CN1034184A - Producing aluminium oxide by bayer is strengthened the method for stripping - Google Patents
Producing aluminium oxide by bayer is strengthened the method for stripping Download PDFInfo
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- CN1034184A CN1034184A CN 88108014 CN88108014A CN1034184A CN 1034184 A CN1034184 A CN 1034184A CN 88108014 CN88108014 CN 88108014 CN 88108014 A CN88108014 A CN 88108014A CN 1034184 A CN1034184 A CN 1034184A
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- China
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- bauxite
- ore pulp
- stripping
- diaspore type
- remaining tank
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Abstract
Adopt pipeline reactor---remaining tank technology stripping bauxite, especially handle the diaspore type bauxite of indissoluble and can obtain good result of extraction, compare with traditional autoclave stripping or pipeline reactor stripping, have obvious advantages such as equipment is simple, easy handling, hear rate saving.
Description
The invention belongs to a kind of method of producing aluminum oxide, specifically, is a kind of novel process about producing aluminium oxide by bayer.
It is to adopt bayer's process to produce that aluminum oxide more than 95% is arranged at present in the world, and the core of bayer's process aluminium oxide extraction process is the stripping of aluminum ore.
Current, the industrial autoclave stripping bauxite that mostly adopts is handled the high aluminium silicon ratio bauxite that gibbsite type, boehmite type or its mixed type one class are soluble in alkali lye, the result of extraction that can obtain really with it.
But, adopt above-mentioned autoclave to handle the bauxite that diaspore type one class is insoluble in alkali lye, situation then differs widely, the stripping temperature of handling this class bauxite is more much higher than the stripping temperature of handling an above-mentioned class bauxite that is soluble in alkali lye, the concentration of required liquid caustic is also much higher, and its result must bring many difficulties of technology, economic dispatch aspect.
The characteristics of this body structure of autoclave device define the further raising that its realizes stripping temperature, because the autoclave volume is huge, held by the restriction of mechanical strength and can't stand higher pressure.In addition, the sealing problem of the mechanical stirring device of autoclave also is difficult to solve when hypertonia.
Improve the problem that the stripping temperature is strengthened stripping for solving, as far back as the '30s in this century, Miu Lieer (Miller) and Xi Lieer (Hiller) propose to make autoclave the design of coiled reactor into, and have delivered patent.1951～1954 years southern Buddhist nun (Lanyi) make gun barrel into reactor, carried out simulation test, the steam direct heating, temperature can reach 270～300 ℃, thereafter, the Soviet Union, Czech, Hungary, the U.S. all carried out research, up to 1966 West Germany associating Chinalco (VAM) just at first be applied the another kind of technology-pipeline reactor stripping of current bauxite stripping that Here it is industrial.
But adopt this pipeline reactor stripping to handle diaspore type bauxite, still can not reach satisfied result of extraction.Though this is because pipeline reactor can be realized the high temperature stripping, can not keep the enough reaction times, this is limited by the characteristics of its structure own.If make ore pulp in pipeline reactor, stop the long time, certainly will will greatly prolong duct length.For example: by ore pulp flow velocity in pipeline reactor is 2 meter per seconds, when keeping 3 minutes residence time, the length of pipeline reactor pipe only needs 360 meters, duct length then needs 3600 meters when keeping 30 minutes residence time, increased facility investment greatly, too much occupied ground has increased the weight of the transfer pressure and the maintenance of pump and has born, and has increased difficulty for again simultaneously the cleaning of pipeline scarring.
The objective of the invention is to seek a kind of novel process, it can keep pipeline reactor institute inherent advantage, can overcome pipeline reactor again and keep insufficient problem of the residence time.Make it all can obtain satisfied result of extraction for any kind bauxite that comprises diaspore type.This technology is compared with pipeline reactor with traditional autoclave, and it is simple to have a processing unit, processing ease, advantages such as low equipment investment.
