CN102145904B - Method for extracting alumina from fly ash - Google Patents
Method for extracting alumina from fly ash Download PDFInfo
- Publication number
- CN102145904B CN102145904B CN2011101037828A CN201110103782A CN102145904B CN 102145904 B CN102145904 B CN 102145904B CN 2011101037828 A CN2011101037828 A CN 2011101037828A CN 201110103782 A CN201110103782 A CN 201110103782A CN 102145904 B CN102145904 B CN 102145904B
- Authority
- CN
- China
- Prior art keywords
- stripping
- aluminum oxide
- decomposition
- mother liquor
- flyash
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000000034 method Methods 0.000 title claims abstract description 67
- 239000010881 fly ash Substances 0.000 title claims abstract description 48
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 title claims abstract description 28
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 57
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 28
- 238000005406 washing Methods 0.000 claims abstract description 26
- 239000002253 acid Substances 0.000 claims abstract description 25
- 239000012452 mother liquor Substances 0.000 claims abstract description 22
- 238000001704 evaporation Methods 0.000 claims abstract description 16
- 230000008020 evaporation Effects 0.000 claims abstract description 16
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 claims abstract description 14
- 239000013078 crystal Substances 0.000 claims abstract description 11
- 239000007789 gas Substances 0.000 claims abstract description 11
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims abstract description 11
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims abstract description 11
- 229910021502 aluminium hydroxide Inorganic materials 0.000 claims abstract description 10
- 238000001914 filtration Methods 0.000 claims abstract description 9
- 238000002425 crystallisation Methods 0.000 claims abstract description 8
- 230000008025 crystallization Effects 0.000 claims abstract description 8
- 239000000463 material Substances 0.000 claims abstract description 6
- 238000000926 separation method Methods 0.000 claims abstract description 6
- 238000004131 Bayer process Methods 0.000 claims abstract description 4
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 60
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 26
- 239000007788 liquid Substances 0.000 claims description 23
- 239000010802 sludge Substances 0.000 claims description 19
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 18
- 239000012065 filter cake Substances 0.000 claims description 15
- 239000003518 caustics Substances 0.000 claims description 12
- 239000000047 product Substances 0.000 claims description 12
- 239000011734 sodium Substances 0.000 claims description 12
- 230000000694 effects Effects 0.000 claims description 11
- 210000000582 semen Anatomy 0.000 claims description 11
- 239000003513 alkali Substances 0.000 claims description 7
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 6
- 229910052708 sodium Inorganic materials 0.000 claims description 6
- 238000010521 absorption reaction Methods 0.000 claims description 4
- 238000004090 dissolution Methods 0.000 claims description 4
- 239000011552 falling film Substances 0.000 claims description 4
- -1 polytetrafluoroethylene Polymers 0.000 claims description 4
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 4
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 4
- 239000005432 seston Substances 0.000 claims description 4
- 230000002378 acidificating effect Effects 0.000 claims description 2
- 239000000203 mixture Substances 0.000 abstract description 4
- 239000002002 slurry Substances 0.000 abstract 4
- 238000002156 mixing Methods 0.000 abstract 3
- 239000012530 fluid Substances 0.000 abstract 2
- 238000010306 acid treatment Methods 0.000 abstract 1
- 230000029087 digestion Effects 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 description 10
- 239000002699 waste material Substances 0.000 description 10
- 229910001570 bauxite Inorganic materials 0.000 description 9
- 239000000243 solution Substances 0.000 description 9
- 238000011160 research Methods 0.000 description 8
- 230000008901 benefit Effects 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- 238000000605 extraction Methods 0.000 description 6
- 239000006210 lotion Substances 0.000 description 6
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 5
- 239000003245 coal Substances 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 239000002893 slag Substances 0.000 description 5
- 238000003756 stirring Methods 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 238000005245 sintering Methods 0.000 description 3
- 229910001388 sodium aluminate Inorganic materials 0.000 description 3
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- GYHNNYVSQQEPJS-UHFFFAOYSA-N Gallium Chemical compound [Ga] GYHNNYVSQQEPJS-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 229910004298 SiO 2 Inorganic materials 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 238000013459 approach Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000007865 diluting Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- 229910052733 gallium Inorganic materials 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 238000005272 metallurgy Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000006200 vaporizer Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001648 diaspore Inorganic materials 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000011268 mixed slurry Substances 0.000 description 1
- 239000010970 precious metal Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000010117 shenhua Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 229910052814 silicon oxide Inorganic materials 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 1
- 229910001948 sodium oxide Inorganic materials 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 150000004684 trihydrates Chemical class 0.000 description 1
Images
Abstract
The invention discloses a method for extracting alumina from fly ash. The method comprises the following steps of: a), acid treatment, i.e. mixing and feeding hydrochloric acid and the fly ash into a digester lined with a polyfluortetraethylene material for dissolving, carrying out separation on dissolved slurry by a settling tank, carrying out evaporation, crystallization, roasting and decomposition on the upper overflow slurry to form active initial alumina and hydrogen chloride gas, and returning the hydrogen chloride gas to a fly ash dissolving process after the hydrogen chloride gas is recovered to prepare acid; and b), Bayer process treatment, i.e. mixing the active initial alumina and circulating mother liquor, sending the mixture into an autoclave for dissolving, carrying out separation on the dissolved slurry by the settling tank, carrying out fine filtering on the upper overflow slurry to obtain refined fluid, mixing the refined fluid and seed crystals of aluminium hydroxide, carrying out seed crystal digestion to obtain decomposition mother liquor and aluminium hydroxide, returning the decomposition mother liquor to the process of dissolving the active initial alumina after the decomposition mother liquor is evaporated, and carrying out filtering, washing and roasting on the aluminium hydroxide to obtain an alumina product. Due to the adoption of the method, the metallurgical alumina which meets the national standard requirements can be prepared.
