CN107008211A - A kind of fluidized-bed reactor with Independent adjustable inner-outer circulation flow rate - Google Patents
A kind of fluidized-bed reactor with Independent adjustable inner-outer circulation flow rate Download PDFInfo
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- CN107008211A CN107008211A CN201710253312.7A CN201710253312A CN107008211A CN 107008211 A CN107008211 A CN 107008211A CN 201710253312 A CN201710253312 A CN 201710253312A CN 107008211 A CN107008211 A CN 107008211A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1872—Details of the fluidised bed reactor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00548—Flow
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Abstract
The present invention relates to a kind of fluidized-bed reactor with Independent adjustable inner-outer circulation flow rate.The reaction unit includes air compartment (1), air distribution plate (2), fluidized-bed reactor body (3), riser (4), changeover portion (5), transport bed (6), cyclone separator (7), standpipe (8), returning charge valve A (9), returning charge valve B (10), compared with traditional gas-solid fluidization reaction unit, apparatus of the present invention organically combine gas-solid loop flow reactor with lifting the advantage of tubular type recirculating fluidized bed, so as to take into account the inner-outer circulation flow rate of solid material, extend gas-solid contact time, enhance gas-solid contact efficiency, and it is effectively utilized reactor dilute-phase zone space.The reaction unit can be independently controlled and adjust to the interior circulation flow rate and outer circulation flow rate of solid material, and reactor dilute-phase zone space is made full use of.
Description
Technical field
The present invention is a kind of fluidized bed reaction for being applied to the fields such as the energy, chemical industry, and the reaction unit can be to solid
The interior circulation flow rate and outer circulation flow rate of material enter accommodating, independent control and regulation, and fluid bedreactors dilute-phase zone
Space is made full use of.
Background technology
Gas-solid fluidization technology be born from before over half a century since in modern energy, chemical industry, oil, light industry, smelting
The every field such as gold, material and environmental protection has played huge effect, the characteristics of to adapt to various processes in every field, gas
Gas-solids reactors form also develops and perfect continuous.
Bubbling fluidized bed reactor is a kind of classical gas-solid dense-phase fluidized bed reactor being widely applied industrially,
There is its strong agitation caused by bubbly flow so that gas-solid contact efficiency is higher, dense-phase bed good heat transfer to pass
Matter performance, and bed internal temperature is uniform.But the also exactly presence of these bubbles so that portion gas reactant is with bubble
Form reduces the touch opportunity between vapor solid, reduces reaction conversion ratio by bed.
Circulation flow reactor is developed on the basis of bubbling fluidized bed reactor.The circulation flow reactor of an earliest class
It is a kind of solution-air, gas-solid-liquid or liquid-solid heterophase reactor, is widely used in petrochemical industry, biology, metallurgy and environment
The association areas such as chemical industry.Circulation flow reactor combines the advantage of bubble tower and mechanical stirring kettle, with gas holdup height, mass transfer rate
Hurry up, gas-liquid mixed is good, it is simple in construction the features such as.Researchers have used for reference the circulation principle of circulation flow reactor, are extended to gas
Gu fluidization field, it is proposed that the gas-solid loop flow reactor for gas-solid two-phase system.The structure of gas-solid loop flow reactor with it is upper
State circulation flow reactor similar, common feature is all to be arranged concentrically guide shell in Conventional fluidization bed inside reactor, and gas-solid loop flow is anti-
Answer device due to the presence of internal guide cylinder, the combination of controllable laminar flow and limited complete mixing flow is realized, with efficient
Gas-solid contact efficiency, orderly particle flow, controllable particle residence time, outstanding heat transfer, mass-transfer performance and structure letter
Single many advantages, such as.
