CN107879365A - A kind of system and method that aluminum oxide is produced using desiliconization flyash sintering process - Google Patents
A kind of system and method that aluminum oxide is produced using desiliconization flyash sintering process Download PDFInfo
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- CN107879365A CN107879365A CN201711251164.1A CN201711251164A CN107879365A CN 107879365 A CN107879365 A CN 107879365A CN 201711251164 A CN201711251164 A CN 201711251164A CN 107879365 A CN107879365 A CN 107879365A
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- desiliconization
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
- C01F7/08—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals with sodium carbonate, e.g. sinter processes
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
- C01F7/14—Aluminium oxide or hydroxide from alkali metal aluminates
- C01F7/141—Aluminium oxide or hydroxide from alkali metal aluminates from aqueous aluminate solutions by neutralisation with an acidic agent
- C01F7/142—Aluminium oxide or hydroxide from alkali metal aluminates from aqueous aluminate solutions by neutralisation with an acidic agent with carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/44—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water
- C01F7/441—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water by calcination
- C01F7/444—Apparatus therefor
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- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a kind of system that aluminum oxide is produced using desiliconization flyash sintering process, include desiliconization flyash sintering mechanism, aluminium hydroxide extraction element and calciner, desiliconization flyash sintering mechanism includes the first ball mill, feed bin, half shower furnace, cooler, the second ball mill and conveying mechanism, the system that aluminum oxide is produced using desiliconization flyash sintering process not only realizes low energy consumption, further improves productivity ratio.The invention also discloses a kind of method that aluminum oxide is produced using desiliconization flyash sintering process.
Description
Technical field
The present invention relates to pyro metallurgical plant technical field, more particularly to one kind to utilize desiliconization flyash sintering process production oxygen
Change the system and method for aluminium.
Background technology
The method for extracting aluminum oxide from ore at present mainly has：Soda lime sintering process, Bayer-sintering combination method etc..Alkali
Lime sinter process generally use tradition rotary kiln, powdery flyash after rotary kiln sintered turn into bulk, follow-up comminution energy conssumption compared with
Greatly；And the clinker in rotary kiln sinters in block roll, the defects of being easily caused sintering degree difference inside and outside clinker block.Due to passing
The These characteristics of system rotary kiln cause existing sintering process power consumption high and yielded poorly, and limit sintering process production to a certain extent
The development of aluminum oxide.
Therefore, how to improve reduces energy consumption, improves productivity ratio as sintering circuit technical problem urgently to be resolved hurrily.
The content of the invention
The technical problem to be solved in the present invention is to provide a kind of is using what desiliconization flyash sintering process produced aluminum oxide
System and method.
According to a kind of system that aluminum oxide is produced using desiliconization flyash sintering process of the present invention, burnt comprising desiliconization flyash
Mechanism, aluminium hydroxide extraction element and calciner are tied, desiliconization flyash sintering mechanism includes the first ball mill, feed bin, partly hanged
Floating stove, cooler, the second ball mill and conveying mechanism, wherein,
Raw material is mixed ball processed by the first ball mill, and obtained raw material ball is sent into feed bin storage；
The activity that half shower furnace includes body of heater and is arranged in body of heater stops platform, and body of heater is included and is from top to bottom sequentially communicated
Preheating chamber, combustion chamber and clinker area, preheating chamber and clinker are to be connected respectively by the first flue and the second flue with external environment
It is logical；
Cooler is connected with the discharging opening of half shower furnace；
Second ball mill carries out wet-milling dissolution to the material after sintering；
Conveying mechanism includes the helical feed of the conveyer belt for connecting the first ball mill and feed bin, connection feed bin and half shower furnace
Machine and the tray conveyer of connection cooler and the second ball mill.
Further, desiliconization flyash sintering mechanism includes screening machine and kibbler roll, wherein, the material warp after cooling
Screening machine is sieved, and coarse fodder, which enters after roll crushing crusher machine, to be entered the second ball mill and carry out wet-milling dissolution, and fines is directly entered the
Two ball mills carry out wet-milling dissolution.
