CN207619036U - The system for handling gangue - Google Patents
The system for handling gangue Download PDFInfo
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- CN207619036U CN207619036U CN201721203434.7U CN201721203434U CN207619036U CN 207619036 U CN207619036 U CN 207619036U CN 201721203434 U CN201721203434 U CN 201721203434U CN 207619036 U CN207619036 U CN 207619036U
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Abstract
The utility model discloses the systems of processing gangue, including：Mixing device, molding machine, drying device, rotary hearth furnace, leaching device, heavy aluminium device, calciner and silica unit processed, wherein, in rotary hearth furnace feed zone, pre-desiliconizing area, main reaction region and discharge zone are disposed with along material movement direction, feed zone has dry pelletizing entrance, discharge zone is exported with agglomerates, and dry pelletizing entrance is connected with dry pelletizing outlet；Leaching device has agglomerates entrance, sodium carbonate liquor entrance, the outlet of sial leachate and insoluble slag outlet；Heavy aluminium device has sial leachate entrance, carbon dioxide entrance, aluminium hydroxide outlet and the outlet of heavy aluminium extraction raffinate；Calciner has aluminium hydroxide entrance and alundum (Al2O3) outlet；Silica unit processed has heavy aluminium extraction raffinate entrance and silica outlet.Using system processing gangue flow is short, low energy consumption, the aluminium and silicon in gangue can be extracted simultaneously and obtains GOOD TASTE alundum (Al2O3) and silica.
Description
Technical field
The utility model belongs to chemical engineering of materials field, specifically, the utility model is related to handle the system of gangue.
Background technology
Gangue is the solid waste discharged during coal mining process and coal washing, be one kind in coalification course with coal seam companion
A kind of relatively low, harder than the coal black and gray rock of raw phosphorus content.Gangue includes digging gangue during tunnelling, adopts
The spoil produced in top plate and bottom plate and interlayer during pick and that chooses during coal washing wash spoil.If gangue is abandoned
It sets and does not have to, do not only take up tract, and there are various hidden danger, can be polluted greatly as the sulfide in gangue is escaped or leached
Fire occurs for the easy spontaneous combustion of gas, farmland and water body, coal gangue hill or silts river up in rainy season avalanche to cause disaster.China accumulates bastard coal
100,000,000 tons of gangue will be also discharged up to 1,000,000,000 tons or more in stone every year.Therefore, how so that gangue obtain efficiently using need into
One step research.
Utility model content
The utility model is intended to solve at least some of the technical problems in related technologies.For this purpose, this reality
It is the system for proposing processing gangue with a novel purpose.Using system processing gangue, not only flow is short, energy consumption
It is low, moreover it is possible to while the aluminium in gangue and silicon are extracted, and high-quality alundum (Al2O3) and silica are obtained, and then realize solid waste
The efficient and innoxious use of gangue has preferable economic benefit.
One side according to the present utility model, the utility model proposes a kind of systems of processing gangue, including：
There is gangue entrance, lime stone entrance, magnesite entrance and mixed material to go out for mixing device, the mixing device
Mouthful；
Molding machine, the molding machine has mixed material entrance, starch solution entrance and the outlet of mixing pelletizing, described
Mixed material entrance is connected with mixed material outlet；
There is mixing pelletizing entrance and dry pelletizing to export for drying device, the drying device, the mixing pelletizing entrance
It is connected with mixing pelletizing outlet；
Rotary hearth furnace, in the rotary hearth furnace along material movement direction be disposed with feed zone, pre-desiliconizing area, main reaction region and
There is dry pelletizing entrance, the discharge zone to be exported with agglomerates for discharge zone, the feed zone, the dry pelletizing entrance
It is connected with the dry pelletizing outlet；
Leaching device, the leaching device have agglomerates entrance, sodium carbonate liquor entrance, sial leachate outlet and
Insoluble slag exports, and the agglomerates entrance is connected with agglomerates outlet；
Heavy aluminium device, the heavy aluminium device have sial leachate entrance, carbon dioxide entrance, aluminium hydroxide outlet and sink
Aluminium extraction raffinate exports, and the sial leachate entrance is connected with sial leachate outlet；
There is aluminium hydroxide entrance and alundum (Al2O3) to export for calciner, the calciner, and the aluminium hydroxide enters
Mouth is connected with aluminium hydroxide outlet；
Silica unit processed, the silica unit processed has heavy aluminium extraction raffinate entrance and silica outlet, described
Heavy aluminium extraction raffinate entrance is connected with the heavy aluminium extraction raffinate outlet.
According to the system of the processing gangue of the utility model above-described embodiment, mixing device, molding can be utilized successively
Device, drying device and rotary hearth furnace carry out mixed-forming and drying and roasting to lime stone, magnesite and gangue, obtain roasting ball
Group, and make the aluminium in agglomerates and silicon leaching using sodium carbonate liquor in leaching device, obtain sial leachate；Again heavy
Heavy aluminium is carried out in aluminium device to sial leachate using carbon dioxide to handle to obtain aluminium hydroxide and heavy aluminium extraction raffinate；Finally exist respectively
Calciner and silica unit processed handle aluminium hydroxide and heavy aluminium extraction raffinate, obtain high-quality alundum (Al2O3) and
Silica.Gangue is handled by using the system of the processing gangue of the utility model above-described embodiment as a result, is not only flowed
Journey is short, low energy consumption, can also extract aluminium and silicon in gangue simultaneously, and obtains the oxidation of high-quality three that purity is all higher than 99%
Two aluminium and silica, and then realize the efficient and innoxious use of solid waste gangue, there is preferable economic benefit.
