CN1887714A - Lime slaking process for alumina production - Google Patents
Lime slaking process for alumina production Download PDFInfo
- Publication number
- CN1887714A CN1887714A CN 200610103784 CN200610103784A CN1887714A CN 1887714 A CN1887714 A CN 1887714A CN 200610103784 CN200610103784 CN 200610103784 CN 200610103784 A CN200610103784 A CN 200610103784A CN 1887714 A CN1887714 A CN 1887714A
- Authority
- CN
- China
- Prior art keywords
- lime
- milk
- red mud
- alumina
- digestion
- 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.)
- Pending
Links
- 235000008733 Citrus aurantifolia Nutrition 0.000 title claims abstract description 50
- 235000011941 Tilia x europaea Nutrition 0.000 title claims abstract description 50
- 239000004571 lime Substances 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title claims abstract description 37
- 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
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 22
- 230000008569 process Effects 0.000 title abstract description 16
- 239000002893 slag Substances 0.000 claims abstract description 7
- 239000000463 material Substances 0.000 claims abstract description 4
- 239000000920 calcium hydroxide Substances 0.000 claims description 36
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 36
- 230000029087 digestion Effects 0.000 claims description 25
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 18
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 14
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 claims description 6
- 238000001704 evaporation Methods 0.000 claims description 6
- 230000008020 evaporation Effects 0.000 claims description 6
- 230000002950 deficient Effects 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 239000012535 impurity Substances 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 101100399296 Mus musculus Lime1 gene Proteins 0.000 abstract description 46
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 abstract description 18
- 239000003513 alkali Substances 0.000 abstract description 14
- 229910001648 diaspore Inorganic materials 0.000 abstract description 13
- 238000002386 leaching Methods 0.000 abstract description 13
- 229910001570 bauxite Inorganic materials 0.000 abstract description 11
- 238000004131 Bayer process Methods 0.000 abstract description 9
- 230000000694 effects Effects 0.000 abstract description 7
- 238000005516 engineering process Methods 0.000 abstract description 5
- 239000000377 silicon dioxide Substances 0.000 abstract description 5
- 229910052681 coesite Inorganic materials 0.000 abstract 2
- 229910052906 cristobalite Inorganic materials 0.000 abstract 2
- 235000012239 silicon dioxide Nutrition 0.000 abstract 2
- 229910052682 stishovite Inorganic materials 0.000 abstract 2
- 229910052905 tridymite Inorganic materials 0.000 abstract 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 abstract 1
- 239000011575 calcium Substances 0.000 abstract 1
- 229910052791 calcium Inorganic materials 0.000 abstract 1
- 229910052593 corundum Inorganic materials 0.000 abstract 1
- 229910052500 inorganic mineral Inorganic materials 0.000 abstract 1
- 239000011707 mineral Substances 0.000 abstract 1
- 229910001845 yogo sapphire Inorganic materials 0.000 abstract 1
- 229910052782 aluminium Inorganic materials 0.000 description 11
- 239000000404 calcium aluminium silicate Substances 0.000 description 8
- 235000012215 calcium aluminium silicate Nutrition 0.000 description 8
- 229940078583 calcium aluminosilicate Drugs 0.000 description 8
- 239000000292 calcium oxide Substances 0.000 description 8
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 8
- 239000012141 concentrate Substances 0.000 description 8
- 229910052814 silicon oxide Inorganic materials 0.000 description 8
- WNCYAPRTYDMSFP-UHFFFAOYSA-N calcium aluminosilicate Chemical compound [Al+3].[Al+3].[Ca+2].[O-][Si]([O-])=O.[O-][Si]([O-])=O.[O-][Si]([O-])=O.[O-][Si]([O-])=O WNCYAPRTYDMSFP-UHFFFAOYSA-N 0.000 description 7
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 7
- 238000005188 flotation Methods 0.000 description 6
- 238000000227 grinding Methods 0.000 description 5
- KIZFHUJKFSNWKO-UHFFFAOYSA-M calcium monohydroxide Chemical compound [Ca]O KIZFHUJKFSNWKO-UHFFFAOYSA-M 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 3
- 238000004090 dissolution Methods 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 238000009776 industrial production Methods 0.000 description 3
- 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 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 239000004411 aluminium Substances 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- OSMSIOKMMFKNIL-UHFFFAOYSA-N calcium;silicon Chemical compound [Ca]=[Si] OSMSIOKMMFKNIL-UHFFFAOYSA-N 0.000 description 2