Further, aluminium hydroxide extraction element includes the dissolution subsider flowed successively through for stripping slurry, clear liquid groove, pipe
Road desiliconization device, leaf filter, desiliconization subsider, multiple carbon divide groove and horizontal table filter.
Further, combustion chamber is in circular groove shape, and the first burner and the second burner are provided with sidewall of combustion chamber.
Further, activity stops platform and included and closes on the first activity of the first burner setting and stop platform and close on the
The second activity that two burners are set stops platform, and the first activity stop platform and the second activity leave second between stopping platform
Material dropping channel, track is provided with the side wall of combustion chamber, the first burner and the second burner independent can exist along track
It is both vertically and horizontally upper to move.
According to a kind of method that aluminum oxide is produced using desiliconization flyash sintering process of the present invention, the requirement of method usage right
Any one of 1-5 system, method comprise the steps of：
Step 1：Mass ratio is met into NaO2：Al2O3=0.9~0.98, CaO：SiO2=1.9~2.1 desiliconization fine coal
Ash and lime stone, sodium carbonate add the first ball mill, and binding agent is added in a manner of spray, 1mm~3mm raw material ball is made,
And raw material ball is sent into feed bin storage by conveyer belt；
Step 2：Raw material ball is sent into by temperature of half shower furnace at 1200 DEG C~1400 DEG C by feed bin by conveying worm
Under be sintered；
Step 3：Material after sintering is cooled to less than 150 DEG C into cooler；
Step 4：Wet-milling dissolution is carried out to the material after cooling using the second ball mill；
Step 5：The subsider of stripping slurry warp is settled, gained clear liquid flows into the storage of clear liquid groove, and the clear liquid of storage is successively
Filtered into the one section of desiliconization of pipeline desiliconization device, through leaf filter and enter the secondary desiliconization of desiliconization subsider, obtain the aluminium after desiliconization
Acid sodium solution；
Step 6：Sodium aluminate solution after desiliconization successively flows through multiple carbon and divides groove to be reacted, and obtains containing aluminium hydroxide
Slurry, each of which carbon divides trench bottom to be passed through CO2Gas；
Step 7：Slurry containing aluminium hydroxide is filtered into horizontal table filter, obtains aluminium hydroxide；
Step 8：Aluminium hydroxide is calcined to obtain aluminum oxide through gaseous suspension stove.
Further, step 2 includes：Raw material ball is entered by half shower furnace top, in activity after the uniform preheating in preheated room
Short stay on platform is stopped, is heated by burner and carries out high temperature sintering reaction.
Further, step 2 includes：Position by adjusting burner controls sintering region；By adjusting the length of flame
Control sintering temperature.
Further, step 4 includes：The screened machine screening of material after cooling, after coarse fodder enters roll crushing crusher machine
Wet-milling dissolution is carried out into the second ball mill, fines is directly entered the second ball mill and carries out wet-milling dissolution.
Further, step 5 includes：The slurry of dissolution subsider bottom is put into hot wash in washing settling groove to sink
Drop, gained precipitation are discharged after filter press press filtration obtains calcium silicate slag；Step 7 includes：The mother liquid obtained sodium carbonate that is back to is filtered to steam
Hair station is evaporated, dispensing again after the crystallization gained filtered drying of sodium carbonate.
Due to being used in upper technical scheme, the present invention has advantages below compared with prior art：
(1) using the technique of dry mixing sintering, avoid energy consumption that wet laid furnishes evaporation moisture, preheating material bring compared with
The shortcomings that high；
(2) in sintering process and mixed combining method, slurry is calcined in rotary kiln with rolling condition, and material rolls in block, this
Technique uses dry method blanking, and bulk material preheats in flue gas in dropping process, thorough in burner hearth high-temperature region reaction-sintered ripe material
The shortcomings that burning caused by bottom avoids the mass transfer rate difference of different size lump material and raw burn.
(3) half shower furnaces take double burner to configure, it is ensured that have a larger thermal field.
(4) below the burner front end of half shower furnace, powdered coal ash blanking point, it is flat that a material activity stop is installed
Platform, powdered coal ash falls to stay for some time on platform drops into down cooler again, and raw burn, the ratio of overburnt clinker occurs in reduction
Rate.