Although the inner circulation reactor of gas-solid loop flow type improves gas-solid contact efficiency and Heat and Mass Transfer Characteristics, with compared with
Long solid retention time, but be difficult to the outer circulation of solid material, therefore need to realize for some and followed outside solid material
Ring is (such as by the catalyst regeneration of inactivation, CO2Trap technique etc.) technology for, it is clear that be inapplicable, Er Qiechang
The space of its dilute-phase zone of the inner circulation reactor of gas-solid loop flow type of rule also fails to make full use of.Industrially realize solid material
Using the circulating fluid bed reactor that operating gas velocity is higher more than outer circulation.Relative to the inner circulation reactor of gas-solid loop flow type,
Circulating fluid bed reactor can realize the effective control and regulation of material outside circulation flow rate, but due to circulating fluid bed reactor
It is generally in fast fluidization or Dense Phase Pneumatic Conveying fluidised form, its higher operating gas velocity and larger solid material circulation flow-rate
So that the residence time of gas and solid is all very short, therefore it is unfavorable for the depth of gas-solid reaction and carries out, solid and gas material
It is not high using conversion ratio.Meanwhile, when designing such reactor, for the gas-solid contact time needed for ensureing reaction, reactor leads to
Often be designed to it is higher, cause space reactor arrangement it is not compact enough；In addition, higher height for reactor also further increases fortune
Fan energy consumption in row, reduces the economy of operation.It is to continue to improve fluidising air velocity on the basis of recirculating fluidized bed to transport bed
Formed by a kind of new fluidizing reactor, its flow pattern features is that circulation flow-rate is big, riser inner section solid net flux
All upwards, and between solid particle and between gas-particle two-phase there is strong momentum and energy exchange, thus with traditional circulation
Fluidized-bed reactor is compared, and transports that gas-solid contact in the bed of bed technique is good, heat transfer/mass transfer rate fast, gas-solid back-mixing is small.But by
The operation wind speed needed in the reactor of the form is higher, therefore there is also such as traditional Circulating Fluidized Bed residence time
The shortcomings of short, reactor whole height is high, fan energy consumption is big.
In summary, the inner circulation reactor of conventional gas-solid loop flow type, circulating fluid bed reactor and new defeated
Fortune bed all haves the shortcomings that certain, and the interior circulation and outer circulation flow rate of solid material are difficult to take into account, and due to gas-solid loop flow
The inner circulation reactor operating gas velocity of type is low, and bed entrainment is small, causes dilute-phase zone material particles concentration low so that dilute-phase zone
Space can not be fully utilized.Therefore, the inner circulation reactor of conventional gas-solid loop flow type and lifting tubular circulation
Fluid bed can not meet demand of some technologies to controllable solid material interior circulation flow rate and outer circulation flow rate, and
The inner circulation reactor reactor dilute-phase zone space of conventional gas-solid loop flow type also fails to be fully utilized, and reduces life
The economy of production. art.But do not see at present correlation can inner loop flow rate and outer circulation flow rate be independently controlled and
Regulation, and the report for the type of reactor that reactor dilute-phase zone space can be made full use of.
The content of the invention
Technical problem：A technical problem to be solved by this invention is to provide a kind of with Independent adjustable inner-outer circulation stream
The fluidized-bed reactor of rate, the reaction unit interior circulation flow rate and outer circulation flow rate of solid material can be independently controlled and
Regulation, and reactor dilute-phase zone space is made full use of.
Technical scheme：The present invention is a kind of fluidized-bed reactor with Independent adjustable inner-outer circulation flow rate, reaction dress
Put including air compartment, air distribution plate, fluidized-bed reactor body, riser, changeover portion, transport bed, cyclone separator, standpipe, returning charge
Valve A, returning charge valve B；
The intrinsic top of fluidized-bed reactor is dilute-phase zone, and bottom is emulsion zone, and the bottom of emulsion zone is air distribution plate, cloth
The bottom of aerofoil is air compartment, and the top of fluidized-bed reactor body is connected by changeover portion with transporting bed, transport bed top and
The upper entrance connection of cyclone separator, the bottom material outlet of cyclone separator is entered by standpipe with returning charge valve A and returning charge valve B
Mouth connection, returning charge valve A outlet is connected with fluidized-bed reactor body dilute-phase zone stage casing, and returning charge valve B outlet and fluid bed are anti-
Device body emulsion zone is answered to connect；Many risers run through air compartment and air distribution plate, and lifting tube inlet is located on the outside of air compartment, and riser goes out
Mouth is located at the dilute-phase zone in fluidized-bed reactor body.