- 239000003518 caustics Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 2
- 235000012204 lemonade/lime carbonate Nutrition 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 230000001681 protective effect Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- GROMGGTZECPEKN-UHFFFAOYSA-N sodium metatitanate Chemical compound [Na+].[Na+].[O-][Ti](=O)O[Ti](=O)O[Ti]([O-])=O GROMGGTZECPEKN-UHFFFAOYSA-N 0.000 description 2
- 238000005728 strengthening Methods 0.000 description 2
- 229910001773 titanium mineral Inorganic materials 0.000 description 2
- 229910000737 Duralumin Inorganic materials 0.000 description 1
- 206010039509 Scab Diseases 0.000 description 1
- 229910010413 TiO 2 Inorganic materials 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical group O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- JTCFNJXQEFODHE-UHFFFAOYSA-N [Ca].[Ti] Chemical compound [Ca].[Ti] JTCFNJXQEFODHE-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000004380 ashing Methods 0.000 description 1
- SVPXDRXYRYOSEX-UHFFFAOYSA-N bentoquatam Chemical compound O.O=[Si]=O.O=[Al]O[Al]=O SVPXDRXYRYOSEX-UHFFFAOYSA-N 0.000 description 1
- 238000009993 causticizing Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000008570 general process Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052622 kaolinite Inorganic materials 0.000 description 1
- 238000003801 milling Methods 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- LIVNPJMFVYWSIS-UHFFFAOYSA-N silicon monoxide Chemical compound [Si-]#[O+] LIVNPJMFVYWSIS-UHFFFAOYSA-N 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
- 239000007790 solid phase Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Landscapes
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
The present invention relates to alumina producing technology, and is especially lime slaking process for producing alumina through Bayer process with diaspore type bauxite as material. The present invention features that lime is slaked with low concentration solution of Al2O3<80 g/L and SiO2<0.8 g/L. The lime slaking process can raise activity of lime, raise SiO2 saturation coefficient of red mud leaching calcium silica slag, lower the mineral consumption and alkali consumption in alumina production, low production cost, lower red mud discarding rate and raise apparatus capacity.
Description
Technical field
The invention discloses the digestion method of lime in a kind of alumina producing, relate to the alumina producing technology, being specially adapted to the diaspore type bauxite is the lime slaking production process of alumina producing Bayer process of raw material.
Background technology
The industrial production method of alumina mainly contains Bayer process, sintering process and mixed combining method.Bayer process has that Production Flow Chart is simple, and energy consumption is low, and production cost is low, good product quality, the characteristics that purity is high.For the consideration of economy, generally adopt sintering process or producing alumina by mixed combined process for diaspore type bauxite, its technical process complexity, consumption are greatly, quality product is low, process is wayward.
For reducing production costs and improving the alumina product quality, at present, Application and Development based on alumina-producing methods such as the Liquor of Ore Dressing Bayer process of Bayer process, lime bayer methods, be one of major technique all in these methods with the stripping of strengthening diaspore type bauxite.
Strengthen the diaspore stripping, must add leaching additive.In industrial production, the general process for preparation interpolation lime that adopts at the stripping raw pulp just adds calcium oxide, and its purpose is to eliminate TiO in the bauxite
2Detrimentally affect; Promote the transformation of pyrrhosiderite, improve the effect of settling of red mud to rhombohedral iron ore; Improve the solubility rate of aluminum oxide; Impel a part of SiO
2Change calcium aluminosilicate hydrate into, reduce the content of hydrated aluminum silicate, reduce alkaline consumption; The influence of removal of contamination.
In the industrial production, adopt lime and bauxite together to go into mill usually, grind into qualified raw pulp in the ratio of production requirement.But this method has reduced the production capacity of grinding machine, and undecomposed lime carbonate enters anti-causticizing reaction takes place after the flow process, reduces result of extraction and increases the leached amount of salt of mother liquid evaporation, and is very unfavorable to producing.
