CN105753024A - Method for extracting aluminum oxide from coal ash on basis of lime sinter process - Google Patents
Method for extracting aluminum oxide from coal ash on basis of lime sinter process Download PDFInfo
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- CN105753024A CN105753024A CN201610149727.5A CN201610149727A CN105753024A CN 105753024 A CN105753024 A CN 105753024A CN 201610149727 A CN201610149727 A CN 201610149727A CN 105753024 A CN105753024 A CN 105753024A
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- dissolution
- flyash
- lime
- roasting
- sintering
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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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/20—Silicates
- C01B33/24—Alkaline-earth metal silicates
Abstract
The invention discloses a method for extracting aluminum oxide from coal ash on basis of a lime sinter process.The method includes steps: (1) grinding and mixing; (2) raw material balling; (3) shaft furnace calcining; (4) autogenous pulverizing and cooling; (5) dissolving out; (6) separating and washing; (7) carbonizing and decomposing; (8) filtering; (9) treating according to a low-temperature Bayer process, so that metallurgical aluminum oxide is obtained.The method has the advantages that by shaft furnace calcinations, energy consumption is greatly reduced, and production cost is evidently reduced; by the method, sintering under high-temperature large-scale operating conditions can be realized easily, product sintering quality is guaranteed, and the method is suitable for large-scale industrial production.
Description
Technical field
The invention belongs to the recycling field of flyash, the resource relating to flyash effectively utilizes, and particularly relates to a kind of method that flyash based on lime sinter process extracts aluminium oxide.
Background technology
Currently for the Large Electrolytic Aluminium enterprise of alumina-free self-sufficiency supportability, along with external aluminium oxide export policy risk height domestic alumina resource of reaching tends to exhausted impact and constantly ferments, there is risk in long-term alumina raw material supply.
Meanwhile, domestic high alumina coal Prospective resources about 100,000,000,000 tons, rich in aluminium oxide 10,000,000,000 tons.In view of the enterprise such as electrolytic aluminium, iron and steel needs to consume a large amount of thermal coal, particularly electrolytic aluminium, integrated iron and steel works.Hence for this type of enterprise, take the flyash that the circular economy industrial thinking of development of high alumina coal power generation → generation aluminous fly-ash → extraction aluminium oxide → production electrolytic aluminium, exploitation give full play to business excellence to extract alumina production line and this type of enterprise is had the needs of reality and the urgency of industry by method.
At present, the technology utilizing flyash production aluminium oxide is a lot, for instance limestone sintering process, soda lime sintering process, the acid-hatching of young eggs, ammonium sulfate sintering process, using acid and alkali combination method etc..Wherein sintering process mainly includes limestone sintering process and soda lime sintering process, and its common limitation is in that energy consumption is high, and cost is high.
Summary of the invention
The present invention is directed to prior art Problems existing, it is provided that a kind of application shaft furnace is sintered, it is achieved the method for aluminous fly-ash low-energy consumption extracting aluminium oxide and production line.
For this, the present invention adopts the following technical scheme that a kind of method that flyash based on lime sinter process extracts aluminium oxide, and step is as follows: (1) grinding batch mixing: mixed with enough Calx by flyash, abrasive material, and mixed material powder is not more than 200 orders；Added amount of lime makes after batch mixing CaO and SiO in material according to flyash material composition2Mol ratio be 2:1, CaO and Al2O3Mol ratio be 1:1；
(2) raw material ball: mixed with the slaked lime solution that mass concentration is 5%-6% by described the joined mixed material of (1) step, adopts high frequency vibrating pressure agglomerate balling-up legal system ball and makes aluminous fly-ash sintering bead through cold drying；Described aluminous fly-ash sintering bead granularity 3-8mm, moisture is lower than 6%；
(3) shaft roasting: described aluminous fly-ash is sintered bead at shaft furnace uniform distribution, through super-dry, preheating, roasting, soaking, five stages of cooling, raw material ball roasting maturation pellet；Described sintering temperature 1300 DEG C-1450 DEG C, controls roasting time 30-50 minute；
(4) cool down from efflorescence: first grog is incubated 20-30 minute when being cooled to 500-550 DEG C in efflorescence cooling device, chilling after being subsequently cooled to less than 400 DEG C, then with standardization sieve screening, remove the caking that sintering is bad；
(5) dissolution: dissolution in the aluminous fly-ash grog sodium carbonate liquor of efflorescence；Leaching temperature is 60-75 DEG C；Contained Na in sodium carbonate liquor2CO3With Al in grog2O3Mol ratio is more than 2:1；Dissolution time is 30-45 minute；Obtain dissolution serosity and the thick slag of dissolution；
(6) separate and washing: utilizing precipitation separation tank to separate in dissolution serosity (5), the thick slag of dissolution carries out continuous several times back flush trough washery；The dissolution serosity time of staying in subsider is 4-8h, processing temperature 90-105 DEG C；The back flush number of times of dissolution thick slag 3-5 time；
(7) carbonization is decomposed: to after (6) settlement separate containing crude liquor of sodium aluminate passes into C02So that it is in most of soluble aluminum be converted into aluminum hydroxide precipitate；Passed into C02Volumetric concentration be 30%-50%, reaction temperature is 60-100 DEG C, and the response time is 2h-4h；
(8) filtering: by carbonization decomposition nut liquid through being filtrated to get aluminium hydroxide and sodium carbonate liquor two parts, sodium carbonate liquor is recycled；
(9) low temperature Bayer process processes: (8) step is filtrated to get aluminium hydroxide, carries out low temperature bayer process process with circulation alkali solution, obtain metallurgical grade sandy alumina and high white residue.
Further, the calcium silicate slag that (6) step produces is for producing cement.
Further, the C0 that (7) step adds2It is that (3) step produces and the C0 of purified process2。
Preferably, step (7) carbonization carries out when decomposing under agitation.
(8) described step is filtrated to get the A/S of aluminium hydroxide is 65-75.
Described step is described low temperature Bayer process flow process (9), including the evaporation of raw ore slurry allotment, low temperature dissolution, red mud separating, washing, decomposing sodium aluminate solution, aluminium hydroxide separating, washing, Aluminium hydroxide roasting and circulation alkali liquor and allotment operation.
The invention has the beneficial effects as follows: major downside is that energy consumption is high due to limestone sintering process, and the shaft furnace that employs of novelty of the present invention is sintered, make the method sintering energy consumption compared with traditional limestone sintering process that (shaft furnace and other type of furnace phase specific energy consumption be minimum) is greatly reduced on the one hand, hence it is evident that to be beneficial to reduction production cost；On the other hand, shaft furnace high temperature and the big feature of yield so that the method easily realizes the sintering under high temperature, extensive operating mode, has not only ensured the sintering quality of product, and suitable large-scale industrial production；Additionally, shaft furnace simple in construction, equipment and technology is ripe so that the method investment intensity is low, it is easy to industrialization.
Accompanying drawing explanation
Fig. 1: the production line composition diagram of the present invention；
Fig. 2: the process chart of the present invention.
Detailed description of the invention
Below in conjunction with specific embodiment, the present invention is further illustrated.The present invention is further described below in conjunction with specific embodiment.
Aluminous fly-ash used by instantiation becomes to be grouped into as shown in table 1.