The fluidized-bed reactor also includes CO2Desorption reaction device, refeed line A, refeed line B；Described standpipe bottom connection
One CO2Desorption reaction device, the CO2Desorption reaction device meets returning charge valve A, equally, the CO by refeed line A2Desorption reaction device passes through
Refeed line B meets returning charge valve B；Returning charge valve A outlet is connected with fluidized-bed reactor body dilute-phase zone stage casing, returning charge valve B outlet
Connected with fluidized-bed reactor body emulsion zone.
Described riser arranges two or more than two according to actual needs, and high with low riser using high riser
The arrangement of low collocation, the outlet of high riser is located at fluidized-bed reactor body dilute-phase zone at changeover portion, low lifting
The outlet of pipe is located at fluidized-bed reactor body dilute-phase zone bottom, and the outlet caliber of riser can be appropriate expanding as needed, makes
Riser entrained with material can even dispersion in dilute-phase zone.
Described lifting tube wall is being furnished with multiple charging apertures at air distribution plate.
The speed of lifting wind is higher than the superficial gas velocity of fluidized-bed reactor body emulsion zone in riser.
Described fluidized-bed reactor body, changeover portion, bed is transported for overall structure.
Described fluidized-bed reactor body, changeover portion, transport bed and be coaxially set.
A kind of operation principle of above-mentioned fluidized-bed reactor with Independent adjustable inner-outer circulation flow rate is：The plant running
When, the wind speed of height riser is passed through by control and the wind speed of fluidized wind in fluidized-bed reactor body is passed through so that lifting
The wind speed of wind is higher than the wind speed of fluidized wind, so that outside forms differential pressure in riser aperture so that fluidized reactor emulsion zone
Material under the promotion of differential pressure, boosted pipe aperture enter riser in, then lifting wind entrainment under upwards motion carry
Rise to fluidized-bed reactor body dilute-phase zone.Relatively low leg outlet is located at fluidized-bed reactor body dilute-phase zone bottom, lifting
The particle that wind is carried is decelerated during dilute-phase zone is entered, and is then moved downward under gravity, forms material
Interior circulation, and then the material particles concentration substantial increase of fluidized-bed reactor body dilute-phase zone；Higher leg outlet is located at stream
Fluidized bed reactor body dilute-phase zone top is close to changeover portion part, and the partial particulate that lifting wind is carried may proceed to upward motion, warp
The accelerating into of changeover portion transports bed and is transported wind conveying to form the outer circulation of material.Therefore can be by changing fluid bed
Conveying of the wind speed of wind speed and height riser the lifting wind of the fluidized wind of reactor body to height riser solid material
Amount is adjusted, so as to effectively control the interior circulation and outer circulation amount of solid material.The returning charge of the fluidized-bed reactor passes through
Returning charge valve A and returning charge valve B realizes that wherein returning charge valve A outlet is located at fluidized-bed reactor body dilute-phase zone stage casing, can be further
Increase dilute-phase zone granule density, strengthen gas-solid contact.
