CN106215816B - Gas-solid fluidized bed calcination reactor - Google Patents
Gas-solid fluidized bed calcination reactor Download PDFInfo
- Publication number
- CN106215816B CN106215816B CN201610818788.6A CN201610818788A CN106215816B CN 106215816 B CN106215816 B CN 106215816B CN 201610818788 A CN201610818788 A CN 201610818788A CN 106215816 B CN106215816 B CN 106215816B
- Authority
- CN
- China
- Prior art keywords
- gas
- shell
- guide shell
- fluidized bed
- distributor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- 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
-
- 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
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
- B01J8/0025—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor by an ascending fluid
-
- 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
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
-
- 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
- B01J8/1845—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised
- B01J8/1854—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised followed by a downward movement inside the reactor to form a loop
-
- 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
- B01J2208/00743—Feeding or discharging of solids
- B01J2208/00769—Details of feeding or discharging
Abstract
Disclose a kind of gas-solid fluidized bed calcination reactor, including shell, and the guide shell in shell, shell is equipped with primary air inlet, gas outlet, feed inlet and discharging structure, wherein, primary air inlet is located at the lower part of guide shell, for the conveying high-temperature gas into guide shell, gas outlet is located at the top of shell, for flue gas to be discharged, feed inlet and discharging structure are located at the guide shell peripheral side, feed inlet is for providing to calcining materials, discharging structure is for collecting and calcining waste material being discharged, the both 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 waits for that calcining materials enter in the shell from feed inlet, high-temperature gas enters the guide shell from primary air inlet, and it drives to calcining materials in the circulation canal Interior Cyclic Calcination reaction.The reactor makes solid particle realize macroscopical directed flow and microcosmic strong turbulence.
Description
Technical field
The present invention relates to fluidized bed calcination equipment technical fields, more particularly, to a kind of gas-solid fluidized bed calcination reaction
Device.
Background technique
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 gradually replaces traditional Static Calcination furnace because of the advantages that gas-solid contact is abundant, gas-particle heat transfer is high-efficient, homogeneous heating,
It is used widely in chemical industry and mining industry.
The fluidized bed calcining device industrially applied at present mainly has ordinary fluidized bed, multilayer or multi-cell fluidized bed and follows
Ring fluidized bed etc..Ordinary fluidized bed, that is, single layer or single chamber fluidized bed, solid are heated in the state of fluidization by gas real
It now thermally decomposes, the calcining furnace of a kind of lime stone as disclosed in patent WO9712188 (A1).The fluidized bed calcination hearth layer is close
The motive force of complete mixing flow, mass-and heat-transfer is low, and the distribution of residence time is wide in range, and reaction conversion ratio is lower.
Multicompartment fluidized bed or multi-cell fluidized bed, actually a kind of cascade form of fluidized bed.It can be efficiently used by cascade
Mass-and heat-transfer motive force extends mean residence time, improves reaction conversion ratio.As Chinese invention patent CN I04833208A is public
A kind of ladder-like cascade multi-cell fluidized bed roaster of cloth.But in multilayer or multi-cell fluidized bed reactor particle when space division
Cloth is still than broad, and back-mixing is usually than more serious between interlayer or room.Increase particle residence time in a fluidized bed, improve it is anti-
The another way for answering depth is using recirculating fluidized bed.This device is usually made of fluidized bed, separator, down-comer.?
Grain is fluidized and is promoted by air-flow in a fluidized bed, is separated by cyclone separator with gas in bed outlet, the particle after separation
It is sent into the down-comer being connected with fluidized bed, is then recycled in fluidized bed again, such circular response, until reaching what reaction needed
Conversion ratio can control Mean Residence Time Distributions by circulation time of the control particle in bed and down-comer.Such as China
Patent of invention CN 1884049A discloses a kind of method for preparing sulfur dioxide using roasting troilite in circulating fluidized bed.But this
The defect of kind of reactor is that descending branch does not have gas to convey heat, therefore very low in the reaction efficiency of this section, and space reactor does not have
It is used effectively, and air once passes through, heat does not make full use of.
Summary of the invention
In view of this, the purpose of the present invention is to provide one kind, and solid particle can be made to realize the directed flow and micro- of macroscopic view
The gas-solid fluidized bed calcination reactor for the strong turbulence seen.