Publication application number on the 8th CN02125586.5 patent January in 2003 " the adding method of lime in a kind of alumina producing ", its characteristics are at first to adopt mother liquor to change into milk of lime with lime slaking machine commercial lime, remove by filter undecomposed lime carbonate and imperfect combustion breeze, it is 50～200g/l that milk of lime after the ashing contains admittedly, and milk of lime conduct behind bauxite Milling enters conventional aluminum oxide production process towards ore discharge liquid.This patented method has reduced the detrimentally affect of impurity in Bayer process is produced in the lime, has improved the production capacity of raw material mill, has reduced leached amount of salt, has improved the operating environment of belt conveyor system.
The patent No. is in ZL00113438.8's " a kind of duralumin stone type bauxite preparing alumina from concentrate method " patent, disclose a kind of with in the diaspore type bauxite of low alumina silica ratio (A/S:4～8), behind direct-flotation desiliconisation, obtain aluminium concentrate (A/S＞10) and be the raw material production method of alumina.Its process is: the aluminium concentrate, circulation alkali liquor, milk of lime that does not need again ore grinding ratio on request adds pulp tank and carries out ore pulp and be mixed with qualified ore pulp, milk of lime obtains with circulation alkali liquor digestion lime, ore pulp is sent into the high pressure digester and is carried out the high pressure stripping after pre-desiliconization is handled, carry out conventional Bayer process production then.
In above-mentioned two patents, the lime in the preparation of stripping raw pulp all is the milk of lime that adopts circulation alkali liquor digestion to obtain.
For pursuing result of extraction preferably, the caustic sodium concentration Nk of Control Circulation alkali lye is than higher aborning, generally at 200～260g/l, and Al in its solution accordingly
2O
3Content at 90～160g/l, SiO
2Content about 0.5～1.5g/l.In production application, digest the raw pulp that lime is allocated with circulation alkali liquor, its stripping index is often relatively poor, even by strengthening the addition of lime, the calcium silicon that promptly improves the raw pulp solid phase is than (weight ratio of calcium oxide and silicon oxide) [C/S], also be difficult to make index to take a turn for the better, exsolution red mud alumina silica ratio (weight ratio of aluminum oxide and silicon oxide) A/S is up to more than 3.00 when serious, and the sodium-silicon-rate of red mud (weight ratio of sodium oxide and silicon oxide) N/S reaches more than 0.40.
Detect through above-mentioned red mud being carried out the thing phase composition, discovery has 1%～5% titaniferous ore that exists with anatase form, the milk of lime that adopts circulation alkali liquor digestion lime to obtain is described, calcium oxide does not play due effect in the milk of lime in process in leaching, cause exsolution red mud A/S higher, influenced the reduction of alkaline consumption in the raising of digesting efficiency of alumina and the alumina producing.
Analyzing its reason, mainly is that aluminum oxide, silicon oxide in the lime slaking process in calcium oxide and the circulation alkali liquor react with the milk of lime of circulation alkali liquor digestion, generates calcium aluminosilicate hydrate, and its molecular formula is 3CaO.Al
2O
3.xSiO
2. (6-2x) H
2O, because the concentration of aluminum oxide is far longer than the concentration of silicon oxide, so the value of x is less, promptly the weight ratio A/S of aluminum oxide and silicon oxide is bigger in the calcium aluminosilicate hydrate.
For diaspore type bauxite, scab for avoiding kaolinite in the ore to produce when the preheating, before the high pressure stripping, must to carry out 8～12 hours pre-desilicification process earlier.Calcium aluminosilicate hydrate is through for a long time pre-desiliconization, and its crystalline structure is progressively perfect, and it is very complete to observe its crystallization by Electronic Speculum.At process in leaching; the calcium aluminosilicate hydrate of complete crystallization decomposes slower; the activity that is lime reduces; calcium oxide can not be fully, react with titanium mineral in time, causes titanium mineral to be wrapped in the surface of diaspore, forms the sodium titanate protective membrane; hindered the stripping of diaspore; thereby the stripping index is worsened, and red mud A/S height causes the ore deposit consumption and the alkaline consumption of alumina producing to raise.