(5) half shower furnaces belong to static furnace, more easy to maintenance than rotary kiln general at present, and investment construction cost is low.
Brief description of the drawings
The above-mentioned and/or additional aspect and advantage of the present invention will become from the following description of the accompanying drawings of embodiments
Obviously and it is readily appreciated that, wherein：
Fig. 1 is the schematic diagram according to the example system of the present invention；
Fig. 2 is the schematic diagram according to exemplary half shower furnace of the present invention；
Fig. 3 is the sectional view of the shower furnace of the sintering of desiliconization flyash shown in Fig. 2 half；
Fig. 4 is the flow chart according to the illustrative methods of the present invention.
Description of reference numerals：
1 preheating chamber, 11 first feeding mouths, 12 second feeding mouths, 2 combustion chambers, 21 first burners, 22 second burners, 3
Clinker room, 31 discharging openings, 41 first activities stop platforms, and 42 second activities stop platforms, 51 first material dropping channels, and 52 the
Two material dropping channels, 6 first flues, 7 second flues, 8 coolers.
Embodiment
Embodiments of the invention are described below in detail, the example of embodiment is shown in the drawings, wherein identical from beginning to end
Or similar label represents same or similar element or the element with same or like function.Retouched below with reference to accompanying drawing
The embodiment stated is exemplary, is only used for explaining the present invention, and is not considered as limiting the invention.
As shown in figure 1, the example system that aluminum oxide is produced using desiliconization flyash sintering process according to the present invention is overall
Include desiliconization flyash sintering mechanism, aluminium hydroxide extraction element and the calciner being sequentially connected.
Specifically, flyash sintering mechanism of derailing includes the first ball mill, conveyer belt, feed bin, conveying worm, half suspension
Stove, cooler, tray conveyer, screening machine, kibbler roll and the second ball mill.Wherein, the first ball mill is used for original
Material mixes and 1mm-3mm bead is made, and bead is sent into feed bin by conveyer belt and stored；Small ball warp spiral transferring in feed bin
Send machine to be sent into half shower furnace to be sintered, burned pelletizing is cooled to through being connected to the single cylinder cooling machine of half shower furnace discharging opening
Less than 150 DEG C；The screened machine screening of pelletizing after cooling, gained fines are directly entered the second ball mill and carry out wet-milling dissolution, slightly
Material then enters back into the second ball mill wet-milling dissolution after roll crushing crusher machine, obtains dissolution slurry.
Aluminium hydroxide extraction element include the dissolution subsider flowed successively through for stripping slurry, clear liquid groove, pipeline desiliconization device,
Leaf filter, desiliconization subsider, multiple carbon divide groove and horizontal table filter.Dissolution slurry settles through dissolution subsider, and clear liquid enters
The desiliconization system being made up of clear liquid groove, pipeline desiliconization device, leaf filter, desiliconization liquid subsider obtains desiliconization liquid, and pug successively passes through
Multiple washing settling grooves carry out hot wash sedimentation separation and go out calcium silicate slag slurry, then extrude the low calcium silicate slag of water content by filter press
And calcium silicate slag is discharged；Desiliconization liquid is passed through CO through multiple by bottom2The carbon of gas decomposites aluminium hydroxide and hydroxide after dividing groove
Sodium, wherein, it is that station is evaporated that the mother liquor containing sodium hydroxide, which returns to evaporation, is matched somebody with somebody again after the crystallization gained filtered drying of sodium carbonate
Material, the slurry of the aluminium hydroxide output aluminium hydroxide after horizontal table filter.
The fired device roasting of gained aluminium hydroxide can obtain aluminum oxide.In an embodiment of the present invention, calciner
From gaseous suspension stove, those skilled in the art can also select other calciners according to needs of production.
