are two problems: 1. in valve body, form and stop up, cause V-shaped valve to lose the ability of convey materials; 2.V the granule materials in the dipleg part that the type valve requires to link with it is in a kind of initial fluidized state, so that successfully mass transport is entered the valve body of V-shaped valve.But for sticky particle, particularly for the stronger particle of adhesiveness, the poly-group that occurs in its fluid mapper process, channel, phenomenons such as bridge formation make and to keep the fluidized state of sticky particle in the dipleg difficulty that becomes, and consequently cause the work that V-shaped valve can not be stable.
Summary of the invention
The object of the invention is to solve above-mentioned prior art problems, and provide a kind of circulating fluid bed reactor that is applicable to ultra-fine and sticky particle, this reactor makes ultra-fine and the normal fluidisation of sticky particle, thoroughly eliminate the attached wall phenomenon of sticky particle in riser, can strengthen the fragmentation-aggregation procedure of the poly-group of fluidisation, mixing between reinforcing particle improves processes such as the inner heat transfer of processes such as gathering group's heat transfer alternate with main body, mass transfer and poly-group, mass transfer; And be easy to that implementation procedure is used and amplify, operation control is simple, stable operation, and conserve energy need not the gas-solid phase fluidized-bed reactor of later stage feed separation.Can access ultra-fine sticky particle stream stable, that can control by this reactor.
Technical scheme of the present invention is as follows:
The circulating fluid bed reactor that is applicable to ultra-fine and sticky particle provided by the invention, comprise riser 2, ultra-fine grain trapping system 11 and material return system, this material return system is the dipleg with V-shaped valve, the top of riser 2 links to each other with ultra-fine grain trapping system 11, the bottom of ultra-fine grain trapping system 11 links to each other with material return system, and the dipleg of material return system links to each other with riser 2 by V-shaped valve; It is characterized in that in riser 2, being placed with the inner member 3 that swims; Described dipleg bottom is taper, and the charging aperture of V-shaped valve is positioned at conical section; Described V-shaped valve is the pneumatic feeding valve 4 of V-type; The described inner member 3 that swims is for having sphere or almost spherical granular substance or irregularly shaped, and its diameter or equivalent diameter are 50～3000 microns, and density or apparent density are 500～3000kg/m
3The angle of taper of described dipleg 1 bottom is 5～60 °; Described dipleg bottom is provided with dipleg fluidizing gas import 6 and dipleg gas distribution grid 8; The pneumatic feeding valve of described V-type has V-shaped valve auxilairy air intake and V-shaped valve assist gas distribution grid 10.
Description of drawings
Fig. 1 is a structural representation of the present invention;
Fig. 2 a is the side view of taper material return system of the present invention;
Fig. 2 b is the front view of taper material return system of the present invention;
Wherein: dipleg 1 riser 2 inner member 3 that swims
V-shaped valve 4 riser fluidizing gas imports 5 dipleg fluidizing gas imports 6
Riser gas distribution grid 7 dipleg gas distribution grids 8
V-shaped valve auxilairy air intake 9
V-shaped valve assist gas distribution grid 10 ultra-fine grain trapping systems 11
Stream of fine particles 12 riser fluidizing gas 13
Conical dipleg fluidizing gas 14 V-shaped valve assist gas 15
Discharge currents oxidizing gases 16 V-shaped valve charging apertures 41
V-shaped valve discharge gate 42 V-shaped valve drainage conduit 43
Concrete embodiment
The present invention also will be described in further detail embodiment in conjunction with the accompanying drawings:
Operation principle of the present invention is as follows:
1, the realization and the effect of the inner member that swims in the riser of the present invention
According to the character of ultra-fine sticky particle, choose the inner member 3 that swims of suitable density and diameter.Under the effect of fluidizing gas, the inner member 3 that swims forms classical fluidized state or turbulence fluidized state in recirculating fluidized bed riser 2, and cohesive particle then forms the fast fluidized bed state.
If U
Min, U
MaxThe minimum that is respectively ultra-fine grain in the recirculating fluidized bed riser 2 is taken the dilute phase transporting velocity of gas superficial velocity and ultra-fine grain out of; U
Mb, f, U
T, fBe respectively the minimum fluidization velocity and the terminal velocity of the inner member that swims; The so selected inner member 3 that swims should have such character: U
Mb, f＜U
Min, U
Max＜U
T, fThe U of inner member swims
Mb, f, U
T, fCalculating with reference to general A or category-B particle u
Mb, u
tComputational methods.
In normal operating conditions, the inner member 3 that swims is not fluidized the riser 2 that gas is taken recirculating fluidized bed out of.That is to say that the inner member 3 that swims does not enter the particle circulation of recirculating fluidized bed.