Description
Technical field
The present invention relates to a kind ofly extract method of alumina, more particularly, relate to a kind of method of handling aluminous fly-ash extraction metallurgical-grade aluminum oxide with hydrochloric acid-bayer's process by flyash.
Background technology
Produce about 7,000 ten thousand tons of aluminum oxide every year in the world at present, and it is raw material that each alumina producer almost adopts bauxite entirely.China is maximum in the world alumina producing state, produces about 2,100 ten thousand tons of aluminum oxide, and accounts for 30% of Gross World Product in 2008.But China's bauxite resource is poor relatively, and the bauxite reserves only account for about 6% of world's total reserves, and ore grade is lower, and ore type is main with unmanageable diaspore mainly, complex treatment process, energy consumption height, and production cost is also higher.Because China's bauxite resource is not enough, China's import bauxite ore was about 2,500 ten thousand tons in 2008, accounted for about 50% of domestic bauxite usage quantity.Ore resource is not enough, has had a strong impact on the development of China's aluminum oxide industry, seeks new aluminum oxide industry raw material, researchs and produces the task of top priority that the new Technology of aluminum oxide becomes China's aluminium industrial development.
Coal resources in China is very abundant, and coal production accounts for the first in the world, more than 20 hundred million tons of coals of annual output, and the coal major part is used for thermal power plant's generating, will discharge a large amount of flyash behind the coal burning, and China's annual approximately discharging aluminous fly-ash (refers to Al in the flyash
2O
3>=38wt%) more than 100,000,000 tons.Analyze after deliberation; Aluminous fly-ash mainly is made up of aluminum oxide, silicon oxide; The content of 2 kinds of compositions accounts for 80wt%, and other compositions such as iron content, magnesium, titanium, calcium also contain abundant rare precious metals such as gallium in the flyash that has in addition; Be the raw material that metallurgical-grade aluminum oxide and GALLIUM metal pure are extracted in comprehensive utilization, have high industrial utilization and be worth.Alumina content generally is higher than southern area in the flyash of north China; Like alumina content in the flyash of ground outputs such as Shanxi, Shaanxi, Inner Mongol, Ningxia usually about 40wt%; Belong to aluminous fly-ash, in the Erdos area flyash of the Inner Mongol there be alumina content up to 45～50wt%, almost with external bauxite trihydrate in alumina content suitable; From chemical composition analysis, can be used as one of raw material that extracts metallurgical-grade aluminum oxide fully.
At present flyash thermal power plant's waste of discharging is normally stored up mainly as a kind of industrial residue, and this had both taken a large amount of soils, and severe contamination environment, be unfavorable for the safe operation in lime-ash stockyard, also increased the production cost of power plant.The coastland because populous, industry is flourishing, sometimes with flyash be used to build the road, material of construction such as brickmaking, this only belongs to low-grade, low value-added application, and economically underdeveloped area or west area, flyash is still stored up mainly as industrial residue.On the whole, China and world developed country still are in the experimental study stage to the total utilization of PCA problem, are seeking the approach that it rationally utilizes.
In recent years, to the present situation of China's bauxite resource wretched insufficiency, many scientific research departments of China and universities and colleges actively develop non-bauxite resource production metallurgy grade aluminum oxide research, and emphasis is a research aluminous fly-ash comprehensive utilization production metallurgy grade aluminum oxide.Each research unit's basis achievement in research has separately proposed some and has handled the new process of aluminous fly-ashs, and main direction of studying is following:
(1) alkaline process: the main stream approach that is the aluminous fly-ash comprehensive utilizating research.It mainly uses for reference the existing sophisticated sintering process production technique of alumina industry; Utilize sintering process technology can processing low-grade, the characteristics of low alumina silica ratio ore; Aluminous fly-ash, Wingdale (or lime), alkali are pressed certain proportioning; Be prepared into charge pulp and carry out sintering, sintered clinker is through stripping, desiliconization, decomposition, roasting and obtain the metallurgical-grade aluminum oxide product.The advantage of this method is that Technology is ripe, can obtain qualified alumina product.But the shortcoming of this method is a lot, mainly is that the lime dosage is huge, red mud amount big, the concentration of sodium aluminate solution is low, production energy consumption is high, and its investment and cost are high.