The present invention realizes the sintering of flyash using the traditional rotary kiln of half shower furnace replacement.As shown in Figures 2 and 3, according to
The activity for including body of heater according to half shower furnace of the invention and being arranged in body of heater stops platform.Specifically, body of heater is from top to bottom successively
It is provided with preheating chamber 1, combustion chamber 2 and clinker room 3.Powdered coal ash from top to bottom does the movement of falling object since preheating chamber 1,
Make a brief stay by being stopped during combustion chamber 2 in activity on platform, fallen into after the completion of reaction fully to be sintered in clinker room 3.It is excellent
Selection of land, it can realize that the activity stops platform in certain altitude by stopping the modes such as platform lower installation hydraulic means in activity
In the range of lifting, with facilitate optionally determine sintering region.
Preheating chamber 1 is symmetrically arranged with the first feeding mouth 11 and the second feeding mouth 12 in the side wall at top, and two enter
Material mouth each with such as conveying worm as conveying device be connected, and the He of the first feeding mouth 11 is passed through by conveying device respectively
Powdered coal ash to be sintered is sent into half shower furnace by the second feeding mouth 12.It is pre- that connection is additionally provided with the side wall of preheating chamber 1
Hot cell 1 and the first flue 6 of external environment condition.First flue 6 is preferably sunk type flue, and operator can pass through control first
The butterfly valve of the end of flue 6 controls the flue gas flow of the flue, so as to control the waste heat speed of powdered coal ash.Preferably, this
The junction of one flue 6 and preheating chamber 1 is arranged to be less than feeding mouth 11.The height of first flue 6 is less than feeding mouth 11, a side
Face can prevent flue gas from being escaped from feeding mouth, on the other hand damage pan feeding conveyer prevented also from flue gas.In the reality of the present invention
Apply in example, preheating chamber 1 can be arranged to diameter 3m-4m, more than height 20m cylinder, and those skilled in the art also can foundation
Actual production scale designs the diameter and height of preheating chamber 1.
Overall positioned at the combustion chamber 2 of the lower section of preheating chamber 1 is in circular groove shape, i.e. the diameter of combustion chamber 2 is more than preheating chamber 1 and clinker
The diameter of room 3, combustion chamber 2 include preheating chamber-combustion chamber transition region that diameter gradually increases, the stable region of constant diameter and straight
The combustion chamber that footpath is gradually reduced-clinker room transition region.The first combustion has been arranged relative to each other in the side wall of the steady component of combustion chamber 2
The burner 22 of burner 21 and second, the two is each in the horizontal direction towards the central area jet flames of combustion chamber 2, so that burner hearth
Inside has thermal-flame eddy flow, it is ensured that has 1200 DEG C -1400 DEG C of high-temperature region in combustion chamber 2.Preferably, can be in combustion chamber
Guide rail is set in 2 side wall, so that the first burner 21 and the second burner 22 can be independently along tracks in vertical direction
Moved in upper and horizontal direction.
In an embodiment of the present invention, the first burner 21 and the second burner 22 can respectively along track be moved horizontally to
Body of heater tangent line makes an angle alpha the position for 30 ° -90 °, in favor of the generation of burner hearth internal high temperature flame vortex.When the first burning
When the solid accumulation that the activity of the front end of 21 and second burner of device 22 is stopped on platform is excessive, the first burner 21 and the can be reduced
The height of two burners 22, the material that activity is stopped on platform is set to drop down onto clinker room 3.Preferably, the first burner 21 and second
Burner 22 can be coal burner, and operator can control the length of flame by adjusting the flow of coal dust, so as to adjust
Temperature in combustion chamber 2.The diameter of the stable region of combustion chamber 2 can be arranged to 20m, and the height at its maximum height can be arranged to
6m, those skilled in the art also can be according to the diameters and height of actual production scale designed combustion room 2.
The discharging opening 31 of the lower end of clinker room 3 is connected with cooler 8, and the clinker for falling into clinker room 3 is entered by discharging opening 31
In cooler 8, the rotation through cooler cools to less than 150 DEG C.In addition, clinker area 3 can also be set and external environment
Second flue 7 of connection, second flue 7 are preferably horizontal flue, and operator can be by controlling the end of the second flue 7
Butterfly valve controls the flue gas flow of the flue, so as to control the falling speed of clinker.In an embodiment of the present invention, clinker room 3 can
To be arranged to diameter 5m, height 5m cylinder, those skilled in the art also can design clinker room 3 according to actual production scale
Diameter and height.
Activity stops platform and is made up of the 41 and second movable platform 42 that stops of the first activity stop platform separated each other.Its
In, the first activity stops platform 41 and fallen positioned at the first burner front end 21 with the powdered coal ash entered by the first feeding mouth 11
The lower section of point；Similarly, the second activity stops platform 42 positioned at the second burner 42 and the fine coal entered by the second feeding mouth 12
The lower section in grey raw material setting point.As shown in Fig. 2 the surrounding of the activity stop platform 42 of platform 41 and second is stopped around the first activity
The first material dropping channel 51 of annular is left, is left between the activity stop platform 42 of the first activity stop platform 41 and second straight
The second material dropping channel 52 of line style.Powdered coal ash after preheating falls to the first activity and stops the work of platform 41 and second
It can be made a brief stay after on dynamic stop platform 42 in the high-temperature region of combustion chamber 3, so that sintering reaction is fully carried out, treat solid accumulation
Clinker room 3 will be fallen to after to certain altitude through first material dropping channel 51 or second material dropping channel 52 automatically.
Powdered coal ash is sent into half shower furnace by feeding mouth 11, and powdered coal ash is in dropping process in preheating chamber 1
Uniformly preheating.Then, activity is dropped down onto under powdered coal ash to stop on platform, and 1200 DEG C of -1400 DEG C of progress are heated to by burner
High temperature sintering reacts, wherein, the position by adjusting burner controls sintering region, by adjusting flame length control sintering temperature
Degree.After flyash falls into high-temperature area, the Al among particle2O3With Na2O, CaO and SiO2Pyroreaction is into sodium aluminate and silicic acid
Dicalcium.Sintering reaction product under the continuous accumulation of powdered coal ash because dropping down onto clinker room 3.
As shown in figure 4, according to the present invention using desiliconization flyash sintering process produce aluminum oxide method totally include with
Lower step：
Step 1：Desiliconization flyash and lime stone, sodium carbonate are added into the first ball mill, bonding is added in a manner of spray
Agent, 1mm~3mm raw material ball is made, and raw material ball is sent into feed bin storage by conveyer belt.Wherein, for the powder of different sources
Gap be present in the alumina content of coal ash, for example, the alumina content of Inner Mongol aluminous fly-ash is in 35~40%, and not
The active calcium ion content of comprovincial lime stone also differs, and therefore, each raw material proportioning only needs to meet mass ratio NaO2：Al2O3=
0.9~0.98, CaO：SiO2=1.9~2.1.Wherein, Al2O3From flyash, CaO comes from lime stone, and NaO comes from
Sodium carbonate, SiO2Come from flyash.
Step 2：Raw material ball is sent into by temperature of half shower furnace at 1200 DEG C~1400 DEG C by feed bin by conveying worm
Under be sintered, wherein, raw material ball is entered by half shower furnace top, preheated room uniformly preheating after activity stop platform on it is short
Pause is stayed, and is heated by burner and is carried out high temperature sintering reaction, and sintering zone is controlled by adjusting the position of burner in sintering process
Domain；By adjusting flame length control sintering temperature.
Step 3：Material after sintering is cooled to less than 150 DEG C into cooler.
Step 4：The screened machine screening of material after cooling, coarse fodder enter the second ball milling after entering roll crushing crusher machine
Machine carries out wet-milling dissolution, and fines is directly entered the second ball mill and carries out wet-milling dissolution.
Step 5：The subsider of stripping slurry warp is settled, gained clear liquid flows into the storage of clear liquid groove, and the clear liquid of storage is successively
Filtered into the one section of desiliconization of pipeline desiliconization device, through leaf filter and enter the secondary desiliconization of desiliconization subsider, obtain the aluminium after desiliconization
Acid sodium solution；The slurry of dissolution subsider bottom is put into hot wash in washing settling groove to settle, gained is precipitated through filter press
Press filtration is discharged after obtaining calcium silicate slag.