Because the inner member 3 that swims is in classical fluidisation or turbulence fluidized state, swim between the inner member 3, the inner member 3 that swims roll into a ball with ultra-fine sticky particle fluidisation is poly-between and swim and be in a kind of collision status of fierceness between inner member 3 and the fluid bed wall.The collision of this fierceness, mainly contain following effect: 1. can prevent that the high viscosity ultra-fine grain from forming the poly-group of the fluidisation of too growing up in fluid mapper process, and too growing up of this poly-group can form dead bed zone usually in riser 2, causes the abnormal operation of fluid bed; 2. this collision effect can also prevent that cohesive particle from forming adhesion layer on riser 2 inwalls, almost can thoroughly eliminate the attached wall phenomenon of sticky particle in main reactor riser 2; 3. can strengthen the fragmentation-aggregation procedure of the poly-group of fluidisation, the mixing between reinforcing particle improves processes such as the inner heat transfer of processes such as gathering group's heat transfer alternate with main body, mass transfer and poly-group, mass transfer; 4. swim collision between the inner member 3, inner member 3 surfaces that can guarantee to swim do not adhere to fine grained.
2, taper material return system
The taper material return system comprises two parts: conical dipleg 1 and V-type aerodynamic particle feeding valve 4.Granule materials in the conical dipleg 1 is controlledly carried back riser 2 by V-type feeding valve 4; The fluidizing gas of V-shaped valve in can also shutoff riser 2 simultaneously prevents that fluidizing gas in the riser 2 from returning string and entering dipleg 1.
In order particle transport to be entered V-shaped valve 4, must guarantee that the material in the dipleg 1 is in a kind of free-flowing.The sticky particle that is kept in motion just might be transported into V-shaped valve 4.
Can form the bigger poly-group of diameter in the fluid mapper process of ultra-fine sticky particle under some lower fluidization gas velocity, and sink, form dead bed zone to the bed bottom.Along with the carrying out of fluid mapper process, dead bed zone can constantly enlarge, and finally causes whole bed that dead bed takes place.
Improve the fluidizing velocity of ultra-fine sticky particle, the collision aggravation between the particle agglomeration, the average-size of the poly-group of the fluidisation that can reduce to form in the fluid mapper process, and prolong the time that dead bed appears in fluidized-bed layer.Fluidization gas velocity is thus lifted to when enough high, even can avoid the generation of dead bed phenomenon.
But along with the raising of fluidization gas velocity, ultra-fine grain also increases with the rate of taking out of of fluidizing gas, causes the loss of material in the dipleg 1.Simultaneously, adopt too high gas velocity in the dipleg 1, bring negative effect can for the operate as normal of the material trapping system 11 of recirculating fluidized bed.Such as, reduce the separative efficiency of gas-solid separator, even destroy the operate as normal of gas-solid separator fully.Therefore, recirculating fluidized bed requires to operate under lower dipleg 1 superficial gas velocity usually, realizes ultra-fine sticky particle flowing freely in dipleg 1 simultaneously.Yet this realizes the where the shoe pinches of ultra-fine sticky particle circulating fluidization just.
Different with the straight pipe type dipleg is that conical dipleg 1 can provide different superficial velocities in the axial direction: conical dipleg 1 is G at the unit mass flow
gThe air inlet state under, the superficial gas velocity on a certain cross section is: u=G
g/ (ρ
gπ h
2Tan
2(θ/2)), ρ wherein
gBe gas density, h is the height of this cross section to how much summits of taper, and θ is the drift angle of conical dipleg 1.The superficial velocity of fluidizing gas with cross section geometric height h square inverse change.Along with the reduction of geometric height h, apparent fluidization gas velocity u increases sharply, and along with the increase of h, apparent fluidization gas velocity u then reduces rapidly.
The bottom of conical dipleg falls to entering in the poly-group of the larger-diameter fluidisation that the viscosity ultra-fine grain forms in fluid mapper process, runs into higher fluidization gas velocity, and this higher fluidization gas velocity enough keeps these larger-diameter poly-groups to be in fluidized state.And, because the more violent poly-group collision that higher fluidization gas velocity causes makes the fragmentation of the poly-group of large diameter fluidisation reduce to become the poly-group of the less fluidisation of diameter.These poly-groups of fluidisation than minor diameter are fluidized the top that gas is sent into conical dipleg again, and simultaneously, new big poly-group sinks again and enters the bottom of conical dipleg.So just guaranteed that conical dipleg can not cause dead bed because forming the poly-group of big fluidisation, thereby in dipleg, formed stable fluidized state.
Square being inversely proportional to of the geometric height h in superficial gas velocity and conical bed cross section in the conical bed, so along with reduce (decline in cross section) of h, gas superficial velocity increases sharply.When less dipleg air inflow, just can satisfy broken big poly-group like this, keep the requirement of dipleg stabilization fluid.
Along with the increase gas superficial velocity of conical dipleg geometric height reduces rapidly, can not form serious entrained particle at the top of conical dipleg bed and carry secretly.
For the big particle of adhesiveness, reduce the θ angle, help the descending of particle.According to different particle properties, the θ angle of fluid bed design is between 5～60 °.