(2) acid system: mainly contain 2 kinds of sulfuric acid process, salt acid systems.Promptly adopt sulfuric acid or hydrochloric acid and aluminous fly-ash to prepare burden in proportion; Aluminum oxide under certain temperature and pressure in the stripping flyash; Obtain purified aluminum salt solution through slagging-off and deironing then; Obtain alumina product through evaporation, roasting, its advantage is that flow process is simple, the quantity of slag is little, production cost is low.Shortcoming is that deironing and removal of impurities are difficult, and alumina product quality and traditional national standard have difference, and some technological problemses still need be studied and tested.
Patented claim CN 1927716A discloses method of alumina in a kind of extraction flyash; Its advantage is to have concentrated acid system and alkaline process to prepare the advantage of aluminum oxide; But owing to receive the restriction of processing unit; There is following problems in this method: adopt the unreasonable economically evaporization process that causes of " carrying out negative pressure in the concentration tank concentrates " technology industriallization to use, can only be used for laboratory study; Slip after the stripping in subsider, separate and wash after obtain soaking slag liquid contain rate up to 70～80wt%, directly be sent to the waste residue stockyard, big to surrounding environment influence; Acid stripping temperature is 90～110 ℃, finds that through test the hydrochloric acid solubility rate of aluminum oxide has only about 60% the too low manufacturing cost of aluminum oxide that then increased of solubility rate under this temperature.Improve the solubility rate that the stripping temperature can improve aluminum oxide in the flyash, but high temperature stripping meeting increases the weight of acid to corrosion on Equipment.Therefore be necessary to research and develop a kind of reliable process method with the result of extraction that improves aluminum oxide in the flyash and solve under the high temperature hydrochloric acid medium to the corrosion on Equipment problem.
Summary of the invention
The objective of the invention is provides a kind of method that adopts hydrochloric acid-Bayer process from flyash, to extract metallurgical-grade aluminum oxide to deficiency of the prior art.The alumina product that makes through method provided by the invention is the metallurgical grade first grade (n YS/T274-1998) that complies with the national standard requirements, and can satisfy electrolytic aluminum industry request for utilization fully.
Method provided by the invention comprises the steps:
A) acidic process: hydrochloric acid and flyash batching and the digester of sending into the inner liner polytetrafluoroethylene material are carried out stripping; The slip of stripping obtains active just aluminum oxide and hydrogen chloride gas through separation, evaporative crystallization, roasting decomposition;
B) Bayer process is handled: the active aluminum oxide just that obtains in the step a) is prepared burden with circulating mother liquor and sent into autoclave and carry out stripping, ratio of components α
kBe 1.35～1.55, while feeding-in liquid caustic alkali, the caustic sodium concentration Na in the said circulating mother liquor
2O
kBe controlled at 160～230g/l; The slip of stripping is after separation, smart filter, and gained seminal fluid and aluminium hydroxide crystal seed carry out kind of a branch decomposition and obtain white lake and decomposition nut liquid in decomposer; Said decomposition nut liquid returns active aluminum oxide stripping operation just and uses as circulating mother liquor after evaporation, said white lake obtains the metallurgical-grade aluminum oxide product through filtration, washing, roasting.
According to method provided by the invention, adopt flyash and hydrochloric acid reaction raw materials in the said step a), the Al of said flyash as the stripping reaction
2O
3Content>=38wt%, the concentration of said hydrochloric acid is 25～31wt%.
According to method provided by the invention, wherein, the flyash in the step a) is taked the mode of continuous stripping, the stripping temperature is 140～160 ℃, dissolution time is 1～2 hour, preferably under alr mode, flyash is carried out stripping, wherein Al
2O
3Solubility rate>=80%.
According to method provided by the invention, wherein settlement separate in subsider through the slip of step a) stripping, underflow is an acid sludge, and overflow is the thick liquid of aluminum chloride; Said acid sludge gets into rinse bath, carries out backflush 4～6 times with 60～85 ℃ hot water, and the add-on of hot water is 1.5～2.5t/t acid sludge, and the washing lotion behind the washing acid sludge is used for diluting the slip of digester stripping; Acid sludge after the last washing after filtering, gained filtrating is returned in the rinse bath and is recycled, the water ratio≤35wt% of gained filter cake is sent to the waste residue stockyard with filter cake.