Summary of the invention
Purpose of the present invention is exactly at the deficiency in the above Technology, to existing be that the alumina producing Bayer process technology of raw material is improved with the diaspore type bauxite, propose the method for digestion lime in a kind of alumina producing, improve the result of extraction of the active of lime and then raising diaspore.
The digestion method of lime in a kind of alumina producing is characterised in that and adopts Al in the aluminum oxide production process
2O
3＜80g/l, SiO
2＜0.8g/l low concentration solution carries out commercial lime digestion, and milk of lime is 50～500g/l by after removing slag system removal breeze and indigested lime block impurity wherein admittedly contain.
Method of the present invention is characterized in that low concentration solution is one or more the mixture in the defective water of intermediate material aluminum hydroxide wash liquor, red mud wash liquor, evaporation of aluminum oxide production process, 30～96 ℃ of its solution temperatures.
Method of the present invention adopts the low concentration solution digestion lime in the aluminum oxide production process.During digestion lime, the concentration of calcium oxide is greater than the concentration of aluminum oxide and silicon oxide, so the calcium aluminosilicate hydrate amount that generates seldom, and the overwhelming majority exists with calcium hydroxide, thereby has improved the activity of lime.At the initial stage of raw pulp preheating and process in leaching, calcium hydroxide can very fast decomposition, makes CaO and TiO
2Reaction generates uhligite, hydroxyl calcium titanate or titanium calcium aluminosilicate hydrate, makes not regeneration sodium titanate protective membrane of diaspore surface, thereby accelerates the dissolution rate of diaspore, improves the solubility rate of aluminum oxide.
During operation, be 30～96 ℃, Al with lime slaking machine with temperature with commercial lime
2O
3Concentration＜80g/l, SiO
2The low concentration solution of concentration＜0.8g/l alumina producing pilot process digests, because the concentration of calcium oxide is greater than the concentration of aluminum oxide and silicon oxide in the milk of lime, so the calcium aluminosilicate hydrate amount that generates seldom, and the overwhelming majority exists with calcium hydroxide, thereby improved the activity of lime.Milk of lime is by removing slag system removal breeze and indigested lime block wherein.Its slag removal equipment can be a kind of among grading machine, roto-sifter, the swirler three, or the combination of any two kinds and two or more equipment.It is 50～500g/l that milk of lime after slagging-off contains admittedly.With this milk of lime allotment stripping raw pulp, through the pre-desiliconization of 8～12h, 260 ℃ of stripping temperature, time 60min after the conventional high pressure stripping of dissolution fluid caustic sodium concentration Nk210g/l, can obtain lower exsolution red mud A/S and N/S index.The present invention has optimized the stripping index, has both improved the solubility rate of aluminum oxide, has reduced alkaline consumption again.
Method of the present invention can improve the activity of digestion lime, improves SiO in the exsolution red mud calcium-silicon slag
2Saturation factor, reduce the A/S and the N/S of exsolution red mud, promptly reduced the ore deposit consumption and the alkaline consumption of alumina producing, reduce to produce consuming.Simultaneously, adopt the method for the solution digestion lime of lower concentration in the aluminum oxide production process, can reduce the addition of milk of lime in the raw pulp, reduce [C/S] of raw pulp, reduce the red mud output capacity, improve the effective capacity of equipment.
Embodiment
The digestion method of lime in a kind of alumina producing adopts Al in the aluminum oxide production process
2O
3＜80g/l, SiO
2＜0.8g/l low concentration solution carries out commercial lime digestion, milk of lime by remove slag system remove wherein breeze and impurity such as indigested lime block after to contain admittedly be 50～500g/l.Its low concentration solution is one or more the mixture in the defective water of intermediate material aluminum hydroxide wash liquor, red mud wash liquor, evaporation of aluminum oxide production process, 30～96 ℃ of its solution temperatures.
Embodiment 1
With 30 ℃, Al
2O
3: 55g/l, SiO
2: the aluminum hydroxide wash liquor digestion commercial lime of 0.42g/l, milk of lime after slagging-off contains admittedly and is 322g/l, ore pulp allotment stripping raw pulp with this milk of lime and after grinding, after 8 hours pre-desiliconization, 260 ℃ of stripping temperature, time 60min carries out conventional high pressure stripping under the leaching condition of dissolution fluid Nk210g/l, the exsolution red mud A/S that obtains is 1.46, and N/S is 0.21.