In addition, can also have following additional skill according to the system of the processing gangue of the utility model above-described embodiment
Art feature：
In the present invention, the feed zone, the pre-desiliconizing area, the main reaction region and the discharge zone are described
Radian in the circumference of rotary hearth furnace be followed successively by 25 degree, 110-130 degree, 155-175 degree and 50 degree.Thus, it is possible to make drying
Pelletizing fully reacts in pre-desiliconizing area and main reaction region, and obtains agglomerates.
In the present invention, the system for handling gangue further comprises：Fine grinding device, the fine grinding device setting exist
It is connected before the mixing device and with the gangue entrance.Thus, it is possible to keep gangue and lime stone and magnesite abundant
Contact, and then further increase the conversion of alumina silicate and free silicon dioxide in the efficiency and gangue that follow-up drying and roasting is handled
Rate.
Description of the drawings
Fig. 1 is the structural schematic diagram according to the system of the processing gangue of the utility model one embodiment.
Fig. 2 is the method flow using the system processing gangue of the processing gangue of the utility model one embodiment
Figure.
Fig. 3 is the method flow of the system processing gangue for the processing gangue for utilizing another embodiment of the utility model
Figure.
Specific implementation mode
The embodiments of the present invention are described below in detail, examples of the embodiments are shown in the accompanying drawings, wherein from beginning
Same or similar element or element with the same or similar functions are indicated to same or similar label eventually.Below by ginseng
The embodiment for examining attached drawing description is exemplary, it is intended to for explaining the utility model, and should not be understood as to the utility model
Limitation.
One side according to the present utility model, the utility model proposes a kind of systems of processing gangue, such as Fig. 1 institutes
Show, including：
Mixing device 100, molding machine 200, drying device 300, rotary hearth furnace 400, leaching device 500, heavy aluminium device
600, calciner 700 and silica unit 800 processed.
Wherein, mixing device 100 has gangue entrance 110, lime stone entrance 120, magnesite entrance 130 and mixture
Material outlet 140；Molding machine 200 has mixed material entrance 210, starch solution entrance 220 and mixing pelletizing outlet 230, mixes
Material inlet 210 is closed with mixed material outlet 140 to be connected；There is drying device 300 mixing pelletizing entrance 310 and dry pelletizing to go out
Mouth 320, mixing pelletizing entrance 310 are connected with mixing pelletizing outlet 230；It is set gradually along material movement direction in rotary hearth furnace 400
There are feed zone 410, pre-desiliconizing area 420, main reaction region 430 and discharge zone 440, feed zone 410 that there is dry pelletizing entrance 411,
There are agglomerates to export 441 for discharge zone 440, and dry pelletizing entrance 411 is connected with dry pelletizing outlet 320；Leaching device 500
With agglomerates entrance 510, sodium carbonate liquor entrance 520, sial leachate outlet 530 and insoluble slag outlet 540, ball is roasted
Group's entrance 510 is connected with agglomerates outlet 441；Heavy aluminium device 600 has sial leachate entrance 610, carbon dioxide entrance
620, aluminium hydroxide outlet 630 and heavy aluminium extraction raffinate outlet 640, sial leachate entrance 610 exports 530 phases with sial leachate
Even；Calciner 700 has aluminium hydroxide entrance 710 and alundum (Al2O3) outlet 720, aluminium hydroxide entrance 710 and hydroxide
Aluminium outlet 630 is connected；Silica unit 800 processed has heavy aluminium extraction raffinate entrance 810 and silica outlet 820, heavy aluminium extraction raffinate
Entrance 810 is connected with heavy aluminium extraction raffinate outlet 640.
According to the utility model above-described embodiment processing gangue system, can utilize successively mixing device 100, at
Type device 200, drying device 300 and rotary hearth furnace 400 carry out mixed-forming and dry roasting to lime stone, magnesite and gangue
It burns, obtains agglomerates, and make the aluminium in agglomerates and silicon leaching using sodium carbonate liquor in leaching device 500, obtain
Sial leachate；Heavy aluminium is carried out to sial leachate using carbon dioxide in heavy aluminium device 600 again to handle to obtain aluminium hydroxide
With heavy aluminium extraction raffinate；Finally respectively at calciner 700 and silica unit 800 processed are to aluminium hydroxide and heavy aluminium extraction raffinate
Reason, obtains the alundum (Al2O3) and silica of high-quality.As a result, by using the processing coal of the utility model above-described embodiment
The system of spoil handles gangue, and not only flow is short, low energy consumption, can also extract aluminium and silicon in gangue simultaneously, and obtain
Purity is all higher than 99% GOOD TASTE alundum (Al2O3) and silica, and then realizes the efficient and innoxious profit of solid waste gangue
With with preferable economic benefit.
The system of the processing gangue of the utility model above-described embodiment is described in detail below with reference to Fig. 1.
Embodiment according to the present utility model, mixing device 100 have gangue entrance 110, lime stone entrance 120, water chestnut
Magnesium mine entrance 130 and mixed material outlet 140；Mixing device 100 is suitable for carrying out at batch mixing gangue, lime stone and magnesite
Reason, to obtain mixed material.
Specific embodiment according to the present utility model, inventor have found, SiO in gangue2Content be up to 52-60 weight
Measure %, Al2O3Content be up to 28-38 weight %, the remaining impurity phase for calcium and magnesium, and the aluminium in gangue mainly with alumina silicate
Form exists, and by the way that gangue, lime stone and magnesite are carried out mixed-forming processing in the utility model, can make mixing ball
Group can efficiently use the magnesia difference in calcium oxide and magnesite in lime stone when carrying out sequential reduction calcination process
With in gangue alumina silicate and free silicon dioxide reacted, and then extract gangue in aluminium and silicon.
The mass ratio of specific embodiment according to the present utility model, gangue, lime stone and magnesite can be 100：
(55-81)：(15-23).Inventor has found, on the basis of the quality of gangue, when the addition of lime stone is very few, is equivalent to
The addition of calcium oxide is insufficient, when carrying out sequential reduction calcination process, be not enough to the aluminosilicate reaction in gangue, in turn
Cause the rate of recovery of aluminium and silicon in gangue relatively low, when the addition of lime stone is excessive, gangue can not be further increased
The rate of recovery of middle aluminium can also cause wastage of material and increase the burden and energy consumption of subsequent treatment process；Similarly, adding when magnesite
Enter amount it is very few when, be not enough to react with the free silicon dioxide in gangue, and then cause the rate of recovery of silicon relatively low, and work as lime
When the addition of stone is excessive, the rate of recovery of silicon in gangue can not be further increased, after also causing wastage of material and increasing
The burden and energy consumption of continuous treatment process.It is by controlling the mass ratio of gangue, lime stone and magnesite in the utility model
100：(55-81)：(15-23) can not only be such that the calcium oxide in alumina silicate and lime stone in gangue fully reacts, and generate
Calcium aluminate and dicalcium silicate enable the free silicon dioxide in gangue fully to react and generate with the magnesia in magnesite
Magnesium silicate, moreover it is possible to significantly improve the conversion ratio of alumina silicate and free silicon dioxide.Specific embodiment according to the present utility model, coal
The mass ratio of spoil, lime stone and magnesite can be preferably 100：(60-70)：(16-20), thus, it is possible to further increase
The conversion ratio of alumina silicate and free silicon dioxide in gangue.
Embodiment according to the present utility model, the system for handling gangue may further include fine grinding device, fine grinding dress
It installs before mixing device 100 and is connected with gangue entrance 110.Thus, it is possible to using fine grinding device that gangue is thin
It is milled to grain size and is not more than 0.074mm, make gangue that can be come into full contact with lime stone and magnesite during mixing treatment, into
And further increase the conversion ratio of alumina silicate and free silicon dioxide in the efficiency and gangue that follow-up drying and roasting is handled.
Specific embodiment according to the present utility model, can also be further by lime stone and water chestnut before carrying out mixing treatment
Magnesium mine is finely ground to grain size and is not more than 0.074mm.Thus, it is possible to further increase the efficiency and gangue of follow-up drying and roasting processing
The conversion ratio of middle alumina silicate and free silicon dioxide.
Embodiment according to the present utility model, molding machine 200 have mixed material entrance 210, starch solution entrance 220
With mixing pelletizing outlet 230, mixed material entrance 210 is connected with mixed material outlet 140；Molding machine 200 is suitable for mix
Material and starch solution carry out forming processes, to obtain mixing pelletizing.
Specific embodiment according to the present utility model, when carrying out forming processes, the starch solution that 5-10% can be added is done
Binder, thus, it is possible to make mixing pelletizing that there is certain intensity.In addition, making binder also using the starch solution of 5-10%
It can further reduce the cost.Binder content is too high will to increase cost, and the binder of high mixture ratio keeps pelletizing finer and close, breathe freely
Property be deteriorated, be unfavorable for chemically reacting, proportioning is too low, and cannot be guaranteed the intensity of pelletizing, and experiment finds that binder 5-10% is best.
There is mixing pelletizing entrance 310 and dry pelletizing to export for embodiment according to the present utility model, drying device 300
320, mixing pelletizing entrance 310 is connected with mixing pelletizing outlet 230；Drying device 300 is suitable for mixing pelletizing for being dried
Processing, to obtain dry pelletizing.Thus, it is possible to effectively reduce the energy consumption roasted to dry pelletizing in rotary hearth furnace 400.
Embodiment according to the present utility model, in rotary hearth furnace 400 along material movement direction be disposed with feed zone 410,
Pre-desiliconizing area 420, main reaction region 430 and discharge zone 440, feed zone 410 have dry pelletizing entrance 411, and discharge zone 440 has
Agglomerates outlet 441, dry pelletizing entrance 411 are connected with dry pelletizing outlet 320；Rotary hearth furnace 400 is suitable for making dry pelletizing
Pass through pre-desiliconizing area successively and main reaction region is reacted, to obtain agglomerates.
Specific embodiment according to the present utility model, the temperature in pre-desiliconizing area 420 can be 1300- in rotary hearth furnace 400
1400 degrees Celsius.Thus, it is possible to provide suitable temperature condition with reacting for magnesite for gangue, make free in gangue
Silica can fully react under above-mentioned temperature condition with the magnesia in magnesite and generate magnesium silicate, and then significantly carry
The conversion ratio of free silicon dioxide in high gangue.Specific embodiment according to the present utility model, pre-desiliconizing area in rotary hearth furnace 400
420 temperature can be preferably 1320-1380 degrees Celsius, thus, it is possible to further increase free silicon dioxide in gangue
Conversion ratio.
Specific embodiment according to the present utility model, the temperature of main reaction region 430 can be 1350- in rotary hearth furnace 400
1500 degrees Celsius.Thus, it is possible to which the reaction for gangue and lime stone provides suitable temperature condition, make the silicic acid in gangue
Aluminium can fully react under above-mentioned temperature condition with the calcium oxide in lime stone and generate calcium aluminate and dicalcium silicate, Jin Erxian
Write the conversion ratio for improving the alumina silicate in gangue.Specific embodiment according to the present utility model, main reaction region in rotary hearth furnace 400
430 temperature can be preferably 1370-1450 degrees Celsius, thus, it is possible to further increase the conversion of the alumina silicate in gangue
Rate.