According to method provided by the invention, wherein, the thick liquid of said aluminum chloride is imitated pump feed evaporator through 2～4 and is evaporated, and removes the moisture in the thick liquid of aluminum chloride and makes aluminum chloride with AlCl
36H
2The crystallization of O form is separated out.
According to method provided by the invention, wherein, adopt rotary kiln or fluidized roaster to AlCl
36H
2Roasting is carried out in the O crystallization, and maturing temperature is 600～800 ℃, and aluminum chloride resolves into active just aluminum oxide and hydrogen chloride gas, Al in the first aluminum oxide of said activity
2O
3Content>=92wt%.
According to method provided by the invention, wherein, the hydrogen chloride gas in the said step a) returns flyash stripping operation and recycles after the hydrochloric acid that concentration is 25～31wt% is processed on 2～3 grade hydrochloric acid absorption towers.
According to method provided by the invention, wherein, the active stripping temperature of aluminum oxide just is 210～250 ℃ in the said step b), is preferably 230～240 ℃, and stripping pressure is 1.8～4.0MPa, is preferably 2.3～3.4MPa, and dissolution time is 0.5～1.5 hour.
Preferably, the mixed slurry of first aluminum oxide of said activity and circulating mother liquor carries out stripping under alr mode, Al in the active aluminum oxide just
2O
3Solubility rate>=93%.
According to method provided by the invention, wherein settlement separate in subsider through the slip of step b) stripping, underflow is a red mud, makes seminal fluid through overflow being carried out the essence filter; Content≤15mg/l of seston in the said seminal fluid; Said red mud gets into rinse bath; Carry out backflush 3～5 times with 80～90 ℃ hot water; The add-on of hot water is 2～4t/t red mud, and the washing lotion of washing behind the red mud is used for diluting the slip of autoclave stripping, interior temperature>=85 of subsider and rinse bath ℃; Red mud after the last washing after filtering, gained filtrating is returned rinse bath and is recycled, the water ratio≤35wt% of gained filter cake is sent to the waste residue stockyard with filter cake.
According to method provided by the invention, wherein, the add-on of aluminium hydroxide crystal seed is 500～850g/l in the said step b); The decomposer groove number that adopts is 12～16, and decomposing first-cell temperature is 59～72 ℃, and last groove temperature is 48～60 ℃; Resolving time is 38～45 hours, Al in the said seminal fluid
2O
3Rate of decomposition be 46～51%.
According to method provided by the invention, adopt multiple-effect falling film formula vaporizer or full flash vaporizer that the decomposition nut liquid in the step b) is evaporated, the mother liquor after the evaporation returns active aluminum oxide stripping operation just and uses as circulating mother liquor.
According to method provided by the invention, the white lake that obtains in the step b) obtains the metallurgical-grade aluminum oxide product after carrying out fluosolids roasting under 950～1100 ℃.
Compared with prior art, the present invention can overcome the technological deficiency that prior art is handled the aluminous fly-ash aluminium oxide extraction process, has following advantage:
(1) the stripping temperature of available technology adopting salt s.t. flyash is merely 90～110 ℃; Cause the solubility rate of aluminum oxide to have only 60%, the inventive method adopts the digester of inner liner polytetrafluoroethylene material and through stirring the mode of stripping, the stripping temperature is increased to 140～160 ℃; The solubility rate of aluminum oxide reaches more than 80%; Greatly improve result of extraction, improved the utilization of coal ash rate, had bigger economic benefit.
(2) subsider underflow acid sludge and red mud are being carried out in the process of backflush, the present invention adopts hot wash can keep system's heat balance, keeps the higher solubility of aluminum chloride in the solution, aluminum oxide, reduces soltion viscosity, helps the slag sedimentation; And acid sludge and red mud after the present invention washs last filter with filter; Water ratio≤the 35wt% of control filter cake can further reclaim filtrating, reduces discharging of waste liquid; Waste residue volume-diminished after the filtration; Save the stacking space of slag field, both effectively prolonged the working life of traditional slag field, practiced thrift valuable land resources again.
(3) in the methods of the invention, AlCl
36H
2O crystalline maturing temperature is 600～800 ℃, can make aluminum chloride crystalline dehydration reaction complete, and the cl ions of avoiding being mingled with in the active aluminum oxide just produces adverse influence to follow-up alkali process, equipment, has guaranteed the active activity of aluminum oxide just simultaneously.
(4) in the methods of the invention, through under alr mode, utilizing circulating mother liquor and replenishing small amount of liquid caustic alkali the first aluminum oxide of activity is carried out stripping, make Al in the active aluminum oxide just
2O
3Solubility rate>=93%, economic benefit is particularly considerable.
(5) decomposition nut liquid that obtains after kind of branch is decomposed of the present invention adopts multiple-effect falling film or full flash evaporation technology, can get rid of redundant moisture in the flow process, has guaranteed the water balance of production technique system.