Detailed description of the present invention
Learn by test, when adopting technology of the present invention and equipment, stripping to the diaspore type bauxite of indissoluble, the conventional bayer's process autoclave stripping temperature of its stripping temperature improves 10～15 ℃, process in leaching just can greatly be strengthened, under the prerequisite that obtains identical digesting efficiency of alumina, dissolution time was reduced to 30 fens by 120 minutes, and required caustic sodium concentration is also by original Na
2O
Severe240 grams per liters drop to Na
2O
Severe140 grams per liters.The reason that can obtain unusual effect like this is the advantage that the present invention has pipeline reactor and autoclave simultaneously.
Pipeline reactor can be realized the high temperature stripping, stripping temperature even can reach more than 300 ℃, simultaneously, pipeline reactor process in leaching ore pulp is plug flow and flows in pipeline, this plug flow has guaranteed that the reaction between bauxite and initiate high causticity ratio's the alkali lye is carried out effectively, thereby process in leaching is strengthened, on the contrary, in autoclave, be Turbulence Flow owing to ore pulp, both made and added free caustic alkali causticity than very high alkali lye, but after entering in the still, with early be introduced into and reacted or partial reaction ore pulp be in together in the large container, thereby can not bring into play the effect of high causticity ratio's alkali lye.
Also learn by test, diaspore type bauxite stripping to indissoluble, the stripping temperature is up to 310 ℃, when 3.4 minutes pipeline internal reaction time, the relative solubility rate of aluminum oxide is also very low, still less than 40%, its explanation only relies on pipeline reactor still can not solve the stripping problem of the diaspore of indissoluble, still must keep certain dissolution time, the front is narrated, realize that by the duct length of unlimited prolongation tubular reactor it is uneconomic prolonging the practice of the residence time, then can reach the purpose that prolongs the reaction times with autoclave.
Main points of the present invention are that the exit end at pipeline reactor connects one group of remaining tank, realize prolonging the purpose of dissolution time by remaining tank, this remaining tank is different from the general high voltage still, it is to be composed in series by one group of diameter tank body long than low height, because its diameter is more much smaller than autoclave, therefore can sustain the high pressure that high temperature brings, because belt stirrer not, therefore need not consider the high pressure seal problem, industrial very easily realization.Moreover because remaining tank is an elongated tank body, ore pulp is the flow state between plug flow and turbulent flow in jar, and ore reacts more effectively with the liquid caustic continuation thereby help not act on completely.
Concrete processing condition of the present invention are: bauxite makes ore grain size-0.076 micron＞50% after crushed, and is levigate-0.076 micron＞70% to diaspore type bauxite, caustic sodium concentration Na
2O
Severe100～200 grams per liters, when handling the diaspore type bauxite of indissoluble, caustic sodium concentration 130～240 grams per liters.Adding solubility promoter lime quantity is 2～10% of bauxite amount, and diaspore optimum range 5～15% lime need activate, and its effective CaO is not less than 50%.
Breeze, alkali lye and lime at first join and give desiliconization slot, give 90～100 ℃ of desiliconization temperature, and the time is more than 5 hours, and giving desiliconization effect is 40～90%.
Hot ore pulp after giving desiliconization injects the high pressure slurry pump supercharging and sends in the pipeline reactor, pipeline reactor give hot arc by from the steam-heated cal(l)andria of ore pulp flash-pot, ore pulp enters high temperature section by giving hot arc, high temperature section can adopt the heating of dissolved salt sleeve pipe, also can adopt the alternate manner heating, high temperature section that is to say that the temperature of stripping section is 100～300 ℃, and the diaspore type bauxite optimum temps of handling indissoluble be should be 240～280 ℃.Ore pulp is not less than 1 meter per second at the flow velocity of stripping section, should not be lower than 1.7 meter per seconds to its flow velocity of diaspore type bauxite of handling indissoluble.Ore pulp should keep stopping 0.5～5 fen in the stripping section, should keep stopping 1～10 fen to diaspore type bauxite.
