CN102476820A - Method for extracting alumina from coal ash through wet process - Google Patents
Method for extracting alumina from coal ash through wet process Download PDFInfo
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Abstract
The invention provides a method for extracting alumina from coal ash through a wet process. The method comprises the following steps: 1, mixing the coal ash, calcium oxide and an alkaline solution, reacting, carrying out flash evaporation, and filtering to obtain an alkaline solution containing sodium aluminate and aluminum removed slag; 2, cooling and crystallizing the alkaline solution obtained in step 1 to obtain a coarse hydrated sodium aluminate crystal and a crystallization mother solution; 3, circulatingly applying the crystallization mother solution obtained in step 2 to a leaching reaction, dissolving the coarse hydrated sodium aluminate crystal with water or a diluted alkaline solution, carrying out silicon removal and seed decomposition to obtain aluminum hydroxide, and calcining aluminum hydroxide to obtain alumina; 4, evaporating the seed-decomposed mother solution, and mixing the evaporated seed-decomposed mother solution with the alkaline solution obtained in the step 1; and 5, carrying out hydrolysis sodium removal on the aluminum removed slag obtained in the step 1 in the diluted alkaline solution, filter-separating, and carrying out multistage countercurrent washing on the sodium removed slag. According to the method, the dissolving-out temperature and the dissolving-out pressure are low, the dissolving-out rate of alumina can reach above 90%, and the content of sodium oxide in the sodium removed slag is less than 1%.
Description
Technical field
A kind of from flyash extraction method of alumina, particularly a kind of wet method reclaims method of alumina from flyash.
Background technology
At present, the production of aluminum oxide mainly is that raw material adopts alkaline process production with bauxite, comprises Bayer process, sintering process and integrated process.China has become alumina producing big country, but the bauxite resource degree of protection is low, and resource problem has become the main bottleneck of China's aluminum oxide industry Sustainable development.
Flyash is one of solid waste that produces behind the coal burning, adds up volume of cargo in storage at present and has reached 2,000,000,000 tons.Development and use flyash is produced aluminum oxide, all has great importance undoubtedly to solving China's bauxite resource problem of environmental pollution in short supply and coal-fired.
Be that the technology that raw material extracts aluminum oxide has the series of patents application with flyash.These technology are broadly divided into two types; One type is alkaline process high-temperature roasting activation; Like a kind of method (patent No. ZL03131079.6) of utilizing fly-ash Preparation aluminum and coproducing cement grog of Mengxi Hi-Tech Group Corp., Ltd., Inner Mongolia's invention, sintering temperature is more than 1300 ℃, so energy consumption is very high; And when sintering, also need add a large amount of quicklime, cause the level of residue that extracts behind the aluminum oxide big.Another kind of is the acid system pyrolytic decomposition, like a kind of method (number of patent application 200810011311.2) of utilizing fly-ash Preparation Tai-Ace S 150 of Shenyang Aluminium Magnesium Design & Research Inst's invention, behind the flyash mechanical activation, adopts the vitriol oil to decompose about 200 ℃ of decomposition temperatures.The subject matter of acidic process flyash is that corrosive medium is strong, and equipment material is required height, and spent acid recovery difficulty, causes secondary pollution easily.Just because of the existence of the problems referred to above, restricted flyash and extracted the technological commercial application of aluminum oxide.So far do not find to prepare the document and the granted patent of aluminum oxide series compound as yet about flyash alkaline process low temperature.
Summary of the invention
High-temperature operation when the objective of the invention is to overcome high-temperature sintering process and handling flyash and the energy consumption that causes is high, operational difficulty and acid system equipment corrosion are serious, the defective that has secondary pollution hidden danger; Provide low temperature wet method under a kind of alkaline medium from aluminous fly-ash, to extract the novel method of aluminum oxide; Digesting efficiency of alumina is high; Level of residue is little, and residue detrimental impurity content is low, is prone to realize the recycling of waste.
