CN108726545A - A kind of impurity-removing method of middle-low bauxite - Google Patents
A kind of impurity-removing method of middle-low bauxite Download PDFInfo
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- CN108726545A CN108726545A CN201710260854.7A CN201710260854A CN108726545A CN 108726545 A CN108726545 A CN 108726545A CN 201710260854 A CN201710260854 A CN 201710260854A CN 108726545 A CN108726545 A CN 108726545A
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- Prior art keywords
- bauxite
- roasting
- impurity
- desiliconization
- lye
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- 229910001570 bauxite Inorganic materials 0.000 title claims abstract description 128
- 238000000034 method Methods 0.000 title claims abstract description 93
- 239000007788 liquid Substances 0.000 claims abstract description 55
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 44
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 39
- 230000008569 process Effects 0.000 claims abstract description 38
- 238000006243 chemical reaction Methods 0.000 claims abstract description 32
- 238000000926 separation method Methods 0.000 claims abstract description 29
- 239000012141 concentrate Substances 0.000 claims abstract description 26
- 239000005864 Sulphur Substances 0.000 claims abstract description 25
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 22
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 22
- 238000012545 processing Methods 0.000 claims abstract description 17
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims abstract description 16
- 235000011941 Tilia x europaea Nutrition 0.000 claims abstract description 16
- 239000004571 lime Substances 0.000 claims abstract description 16
- 238000005065 mining Methods 0.000 claims abstract description 7
- 239000000378 calcium silicate Substances 0.000 claims abstract description 6
- 229910052918 calcium silicate Inorganic materials 0.000 claims abstract description 6
- OYACROKNLOSFPA-UHFFFAOYSA-N calcium;dioxido(oxo)silane Chemical compound [Ca+2].[O-][Si]([O-])=O OYACROKNLOSFPA-UHFFFAOYSA-N 0.000 claims abstract description 6
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Substances [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 81
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 34
- 239000011593 sulfur Substances 0.000 claims description 24
- 229910052717 sulfur Inorganic materials 0.000 claims description 24
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims description 16
- 239000000377 silicon dioxide Substances 0.000 claims description 13
- 239000000920 calcium hydroxide Substances 0.000 claims description 10
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 10
- 239000007787 solid Substances 0.000 claims description 8
- 229910052782 aluminium Inorganic materials 0.000 claims description 6
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 6
- 239000004411 aluminium Substances 0.000 claims description 6
- 238000001354 calcination Methods 0.000 claims description 6
- 239000000779 smoke Substances 0.000 claims description 6
- 238000010521 absorption reaction Methods 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 5
- 238000000227 grinding Methods 0.000 claims description 4
- 230000035484 reaction time Effects 0.000 claims description 4
- 238000003723 Smelting Methods 0.000 claims description 2
- CREMABGTGYGIQB-UHFFFAOYSA-N carbon carbon Chemical compound C.C CREMABGTGYGIQB-UHFFFAOYSA-N 0.000 claims description 2
- 239000011203 carbon fibre reinforced carbon Substances 0.000 claims description 2
- 239000000725 suspension Substances 0.000 claims 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 abstract description 17
- 229910052710 silicon Inorganic materials 0.000 abstract description 17
- 239000010703 silicon Substances 0.000 abstract description 17
- 239000012535 impurity Substances 0.000 abstract description 15
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 239000003513 alkali Substances 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract description 3
- 238000002386 leaching Methods 0.000 abstract description 2
- 239000002910 solid waste Substances 0.000 abstract 1
- 238000006477 desulfuration reaction Methods 0.000 description 18
- 239000002994 raw material Substances 0.000 description 14
- 230000023556 desulfurization Effects 0.000 description 13
- 239000000203 mixture Substances 0.000 description 10
- 239000011734 sodium Substances 0.000 description 10
- 238000004131 Bayer process Methods 0.000 description 9
- 235000012241 calcium silicate Nutrition 0.000 description 9
- 230000000052 comparative effect Effects 0.000 description 9
- 238000005188 flotation Methods 0.000 description 9
- 239000005416 organic matter Substances 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 239000007789 gas Substances 0.000 description 6
- 229910052900 illite Inorganic materials 0.000 description 6
- 229910052500 inorganic mineral Inorganic materials 0.000 description 6
- 235000010755 mineral Nutrition 0.000 description 6
- 239000011707 mineral Substances 0.000 description 6
- VGIBGUSAECPPNB-UHFFFAOYSA-L nonaaluminum;magnesium;tripotassium;1,3-dioxido-2,4,5-trioxa-1,3-disilabicyclo[1.1.1]pentane;iron(2+);oxygen(2-);fluoride;hydroxide Chemical compound [OH-].[O-2].[O-2].[O-2].[O-2].[O-2].[F-].[Mg+2].[Al+3].[Al+3].[Al+3].[Al+3].[Al+3].[Al+3].[Al+3].[Al+3].[Al+3].[K+].[K+].[K+].[Fe+2].O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2.O1[Si]2([O-])O[Si]1([O-])O2 VGIBGUSAECPPNB-UHFFFAOYSA-L 0.000 description 6
- 238000002360 preparation method Methods 0.000 description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000003546 flue gas Substances 0.000 description 5
- 239000012452 mother liquor Substances 0.000 description 4
- 230000002829 reductive effect Effects 0.000 description 4
- QJZYHAIUNVAGQP-UHFFFAOYSA-N 3-nitrobicyclo[2.2.1]hept-5-ene-2,3-dicarboxylic acid Chemical compound C1C2C=CC1C(C(=O)O)C2(C(O)=O)[N+]([O-])=O QJZYHAIUNVAGQP-UHFFFAOYSA-N 0.000 description 3
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- KZHJGOXRZJKJNY-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Si]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O KZHJGOXRZJKJNY-UHFFFAOYSA-N 0.000 description 3
- 239000011521 glass Substances 0.000 description 3
- 239000004021 humic acid Substances 0.000 description 3
- 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 3
- 229910052622 kaolinite Inorganic materials 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 229910052863 mullite Inorganic materials 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 230000002441 reversible effect Effects 0.000 description 3
- 239000004575 stone Substances 0.000 description 3
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 2
- 239000004115 Sodium Silicate Substances 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 238000011953 bioanalysis Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000005261 decarburization Methods 0.000 description 2
- 229910001648 diaspore Inorganic materials 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 235000019795 sodium metasilicate Nutrition 0.000 description 2
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 description 2
- 229910052911 sodium silicate Inorganic materials 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000005995 Aluminium silicate Substances 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- KMWBBMXGHHLDKL-UHFFFAOYSA-N [AlH3].[Si] Chemical compound [AlH3].[Si] KMWBBMXGHHLDKL-UHFFFAOYSA-N 0.000 description 1