Embodiment 2
With 52 ℃, Al
2O
3: 79g/l, SiO
2: the aluminum hydroxide wash liquor digestion commercial lime of 0.46g/l, milk of lime after slagging-off contains admittedly and is 179g/l, allocate the stripping raw pulp with this milk of lime and the concentrate that obtains through flotation, circulation alkali liquor, pre-desiliconization and leaching condition are with embodiment one, the exsolution red mud A/S that obtains is 1.48, and N/S is 0.19.
Embodiment 3
With 92 ℃, Al
2O
3: 58g/l, SiO
2: the red mud wash liquor digestion commercial lime of 0.45g/l, milk of lime after slagging-off contains admittedly and is 285g/l, and with this milk of lime and the concentrate that obtains through flotation, circulation alkali liquor allotment stripping raw pulp, desiliconization and leaching condition are with embodiment one in advance, exsolution red mud A/S is 1.52, and N/S is 0.07.
Embodiment 4
With 63 ℃, Al
2O
3: 21.5g/l, SiO
2: the secondary red mud wash liquor digestion commercial lime of 0.31g/l, milk of lime after slagging-off contains admittedly and is 321g/l, and with this milk of lime and the concentrate that obtains through flotation, circulation alkali liquor allotment stripping raw pulp, desiliconization and leaching condition are with embodiment one in advance, exsolution red mud A/S is 1.42, and N/S is 0.11.
Embodiment 5
With 56 ℃, Al
2O
3: 66g/l, SiO
2: the aluminum hydroxide wash liquor digestion commercial lime of 0.44g/l, milk of lime after slagging-off contains admittedly and is 230g/l, and with this milk of lime and the concentrate that obtains through flotation, circulation alkali liquor allotment stripping raw pulp, desiliconization and leaching condition are with embodiment one in advance, exsolution red mud A/S is 1.50, and N/S is for O.12.
Embodiment 6
With 96 ℃, Al
2O
3: 0.25g/l, SiO
2: the defective water digestion of the evaporation of 0.002g/l commercial lime, milk of lime after slagging-off contains admittedly and is 210g/l, and with this milk of lime and the concentrate that obtains through flotation, circulation alkali liquor allotment stripping raw pulp, desiliconization and leaching condition are with embodiment one in advance, exsolution red mud A/S is 1.35, and N/S is 0.12.
Embodiment 7
With 94 ℃, Al
2O
3: 0.15g/l, SiO
2: the defective water digestion of the evaporation of 0.002g/l commercial lime, milk of lime after slagging-off contains admittedly and is 210g/l, and with this milk of lime with the allotment of the ore pulp after grinding stripping raw pulp, desiliconization and leaching condition are with embodiment one in advance, exsolution red mud A/S is 1.31, and N/S is 0.09.
Embodiment 8
With 86 ℃, Al
2O
3: 21.5g/l, SiO
2: the secondary red mud wash liquor digestion commercial lime of 0.31g/l, milk of lime after slagging-off contains admittedly and is 303g/l, and with this milk of lime with the allotment of the ore pulp after grinding stripping raw pulp, desiliconization and leaching condition are with embodiment one in advance, exsolution red mud A/S is 1.37, and N/S is 0.12.
Claims (2)
1. the digestion method of lime in the alumina producing is characterised in that and adopts Al in the aluminum oxide production process
2O
3＜80g/l, SiO
2＜0.8g/l low concentration solution carries out commercial lime digestion, and milk of lime is 50～500g/l by after removing slag system removal breeze and indigested lime block impurity wherein admittedly contain.
