CN1017137B - Method for processing bauxite into alumina - Google Patents
Method for processing bauxite into aluminaInfo
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- CN1017137B CN1017137B CN87104732.2A CN87104732A CN1017137B CN 1017137 B CN1017137 B CN 1017137B CN 87104732 A CN87104732 A CN 87104732A CN 1017137 B CN1017137 B CN 1017137B
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- bauxite
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- 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
- C01F7/0613—Pretreatment of the minerals, e.g. grinding
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- Inorganic Chemistry (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
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Abstract
The present invention relates to a method for preparing alumina from bauxite. The method comprises the steps that bauxite is milled under the condition of the existence of calcic additives; the molar ratio of CaO to TiO2 is from 0.7 to 2.0. As a result, ore pulp is obtained and then heated to 200 to 280 DEG C; the calcic additives are added to the heated ore pulp so that the molar ratio of CaO to Fe2O3 is from 0.1 to 0.3; the ore pulp is then diluted by fresh water; a solid phase is separated from an aluminate solution containing sodium aluminate. Under the condition of the existence of a crystal seed, the aluminate solution is cooled to 40 to 50 DEG C so that a suspension is obtained. Aluminum hydroxide is used as the crystal seed for separating formed aluminum hydroxide from the suspension.
Description
The present invention relates to the production technique of aluminum oxide, particularly relate to and produce method of alumina with bauxite.
Bauxite products obtained therefrom after treatment is aluminum oxide, and this product is widely used in the national economy, can produce metallic aluminium from aluminum oxide, electric furnace aluminum oxide, the necessary multiple other products of abrasive material and industrial production all departments.Producing with bauxite in the technology of aluminum oxide, is that aluminum oxide reclaims fully and has epochmaking meaning with effective constituent in the raw material, the economy that the recovery rate of aluminum oxide can the final decision whole production.
Extracting aluminum oxide from bauxite has had a lot of methods, and owing to the complicacy of mineral constituent in the raw material and the existence of impurity, the recovery rate of aluminum oxide alters a great deal.
Handling bauxite at present in the factory generally is to adopt bayer's process.In order to strengthen the technology of extracting aluminum oxide from bauxite, can add lime (milk of lime) and other calcareous compound.When bauxite in backspace solution when levigate, lime is added wherein.The optimal addn of lime is the 4%(Л of bauxite weight when levigate. И. draw " alumina producing " according to the Neil work, nineteen sixty, the metallurgical press in Moscow, the 201st page).
Most of factory adopted extracts aluminum oxide by Bayer process from bauxite main technique flow process comprises following technology.
With block bauxite and 200～350 grams per liter Na that contain the existence of sodium hydroxide form
2The alkaline solution that returns of O joins in the pulverizer, so that broken, these alkali lye are from evaporation section, and temperature is 105～120 ℃.Add milk of lime by a certain percentage according to calculating in ball mill, wherein the amount of calcium oxide is 3～4% of the dried bauxite weight that adds.The ore pulp that obtains after levigate (raw material ore pulp) temperature is 90～100 ℃, keeps 2～10 hours to carry out desiliconization process.
The ore pulp that obtains is sent into heat exchanger, and it is heated to 100～200 ℃ temperature (150 ℃ of average out to) on heat exchange surface.Then the ore pulp that heated is sent into the autoclave group.In several leading autoclave, pass through heat exchange surface, or ore pulp is heated to 200～280 ℃, and in remaining autoclave, under top temperature, leave standstill with special high temperature heat transfer device with strong steam.The interior pressure of autoclave this moment reaches 25～40 normal atmosphere or higher, and ore pulp total residence time in the autoclave group is 3 hours.Aluminum oxide leaches from bauxite and generates sodium aluminate during this period, and enters in the liquid phase of the sodium hydroxide that contains some surpluses.Pressure is boiled the result of process, obtains the suspension of being made up of aluminate alkaline solution and the solid residue (red mud) that is insoluble to alkaline solution (pressure is boiled liquid).
After the leaching, aluminate solution contains Na
2O180～300 grams per liters and Al
2O
3190～300 grams per liters.Then pressure is boiled liquid and send in the flash-pot of multistage (separator), make it be as cold as 105～110 ℃ temperature.In the end pressure is also corresponding in several sections flash-pots is reduced near normal atmosphere.
Boil liquid with process water (the first segment process water behind the washing red mud) the cooled pressure of dilution.Boil ore pulp by means of the pressure of diluting then and in collection surface, precipitate and sodium aluminate solution is separated with solid residue (red mud), aluminate solution (collection surface overflow) is sent to controlled filter isolating the particle of being taken out of by overflow, and is for further processing.