- YKTSYUJCYHOUJP-UHFFFAOYSA-N [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] Chemical compound [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] YKTSYUJCYHOUJP-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 235000012211 aluminium silicate Nutrition 0.000 description 1
- 229910000323 aluminium silicate Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- ZOOODBUHSVUZEM-UHFFFAOYSA-N ethoxymethanedithioic acid Chemical compound CCOC(S)=S ZOOODBUHSVUZEM-UHFFFAOYSA-N 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000009931 harmful effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000000670 limiting effect Effects 0.000 description 1
- 235000006408 oxalic acid Nutrition 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 229920001296 polysiloxane Polymers 0.000 description 1
- 238000012805 post-processing Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 description 1
- 229910052683 pyrite Inorganic materials 0.000 description 1
- 239000011028 pyrite Substances 0.000 description 1
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical class O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000012991 xanthate Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
- C01F7/06—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process
- C01F7/0606—Making-up the alkali hydroxide solution from recycled spent liquor
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/20—Silicates
- C01B33/24—Alkaline-earth metal silicates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/46—Sulfates
- C01F11/464—Sulfates of Ca from gases containing sulfur oxides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
The present invention provides a kind of impurity-removing methods of middle-low bauxite, the described method comprises the following steps：(1) bauxite feeding fluidized roaster is roasted, air is passed through in roasting process, the bauxite after being roasted；(2) bauxite after the roasting obtained is mixed with lye carries out desilication reaction, is separated by solid-liquid separation, obtains bauxite concentrate and desiliconization liquid；(3) it after the desiliconization liquid carries out desiliconization processing, is separated by solid-liquid separation, obtains calcium silicate products and lye, return to step (2) recycles after gained lye adjustment concentration.The present invention not only improves the grade of ore, more realizes the recycling of difficult mining seam by removing the impurity such as silicon, sulphur and carbon in middle-low bauxite；Reduce the consumption of alkali, lime in alumina leaching process, while reducing the discharge capacity of red mud.Present invention reduces alumina production costs, reduce solid waste discharge, and roasting process energy consumption is relatively low, have good economic and environment-friendly benefit.
Description
Technical field
The invention belongs to bauxite impurity removing technology fields, are related to a kind of impurity-removing method of middle-low bauxite, especially relate to
And a kind of impurity-removing method of middle-low grade fluosolids roasting.
Background technology
The bauxite resource in China has the characteristics that high alumina, high silicon and low alumina -silica ratio, alumina silica ratio account for money in 5 ores below
70% or more of source total amount.In recent years, domestic alumina industry development is swift and violent, consumes a large amount of bauxite, China's alumina silica ratio is 7
Above high-grade bauxite has been on the verge of exhaustion, and numerous Alumina Enterprises are forced to use middle-low bauxite.Middle-low grade aluminium
Impurity is more in native mine, wherein it is mainly silicon, sulphur and organic matter to influence maximum impurity to alumina producing Bayer process technique.Directly
It connects and uses such raw material, equipment and the technical indicator of Bayer process flow will face significant challenge, and production cost sharply increases, therefore
It need to clean to such bauxite to meet the requirement of bayer process.
When producing aluminium oxide using bayer process, the SiO in ore2It will react with sodium hydroxide, calcium oxide, disappear simultaneously
It consumes partial oxidation aluminium and generates red mud.Therefore, the silicone content in middle-low bauxite is excessively high, will increase cost of material, influences oxygen
Change the rate of recovery of aluminium, while increasing red mud discharge capacity.Sulfur-type middle-low bauxite accounts for about China's alumina ore reserves
4.7%, wherein total sulphur content is known as high-sulfur mine higher than 0.7%.Since sulphur can be with S in aluminum oxide production process2-、S2O3 2-、
SO3 2-And SO4 2-Etc. forms accumulated in circulating mother liquor, influence evaporate and plant operation break-down, to equipment and operation bring harm, so
For high sulfur type middle-low bauxite, desiliconization is not only needed, it is also desirable to desulfurization.In China's bauxite, there is also 0.1%~
0.3% organic carbon, in high-sulfur mine, organic carbon content higher, up to 0.5%~2.0%, although the organic matter in raw ore contains
Amount is not high, but organic matter can be accumulated gradually in Bayer process flow, until reaching balance.Organic matter makes solution viscosity increase
Add, reduce red-mud settlement speed, increases washing difficulty, while influencing kind of a point process, reduce decomposition rate, then influence aluminium oxide
Yield and product quality.
Currently, the method for bauxite desilication includes mainly bioanalysis, Physical and chemical method.Bioanalysis refers to utilizing silicic acid
Salt bacterium can dissolve the characteristic of aluminium silicate mineral, convert the silicon in bauxite to soluble matter；Physical uses flotation medicine
Agent carries out direct flotation or reverse flotation, to obtain concentrate to ore；Chemical method includes preroast-alkali liquor desiliconization method and lye
Desiliconization method is directly dissolved out, after the former refers to the fired processing of bauxite, the higher amorphous silica of activity is obtained, uses lye
Leach the activated silica in roasted ore, lifting ore alumina silica ratio；The latter is using gangue with diaspore in specified conditions and medium
Dissolubility difference under environment carries out desiliconization.Desulfurization technology includes mainly the methods of reverse flotation desulfurizing and desulfurization with roasting technique.Reverse flotation
Sulfur removal technology uses xanthate collectors flotation containing sulfur minerals；Desulfurization with roasting technique technology roasts sulfur bauxite under middle low temperature, leads to
Enter air and sulphur is oxidized to sulfur dioxide gas, realizes sulphur, mine separation.The method for removing of organic matter include to ore or mother liquor into
Row processing, the former removes organic carbon including the use of the mode of roast ore；The latter include mother liquor calcining, absorption, precipitation etc., but this
A little methods are all to carry out in the solution, i.e., the organic matter in bauxite first dissolves post-processing, increases operating cost.