2. method according to claim 1 is characterized in that low concentration solution is one or more the mixture in the defective water of intermediate material aluminum hydroxide wash liquor, red mud wash liquor, evaporation of aluminum oxide production process, 30～96 ℃ of its solution temperatures.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200610103784 CN1887714A (en) | 2006-08-01 | 2006-08-01 | Lime slaking process for alumina production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200610103784 CN1887714A (en) | 2006-08-01 | 2006-08-01 | Lime slaking process for alumina production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1887714A true CN1887714A (en) | 2007-01-03 |
Family
ID=37576994
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200610103784 Pending CN1887714A (en) | 2006-08-01 | 2006-08-01 | Lime slaking process for alumina production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1887714A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102674416A (en) * | 2012-05-18 | 2012-09-19 | 义马煤业集团股份有限公司 | Method for producing aluminum oxide-lime blend ores by Bayer process |
| CN103663517A (en) * | 2013-11-26 | 2014-03-26 | 中国铝业股份有限公司 | Method for reducing proportion of sodium and silicone in red mud dissolved out by ore dressing Bayer process |
| CN105621379A (en) * | 2016-04-13 | 2016-06-01 | 四川绵竹市盘龙矿物质有限责任公司 | Improved three-stage neutralization crystallization method in feed-grade calcium hydrogen phosphate production technique |
-
2006
- 2006-08-01 CN CN 200610103784 patent/CN1887714A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102674416A (en) * | 2012-05-18 | 2012-09-19 | 义马煤业集团股份有限公司 | Method for producing aluminum oxide-lime blend ores by Bayer process |
| CN102674416B (en) * | 2012-05-18 | 2014-02-05 | 义马煤业集团股份有限公司 | Method for producing aluminum oxide-lime blend ores by Bayer process |
| CN103663517A (en) * | 2013-11-26 | 2014-03-26 | 中国铝业股份有限公司 | Method for reducing proportion of sodium and silicone in red mud dissolved out by ore dressing Bayer process |
| CN103663517B (en) * | 2013-11-26 | 2016-07-13 | 中国铝业股份有限公司 | A kind of method reducing Liquor of Ore Dressing Bayer process exsolution red mud sodium-silicon-rate |
| CN105621379A (en) * | 2016-04-13 | 2016-06-01 | 四川绵竹市盘龙矿物质有限责任公司 | Improved three-stage neutralization crystallization method in feed-grade calcium hydrogen phosphate production technique |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US9139445B2 (en) | Method for co-producing alumina and activated calcium silicate from high-alumina fly ash | |
| CN1956925A (en) | Improvement to the bayer process for the production of alumina trihydrate by means of alkaline leaching of bauxite, said method comprising a predesilicification step | |
| CN101054626A (en) | Stripping method for diasporite type bauxite | |
| CN1156399C (en) | Alumina producing process with hydraulic duralumin-type bauxite concentrate | |
| CN103130254A (en) | Method for producing aluminum oxide by using alkaline method | |
| US7767190B2 (en) | Inhibiting the formation of TCA in a Bayer causticisation process | |
| CN108840361B (en) | A method of high-purity calcium carbonate is refined using green liquor causticizing | |
| CN113979457A (en) | Dealkalization method for Bayer process red mud | |
| CN1186259C (en) | Bayer production method for aluminium oxide | |
| CN1887714A (en) | Lime slaking process for alumina production | |
| CN1092604C (en) | Removal of silica from bauxite | |
| CN1238085C (en) | Improved process for filter aid production in alumina refineries | |
| CN101734696B (en) | Method for removing organic matter by Bayer process | |
| CN1868881A (en) | Technological process method of producing aluminium oxide using high aluminium slag | |
| CN1281503C (en) | Silicon slag treatment method in aluminium oxide production process | |
| CN1686809A (en) | Method of reverse flotation for preparing alumina from concentrate of beauxite | |
| CN1565974A (en) | Normal pressure low temperature leaching production method for alumina | |
| CN1380253A (en) | Alumina production process by using monohydrate bauxite lime Bayer process | |
| CN1280099A (en) | Technology for producing alumina via high alumina to silica ratio sintering process | |
| CN113772700A (en) | Medicament for improving stability of Bayer process red mud slurry and preparation method and application thereof | |
| CN102976376A (en) | Dissolving out method of high-sulfur bauxite | |
| CN1631783A (en) | Combined method for producing alumina to decrease alpha k of Bayer process concentrated liquid | |
| CN1267354C (en) | Desilication method for sodium aluminate solution with high concentration | |
| CN1775686A (en) | Method for producing alumina by adding ore and concentrating after hydraulic aluminous stone type bauxite stripping | |
| CN1597525A (en) | Silicon slag removal treatment method in aluminium oxide production process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |