CN101343074A - Bauxite dissolving out method for reducing caustic alkali combined in prepared red mud - Google Patents
Bauxite dissolving out method for reducing caustic alkali combined in prepared red mud Download PDFInfo
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- CN101343074A CN101343074A CNA2008100321505A CN200810032150A CN101343074A CN 101343074 A CN101343074 A CN 101343074A CN A2008100321505 A CNA2008100321505 A CN A2008100321505A CN 200810032150 A CN200810032150 A CN 200810032150A CN 101343074 A CN101343074 A CN 101343074A
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Abstract
The invention discloses a bauxite stripping method, and the bauxite can make the caustic alkali combined in produced red mud be lowered. The stripping method is as follows: (A) anterior stage: a boehmite type bauxite, lime and sodium aluminate solution are mixed, and the mixed pulp is heat preserved for long enough time between 90 DEG C and 260 DEG C so that silica in the bauxite is transformed into hydrogarnet as much as possible; (B) posterior stage: then concentrated circulating mother liquid is supplemented to the pulp under such temperature, or the concentrated circulating mother liquid is supplemented to the pulp after the temperature of the pulp is raised between 230 DEG C and 290 DEG C, and finally, the bauxite is stripped for half an hour to three hours under the raised temperature. The molecular ratio aK is more than 4 of the caustic alkali of the sodium aluminate solution mixed with the boehmite type bauxite and the lime in the anterior stage to alumina. The bauxite stripping method has the advantages of simple process, being easily industrialized and low production cost.
Description
Technical field
The present invention relates to a kind of bauxite dissolving out method that bonded caustic alkali reduces in the output red mud that makes, particularly relate to a kind of dissolving-out method that makes the siliceous high bauxite that bonded caustic alkali reduces in the output red mud.
Background technology
Alumina producing Bayer process is directly to utilize the circulating mother liquor that contains a large amount of free caustic alkali to handle bauxite, stripping wherein aluminum oxide obtains sodium aluminate solution, adds aluminium hydroxide crystal seed in the sodium aluminate solution and just can divide through long-time stirring and parse crystalline aluminum hydroxide.Decomposition nut liquid is used further to stripping next batch bauxite after evaporation.
A big chunk production cost of aluminum oxide (about 15～25%) is to be used for by joining Bayer circulation that the price of the sodium hydroxide of sodium hydroxide loss causes in the replenishment cycles.Therefore, reduce the caustic soda loss is one of target of Bayer process alumina producer pursuit always.
The bauxite that is used for producing aluminum oxide divides three types: gibbsite, boehmite and diaspore, both are collectively referred to as a diaspore back.Gibbsite can be by caustic fusion in lower temperature (120 ℃～140 ℃), but, contain the higher stripping temperature (being higher than 200 ℃) of bauxite needs of a diaspore from the bauxite that exists with boehmite or diaspore state in order quickly aluminum oxide to be extracted.
The method of monohydrate bauxite ore stripping is made up of following steps:
Bauxite is levigate formation ore pulp in liquid caustic; Ore pulp is heated to 90～108 ℃, and in this temperature insulation sufficiently long time, the pure aluminium silicate that bauxite is contained partly changes into insoluble sodium aluminium silicate; Make slurry temperature reach 230～290 ℃ by the steam indirect heating then, insulation makes at least 90% extractible aluminum oxide stripping; By the vapor expansion operation recovered steam of succession, the pressure of ore pulp becomes normal pressure at last.
The major part of sodium hydroxide loss is to be caused by so-called " combination " alkali loss, it depends in the process in leaching active silica generates from bauxite the hydrated aluminum silicate and the amount of calcium aluminosilicate hydrate, the amount of the sodium titanate that titanium oxide generates from bauxite when also depending on stripping.Along with the continuous consumption of high-quality bauxite, silicone content improves constantly in the bauxite, thereby causes combined alkali height in the red mud, therefore, reduces combined alkali when handling high-silica diaspore ore with Bayer process and has more important meaning.
In addition, the sodium hydroxide loss is also because so-called " dissolving " alkali loss that laterite washing not exclusively causes.Sodium hydroxide enters on the red mud on red mud dam after being bonded to washing.
The content of the caustic alkali that dissolved oxygen aluminium is worked further reduces by carbonate minerals in the bauxite, and carbonate minerals changes into yellow soda ash with sodium hydroxide in process in leaching.Carbonate minerals mainly contains calcite (CaCO in the bauxite
3), rhombspar (CaMg (CO
3)
2) and spathic iron ore (FeCO
3).Other sources that yellow soda ash produces are organism, carbon dioxide in air and the flocculation agents etc. in the bauxite.These materials change into yellow soda ash when stripping.
Industrially reduce the amount that is enriched in the yellow soda ash in the circulation, and reclaim sodium hydroxide from yellow soda ash with causticizing process.Handle with milk of lime from the yellow soda ash that the Bayer circulation obtains by filtration or centrifugation, obtaining concentration like this is 40～100g/l Na
2The alkali lye of O enters circulation or is directly used in laterite washing after the evaporation.
Industrial another kind of method is to use the lime treatment red mud wash liquor, and dissolved yellow soda ash is changed into sodium hydroxide (U.S. Patent number 3120996).
The combined alkali of the red mud that the bauxite stripping produces is main relevant with two kinds of compounds: contain sodium aluminosilicate of water (Na
2OAl
2O
31.7SiO
2NH
2O) and calcium aluminosilicate hydrate (3CaOAl
2O
3KSiO
2(6-2k) H
2O), k is called the saturation factor of silicon-dioxide, is a parameter, and its size depends on the formation condition of calcium aluminosilicate hydrate.
During the stripping of bauxite high temperature, the SiO in the ore
2And TiO
2With the sodium aluminate solution reaction, generation contains sodium aluminosilicate of water and sodium titanate, causes alkali and alumina loss in process in leaching.After in stripping, adding lime, TiO
2With a part of SiO
2Change calcium titanate and calcium aluminosilicate hydrate into, like this Na that exists with sodium titanate and hydrated sodium silicate
2O reduces, and just makes Na in the red mud
2O/SiO
2Reduce, promptly combined alkali reduces.
Alkaline consumption is with one ton of soda ash (Na that aluminum oxide consumed of every production
2CO
3) quality representation, unit is kg/t-Al
2O
3Combined alkali Na in the red mud
2O and SiO
2The ratio (N/S, be called for short sodium-silicon-rate) of quality weigh.
Under the technical qualification of present stripping monohydrate bauxite ore, when calcium oxide and siliconoxide mass compare CaO/SiO
2(be called for short calcium silicon ratio, C/S)=1.3～1.5 o'clock, aluminum oxide and siliconoxide mass compare Al in the red mud
2O
3/ SiO
2(be called for short alumina silica ratio, A/S)=1.1～2.0, the mass ratio Na of sodium oxide and silicon oxide
2O/SiO
2(be called for short sodium-silicon-rate, N/S)=0.4～0.5.Alkali in the red mud does not reclaim, and then makes alkaligenous a large amount of loss, and also because alumina loss descends the utilization ratio of ore, particularly alkali and alumina loss are bigger when the alumina silica ratio of ore hangs down.At present, generally adopt sintering process to reclaim alkali and aluminum oxide in the Bayer process red mud.But sintering process energy consumption height, complex process improves alumina production cost.The another kind of method that reclaims the red mud combined alkali is the causticization of red mud.Milk of lime joins in the red mud slurry after the washing, heats several hours, carries out liquid-solid separation by filtration.The sig water that obtains is used for laterite washing.But this method effect is limited.If in process in leaching, silicon institute bonded alkali can be reduced, obviously be favourable.
Adding additive in dissolved mineral slurry is the common method that reduces the red mud combined alkali, and lime is the most frequently used additive.Usually, increase along with the lime addition, the N/S of exsolution red mud reduces gradually, and its reason is because the sodium white residue can be converted into calcium aluminosilicate hydrate under the condition that lime exists, and helps reducing the N/S of red mud, but increase along with the lime addition, alumina loss increases, and the amount of red mud increases, the settling property variation of red mud, so the addition of lime must be controlled.