The course of work of the above-mentioned fluidized-bed reactor with Independent adjustable inner-outer circulation flow rate is：The stream come out from air compartment
Wind transmission enters fluidized-bed reactor body through air distribution plate, and the solid material in fluidized-bed reactor body is fluidized, and makes at it
The lifting wind compared with high gas velocity is passed through in bubbling state or the state of turbulent fluidization, riser so that riser lifts the wind of wind
Speed is higher than the superficial gas velocity in fluidized-bed reactor body, so forms differential pressure, fluidized reaction in the interior outside of riser aperture
The material of device emulsion zone under the promotion of differential pressure, boosted pipe aperture enter riser in, then lifting wind entrainment under to
Upper motion, relatively low leg outlet is located at fluidized-bed reactor body dilute-phase zone bottom, and the particle that lifting wind is carried is primarily formed
The interior circulation of material, and then the material particles concentration substantial increase of fluidized-bed reactor body dilute-phase zone bottom；Higher riser
Outlet is located at fluidized-bed reactor body dilute-phase zone close to changeover portion part, and the partial particulate that lifting wind is carried may proceed to upward fortune
Dynamic accelerating into through changeover portion transports bed, transports bed and is in Geldart-D particle or fast fluidization, is taken out of by air-flow and transport bed
Material, most granule materials therein are trapped by cyclone separator, are returned respectively via standpipe and returning charge valve A and returning charge valve B
Fluidized-bed reactor body dilute-phase zone stage casing and fluidized-bed reactor body emulsion zone are delivered to, is not trapped on a small quantity by cyclone separator
Fine particle discharged through Cyclone outlet.
Beneficial effect：Compared with prior art, the invention has the advantages that：
1. interior circulation flow rate and outer circulation flow rate with Independent adjustable, by controllable interior circulation flow rate, enhance gas
It is affixed to touch, and take full advantage of reactor dilute-phase zone space.Compared with traditional gas-solid fluidization reaction unit, apparatus of the present invention
Gas-solid loop flow reactor is organically combined with lifting the advantage of tubular type recirculating fluidized bed, so as to take into account solid material
Inner-outer circulation flow rate, extends gas-solid contact time, enhances gas-solid contact efficiency, and it is empty to be effectively utilized reactor dilute-phase zone
Between.In apparatus of the present invention, riser runs through air compartment and air distribution plate, and it, which is exported, is located at fluidized-bed reactor body dilute-phase zone, entrance
On the outside of air compartment, lifting tube wall is furnished with multiple charging apertures at higher than air distribution plate height, and outlet is located at fluidized-bed reaction
Lifting wind is passed through in device body dilute-phase zone, riser, the wind speed of riser lifting wind is higher than the table in fluidized-bed reactor body
Gas velocity is seen, the interior outside of riser aperture forms differential pressure, and the material of fluidized reactor emulsion zone is boosted under the promotion of differential pressure
Pipe aperture enters in riser, is then moved upwards under the entrainment of lifting wind, and relatively low leg outlet is located at fluidized-bed reaction
Device body dilute-phase zone bottom, the particle that lifting wind is carried is decelerated during dilute-phase zone is entered, then in the effect of gravity
Under move downward, formed material interior circulation, and then fluidized-bed reactor body dilute-phase zone material particles concentration substantial increase；
Higher leg outlet is located at the part that fluidized-bed reactor body dilute-phase zone top is carried close to changeover portion part, lifting wind
Grain may proceed to motion upwards, and accelerating into through changeover portion transports bed and be transported wind conveying to form the outer circulation of material.Cause
Wind air quantity is lifted in this riser by controlling different height, particle inner-outer circulation flow rate can be carried out flexibly and effectively respectively
Control.
2. it is simple in construction, compact.The present invention is changeover portion, defeated by air compartment, air distribution plate, fluidized-bed reactor body, riser
Transport bed, cyclone separator, standpipe, returning charge valve A, returning charge valve B.Simple in construction, whole height is low, and space layout is compact, effectively profit
With the dilute-phase zone space of fluidized-bed reactor body, up-front investment is small.
Brief description of the drawings
Fig. 1 is structural representation of the invention；
Fig. 2 is the structural representation of another embodiment of the invention；
Have in figure：Air compartment 1, air distribution plate 2, fluidized-bed reactor body 3, riser 4, changeover portion 5, transport bed 6, whirlwind point
From device 7, standpipe 8, returning charge valve A9, returning charge valve B10, CO2Desorption reaction device 11, refeed line A12, refeed line B13.
Embodiment
Below in conjunction with the accompanying drawings, detailed technology is carried out to the present invention program to illustrate, but protection scope of the present invention is not
It is confined to embodiment.