The method of alumina of from flyash, extracting provided by the invention, its step is following:
(1) batching: with flyash, quicklime and mass percent concentration is that the NaOH alkaline solution of 30%-50% mixes and joins in the reactor drum; Alkaline solution and flyash quality proportioning (8-25): 1, the mass ratio of quicklime and flyash is (0.35-0.50): 1;
(2) reaction: the material that step (1) is obtained leaches reaction in reactor drum, temperature is 180-300 ℃, and extraction time 0.2-10h leaches pressure 0.4-6.2MPa, leaches to obtain slip after reaction is accomplished; With this slurry filtration, obtain containing the alkali lye and the dealuminzation slag of sodium aluminate;
(3) crystallization: the alkali lye that contains sodium aluminate adds crystal seed 50-100 ℃ of following crystallization, obtains aluminate hydrates sodium coarse-grain and crystalline mother solution, and the crystalline mother solution circulation is used for leaching reaction;
(4) purification and decomposition: aluminate hydrates sodium coarse-grain water or sig water dissolving with step (3) obtains, obtain white lake through desiliconization, seed operation splitting then, with the white lake calcining that obtains, just make aluminum oxide again;
(5) evaporative crystallization: it is 520-600g/L that the seed decomposition nut liquid that step (4) is obtained is evaporated to sodium oxide concentration; Add crystal seed then and under 50-100 ℃, carry out crystallization reaction; Or join in step (2) the gained sodium aluminate solution and carry out crystallization reaction together, crystalline mother solution is used for leaching reaction; Mix with step (4) gained desiliconization sodium aluminate solution sodium aluminate crystallization dissolving back, carries out seed and decompose;
(6) take off sodium: the dealuminzation slag that step (2) is obtained joins in the dilute alkaline soln; Add quicklime simultaneously and take off the sodium reaction; Sig water concentration is 0-80g/L, and the quicklime add-on is the 0-30% of dealuminzation slag amount, and liquid-solid mass ratio is (6-10): 1; Taking off the sodium temperature is 80-180 ℃, and the reaction times is 0.5-10h;
(7) washing: take off sodium slag water and carry out repeatedly countercurrent washing, wash temperature is 50-95 ℃, and its washings is used for step (3) or the macrocrystalline dissolving of step (5) aluminate hydrates sodium, takes off the sodium slag after the washing as the raw material of producing material of construction;
Described alkaline solution is the NaOH aqueous solution;
The extraction time of said leaching reaction is that 0.5-3h is good;
The said concentration of lye that takes off the sodium reaction is that 40-70g/L is good;
It is good that said temperature of reaction of taking off the sodium reaction is 80-95 ℃.
Method of alumina has following obviously meliority in the recovery flyash provided by the invention:
(1) the present invention adopts the low temperature alkaline process to handle flyash, and extraction temperature is 180-300 ℃, and the higher temperatures sintering process reduces 900-1000 ℃, and leaching process is carried out under mesolow, can significantly cut down the consumption of energy; Significantly reduce corrosion on Equipment property than acid system;
(2) the present invention leaches the reaction digesting efficiency of alumina up to more than 95%, and resource utilization is high;
(3) there is not a large amount of concentration and evaporations in processes such as high high alkali liquid circulation, purification, separation among the present invention, greatly reduce production energy consumption, have simplified production technique, have reduced the equipment input, have improved industrial operability, have reduced production cost;
(4) reaction conditions of the present invention is gentle, and industry is workable.
Description of drawings
Fig. 1 has provided the alumina technology route map in the low temperature hydrometallurgic recovery flyash.