Classical V-type feeding valve can not be carried the particle of high-adhesiveness, in addition assist gas.Particle in the conical dipleg 1 enters in the V-shaped valve 4 via the connector 41 between V-shaped valve 4 and the dipleg 1, and forms accumulation in valve.Classical V-shaped valve, by means of the gas that from dipleg, enters in the V-shaped valve, can be stacked into to a certain degree, flowability preferably material send into riser.But for sticky particle, needed motive force is much bigger, therefore must apply additional-air inlet to V-shaped valve.By means of assist gas 15, V-shaped valve 4 will be stacked into a certain amount of sticky particle and send into riser 2, then form material envelope interval, prevent that gas in the riser 2 from returning string and entering dipleg 1.
Embodiment
A kind of circulating fluid bed reactor that is applicable to ultra-fine and sticky particle, comprise riser 2, ultra-fine grain trapping system 11 and material return system, this material return system has the dipleg with V-shaped valve, the top of riser 2 links to each other with ultra-fine grain trapping system 11, the bottom of ultra-fine grain trapping system 11 links to each other with material return system, and the dipleg of material return system links to each other with riser 2 by V-shaped valve drainage conduit 42; In riser 2, be placed with the inner member 3 that swims; Establish riser fluidizing gas import 5 and riser gas distribution grid 7 in riser 2 bottoms; Described granular substance or the erose granular substance of inner member 3 that swim for having sphere or almost spherical, its diameter or equivalent diameter are 50～3000 microns, density or apparent density are 500～3000kg/m
3, its surface is smooth or coarse.The angle of taper of described conical dipleg 1 is 5～60 °.
Described dipleg is a conical dipleg; Described V-shaped valve is the pneumatic feeding valve of V-type.
Described conical dipleg 1 bottom is provided with conical dipleg fluidizing gas import 6 and conical dipleg gas distribution grid 8.
The pneumatic feeding valve of described V-type has V-shaped valve assist gas 15 and V-shaped valve assist gas distribution grid 10.
The speed of the riser fluidizing gas 13 in the described riser 2 is greater than the speed of conical dipleg fluidizing gas 14.
Above-mentioned recirculation reactor is carried out following test: adopt the unmodified calcium carbonate of primary particle diameter 0.1 μ m to carry out the fluidisation experiment.This material has very strong adhesiveness, is typical adhesiveness ultra-fine grain.Fluid bed riser 2 internal diameter 0.075m, high 3.2m; Material trapping system 11 adopts secondary cyclone, and the fine grained that trapping system 11 is captured is sent back to dipleg 1 again; Final gas discharges after by sack cleaner; Dipleg straight-tube portion internal diameter 0.08m, the tapering of tapering part is 5 °, geometric height 0.8m; Diameter 0.0012m is housed, density 2100kg/m in the riser
3The inner member 0.5～2.0kg that swims.Riser operation superficial gas velocity 1.8～4.5m/s, conical dipleg advance 25 ℃ of air 2.78～11.1 * 10
-4m
3/ s, V-shaped valve assist into 25 ℃ of air 1.39～6.94 * 10
-4m
3/ s.Realized that calcium carbonate solid particle cycling rate is 5～25kg/ (m
2S) stable circulation fluidization operation.
Claims (5)
1, a kind of circulating fluid bed reactor that is applicable to ultra-fine and sticky particle, comprise riser, ultra-fine grain trapping system and material return system, this material return system is the dipleg with V-shaped valve, the top of riser links to each other with the ultra-fine grain trapping system, the bottom of ultra-fine grain trapping system links to each other with material return system, and the dipleg of material return system links to each other with riser by V-shaped valve; It is characterized in that, in riser, be placed with the inner member that swims; Described dipleg bottom is taper, and the charging aperture of V-shaped valve is positioned at conical section; Described V-shaped valve is the pneumatic feeding valve of V-type.
2, the circulating fluid bed reactor that is applicable to ultra-fine and sticky particle as claimed in claim 1, it is characterized in that the described inner member that swims is for having sphere or almost spherical granular substance or irregularly shaped, its diameter or equivalent diameter are 50～3000 microns, and density or apparent density are 500～3000kg/m
3
3, the circulating fluid bed reactor that is applicable to ultra-fine and sticky particle as claimed in claim 1, the angle of taper that it is characterized in that described dipleg bottom is 5～60 °.
4, the circulating fluid bed reactor that is applicable to ultra-fine and sticky particle as claimed in claim 1 is characterized in that described dipleg bottom is provided with import of dipleg fluidizing gas and dipleg gas distribution grid.
5, the circulating fluid bed reactor that is applicable to ultra-fine and sticky particle as claimed in claim 1 is characterized in that the pneumatic feeding valve of described V-type has V-shaped valve auxilairy air intake and V-shaped valve assist gas distribution grid.
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| CN105598035B (en) * | 2016-01-08 | 2018-09-07 | 浙江大学 | A kind of parallel connection fluid bed dry separation device and method |
| CN112588213B (en) * | 2020-11-24 | 2022-05-31 | 中国五环工程有限公司 | Fast bed reaction method for ultrafine particles and fast reaction bed |
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