As shown in figure 1, should with Independent adjustable inner-outer circulation flow rate fluidized-bed reactor include air compartment 1, air distribution plate 2,
Fluidized-bed reactor body 3, riser 4, changeover portion 5, transport bed 6, cyclone separator 7, standpipe 8, returning charge valve A9, returning charge valve
B10。
Fluidized-bed reactor body 3 is made up of emulsion zone and dilute-phase zone, and its bottom is connected with air distribution plate 2, air distribution plate 2 and wind
The top connection of room 1, the top of fluidized-bed reactor body 3 is connected by changeover portion 5 with transporting bed 6, transport bed 6 top and
The entrance connection of cyclone separator 7, the material outlet of cyclone separator 7 passes through standpipe 8 and returning charge valve A9 and returning charge valve B10 entrances
Connection, returning charge valve A9 outlet is connected with the dilute-phase zone of fluidized-bed reactor body 3, returning charge valve B10 outlet and fluidized-bed reaction
The emulsion zone of device body 3 is connected；Air distribution plate 2 is connected between fluidized-bed reactor body 3 and air compartment 1；Fluidized-bed reactor body 3
The mode of operation of bubbling bed or turbulent bed can be used, riser 4 can use the mode of operation of Geldart-D particle, and transporting bed 6 can
Using the mode of operation of Geldart-D particle or fast bed, the wall of air compartment 1 is provided with fluidized wind entrance, and fluidized wind passes through fluidized wind
Entrance is passed through in air compartment 1, then enters fluidized-bed reactor body 3 by air distribution plate 2 again；Many risers 4 run through the He of air compartment 1
Air distribution plate 2, and using high level matches with low level arrangement, riser 4 is fixedly connected on the wall of air compartment 1 and air distribution plate 2, and junction is close
Envelope.The entrance of riser 4 is located at the outside of air compartment 1, and higher leg outlet is located at the dilute-phase zone of fluidized-bed reactor body 3 close to transition
Section 5, the relatively low outlet of riser 4 is located in the dilute-phase zone of fluidized-bed reactor body 3, and riser 4 is passed through lifting wind.
The fluidized-bed reactor also includes CO2Desorption reaction device 11, refeed line A12, refeed line B13；Under described standpipe 8
Portion connects a CO2Desorption reaction device 11, the CO2Desorption reaction device 11 meets returning charge valve A9, equally, the CO by refeed line A122
Desorption reaction device 11 meets returning charge valve B10 by refeed line B13；Returning charge valve A9 outlet and the dilute-phase zone of fluidized-bed reactor body 3
Stage casing is connected, and returning charge valve B10 outlet is connected with the emulsion zone of fluidized-bed reactor body 3.
A kind of described fluidized-bed reactor riser 4 with Independent adjustable inner-outer circulation flow rate is according to actual conditions cloth
Put two or some, and using the arrangement of high level matches with low level, the tube wall of riser 4 be furnished with air distribution plate 2 it is multiple enter
Expect aperture, the outlet of higher riser 4 is located at the dilute-phase zone of fluidized-bed reactor body 3 at changeover portion 5, relatively low riser 4
Outlet be located at the dilute-phase zone bottom of fluidized-bed reactor body 3, outlet caliber can be appropriate expanding as needed so that riser institute
The material of entrainment can even dispersion in dilute-phase zone.This height design can preferably form the inner-outer circulation of material, and pole
Big raising dilute-phase zone granule materials concentration, extends gas-solid contact time, strengthens gas-solid contact, makes full use of fluidized-bed reactor
The dilute-phase zone space of body 3.
The wind speed of the described lifting wind of riser 4 is higher than the superficial gas velocity in fluidized-bed reactor body 3.It is so more favourable
Differential pressure is formed in the interior outside of the aperture of riser 4 so that the material of the emulsion zone of fluidized-bed reactor body 3 is under the promotion of differential pressure
Into riser 4.