CN 102151614A disclose a kind of ore dressing and desiliconizing sulfur method of sulfur bauxite to be made using the method for ore dressing
With sulphur acid for adjusting pH, silicate collecting agent, sulfur-bearing gangue mineral collecting agent, after stirring flotation, siliceous, sulphur impurity mine are added
Stone emersion is as foam tailing, and the ore pulp after flotation is as concentrate.Though this method can effectively remove silicon, sulphur impurity in ore,
The sulfuric acid and various medicaments used not only increases cost, also increases the cumulant of floating agent in the solution, to follow-up molten
Go out, plant process of grading and cause harmful effect.
CN 105562212A disclose silicon, the sulphur that bauxite is removed using the method for flotation, but flow is complicated, water consumption
Greatly, using compared with multi-agent, bauxite dissolution is influenced.
CN 1266816A disclose a kind of process for desiliconizing diasporite type bauxite, using belt type roasting machine at 950 DEG C
Lower roasting bauxite, then through alkali leaching dissolution, be separated by solid-liquid separation, can effective desiliconization, ore alumina silica ratio is promoted to 9.3 by 4.4.
But it needs to pre-process ore, roasting process is used for the purpose of desiliconization, and does not consider the removing of other impurities, roasts
Journey energy consumption is higher, and heat recovery is difficult.
CN 103408047A mention a kind of high-sulfur bauxite suspended state preheating and baking desulfurization-and are quickly cooled down technique, 450
Bauxite is roasted under conditions of~750 DEG C, desulfuration efficiency is more than 60%.It roasts more using cyclone separator progress in cooling procedure
Grade heat exchange, for recycling heat to preheat ore, energy consumption is relatively low, but can not lifting ore alumina silica ratio.
Invention content
For problems of the prior art, the present invention provides a kind of impurity-removing methods of middle-low bauxite.This
Invention uses high-temperature roasting bauxite, under conditions of being passed through sufficient air, removes the sulphur and carbon impurity in ore, while making height
The siliceous minerals such as ridge stone, pyrophillite and illite decompose, and obtain amorphous amorphous silica, improve silicon dioxde reaction
Activity.It is reacted at low temperature after bauxite after roasting is mixed with sig water, through filtering, you can realize desilication.Desiliconization
After obtain concentrate, can be used for bayer process production aluminium oxide.The present invention by removing the impurity such as silicon, sulphur and carbon in ore,
The grade of ore is improved, the middle-low bauxite that largely not up to Bayer process raw material technology requires is made to have utility value；
Lye and lime consumption are reduced simultaneously, reduce cost of material.The present invention does not add additive, and alumina recovery rate can be made to improve,
Red mud amount is reduced, and is not only reduced the wasting of resources, is more reduced the influence to environment.It, can be with into the silicon in sig water in the present invention
Lime reaction generates calcium silicates class product, has not only realized efficiently separating for aluminium silicon in raw material, but also provide for efficiently using for silicon
Prerequisite.Milk of lime or red mud can be used to absorb for the sulfide that roasting process generates, and widen making for high-sulfur bauxite significantly
With approach, and environmental hazard can minimize.
For this purpose, the present invention uses following technical scheme：
The present invention provides a kind of impurity-removing methods of middle-low bauxite, the described method comprises the following steps：
(1) bauxite feeding fluidized roaster is roasted, air is continually fed into roasting process, after obtaining roasting
Bauxite；
(2) bauxite after the roasting obtained through step (1) is mixed with lye carries out desilication reaction, is separated by solid-liquid separation, obtains
Bauxite concentrate and desiliconization liquid；
(3) it after desiliconization liquid described in step (2) being carried out desiliconization processing, is separated by solid-liquid separation, obtains calcium silicate products and lye,
Return to step (2) recycles after gained lye adjustment concentration.
The present invention uses high-temperature roasting bauxite, and under conditions of being passed through sufficient air, the sulphur and carbon in removing ore are miscellaneous
Matter, while the siliceous minerals such as kaolinite, pyrophillite and illite being made to decompose, amorphous amorphous silica is obtained, is improved
Silicon dioxde reaction activity.
Following reaction specifically mainly occurs in roasting process：
Kaolinite, pyrophillite and illite etc. decompose at high temperature containing silicon impurities, and kaolinite is finally decomposed to spinelle, weak
Crystallize mullite and amorphous silica.
Pyrophillite is finally decomposed to mullite and amorphous silica.
Illite dehydration after through glass phase transition be mullite.
The oxidation by air at high temperature of the sulfur-containing impurities such as pyrite.
The oxidation by air at high temperature of the organic matters such as humic acid.
Desiliconization processing carried out to the bauxite after roasting with lye in step (2), amorphous silica or glass phase
Silicon in dehydration illite can react at low temperature with sodium hydroxide, generate sodium metasilicate and enter solution, reaction is as follows：
It is used as currently preferred technical solution below, but not as the limitation of technical solution provided by the invention, passes through
Following technical scheme can preferably reach and realize the technical purpose and advantageous effect of the present invention.