Embodiment
Embodiment 1
With the aluminum oxide in the low temperature hydrometallurgic recovery flyash provided by the invention, be example with somewhere, Inner Mongol flyash, the percentage composition of this flyash principal element oxide compound is following:
Al
2O
3SiO
2Fe
2O
3CaO TiO
2Na
2O H
2O igloss A/S
41.41?39.54?2.40 3.67?1.38?0.21?6.1?2.81?1.05
Its recovering step is:
With flyash and mass percent is that 50% NaOH solution mixes and is placed in the reaction kettle, and alkaline solution and flyash quality proportioning are 10.3: 1, and the quicklime addition is 50% of a flyash quality; Be warming up to 260 ℃; Reaction 1h under 1.6MPa obtains containing the reaction product mixture of the alkali lye and the dealuminzation slag of sodium aluminate, and reaction product to be mixed is filtered after being cooled to 100 ℃; Separate the alkaline solution and the dealuminzation slag that obtain containing sodium aluminate; A/S=0.23 (A is an aluminum oxide quality per-cent, and S is a siliconoxide mass per-cent) in this moment dealuminzation slag, the recovery of aluminum oxide is 81.82% in the flyash.
The sodium aluminate alkali solution (filtrated stock) that contains that obtains is put into crystallization reactor; 50 ℃, add crystallization 6h under the situation of 5% crystal seed; The crystalline mother solution causticity ratio that filtration obtains is elevated to 28; The causticity ratio of aluminate hydrates sodium crystal is 1.35, then to the aluminate hydrates sodium crystal dissolve, desiliconization, kind branch, calcining can make sandy alumina.
The dealuminzation slag adds water and under 150 ℃, carries out dealkalize, and liquid-solid mass ratio is 10: 1, does not add quicklime, reaction 10h, and solid phase is through countercurrent washing after the dealkalize, and wash temperature is 90 ℃.Sodium oxide content is 0.86% in the residue.
Embodiment 2
The flyash of embodiment 1 mixed being placed in the reaction kettle with crystalline mother solution among the embodiment 1, mother liquor and flyash quality proportioning are 12.98: 1, and the quicklime addition is 35% of a flyash quality; Be warming up to 300 ℃; React 2h, obtain containing the reaction product mixture of alkali lye, sodium aluminate and dealuminzation slag, carry out suction filtration after reaction product to be mixed is cooled to 100 ℃; Separate the alkaline solution and the dealuminzation slag that obtain containing sodium aluminate; A/S=0.02 (A is an aluminum oxide quality per-cent, and S is a siliconoxide mass per-cent) in this moment dealuminzation slag, the recovery of aluminum oxide is 98% in the flyash.
The sodium aluminate alkali solution (filtrated stock) that contains that obtains is put into crystallization reactor; 100 ℃, add crystallization 10h under the situation of 8% crystal seed; The crystalline mother solution causticity ratio that filtration obtains is elevated to 25; The causticity ratio of aluminate hydrates sodium crystal is 1.58, then to the aluminate hydrates sodium crystal dissolve, desiliconization, kind branch, calcining can make sandy alumina.
The dealuminzation slag joins in the sodium hydroxide solution of 40g/L, under 80 ℃, carries out dealkalize, and liquid-solid mass ratio 6: 1 adds 10% quicklime, reaction 10h, and solid phase is through countercurrent washing after the dealkalize, and wash temperature is 90 ℃.Sodium oxide content is 0.98% in the residue.
Embodiment 3
With the flyash of embodiment 1 and mass percent is that 30% NaOH solution mixes and is placed in the reaction kettle, and alkaline solution and flyash quality proportioning are 17.45: 1, and the quicklime addition is 60% of a flyash quality; Be warming up to 300 ℃; Reaction 0.5h under 6.2MPa obtains containing the reaction product mixture of the alkali lye and the dealuminzation slag of sodium aluminate, carries out suction filtration after reaction product to be mixed is cooled to 100 ℃; Separate the alkaline solution and the dealuminzation slag that obtain containing sodium aluminate; A/S=0.35 (A is an aluminum oxide quality per-cent, and S is a siliconoxide mass per-cent) in this moment dealuminzation slag, the recovery of aluminum oxide is 66.67% in the flyash.
The sodium aluminate alkali solution (filtrated stock) that contains that obtains is put into crystallization reactor; 60 ℃, add under the situation of 5% crystal seed behind the crystallization 3h; The crystalline mother solution causticity ratio that filtration obtains is elevated to 25; The causticity ratio of aluminate hydrates sodium crystal is 1.60, then to the aluminate hydrates sodium crystal dissolve, desiliconization, kind branch, calcining can make sandy alumina.