Aluminous fly-ash composition (%) used in table 1 example
Embodiment 1
(1) grinding batch mixing: flyash 80Kg and Calx 146Kg add batch mixer (ball mill) interior grinding batch mixing, mixed material grinding is to 200 orders；
(2) raw material ball: by described the joined compound of (1) step and slaked lime (bonding agent) weak solution (mass concentration is 5%-6%), adopts high frequency vibrating pressure agglomerate balling-up legal system ball, and makes aluminous fly-ash sintering bead through cold drying；Gained aluminous fly-ash sintering bead granularity 4-8mm, moisture is lower than 6%；
(3) shaft roasting: described aluminous fly-ash is sintered bead at shaft furnace uniform distribution, through super-dry, preheating, roasting, soaking, five stages of cooling, raw material ball roasting maturation pellet；Described sintering temperature 1300 DEG C-1450 DEG C, roasting time 40 minutes；
(4) cool down from efflorescence: first grog is incubated 20-30 minute when being cooled to 500-550 DEG C in efflorescence cooling device, chilling after being subsequently cooled to less than 400 DEG C, then with standardization sieve screening, remove the caking that sintering is bad；
(5) dissolution: from the dissolution in sodium carbonate liquor under churned mechanically operating mode of the aluminous fly-ash grog of efflorescence；Best leaching temperature is 60-75 DEG C；Na in sodium carbonate liquor2CO3With Al in grog2O3Mol ratio is more than 2:1；Best dissolution time is 30-45 minute；
(6) separate and washing: thick to Clinker digestion serosity and dissolution slag utilizes the flow process of precipitation separation tank+continuous several times back flush groove be easily separated and wash；The described serosity time of staying in subsider is 4-8h, processing temperature 90-105 DEG C；The back flush number of times of the thick slag of described dissolution: 3-5 time；The calcium silicate slag separating, washing generation is used for producing cement；
(7) carbonization is decomposed: passes into step in the thick liquid containing sodium aluminate after settlement separate and (3) produces and the C0 of purified process2So that it is in most of soluble aluminum be converted into the process of aluminum hydroxide precipitate；C0 used2Volumetric concentration is 30%-50%, and reaction temperature is 60-100 DEG C, and the response time is 2h-4h, and carries out under agitation；
(8) filtering: by carbonization decomposition nut liquid through being filtrated to get aluminium hydroxide and sodium carbonate liquor two parts, wherein said sodium carbonate liquor is used for step dissolution (5) after evaporation and concentration；
(9) low temperature Bayer process processes: will be filtrated to get the aluminium hydroxide that A/S is about 70, and carry out low temperature bayer process process with circulation alkali solution, and obtain metallurgical grade sandy alumina and high white residue.Described low temperature Bayer process flow process, including the evaporation of raw ore slurry allotment, low temperature dissolution, red mud separating, washing, decomposing sodium aluminate solution, aluminium hydroxide separating, washing, Aluminium hydroxide roasting and circulation alkali liquor and allotment operation.Obtain sandy alumina 25.1Kg, alumina extraction ratio 69.47%.
Embodiment 2
(1) grinding batch mixing: flyash 60Kg and Calx 110Kg add batch mixer (ball mill) interior grinding batch mixing, mixed material grinding is to 200 orders；
(2) raw material ball: by described the joined compound of (1) step and slaked lime (bonding agent) weak solution (mass concentration is 5%-6%), adopts high frequency vibrating pressure agglomerate balling-up legal system ball, and makes aluminous fly-ash sintering bead through cold drying；Gained aluminous fly-ash sintering bead granularity 4-8mm, moisture is lower than 6%；
(3) shaft roasting: described aluminous fly-ash is sintered bead at shaft furnace uniform distribution, through super-dry, preheating, roasting, soaking, five stages of cooling, raw material ball roasting maturation pellet；Described sintering temperature 1300 DEG C-1450 DEG C, roasting time 40 minutes；
(4) cool down from efflorescence: first grog is incubated 20-30 minute when being cooled to 500-550 DEG C in efflorescence cooling device, chilling after being subsequently cooled to less than 400 DEG C, then with standardization sieve screening, remove the caking that sintering is bad；
(5) dissolution: from the dissolution in sodium carbonate liquor under churned mechanically operating mode of the aluminous fly-ash grog of efflorescence；Best leaching temperature is 60-75 DEG C；Na in sodium carbonate liquor2CO3With Al in grog2O3Mol ratio is more than 2:1；Best dissolution time is 30-45 minute；