As currently preferred technical solution, in step (1) described bauxite the content of silica be 10wt%~
30wt%, such as 11wt%, 13wt%, 15wt%, 17wt%, 20wt%, 23wt%, 25wt% or 27wt% etc., but not
It is only limitted to cited numerical value, other unrequited numerical value are equally applicable in the numberical range；Total sulphur content be 0.7wt%~
5wt%, for example, 0.8wt%, 1wt%, 1.5wt%, 2wt%, 2.5wt%, 3wt%, 3.5wt%, 4wt%, 4.5wt% or
4.7wt% etc., it is not limited to cited numerical value, other interior unrequited numerical value of the numberical range are equally applicable；It is organic
The content of carbon be 0.1wt%~2wt%, such as 0.3wt%, 0.5wt%, 0.7wt%, 1wt%, 1.3wt%, 1.5wt%,
1.7wt% or 1.9wt% etc., it is not limited to cited numerical value, other interior unrequited numerical value of the numberical range are same
It is applicable in.
In the present invention, the bauxite is middle-low bauxite, and wherein impurity content is higher, most for quality in bauxite
The bauxite of difference.
Preferably, step (1) described bauxite is sent into fluidized roaster after pretreatment.
Preferably, the pretreatment is grinding and preheating.
Preferably, described to be ground to：70%~90% of the bauxite by grinding is set to sieve with 100 mesh sieve.
Preferably, the preheating temperature be 300 DEG C~500 DEG C, such as 300 DEG C, 330 DEG C, 350 DEG C, 370 DEG C, 400 DEG C,
430 DEG C, 450 DEG C, 470 DEG C or 500 DEG C etc., it is not limited to cited numerical value, other are unrequited in the numberical range
Numerical value is equally applicable.
As currently preferred technical solution, fluidized roaster described in step (1) is gaseous pollutant control, stream
Change any one in bed circulating roaster or Flash Smelting Furnace.
Preferably, the calcination temperature of step (1) described roasting be 800 DEG C~1100 DEG C, such as 810 DEG C, 830 DEG C, 850
DEG C, 870 DEG C, 900 DEG C, 930 DEG C, 950 DEG C, 970 DEG C, 1000 DEG C, 1030 DEG C, 1050 DEG C or 1070 DEG C etc., it is not limited to
Cited numerical value, other interior unrequited numerical value of the numberical range are equally applicable, preferably 900 DEG C~1050 DEG C.
In the present invention, the roasting needs to control to be carried out under the high temperature conditions, if temperature is too low, siliceous mineral can be made to decompose
Not exclusively；But also not the higher the better for temperature, amorphous silica can be made to be recombined into not with aluminium oxide if temperature is excessively high
Carry out stone, and then influences final impurity-eliminating effect.
Preferably, the roasting time of step (1) described roasting be 0.1min~60min, such as 0.3min, 1min, 5min,
10min, 15min, 20min, 25min, 30min, 35min, 40min, 45min, 50min, 55min or 57min etc., but simultaneously not only
It is limited to cited numerical value, other unrequited numerical value are equally applicable in the numberical range, preferably 1min~10min.
In the present invention, enough air are passed through into roasting process, its object is to make to keep abundance in roasting process
Air refers to also needing to consider sulphur and organic carbon content in ore, making air not in addition to considering roasting apparatus pattern and fuel type
Be only capable of making ore fluidization, also can fully in ore sulphur and organic carbon react.
Preferably, total sulphur content < 0.1wt% in the bauxite after step (1) described roasting, such as 0.09wt%,
0.07wt%, 0.05wt% or 0.03wt% etc. and lower loading, it is not limited to cited numerical value, the numberical range
Other interior unrequited numerical value are equally applicable；Organic carbon content < 0.1wt%, such as 0.09wt%, 0.07wt%, 0.05wt%
Or 0.03wt% etc. and lower loading, it is not limited to cited numerical value, other unrequited numbers in the numberical range
It is worth equally applicable.
As currently preferred technical solution, the sulfur-containing smoke gas generated in step (1) described roasting process carries out tail gas
Absorption is handled.
Preferably, the tail gas absorption, which is handled, is：The sulfur-containing smoke gas of generation is passed through in milk of lime and is reacted, is then consolidated
Liquid detaches, and obtains calcium sulfate product.
As currently preferred technical solution, the bauxite after being roasted described in step (2) is mixed with lye after cooling
It closes.
Preferably, described to be cooled to：Bauxite after roasting is cooled down through cyclone separator, is cooled to out material temperature
Degree.
Preferably, the drop temperature be 80 DEG C~200 DEG C, such as 80 DEG C, 100 DEG C, 120 DEG C, 140 DEG C, 160 DEG C, 180
DEG C or 200 DEG C etc., it is not limited to cited numerical value, other unrequited numerical value are equally applicable in the numberical range.
Preferably, the high temperature air generated in the cooling procedure is for preheating bauxite.
Preferably, the temperature of the high temperature air be 200 DEG C~400 DEG C, such as 200 DEG C, 230 DEG C, 250 DEG C, 270 DEG C,
300 DEG C, 330 DEG C, 350 DEG C, 370 DEG C or 400 DEG C etc., it is not limited to cited numerical value, in the numberical range, other are not
The numerical value enumerated is equally applicable.
As currently preferred technical solution, Na in step (2) described lye2A concentration of 50g/L~140g/L of O,
Such as 53g/L, 55g/L, 60g/L, 65g/L, 70g/L, 75g/L, 80g/L, 85g/L, 90g/L, 95g/L, 100g/L, 105g/
L, 110g/L, 115g/L, 120g/L, 125g/L, 130g/L, 135g/L or 137g/L etc., it is not limited to cited number
Value, other interior unrequited numerical value of the numberical range are equally applicable, preferably 80g/L~120g/L.
The present invention carries out desiliconization processing using sig water, can make amorphous silica or the dehydration illite of glass phase
In silicon can be reacted at low temperature with sodium hydroxide, generate sodium metasilicate enter solution.The concentration of sig water needs to control one
Determine in range, if concentration of lye is excessively high, desilication efficiency will not continue to improve；If concentration of lye is too low, silicon dioxde reaction can be made
It is not thorough.
