CN206199225U - Gas-solid fluidized bed calcination reactor - Google Patents
Gas-solid fluidized bed calcination reactor Download PDFInfo
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- CN206199225U CN206199225U CN201621052355.6U CN201621052355U CN206199225U CN 206199225 U CN206199225 U CN 206199225U CN 201621052355 U CN201621052355 U CN 201621052355U CN 206199225 U CN206199225 U CN 206199225U
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Abstract
A kind of gas-solid fluidized bed calcination reactor,Including shell,And the guide shell in shell,Shell is provided with primary air inlet,Gas outlet,Charging aperture and discharging structure,Wherein,Primary air inlet is located at the bottom of guide shell,For to conveying high-temperature gas in guide shell,Gas outlet is located at the top of shell,For discharging flue gas,Charging aperture and discharging structure are located at the guide shell outer circumferential side respectively,Charging aperture treats calcining materials for offer,Discharging structure is used to collect and discharge calcining waste material,The two ends of guide shell are spaced apart with outer casing inner wall respectively,Guide shell,Space between guide shell and the outer casing inner wall forms the circulation canal of calcination reaction,Powdery treats that calcining materials enter in the shell from charging aperture,High-temperature gas enters the guide shell from primary air inlet,And drive treats calcining materials in the circulation canal interior circulation calcination reaction.The reactor makes solid particle realize the directed flow of macroscopic view and microcosmic strong turbulence.
Description
Technical field
The utility model is related to fluidized bed calcination equipment technical field, more particularly, to a kind of gas-solid fluidized bed calcining
Reactor.
Background technology
Calcination process is widely used in the processes such as the thermal decomposition of solid, crystal transfer.In recent years, gas-solid fluidized bed calcining
Device because of gas-solid contact fully, gas-particle heat transfer efficiency high, homogeneous heating the advantages of, and gradually replace traditional Static Calcination stove,
It is used widely in chemical industry and mining industry.
The fluidized bed calcining device of industrial application mainly has ordinary fluidized bed, multilayer or multi-cell fluidized bed and follows at present
Ring fluid bed etc..Ordinary fluidized bed is individual layer or single chamber fluid bed, and solid is real by gas heating in the state of fluidization
Now thermally decompose, the calcining furnace of a kind of lime stone as disclosed in patent WO9712188 (A1).The fluidized bed calcination hearth layer is approached
Complete mixing flow, the motive force of mass-and heat-transfer is low, and the distribution of residence time is wide in range, and reaction conversion ratio is relatively low.
A kind of cascade form of multicompartment fluidized bed or multi-cell fluidized bed, actually fluid bed.Can effectively be utilized by cascade
Mass-and heat-transfer motive force, extends mean residence time, improves reaction conversion ratio.Such as Chinese utility model patent CN
I04833208A discloses a kind of multi-cell fluidized bed roaster of stepped cascade.But in multilayer or multi-cell fluidized bed reactor
The spatial and temporal distributions of particle are still more wide in range, and back-mixing is generally than more serious between interlayer or room.Increase particle stopping in fluid bed
It is to use recirculating fluidized bed to stay time, the another way of raising reaction depth.This device generally by fluid bed, separator,
Down-comer is constituted.Particle is fluidized and lifted in fluid bed by air-flow, is separated with gas by cyclone separator in bed outlet,
The down-comer that particle feeding after separation is connected with fluid bed, is then recycled in fluid bed, such circular response, until reaching again
To the conversion ratio that reaction needs, by controlling circulation time of the particle in bed and down-comer, when can control averagely to stop
Between be distributed.As Chinese utility model patent CN 1884049A disclose a kind of using roasting troilite in circulating fluidized bed preparation two
The method of sulfur oxide.But the defect of this reactor is that descending branch does not have gas to convey heat, therefore in the reaction efficiency of this section
Very low, space reactor is not used effectively, and air once passes through, and heat does not make full use of.
Utility model content
In view of this, the purpose of this utility model is to provide a kind of directed flow that solid particle can be made to realize macroscopic view
With the gas-solid fluidized bed calcination reactor of microcosmic strong turbulence.