The dense red mud that has a certain amount of sodium aluminate solution is carried out the multistage counter current washing in the collection surface system.In last washing device, send into hot water.The dense red mud that obtains in the last washing device is sent to the slag field, and overflow then is defeated by last washing device and is used for dense red mud pulp.Liquid dilution usefulness is boiled in the overflow that first washing device comes out then voltage supply.(gathered carbonate in the solution, oxalate) in case of necessity, light washing water (for example the 2nd of laterite washing the and the overflow of 3rd level collection surface) have been sent to the causticization device.So that make sodium carbonate causticization, and remove part organic impurity contained in the overflow with the lime treatment overflow.Produce solid sediment in the causticization process, be referred to as the causticization body refuse, contain the aluminum oxide of a great deal of in the causticization body refuse, also be sent to the slag field.Washing water after the purification return for the red mud countercurrent washing and use.
The sodium hydroxide (crystal seed) that makes the sodium aluminate solution after the filtration and be suspended in wherein keeps Long contact time, reduces temperature simultaneously, and this process is carried out in air or churned mechanically device.Begin to produce decomposition (hydrolysis) reaction of sodium aluminate under 55～75 ℃ temperature, and finish under 40～50 ℃ of temperature, the reaction process time length is 55～70 hours.The result obtains suspension, it is concentrated, from aluminium hydroxide, isolate mother liquor, aluminium hydroxide is sent to washing, mother liquid evaporation makes it reach the necessary concentration of rework solution, for the leaching of bauxite, the mother liquor after concentrating returns the fs of technical process, with the part of the rework solution that leaches as bauxite.
Oxygen aluminium oxide calcining (calcining) after cleaning removing moisture, and is obtained anhydrous alumina, and the incinerating temperature is 1200 ℃.
Processing contains TiO
2And iron (pyrrhosiderite, the currently known methods of bauxite FeOOH) also will use lime (SU, A, 3,737,514).This method is to leach bauxite earlier with alkaline solution in the mixture of calcium containing compound, and this moment, the amount of CaO should keep following ratio: CaO: Ti
3O
2=0.5～1.0(preferably 0.8～1.0).Extraction temperature is 280～350 ℃ (280～320 ℃), and extraction time should be able to be enough to make all pyrrhosiderites to be converted into rhombohedral iron ore and to generate calcium titanate.Should make ore pulp carry out the leaching of subordinate phase after the leaching of fs, temperature is 200～350 ℃ (200～255 ℃), and its time should be enough to reclaim all soluble alumina in the ore: the I stage is 30 minutes, and the II stage is 45 minutes; The 3rd, 737, No. 514 the described method of patent is very complicated, because it needs two sections leaching flow process, and temperature profile also very strict (leach and under 280～320 ℃, carry out).This just makes the processing unit manufacturing become complicated and expensive.In order under 280～320 ℃ temperature, to realize leaching process, just need autoclave and other auxiliary facilitys of research special construction.In addition, obtain high performance heat transmitter and solve the special technique problem with regard to needs.
What proposed is processed into method of alumina to bauxite under the situation of lime and need adds lime in the bauxite levigated stage having, this will produce its insufficient shortcoming of utilization ratio, because in the levigate process before temperature is 90～105 ℃ of preheater internal heating, lime just produces chemical reaction, generate calcium titanate, calcium aluminate, therefore its major part unable to get up reaction in fact before pressure is boiled process.
Some trials had been done, exactly lime directly is added in the reaction zone to improve its working efficiency (US, A, 3,966,874), according to the method for this patent, contain when being no less than 1% pyrrhosiderite (1～25%) and being no less than the bauxite in 1% boehmite ore deposit (1～60%) in leaching, promptly be not less than 200 ℃ of ability to the decomposition temperature that slurry is heated to bauxite lime is added.The raw material bauxite slurry is heated to the temperature that is not less than 200 ℃, again hot ore pulp is sent into reaction that temperature is not less than 225 ℃ (230～250 ℃) with (sending into the resolver) in the autoclave, is wherein added simultaneously and be no less than 1%(1～3%) the calcic material: CaO, Ca(OH)
2Or CaCO
3, ore pulp was stopped in autoclave 45 minutes.Al according to the method
2O
3Recovery rate be 87%.When lime being joined in the ore pulp in the levigate stage of bauxite, promptly before heating, add, leach its Al according to present known and general general technology
2O
3Recovery rate be 86%.
Though this method can improve the recovery rate of aluminum oxide slightly, with respect to reclaim their this point fully from bauxite, its value is still not high, because the utilization of lime is incomplete under the condition of this method.At first this is because calcium titanate and moisture garnet formation have consumed a part of lime, and remaining lime is owing to generate the protective membrane of above-claimed cpd on its particle, and makes activity be subjected to remarkable loss.
Therefore, in the method that formerly has, there is not a kind of method can not utilize complicated technology and equipment just can from bauxite, leach aluminum oxide with sufficiently high recovery rate.
Main purpose of the present invention is to improve the processing condition produce aluminum oxide from bauxite, makes its bauxite that can handle the different minerals component with simple technology, and therefrom reclaims aluminum oxide with degree the most completely.