Preferably, the reaction temperature of desilication reaction described in step (2) be 70 DEG C~110 DEG C, such as 73 DEG C, 75 DEG C, 80
DEG C, 83 DEG C, 85 DEG C, 90 DEG C, 95 DEG C, 100 DEG C, 105 DEG C or 107 DEG C etc., it is not limited to cited numerical value, the numerical value model
Other unrequited numerical value are equally applicable in enclosing, preferably 90 DEG C~100 DEG C.
Preferably, the reaction time of desilication reaction described in step (2) be 20min~210min, such as 23min,
25min, 30min, 50min, 70min, 100min, 130min, 150min, 170min or 200min etc., it is not limited to institute
The numerical value enumerated, other interior unrequited numerical value of the numberical range are equally applicable, preferably 30min~100min.
Preferably, the liquid-solid ratio of desilication reaction described in step (2) is (2~15):1, such as 2.5:1,3:1,4:1,5:
1,6:1,7:1,8:1,9:1,10:1,11:1,12:1,13:1 or 14:1 etc., it is not limited to cited numerical value, the numerical value
Other unrequited numerical value are equally applicable in range, and preferably 5:1.
As currently preferred technical solution, alumina content is 60wt% in bauxite concentrate described in step (2)
~80wt%, dioxide-containing silica < 10wt%, total sulphur content < 0.1wt%, organic carbon carbon content < 0.1wt%.
As currently preferred technical solution, the processing of desiliconization described in step (2) is：Desiliconization liquid is mixed with lime.
Preferably, the lime consumption is：The molar ratio of lime and silica in desiliconization liquid>2, for example, 3,4,5,6,7,
8 or 9 etc. and higher, it is not limited to cited numerical value, other unrequited numerical value are equally applicable in the numberical range.
As currently preferred technical solution, the described method comprises the following steps：
(1) bauxite is ground with after preheating, is sent into fluidized roaster and carries out roasting 1min at 900 DEG C~1050 DEG C
~10min is continually fed into air in roasting process, and the bauxite after being roasted, wherein total sulphur content < 0.1wt% are organic
Carbon content < 0.1wt%；The sulfur-containing smoke gas generated in roasting process, which is passed through in milk of lime, to react, and is then separated by solid-liquid separation, is obtained
To calcium sulfate product；
(2) the mining cyclone separator of alumina after the roasting obtained through step (1) is cooled down, and is cooled to drop temperature,
Then with Na2The lye of a concentration of 80g/L~120g/L of O be blended at 90 DEG C~100 DEG C carry out desilication reaction 30min~
The liquid-solid ratio of 100min, desilication reaction are 5:1, it is then separated by solid-liquid separation, obtains bauxite concentrate and desiliconization liquid；
(3) desiliconization liquid described in step (2) is mixed after carrying out desiliconization processing with lime, is separated by solid-liquid separation, obtains calcium silicates
Product and lye, return to step (2) recycles after gained lye adjusts concentration.
Compared with prior art, the invention has the advantages that：
(1) present invention is passed through sufficient air using fluidized roaster at 800 DEG C~1100 DEG C, is carried out to bauxite
High-temperature roasting cleans, and desiliconization and desulfuration efficiency are high, and desilication efficiency is up to 75%, and desulfuration efficiency is up to 90% or more；Meanwhile it removing
The removal efficiency of organic carbon in ore, organic carbon alleviates the impurity such as silicon, sulphur and carbon to alumina producing Bayer process up to 75%
The harm of process；
(2) heat of bauxite after the present invention is roasted using cyclone separator recycling, and to preheat bauxite, roasted
The comprehensive energy consumption of journey is relatively low；
(3) present invention using sig water at low temperature to after roasting bauxite carry out desiliconization processing, desiliconization mild condition,
It is easy to operate, the alumina silica ratio of middle-low bauxite is effectively improved, it is difficult to provide cost-effective utilization side using resource
Method；
(4) present invention absorbs the sulfide in flue gas with milk of lime or red mud after Desilication by roasting；It is extracted using lime
Calcium silicate products is made in silicate in sig water, and technique is environmentally protective, without pollutant emission；
(5) in ore organic matter removing, avoid the organic matters such as humic acid, oxalic acid and humic acid in circulating mother liquor
Accumulation, improves follow-up solid-liquid separation process, such as settles, the separative efficiency of filtering.
Description of the drawings
Fig. 1 is the process fluid figure of the impurity-removing method of 1 middle-low bauxite of the embodiment of the present invention.
Specific implementation mode
For the present invention is better described, it is easy to understand technical scheme of the present invention, below further specifically to the present invention
It is bright.But following embodiments is only the simple example of the present invention, does not represent or limit the scope of the present invention, this
Invention protection domain is subject to claims.
Specific embodiment of the invention part provides a kind of impurity-removing method of middle-low bauxite, the method includes with
Lower step：
(1) bauxite feeding fluidized roaster is roasted, air is passed through in roasting process, the aluminium after being roasted
Tu Kuang；
(2) bauxite after the roasting obtained through step (1) is mixed with lye carries out desilication reaction, is separated by solid-liquid separation, obtains
Bauxite concentrate and desiliconization liquid；
(3) it after desiliconization liquid described in step (2) being carried out desiliconization processing, is separated by solid-liquid separation, obtains calcium silicate products and lye,
Return to step (2) recycles after gained lye adjustment concentration.
It is present invention typical case but non-limiting embodiment below：
Embodiment 1：
The present embodiment uses middle-low bauxite of the present invention by raw material of Henan somewhere middle-low bauxite
Impurity-removing method clean, the composition of the bauxite (mass percent, wt%, similarly hereinafter) is as shown in table 1.