Described fluidized-bed reactor body 3, changeover portion 5, bed 6 is transported in overall structure.Monolithic construction one side side
Just manufacture, be on the other hand conducive to improving the stability of part connection
Described fluidized-bed reactor body 3, changeover portion 5 and transport bed 6 and be coaxially disposed.So be more beneficial for dilute-phase zone and
The material of changeover portion 5, which enters, transports bed 6.
Described transports the caliber that the caliber of bed 6 is less than fluidized-bed reactor body 3, so as to improve the table transported in bed 6
Gas velocity is seen, is easy to it to reach the state of Geldart-D particle or fast fluidization.
Described returning charge valve A9 outlet is located at the dilute-phase zone stage casing of fluidized-bed reactor body 3, so as to further increase
Dilute-phase zone granule density, strengthens gas-solid contact.
The described lifting of riser 4 wind can according to the application field of the invention device mixed with a certain amount of reaction wind, due to
Riser 4 is in the state of Geldart-D particle, and gas-solid mixing acutely, can so cause the reacting gas can be with riser 4
Carry out more sufficiently reaction to improve reaction rate with granule materials.
With reference to embodiment, by a kind of novel fluidized bed reactor of the present invention be applied to carbon dioxide continuously adsorb-
It is desorbed in comprehensive experimental device：
A kind of novel fluidized bed reactor of the present invention is mainly as CO2Adsorptive reactor is used.Carbon dioxide is continuously inhaled
Attached-desorption comprehensive experimental device includes air compartment 1, air distribution plate 2, fluidized-bed reactor body 3, riser 4, changeover portion 5, transports bed
6th, cyclone separator 7, standpipe 8, returning charge valve A9, returning charge valve B10, CO2Desorption reaction device 11.The bottom of fluidized-bed reactor body 3
End is connected with air distribution plate 2, and air distribution plate 2 is connected with the top of air compartment 1, the top of fluidized-bed reactor body 3 by changeover portion 5 and
Transport bed 6 to connect, the top for transporting bed 6 is connected with the entrance of cyclone separator 7, the material outlet of cyclone separator 7, which passes through, to be stood
Pipe 8 and CO2Desorption reaction device 11 is connected, and returning charge valve A9 and returning charge valve B10 entrances pass through refeed line A12 and refeed line B13 respectively
With CO2The emulsion zone of desorption reaction device 11 is connected, and returning charge valve A9 outlet is connected with the dilute-phase zone of fluidized-bed reactor body 3, returning charge
Valve B10 outlet is connected with the emulsion zone of fluidized-bed reactor body 3；The wall of air compartment 1 is provided with fluidized wind entrance, and fluidized wind leads to
Cross fluidized wind entrance to be passed through in air compartment 1, fluidized-bed reactor body 3 is then entered by air distribution plate 2 again；Many risers 4 are passed through
Air compartment 1 and air distribution plate 2 are worn, and using high level matches with low level arrangement, riser 4 is fixedly connected on the wall of air compartment 1 and air distribution plate 2, and
And junction is sealed.The entrance of riser 4 is located at the outside of air compartment 1, and it is dilute that the higher outlet of riser 4 is located at fluidized-bed reactor body 3
Phase region is located at the dilute-phase zone bottom of fluidized-bed reactor body 3 close to changeover portion 5, the relatively low outlet of riser 4, and riser 4, which is passed through, to be carried
Wind is risen, the tube wall of riser 4 is furnished with multiple charging apertures at higher than the height of air distribution plate 2, is easy to the thing of fluidized reactor emulsion zone
Material enters riser 4, and the outlet of higher riser 4 is located at the dilute-phase zone top of fluidized-bed reactor body 3 at changeover portion 5,
The outlet of relatively low riser 4 is located at the dilute-phase zone bottom of fluidized-bed reactor body 3, and outlet caliber can be appropriate expanding as needed,
Enable riser entrained with material even dispersion in dilute-phase zone.This high level matches with low level can preferably form the interior of material
Outer circulation, and dilute-phase zone granule density is greatly improved, strengthen gas-solid contact, make full use of the dilute phase of fluidized-bed reactor body 3
Area space.