Specific embodiment according to the present utility model, feed zone 410, pre-desiliconizing area 420, main reaction region 430 and discharge zone
440 radian in the circumference of rotary hearth furnace 400 can be followed successively by 25 degree, 110-130 degree, 155-175 degree and 50 degree.This reality
With can effectively distribute the feed time of dry pelletizing, the coal carried out in pre-desiliconizing area 420 by using above-mentioned setting in novel
The reaction time of spoil and magnesite, main reaction region 430 carry out gangue and lime stone reaction time and agglomerates
Discharging time, thus, it is possible to realized respectively in rotary hearth furnace 400 gangue and magnesite react and gangue and lime stone
Reaction, and control the reaction condition of gangue and magnesite and gangue and lime stone respectively, and then can effectively facilitate dry
Dry calcination process is smoothed out, and further carries the conversion ratio of alumina silicate and free silicon dioxide in gangue.
Specific embodiment according to the present utility model, residence time of the dry pelletizing in rotary hearth furnace 400 can be 0.8-
1.5 hour.Thus, it is possible to make reacting and being carried out in main reaction region 430 for the gangue carried out in pre-desiliconizing area 420 and magnesite
The reaction of gangue and lime stone all have the enough reaction time, and then further increase free silicon dioxide in gangue
With the conversion ratio of alumina silicate.
Specific embodiment according to the present utility model, fabric thickness of the dry pelletizing in rotary hearth furnace 400 can be 100-
160mm.Thus, it is possible to further increase gangue and magnesite react and the reaction efficiency of gangue and lime stone.
Specific embodiment according to the present utility model, by using the processing gangue system of the utility model above-described embodiment
System processing gangue, can make the conversion ratio of free silicon dioxide in gangue reach 83-90%, the conversion ratio of alumina silicate reaches
85-95%.
Embodiment according to the present utility model, leaching device 500 have agglomerates entrance 510, sodium carbonate liquor entrance
520, sial leachate outlet 530 and insoluble slag outlet 540, agglomerates entrance 510 are connected with agglomerates outlet 441；Leaching
Go out device 500 to be suitable for carrying out leaching process to agglomerates using sodium carbonate liquor, to obtain sial leachate and insoluble slag.
The concentration of specific embodiment according to the present utility model, sodium carbonate liquor can be 105-125g/L.This practicality is new
By using the sodium carbonate liquor of above-mentioned concentration in type, it on the one hand can make calcium aluminate in agglomerates in aqueous solution and carbon
Sour sodium fully reacts the sodium aluminate and precipitation of calcium carbonate for generating solubility, dicalcium silicate and sodium carbonate fully reacts and generates calcium carbonate
Precipitation and soluble sodium metasilicate, magnesium silicate and sodium carbonate, which fully react, generates carbonic acid magnesium precipitate and sodium metasilicate, and then makes roasting
Aluminium and silicon in pelletizing are effectively leached and are enriched with, and the efficiency of leaching process on the other hand can also be further increased.
Specific embodiment according to the present utility model, when carrying out leaching process to agglomerates using sodium carbonate liquor, roasting
The temperature for burning pelletizing can be 100-120 degrees Celsius, and the time of leaching process can be 20-35 minutes, thus, it is possible to make carbonic acid
Calcium aluminate, dicalcium silicate and magnesium silicate in sodium water solution and agglomerates fully react, so make aluminium in agglomerates and
Silicon is effectively leached, and can arrive the sial leachate containing sodium metasilicate and sodium aluminate, realization and calcium carbonate by filtration treatment
Deng the separation of not slag.
Specific embodiment according to the present utility model, by using the processing gangue of the utility model above-described embodiment
System handles gangue, the leaching rate of aluminium in agglomerates can be made to reach 90-95%, and then can further increase gangue
The rate of recovery of middle aluminium.
Embodiment according to the present utility model, the aluminium device 600 that sinks have sial leachate entrance 610, carbon dioxide entrance
620, aluminium hydroxide outlet 630 and heavy aluminium extraction raffinate outlet 640, sial leachate entrance 610 exports 530 phases with sial leachate
Even；Heavy aluminium device 600 is suitable for carrying out heavy aluminium to sial leachate using carbon dioxide handling, to obtain aluminium hydroxide and heavy aluminium
Extraction raffinate.
Specific embodiment according to the present utility model, the flow velocity that carbon dioxide is passed through into sial leachate are 20-35L/
min.Not only carbon dioxide can be made fully to be reacted with the sodium aluminate in sial leachate as a result, and generate aluminum hydroxide precipitation,
The efficiency of heavy aluminium processing can also be further increased and improve the utilization rate of carbon dioxide.
Specific embodiment according to the present utility model is passed through after carbon dioxide fully reacts into sial leachate and carried out
Filter, can obtain solid aluminum hydroxide and the heavy aluminium extraction raffinate containing sodium metasilicate, realize efficiently separating for aluminium and silicon.
There is aluminium hydroxide entrance 710 and alundum (Al2O3) to export for embodiment according to the present utility model, calciner 700
720, aluminium hydroxide entrance 710 is connected with aluminium hydroxide outlet 630；Calciner 700 is suitable for carrying out aluminium hydroxide at roasting
Reason, to obtain alundum (Al2O3).
Aluminium hydroxide can be carried out calcination process after washing and prepare three by specific embodiment according to the present utility model
Al 2 O.Specific embodiment according to the present utility model, the temperature that calcination process is carried out to aluminium hydroxide can be 1200-
1250℃.Thus, it is possible to which aluminium hydroxide is made fully to decompose, and obtain the high-grade alundum (Al2O3) that purity is not less than 99%.