Another object of the present invention is to provide it is a kind of heat transfer, mass-transfer performance it is good, solid particle spatial and temporal distributions are uniform, stop
Time is long, the gas-solid fluidized bed calcination reactor that solid particle pyrolysis is efficient, low energy consumption.
The gas-solid fluidized bed calcination reactor provided according to the present invention, including shell, and leading in the shell
Flow cartridge,
The shell is equipped with primary air inlet, gas outlet, feed inlet and discharging structure, wherein
The primary air inlet is located at the lower part of the guide shell, is used for the conveying high-temperature gas into the guide shell,
The gas outlet is located at the top of the shell, for flue gas to be discharged,
The feed inlet and discharging structure are located at the guide shell peripheral side, and the feed inlet is for providing wait calcine
Material, the discharging structure are used to collecting and being discharged calcining waste material,
The both ends of the guide shell are spaced apart with outer casing inner wall respectively, the guide shell, guide shell and described outer
Space between shell inner wall forms the circulation canal of calcination reaction, enters in the shell to calcining materials from the feed inlet,
High-temperature gas enters the guide shell from the primary air inlet, and recycles in the circulation canal described in drive to calcining materials
Calcination reaction.
Preferably, the shell includes conversion zone, and the segregation section positioned at the conversion zone upper end, and the conversion zone is used
In the progress of Cyclic Calcination reaction, the segregation section is used to calcine the separation of waste material and flue gas.
Preferably, the conversion zone is tubular, and ratio of height to diameter is 6:1~12:1.
Preferably, the ratio between annular space width that conversion zone and guide shell surround is 1.2:1~0.5:1.
Preferably, the segregation section includes the cone cylinder portion positioned at its lower end, the segregation section through the cone cylinder portion with it is described
The upper end of shell connects.
Preferably, the discharging structure includes discharge gate and the discharge groove that is connected to the discharge gate, wherein
The discharge gate is set on the outer wall of the shell, for calcining waste material to be discharged,
The discharge groove is set on the outer casing inner wall, for collecting calcining waste material and being transported to the discharge gate.
Preferably, the guide shell includes at least one diversion section being arranged axially along, the height in the guide shell
The gaseous mixture of wet body and calcining materials is entered the space between guide shell and outer casing inner wall between adjacent diversion section, formed
Multistage high-temperature gas circulation.
Preferably, the height of each diversion section and diameter ratio are 3:1~8:1.
Preferably, the lower end of the shell is equipped with the main distributor being connected to the primary air inlet, the main distributor position
In the lower part of the guide shell, high-temperature gas through the primary air inlet enter the main distributor, and through the main distributor into
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.
It preferably, further include distributor between air inlet and the grade that air inlet is connected between the grade between grade, between the grade
Distributor is set between adjacent diversion section, and high-temperature gas enters corresponding diversion section through distributor between the grade.
Preferably, distributor is ring type distributor between the grade.
Preferably, the ratio between distributor diameter and draft tube diameter are 0.8:1~0.2:1 between the grade.
Preferably, the lower end of the guide shell is equipped 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.
It preferably, further include elevated bunker, the elevated bunker is connect with the feed inlet, and being used for will be defeated to calcining materials
It is sent into the shell.
Preferably, auxiliary heat exchanging device is equipped on the bottom wall of the shell.
It is that the present invention realizes the utility model has the advantages that the gas-solid fluidized bed calcination reactor make solid particle realize macroscopic view orientation
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 particle
Pyrolysis is efficiently, low energy consumption.It is compared with traditional recirculating fluidized bed calciner plant, internal circulating fluidized bed circulation of the invention
Rate is fast, and descending branch is still located inside reactor, and reaction is still carrying out, and realizes cascade simultaneously, is effectively utilized mass transfer biography
Thermal driving force.
Detailed description of the invention
By referring to the drawings to the description of the embodiment of the present invention, above-mentioned and other purposes of the invention, feature and
Advantage will be apparent from.
Fig. 1 shows the structural schematic diagram of gas-solid fluidized bed calcination reactor according to an embodiment of the present invention.