Another object of the present utility model is to provide that a kind of heat transfer, mass-transfer performance are good, and solid particle spatial and temporal distributions are uniform,
Residence time is long, the gas-solid fluidized bed calcination reactor that solid particle pyrolysis are efficient, energy consumption is low.
According to the gas-solid fluidized bed calcination reactor that the utility model is provided, including shell, and in the shell
Guide shell,
The shell is provided with primary air inlet, gas outlet, charging aperture and discharging structure, wherein,
The primary air inlet is located at the bottom of the guide shell, for conveying high-temperature gas in the guide shell,
The gas outlet is located at the top of the shell, for discharging flue gas,
The charging aperture and discharging structure are located at the guide shell outer circumferential side respectively, and the charging aperture is used to provide to wait to calcine
Material, the discharging structure is used to collect and discharge calcining waste material,
The two ends of the guide shell are spaced apart with outer casing inner wall respectively, and the guide shell, guide shell are outer with described
Space between shell inwall forms the circulation canal of calcination reaction, treats that calcining materials enter in the shell from the charging aperture,
High-temperature gas enters the guide shell from the primary air inlet, and treats calcining materials in the circulation canal interior circulation described in drive
Calcination reaction.
Preferably, the shell includes conversion zone, and positioned at the segregation section of the conversion zone upper end, the conversion zone is used
In the carrying out of Cyclic Calcination reaction, the segregation section is separated for calcining waste material with flue gas.
Preferably, the conversion zone is tubular, and its ratio of height to diameter is 6:1~12:1.
Preferably, the ratio between annular space width that conversion zone is surrounded with guide shell is 1.2:1~0.5:1.
Preferably, the segregation section include positioned at its lower end cone cylinder portion, the segregation section through the cone cylinder portion with it is described
The upper end connection of shell.
Preferably, the discharging structure includes discharge gate and the discharge groove connected with the discharge gate, wherein,
The discharge gate calcines waste material on the outer wall of the shell for discharging,
The discharge groove calcines waste material and is transported to the discharge gate on the outer casing inner wall for collecting.
Preferably, the guide shell includes at least one diversion section for setting axially along, the height in the guide shell
The gaseous mixture of wet body and calcining materials is formed through entering the space between guide shell and outer casing inner wall between adjacent diversion section
Multistage high-temperature gas circulation.
Preferably, the height and diameter ratio of each diversion section are 3:1~8:1.
Preferably, the lower end of the shell is provided with the main distributor connected with the primary air inlet, the main distributor position
In the bottom of the guide shell, high-temperature gas enters the main distributor through the primary air inlet, and enters through the main distributor
Enter the guide shell.
Preferably, the main distributor is sieving-disc type distributor.
Preferably, the ratio between the main distributor diameter and draft tube diameter are 1.5:1~0.5:1.
Preferably, also including between air inlet between level and air inlet is connected between the level level between distributor, the level
Between adjacent diversion section, high-temperature gas enters corresponding diversion section to distributor through distributor between the level.
Preferably, distributor is ring type distributor between the level.
Preferably, the ratio between distributor diameter and draft tube diameter are 0.8 between the level:1~0.2:1.
Preferably, the lower end of the guide shell is provided with tapered expansion section, and the tapered expansion section covers the main distributor,
For collecting the high-temperature gas from main distributor.
Preferably, the tapered expansion section taper is 1:1~1:4.
Preferably, the ratio between the tapered expansion section bottom opening diameter and draft tube diameter are 1.5~1:1.
Preferably, also including elevated bunker, the elevated bunker is connected with the charging aperture, for that will treat that calcining materials are defeated
It is sent into the shell.
Preferably, it is provided with auxiliary heat exchanging device on the bottom wall of the shell.
The beneficial effect that the utility model is realized：The gas-solid fluidized bed calcination reactor makes solid particle realize macroscopic view
Directed flow and microcosmic strong turbulence, heat transfer, mass-transfer performance are good, and solid particle spatial and temporal distributions are uniform, and the residence time is long, solid
Particle pyrolysis are efficient, energy consumption is low.Compared with traditional recirculating fluidized bed calciner plant, inner recirculation flow of the present utility model
Change bed cycle rate fast, descending branch is still located inside reactor, reaction realizes cascade simultaneously still carrying out, effectively utilization
Mass-and heat-transfer motive force.