Table 1
Specific dedoping step is as shown in Figure 1, include the following steps：
(1) bauxite is ground, until 80% sieves with 100 mesh sieve, fluidized roaster is sent into after preheated at 950 DEG C
Roasting 10min is carried out, enough air is passed through in roasting process, the bauxite after being roasted, the wherein mass fraction of S is
0.01wt%, desulfurization degree 89%；The mass fraction of C is 0.1wt%, carbon-drop rate 67%；The sulfur-bearing generated in roasting process
Flue gas, which is passed through in milk of lime, to react, and is then separated by solid-liquid separation, obtains calcium sulfate product；
(2) the mining cyclone separator of alumina after the roasting obtained through step (1) is cooled down, and is cooled to drop temperature,
Then with Na2The lye of a concentration of 110g/L of O is blended in progress desilication reaction 90min, the liquid-solid ratio of desilication reaction at 100 DEG C
It is 4:1, it is then separated by solid-liquid separation, obtains bauxite concentrate and desiliconization liquid；Wherein, Al in concentrate2O3Mass fraction be 72.34%,
A/S is 5.79, and desiliconization rate is 63.0%；
(3) desiliconization liquid described in step (2) is mixed after carrying out desiliconization processing with lime, is separated by solid-liquid separation, obtains calcium silicates
Product and lye, return to step (2) recycles after gained lye adjusts concentration.
Embodiment 2：
The present embodiment uses middle-low bauxite of the present invention by raw material of Henan somewhere middle-low bauxite
Impurity-removing method clean, the composition of the bauxite (mass percent, wt%, similarly hereinafter) is as shown in table 2.
Table 2
Specific dedoping step includes the following steps：
(1) bauxite is ground, until 73% sieves with 100 mesh sieve, fluidized roaster is sent into after preheated at 1000 DEG C
Under carry out roasting 5min, be passed through enough air in roasting process, the bauxite after being roasted, the wherein mass fraction of S is
0.01wt%, desulfurization degree 90%；The mass fraction of C is 0.1wt%, carbon-drop rate 64%；The sulfur-bearing generated in roasting process
Flue gas, which is passed through in milk of lime, to react, and is then separated by solid-liquid separation, obtains calcium sulfate product；
(2) the mining cyclone separator of alumina after the roasting obtained through step (1) is cooled down, and is cooled to drop temperature,
Then with Na2The lye of a concentration of 100g/L of O is blended in progress desilication reaction 60min, the liquid-solid ratio of desilication reaction at 90 DEG C
It is 2:1, it is then separated by solid-liquid separation, obtains bauxite concentrate and desiliconization liquid；Wherein, Al in concentrate2O3Mass fraction be 75.64%,
A/S is 8.94, and desiliconization rate is 65.8%；
(3) desiliconization liquid described in step (2) is mixed after carrying out desiliconization processing with lime, is separated by solid-liquid separation, obtains calcium silicates
Product and lye, return to step (2) recycles after gained lye adjusts concentration.
Embodiment 3：
The present embodiment uses middle-low bauxite of the present invention by raw material of Henan somewhere middle-low bauxite
Impurity-removing method clean, the composition of the bauxite (mass percent, wt%, similarly hereinafter) is as shown in table 3.
Table 3
Specific dedoping step includes the following steps：
(1) bauxite is ground, until 89% sieves with 100 mesh sieve, fluidized roaster is sent into after preheated at 1050 DEG C
Under carry out roasting 30min, be passed through enough air in roasting process, the bauxite after being roasted, the wherein mass fraction of S is
0.01wt%, desulfurization degree 96%；The mass fraction of C is 0.1wt%, carbon-drop rate 75%；The sulfur-bearing generated in roasting process
Flue gas, which is passed through in milk of lime, to react, and is then separated by solid-liquid separation, obtains calcium sulfate product；
(2) the mining cyclone separator of alumina after the roasting obtained through step (1) is cooled down, and is cooled to drop temperature,
Then with Na2The lye of a concentration of 90g/L of O is blended in progress desilication reaction 40min, the liquid-solid ratio of desilication reaction at 105 DEG C
It is 5:1, it is then separated by solid-liquid separation, obtains bauxite concentrate and desiliconization liquid；Wherein, Al in concentrate2O3Mass fraction be 76.79%,
A/S is 16.10, and desiliconization rate is 71.7%；
(3) desiliconization liquid described in step (2) is mixed after carrying out desiliconization processing with lime, is separated by solid-liquid separation, obtains calcium silicates
Product and lye, return to step (2) recycles after gained lye adjusts concentration.
Embodiment 4：
The present embodiment uses middle-low grade alumina of the present invention by raw material of Guizhou somewhere high-sulfur low-grade bauxite
The impurity-removing method of mine cleans, and the composition of the bauxite (mass percent, wt%, similarly hereinafter) as shown in table 4.
Table 4
Specific dedoping step includes the following steps：
(1) bauxite is ground, until 80% sieves with 100 mesh sieve, fluidized roaster is sent into after preheated at 980 DEG C
Roasting 60min is carried out, enough air is passed through in roasting process, the bauxite after being roasted, the wherein mass fraction of S is
0.01wt%, desulfurization degree 99%；The mass fraction of C is 0.1wt%, carbon-drop rate 74%；The sulfur-bearing generated in roasting process
Flue gas, which is passed through in milk of lime, to react, and is then separated by solid-liquid separation, obtains calcium sulfate product；
(2) the mining cyclone separator of alumina after the roasting obtained through step (1) is cooled down, and is cooled to drop temperature,
Then with Na2The lye of a concentration of 105g/L of O is blended in progress desilication reaction 120min, the liquid-solid ratio of desilication reaction at 95 DEG C
It is 10:1, it is then separated by solid-liquid separation, obtains bauxite concentrate and desiliconization liquid；Wherein, Al in concentrate2O3Mass fraction be
52.48%, A/S 5.56, desiliconization rate are 75.4%；
(3) desiliconization liquid described in step (2) is mixed after carrying out desiliconization processing with lime, is separated by solid-liquid separation, obtains calcium silicates
Product and lye, return to step (2) recycles after gained lye adjusts concentration.
Embodiment 5：
The present embodiment uses middle-low bauxite of the present invention by raw material of Henan somewhere middle-low bauxite
Impurity-removing method clean, the composition of the bauxite is in the same manner as in Example 1.