Terminological interpretation:
" active aluminum oxide just " among the present invention is meant Al
2O
3The intermediate product of content>=92wt%.
" caustic sodium concentration Na among the present invention
2O
k" being meant the concentration of the sodium oxide that exists with the caustic alkali form in " circulating mother liquor ", unit is g/l.
" ratio of components α among the present invention
k" also refer to the causticization coefficient or the caustic ratio of sodium aluminate solution, the mol ratio of contained caustic alkali and aluminum oxide in the expression solution, method of calculation are α
k=1.645 * (caustic sodium concentration Na
2O
k/ alumina concentration), wherein alumina concentration unit is g/l.
" plant divide decompose " among the present invention be meant in oversaturated sodium aluminate solution and add aluminium hydroxide crystal seed, makes aluminum oxide in the sodium aluminate solution with the form process that crystallization is separated out from solution of white lake.
" decomposition nut liquid " among the present invention is meant the solution that oversaturated sodium aluminate solution obtains after " plant and decompose " separated out white lake.
" circulating mother liquor " among the present invention is meant that " decomposition nut liquid " returns the mother liquor that active aluminum oxide stripping operation just recycles after evaporation.
Description of drawings
Fig. 1 is the process flow diagram according to the inventive method.
Embodiment
Below in conjunction with accompanying drawing and specific embodiment the present invention is described further, still, the present invention is not limited in following examples.
Embodiment 1
Al by 85%
2O
3Solubility rate calculates the consumption of hydrochloric acid, with the aluminous fly-ash (Al of coal gangue power plant of accurate ability company of Shenhua
2O
3Content 48.2wt%, SiO
2Content 38.33wt%) is that the hydrochloric acid batching of 28wt% is processed the flyash slip with concentration, is sent to the digester of inner liner polytetrafluoroethylene material, under 150 ℃ of conditions, stopped 1.5 hours and constantly stir; The slip of stripping is sent to subsider carries out flash liberation, the underflow acid sludge of subsider gets into rinse bath, carries out backflush 5 times with 85 ℃ of hot water; The hot water add-on is the 2.0t/t acid sludge; Washing lotion behind the washing acid sludge can be diluted the slip of stripping, and the acid sludge after the last washing filters through filter, and filtrating is returned rinse bath; Water ratio≤the 35wt% of control filter cake; Said filter cake is sent to the waste residue stockyard, the subsider overflow is sent to 3 imitates pump feed evaporator, after evaporation concentration, obtain AlCl
36H
2The O crystallization obtains active just aluminum oxide, wherein Al through fluosolids roasting under 700 ℃
2O
3Content be 93wt%, the hydrogen chloride gas that produces in the roasting process is sent to 2 grade hydrochloric acid absorption towers and is prepared into the hydrochloric acid that concentration is 28wt%, return hydrochloric acid stripping operation and flyash the batching.
With first aluminum oxide of said activity and caustic sodium concentration Na
2O
kBe the circulating mother liquor batching of 200g/l, ratio of components α
kBe 1.40, be mixed with ore pulp and be sent to autoclave and carry out stripping that under 220 ℃ of conditions, stopped 1.5 hours and constantly stir, stripping pressure is 2.3MPa, the wherein active contained Al of aluminum oxide just
2O
3Solubility rate be 93%, the slip of stripping is sent to subsider carries out flash liberation, the underflow red mud of subsider gets into rinse bath; Carry out backflush 4 times with 90 ℃ of hot water, the hot water add-on is the 3t/t red mud, and subsider and rinse bath temperature are 90 ℃; Washing lotion behind the washing red mud can be diluted the slip of stripping; Red mud after the last washing filters through filter, and the water ratio≤35wt% of gained filter cake is sent to the waste residue stockyard with filter cake.The subsider overflow filters seminal fluid through essence, and the content of its seston is 12mg/l, and said seminal fluid is mixed with aluminium hydroxide crystal seed, forms aluminum hydroxide slime, and the content of crystal seed is 800g/l in the aluminum hydroxide slime, gets into decomposer and carries out kind of a branch decomposition.Adopt 13 decomposers, decomposing first-cell temperature is 61 ℃, and last groove temperature is 53 ℃, and the resolving time is 45 hours, Al
2O
3Rate of decomposition be 50%.Plant branch and decompose the decomposition nut liquid warp 5 effect falling film evaporations that obtain, the mother liquid evaporation that obtains returns the first aluminum oxide stripping operation of activity and uses as circulating mother liquor; The white lake that the kind decomposition obtains carries out fluosolids roasting through filtration washing under 1050 ℃ maturing temperature, obtain qualified metallurgical-grade aluminum oxide product, wherein Al
2O
3Content be 98.6wt%.