Brief description of the drawings
By description referring to the drawings to the utility model embodiment, of the present utility model above-mentioned and other mesh
, feature and advantage will be apparent from.
Fig. 1 shows the structural representation of the gas-solid fluidized bed calcination reactor according to the utility model embodiment.
The structure that Fig. 2-3 respectively illustrates two kinds of guide shells of different embodiments according to the utility model embodiment is shown
It is intended to.
Fig. 4 shows the working state figure of the gas-solid fluidized bed calcination reactor according to the utility model embodiment.
In figure：Primary air inlet 11, gas outlet 12, charging aperture 13, discharging structure 14, discharge gate 141, discharge groove 142, reaction
Section 15, segregation section 16, cone cylinder portion 161, the 21, first diversion section 22 of guide shell 2, tapered expansion section, the second diversion section the 23, the 3rd are led
Stream section 24, distributor 4, air inlet pipe 5 between gap 25, sieve aperture 26, main distributor 3, level.
Specific embodiment
Various embodiments of the present utility model are more fully described hereinafter with reference to accompanying drawing.In various figures, identical
Element is represented using same or similar reference.For the sake of clarity, the various pieces in accompanying drawing are not drawn to paint
System.
Fig. 1 shows the structural representation of the gas-solid fluidized bed calcination reactor according to the utility model embodiment.Such as Fig. 1
It is shown, the gas-solid fluidized bed calcination reactor, including shell, and the guide shell 2 in the shell.Set on the shell
There are primary air inlet 11, gas outlet 12, charging aperture 13 and discharging structure 14.Wherein, the primary air inlet 11 is located at the guide shell 2
Bottom, and connected with the guide shell 2, for conveying high-temperature gas in the guide shell 2.The gas outlet 12 is located at institute
The top of shell is stated, for discharging flue gas.
The charging aperture 13 and discharging structure 14 are located at the outer circumferential side of the guide shell 2 respectively, and the charging aperture 13 is used to carry
For treating calcining materials, the calcining materials are graininess, or even powdered, can be flowed under the drive of high-temperature gas.It is described
Discharging structure 14 is used to collect and discharge calcining waste material.The calcining waste material refers to calcining fully, and density is reduced to certain journey
The waste material of degree.The two ends of the guide shell 2 are spaced apart with outer casing inner wall respectively, the guide shell 2, guide shell 2 and institute
The circulation canal that the space between outer casing inner wall forms calcination reaction is stated, powdery treats that calcining materials enter institute from the charging aperture 13
State in shell, high-temperature gas enters the guide shell 2 from the primary air inlet 11, and treats that calcining materials are followed described described in drive
Ring passage interior circulation calcination reaction.
Further, the shell includes conversion zone 15, and positioned at the segregation section 16 of the upper end of the conversion zone 15, it is described
Conversion zone 15 is used for the carrying out of Cyclic Calcination reaction, and the segregation section 16 is separated for calcining waste material with flue gas.In the implementation
In example, the conversion zone 15 and segregation section 16 are respectively cylindrical shape, the diameter with diameter greater than shell of the segregation section 16.It is described
Conversion zone 15 is tubular, and its ratio of height to diameter is 6:1~12:1, and the ratio between the annular space width that is surrounded with guide shell 2 of conversion zone 15 is
2:1~0.5:1, preferably 1.2:1~0.5:1.The calcining waste material refers to calcining fully, and density is reduced to a certain degree of
Waste material, the waste material can enter the segregation section 16 with flue gas, after being separated with flue gas, be discharged through the discharging structure 14.As excellent
Selection of land, the segregation section 16 include positioned at its lower end cone cylinder portion 161, the segregation section 16 through the cone cylinder portion 161 with it is described
The upper end connection of shell.Due to the diameter with diameter greater than the conversion zone 15 of the segregation section 16, flue gas entrainment waste material is herein
Place is diffused, and falls the cone cylinder portion 161, and discharging structure 14 is slided into through cone cylinder portion 161, and is finally discharged, after separation
Flue gas is discharged through the exhaust outlet.
Preferably, also including cyclone separator (not shown), the cyclone separator connects with the gas outlet 12
Connect, enable to calcining materials rapidly and efficiently to be separated with flue gas.