In order to realize this purpose, in this method that is proposed by bauxite into alumina, comprise that levigate bauxite is to obtain ore pulp, add calcareous additive, ore pulp is heated to 200～280 ℃ temperature, dilute ore pulp with process water, from aluminate solution, isolate solid phase and then decompose the sodium aluminate that is contained in the aluminate solution, its way is under the condition that crystal seed exists solution to be cooled to 40～50 ℃, utilize aluminium hydroxide to make crystal seed and obtain suspension, from wherein isolating formed aluminium hydroxide.According to this patent, the calcic additive added in the levigate stage of bauxite, and add-on should be CaO by mole ratio: TiO
2=0.7～2.0, add-on should be CaO by mole ratio in ore pulp heating back: Fe
2O
3=0.1～0.3.
The method that is proposed can be used in the bauxite and the bauxite that different mineral constituent (gibbsite, boehmite, diasporite) arranged in various orefields.Adopt this method of being recommended, the activity that can improve the calcic additive owing to it is strengthened leaching process, and the ferric oxide that can make the hydrate form is pyrrhosiderite for example, contain alumogoethite and be converted into anhydrous hematite, and can guarantee the non-reversibility of this conversion, thereby can strengthen the dense and washing process of red mud.
At levigate and pre-heating stage lime is added in the raw material of ore, the compound of titanium in the reaction zone is interacted with lime and generation CaOTiO
2
Known when extracting aluminum oxide from bauxite, there is layer protecting film on the surface that the reason that its yield is not high is salic mineral, and this tunic can hinder in the mineral that alkali enters aluminium.The sodium titanate that generates at mineral surface is very thin layer protecting film, can generate uhligite when adding calcium oxide, so it can promote that alkali enters among the aluminum oxide.Under this reaction mechanism, begin to generate calcium aluminate and sodium titanate precipitates in a large number.Calcium aluminate decomposes and isolates free lime behind the elevated temperature, and the latter and titanium dioxide and sodium titanate reaction generate crystalloid calcium titanate precipitation, throw out be closely knit and solution in the Al that receives
2O
3Increase.So; Lime can be eliminated TiO as chemical reagent on the one hand
2Harmful effect, can promote generate the such intermediate compound of calcium aluminate hydrate as catalyzer again on the other hand.(BAMN analects No.39, nineteen fifty-seven, the 62nd page, Leningrad, H.K. Te Luxinna " effect of lime in the bauxite leaching process ").
The way that adds lime in two stages, promptly (leaching stage) adds lime after levigate stage of bauxite and ore pulp heating, can utilize additives containing calcium most effectively.
When being heated to temperature 90-200 ℃ in advance in the levigate stage of bauxite with it, the calcic additive calcium oxide of adding and titanium compound and sodium aluminate react, and generate calcium titanium compound and calcium aluminate hydrate.Should be taken into account in the amount of calcium containing compound that this stage adds and to make TiO
2Combination without repetition becomes CaOTiO
2Also to estimate the chemically active partial loss of lime, and owing to generate six water calcium aluminate 3CaOAl
2O
36H
2O and part garnet hydrate and the consumption that causes.Test shows that the amount that adds lime in this stage should be able to guarantee following mole ratio CaO: TiO
2=0.7～2.0.
When forming uhligite, can come out from the protective membrane internal disintegration in the surface of salic material and other materials, and make sodium hydroxide and easier the entering wherein of these reagent of lime.Most silicon-dioxide will combine with the garnet hydrate in fs.
The result who reacts in the above-mentioned fs chemistry makes the process of finishing titanyl compound, silicon-dioxide chemical reaction in the reaction zone, and has increased the exposed surface of raw mineral materials.
Ore pulp heating back (leaching stage) restock under 200～280 ℃ temperature adds the calcium containing compound of some amount, can impel aluminum oxide from stable especially mineral such as alumogoethite, separate in aluminium garnet and the diasporite and dissolving more fully, and make the ferric oxide (pyrrhosiderite) of hydrate form change dry oxidation iron (rhombohedral iron ore) into, because in fact these calcareous additives only play catalyzer in the alumina dissolution process, and do not consume in attached reaction.
Rationally utilize waste material for the reactivation process of strengthening bauxite reaches, as calcareous additive, can adopt the compound that contains iron, calcium, Si oxide, its mole ratio is: Fe
2O
3: CaO=0.05～0.11 and SiO
2: CaO=0.02～0.05, can use in order to obtain this ratio that to contain ferric oxide be 2.5～25.0(weight) %, calcium oxide be 55～85.0(weight) raw material of %, and silicon oxide-containing is 1.0～35.0(weight) raw material of %, is calcining under 950～1100 ℃ with it in temperature, and the calcining back is containing the Na that exists with the sodium hydroxide form
2The solution of making of O15～70 grams per liters and aluminum oxide 5～20 grams per liters is added in the said products.