Fig. 2-3 respectively illustrates the structural representation of the guide shell of two kinds of different embodiments according to an embodiment of the present invention
Figure.
Fig. 4 shows the working state figure of gas-solid fluidized bed calcination reactor according to an embodiment of the present invention.
In figure: primary air inlet 11, gas outlet 12, feed inlet 13, discharging structure 14, discharge gate 141, discharge groove 142, reaction
Section 15, segregation section 16, cone cylinder portion 161, guide shell 2, tapered expansion section 21, the first diversion section 22, the second diversion section 23, third are led
Flow distributor 4, air inlet pipe 5 between section 24, gap 25, sieve pore 26, main distributor 3, grade.
Specific embodiment
The various embodiments that the present invention will be described in more detail that hereinafter reference will be made to the drawings.In various figures, identical element
It is indicated using same or similar appended drawing reference.For the sake of clarity, the various pieces in attached drawing are not necessarily to scale.
Fig. 1 shows the structural schematic diagram of gas-solid fluidized bed calcination reactor according to an embodiment of the present invention.Such as Fig. 1 institute
Show, the gas-solid fluidized bed calcination reactor, including shell, and the guide shell 2 in the shell.The shell is equipped with
Primary air inlet 11, gas outlet 12, feed inlet 13 and discharging structure 14.Wherein, the primary air inlet 11 is located at the guide shell 2
Lower part, and be connected to the guide shell 2, for the conveying high-temperature gas into the guide shell 2.The gas outlet 12 is located at described
The top of shell, for flue gas to be discharged.
The feed inlet 13 and discharging structure 14 are located at 2 peripheral side of guide shell, and the feed inlet 13 is for mentioning
For to 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 for collecting and calcining waste material being discharged.The calcining waste material refers to calcining sufficiently, and density is reduced to certain journey
The waste material of degree.The both 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 waits for that calcining materials enter institute from the feed inlet 13
It states in shell, high-temperature gas enters the guide shell 2 from the primary air inlet 11, and follows to calcining materials described described in drive
Cyclic Calcination reacts in ring channel.
Further, the shell includes conversion zone 15, and the segregation section 16 positioned at 15 upper end of conversion zone, described
Conversion zone 15 is used for the progress of Cyclic Calcination reaction, and the segregation section 16 is used to calcine the separation of waste material and flue gas.In the implementation
In example, the conversion zone 15 and segregation section 16 are respectively cylindrical shape, and the diameter of the segregation section 16 is greater than the diameter of shell.It is described
Conversion zone 15 is tubular, and ratio of height to diameter is 6:1~12:1, and the ratio between the annular space width that conversion zone 15 is surrounded with guide shell 2 is
2:1~0.5:1, preferably 1.2:1~0.5:1.The calcining waste material refers to calcining sufficiently, and density is reduced to a degree of
Waste material, the waste material can enter the segregation section 16 with flue gas, after separating with flue gas, be discharged through the discharging structure 14.As excellent
Selection of land, the segregation section 16 include the cone cylinder portion 161 positioned at its lower end, the segregation section 16 through the cone cylinder portion 161 with it is described
The upper end of shell connects.Since the diameter of the segregation section 16 is greater than the diameter of the conversion zone 15, flue gas carries waste material secretly herein
Place is diffused, and falls on the cone cylinder portion 161, discharging structure 14 is slided into through cone cylinder portion 161, and be finally discharged, after separation
Flue gas is discharged through the exhaust outlet.
It preferably, further include cyclone separator (not shown), the cyclone separator and the gas outlet 12 connect
It connects, enables to the separation of calcining materials and flue gas progress rapidly and efficiently.
The discharging structure 14 includes discharge gate 141 and the discharge groove 142 being connected to the discharge gate 141.Wherein, institute
Discharge gate 141 is stated on the outer wall of the shell, for calcining waste material to be discharged；The discharge groove 142 is set 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 being arranged axially along, the high-temperature gas in the guide shell 2
Gaseous mixture with calcining materials is entered the space between guide shell 2 and outer casing inner wall between adjacent diversion section, formed multistage
High-temperature gas circulation, can be fully calcined to material.The lower end of the guide shell 2 is equipped with tapered expansion section 21, and the taper expands
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, and bottom opening diameter and 2 diameter ratio of guide shell are 1.5~1:1.