The discharging structure 14 includes discharge gate 141 and the discharge groove 142 connected with the discharge gate 141.Wherein, institute
Discharge gate 141 is stated on the outer wall of the shell, for discharging calcining waste material；The discharge groove 142 is in the shell
On wall, for collecting calcining waste material and being transported to the discharge gate 141.
The guide shell 2 includes at least one diversion section for setting axially along, the high-temperature gas in the guide shell 2
With the gaseous mixture of calcining materials through entering the space between guide shell 2 and outer casing inner wall between adjacent diversion section, form multistage
High-temperature gas is circulated, can be fully calcined to material.The lower end of the guide shell 2 is provided with tapered expansion section 21, and the taper is expanded
Big section 21 covers the main distributor 3, for collecting the high-temperature gas from main distributor 3.Preferably, the tapered expansion section
21 taper is 1:1~1:4, bottom opening diameter is 1.5~1 with the diameter ratio of guide shell 2:1.
Fig. 2-3 respectively illustrates two kinds of structures of the guide shell of different embodiments 2 according to the utility model embodiment
Schematic diagram.In two kinds of implementation methods, the number of the diversion section is three, including first for once setting from bottom to top is led
Stream section 22, the second diversion section 23 and the 3rd diversion section 24.Except that, in the embodiment shown in figure 2, the guide shell
2 is split-type structural, is monolithic construction in the implementation method shown in Fig. 2.The guide shell 2 is split-type structural, i.e., adjacent
Diversion section between setting spaced apart.Wherein, between the diversion section 23 of first diversion section 22 and second, and second
Space is formed between the diversion section 24 of diversion section 23 and the 3rd respectively, a small amount of gas can flow out from the gap 25, but these gases
The resistance of rising is big, and speed is small, is not enough to prevent flowing downward for particle.In the embodiment shown in fig. 3, the guide shell 2
To be integrally formed, direction sets gradually 26 groups of 26 groups of the first sieve aperture and the second sieve aperture, two sieve apertures from bottom to top axially along
26 groups respectively as the segmentation boundary between different diversion sections.26 groups of the sieve aperture can through drilling etc. mode obtain.Described
One to the second 26 groups of sieve aperture is circumferentially disposed around the guide shell 2.Likewise, a small amount of gas can be from two 26 groups of sieve apertures
Outflow, but the resistance that these gases rise is big, and speed is small, is not enough to prevent flowing downward for particle.Each diversion section
Height and diameter ratio are preferably 3:1~8:1.
The specific number of the diversion section is not limited to three, or has one, two or four, even more,
Its specific number sets as needed.
The lower end of the shell is provided with the main distributor 3 connected with the primary air inlet 11, and the main distributor 3 is located at institute
The bottom of guide shell 2 is stated, high-temperature gas enters the main distributor 3 through the primary air inlet 11, and enters through the main distributor 3
Enter the guide shell 2.The diameter of the main distributor 3 is preferably 1.5 with the diameter ratio of guide shell 2:1~0.5:1.The main distribution
Device 3 is specifically chosen as sieve aperture disc type distributor or ring type distributor.The High Temperature Gas scale of construction for wherein entering from main distributor 3 is not less than
The 50% of gas gross.
Further, air inlet and the air inlet company between the level between the gas-solid fluidized bed calcination reactor also includes level
Distributor 4 is between adjacent diversion section between distributor 4 between logical level, the level.Specifically, being connected on distributor 4 between level
There is an air inlet pipe 5, the air inlet pipe 5 extends to housing exterior, high-temperature gas enters distributor 4 between level through respective air inlet pipe 5, and
Enter corresponding diversion section through distributor 4 between the level.The diameter of distributor 4 is preferably with the diameter ratio of guide shell 2 between the level
0.8:1~0.2:1.Distributor 4 is specifically chosen as ring type distributor between the level.
Further, the gas-solid fluidized bed calcination reactor also includes elevated bunker (not shown), the elevated bunker
It is connected with the charging aperture 13, for that will treat that calcining materials are conveyed into the shell, and is provided with the bottom wall of the shell
Auxiliary heat exchanging device.
Fig. 4 shows the working state figure of the gas-solid fluidized bed calcination reactor according to the utility model embodiment.With reference to
Fig. 4, below with regard to the utility model in the use of gas-solid fluidized bed calcination reactor be described in detail by embodiment 1-5.
Embodiment 1:Two sections of gas-solid fluidized bed calcination reactors of interior circulation
Concrete structure parameter is as follows：In the embodiment, 2 points of guide shell is two diversion sections, the internal diameter 125mm of conversion zone 15,
Height 750mm, segregation section 16 internal diameter 175mm, height 250mm；The diameter 62mm of guide shell 2, is divided to two sections, the 1st section high from top to bottom
350mm, the 2nd section of 280mm high, take many modes of arrangement, space 40mm between two, the under shed diameter 80mm of guide shell 2, cone
Degree 1:2；Guide shell 2 is apart from outer casing bottom 30mm.Main distributor 3 is sieving-disc type distributor, a diameter of 80mm；Distributor 4 between level
It is ring type distributor, diameter 40mm.
With calcium carbonate (10 microns of average grain diameter) for model solid particle, initial fluidizing gas velocity (mark condition) is determined
0.054m/s；It is 0.2m/s in gas empty bed speed, the apparent above-mentioned speed of solid particle is 1.2m/s in guide shell 2, declines segment table
Sight fall rate is 0.4m/s.
Embodiment 2:Three sections of ICFB calcination reactors
Concrete structure parameter is as follows：Conversion zone 15 internal diameter 125mm, height 950mm, the internal diameter 175mm of segregation section 16, height
220mm；The diameter 56mm of guide shell 2, divides 3 sections, and the 1st section of 320mm high, the 2nd section of 280mm high, the 3rd section of 260mm high take intersegmental opening
The mode in hole, the two intersegmental perforate gross areas are 16cm2, total a height of 50mm shared by two sections of perforates；The under shed diameter of guide shell 2
80mm, taper 1:2.Guide shell 2 is apart from outer casing bottom 30mm.Main distributor 3 is sieving-disc type distributor, a diameter of 80mm；Between level
Distributor 4 is ring type distributor, diameter 35mm.
It is 0.2m/s in gas empty bed speed with calcium carbonate (10 microns of average grain diameter) for model solid particle, it is solid in guide shell 2
The apparent above-mentioned speed of body particle is 1.4m/s, and the apparent fall rate of descending branch is 0.5m/s.
Embodiment 3:Calcine a hydrated magnesium chloride and prepare basic magnesium chloride Mg (OH) Cl
Using the calcination reactor in embodiment 1, high-temperature gas is hot-air, and temperature is 340 DEG C, and MgCl2H2O is used
MgCl26H2O prepares (crystallization water mass fraction is 19.2%) in advance, and reactor is continuously added into by elevated bunker；Reactor
Atmospheric operation, total throughput (mark condition) is 1800L/h, wherein 70% gas is passed through from the main distributor 3 of bottom, remaining is from 1
Distributor 4 is passed through between individual level.Average bed density is 580kg/m3 in reactor；Feed rate is 8kg/h.Operation reaches stable state
When, 274 DEG C of the mean temperature of reactor first paragraph, 276 DEG C of the 2nd section of mean temperature；The matter of basic magnesium chloride in products obtained therefrom
Amount fraction is 78%.
Embodiment 4：Calcine a hydrated magnesium chloride and prepare magnesia
Using the reactor in embodiment 2, high-temperature gas is hot-air, and temperature is 500 DEG C,
MgCl2H20 uses MgCl26H20 to prepare (crystallization water mass fraction is 19.2%) in advance, is expected by a high position
Groove is continuously added into reactor；Reactor atmospheric operation, total throughput (mark condition) is 1400L/h, wherein 62% gas is from bottom
Main distributor 3 be passed through, 20% gas is passed through from distributor 4 between the 1st level, and remaining is passed through from distributor 4 between the 2nd level,
Average bed density is 595kg/m3 in reactor；Feed rate is 8.2kg/h.Reactor first paragraph (under) mean temperature
420 DEG C, the 2nd section of reactor (in) 412 DEG C of mean temperature；Reactor second segment (on) 413 DEG C of mean temperature；Products obtained therefrom
Distribution is as shown in table 1 below.