Ore pulp enters remaining tank by the pipeline reactor outlet, remaining tank can be one, also can a plurality ofly be connected into one group by what vary in size, ore pulp here is incubated, it can be a natural thermal insulation, also can be incubated with the steam or the alternate manner of ore pulp flash-pot, ore pulp keeps 90～280 ℃ of temperature in remaining tank, can not be lower than 230 ℃ for handling diaspore bauxite.The time that ore pulp stops in remaining tank was generally 5～60 fens, can not be lower than 10 minutes for handling the diaspore type bauxite residence time.
After above-mentioned processing, the relative solubility rate of aluminum oxide can reach 90～98% in the bauxite, compares with autoclave, reaction times reduces 3/4ths, caustic sodium concentration is reduced to 140 grams per liters by 240 grams per liters, has greatly alleviated the decomposition nut liquid evaporation load, and hear rate is saved over half.
Embodiment
The employing diaspore type bauxite is a raw material, its chemical composition (%):
Al
2O
3-56.30 CaO-0.43
SiO
2-6.00 Na
2O-0.17
Fe
2O
3-19.05 K
2O-0.22
TiO
2-3.40 iglosss-13.86
Its mineral composition (%):
Diaspore-60.25 rutile-0.48
Gibbsite-2.18 calcite-0.49
Pyrrhosiderite-15.41 illite-4.04
Rhombohedral iron ore-5.48 beryls-trace
Anatase octahedrite-2.69 agalmatolites-trace
Ore is its size composition (%) millimeter after grinding:
+0.154-0.2 0.076～0.050-64.0
0.154～0.098-10.5 -0.050-8.0
0.098～0.076-17.1
Stripping alkali lye (grams per liter):
Na
2O
Entirely-160 Al
2O
3-72.5
Na
2O
Severe-141 molecular ratios-3.20
Lime:
Being crushed to 0.25 millimeter through digestion sieves again through 1000 ℃ of calcinings 1 hour.
Above-mentioned raw materials and alkali lye blended together at first to enter behind the ore pulp gives desiliconization slot, under 95～98 ℃ of temperature, gave desiliconization 8 hours, give desiliconization efficient and reach 54.6%, with slush pump with 2～3 kilograms per centimeter
2Pressure will give ore pulp after the desiliconization and inject high pressure slurry pump and increase to 150 kilograms per centimeter
2Send into pipeline reactor, stripping section temperature is 255 ℃ in the pipe, the flow velocity of ore pulp in pipe is 1.8 meter per seconds, enter remaining tank then, remaining tank is composed in series natural thermal insulation by 4 different jars of volume size, ore pulp is through behind the remaining tank, the stripping temperature is reduced to 248 ℃, and the total time that ore pulp stops in jar is 30 minutes, and the relative solubility rate of aluminum oxide reaches 94%.
The method that connects remaining tank after pipeline reactor both had been suitable for handling various types of bauxite, also was suitable for handling the hydrometallurgical extraction of uranium, tungsten, molybdenum, vanadium, nickel, cobalt, copper etc.
Claims (12)
1, a kind of bayer's process extracts method of alumina and it is characterized in that connecting remaining tank after pipeline reactor from bauxite, so that ore pulp at high temperature keeps the certain reaction time.
2, by the method for claim 1, used aluminium ore need be ground into-0.076 micron＞50%, handles diaspore type bauxite-0.076 micron＞70%.
3, by the method for claim 1, used alkali lye caustic sodium concentration is 100～200 grams per liters, handles diaspore type bauxite caustic sodium concentration 130～240 grams per liters.
4, by the method for claim 1, used lime solubility promoter should be 2～10% of bauxite amount, handles diaspore type bauxite optimum range 5～15%.
5, by the method for claim 1, the stripping temperature of described pipeline reactor ore pulp is 100～300 ℃, and handling the diaspore type bauxite optimum temps is 240～280 ℃.
6, by the method for claim 1, described pipeline reactor can be divided into and gives hot arc and stripping section, gives hot arc and can adopt heating of flash-pot sleeve pipe or alternate manner heating, and the stripping section can adopt heating of fused salt sleeve pipe or alternate manner heating.
7, by the method for claim 1, ore pulp should be greater than 1 meter per second at the flow velocity of pipeline stripping section, should be greater than 1.7 meter per seconds to handling its flow velocity of diaspore type bauxite.
8, by the method for claim 1, ore pulp is in 0.5～5 minute time that pipeline stripping section stops, to 1～10 minute diaspore type bauxite ore pulp residence time.
9, according to claim 1 described remaining tank, ore pulp keeps 90～280 ℃ in remaining tank, should keep temperature to be not less than 230 ℃ to diaspore type bauxite.
10, according to claim 1 described remaining tank, ore pulp is 5～60 minutes residence time in remaining tank, and the diaspore type bauxite residence time was not less than 10 minutes.
11, by the described remaining tank of claim 1, can be one, also can be connected into one group by a plurality of remaining tanks.
12, by the described method of claim 1, both be suitable for handling various types of bauxite, also be suitable for handling the hydrometallurgical extraction of uranium, tungsten, molybdenum, vanadium, nickel, cobalt, copper etc.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 88108014 CN1013191B (en) | 1988-11-24 | 1988-11-24 | Prepn. of alumina by improved bayer's digestion process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 88108014 CN1013191B (en) | 1988-11-24 | 1988-11-24 | Prepn. of alumina by improved bayer's digestion process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1034184A true CN1034184A (en) | 1989-07-26 |
| CN1013191B CN1013191B (en) | 1991-07-17 |
Family
ID=4834886
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 88108014 Expired CN1013191B (en) | 1988-11-24 | 1988-11-24 | Prepn. of alumina by improved bayer's digestion process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1013191B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100398447C (en) * | 2005-01-21 | 2008-07-02 | 中南大学 | Method for extracting alumina from high silicon bauxite |
| CN100418883C (en) * | 2005-09-30 | 2008-09-17 | 东北大学 | Inside circumfluence superposed pipe reactor for leaching |
| CN102009990A (en) * | 2010-12-15 | 2011-04-13 | 中国铝业股份有限公司 | Method for leaching bauxite ore pulp |
| CN101811713B (en) * | 2009-08-21 | 2012-06-13 | 东北大学设计研究院（有限公司） | Pipeline and dwell tank desiliconization method of fly ash |
| CN102560097A (en) * | 2010-12-22 | 2012-07-11 | 贵阳铝镁设计研究院有限公司 | Method and device for improving leaching efficiency of aluminum ores by acid treatment |
| CN107140665A (en) * | 2017-05-27 | 2017-09-08 | 广西大学 | The dissolving-out method of complicated titaniferous aluminium concentrate |
-
1988
- 1988-11-24 CN CN 88108014 patent/CN1013191B/en not_active Expired
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100398447C (en) * | 2005-01-21 | 2008-07-02 | 中南大学 | Method for extracting alumina from high silicon bauxite |
| CN100418883C (en) * | 2005-09-30 | 2008-09-17 | 东北大学 | Inside circumfluence superposed pipe reactor for leaching |
| CN101811713B (en) * | 2009-08-21 | 2012-06-13 | 东北大学设计研究院（有限公司） | Pipeline and dwell tank desiliconization method of fly ash |
| CN102009990A (en) * | 2010-12-15 | 2011-04-13 | 中国铝业股份有限公司 | Method for leaching bauxite ore pulp |
| CN102560097A (en) * | 2010-12-22 | 2012-07-11 | 贵阳铝镁设计研究院有限公司 | Method and device for improving leaching efficiency of aluminum ores by acid treatment |
| CN107140665A (en) * | 2017-05-27 | 2017-09-08 | 广西大学 | The dissolving-out method of complicated titaniferous aluminium concentrate |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1013191B (en) | 1991-07-17 |
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