CO2Fluidized-bed reactor body 3 is using the mode of operation of bubbling fluidized bed, fluidized-bed reactor in adsorptive reactor
Material in body 3 is CO2Adsorbent, CO2The fluidized wind of fluidized-bed reactor body 3 is to be taken off by desulfurization in adsorptive reactor
Flue gas after nitre and pressurized treatment, lifting bypass of the wind from fluidized wind of riser 4, CO2The fluidized wind of desorption reaction device 11
For the pure CO recycled2。
During the plant running, the fluidized wind of the flue gas formation through pressurized treatment enters CO by air distribution plate 22Adsorption reaction
Device, the solid amine absorber of high activity in reactor is fluidized, and it is adsorbed the CO in flue gas2.Fluidized wind wind speed is adjusted simultaneously,
Reactor is set to be run under bubbling fluidized bed state, to extend the residence time of solid amine absorber in the reactor.Adjust simultaneously
Save the wind speed of lifting wind in height riser 4 so that the wind speed of the lifting wind of riser 4 is higher than in fluidized-bed reactor body 3
Superficial gas velocity, so forms differential pressure, the solid amine absorber of fluidized reactor emulsion zone is in difference in the interior outside of the aperture of riser 4
Under the promotion of pressure, the boosted aperture of pipe 4 enters in riser 4, is then moved upwards under the entrainment of lifting wind, relatively low riser
4 outlets are located at the dilute-phase zone bottom of fluidized-bed reactor body 3, and the material that lifting wind is carried is subtracted during dilute-phase zone is entered
Speed, is then moved downward under gravity, the interior circulation of formation material, and then the dilute-phase zone of fluidized-bed reactor body 3
Solid amine absorbent particles concentration rolls up, and further extends gas-solid contact time, strengthens decarburization efficiency；Higher riser 4
Outlet is located at the dilute-phase zone top of fluidized-bed reactor body 3 close to the part of changeover portion 5, and agent that what lifting wind was carried partially absorb can be after
Continuous move across upwards crosses accelerating into for section 5 and transports bed 6, transports bed 6 and is in Geldart-D particle or fast fluidization, therefore enters
The absorbent for transporting bed 6 all brings cyclone separator 7 into air-flow, the solid amine absorber trapped by cyclone separator 7 via
Cyclone separator standpipe 8 enters CO2Desorption reaction device 11 is desorbed, in CO2The solid amine absorber regenerated in desorption reaction device 11
Returning charge valve A9 and returning charge valve B10 are respectively enterd by refeed line A12 and refeed line B13, fluid bed is then returned to respectively anti-
Answer the dilute-phase zone stage casing of device body 3 and the emulsion zone of fluidized-bed reactor body 3.The CO generated in desorption process2And H2O gaseous mixture
Body, after condensed device dehydration, can obtain the CO of high-purity2, a part of CO therein2CO can be used as2The stream of desorption reaction device 11
Wind transmission, remaining CO2Storage can be filled or commercial Application is carried out.
Obviously, above-described embodiment is only intended to clearly illustrate example, and the not restriction to embodiment.For
For those of ordinary skill in the art, other various forms of changes or change can also be made on the basis of the above description
It is dynamic.There is no necessity and possibility to exhaust all the enbodiments.And the obvious change or change thus extended out
Among moving still in the protection domain of the invention.