The calcination product of table 1 is distributed
| Component | MgO | Mg(OH)Cl | MgCl2 | H2O |
| Mass fraction (%) | 64 | 21 | 11 | 4 |
Embodiment 5：Calcining sodium acid carbonate prepares sodium carbonate
Using the reactor in embodiment 1, high-temperature gas is hot-air, and temperature is 340 DEG C；Principle sodium acid carbonate (contains
The water of mass fraction 12%) reactor is continuously added into by elevated bunker；Calcination reactor atmospheric operation, total throughput (mark condition)
It is 1200L/h, wherein 70% gas is passed through from the main distributor 3 of bottom, remaining is passed through from distributor 4 between 1 level.Reactor
Interior average bed density is 420kg/m3；Feed rate is 5.4kg/h.Operation is when reaching stable state, the 1st section of reactor (under) it is flat
Equal 284 DEG C of temperature, 286 DEG C of the mean temperature that the 2nd section of reactor；The mass fraction of sodium carbonate is 94% in products obtained therefrom.
Distributor 4 and main distributor 3 are used cooperatively between multiple levels, high-temperature gas each leads into, and multiple diversion sections set
Put, reaction mixture gas body is constantly discharged from the gap 25 between sieve aperture 26 or adjacent guide section, is circulated again, forms one kind
The multistage gas-solid fluidized bed calcination reactor of interior circulation.The gas-solid fluidized bed calcination reactor makes solid particle realize determining for macroscopic view
To flowing and microcosmic strong turbulence, heat transfer, mass-transfer performance are good, and solid particle spatial and temporal distributions are uniform, and the residence time is long, solid
Grain pyrolysis are efficient, energy consumption is low.Compared with traditional recirculating fluidized bed calciner plant, it is of the present utility model inner circulation fluidized
Bed cycle rate is fast, and descending branch is still located inside reactor, and reaction realizes cascade simultaneously still carrying out, and is effectively utilized
Mass-and heat-transfer motive force.
It should be noted that herein, such as first and second or the like relational terms are used merely to a reality
Body or operation make a distinction with another entity or operation, and not necessarily require or imply these entities or deposited between operating
In any this actual relation or order.And, term " including ", "comprising" or its any other variant be intended to
Nonexcludability is included, so that process, method, article or equipment including a series of key elements not only will including those
Element, but also other key elements including being not expressly set out, or also include being this process, method, article or equipment
Intrinsic key element.In the absence of more restrictions, the key element limited by sentence "including a ...", it is not excluded that
Also there is other identical element in process, method, article or equipment including the key element.
Finally it should be noted that：Obviously, above-described embodiment is only intended to clearly illustrate the utility model example,
And not to the restriction of implementation method.For those of ordinary skill in the field, may be used also on the basis of the above description
To make other changes in different forms.There is no need and unable to be exhaustive to all of implementation method.And thus
Among the obvious change or variation amplified out are still in protection domain of the present utility model.
Claims (19)
1. a kind of gas-solid fluidized bed calcination reactor, it is characterised in that including shell, and the water conservancy diversion in the shell
Cylinder,
The shell is provided with primary air inlet, gas outlet, charging aperture and discharging structure, wherein,
The primary air inlet is located at the bottom of the guide shell, for conveying high-temperature gas in the guide shell,
The gas outlet is located at the top of the shell, for discharging flue gas,
The charging aperture and discharging structure are located at the guide shell outer circumferential side respectively, and the charging aperture treats calcined material for offer
Material, the discharging structure is used to collect and discharge calcining waste material,
The two ends of the guide shell are spaced apart with outer casing inner wall respectively, in the guide shell, guide shell and the shell
Space between wall forms the circulation canal of calcination reaction, treats that calcining materials enter in the shell from the charging aperture, high temperature
Gas enters the guide shell from the primary air inlet, and treats that calcining materials are calcined in the circulation canal interior circulation described in drive
Reaction.
2. gas-solid fluidized bed calcination reactor according to claim 1, it is characterised in that the shell includes conversion zone,
And positioned at the segregation section of the conversion zone upper end, the conversion zone is used for the carrying out of Cyclic Calcination reaction, the segregation section is used
Separated with flue gas in calcining waste material.