(6) separate and washing: thick to Clinker digestion serosity and dissolution slag utilizes the flow process of precipitation separation tank+continuous several times back flush groove be easily separated and wash；The described serosity time of staying in subsider is 4-8h, processing temperature 90-105 DEG C；The back flush number of times of the thick slag of described dissolution: 3-5 time；The calcium silicate slag separating, washing generation is used for producing cement；
(7) carbonization is decomposed: passes into step in the thick liquid containing sodium aluminate after settlement separate and (3) produces and the C0 of purified process2So that it is in most of soluble aluminum be converted into the process of aluminum hydroxide precipitate；C0 used2Volumetric concentration is 30%-50%, and reaction temperature is 60-100 DEG C, and the response time is 2h-4h, and carries out under agitation；
(8) filtering: by carbonization decomposition nut liquid through being filtrated to get aluminium hydroxide and sodium carbonate liquor two parts, wherein said sodium carbonate liquor is used for step dissolution (5) after evaporation and concentration；
(9) low temperature Bayer process processes: will be filtrated to get the aluminium hydroxide that A/S is about 70, and carry out low temperature bayer process process with circulation alkali solution, and obtain metallurgical grade sandy alumina and high white residue.Described low temperature Bayer process flow process, including the evaporation of raw ore slurry allotment, low temperature dissolution, red mud separating, washing, decomposing sodium aluminate solution, aluminium hydroxide separating, washing, Aluminium hydroxide roasting and circulation alkali liquor and allotment operation.Obtain sandy alumina 19.26Kg, alumina extraction ratio 71.08%.
Claims (6)
1. the method that the flyash based on lime sinter process extracts aluminium oxide, it is characterised in that step is as follows: (1) grinding batch mixing: mixed with enough Calx by flyash, abrasive material, and mixed material powder is not more than 200 orders；Added amount of lime makes after batch mixing CaO and SiO in material according to flyash material composition2Mol ratio be 2:1, CaO and Al2O3Mol ratio be 1:1；
(2) raw material ball: mixed with the slaked lime solution that mass concentration is 5%-6% by described the joined mixed material of (1) step, adopts high frequency vibrating pressure agglomerate balling-up legal system ball and makes aluminous fly-ash sintering bead through cold drying；Described aluminous fly-ash sintering bead granularity 3-8mm, moisture is lower than 6%；
(3) shaft roasting: described aluminous fly-ash is sintered bead at shaft furnace uniform distribution, through super-dry, preheating, roasting, soaking, five stages of cooling, raw material ball roasting maturation pellet；Described sintering temperature 1300 DEG C-1450 DEG C, controls roasting time 30-50 minute；
(4) cool down from efflorescence: first grog is incubated 20-30 minute when being cooled to 500-550 DEG C in efflorescence cooling device, chilling after being subsequently cooled to less than 400 DEG C, then with standardization sieve screening, remove the caking that sintering is bad；
(5) dissolution: dissolution in the aluminous fly-ash grog sodium carbonate liquor of efflorescence；Leaching temperature is 60-75 DEG C；Contained Na in sodium carbonate liquor2CO3With Al in grog2O3Mol ratio is more than 2:1；Dissolution time is 30-45 minute；Obtain dissolution serosity and the thick slag of dissolution；
(6) separate and washing: utilizing precipitation separation tank to separate in dissolution serosity (5), the thick slag of dissolution carries out continuous several times back flush trough washery；The dissolution serosity time of staying in subsider is 4-8h, processing temperature 90-105 DEG C；The back flush number of times of dissolution thick slag 3-5 time；
(7) carbonization is decomposed: to after (6) settlement separate containing crude liquor of sodium aluminate passes into C02So that it is in most of soluble aluminum be converted into aluminum hydroxide precipitate；Passed into C02Volumetric concentration be 30%-50%, reaction temperature is 60-100 DEG C, and the response time is 2h-4h；
(8) filtering: by carbonization decomposition nut liquid through being filtrated to get aluminium hydroxide and sodium carbonate liquor two parts, sodium carbonate liquor is recycled；
(9) low temperature Bayer process processes: (8) step is filtrated to get aluminium hydroxide, carries out low temperature bayer process process with circulation alkali solution, obtain metallurgical grade sandy alumina and high white residue.