Specific dedoping step in addition in step (1) calcination temperature be 1100 DEG C, roasting time 10min；In step (2)
Na in lye2A concentration of 53g/L of O, desilication reaction temperature are 110 DEG C, and the desilication reaction time is 25min, solid-to-liquid ratio 15:1
Outside, unclassified stores dosage and preparation process are same as Example 1.
The mass fraction of S is 0.01wt%, desulfurization degree 88.88% in bauxite in step (1) after roasting；The matter of C
Amount score is 0.1wt%, decarburization efficiency 66.67%；
Al in concentrate obtained by step (2)2O3Mass fraction be 71.59%, A/S 5.43, desiliconization rate be 60.65%.
Embodiment 6：
The present embodiment uses middle-low bauxite of the present invention by raw material of Henan somewhere middle-low bauxite
Impurity-removing method clean, the composition of the bauxite is in the same manner as in Example 1.
Specific dedoping step is in addition to Na in lye in step (2)2A concentration of 140g/L of O, desilication reaction temperature are 70
DEG C, the desilication reaction time is outside 210min, and unclassified stores dosage and preparation process are same as Example 1.
Al in concentrate obtained by step (2)2O3Mass fraction be 73.60%, A/S 6.25, desiliconization rate be 65,78%.
Comparative example 1：
This comparative example uses middle-low bauxite of the present invention by raw material of Henan somewhere middle-low bauxite
Impurity-removing method clean, the composition of the bauxite is in the same manner as in Example 1.
The dedoping step in addition to the calcination temperature in step (1) be 650 DEG C (800 DEG C of <) other than, unclassified stores dosage with
Preparation process is same as Example 1.
The mass fraction of S is 0.02wt%, desulfurization degree 77% in bauxite in step (1) after roasting；The quality of C point
Number is 0.14wt%, decarburization efficiency 53%；
Al in concentrate obtained by step (2)2O3Mass fraction be 53.69%, A/S 2.67, desiliconization rate be 19.85%.
Comparative example 2：
This comparative example uses middle-low bauxite of the present invention by raw material of Henan somewhere middle-low bauxite
Impurity-removing method clean, the composition of the bauxite is in the same manner as in Example 1.
The dedoping step is other than the calcination temperature in step (1) is 1300 DEG C (1100 DEG C of >), unclassified stores dosage
It is same as Example 1 with preparation process.
The mass fraction of S is 0.01wt%, desulfurization degree 89% in bauxite in step (1) after roasting；The quality of C point
Number is 0.1wt%, and it is 67% to take off efficiency；
Al in concentrate obtained by step (2)2O3Mass fraction be 70.15%, A/S 4.07, desiliconization rate be 47.4%.
Comparative example 3：
This comparative example uses middle-low bauxite of the present invention by raw material of Henan somewhere middle-low bauxite
Impurity-removing method clean, the composition of the bauxite is in the same manner as in Example 1.
The dedoping step is in addition to Na in lye in step (2)2A concentration of 30g/L (< 50g/L) of O outside, unclassified stores
Dosage is same as Example 1 with preparation process.
The mass fraction of S is 0.01wt%, desulfurization degree 89% in bauxite in step (1) after roasting；The quality of C point
Number is 0.1wt%, and it is 67% to take off efficiency；
Al in concentrate obtained by step (2)2O3Mass fraction be 62.37%, A/S 3.16, desiliconization rate be 32.3%.
Comparative example 4：
This comparative example uses middle-low bauxite of the present invention by raw material of Henan somewhere middle-low bauxite
Impurity-removing method clean, the composition of the bauxite is in the same manner as in Example 1.
The dedoping step is in addition to Na in lye in step (2)2A concentration of 160g/L (> 140g/L) of O outside, other objects
Expect that dosage and preparation process are same as Example 1.
The mass fraction of S is 0.01wt%, desulfurization degree 89% in bauxite in step (1) after roasting；The quality of C point
Number is 0.1wt%, carbon-drop rate 67%；
Al in concentrate obtained by step (2)2O3Mass fraction be 72.44%, A/S 5.80, desiliconization rate be 63.1%.
The present invention is can be seen that with comparative example based on the above embodiments using fluidized roaster at 800 DEG C~1100 DEG C
Under be passed through sufficient air, high-temperature roasting removal of impurities is carried out to bauxite, desiliconization and desulfuration efficiency are high, desulfuration efficiency up to 90% with
On；Meanwhile organic carbon in ore is removed, the removal efficiency of organic carbon is up to 75%；Sulfur content is less than 0.1% in concentrate, and carbon contains
Amount is less than 0.1%, and desiliconization rate can be more than 60%, alleviate danger of the impurity such as silicon, sulphur and carbon to alumina producing Bayer process process
Evil.
Applicant states that the present invention illustrates detailed process equipment and the technological process of the present invention by above-described embodiment,
But the invention is not limited in above-mentioned detailed process equipment and technological processes, that is, it is above-mentioned detailed not mean that the present invention has to rely on
Process equipment and technological process could be implemented.Person of ordinary skill in the field it will be clearly understood that any improvement in the present invention,
The addition of equivalence replacement and auxiliary element to each raw material of product of the present invention, the selection etc. of concrete mode all fall within the present invention's
Within protection domain and the open scope.
Claims (9)
1. a kind of impurity-removing method of middle-low bauxite, which is characterized in that the described method comprises the following steps：
(1) bauxite feeding fluidized roaster is roasted, air is continually fed into roasting process, the aluminium after being roasted
Tu Kuang；
(2) bauxite after the roasting obtained through step (1) is mixed with lye carries out desilication reaction, is separated by solid-liquid separation, obtains alumina
Mine concentrate and desiliconization liquid；
(3) it after desiliconization liquid described in step (2) being carried out desiliconization processing, is separated by solid-liquid separation, obtains calcium silicate products and lye, gained
Return to step (2) recycles after lye adjustment concentration.
2. impurity-removing method according to claim 1, which is characterized in that silica contains in step (1) described bauxite
Amount is 10wt%~30wt%, and total sulphur content is 0.7wt%~5wt%, and the content of organic carbon is 0.1wt%~2wt%；
Preferably, step (1) described bauxite is sent into fluidized roaster after pretreatment；
Preferably, the pretreatment is grinding and preheating；
Preferably, described to be ground to：70%~90% of the bauxite by grinding is set to sieve with 100 mesh sieve；
Preferably, the preheating temperature is 300 DEG C~500 DEG C.
3. impurity-removing method according to claim 1 or 2, which is characterized in that fluidized roaster described in step (1) is gas
Any one in state suspension roaster, fluidized bed circulation roaster or Flash Smelting Furnace；
Preferably, the calcination temperature of step (1) described roasting is 800 DEG C~1100 DEG C, preferably 900 DEG C~1050 DEG C；
Preferably, the roasting time of step (1) described roasting is 0.1min~60min, preferably 1min~10min；
Preferably, total sulphur content < 0.1wt%, organic carbon content < 0.1wt% in the bauxite after step (1) described roasting.
4. according to claim 1-3 any one of them impurity-removing methods, which is characterized in that produced in step (1) described roasting process
Raw sulfur-containing smoke gas carries out tail gas absorption processing；
Preferably, the tail gas absorption, which is handled, is：The sulfur-containing smoke gas of generation is passed through in milk of lime and is reacted, solid-liquid point is then carried out
From obtaining calcium sulfate product.
5. according to claim 1-4 any one of them impurity-removing methods, which is characterized in that the aluminium after being roasted described in step (2)
Tu Kuang is mixed with lye after cooling；
Preferably, described to be cooled to：Bauxite after roasting is cooled down through cyclone separator, is cooled to drop temperature；
Preferably, the drop temperature is 80 DEG C~200 DEG C；
Preferably, the high temperature air generated in the cooling procedure is for preheating bauxite；
Preferably, the temperature of the high temperature air is 200 DEG C~400 DEG C.
6. according to claim 1-5 any one of them impurity-removing methods, which is characterized in that Na in step (2) described lye2O's is dense
Degree is 50g/L~140g/L, preferably 80g/L~120g/L；
Preferably, the reaction temperature of desilication reaction described in step (2) is 70 DEG C~110 DEG C, preferably 90 DEG C~100 DEG C；
Preferably, the reaction time of desilication reaction described in step (2) be 20min~210min, preferably 30min~
100min；
Preferably, the liquid-solid ratio of desilication reaction described in step (2) is (2~15):1, preferably 5:1.
7. according to claim 1-6 any one of them impurity-removing methods, which is characterized in that bauxite concentrate described in step (2)
Middle alumina content is 60wt%~80wt%, dioxide-containing silica < 10wt%, total sulphur content < 0.1wt%, organic carbon carbon
Content < 0.1wt%.
8. according to claim 1-7 any one of them impurity-removing methods, which is characterized in that desiliconization described in step (2), which is handled, is：
Desiliconization liquid is mixed with lime；
Preferably, the lime consumption is：The molar ratio of lime and silica in desiliconization liquid>2.
9. according to claim 1-8 any one of them impurity-removing methods, which is characterized in that the described method comprises the following steps：
(1) bauxite it is ground and preheating after, be sent into fluidized roaster carried out at 900 DEG C~1050 DEG C roasting 1min~
10min is continually fed into air in roasting process, the bauxite after being roasted, wherein total sulphur content < 0.1wt%, organic carbon
Content < 0.1wt%；The sulfur-containing smoke gas generated in roasting process, which is passed through in milk of lime, to react, and is then separated by solid-liquid separation, is obtained
Calcium sulfate product；
(2) the mining cyclone separator of alumina after the roasting obtained through step (1) is cooled down, and is cooled to drop temperature, then
With Na2The lye of a concentration of 80g/L~120g/L of O be blended at 90 DEG C~100 DEG C carry out desilication reaction 30min~
The liquid-solid ratio of 100min, desilication reaction are 5:1, it is then separated by solid-liquid separation, obtains bauxite concentrate and desiliconization liquid；
(3) desiliconization liquid described in step (2) is mixed after carrying out desiliconization processing with lime, is separated by solid-liquid separation, obtains calcium silicate products
And lye, return to step (2) recycles after gained lye adjusts concentration.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111484054A (en) * | 2019-01-25 | 2020-08-04 | 遵义能矿投资股份有限公司 | Treatment method of refractory bauxite desulfuration active silicon and active aluminum |
| CN111484048A (en) * | 2019-01-25 | 2020-08-04 | 遵义能矿投资股份有限公司 | Treatment method for low-energy-consumption desulfurization and desilication high-efficiency alumina dissolution of refractory bauxite |
| CN112939041A (en) * | 2021-02-11 | 2021-06-11 | 贵州大学 | Method for strengthening low-grade bauxite desilication by using brown corundum fly ash |
| CN113880122A (en) * | 2021-10-13 | 2022-01-04 | 遵义能矿投资股份有限公司 | Method for preparing fine ore from bauxite |
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| CN106315636A (en) * | 2015-06-26 | 2017-01-11 | 沈阳铝镁设计研究院有限公司 | Method for producing aluminum oxide with low-grade high-sulfur bauxite |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111484054A (en) * | 2019-01-25 | 2020-08-04 | 遵义能矿投资股份有限公司 | Treatment method of refractory bauxite desulfuration active silicon and active aluminum |
| CN111484048A (en) * | 2019-01-25 | 2020-08-04 | 遵义能矿投资股份有限公司 | Treatment method for low-energy-consumption desulfurization and desilication high-efficiency alumina dissolution of refractory bauxite |
| CN112939041A (en) * | 2021-02-11 | 2021-06-11 | 贵州大学 | Method for strengthening low-grade bauxite desilication by using brown corundum fly ash |
| CN113880122A (en) * | 2021-10-13 | 2022-01-04 | 遵义能矿投资股份有限公司 | Method for preparing fine ore from bauxite |
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