Step 6：Sodium aluminate solution after desiliconization successively flows through multiple carbon and divides groove to be reacted, and obtains containing aluminium hydroxide
Slurry, each of which carbon divides trench bottom to be passed through CO2Gas.
Step 7：Slurry containing aluminium hydroxide is filtered into horizontal table filter, obtains aluminium hydroxide；Filtering gained
Mother liquor is back to sodium carbonate evaporation station and is evaporated, dispensing again after the crystallization gained filtered drying of sodium carbonate.
Step 8：Aluminium hydroxide is calcined to obtain aluminum oxide through gaseous suspension stove.
Raw material proportioning and the sintering temperature that the embodiment of aluminium hydroxide is produced by the above method are as shown in table 1：
Table 1
| NaO2：Al2O3 | CaO：SiO2 | Sintering temperature (DEG C) | |
| Embodiment 1 | 0.95 | 2.1 | 1300 |
| Embodiment 2 | 0.9 | 1.9 | 1200 |
| Embodiment 3 | 0.98 | 2 | 1400 |
The reason for conventional sintering method and high mixed combining method material breakage essentially consist in preheating and maintain material to 1300 DEG C~
1400 DEG C, and the method for the present invention does not have 30% moisture of material among sintering process and mixed combining method, and material sinters in bulk, and
It is not caking, effectively reduces energy consumption, has saved production cost.
Although an embodiment of the present invention has been shown and described, it will be understood by those skilled in the art that：Not
In the case of departing from the principle and objective of the present invention a variety of change, modification, replacement and modification can be carried out to these embodiments, this
The scope of invention is limited by claim and its equivalent.
Claims (10)
1. a kind of system that aluminum oxide is produced using desiliconization flyash sintering process, it is characterised in that sintered comprising desiliconization flyash
Mechanism, aluminium hydroxide extraction element and calciner, the desiliconization flyash sintering mechanism include the first ball mill, feed bin, half
Shower furnace, cooler, the second ball mill and conveying mechanism, wherein,
Raw material is mixed ball processed by first ball mill, and obtained raw material ball is sent into the feed bin and stored；
The activity that half shower furnace includes body of heater and is arranged in the body of heater stops platform, and the body of heater includes from top to bottom
Preheating chamber, combustion chamber and the clinker area being sequentially communicated, the preheating chamber and the clinker are respectively by the first flue and second
Flue connects with external environment；
The cooler is connected with the discharging opening of half shower furnace；
Second ball mill carries out wet-milling dissolution to the material after sintering；
The conveying mechanism includes the conveyer belt for connecting first ball mill and the feed bin, the connection feed bin and described half
The conveying worm of shower furnace and the tray conveyer for connecting the cooler and second ball mill.
2. system according to claim 1, it is characterised in that the desiliconization flyash sintering mechanism includes screening machine and roller
Formula disintegrating machine, wherein, the material after the cooling sieves through the screening machine, and it is laggard that coarse fodder enters the roll crushing crusher machine
Enter second ball mill and carry out wet-milling dissolution, fines is directly entered second ball mill and carries out wet-milling dissolution.
3. system according to claim 1, it is characterised in that the aluminium hydroxide extraction element include for stripping slurry according to
The secondary dissolution subsider flowed through, clear liquid groove, pipeline desiliconization device, leaf filter, desiliconization subsider, multiple carbon divide groove and square position to filter
Machine.
4. system according to claim 1, it is characterised in that the combustion chamber is in circular groove shape, and the combustion chamber side
The first burner and the second burner are provided with wall.
5. system according to claim 4, it is characterised in that the activity, which stops platform and included, closes on first burning
The first activity that device is set, which stops platform and closes on the second activity that second burner is set, stops platform, and described first lives
Dynamic stop between platform and the second activity stop platform leaves second material dropping channel, is set in the side wall of the combustion chamber
Be equipped with track, first burner and second burner can it is independent along the track both vertically and horizontally
Upper movement.