Claims (7)
1. a kind of fluidized-bed reactor with Independent adjustable inner-outer circulation flow rate, it is characterised in that the reaction unit includes wind
Room (1), air distribution plate (2), fluidized-bed reactor body (3), riser (4), changeover portion (5), transport bed (6), cyclone separator
(7), standpipe (8), returning charge valve A (9), returning charge valve B (10)；
Top in fluidized-bed reactor body (3) is dilute-phase zone, and bottom is emulsion zone, and the bottom of emulsion zone is air distribution plate (2),
The bottom of air distribution plate (2) is air compartment (1), and the top of fluidized-bed reactor body (3) is connected by changeover portion (5) with transporting bed (6)
Connect, the top (6) for transporting bed is connected with the upper entrance of cyclone separator (7), the bottom material outlet of cyclone separator (7) leads to
Cross standpipe (8) to be connected with returning charge valve A (9) and returning charge valve B (10) entrance, returning charge valve A (9) outlet and fluidized-bed reactor body
(3) dilute-phase zone stage casing is connected, and returning charge valve B (10) outlet is connected with fluidized-bed reactor body (3) emulsion zone；Many risers
(4) air compartment (1) and air distribution plate (2) are run through, riser (4) entrance is located on the outside of air compartment (1), riser (4) outlet is located at fluidisation
Dilute-phase zone in bed reactor body (3).
2. the fluidized-bed reactor according to claim 1 with Independent adjustable inner-outer circulation flow rate, it is characterised in that should
Fluidized-bed reactor also includes CO2Desorption reaction device (11), refeed line A (12), refeed line B (13)；Described standpipe (8) bottom
Connect a CO2Desorption reaction device (11), the CO2Desorption reaction device (11) meets returning charge valve A (9) by refeed line A (12), equally,
The CO2Desorption reaction device (11) meets returning charge valve B (10) by refeed line B (13)；Returning charge valve A (9) outlet and fluidized-bed reaction
Device body (3) dilute-phase zone stage casing is connected, and returning charge valve B (10) outlet is connected with fluidized-bed reactor body (3) emulsion zone.
3. the fluidized-bed reactor according to claim 1 or 2 with Independent adjustable inner-outer circulation flow rate, it is characterised in that
Described riser (4) arranges two or more than two according to actual needs, and is taken using high riser with low riser height
The arrangement matched somebody with somebody, the outlet of high riser is located at fluidized-bed reactor body (3) dilute-phase zone at changeover portion, low riser
Outlet be located at fluidized-bed reactor body (3) dilute-phase zone bottom, the outlet caliber of riser (4) can suitably expand as needed
Footpath so that the material of riser entrained with can even dispersion in dilute-phase zone.
4. the fluidized-bed reactor according to claim 1 or 2 with Independent adjustable inner-outer circulation flow rate, it is characterised in that
Described riser (4) tube wall is being furnished with multiple charging apertures close to air distribution plate (2) place.
5. the fluidized-bed reactor according to claim 1 or 2 with Independent adjustable inner-outer circulation flow rate, it is characterised in that
The speed of lifting wind is higher than the superficial gas velocity of fluidized-bed reactor body (3) emulsion zone in riser (4).
6. the fluidized-bed reactor according to claim 1 or 2 with Independent adjustable inner-outer circulation flow rate, it is characterised in that
Described fluidized-bed reactor body (3), changeover portion (5), bed (6) is transported for overall structure.
7. the fluidized-bed reactor according to claim 1 or 2 with Independent adjustable inner-outer circulation flow rate, it is characterised in that
Described fluidized-bed reactor body (3), changeover portion, transport bed and be coaxially set.
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| CN113266819A (en) * | 2021-04-09 | 2021-08-17 | 东南大学 | Surge reactor device and surge characteristic characterization method |
| CN114028903A (en) * | 2021-10-22 | 2022-02-11 | 国能国华(北京)电力研究院有限公司 | System for catching carbon dioxide in flue gas |
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| CN103120919A (en) * | 2013-01-30 | 2013-05-29 | 东南大学 | Transport bed coupling reaction device of fluidized bed |
| CN103756712A (en) * | 2014-01-13 | 2014-04-30 | 东南大学 | Biomass quick cracking device based on internal-external circulation spouted fluidized bed |
| CN104197323A (en) * | 2014-09-19 | 2014-12-10 | 东南大学 | Inner and outer circulation coupled device for separating carbon dioxide by burning coal-based chemical loopings |
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