The dealuminzation slag joins in the sodium hydroxide solution of 60g/L, under 80 ℃, carries out dealkalize, and liquid-solid mass ratio 10: 1 adds 30% quicklime, reaction 10h, and solid phase is through countercurrent washing after the dealkalize, and wash temperature is 90 ℃.Sodium oxide content is 0.98% in the residue.
Embodiment 4
From flyash, extracting method of alumina with low temperature wet method of the present invention, is the extraction that raw material carries out aluminum oxide with another regional flyash of Inner Mongol, and the percentage composition of this flyash principal element oxide compound is following:
Al
2O
3SiO
2Fe
2O
3CaO TiO
2Na
2O H
2O igloss A/S
48.02?36.38?1.05 2.56?1.40?0.16?5.9?2.57?1.32
With flyash and mass percent is that 45% NaOH solution mixes and is placed in the reaction kettle, and alkaline solution and flyash quality proportioning are 8: 1, and the quicklime addition is 40% of a flyash quality; Be warming up to 300 ℃, reaction 0.5h under 3.1MPa obtains containing the reaction product mixture of the alkali lye and the dealuminzation slag of sodium aluminate; After reaction product to be mixed is cooled to 100 ℃; Carry out suction filtration, separate alkaline solution and the dealuminzation slag obtain containing sodium aluminate, at this moment in the dealuminzation slag A/S=0.08 (A is an aluminum oxide quality per-cent; S is a siliconoxide mass per-cent), the recovery of aluminum oxide is 93.94% in the flyash.
The sodium aluminate alkali solution (filtrated stock) that contains that obtains is put into crystallization reactor; 60 ℃, add under the situation of 5% crystal seed behind the crystallization 6h; The crystalline mother solution causticity ratio that filtration obtains is elevated to 26; The causticity ratio of aluminate hydrates sodium crystal is 1.36, then to the aluminate hydrates sodium crystal dissolve, desiliconization, kind branch, calcining can make sandy alumina.
The dealuminzation slag adds water and under 180 ℃, carries out dealkalize, and liquid-solid mass ratio 10: 1 does not add quicklime, reaction 0.5h, and solid phase is through countercurrent washing after the dealkalize, and wash temperature is 90 ℃.Sodium oxide content is 0.93% in the residue.
Embodiment 5
The flyash of embodiment 4 mixed being placed in the reaction kettle with embodiment 4 crystalline mother solutions, mother liquor and flyash quality proportioning are 25: 1, and the quicklime addition is 35% of a flyash quality; Be warming up to 180 ℃, reaction 10h under 0.4MPa obtains containing the reaction product mixture of the alkali lye and the dealuminzation slag of sodium aluminate; After reaction product to be mixed is cooled to 100 ℃; Carry out suction filtration, separate alkaline solution and the dealuminzation slag obtain containing sodium aluminate, at this moment in the dealuminzation slag A/S=0.07 (A is an aluminum oxide quality per-cent; S is a siliconoxide mass per-cent), the recovery of aluminum oxide is 94.66% in the flyash.
The sodium aluminate alkali solution (filtrated stock) that contains that obtains is put into crystallization reactor; 60 ℃, add under the situation of 5% crystal seed behind the crystallization 6h; The crystalline mother solution causticity ratio that filtration obtains is elevated to 24; The causticity ratio of aluminate hydrates sodium crystal is 1.30, then to the aluminate hydrates sodium crystal dissolve, desiliconization, kind branch, calcining can make sandy alumina.
The dealuminzation slag adds in the sodium hydroxide solution of 40g/L, under 150 ℃, carries out dealkalize, and liquid-solid mass ratio 10: 1 does not add quicklime, reaction 6h, and solid phase is through countercurrent washing after the dealkalize, and wash temperature is 90 ℃.Sodium oxide content is 0.89% in the residue.
Claims (2)
1. a wet method is extracted method of alumina from flyash, may further comprise the steps:
(1) batching: with flyash, quicklime and mass percent concentration is that the NaOH alkaline solution of 30%-50% mixes and joins in the reactor drum; Alkaline solution and flyash quality proportioning (8-25): 1, the mass ratio of quicklime and flyash is (0.35-0.50): 1;
(2) reaction: the material that step (1) is obtained leaches reaction in reactor drum, temperature is 180-300 ℃, and extraction time 0.2-10h leaches pressure 0.4-6.2MPa, leaches to obtain slip after reaction is accomplished; With this slurry filtration, obtain containing the alkaline solution and the dealuminzation slag of sodium aluminate;
(3) crystallization: the alkaline solution cooling that contains sodium aluminate with step (2) obtains, add crystal seed 50-100 ℃ of following crystallization, obtain aluminate hydrates sodium coarse-grain and crystalline mother solution, the crystalline mother solution circulation is used for leaching reaction;
(4) purification and decomposition: aluminate hydrates sodium coarse-grain water or sig water dissolving with step (3) obtains, obtain white lake through desiliconization, seed operation splitting then, with the white lake calcining that obtains, just make aluminum oxide again;
(5) evaporative crystallization: it is 520-600g/L that the seed decomposition nut liquid that step (4) is obtained is evaporated to sodium oxide concentration; Add crystal seed then and under 50-100 ℃, carry out crystallization reaction; Or join in step (2) the gained sodium aluminate solution and carry out crystallization reaction together, crystalline mother solution is used for leaching reaction; Mix with step (4) gained desiliconization sodium aluminate solution sodium aluminate crystallization dissolving back, carries out seed and decompose;
(6) take off sodium: the dealuminzation slag that step (2) is obtained joins and takes off the sodium reaction in the dilute alkaline soln; Sig water concentration is 0-80g/L, and the quicklime add-on is the 0-30% of dealuminzation slag amount, and liquid-solid mass ratio is (6-10): 1; Temperature of reaction 80-180 ℃, reaction times 0.5-10h;
(7) washing: take off sodium slag water and carry out repeatedly countercurrent washing, wash temperature is 50-95 ℃, and its washings is used for step (3) or the macrocrystalline dissolving of step (5) aluminate hydrates sodium, takes off the sodium slag after the washing as the raw material of producing material of construction.
2. method according to claim 1 is characterized in that, the reaction pressure of taking off the sodium reaction is 0-0.9MPa.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103553100A (en) * | 2013-11-19 | 2014-02-05 | 南京天华化学工程有限公司 | Method for extracting aluminum oxide from coal ash through hot-wall reaction |
| CN103663516A (en) * | 2012-09-26 | 2014-03-26 | 中国科学院过程工程研究所 | Method for preparing aluminum hydroxide by utilizing high-alumina coal ash |
| CN103803613A (en) * | 2012-11-06 | 2014-05-21 | 贵阳铝镁设计研究院有限公司 | Method using high temperature activation-high pressure water chemical method to treat fly ash to produce alumina |
| CN104140121A (en) * | 2013-05-09 | 2014-11-12 | 中国科学院过程工程研究所 | Method for preparing sodium aluminate solution from coal-series kaolinite or coal gangue used as raw material |
| CN104445310A (en) * | 2013-09-25 | 2015-03-25 | 贵阳铝镁设计研究院有限公司 | Novel process for treating middle-low bauxite in complete wet method alkali system |
| CN106145169A (en) * | 2015-04-09 | 2016-11-23 | 中国科学院过程工程研究所 | A kind of method of wet underwater welding aluminium oxide from aluminous fly-ash |