A kind of 6. method that aluminum oxide is produced using desiliconization flyash sintering process, it is characterised in that methods described usage right will
The system described in any one of 1-5 is sought, methods described comprises the steps of：
Step 1：Mass ratio is met into NaO2：Al2O3=0.9~0.98, CaO：SiO2=1.9~2.1 desiliconization flyash and stone
Lime stone, sodium carbonate add the first ball mill, and binding agent is added in a manner of spray, is made 1mm~3mm raw material ball, and by institute
State raw material ball and feed bin storage is sent into by conveyer belt；
Step 2：The raw material ball is sent at 1200 DEG C~1400 DEG C by half shower furnace by the feed bin by conveying worm
At a temperature of be sintered；
Step 3：Material after sintering is cooled to less than 150 DEG C into cooler；
Step 4：Wet-milling dissolution is carried out to the material after cooling using the second ball mill；
Step 5：The dissolution subsider of stripping slurry warp is settled, gained clear liquid flows into the storage of clear liquid groove, and the clear liquid of storage is successively
Filtered into the one section of desiliconization of pipeline desiliconization device, through leaf filter and enter the secondary desiliconization of desiliconization subsider, obtain the aluminium after desiliconization
Acid sodium solution；
Step 6：Sodium aluminate solution after the desiliconization successively flows through multiple carbon and divides groove to be reacted, and obtains containing aluminium hydroxide
Slurry, carbon described in each of which divides trench bottom to be passed through CO2Gas；
Step 7：The slurry containing aluminium hydroxide is filtered into horizontal table filter, obtains aluminium hydroxide；
Step 8：The aluminium hydroxide is calcined to obtain aluminum oxide through gaseous suspension stove.
7. according to the method for claim 6, it is characterised in that the step 2 includes：The raw material ball is outstanding by described half
Floating stove top enters, and stops short stay on platform in the activity after the preheating chamber uniformly preheating, is heated by burner
Carry out high temperature sintering reaction.
8. according to the method for claim 7, it is characterised in that the step 2 includes：
Position by adjusting the burner controls sintering region；
By adjusting flame length control sintering temperature.
9. according to the method for claim 6, it is characterised in that the step 4 includes：The screened machine of material after cooling
Screening, coarse fodder enter second ball mill progress wet-milling dissolution after entering roll crushing crusher machine, and fines is directly entered described
Second ball mill carries out wet-milling dissolution.
10. according to the method for claim 6, it is characterised in that the step 5 includes：By the material of dissolution subsider bottom
Slurry is put into hot wash in washing settling groove and settled, and gained precipitation is discharged after filter press press filtration obtains calcium silicate slag；Step 7 bag
Contain：Filter the mother liquid obtained sodium carbonate evaporation station that is back to be evaporated, dispensing again after the crystallization gained filtered drying of sodium carbonate.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109809716A (en) * | 2019-03-29 | 2019-05-28 | 东北大学 | Low-grade magnesite calcining decalcification removes the method that silicon prepares high-purity light calcined magnesia |
| CN111233016A (en) * | 2020-02-24 | 2020-06-05 | 河北科技大学 | Method for extracting aluminum oxide from medium-low grade aluminum-containing raw material |
| CN113800544A (en) * | 2021-09-24 | 2021-12-17 | 内蒙古茂燊科技有限公司 | Method and system for preparing high-whiteness and high-purity aluminum hydroxide by utilizing solid waste |
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2017
- 2017-12-01 CN CN201711251164.1A patent/CN107879365A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109809716A (en) * | 2019-03-29 | 2019-05-28 | 东北大学 | Low-grade magnesite calcining decalcification removes the method that silicon prepares high-purity light calcined magnesia |
| CN111233016A (en) * | 2020-02-24 | 2020-06-05 | 河北科技大学 | Method for extracting aluminum oxide from medium-low grade aluminum-containing raw material |
| CN113800544A (en) * | 2021-09-24 | 2021-12-17 | 内蒙古茂燊科技有限公司 | Method and system for preparing high-whiteness and high-purity aluminum hydroxide by utilizing solid waste |
| CN113800544B (en) * | 2021-09-24 | 2023-11-10 | 内蒙古会原科技有限公司 | Method and system for preparing high Bai Gaochun aluminum hydroxide by utilizing solid waste |
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