Add above-mentioned calcic additive in levigate stage of bauxite and ore pulp heating back, to improve the recovery rate of from the diasporite that is difficult to expose or the bauxite that contains alumogoethite, extracting aluminum oxide, when the essence that recovery rate improves is the above-mentioned oxide compound of roasting, make to generate following compound: the wustite 2CaOFe of two calcium
2O
3, the silicate 2CaOSiO of calcium oxide CaO and two calcium
2These oxide compounds are added in the Manufactured solution that contains alkali and aluminum oxide, and all above-mentioned three kinds of compounds just can react rapidly with water and the bauxite that is dissolved in wherein, generate the silicate aquation thing of ferro-aluminum calcium.
Suggestion utilizes red mud as the raw material that contains ferric oxide.As mentioned above, red mud is the waste material of gained when handling bauxite by bayer's process, the component (weight %) that its tool is following:
Fe
2O
342～61
Al
2O
38～19
CaO 6～12
SiO
23～12
Na
2O 1.5～7
Loss of calcination 8～15
The sintering of the oxide product of calcic and silicon can impel Al
2O
3And Na
2O is converted into soluble compound, when using these additives, boils Al in the process in pressure
2O
3And Na
2O can obtain extra leaching.
For the raw material that contains calcium oxide, suggestion utilizes Wingdale, the body refuse of process water causticization, oxalate body refuse.Causticization body refuse and oxalate body refuse are the yellow soda ash (Na that eliminates in alumina producing in the alkaline solution
2CO
3) and organic impurity generate.Alumina loss reaches 6(weight during purification) %, utilize these body refuses to make additive and can reclaim aluminum oxide during the course and reduce its loss.This has just reduced the direct loss when producing aluminum oxide by bauxite.
As the raw material of silicon oxide-containing, underproof high-silica diaspore ore is used in suggestion, and this bauxite can not be handled with Bayer process.
Compare with currently known methods, what proposed can reclaim aluminum oxide at leaching process the most completely from bauxite extraction method of alumina, and recovery rate reaches 96%.
In addition, the technology of the method that is proposed and device fabrication are all very simple, and are applicable to that processing contains the bauxite of various mineral constituents.
According to the method that is proposed, the leaching of bauxite is in carrying out in a stage under 280 ℃ the temperature, and it need not use the very high heat transmitter of special equipment and parameter request.
The reinforcement of leaching process is achieved in that to be that lime or other calcic additives join among the technological process in two stages: directly add reaction zone during in the broken stage of bauxite with in leaching.Present method depends on raw materials used composition in the concrete add-on in each stage, so just might effectively utilize the calcic additive in the process of being added to, improve its chemically reactive, thereby significantly increase from bauxite the recovery rate of extracting aluminum oxide, and the ferric oxide that pyrrhosiderite is formed that creates conditions irreversibly changes into rhombohedral iron ore, thereby significantly improves laterite washing and spissated technological process.
The method of the processing bauxite that is proposed need not during the course to add deleterious useless (
) salt, this point is special little in the existing certain methods.Therefore boil in leaching and the evaporative process in pressure and can not produce a series of technical difficulty.In addition, as mentioned above, when the calcareous additive of preparation, can use by the causticization body refuse mixture that oxalate body refuse and red mud are formed.Waste material when all these products all are alumina producing, as discard also and will lose wherein contained aluminum oxide.Utilize these waste materials to prepare the recyclable most aluminum oxide of additive, and additionally increased the output of useful products.
Therefore, the method that proposes special little is the utilization ratio height that technological process and device fabrication are simple, be added to the additive among the technological process, and, because it can be applicable to the bauxite of any kind, so economy and versatility are good.
Extracting aluminum oxide with this method from bauxite is simple in technological operation, can be undertaken by following mode.
Bauxite, rework solution, calcic additive are added to in the ball mill of levigate usefulness.The add-on of calcic additive depends on the composition of bauxite, and should guarantee mole ratio CaO: TiO
2=0.7～2.0.To the temperature that is obtained is 90～100 ℃ raw material flowsheet of slurry agitation 2～10 hours, to carry out desiliconization process.The temperature of heating raw ore pulp to 100～200 ℃ and send into the autoclave group then, ore pulp therein heat to 200～280 ℃.After reaching this temperature, add the calcic additive in autoclave, the mole ratio in the aluminiferous ore deposit mixture that its amount should be enough to guarantee to make is CaO: Fe
2O
3=0.1～0.3.Under 200～280 ℃ temperature ore pulp is left standstill, the time is no less than 30～60 minutes.The pressure that ejects from autoclave is boiled ore pulp and is sent to separator, is cooled to 105～110 ℃, and dilutes with first section washing water that laterite washing produced.
Pressure after the dilution is boiled ore pulp send into collection surface, aluminate solution is separated with solid phase (red mud) by the precipitation in groove.Red mud is sent to the multistage counter current washup, and first section washing water are used for the dilution pressure and boil ore pulp, use the washing water of second, third section of lime treatment in case of necessity, to remove vitriol and organic substance.The solid sediment (causticization body refuse) that obtains is separated from solution, and the solution after the purification is used further to wash red mud, and the causticization body refuse is then sent to for preparation calcic additive and used.
Transport the red mud after the washing to the slag field.