Fig. 2-3 respectively illustrates the structural representation of the guide shell 2 of two kinds of different embodiments according to an embodiment of the present invention
Figure.In two kinds of embodiments, the number of the diversion section is three, including the first diversion section being once arranged from bottom to top
22, the second diversion section 23 and third diversion section 24.The difference is that in the embodiment shown in figure 2, the guide shell 2 is
Split type structure is monolithic construction in embodiment shown in Fig. 2.The guide shell 2 is split type structure, i.e., adjacent leads
Flow setting spaced apart between section.Wherein, between first diversion section 22 and the second diversion section 23 and the second water conservancy diversion
It is respectively formed gap between section 23 and third diversion section 24, a small amount of gas can be flowed out from the gap 25, but these gases rise
Resistance it is big, speed is small, is not enough to prevent flowing downward for particle.In the embodiment shown in fig. 3, the guide shell 2 is whole
Body is formed, and direction sets gradually 26 groups of 26 groups of the first sieve pore and the second sieve pore from bottom to top axially along, and two 26 groups of sieve pore
Respectively as the segmentation boundary between different diversion sections.26 groups of the sieve pore can be obtained through modes such as drillings.Described first to
Circumferential setting of second 26 groups of the sieve pore around the guide shell 2.Likewise, a small amount of gas can be from two sieve pores, 26 groups of streams
Out, but the resistance of these gases rising is big, and speed is small, is not enough to prevent flowing downward for particle.The height of each diversion section
Degree and diameter ratio are preferably 3:1~8:1.
The specific number of the diversion section is not limited to three, can also be to have one, two or four, even more,
Its specific number is set as needed.
The lower end of the shell is equipped with the main distributor 3 being connected to the primary air inlet 11, and the main distributor 3 is located at institute
State the lower part of guide shell 2, high-temperature gas enters the main distributor 3 through the primary air inlet 11, and through the main distributor 3 into
Enter the guide shell 2.3 diameter of main distributor and 2 diameter ratio of guide shell are preferably 1.5:1~0.5:1.The main distribution
Device 3 is specifically chosen as sieve pore disc type distributor or ring type distributor.Wherein it is not less than from the High Temperature Gas scale of construction that main distributor 3 enters
The 50% of gas gross.
Further, which further includes air inlet and the air inlet company between the grade between grade
Distributor 4 between logical grade, distributor 4 is set between adjacent diversion section between the grade.Specifically, being connected on distributor 4 between grade
There is an air inlet pipe 5, the air inlet pipe 5 extends to shell exterior, and high-temperature gas enters distributor 4 between grade through respective air inlet pipe 5, and
Enter corresponding diversion section through distributor 4 between the grade.4 diameter of distributor is preferably with 2 diameter ratio of guide shell between the grade
0.8:1~0.2:1.Distributor 4 is specifically chosen as ring type distributor between the grade.
Further, which further includes elevated bunker (not shown), the elevated bunker
It connect with the feed inlet 13, for that will be conveyed to calcining materials into the shell, and is equipped on the bottom wall of the shell
Auxiliary heat exchanging device.
Fig. 4 shows the working state figure of gas-solid fluidized bed calcination reactor according to an embodiment of the present invention.With reference to Fig. 4,
Just the use of the gas-solid fluidized bed calcination reactor in the present invention is described in detail by embodiment 1-5 below.
Gas-solid fluidized bed calcination reactor is recycled in 1: two section of embodiment
Specific structure parameter is as follows: in the embodiment, guide shell 2 divides for two diversion sections, 15 internal diameter 125mm of conversion zone,
Height 750mm, segregation section 16 internal diameter 175mm, height 250mm；2 diameter 62mm of guide shell, is divided to two sections, and paragraph 1 is high from top to bottom
350mm, the 2nd section of high 280mm take the mode of more arrangements, gap 40mm, 2 under shed diameter 80mm of guide shell between two, cone
Spend 1:2；Guide shell 2 is apart from outer casing bottom 30mm.Main distributor 3 is sieving-disc type distributor, diameter 80mm；Distributor 4 between grade
For ring type distributor, diameter 40mm.
With calcium carbonate (10 microns of average grain diameter) for model solid particle, starting fluidizing gas velocity (mark condition) is determined
0.054m/s；It is 0.2m/s in gas empty bed speed, the apparent above-mentioned rate of solid particle is 1.2m/s in guide shell 2, declines segment table
Sight fall rate is 0.4m/s.
2: three sections of internal circulating fluidized bed calcination reactors of embodiment
Specific structure parameter is as follows: conversion zone 15 internal diameter 125mm, height 950mm, 16 internal diameter 175mm of segregation section, height
220mm；2 diameter 56mm of guide shell, takes and opens between section by points 3 sections, paragraph 1 high 320mm, the 2nd section of high 280mm, the 3rd section of high 260mm
The mode in hole, the aperture gross area is 16cm2, total a height of 50mm shared by two sections of apertures between two sections；2 under shed diameter of guide shell
80mm, taper 1:2.Guide shell 2 is apart from outer casing bottom 30mm.Main distributor 3 is sieving-disc type distributor, diameter 80mm；Between grade
Distributor 4 is ring type distributor, diameter 35mm.
With calcium carbonate (10 microns of average grain diameter) for model solid particle, it is 0.2m/s in gas empty bed speed, consolidates in guide shell 2
The apparent above-mentioned rate of body particle is 1.4m/s, and the apparent fall rate of descending branch is 0.5m/s.
Embodiment 3: one hydrated magnesium chloride of calcining prepares 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, is continuously added into reactor by elevated bunker；Reactor
Atmospheric operation, total ventilatory capacity (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 a grade.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 segment, 276 DEG C of the 2nd section of mean temperature；The matter of basic magnesium chloride in products obtained therefrom
Measuring score is 78%.
Embodiment 4: one hydrated magnesium chloride of calcining prepares magnesia
Using the reactor in embodiment 2, high-temperature gas is hot-air, and temperature is 500 DEG C,
MgCl2H2O uses MgCl26H2O to prepare (crystallization water mass fraction for 19.2%) in advance, passes through high-order material
Slot is continuously added into reactor；Reactor atmospheric operation, total ventilatory capacity (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 grade, remaining is passed through from distributor 4 between the 2nd grade,
Average bed density is 595kg/m3 in reactor；Feed rate is 8.2kg/h.Reactor first segment (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 distribution of 1 calcination product of table
| Component | MgO | Mg(OH)Cl | MgCl2 | H2O |
| Mass fraction (%) | 64 | 21 | 11 | 4 |
Embodiment 5: calcining sodium bicarbonate prepares sodium carbonate
Using the reactor in embodiment 1, high-temperature gas is hot-air, and temperature is 340 DEG C；Principle sodium bicarbonate (contains
The water of mass fraction 12%) reactor is continuously added by elevated bunker；Calcination reactor atmospheric operation, total ventilatory capacity (mark condition)
For 1200L/h, wherein 70% gas is passed through from the main distributor 3 of bottom, remaining is passed through from distributor 4 between 1 grade.Reactor
Interior average bed density is 420kg/m3；Feed rate is 5.4kg/h.Operation is when reaching stable state, reactor paragraph 1 (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 grades, and high-temperature gas is each led into, and multiple diversion sections are set
It sets, reaction mixture gas body is constantly discharged from the gap 25 between sieve pore 26 or adjacent guide section, recycles again, forms one kind
The gas-solid fluidized bed calcination reactor of circulation in multistage.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 is efficiently, low energy consumption.It is compared with traditional recirculating fluidized bed calciner plant, internal circulating fluidized bed of the invention is followed
Ring rate is fast, and descending branch is still located inside reactor, and reaction is still carrying out, and realizes cascade simultaneously, is effectively utilized mass transfer
Driving force of heat transfer.
It should be noted that herein, relational terms such as first and second and the like are used merely to a reality
Body or operation are distinguished with another entity or operation, are deposited without necessarily requiring or implying between these entities or operation
In any actual relationship or order or sequence.Moreover, the terms "include", "comprise" or its any other variant are intended to
Non-exclusive inclusion, so that the process, method, article or equipment including a series of elements is not only wanted including those
Element, but also including other elements that are not explicitly listed, or further include for this process, method, article or equipment
Intrinsic element.In the absence of more restrictions, the element limited by sentence "including a ...", it is not excluded that
There is also other identical elements in process, method, article or equipment including the element.
Finally, it should be noted that obviously, the above embodiment is merely an example for clearly illustrating the present invention, and simultaneously
The non-restriction to embodiment.For those of ordinary skill in the art, it can also do on the basis of the above description
Other various forms of variations or variation out.There is no necessity and possibility to exhaust all the enbodiments.And thus drawn
The obvious changes or variations that Shen goes out are still in the protection scope of this invention.
Claims (14)
1. a kind of gas-solid fluidized bed calcination reactor, which is characterized in that including shell, and the water conservancy diversion in the shell
Cylinder,
The shell is equipped with primary air inlet, gas outlet, feed inlet and discharging structure, wherein
The primary air inlet is located at the lower part of the guide shell, is used for the conveying high-temperature gas into the guide shell,
The gas outlet is located at the top of the shell, for flue gas to be discharged,
The feed inlet and discharging structure are located at the guide shell peripheral side, and the feed inlet is for providing to calcined material
Material, the discharging structure are used to collecting and being discharged calcining waste material,
The both 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, enters in the shell to calcining materials from the feed inlet, high temperature
Gas enters the guide shell from the primary air inlet, and drive it is described to calcining materials in the circulation canal Cyclic Calcination
Reaction；
The guide shell includes the multiple diversion sections being arranged axially along, high-temperature gas and calcining materials in the guide shell
Gaseous mixture entered space between guide shell and outer casing inner wall between adjacent diversion section, form multistage high-temperature gas and follow
Ring；
The shell includes conversion zone, and the segregation section positioned at the conversion zone upper end, and the conversion zone is used for Cyclic Calcination
The progress of reaction, the segregation section are used to calcine the separation of waste material and flue gas, and the segregation section includes the cone cylinder positioned at its lower end
Portion, the segregation section are connect through the cone cylinder portion with the upper end of the shell；
The lower end of the guide shell is equipped with tapered expansion section, and the tapered expansion section covers main distributor, comes from institute for collecting
State the high-temperature gas of main distributor.
2. gas-solid fluidized bed calcination reactor according to claim 1, which is characterized in that the conversion zone is tubular,
Ratio of height to diameter is 6:1 ~ 12:1.
3. gas-solid fluidized bed calcination reactor according to claim 2, which is characterized in that conversion zone was surrounded with guide shell
The ratio between annular space width is 1.2:1 ~ 0.5:1.
4. gas-solid fluidized bed calcination reactor according to claim 1, which is characterized in that the discharging structure includes discharge
Mouth and the discharge groove being connected to the discharge gate, wherein
The discharge gate is set on the outer wall of the shell, for calcining waste material to be discharged,
The discharge groove is set on the outer casing inner wall, for collecting calcining waste material and being transported to the discharge gate.
5. gas-solid fluidized bed calcination reactor according to claim 1, which is characterized in that the lower end of the shell be equipped with
The main distributor of the primary air inlet connection, the main distributor are located at the lower part of the guide shell, and high-temperature gas is through institute
Primary air inlet is stated into the main distributor, and enter the guide shell through the main distributor；
It further include distributor between air inlet and the grade that air inlet is connected between the grade between grade, distributor is set to phase between the grade
Between adjacent diversion section, high-temperature gas enters corresponding diversion section through distributor between the grade.
6. gas-solid fluidized bed calcination reactor according to claim 5, which is characterized in that the height of each diversion section
It is 3:1 ~ 8:1 with diameter ratio.
7. gas-solid fluidized bed calcination reactor according to claim 5, which is characterized in that the main distributor is sieving-disc type
Distributor.
8. gas-solid fluidized bed calcination reactor according to claim 5, which is characterized in that the main distributor diameter with lead
Flow cartridge diameter ratio is 1.5:1 ~ 0.5:1.
9. gas-solid fluidized bed calcination reactor according to claim 5, which is characterized in that distributor is ring type between the grade
Distributor.
10. gas-solid fluidized bed calcination reactor according to claim 5, which is characterized in that distributor diameter between the grade
It is 0.8:1 ~ 0.2:1 with the ratio between draft tube diameter.
11. gas-solid fluidized bed calcination reactor as claimed in any of claims 1 to 10, which is characterized in that described
Tapered expansion section taper is 1:1 ~ 1:4.
12. gas-solid fluidized bed calcination reactor as claimed in any of claims 1 to 10, which is characterized in that described
The ratio between tapered expansion section bottom opening diameter and draft tube diameter are 1.5 ~ 1:1.
13. gas-solid fluidized bed calcination reactor according to claim 1, which is characterized in that it further include elevated bunker, it is described
Elevated bunker is connect with the feed inlet, for that will convey to calcining materials into the shell.
14. gas-solid fluidized bed calcination reactor according to claim 1, which is characterized in that on the bottom wall of the shell
Equipped with auxiliary heat exchanging device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610818788.6A CN106215816B (en) | 2016-09-12 | 2016-09-12 | Gas-solid fluidized bed calcination reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610818788.6A CN106215816B (en) | 2016-09-12 | 2016-09-12 | Gas-solid fluidized bed calcination reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106215816A CN106215816A (en) | 2016-12-14 |
| CN106215816B true CN106215816B (en) | 2019-05-03 |
Family
ID=58074925
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610818788.6A Active CN106215816B (en) | 2016-09-12 | 2016-09-12 | Gas-solid fluidized bed calcination reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106215816B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109331746B (en) * | 2018-09-28 | 2021-11-19 | 大连理工大学 | Novel solid particle thermochemical reaction device and method |
| CN110496573A (en) * | 2019-09-11 | 2019-11-26 | 哈尔滨理工大学 | A kind of dock fluidized-bed reactor |
| CN114797726A (en) * | 2022-04-29 | 2022-07-29 | 浙江长城搅拌设备股份有限公司 | Preparation device for precursor of lithium ion battery anode material |
| CN114963739A (en) * | 2022-05-23 | 2022-08-30 | 哈尔滨理工大学 | Pulsating airflow is spouted air current spouted bed drying device in coordination |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2581670A (en) * | 1947-07-19 | 1952-01-08 | Universal Oil Prod Co | Regeneration of fluidized catalyst |
| US2885272A (en) * | 1953-10-07 | 1959-05-05 | Exxon Research Engineering Co | Apparatus for fluid bed coking of heavy oils |
| US5117770A (en) * | 1990-01-29 | 1992-06-02 | Tampella Power Oy | Combustion unit |
| CN1959207A (en) * | 2005-11-03 | 2007-05-09 | 中国石油大学(北京) | Method for burning petroleum coke or gasified remained coke, and inner mixed type combustion equipment |
| CN101259398A (en) * | 2008-03-21 | 2008-09-10 | 中国石油大学(北京) | Device for improving pipe and gas-solid circumfluence bed coupling reaction |
| CN101274245A (en) * | 2007-03-28 | 2008-10-01 | 中国石油大学(北京) | Annular space air-lift gas-solid loop flow reactor |
| CN102166501A (en) * | 2011-03-04 | 2011-08-31 | 清华大学 | Airlift-jet multi-stage loop reactor |
| CN201971790U (en) * | 2011-01-24 | 2011-09-14 | 中国石油化工股份有限公司 | Inward flow slurry bed reactor |
| CN105400544A (en) * | 2015-12-03 | 2016-03-16 | 天津如有科技有限公司 | Method for preparing alkylate oil by using multistage circulating flow reactor |
| CN206199225U (en) * | 2016-09-12 | 2017-05-31 | 原初科技（北京）有限公司 | Gas-solid fluidized bed calcination reactor |
-
2016
- 2016-09-12 CN CN201610818788.6A patent/CN106215816B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2581670A (en) * | 1947-07-19 | 1952-01-08 | Universal Oil Prod Co | Regeneration of fluidized catalyst |
| US2885272A (en) * | 1953-10-07 | 1959-05-05 | Exxon Research Engineering Co | Apparatus for fluid bed coking of heavy oils |
| US5117770A (en) * | 1990-01-29 | 1992-06-02 | Tampella Power Oy | Combustion unit |
| CN1959207A (en) * | 2005-11-03 | 2007-05-09 | 中国石油大学(北京) | Method for burning petroleum coke or gasified remained coke, and inner mixed type combustion equipment |
| CN101274245A (en) * | 2007-03-28 | 2008-10-01 | 中国石油大学(北京) | Annular space air-lift gas-solid loop flow reactor |
| CN101259398A (en) * | 2008-03-21 | 2008-09-10 | 中国石油大学(北京) | Device for improving pipe and gas-solid circumfluence bed coupling reaction |
| CN201971790U (en) * | 2011-01-24 | 2011-09-14 | 中国石油化工股份有限公司 | Inward flow slurry bed reactor |
| CN102166501A (en) * | 2011-03-04 | 2011-08-31 | 清华大学 | Airlift-jet multi-stage loop reactor |
| CN105400544A (en) * | 2015-12-03 | 2016-03-16 | 天津如有科技有限公司 | Method for preparing alkylate oil by using multistage circulating flow reactor |
| CN206199225U (en) * | 2016-09-12 | 2017-05-31 | 原初科技（北京）有限公司 | Gas-solid fluidized bed calcination reactor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106215816A (en) | 2016-12-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106215816B (en) | Gas-solid fluidized bed calcination reactor | |
| CN102875036B (en) | Heat storage type lime rotary kiln | |
| CN102502744B (en) | Slagging-free type and multilevel differential temperature fluidized roasting system for crystallized aluminum salt and method thereof | |
| CN87103862A (en) | The method of secondary cycle fluidized bed reactor and its operating | |
| CN103373822B (en) | Light calcined magnesia powder calcination device | |
| CN1016889B (en) | Fluid-bed combustion reactor and method for operation of such fluid-bed combustion reactor | |
| US3578798A (en) | Cyclonic fluid bed reactor | |
| CN103836948B (en) | A kind of fluidizing reactor of high-carbon molybdenum-nickel ore and system | |
| CN106568331A (en) | Large suspension kiln and production process thereof | |
| CN104803618A (en) | Annular lime shaft kiln | |
| CN205535775U (en) | Hood for circulating fluidized bed | |
| WO2012126389A1 (en) | External-circulation decomposition reactor with high solid-gas ratio using horizontal cyclone cylinder | |
| JPH02243545A (en) | Method and device for manufacture of cement clinker from raw material metal | |
| CN206199225U (en) | Gas-solid fluidized bed calcination reactor | |
| CN1039593C (en) | Calcining system and technique for fluidized bed-mobile bed mixed reactor | |
| CN103318963A (en) | Method for preparing fullerene-structured nano-WS2 and special fluidized bed reactor thereof | |
| US4318692A (en) | Helical duct gas/meal separator | |
| CN203474652U (en) | Heat accumulating type lime rotary kiln | |
| CN204550403U (en) | Annular lime shaft kiln | |
| CN104628275A (en) | Phosphogypsum calcining system and phosphogypsum calcining process | |
| CN212504609U (en) | Device for preparing light-burned magnesium oxide through suspension calcination | |
| CN210127193U (en) | Powdery lime calcining, decomposing and preparing system | |
| CN100368297C (en) | Device for preparing aluminum oxide self-efflorescence grog by fusion method and preparation method thereof | |
| CN208562167U (en) | A kind of light-burned MgO suspension kiln coproduction Mg (OH)2Process units | |
| CN208886756U (en) | A kind of circulating fluid bed reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20200115 Address after: Room 5032, 5th floor, Building No. 8, Beichen East Road, Chaoyang District, Beijing Patentee after: YUANCHU TECHNOLOGY (BEIJING) Co.,Ltd. Address before: Room 5032, floor 5, building 3, No. 8, Beichen East Road, Chaoyang District, Beijing Patentee before: Ding Haichuan Effective date of registration: 20200115 Address after: Room 5032, 5th floor, Building No. 8, Beichen East Road, Chaoyang District, Beijing Patentee after: Ding Haichuan Address before: 100085, No. 5, 526 floor, No. 23 Anning East Road, Beijing, Haidian District Co-patentee before: Tsinghua University Patentee before: YUANCHU TECHNOLOGY (BEIJING) Co.,Ltd. |