Embodiment 2
Al by 80%
2O
3Solubility rate calculates the consumption of hydrochloric acid, the aluminous fly-ash that power plant's fluidized-bed combustion boiler is produced (Al
2O
3Content 42.5wt%, SiO
2Content 40.38wt%) be that the hydrochloric acid batching of 25wt% is processed the flyash slip with concentration, be sent to embodiment 1 in identical digester, under 142 ℃ of conditions, stopped 2.0 hours and constantly stir; The slip of stripping is sent to subsider carries out flash liberation, the underflow acid sludge of subsider is sent into rinse bath, carry out backflush 6 times with 80 ℃ of hot water; The hot water add-on is the 2.5t/t acid sludge; Washing lotion behind the washing acid sludge can be diluted the slip of stripping, and the acid sludge after the last washing filters through filter, and filtrating is returned rinse bath; Water ratio≤the 35wt% of control filter cake; The gained filter cake is sent to the waste residue stockyard, the subsider overflow is sent to 4 imitates pump feed evaporator, after evaporation concentration, obtain AlCl
36H
2The O crystallization obtains active just aluminum oxide, wherein Al through fluosolids roasting under 800 ℃
2O
3Content be 92wt%, the hydrogen chloride gas that produces in the roasting process is sent to 2 grade hydrochloric acid absorption towers and is prepared into the hydrochloric acid that concentration is 25wt%, return hydrochloric acid stripping operation and flyash the batching.
With first aluminum oxide of said activity and caustic sodium concentration Na
2O
kBe the circulating mother liquor batching of 220g/l, ratio of components α
kBe 1.35, be mixed with ore pulp and be sent to autoclave and carry out stripping that under 245 ℃ of conditions, stopped 1.0 hours and constantly stir, stripping pressure is 3.5MPa, the wherein active contained Al of aluminum oxide just
2O
3Solubility rate be 95%, carry out flash liberation at the bottom of the slip of stripping is sent to subsider, the underflow red mud of subsider gets into rinse bath; Carry out 5 washings with 85 ℃ of hot water, the hot water add-on is the 2.5t/t red mud, and subsider and rinse bath temperature are 90 ℃; Washing lotion behind the washing red mud can be diluted the slip of stripping; Red mud after the last washing filters through filter, and the water ratio≤35wt% of control filter cake is sent to the waste residue stockyard with the gained filter cake.The subsider overflow filters seminal fluid through essence, and the content of its seston is 15mg/l, and said seminal fluid mixes with aluminium hydroxide crystal seed, forms aluminum hydroxide slime, and the content of crystal seed is 820g/l in the aluminum hydroxide slime, gets into decomposer and carries out kind of a branch decomposition.Adopt 15 decomposers, decomposing first-cell temperature is 70 ℃, and last groove temperature is 56 ℃, and the resolving time is 42 hours, Al
2O
3Rate of decomposition be 48%.Kind divide to decompose the decomposition nut liquid that obtains through full flash evaporation, the mother liquid evaporation that obtains returns active aluminum oxide stripping operation just and uses as circulating mother liquor.The white lake that the kind decomposition obtains carries out fluosolids roasting through filtration washing under 1020 ℃ maturing temperature, obtain qualified metallurgical-grade aluminum oxide product, wherein Al
2O
3Content be 98.8wt%.
Claims (10)
1. one kind is extracted method of alumina by flyash, and this method comprises:
A) acidic process: hydrochloric acid and flyash batching and the digester of sending into the inner liner polytetrafluoroethylene material are carried out stripping, flyash is taked the mode of continuous stripping, the stripping temperature is 140～160 ℃, and dissolution time is 1～2 hour; The slip of stripping obtains active just aluminum oxide and hydrogen chloride gas through separation, evaporative crystallization, roasting decomposition;
B) Bayer process is handled: the active aluminum oxide just that obtains in the step a) is prepared burden with circulating mother liquor and sent into autoclave and carry out stripping, ratio of components α
kBe 1.35～1.55, while feeding-in liquid caustic alkali, the caustic sodium concentration Na in the said circulating mother liquor
2O
kBe controlled at 160～230g/l; The slip of stripping is after separation, smart filter, and gained seminal fluid and aluminium hydroxide crystal seed carry out kind of a branch decomposition and obtain white lake and decomposition nut liquid in decomposer; Said decomposition nut liquid returns active aluminum oxide stripping operation just and uses as circulating mother liquor after evaporation, said white lake obtains the metallurgical-grade aluminum oxide product through filtration, washing, roasting.
2. method according to claim 1 is characterized in that, in step a), under alr mode, flyash is carried out stripping.
3. method according to claim 1 and 2 is characterized in that, and is settlement separate in subsider through the slip of step a) stripping, and the top overflow is the thick liquid of aluminum chloride, and underflow is an acid sludge; Acid sludge gets into rinse bath, carries out backflush 4～6 times with 60～85 ℃ hot water, and the add-on of hot water is 1.5～2.5t/t acid sludge, the water ratio≤35wt% of the filter cake that the acid sludge process after the last washing filters; The thick liquid of aluminum chloride is decomposed into active just aluminum oxide and hydrogen chloride gas through rotary kiln or fluidized roaster roasting under 600～800 ℃ after 2～4 effect pump feed evaporator evaporations.