Na in the mother liquor
2CO
3The concentration increase can cause red mud N/S obviously to become big, because Na
2CO
3When existing, calcium aluminosilicate hydrate easily decomposition is transformed into the sodium white residue, causes the increase of red mud combined alkali.Therefore, if can make Na in the mother liquor
2CO
3Concentration reduces, and combined alkali will reduce in the red mud.But will be under present technical qualification with Na
2CO
3It is very big that concentration significantly reduces difficulty.
Add in the process in leaching (Chinese patent application number 200710118667.1) to though can reduce the red mud combined alkali with synthetic hydrated calcium ferrite replacing lime as additive, but want the synthetic a large amount of satisfactory hydrated calcium ferrites of control condition still to have a lot of problems to solve, and synthesis procedure is huge, and cost is very high.
Use alkali lye, calcium ferrite (2CaOFe earlier at process in leaching
2O
3), lime (CaO) carries out pre-treatment to bauxite, carries out liquid-solid separation then, again with the stripping under conventional Bayer process leaching condition of isolating solid; Add lime in the used pre-treatment alkali lye, slough aluminum oxide in the solution, with the pre-treatment alkali liquid regeneration.This processing method (Chinese patent application number 200710099809.4) can make that alumina silica ratio and sodium-silicon-rate reduce in the red mud.But, needing a large amount of synthetic calcium ferrites in the flow process, synthesis technique is loaded down with trivial details, and difficulty is big; Liquid-solid separation also is huge operation, can increase the weight of cost burden.
In sum, can reduce the red mud combined alkali though proposed the whole bag of tricks, technology is all more loaded down with trivial details, and the industrial realization difficulty is very big, therefore, needs a kind of simple, method of being easy to realize industrialized reduction bauxite exsolution red mud combined alkali.
Summary of the invention
Technical problem to be solved by this invention provide a kind of technology simple, be easy to realize industrialization, production cost low make the bauxite dissolving out method that bonded caustic alkali reduces in the output red mud.
By big quantity research has been carried out in the conversion behavior of silicon-containing compound in the bauxite process in leaching, find by changing reaction conditions, can improve the growing amount of calcium aluminosilicate hydrate, perhaps improve the saturation factor of silicon-dioxide in the calcium aluminosilicate hydrate, thereby reduce the growing amount of hydrated aluminum silicate, reduce the combined alkali of red mud.
In the sodium aluminate solution or soda ash liquid of high causticity ratio value, the silicon-dioxide in the bauxite is more changes into calcium aluminosilicate hydrate, thereby has reduced the amount that hydrated aluminum silicate forms.The present invention is mainly based on above discovery.
Method of the present invention is to realize by following technical scheme.
Whole bauxite Bayer process process in leaching is divided into two sections of front and back, and at leading portion, bauxite is worth solution with the high causticity ratio and reacts in the presence of lime.After the leading portion reaction finishes, at the leading portion slurry temperature or after with the rising of leading portion slurry temperature, cover through spissated circulating mother liquor, 230～290 ℃ of following strippings, this process is called back segment again.
The a of leading portion solution
K(molecular ratio of sodium aluminate solution caustic alkali and aluminum oxide) greater than 4, N
K(caustic sodium concentration) is 30g/L～220g/L, and the bauxite add-on is by a after the stripping
KBe 1.4～1.8, temperature of reaction is 90 ℃～260 ℃, and the time is 1h～48h.
Leading portion is under the situation of adding lime, and the reaction product of bauxite in the solution of high causticity ratio, low alkaline concentration mainly is calcium aluminosilicate hydrate, and the amount of sodium white residue seldom.The calcium aluminosilicate hydrate that forms has certain stability after back segment covers high-alkalinity solution, have only few portion to be converted into the sodium white residue, thereby the N/S of exsolution red mud is reduced, and promptly the red mud combined alkali reduces.
Adopt technology provided by the invention, a of leading portion solution
KHigh more, the N/S of exsolution red mud is low more.When conventional stripping, a of the circulating mother liquor of employing
KBe 3.0～3.8, for the N/S that makes exsolution red mud reduces, in the dissolving-out method that the present invention proposes, a of leading portion solution
KMust be greater than 3.8.