2. the method that the flyash based on lime sinter process according to claim 1 extracts aluminium oxide, it is characterised in that the calcium silicate slag that (6) step produces is for producing cement.
3. the method that the flyash based on lime sinter process according to claim 1 extracts aluminium oxide, it is characterised in that the C0 that (7) step adds2It is that (3) step produces and the C0 of purified process2。
4. the method that the flyash based on lime sinter process according to claim 1 extracts aluminium oxide, it is characterised in that step (7) carbonization carries out when decomposing under agitation.
5. the method that the flyash based on lime sinter process according to claim 1 extracts aluminium oxide, it is characterised in that (8) step is filtrated to get the A/S of aluminium hydroxide is 65-75.
6. the method that the flyash based on lime sinter process according to claim 1 extracts aluminium oxide, it is characterized in that, step is described low temperature Bayer process flow process (9), including the evaporation of raw ore slurry allotment, low temperature dissolution, red mud separating, washing, decomposing sodium aluminate solution, aluminium hydroxide separating, washing, Aluminium hydroxide roasting and circulation alkali liquor and allotment operation.
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| CN201610149727.5A CN105753024A (en) | 2016-03-16 | 2016-03-16 | Method for extracting aluminum oxide from coal ash on basis of lime sinter process |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107935005A (en) * | 2016-10-12 | 2018-04-20 | 北京矿冶研究总院 | Method for pretreating fly ash carbonate solution and extracting alumina |
| CN113753929A (en) * | 2021-08-26 | 2021-12-07 | 王俊 | Method for preparing high-whiteness aluminum hydroxide and silicon fertilizer from high-alumina fly ash |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1644506A (en) * | 2004-11-12 | 2005-07-27 | 内蒙古蒙西高新技术集团有限公司 | Method for combination producing alumina and cement from chalk and flyash |
| CN2878353Y (en) * | 2006-09-13 | 2007-03-14 | 内蒙古蒙西高新技术集团有限公司 | Device for producing alumina self-pulverization grog by fusion method |
| CN101058431A (en) * | 2007-01-26 | 2007-10-24 | 长安大学 | Method of extracting aluminum oxide |
-
2016
- 2016-03-16 CN CN201610149727.5A patent/CN105753024A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1644506A (en) * | 2004-11-12 | 2005-07-27 | 内蒙古蒙西高新技术集团有限公司 | Method for combination producing alumina and cement from chalk and flyash |
| CN2878353Y (en) * | 2006-09-13 | 2007-03-14 | 内蒙古蒙西高新技术集团有限公司 | Device for producing alumina self-pulverization grog by fusion method |
| CN101058431A (en) * | 2007-01-26 | 2007-10-24 | 长安大学 | Method of extracting aluminum oxide |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107935005A (en) * | 2016-10-12 | 2018-04-20 | 北京矿冶研究总院 | Method for pretreating fly ash carbonate solution and extracting alumina |
| CN107935005B (en) * | 2016-10-12 | 2019-09-10 | 北京矿冶研究总院 | Method for pretreating fly ash carbonate solution and extracting alumina |
| CN113753929A (en) * | 2021-08-26 | 2021-12-07 | 王俊 | Method for preparing high-whiteness aluminum hydroxide and silicon fertilizer from high-alumina fly ash |
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Application publication date: 20160713 |