| CN107760865A (en) * | 2016-08-17 | 2018-03-06 | 中国科学院过程工程研究所 | A kind of method of the dipped journey leachate gallium lithium ion enrichment of coal ash alkali |
| CN108529658A (en) * | 2018-07-05 | 2018-09-14 | 郑州中科新兴产业技术研究院 | A method of recycling aluminium hydroxide from aluminium ash |
| CN108622920A (en) * | 2018-05-30 | 2018-10-09 | 大唐国际发电股份有限公司高铝煤炭资源开发利用研发中心 | A kind of method of aluminous fly-ash extraction aluminium oxide |
| CN109369286A (en) * | 2018-09-18 | 2019-02-22 | 华南理工大学 | It is a kind of using flyash produce in microelement acidic soil conditioner method and product |
| CN112573552A (en) * | 2020-12-27 | 2021-03-30 | 中南大学 | Method for preparing boehmite by using high-silicon aluminum-containing material |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1565974A (en) * | 2003-06-24 | 2005-01-19 | 中国科学院过程工程研究所 | Normal pressure low temperature leaching production method for alumina |
| CN101857250A (en) * | 2009-04-09 | 2010-10-13 | 刘庆玲 | Process for producing aluminium hydroxide, silicic acid and sodium carbonate by utilizing fly ash |
-
2010
- 2010-11-25 CN CN201010565571.1A patent/CN102476820B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1565974A (en) * | 2003-06-24 | 2005-01-19 | 中国科学院过程工程研究所 | Normal pressure low temperature leaching production method for alumina |
| CN101857250A (en) * | 2009-04-09 | 2010-10-13 | 刘庆玲 | Process for producing aluminium hydroxide, silicic acid and sodium carbonate by utilizing fly ash |
Non-Patent Citations (2)
| Title |
|---|
| MATJIE, RH等: "Extraction of alumina from coal fly ash generated from a selected low rank bituminous South African coal", 《MINERALS ENGINEERING》 * |
| 张亚莉: "钠硅渣湿法处理工艺与理论研究", 《中国优秀博硕士学位论文全文数据库(硕士)工程科技Ⅰ辑》 * |
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| CN103663516B (en) * | 2012-09-26 | 2015-08-19 | 中国科学院过程工程研究所 | A kind of method utilizing aluminous fly-ash to prepare aluminium hydroxide |
| CN103803613A (en) * | 2012-11-06 | 2014-05-21 | 贵阳铝镁设计研究院有限公司 | Method using high temperature activation-high pressure water chemical method to treat fly ash to produce alumina |
| CN104140121A (en) * | 2013-05-09 | 2014-11-12 | 中国科学院过程工程研究所 | Method for preparing sodium aluminate solution from coal-series kaolinite or coal gangue used as raw material |
| CN104445310A (en) * | 2013-09-25 | 2015-03-25 | 贵阳铝镁设计研究院有限公司 | Novel process for treating middle-low bauxite in complete wet method alkali system |
| CN103553100A (en) * | 2013-11-19 | 2014-02-05 | 南京天华化学工程有限公司 | Method for extracting aluminum oxide from coal ash through hot-wall reaction |
| CN106145169A (en) * | 2015-04-09 | 2016-11-23 | 中国科学院过程工程研究所 | A kind of method of wet underwater welding aluminium oxide from aluminous fly-ash |
| CN106145169B (en) * | 2015-04-09 | 2018-02-13 | 中国科学院过程工程研究所 | A kind of method of the wet underwater welding aluminum oxide from aluminous fly-ash |
| CN107760865A (en) * | 2016-08-17 | 2018-03-06 | 中国科学院过程工程研究所 | A kind of method of the dipped journey leachate gallium lithium ion enrichment of coal ash alkali |
| CN108622920A (en) * | 2018-05-30 | 2018-10-09 | 大唐国际发电股份有限公司高铝煤炭资源开发利用研发中心 | A kind of method of aluminous fly-ash extraction aluminium oxide |
| CN108529658A (en) * | 2018-07-05 | 2018-09-14 | 郑州中科新兴产业技术研究院 | A method of recycling aluminium hydroxide from aluminium ash |
| CN108529658B (en) * | 2018-07-05 | 2020-08-07 | 郑州中科新兴产业技术研究院 | Method for recovering aluminum hydroxide from aluminum ash |
| CN109369286A (en) * | 2018-09-18 | 2019-02-22 | 华南理工大学 | It is a kind of using flyash produce in microelement acidic soil conditioner method and product |
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