Leading portion reaction back replenishes spissated circulating mother liquor in this leading portion temperature of reaction to ore pulp, or will replenish spissated circulating mother liquor to ore pulp behind the ore pulp elevated temperature.Wherein, a kind of mode that concentrates Bayer-liquid of replenishing in back more helps making the red mud combined alkali to reduce.
Adopt technology provided by the invention, the leading portion reaction can be carried out under normal pressure, carries out as at solution temperature being 90 ℃～108 ℃, and the normal pressure favourable part of reaction down is that the equipment that needs is simple.But, need keep the sufficiently long reaction times, as 8～48h for silicon-dioxide stripping from ore is as much as possible come.The leading portion reaction also can be carried out in middle temperature (as 160 ℃) or high temperature (as 260 ℃), and its advantage is that silicon-dioxide comes the needed time shorter from the ore stripping, and shortcoming is having relatively high expectations to conversion unit.
Adopt technology provided by the invention, concentration of sodium carbonate is low more in the leading portion solution, helps reducing the N/S of red mud more.
Under the technical qualification of present conventional stripping diaspore type bauxite, be 250～260 ℃ as the stripping temperature, dissolution time is 0.5～3h, when calcium oxide and siliconoxide mass compare CaO/SiO
2=1.3～1.5 o'clock, aluminum oxide and siliconoxide mass compared Al in the red mud
2O
3/ SiO
2=1.1～2.0, the mass ratio Na of sodium oxide and silicon oxide
2O/SiO
2=0.4～0.5.
After adopting the technology of the present invention's proposition, the mass ratio Na of sodium oxide and silicon oxide in the red mud
2O/SiO
2Reduce, low energy reaches 0.23.
The present invention is lower than 10 bauxite for the mass ratio of aluminum oxide and silicon-dioxide, i.e. the high ore of silica content, and it reduces the more remarkable effect of red mud combined alkali.
The present invention is inapplicable to the bauxite based on gibbsite.Bauxite and boehmite type bauxite to diaspore type are suitable for.When containing a small amount of gibbsite in back two types bauxite, the present invention is also effective.
Advantage of the present invention
1, the dissolving-out method of the present invention's proposition is obvious to the effect that reduces high-silica diaspore ore exsolution red mud combined alkali, the mass ratio Na of the sodium oxide of red mud and silicon oxide under the conventional leaching condition
2O/SiO
2=0.4～0.5, and adopt technology stripping bauxite proposed by the invention, the low energy of the sodium oxide of red mud and the mass ratio of silicon oxide reaches 0.23;
2, the dissolving-out method of the present invention's proposition can be handled siliceous high bauxite in less expensive ground, has widened bauxite resource and has utilized scope;
3, simple, the easy handling of the dissolving-out method flow process of the present invention's proposition does not need to add the synthetic additive; Can not increase the red mud output.
In sum, the present invention be a kind of technology simple, be easy to realize industrialization, production cost low make the bauxite dissolving out method that bonded caustic alkali reduces in the output red mud.
Embodiment
The following examples can make those skilled in the art more fully understand the present invention, but do not limit the present invention in any way, and content of the present invention is not limited to this fully.
In following all Comparative Examples and embodiment, the ore of use is the bauxite of Chinese Henan area, and its chemical ingredients is as shown in table 1.X-ray diffraction shows that aluminium mainly exists with the diaspore mineral in the ore, and silicon exists with the white mica mineral, and titanium exists with anatase octahedrite, and iron exists with spathic iron ore and two kinds of mineral of pyrite.Levigate mixing after the bauxite drying is crossed 140 mesh standard sieves.
Lime is that analytical pure lime carbonate is at 1100 ℃ of calcining 60min gained.Sodium hydroxide is analytical pure.Circulating mother liquor is certain Bayer process alumina producer circulating mother liquor (chemical ingredients sees Table 2).
Table 1
The high causticity ratio is worth a
KSolution is to make by the following method: get a certain amount of circulating mother liquor and be heated to 85 ℃, add the calculated amount calcium oxide, constant temperature stirred 2 hours, separated the solid-liquid phase through vacuum filtration, and the gained liquid phase is worth sodium aluminate solution for the high causticity ratio, analyzes its chemical ingredients.