The aluminium hydroxide of using as crystal seed that obtains before an aluminate solution and the part mixed stir and cooling gradually, need lasting 55～70 hours, final temperature is 40～50 ℃.Suspension clarification with the aluminium hydroxide that obtains and mother liquor makes mother liquor separate with aluminium hydroxide.
With mother liquid evaporation, use when supplying bauxite levigate.
Aluminium hydroxide after the washing is calcining under 1200 ℃ of temperature, and just can obtain useful product is aluminum oxide.
Method as described below prepares the calcic additive, iron wherein, and the mole ratio of the oxide compound of calcium and silicon is Fe
2O
3: CaO=0.05～0.11 and SiO
2: CaO=0.02～0.05.
Raw material is red mud, underproof bauxite, Wingdale or causticization body refuse or oxalate body refuse, mixes the back in 950～1100 ℃ of calcinings down of temperature, forms sinter, then with containing the Na that exists with the sodium hydroxide form
2O15～70 grams per liters and Al
2O
3The alkali lye of 5～20 grams per liters is handled, and it is appropriate that the body refuse of use second or third wash water causticization comes replacing lime stone, can reduce Al like this
2O
3Loss, the latter is normally along with the causticization body refuse is abandoned together.
In order to understand the present invention better, enumerate concrete example below.
Example 1
The bauxite of gibbsite and boehmite type, its composition is by weight percentage: ignition loss 26.13, SiO
22.10, Al
2O
348.0, Fe
2O
320.20, TiO
22.8, and other, calculate 100 altogether, the ore deposit is added to wet-milling in the ball mill.In ball mill, send into simultaneously and return alkali lye, wherein total Na
2O is the Na of 255.75 grams per liters, carbonate state
2O is the Na of 21.91 grams per liters, sodium hydroxide state
2O is 233.84 grams per liters, Al
2O
3Be 111.68 grams per liters, carsticity (mole ratio Na
2O: Al
2O
3) be 3.44.Be added to the rework solution that adds 3.61 cubic metres in each ton bauxite in the ball mill, the temperature that the latter enters is 110 ℃.Add the milk of lime that contains 200 grams per liter active calcium oxides in the ball mill, it is CaO: TiO that its add-on should be able to make the mole ratio in the aluminiferous ore deposit mixture of gained
2=0.7.The raw material ore pulp of gained is sent in the steel basin of collecting the raw material ore pulp from the ball mill discharge gate.The raw material slurry temperature that comes out from ball mill is 95 ℃, and stirs 5 hours in the steel basin of collecting the raw material ore pulp under this temperature, is sent to pre-heaters then, is steam heated to 150 ℃ with quiet, and is sent to the autoclave group, is heated to 240 ℃ temperature more therein.After reaching this temperature, by being metered into milk of lime, should make the mole ratio in the gained contain mixtures after the adding is CaO: Fe in autoclave
2O
3=0.3.Ore pulp leaves standstill under 240 ℃ temperature, and the time is no less than 60 minutes.The pressure of coming out from autoclave is boiled ore pulp and is sent to separator, is cooled to 105～110 ℃, and dilutes with first section washing water of washing red mud.
Ore pulp after the dilution is sent to collection surface, by precipitation, the same solid phase of sodium aluminate solution (red mud) is separated in groove.Red mud is sent to the multistage counter current washing, and first section washing water are sent to the dilution pressure and boil ore pulp, and washed red mud is transported to the slag field.
Sneak into the aluminium hydroxide of using as crystal seed of the previous preparation of part in the sodium aluminate solution, stirred 60 hours, and make the temperature of the solution that contains crystal seed be reduced to 45 ℃ gradually.Obtain the suspension of aluminium hydroxide and mother liquor, the suspension post precipitation makes mother liquor separate with aluminium hydroxide.
Return behind the mother liquid evaporation when grinding and use for bauxite.
With the temperature lower calcination of clean aluminium hydroxide, obtain useful alumina product at 1200 ℃.
The recovery rate of aluminum oxide is 94.3% when leaching bauxite.
According to United States Patent (USP) the 3rd, 966, when No. 874 method was handled same bauxite, recovery rate was 91.2%.
Example 2
Bauxite is put into the ball mill wet-milling, add the alkali lye that returns simultaneously, the composition of rework solution and bauxite and their consumption are identical with example 1.The rework solution temperature that adds is 105 ℃.Add the milk of lime that contains active calcium oxide 220 grams per liters in ball mill, it is CaO: TiO that its add-on should be able to make the mole ratio in the mixture of resulting aluminiferous ore deposit
2=0.76.Make the raw material ore pulp, then be sent in the steel basin of collecting the raw material ore pulp, and carry out similar processing by example 1 described technological process, after temperature reaches 240 ℃ in autoclave, by metering milk of lime is added in the autoclave, should make the mole ratio in the mixture of gained aluminiferous ore deposit after the adding is CaO: Fe
2O
3=0.212.Later technological process is identical with example 1, and just the decomposition of aluminate solution will continue 70 hours, and cooled final temperature is 40 ℃.
The recovery rate of aluminum oxide is 94.32% when leaching bauxite.
According to United States Patent (USP) the 3rd, 966, No. 874 described method is handled same bauxite, and the recovery rate of aluminum oxide is 91.2%.
Example 3
Identical with example 1, bauxite, rework solution and milk of lime are added wet-milling in the ball mill.It is CaO: TiO that the different amounts that just adds the milk of lime in the ball mill, add-on should make the interior mole ratio of aluminiferous ore deposit mixture of gained
2=1.02.
The acquisition temperature is 98 ℃ a raw material ore pulp, stirs 8 hours in steel basin, then carries out same technological process like that by example 1, and the different just decomposition of aluminate solution will last 65 hours, and the cooled outlet temperature of aluminate solution is 42 ℃.
The recovery rate of aluminum oxide is 93.97% when leaching bauxite.
According to United States Patent (USP) the 3rd, 966, No. 874 described method is handled same bauxite, and the recovery rate of aluminum oxide is 91.1%.
Example 4
As example 1, bauxite, rework solution and milk of lime are added wet-milling in the ball mill.It is CaO: TiO that the milk of lime amount in the ball mill of adding that different is should be able to make the mole ratio in the aluminiferous ore deposit mixture of acquisition
2=1.53.The carrying out of follow-up process is as example 1.
The recovery rate of aluminum oxide is 94.72% when leaching bauxite.
According to United States Patent (USP) the 3rd, 966, No. 874 described method is handled same bauxite, and the recovery rate of aluminum oxide is 91.4%.
Example 5
As example 1, bauxite, rework solution and milk of lime are added wet-milling in the ball mill.It is Cao: TiO that the milk of lime amount in the ball mill of adding that different is should be able to make the mole ratio in the aluminiferous ore deposit mixture of acquisition
2=2.04.The carrying out of follow-up process is as example 1.
The recovery rate of aluminum oxide is 92.9% when leaching bauxite.
According to United States Patent (USP) the 3rd, 966, No. 874 described method is handled same bauxite, and the recovery rate of aluminum oxide is 90.1%.
Example 6
As example 4, bauxite, rework solution and milk of lime are added wet-milling in the ball mill.The raw material ore pulp that obtains is put into the steel basin stirring of collecting ore pulp as in Example 1, is sent to and preheats gas, then at autoclave internal heating to 240 ℃.Different with example 1 is after reaching this temperature, adds milk of lime by metering in autoclave, and should make the mole ratio in the bauxite mixture of acquisition after the adding is Cao: Fe
2O
3=0.100.The carrying out of follow-up process is as example 1.
The recovery rate of aluminum oxide was 92.62% when bauxite leached.
According to United States Patent (USP) the 3rd, 966, when No. 874 described methods were handled same bauxite, the recovery rate of aluminum oxide was 90.0%.
Example 7
As example 4, bauxite, rework solution and milk of lime are added wet-milling in the ball mill.The raw material ore pulp that obtains is placed in the steel basin of collecting ore pulp as in Example 1 stirs, send into pre-heaters, arrive autoclave then, be heated to 240 ℃ therein.Different with example 1 is reaches in autoclave after this temperature by being metered into milk of lime, and should make the mole ratio in the bauxite mixture of acquisition after the adding is CaO: Fe
2O
3=0.15.The carrying out of follow-up process is as example 1.
The recovery rate of aluminum oxide was 93.95% when bauxite leached.
According to United States Patent (USP) the 3rd, 966, when No. 874 described methods were handled same bauxite, the recovery rate of aluminum oxide was 91.2%.
Example 8
The bauxite of the diasporite type that is adopted, its weight % consists of: loss of calcination 11.5, SiO
22.8, Al
2O
355.0, Fe
2O
325.4, TiO
2Add up to 100 2.49 reach other, this bauxite is added wet-milling in the ball mill.Add in ball mill simultaneously and return alkali lye, it consists of: total Na
2O is the Na of 273,57 grams per liters, carbonate state
2O is the Na of 16.96 grams per liters, sodium hydroxide state
2O is 256.61 grams per liters, Al
2O
3Be 127.24 grams per liters.
Be added to and add 4.17 cubic metres of rework solutions in the bauxite per ton in the ball mill, it is 120 ℃ that solution enters temperature, add the milk of lime contain active calcium oxide 190 grams per liters again in ball mill, wherein going into amount, should be able to make the mole ratio in the bauxite mixture of gained be CaO: TiO
2=1.72.The raw material ore pulp that the result is obtained is sent to the steel basin of collecting the raw material ore pulp from the ball mill discharge gate.The temperature of the raw material ore pulp that comes out from ball mill is 98 ℃, in the steel basin of collecting the raw material ore pulp under this temperature, stirred 4 hours, be sent to pre-heaters then, with the quiet steam heating to 190 ℃ and the autoclave group of packing into, be heated to 235 ℃, after reaching this temperature, by being metered into milk of lime, it is CaO: Fe that add-on should make the mole ratio in the bauxite mixture of acquisition in autoclave
2O
3=0.22.
Ore pulp keeps being no less than 60 minutes under 235 ℃ temperature.Thereafter the carrying out of technological process is identical with example 1.
The recovery rate of aluminum oxide is 94.00% when leaching bauxite.
According to United States Patent (USP) the 3rd, 966, when No. 874 described methods were handled same bauxite, the recovery rate of aluminum oxide was 92.0%.
Example 9
As example 3, bauxite, rework solution and milk of lime are added wet-milling in the ball mill.Subsequent technical steps such as example 1, different is ore pulp be at autoclave internal heating to 200 ℃, and under this temperature in autoclave by being metered into milk of lime, add-on should make that mole ratio is CaO: Fe in the bauxite mixture of acquisition
2O
3=0.3.
The recovery rate of aluminum oxide is 91.9% when leaching bauxite.
According to United States Patent (USP) the 3rd, 966, when No. 874 described methods were handled same bauxite, the recovery rate of aluminum oxide was 89.2%.
Example 10
As example 3, bauxite, rework solution and milk of lime are added wet-milling in the ball mill.Subsequent technical steps such as example 1, different is ore pulp be at autoclave internal heating to 200 ℃, and under this temperature in autoclave by being metered into milk of lime, add-on should make that mole ratio is CaO: Fe in the bauxite mixture of acquisition
2O
3=0.3.
The recovery rate of aluminum oxide is 92.93% when leaching bauxite.
According to United States Patent (USP) the 3rd, 966, when No. 874 described methods were handled same bauxite, the recovery rate of aluminum oxide was 89.7%.
Example 11
As in Example 4 bauxite is processed into aluminum oxide, different being to use contains the product of oxide compound of calcium, iron and silicon as the calcic additive, and the mole ratio in the oxide compound is:
Fe
2O
3: CaO=0.05 and SiO
2: CaO=0.02
In order to prepare calcareous additive, can mix the oxide compound that contains said components mutually with following raw material: underproof bauxite (weight %): Al
2O
338.0, Fe
2O
313.0, SiO
224.9, ignition loss 20, other 5; Wingdale (weight %): CaO54.0, SiO
21.3, Fe
2O
30.4, ignition loss 42.7, (other 1.1, red mud (weight %): Fe
2O
355.0, Al
2O
312.0, CaO9.0, SiO
25.5, ignition loss 13, other 5.
The mixture that obtains was 950 ℃ roasting temperature 2 hours.Then the agglomerate that generates is handled (grams per liter) composed as follows of alkali lye with alkali lye:
The Na of sodium hydroxide state
2O15.5, Al
2O
35.0,65 ℃ of temperature.
The recovery rate of aluminum oxide is 93.5% during leaching.
Example 12
As example 11, bauxite is processed into aluminum oxide, different being to use has the oxide product of calcium, iron and silicon of following mole ratio as the calcic additive:
Fe
2O
3∶CaO＝0.08
SiO
2∶CaO＝0.03
In order to prepare the calcic additive, as in Example 11 underproof bauxite and red mud are mixed, but come replacing lime stone with the causticization body refuse, the causticization body refuse consist of (weight %): Al
2O
311.2, CaO47.8, Na
2O1.0, ignition loss 24.4.
The mixture that obtains was 1050 ℃ roasting temperature 1.5 hours.The agglomerate that obtains is handled the Na that consists of (grams per liter) sodium hydroxide state of alkali lye with the alkali lye of following composition
2O45.0, Al
2O
318.0 70 ℃ of temperature.
The recovery rate of aluminum oxide is 94.0% during leaching.
Example 13
As in Example 11 bauxite is processed into aluminum oxide, different being to use has the oxide product of calcium, iron and silicon of following mole ratio as the calcic additive:
Fe
2O
3∶CaO＝0.11
SiO
2∶CaO＝0.05
The mixture that obtains was 1100 ℃ roasting temperature 1 hour, and the agglomerate of generation is handled with alkali lye, and the composition of alkali lye is (grams per liter): the sodium hydroxide state Na
2O70, Al
2O
320.0,70 ℃ of temperature.
The recovery rate of aluminum oxide is 93.1% during leaching.
Example 14
As example 8, bauxite, rework solution, milk of lime are added wet-milling in the ball mill, the raw material ore pulp that obtains stirred through 10 hours, be sent to pre-heaters then, be heated to 150 ℃, and send into autoclave, be heated to 255 ℃, reach this temperature after, in autoclave, add milk of lime as example 8.Ore pulp kept 45 minutes under 255 ℃ of temperature, and the carrying out of follow-up process is identical with example 1 and 8.
The recovery rate of aluminum oxide is 94.3% when leaching bauxite.
Example 15
As example 8, add in the ball mill bauxite, rework solution, milk of lime levigate, the raw material ore pulp that obtains stirred through 2 hours, in preheater, it is heated to 200 ℃ and send in the autoclave and leach, be heated to 265 ℃ at this place's ore pulp, after reaching this temperature, add milk of lime as example 8 in autoclave, the carrying out of follow-up process is identical with example 1.
The recovery rate of aluminum oxide is 94.7% when leaching bauxite.
Example 16
As example 8, with bauxite, rework solution, that milk of lime is sent into ball mill is levigate, the raw material ore pulp that obtains stirred through 6 hours, was sent to pre-heaters then and was heated to 200 ℃.Then ore pulp is sent into autoclave, is heated to 280 ℃, reach this temperature after, in autoclave, add milk of lime as example 8,13,14.Ore pulp kept 30 minutes under 280 ℃ temperature in autoclave, and the carrying out of follow-up process is as example 8.
The recovery rate of aluminum oxide is 95.0% when leaching bauxite.
Example 17
The leaching process of bauxite such as example 15, different is comes replacing lime stone to be added in the technological process with the calcic additive of special preparation, and the preparation method of additive is as described in the example 12.
The recovery rate of aluminum oxide was 95.94% when bauxite leached.
Example 18
Leach bauxite as in Example 4, different is that bauxite is heated to 280 ℃ in autoclave.
The recovery rate of aluminum oxide was 95.0% when bauxite leached.
Example 19
Leach bauxite as in Example 17, the different calcic additive replacing lime stones with special preparation are added in the technological process, and the preparation method of additive is as described in the example 12.
The recovery rate of aluminum oxide is 95.8% when leaching bauxite.
Claims (5)
1, handle bauxite and produce method of alumina, this method comprises that levigate bauxite is to obtain ore pulp, add the calcic additive, heating ore pulp to 200～280 ℃, dilute ore pulp with process water, from aluminate solution, isolate solid phase, and then separate sodium aluminate in the aluminate solution, way is under the condition that crystal seed exists solution to be cooled to 40～50 ℃ temperature and to obtain suspension, with aluminium hydroxide as crystal seed, from the suspension that obtains, isolate the aluminium hydroxide of generation, it is characterized in that adding the calcic additive and making mole ratio reach CaO: TiO in the levigate stage of bauxite
2=0.7～2.0, and ore pulp heating back adds the calcic additive and makes mole ratio reach CaO: Fe
2O
3=0.1～0.3.
2, according to the method for claim 1, it is characterized in that oxide compound with iron content, calcium and silicon as calcareous additive, the mole ratio of oxide compound is as follows:
Fe
2O
3: CaO=0.05～0.11 and SiO
2: Ca=0.02～0.05, during preparation calcic additive oxycompound iron 2.5～25.0(weight) raw material of %, the raw material and the silicon oxide-containing 1.0～35.0(weight that contain 55.0～85.0 ℃ of (weight) % of calcium oxide) raw material roasting under 950～1100 ℃ of temperature of %, then containing the Na that is the sodium hydroxide state
2The solution of O15～70 grams per liters and aluminum oxide 5～20 grams per liters is added in the sintered products of gained.
3,, it is characterized in that utilizing red mud to be used as containing the raw material of ferric oxide according to the method for claim 2.
4,, it is characterized in that utilizing the body refuse of Wingdale, process water causticization and the raw material that the conduct of oxalate body refuse contains calcium oxide according to the method for claim 2.
5,, it is characterized in that utilizing underproof high-silica diaspore ore to be used as the raw material of silicon oxide-containing according to the method for claim 2.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| IN511/DEL/87A IN168397B (en) | 1983-04-18 | 1987-06-15 | |
| CN87104732.2A CN1017137B (en) | 1983-04-18 | 1987-07-10 | Method for processing bauxite into alumina |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SU3582962 | 1983-04-18 | ||
| CN87104732.2A CN1017137B (en) | 1983-04-18 | 1987-07-10 | Method for processing bauxite into alumina |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1030560A CN1030560A (en) | 1989-01-25 |
| CN1017137B true CN1017137B (en) | 1992-06-24 |
Family
ID=36698716
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN87104732.2A Expired CN1017137B (en) | 1983-04-18 | 1987-07-10 | Method for processing bauxite into alumina |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN1017137B (en) |
| IN (1) | IN168397B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1049875C (en) * | 1996-11-15 | 2000-03-01 | 山西铝厂 | Primary mineral pulp preparation process in Baeyer's alumina producing process |
| CN1095444C (en) * | 1999-07-05 | 2002-12-04 | 中国长城铝业公司中州铝厂 | Production process of alumina by intensified sintering method |
| CN102976377B (en) * | 2012-12-25 | 2014-12-03 | 中南大学 | Dissolution method of monohydrate bauxite ore |
| CN104843799B (en) * | 2015-04-12 | 2017-01-18 | 耿兆翔 | Method for separating and recovering powder alumina and calcium oxide in iron oxide powder |
-
1987
- 1987-06-15 IN IN511/DEL/87A patent/IN168397B/en unknown
- 1987-07-10 CN CN87104732.2A patent/CN1017137B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| IN168397B (en) | 1991-03-23 |
| CN1030560A (en) | 1989-01-25 |
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