Embodiment according to the present utility model, silica unit 800 processed have heavy aluminium extraction raffinate entrance 810 and silica
Outlet 820, heavy aluminium extraction raffinate entrance 810 are connected with heavy aluminium extraction raffinate outlet 640；Calciner 700 is suitable for successively passing through heavy aluminium extraction raffinate
Cross concentration, acidleach, adjustment pH, curing, filtering, washing and drying, to obtain silica.
In order to facilitate the system for the processing gangue for understanding the utility model above-described embodiment, below to utilizing above-mentioned processing
The method of the system processing gangue of gangue is described in detail.
Specific embodiment according to the present utility model handles the method packet of gangue using the system of above-mentioned processing gangue
It includes：(1) gangue, lime stone and magnesite are subjected to mixing treatment, to obtain mixed material；(2) by mixed material and shallow lake
Powder solution carries out forming processes, to obtain mixing pelletizing；(3) by mixing pelletizing for processing is dried, to obtain drying
Pelletizing；(4) dry pelletizing is supplied to rotary hearth furnace, in rotary hearth furnace along material movement direction define feed zone, pre-desiliconizing area,
Main reaction region and discharge zone make dry pelletizing be reacted successively by pre-desiliconizing area and main reaction region, to obtain roasting ball
Group；(5) leaching process is carried out to agglomerates using sodium carbonate liquor, to obtain sial leachate and insoluble slag；(6) to silicon
It is passed through carbon dioxide in aluminium leachate and carries out heavy aluminium processing, to obtain aluminium hydroxide and heavy aluminium extraction raffinate；(7) by aluminium hydroxide into
Row calcination process, to obtain alundum (Al2O3)；(8) by heavy aluminium extraction raffinate successively by concentration, acidleach, adjustment pH, curing, mistake
Filter, washing and drying, to obtain silica.
It, can be first with lime stone and magnesite according to the method for the processing gangue of the utility model above-described embodiment
Mixed-forming and drying and roasting are carried out with gangue, agglomerates is obtained, makes in agglomerates followed by sodium carbonate liquor
Aluminium and silicon leach, then so that aluminium and silicon is detached by heavy aluminium processing and obtain aluminium hydroxide and heavy aluminium extraction raffinate, finally respectively to hydrogen-oxygen
Change aluminium and heavy aluminium extraction raffinate carries out processing and can obtain the alundum (Al2O3) and silica of high-quality.As a result, by using this reality
With the method for the processing gangue of novel above-described embodiment, not only flow is short, low energy consumption, can also extract in gangue simultaneously
Aluminium and silicon, and high-quality alundum (Al2O3) and silica that purity is all higher than 99% are obtained, and then realize solid waste gangue
Efficient and innoxious use has preferable economic benefit.
It is described in detail below with reference to the method for the processing gangue of Fig. 2-3 pairs of the utility model above-described embodiments.
S100：Mixed-forming processing
Gangue, lime stone and magnesite are carried out mixing treatment, to be mixed by embodiment according to the present utility model
Close material；Mixed material and starch solution are subjected to forming processes, to obtain mixing pelletizing.Thus, it is possible to further increase
Carry out the efficiency of follow-up drying and roasting processing.
Specific embodiment according to the present utility model, inventor have found, SiO in gangue2Content be up to 52-60 weight
Measure %, Al2O3Content be up to 28-38 weight %, the remaining impurity phase for calcium and magnesium, and the aluminium in gangue mainly with alumina silicate
Form exists, and by the way that gangue, lime stone and magnesite are carried out mixed-forming processing in the utility model, can make mixing ball
Group can efficiently use the magnesia difference in calcium oxide and magnesite in lime stone when carrying out sequential reduction calcination process
With in gangue alumina silicate and free silicon dioxide reacted, and then extract gangue in aluminium and silicon.
The mass ratio of specific embodiment according to the present utility model, gangue, lime stone and magnesite can be 100：
(55-81)：(15-23).Inventor has found, on the basis of the quality of gangue, when the addition of lime stone is very few, is equivalent to
The addition of calcium oxide is insufficient, when carrying out sequential reduction calcination process, be not enough to the aluminosilicate reaction in gangue, in turn
Cause the rate of recovery of aluminium and silicon in gangue relatively low, when the addition of lime stone is excessive, gangue can not be further increased
The rate of recovery of middle aluminium can also cause wastage of material and increase the burden and energy consumption of subsequent treatment process；Similarly, adding when magnesite
Enter amount it is very few when, be not enough to react with the free silicon dioxide in gangue, and then cause the rate of recovery of silicon relatively low, and work as lime
When the addition of stone is excessive, the rate of recovery of silicon in gangue can not be further increased, after also causing wastage of material and increasing
The burden and energy consumption of continuous treatment process.It is by controlling the mass ratio of gangue, lime stone and magnesite in the utility model
100：(55-81)：(15-23) can not only be such that the calcium oxide in alumina silicate and lime stone in gangue fully reacts, and generate
Calcium aluminate and dicalcium silicate enable the free silicon dioxide in gangue fully to react and generate with the magnesia in magnesite
Magnesium silicate, moreover it is possible to significantly improve the conversion ratio of alumina silicate and free silicon dioxide.Specific embodiment according to the present utility model, coal
The mass ratio of spoil, lime stone and magnesite can be preferably 100：(60-70)：(16-20), thus, it is possible to further increase
The conversion ratio of alumina silicate and free silicon dioxide in gangue.
Specific embodiment according to the present utility model, can before gangue, lime stone and magnesite are carried out mixing treatment
To further comprise：Gangue is finely ground to grain size and is not more than 0.074mm.Thus, it is possible to make gangue and lime stone and magnesite
Mine comes into full contact with, and then further increases alumina silicate and free silicon dioxide in the efficiency and gangue that follow-up drying and roasting is handled
Conversion ratio.
Specific embodiment according to the present utility model, can be further by lime stone and magnesite before carrying out mixing treatment
Mine is finely ground to grain size and is not more than 0.074mm.Thus, it is possible to further increase in the efficiency and gangue that follow-up drying and roasting is handled
The conversion ratio of alumina silicate and free silicon dioxide.
Specific embodiment according to the present utility model, when carrying out forming processes, the starch solution that 5-10% can be added is done
Binder, thus, it is possible to make mixing pelletizing that there is certain intensity.In addition, making binder also using the starch solution of 5-10%
It can further reduce the cost.Binder content is too high will to increase cost, and the binder of high mixture ratio keeps pelletizing finer and close, breathe freely
Property be deteriorated, be unfavorable for chemically reacting, proportioning is too low, and cannot be guaranteed the intensity of pelletizing, and experiment finds that binder 5-10% is best.
S200：Drying and roasting processing
Embodiment according to the present utility model, by mixing pelletizing for processing is dried, to obtain dry pelletizing；It will do
Dry pelletizing is supplied to rotary hearth furnace 400, in rotary hearth furnace 400 along material movement direction define feed zone 410, pre-desiliconizing area 420,
Main reaction region 430 and discharge zone 440 make dry pelletizing be reacted successively by pre-desiliconizing area 420 and main reaction region 430, with
Just agglomerates are obtained.Thus, it is possible to which gangue is made fully to be reacted with lime stone and magnesite.
Specific embodiment according to the present utility model, the temperature in pre-desiliconizing area 420 can be 1300- in rotary hearth furnace 400
1400 degrees Celsius.Thus, it is possible to provide suitable temperature condition with reacting for magnesite for gangue, make free in gangue
Silica can fully react under above-mentioned temperature condition with the magnesia in magnesite and generate magnesium silicate, and then significantly carry
The conversion ratio of free silicon dioxide in high gangue.Specific embodiment according to the present utility model, pre-desiliconizing area in rotary hearth furnace 400
420 temperature can be preferably 1320-1380 degrees Celsius, thus, it is possible to further increase free silicon dioxide in gangue
Conversion ratio.
Specific embodiment according to the present utility model, the temperature of main reaction region 430 can be 1350- in rotary hearth furnace 400
1500 degrees Celsius.Thus, it is possible to which the reaction for gangue and lime stone provides suitable temperature condition, make the silicic acid in gangue
Aluminium can fully react under above-mentioned temperature condition with the calcium oxide in lime stone and generate calcium aluminate and dicalcium silicate, Jin Erxian
Write the conversion ratio for improving the alumina silicate in gangue.Specific embodiment according to the present utility model, main reaction region in rotary hearth furnace 400
430 temperature can be preferably 1370-1450 degrees Celsius, thus, it is possible to further increase the conversion of the alumina silicate in gangue
Rate.
Specific embodiment according to the present utility model, feed zone 410, pre-desiliconizing area 420, main reaction region 430 and discharge zone
440 radian in the circumference of rotary hearth furnace 400 can be followed successively by 25 degree, 110-130 degree, 155-175 degree and 50 degree.This reality
With can effectively distribute the feed time of dry pelletizing, the coal carried out in pre-desiliconizing area 420 by using above-mentioned setting in novel
The reaction time of spoil and magnesite, main reaction region 430 carry out gangue and lime stone reaction time and agglomerates
Discharging time, thus, it is possible to realized respectively in rotary hearth furnace 400 gangue and magnesite react and gangue and lime stone
Reaction, and control the reaction condition of gangue and magnesite and gangue and lime stone respectively, and then can effectively facilitate dry
Dry calcination process is smoothed out, and further carries the conversion ratio of alumina silicate and free silicon dioxide in gangue.
Specific embodiment according to the present utility model, residence time of the dry pelletizing in rotary hearth furnace 400 can be 0.8-
1.5 hour.Thus, it is possible to make reacting and being carried out in main reaction region 430 for the gangue carried out in pre-desiliconizing area 420 and magnesite
The reaction of gangue and lime stone all have the enough reaction time, and then further increase free silicon dioxide in gangue
With the conversion ratio of alumina silicate.
Specific embodiment according to the present utility model, fabric thickness of the dry pelletizing in rotary hearth furnace 400 can be 100-
160mm.Thus, it is possible to further increase gangue and magnesite react and the reaction efficiency of gangue and lime stone.
Specific embodiment according to the present utility model, by using the processing gangue of the utility model above-described embodiment
Method, can make the conversion ratio of free silicon dioxide in gangue reach 83-90%, and the conversion ratio of alumina silicate reaches 85-95%.
S300:Leaching process
Embodiment according to the present utility model carries out leaching process, to obtain using sodium carbonate liquor to agglomerates
Sial leachate and insoluble slag.
The concentration of specific embodiment according to the present utility model, sodium carbonate liquor can be 105-125g/L.This practicality is new
By using the sodium carbonate liquor of above-mentioned concentration in type, it on the one hand can make calcium aluminate in agglomerates in aqueous solution and carbon
Sour sodium fully reacts the sodium aluminate and precipitation of calcium carbonate for generating solubility, dicalcium silicate and sodium carbonate fully reacts and generates calcium carbonate
Precipitation and soluble sodium metasilicate, magnesium silicate and sodium carbonate, which fully react, generates carbonic acid magnesium precipitate and sodium metasilicate, and then makes roasting
Aluminium and silicon in pelletizing are effectively leached and are enriched with, and the efficiency of leaching process on the other hand can also be further increased.According to this
The specific embodiment of utility model, when carrying out leaching process to agglomerates using sodium carbonate liquor, the temperature of agglomerates can
Think 100-120 degrees Celsius, the time of leaching process can be 20-35 minutes, thus, it is possible to make aqueous sodium carbonate and roasting
Calcium aluminate, dicalcium silicate and magnesium silicate in pelletizing fully react, and then aluminium and silicon in agglomerates is made effectively to be leached,
And the sial leachate containing sodium metasilicate and sodium aluminate can be arrived by filtration treatment, realize the separation with the not slag such as calcium carbonate.
Specific embodiment according to the present utility model, by using the processing gangue of the utility model above-described embodiment
Method can make the leaching rate of aluminium in agglomerates reach 90-95%, and then can further increase the recycling of aluminium in gangue
Rate.
S400：Sial leachate prepares alundum (Al2O3) and silica
Embodiment according to the present utility model is passed through carbon dioxide into sial leachate and carries out heavy aluminium processing, so as to
To aluminium hydroxide and heavy aluminium extraction raffinate；Aluminium hydroxide is subjected to calcination process, to obtain alundum (Al2O3)；Successively by heavy aluminium extraction raffinate
By concentration, acidleach, adjustment pH, curing, filtering, washing and drying, to obtain silica.Thus, it is possible to effectively recycle
Aluminium in gangue and silicon, and high-grade alundum (Al2O3) and silica are prepared respectively.
Specific embodiment according to the present utility model, the flow velocity that carbon dioxide is passed through into sial leachate are 20-35L/
min.Not only carbon dioxide can be made fully to be reacted with the sodium aluminate in sial leachate as a result, and generate aluminum hydroxide precipitation,
The efficiency of heavy aluminium processing can also be further increased and improve the utilization rate of carbon dioxide.
Specific embodiment according to the present utility model is passed through after carbon dioxide fully reacts into sial leachate and carried out
Filter, can obtain solid aluminum hydroxide and the heavy aluminium extraction raffinate containing sodium metasilicate, realize efficiently separating for aluminium and silicon.
Aluminium hydroxide can be carried out calcination process after washing and prepare three by specific embodiment according to the present utility model
Al 2 O.Specific embodiment according to the present utility model, the temperature that calcination process is carried out to aluminium hydroxide can be 1200-
1250℃.Thus, it is possible to which aluminium hydroxide is made fully to decompose, and obtain the high-grade alundum (Al2O3) that purity is not less than 99%.
Specific embodiment according to the present utility model, by heavy aluminium extraction raffinate successively by concentration, acidleach, it is adjustment pH, ripe
Change, filtering, wash and be dried, can effectively recycle the silicon in heavy aluminium extraction raffinate, and purity is prepared and is not less than 99%
High-grade silica.
Embodiment 1
SiO in gangue2Content is 52 weight %；Al2O3Content is 28 weight %；It is first that gangue is levigate extremely
0.074mm or less.By gangue, lime stone, magnesite according to mass ratio be 100：55：15 carry out mixing treatments, and to obtaining
Mixed material in addition 5% starch solution carry out forming processes, obtain mixing pelletizing；It will be sent into after mixing pelletizing drying
Rotary hearth furnace is roasted, wherein fabric thickness of the dry pelletizing in rotary hearth furnace is 100mm, rotary hearth furnace feed zone, pre-desiliconizing
Area, main reaction region, the angle of discharge zone are respectively 25 °, 120 °, 165 °, 50 °, the temperature difference in pre-desiliconizing area and main reaction region
For 1320 DEG C and 1380 DEG C, obtained agglomerates are discharged by discharge zone after reaction by rotary hearth furnace run time 0.9h；It will
Agglomerates are cooled to 100 DEG C and carry out leaching process with the sodium carbonate liquor of a concentration of 105g/L, extraction time 20min,
It is filtered after leaching process, obtains the sial leachate containing sodium aluminate and sodium metasilicate, wherein the dissolution rate of aluminium is
91%；It it is passed through into sial leachate carbon dioxide with the rate of 20L/min carries out heavy aluminium and handle and filter, obtain aluminium hydroxide
With the heavy aluminium extraction raffinate containing sodium metasilicate；Aluminium hydroxide is subjected to calcination process under 1210 DEG C of temperature condition, obtains Al2O3；It will
For heavy aluminium extraction raffinate successively by concentration, acidleach, adjustment pH, curing, filtering, washing and drying obtain silica.Wherein, it prepares
Obtained Al2O3It is all higher than 99% with the purity of silica.
Embodiment 2
SiO in gangue2Content is 55 weight %；Al2O3Content is 35 weight %；It is first that gangue is levigate extremely
0.074mm or less.By gangue, lime stone, magnesite according to mass ratio be 100：68：20 carry out mixing treatments, and to obtaining
Mixed material in addition 8% starch solution carry out forming processes, obtain mixing pelletizing；It will be sent into after mixing pelletizing drying
Rotary hearth furnace is roasted, wherein fabric thickness of the dry pelletizing in rotary hearth furnace is 120mm, rotary hearth furnace feed zone, pre-desiliconizing
Area, main reaction region, the angle of discharge zone are respectively 25 °, 110 °, 175 °, 50 °, the temperature difference in pre-desiliconizing area and main reaction region
For 1350 DEG C and 1420 DEG C, obtained agglomerates are discharged by discharge zone after reaction by rotary hearth furnace run time 1.2h；It will
Agglomerates are cooled to 110 DEG C and carry out leaching process with the sodium carbonate liquor of a concentration of 113g/L, extraction time 28min,
It is filtered after leaching process, obtains the sial leachate containing sodium aluminate and sodium metasilicate, wherein the dissolution rate of aluminium is
93%；It it is passed through into sial leachate carbon dioxide with the rate of 27L/min carries out heavy aluminium and handle and filter, obtain aluminium hydroxide
With the heavy aluminium extraction raffinate containing sodium metasilicate；Aluminium hydroxide is subjected to calcination process under 1230 DEG C of temperature condition, obtains Al2O3；It will
For heavy aluminium extraction raffinate successively by concentration, acidleach, adjustment pH, curing, filtering, washing and drying obtain silica.Wherein, it prepares
Obtained Al2O3It is all higher than 99% with the purity of silica.
Embodiment 3
SiO in gangue2Content is 58 weight %；Al2O3Content is 38 weight %；It is first that gangue is levigate extremely
0.074mm or less.By gangue, lime stone, magnesite according to mass ratio be 100：88：22 carry out mixing treatments, and to obtaining
Mixed material in addition 10% starch solution carry out forming processes, obtain mixing pelletizing；It will be sent after mixing pelletizing drying
Enter rotary hearth furnace to be roasted, wherein fabric thickness of the dry pelletizing in rotary hearth furnace is 100mm, rotary hearth furnace feed zone, pre-desiliconizing
Area, main reaction region, the angle of discharge zone are respectively 25 °, 130 °, 155 °, 50 °, the temperature difference in pre-desiliconizing area and main reaction region
For 1370 DEG C and 1450 DEG C, obtained agglomerates are discharged by discharge zone after reaction by rotary hearth furnace run time 1.5h；It will
Agglomerates are cooled to 120 DEG C and carry out leaching process with the sodium carbonate liquor of a concentration of 122g/L, extraction time 32min,
It is filtered after leaching process, obtains the sial leachate containing sodium aluminate and sodium metasilicate, wherein the dissolution rate of aluminium is
91%；It it is passed through into sial leachate carbon dioxide with the rate of 20L/min carries out heavy aluminium and handle and filter, obtain aluminium hydroxide
With the heavy aluminium extraction raffinate containing sodium metasilicate；Aluminium hydroxide is subjected to calcination process under 1250 DEG C of temperature condition, obtains Al2O3；It will
For heavy aluminium extraction raffinate successively by concentration, acidleach, adjustment pH, curing, filtering, washing and drying obtain silica.Wherein, it prepares
Obtained Al2O3It is all higher than 99% with the purity of silica.
In the description of this specification, reference term " one embodiment ", " some embodiments ", " example ", " specifically show
The description of example " or " some examples " etc. means specific features, structure, material or spy described in conjunction with this embodiment or example
Point is contained at least one embodiment or example of the utility model.In the present specification, to the schematic table of above-mentioned term
Identical embodiment or example need not be directed to by stating.Moreover, particular features, structures, materials, or characteristics described can be
It can be combined in any suitable manner in any one or more embodiments or example.In addition, without conflicting with each other, this field
Technical staff can carry out the feature of different embodiments or examples described in this specification and different embodiments or examples
In conjunction with and combination.
Although the embodiments of the present invention have been shown and described above, it is to be understood that above-described embodiment is
Illustratively, it should not be understood as limiting the present invention, those skilled in the art are in the scope of the utility model
Inside it can make changes, modifications, alterations, and variations to the above described embodiments.
Claims (3)
1. a kind of system of processing gangue, which is characterized in that including：
Mixing device, the mixing device have gangue entrance, lime stone entrance, magnesite entrance and mixed material outlet；
Molding machine, the molding machine have mixed material entrance, starch solution entrance and the outlet of mixing pelletizing, the mixing
Material inlet is connected with mixed material outlet；
There is mixing pelletizing entrance and dry pelletizing to export for drying device, the drying device, the mixing pelletizing entrance and institute
The outlet of mixing pelletizing is stated to be connected；
Rotary hearth furnace, the rotary hearth furnace is interior to be disposed with feed zone, pre-desiliconizing area, main reaction region and discharging along material movement direction
There is dry pelletizing entrance, the discharge zone to be exported with agglomerates for area, the feed zone, the dry pelletizing entrance and institute
Dry pelletizing outlet is stated to be connected；
Leaching device, the leaching device have agglomerates entrance, sodium carbonate liquor entrance, sial leachate outlet and it is insoluble
Slag exports, and the agglomerates entrance is connected with agglomerates outlet；
Heavy aluminium device, the heavy aluminium device have more than sial leachate entrance, carbon dioxide entrance, aluminium hydroxide outlet and heavy aluminium
Liquid exports, and the sial leachate entrance is connected with sial leachate outlet；
There is aluminium hydroxide entrance and alundum (Al2O3) to export for calciner, the calciner, the aluminium hydroxide entrance with
The aluminium hydroxide outlet is connected；
Silica unit processed, the silica unit processed have heavy aluminium extraction raffinate entrance and silica outlet, the heavy aluminium
Extraction raffinate entrance is connected with the heavy aluminium extraction raffinate outlet.
2. system according to claim 1, which is characterized in that the feed zone, the pre-desiliconizing area, the main reaction region
With radian of the discharge zone in the circumference of the rotary hearth furnace be followed successively by 25 degree, 110-130 degree, 155-175 degree and 50
Degree.
3. system according to claim 1, which is characterized in that further comprise：Fine grinding device, the fine grinding device setting
It is connected before the mixing device and with the gangue entrance.
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|---|---|---|---|
| CN201721203434.7U CN207619036U (en) | 2017-09-18 | 2017-09-18 | The system for handling gangue |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721203434.7U CN207619036U (en) | 2017-09-18 | 2017-09-18 | The system for handling gangue |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112683052A (en) * | 2020-12-22 | 2021-04-20 | 寿县安固建材有限公司 | Coal gangue brick sintering processing equipment and processing method thereof |
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| CN112683052A (en) * | 2020-12-22 | 2021-04-20 | 寿县安固建材有限公司 | Coal gangue brick sintering processing equipment and processing method thereof |
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