3. gas-solid fluidized bed calcination reactor according to claim 2, it is characterised in that the conversion zone is tubular, its
Ratio of height to diameter is 6:1~12:1.
4. gas-solid fluidized bed calcination reactor according to claim 3, it is characterised in that conversion zone is surrounded with guide shell
The ratio between annular space width is 1.2:1~0.5:1.
5. gas-solid fluidized bed calcination reactor according to claim 2, it is characterised in that the segregation section includes being located at it
The cone cylinder portion of lower end, the segregation section is connected through the cone cylinder portion with the upper end of the shell.
6. gas-solid fluidized bed calcination reactor according to claim 1, it is characterised in that the discharging structure includes discharge
Mouth and the discharge groove connected with the discharge gate, wherein,
The discharge gate calcines waste material on the outer wall of the shell for discharging,
The discharge groove calcines waste material and is transported to the discharge gate on the outer casing inner wall for collecting.
7. gas-solid fluidized bed calcination reactor according to claim 1, it is characterised in that the guide shell include along
Its axially arranged multiple diversion section, the gaseous mixture of high-temperature gas in the guide shell and calcining materials is through adjacent diversion section
Between enter space between guide shell and outer casing inner wall, form multistage high-temperature gas circulation.
8. gas-solid fluidized bed calcination reactor according to claim 7, it is characterised in that the height of each diversion section
It is 3 with diameter ratio:1~8:1.
9. gas-solid fluidized bed calcination reactor according to claim 7, it is characterised in that the lower end of the shell be provided with
The main distributor of the primary air inlet connection, the main distributor is located at the bottom of the guide shell, and high-temperature gas is through the master
Air inlet enters the main distributor, and enters the guide shell through the main distributor.
10. gas-solid fluidized bed calcination reactor according to claim 9, it is characterised in that the main distributor is screen tray
Formula distributor.
11. gas-solid fluidized bed calcination reactors according to claim 9, it is characterised in that the main distributor diameter with
The ratio between draft tube diameter is 1.5:1~0.5:1.
12. gas-solid fluidized bed calcination reactors according to claim 9, it is characterised in that also including air inlet between level with
And distributor between the level that air inlet is connected between the level, between the level distributor between adjacent diversion section, High Temperature Gas
Body enters corresponding diversion section through distributor between the level.
13. gas-solid fluidized bed calcination reactors according to claim 12, it is characterised in that distributor is ring between the level
Formula distributor.
14. gas-solid fluidized bed calcination reactors according to claim 12, it is characterised in that distributor diameter between the level
It is 0.8 with the ratio between draft tube diameter:1~0.2:1.
15. gas-solid fluidized bed calcination reactors according to claim 1, it is characterised in that the lower end of the guide shell sets
There are tapered expansion section, the tapered expansion section covering main distributor, for collecting the high-temperature gas from main distributor.
16. gas-solid fluidized bed calcination reactors according to claim 15, it is characterised in that the tapered expansion section taper
It is 1:1~1:4.
17. gas-solid fluidized bed calcination reactors according to claim 15, it is characterised in that the tapered expansion section bottom
The ratio between opening diameter and draft tube diameter are 1.5~1:1.
18. gas-solid fluidized bed calcination reactors according to claim 1, it is characterised in that described also including elevated bunker
Elevated bunker is connected with the charging aperture, for that will treat that calcining materials are conveyed into the shell.
19. gas-solid fluidized bed calcination reactors according to claim 1, it is characterised in that on the bottom wall of the shell
It is provided with auxiliary heat exchanging device.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201621052355.6U CN206199225U (en) | 2016-09-12 | 2016-09-12 | Gas-solid fluidized bed calcination reactor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106215816A (en) * | 2016-09-12 | 2016-12-14 | 原初科技（北京）有限公司 | Gas-solid fluidized bed calcination reactor |
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2016
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106215816A (en) * | 2016-09-12 | 2016-12-14 | 原初科技（北京）有限公司 | Gas-solid fluidized bed calcination reactor |
| CN106215816B (en) * | 2016-09-12 | 2019-05-03 | 原初科技（北京）有限公司 | Gas-solid fluidized bed calcination reactor |
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