4. method according to claim 3 is characterized in that, Al in the first aluminum oxide of said activity
2O
3Content>=92wt%, said hydrogen chloride gas returns flyash stripping operation and recycles after the hydrochloric acid that concentration is 25～31wt% is processed on 2～3 grade hydrochloric acid absorption towers.
5. method according to claim 1 is characterized in that, the stripping temperature in the step b) is 210～250 ℃, and stripping pressure is 1.8～4.0MPa, and dissolution time is 0.5～1.5 hour.
6. method according to claim 5 is characterized in that, the stripping temperature in the step b) is 230～240 ℃, and stripping pressure is 2.3～3.4MPa, under alr mode, the first aluminum oxide of activity is carried out stripping.
7. according to claim 1 or 5 or 6 described methods, it is characterized in that, settlement separate in subsider through the slip of step b) stripping, make seminal fluid through the top overflow being carried out the essence filter; Content≤15mg/l of seston in the said seminal fluid; The bottom red mud gets into rinse bath; Carry out backflush 3～5 times with 80～90 ℃ hot water; The add-on of hot water is 2～4t/t red mud, and the temperature in subsider and the rinse bath is not less than 85 ℃, the water ratio≤35wt% of the filter cake that the red mud process after the last washing filters.
8. method according to claim 7 is characterized in that, the add-on of aluminium hydroxide crystal seed is 500～850g/l in the said step b); Decomposer groove number is 12～16, and decomposing first-cell temperature is 59～72 ℃, and decomposing last groove temperature is 48～60 ℃; Resolving time is 38～45 hours, Al
2O
3Rate of decomposition be 46～51%.
9. method according to claim 1 is characterized in that, said decomposition nut liquid returns active aluminum oxide stripping operation just and uses as circulating mother liquor through multiple-effect falling film evaporation or full flash evaporator evaporation; Said white lake carries out fluosolids roasting and obtains the metallurgical-grade aluminum oxide product under 950～1100 ℃.
10. method according to claim 1 is characterized in that, in said step a), and the Al of flyash
2O
3Content>=38wt%, the concentration of hydrochloric acid is 25～31wt%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011101037828A CN102145904B (en) | 2010-04-27 | 2011-04-25 | Method for extracting alumina from fly ash |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010161876 CN101811711A (en) | 2010-04-27 | 2010-04-27 | Method for extracting aluminum oxide from fly ash |
| CN201010161876.6 | 2010-04-27 | ||
| CN2011101037828A CN102145904B (en) | 2010-04-27 | 2011-04-25 | Method for extracting alumina from fly ash |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102145904A CN102145904A (en) | 2011-08-10 |
| CN102145904B true CN102145904B (en) | 2012-07-25 |
Family
ID=42619104
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201010161876 Pending CN101811711A (en) | 2010-04-27 | 2010-04-27 | Method for extracting aluminum oxide from fly ash |
| CN2011101037828A Active CN102145904B (en) | 2010-04-27 | 2011-04-25 | Method for extracting alumina from fly ash |
Family Applications Before (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201010161876 Pending CN101811711A (en) | 2010-04-27 | 2010-04-27 | Method for extracting aluminum oxide from fly ash |
Country Status (1)
| Country | Link |
|---|---|
| CN (2) | CN101811711A (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103663511B (en) * | 2012-08-31 | 2015-11-04 | 沈阳铝镁设计研究院有限公司 | HCl treatment coal ash for manufacturing is for the method for aluminum oxide |
| CN104628019A (en) * | 2013-11-15 | 2015-05-20 | 李进凯 | Method for separating and recovering aluminum oxide form coal ash |
| CN103803495A (en) * | 2013-12-30 | 2014-05-21 | 中国神华能源股份有限公司 | Treatment method for liquid waste produced during the acid-process preparation of aluminum oxide |
| CN106669978B (en) * | 2015-11-11 | 2019-09-13 | 神华集团有限责任公司 | A kind of method that charcoal flotation agent and its application and flyash flotation mention charcoal |
| CN107055582B (en) * | 2016-12-15 | 2021-10-22 | 中国恩菲工程技术有限公司 | System for dissolve out aluminium from fly ash |
| CN108863119B (en) * | 2017-05-11 | 2021-01-22 | 神华集团有限责任公司 | Method for preparing sulphoaluminate cement clinker from fly ash |
| CN107285349A (en) * | 2017-07-25 | 2017-10-24 | 东莞市联洲知识产权运营管理有限公司 | A kind of method that aluminum oxide is extracted by raw material of aluminous fly-ash |
| CN111233014B (en) * | 2020-03-04 | 2022-04-26 | 神华准能资源综合开发有限公司 | Method for enhanced dissolution of fly ash |