Lime is pressed mass ratio CaO/SiO
2=1.3 are fitted in the bauxite.Bauxite and solution are by solution a after the stripping
K=1.5 (Rp=1.1) are made into slip.The bauxite stripping is 150 milliliters steel bomb formula autoclave or is that the autoclave of 2L carries out at capacity at volume.It is temperature required to keep stripping that steel bomb formula autoclave is put into Salt heater.Red mud is dried after with the hot water thorough washing, with its chemical ingredients of x-ray fluorescence spectrometry.
Comparative Examples 1 conventional stripping:
Bauxite 11.5g, lime 1.45g and circulating mother liquor 55mL (being concentrated to 35mL in advance) join in the steel bomb formula autoclave, at 260 ℃ of following stripping 180min.The chemical ingredients of stripping generation liquid phase and solid phase is as shown in table 3.
Table 3
The N/S of red mud is 0.42.
Embodiment 1:
Bauxite 115g, lime 14.5g and 41.25g sodium hydroxide and 150mL water (alkali lye N
KBe 213.1g/L) mix the formation slip, join autoclave, stir, at 100 ℃ of reaction 10h, be warming up to 260 ℃, (composition is N to cover decomposition nut liquid at 260 ℃ with high pressure plunger pump then
T=176g/L, N
k=164g/L, Al
2O
3=108g/L is concentrated into 200mL from 585mL in advance), at 260 ℃ of following stripping 60min.The chemical ingredients of stripping generation liquid phase and solid phase is as shown in table 4.
Table 4
The N/S of red mud is 0.28.
Embodiment 2:
Bauxite 115g, lime 14.5g and high a
KSolution 200mL (N
T=101.1g/L, N
k=96.0g/L, Al
2O
3=5.1g/L, a
K=30.8) mix the formation slip, join autoclave, stir,, be warming up to 260 ℃, cover circulating mother liquor (being concentrated into 150mL from 438mL in advance) at 260 ℃ with high pressure plunger pump then, at 260 ℃ of following stripping 60min at 100 ℃ of reaction 10h.The chemical ingredients of stripping generation liquid phase and solid phase is as shown in table 5.
Table 5
The N/S of red mud is 0.23.
Embodiment 3:
Bauxite 115g, lime 14.5g and high a
KSolution 150mL (N
T=134.2g/L, N
k=128.0g/L, Al
2O
3=25.6g/L, a
K=8.1) mix the formation slip, join autoclave, stir,, be warming up to 260, cover circulating mother liquor (being concentrated into 200mL from 438mL in advance) at 260 ℃ with high pressure plunger pump then, at 260 ℃ of following stripping 60min at 100 ℃ of reaction 10h.The chemical ingredients of stripping generation red mud is as shown in table 6.
Table 6
The N/S of red mud is 0.32.
Embodiment 4:
Bauxite 115g, lime 14.5g and high a
KSolution 150mL (N
T=59.5g/L, N
k=52.5g/L, Al
2O
3=21.06g/L, a
K=4.1) mix the formation slip, join autoclave, stir,, be warming up to 260 ℃, cover circulating mother liquor (being concentrated into 200mL from 438mL in advance) at 260 ℃ with high pressure plunger pump then, at 260 ℃ of following stripping 60min at 100 ℃ of reaction 10h.The chemical ingredients of stripping generation red mud is as shown in table 7.
Table 7
The N/S of red mud is 0.40.
Embodiment 5:
Bauxite 11.5g, lime 1.45g, sodium hydroxide 4.1g and 20mL water (alkali lye N
KBe 158.9g/L) mixing formation slip, join steel bomb type autoclave, put into Salt heater, at 160 ℃ of reaction 2h, be cooled to 80～90 ℃ then, open steel bomb, cover circulating mother liquor 41mL (being concentrated into 15mL in advance), steel bomb type autoclave is put into Salt heater, at 260 ℃ of following stripping 60min.The chemical ingredients of stripping generation liquid phase and solid phase is as shown in table 8.
Table 8
The N/S of red mud is 0.26.
Embodiment 6:
Bauxite 11.5g, lime 1.45g, sodium hydroxide 4.1g and 20mL water (alkali lye N
KBe 158.9g/L) mixing formation slip, join steel bomb type autoclave, put into Salt heater, at 200 ℃ of reaction 2h, be cooled to 80～90 ℃ then, open steel bomb, cover circulating mother liquor 41mL (being concentrated into 15mL in advance), steel bomb type autoclave is put into Salt heater, at 260 ℃ of following stripping 60min.The chemical ingredients of stripping generation liquid phase and solid phase is as shown in table 9.
Table 9
The N/S of red mud is 0.27.
Embodiment 7:
Bauxite 11.5g, lime 1.45g, sodium hydroxide 0.83g and 20mL water (alkali lye N
KBe 32.2g/L) mixing formation slip, join steel bomb type autoclave, put into Salt heater, at 260 ℃ of reaction 2h, be cooled to 80～90 ℃ then, open steel bomb, cover circulating mother liquor 52mL (being concentrated into 15mL in advance), steel bomb type autoclave is put into Salt heater, at 260 ℃ of following stripping 60min.The chemical ingredients of stripping generation liquid phase and solid phase is as shown in table 10.
Table 10
The N/S of red mud is 0.35.
Embodiment 8:
Bauxite 11.5g, lime 1.45g, sodium hydroxide 1.65g and 20mL water (alkali lye N
KBe 63.9g/L) mixing formation slip, join steel bomb type autoclave, put into Salt heater, at 260 ℃ of reaction 2h, be cooled to 80～90 ℃ then, open steel bomb, cover circulating mother liquor 49mL (being concentrated into 15mL in advance), steel bomb type autoclave is put into Salt heater, at 260 ℃ of following stripping 60min.The chemical ingredients of stripping generation liquid phase and solid phase is as shown in table 11.
Table 11
The N/S of red mud is 0.31.
Embodiment 9:
Bauxite 11.5g, lime 1.45g, sodium hydroxide 2.48g and 20mL water (alkali lye N
KBe 96.1g/L) mixing formation slip, join steel bomb type autoclave, put into Salt heater, at 260 ℃ of reaction 2h, be cooled to 80～90 ℃ then, open steel bomb, cover circulating mother liquor 46mL (being concentrated into 15mL in advance), steel bomb type autoclave is put into Salt heater, at 260 ℃ of following stripping 60min.The chemical ingredients of stripping generation liquid phase and solid phase is as shown in table 12.
Table 12
The N/S of red mud is 0.29.
Embodiment 10:
Bauxite 11.5g, lime 1.45g, sodium hydroxide 4.13g and 20mL water (alkali lye N
KBe 160.0g/L) mixing formation slip, join steel bomb type autoclave, put into Salt heater, at 260 ℃ of reaction 2h, be cooled to 80～90 ℃ then, open steel bomb, cover circulating mother liquor 46mL (being concentrated into 15mL in advance), steel bomb type autoclave is put into Salt heater, at 260 ℃ of following stripping 60min.The chemical ingredients of stripping generation liquid phase and solid phase is as shown in table 13.
Table 13
The N/S of red mud is 0.36.
Embodiment 11:
Bauxite 11.5g, lime 1.45g and high a
KSolution 17.5mL (N
T=93.4g/L, N
k=85.3g/L, Al
2O
3=4.6g/L, a
K=30.5) mix the formation slip, join steel bomb type autoclave, put into Salt heater, at 260 ℃ of reaction 2h, be cooled to 80～90 ℃ then, open steel bomb, cover circulating mother liquor 49mL (being concentrated into 17.5mL in advance), steel bomb type autoclave is put into Salt heater, at 260 ℃ of following stripping 60min.The chemical ingredients of stripping generation liquid phase and solid phase is as shown in table 14.
Table 14
The N/S of red mud is 0.30.
The present invention can summarize with other the specific form without prejudice to spirit of the present invention or principal character.Therefore, no matter from which point, above-mentioned embodiment of the present invention all can only be thought can not limit the present invention to explanation of the present invention, claims have been pointed out scope of the present invention, and scope of the present invention is not pointed out in above-mentioned explanation, therefore, in implication suitable and any change in the scope, all should think to be included in the scope of claims with claims of the present invention.
Claims (4)
1, a kind of bauxite dissolving out method that makes bonded caustic alkali reduction in the output red mud, this dissolving-out method comprises: (A), leading portion: at first monohydrate bauxite ore, lime and sodium aluminate solution are mixed, the ore pulp that mixing is obtained is incubated the sufficiently long times at 90 ℃～260 ℃, makes the silicon-dioxide in the bauxite change into calcium aluminosilicate hydrate as far as possible; (B), back segment: replenish spissated circulating mother liquor in this temperature to ore pulp then, or will replenish spissated circulating mother liquor to ore pulp behind the ore pulp elevated temperature, raise the temperature to 230 ℃～290 ℃, stripping bauxite 0.5～3 hour under this temperature at last, it is characterized in that: the caustic alkali/alumina molecule at the monohydrate bauxite ore described in the leading portion, lime blended sodium aluminate solution compares a
KGreater than 4.
2, the bauxite dissolving out method that makes bonded caustic alkali reduction in the output red mud according to claim 1 is characterized in that: the solution N in the described leading portion
KBe 30 grams per liters～220 grams per liters.
3, the bauxite dissolving out method that makes bonded caustic alkali reduction in the output red mud according to claim 1, it is characterized in that: the solution reaction time in the described leading portion is 1～48 hour.
4, the bauxite dissolving out method that makes bonded caustic alkali reduction in the output red mud according to claim 1, it is characterized in that: the temperature prioritised of the solution reaction in the described leading portion is controlled at 90～108 ℃, and the reaction times is 8～48 hours.
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| CN103663517A (en) * | 2013-11-26 | 2014-03-26 | 中国铝业股份有限公司 | Method for reducing proportion of sodium and silicone in red mud dissolved out by ore dressing Bayer process |
| CN103964477A (en) * | 2014-04-30 | 2014-08-06 | 东北大学 | Method for reducing alumina-silica ratio of red mud through multistage carbonization |
| CN107792870A (en) * | 2016-08-30 | 2018-03-13 | 中国科学院过程工程研究所 | A kind of method of comprehensive utilization of bauxite |
| CN110950366A (en) * | 2019-12-18 | 2020-04-03 | 中国铝业股份有限公司 | Method for producing alumina by using high carbonate bauxite |
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| CN102826577A (en) * | 2011-06-13 | 2012-12-19 | 长沙瑞德新材料科技发展有限公司 | Two-stage digestion process of boehmite-gibbsite hybrid bauxite |
| CN102757073A (en) * | 2011-09-16 | 2012-10-31 | 东北大学 | Method for producing aluminum oxide based on calcification-carbonization transformation |
| CN102757073B (en) * | 2011-09-16 | 2014-06-18 | 东北大学 | Method for producing aluminum oxide based on calcification-carbonization transformation |
| CN102976376A (en) * | 2012-12-01 | 2013-03-20 | 中南大学 | Dissolving out method of high-sulfur bauxite |
| CN102976376B (en) * | 2012-12-01 | 2014-12-24 | 中南大学 | Dissolving out method of high-sulfur bauxite |
| CN103663517A (en) * | 2013-11-26 | 2014-03-26 | 中国铝业股份有限公司 | Method for reducing proportion of sodium and silicone in red mud dissolved out by ore dressing Bayer process |
| CN103663517B (en) * | 2013-11-26 | 2016-07-13 | 中国铝业股份有限公司 | A kind of method reducing Liquor of Ore Dressing Bayer process exsolution red mud sodium-silicon-rate |
| CN103964477A (en) * | 2014-04-30 | 2014-08-06 | 东北大学 | Method for reducing alumina-silica ratio of red mud through multistage carbonization |
| CN103964477B (en) * | 2014-04-30 | 2016-04-06 | 东北大学 | A kind of method being reduced red mud alumina silica ratio by multistage carbonation |
| CN107792870A (en) * | 2016-08-30 | 2018-03-13 | 中国科学院过程工程研究所 | A kind of method of comprehensive utilization of bauxite |
| CN110950366A (en) * | 2019-12-18 | 2020-04-03 | 中国铝业股份有限公司 | Method for producing alumina by using high carbonate bauxite |
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