| CN115196659B (en) * | 2022-07-21 | 2023-12-05 | 四川顺应动力电池材料有限公司 | Environment-friendly low-consumption system for circularly preparing alumina by leaching acid and alkali from coal solid waste nitric acid and preparation method of industrial grade alumina |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100410174C (en) * | 2006-08-29 | 2008-08-13 | 神华准格尔能源有限责任公司 | Preparation method of alumina |
| CN101054192B (en) * | 2007-04-10 | 2010-05-19 | 吉林大学 | Method of preparing crystal aluminum chloride from circulation fluid bed fly ash |
-
2010
- 2010-04-27 CN CN 201010161876 patent/CN101811711A/en active Pending
-
2011
- 2011-04-25 CN CN2011101037828A patent/CN102145904B/en active Active
Non-Patent Citations (1)
| Title |
|---|
| 袁兵.准格尔矸石电厂CFB灰中提取冶金级氧化铝工艺研究.《中国优秀硕士学位论文全文数据库，工程科技Ⅰ辑》.2008,(第10期),论文24-29页，37-56页，图3-1、. * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102145904A (en) | 2011-08-10 |
| CN101811711A (en) | 2010-08-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102145904B (en) | Method for extracting alumina from fly ash | |
| CN110194478B (en) | Method for preparing villiaumite with aluminum fluoride as main component by using electrolyte-containing material generated by aluminum electrolysis | |
| CN102515220B (en) | Method for extracting alumina and gallium oxide from pulverized fuel ash to prepare aluminum oxide nanometer and polymeric ferric silicate sulfate | |
| CN103570043B (en) | Method for producing high-purity potassium chloride solution for preparation of potassium carbonate and co-producing low sodium salt | |
| CN104386720B (en) | Method for acid-alkali combined extraction of alumina from high-silicon aluminum-containing mineral raw material | |
| CN103145160B (en) | Method for producing alumina by using high-alumina fly ash | |
| CN101418379B (en) | Method for extracting nickel and cobalt by enclosed leaching nickel oxide mine | |
| CN101760613B (en) | Method for leaching zinc-containing ores | |
| CN102502740A (en) | Method for preparing high-alkali high-causticity-ratio solution and improving traditional seed precipitation efficiency | |
| WO2018233688A1 (en) | Method for preparing aluminum hydroxide by treating medium- and low-grade bauxite by using one-step alkali heat process of andradite | |
| CN106966416A (en) | A kind of method that high purity aluminium oxide is extracted from coal-powder boiler flyash | |
| CN102642857A (en) | Process method for producing metal aluminium by high-alumina fly ash | |
| CN103408164B (en) | Recycling method of electroplating wastewater containing copper nitrate | |
| CN107128959A (en) | A kind of bauxite salt Ore Leaching substep electrolytic preparation aluminum oxide and method of comprehensive utilization | |
| CN113120938B (en) | Method for preparing calcium fluoride by using fluorine-containing wastewater | |
| CN100372772C (en) | Method for producing powder form aluminum oxide by low concentration solution seed decomposition | |
| CN104445337B (en) | A kind of ammonia alkali slops and bittern produce the method for low chlorine gypsum | |
| CN103395751A (en) | Wet method used for extracting products from low-grade complex material containing tellurium and selenium | |
| CN107162029B (en) | Red mud method of comprehensive utilization | |
| CN104743586A (en) | Joint production method of alkali leaching of aluminium in Bayer red mud and aluminium oxide decomposed mother liquid evaporation for salt elimination | |
| CN107792870B (en) | Comprehensive utilization method of bauxite | |
| CN103086409A (en) | Method for producing metallurgical grade sandy alumina by mixing and roasting flyash and ammonium sulfate | |
| CN103086411A (en) | Method for producing metallurgical grade sandy alumina by mixing and roasting flyash and ammonium sulfate | |
| CN102398913B (en) | Process for extracting metallurgical grade alumina through treatment of high alumina fly ash by using sulfuric acid method | |
| CN107857285A (en) | A kind of method that aluminic acid sodium crystal is produced using low-grade aluminum-containing raw material |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| ASS | Succession or assignment of patent right |
Free format text: FORMER OWNER: SHENHUA ZHUNGER ENERGY CO., LTD. Effective date: 20111206 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20111206 Address after: 100011 Beijing city Dongcheng District No. 16 Andrew intercontinental 4 storey building Applicant after: China Shenhua Energy Co., Ltd. Address before: 100011 Beijing city Dongcheng District No. 16 Andrew intercontinental 4 storey building Applicant before: China Shenhua Energy Co., Ltd. Co-applicant before: Shenhua Zhunger Energy Co., Ltd. |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |