CN1865145B - Mine adding process after leaching in alumina production - Google Patents
Mine adding process after leaching in alumina production Download PDFInfo
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- CN1865145B CN1865145B CN2005102002892A CN200510200289A CN1865145B CN 1865145 B CN1865145 B CN 1865145B CN 2005102002892 A CN2005102002892 A CN 2005102002892A CN 200510200289 A CN200510200289 A CN 200510200289A CN 1865145 B CN1865145 B CN 1865145B
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- diaspore
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Abstract
This invention discloses a post-digestion mineralizing process, which comprises standard preheating and digestion apparatus for diaspore crude ore slurry and preparing apparatus for gibbsite crude oreslurry. Wherein: send the gibbsite crude ore slurry to the casing preheating apparatus to increase the temperature, and then send the slurry to the sixth(or seventh) ore slurry self-evaporator of thedigestion apparatus to be mixed with the original diaspore crude ore slurry. The digestion and the flash evaporation of the gibbsite crude ore slurry are processed at the same time so as to significantly improve the productivity of the digestion workshop. The digestion slurry output from the final stage ore slurry self-evaporator is sent with red mud cleaning solution and evaporation stock solutionto the dilution tank to adjust the RP value, then the diluted slurry is send to the post-digestion tank to remove the impurities like silicon and ferrum in the solution, and finally send the dilutedslurry to the rud mud settling workshop. This invention can be applied in the production workflow which mainly uses diaspore and applies Belfa process to produce aluminum oxide.
Description
Technical field:
The present invention relates to the dissolving-out process of alumina producing.
Background technology:
China's bauxite is based on diaspore, and when adopting bayer process to produce aluminum oxide, its stripping temperature height, pressure height, alkali concn height, dissolution time are long, and leaching condition is generally: 260～280 ℃ of temperature, Na
2O
K210～248g/l, dissolution time 40～60min.And external alumina producer uses bauxite trihydrate mostly, and its stripping operation is very simple, and the stripping temperature is low, pressure is low, alkali concn is low, dissolution time is short, and leaching condition is generally: 105～145 ℃ of temperature, Na
2O
K170～190g/l, dissolution time 5～10min.From both leaching condition as can be seen, the leaching condition of China's diaspore bauxite is harsh, the also more external three water aluminium height of the steam consumption of stripping.
Stripping is the core process in the aluminum oxide production process, full factory aluminum oxide output is just played a part crucial.Because the stripping workshop belongs to the High Temperature High Pressure workshop, stripping needs to be equipped with high-duty boiler again, so stripping workshop and supporting boiler house system thereof invest bigger.
How utilizing China's alumina producer to handle the characteristics of a hydraulic bauxite stripping operation, utilizing existing dissolving device basically, seldom increase under the situation of stripping workshop investment, increase substantially the alumina producer production capacity, is the problem that the present invention need solve.
Summary of the invention:
The objective of the invention is to: a kind of batching process after leaching in alumina production is provided, utilizes the easily molten characteristics of three water aluminium, in stripping operation ore pulp flash-pot, add the part bauxite trihydrate, can increase substantially the production capacity in stripping workshop.
The present invention is achieved in that at first, and a hydraulic alum clay stone raw pulp enters preheating according to the production technique of routine and stripping equipment carries out temperature raising and stripping; Secondly, a cover bauxite trihydrate raw material grinder preface and a sleeve preheating operation is set, bauxite trihydrate and circulating mother liquor while charging feed mill are carried out ore grinding, three water aluminium raw pulies behind the ore grinding enter the temperature raising of sleeve preheating equipment; The 3rd, three water aluminium raw pulies after the temperature raising are added the 6th grade or the 7th grade of ore pulp flash-pot, converge with the dissolved mineral slurry of diaspore, make gibbsite stripping in flash vaporization process, improve the R of dissolution fluid
PValue (R
PBe aluminum oxide and causticity aluminum oxide (Na in the sodium aluminate solution
2O
k) weight ratio); The 4th, dissolved mineral slurry comes out to enter diluent facilities from the ore pulp flash-pot, and enters the stripping pit behind the red mud wash liquor mixed diluting that adds simultaneously; At last, the stripping slurry of discharging from the stripping pit is sent to the sedimentation operation.
For avoiding the R of dissolution fluid
PValue improves the back and in postorder workshop section hydrolysising loss takes place, and draws the part vaporizing raw liquor in dilution trap in the dilution operation, improves the stability of dissolution fluid.Vaporizing raw liquor can substitute with decomposition nut liquid herein.
The batching process after leaching index:
Diaspore and boehmite content in the bauxite trihydrate :≤1.5%.
Three water aluminium grinding finenesss :+80 orders 20～45% ,-80 orders 20～45%;
Gibbsite slurry sleeve preheating temperature: 160 ℃～170 ℃
Gibbsite slurry sleeve preheating progression: five～six grades
Gibbsite slurry sleeve preheating steam: based on the secondary steam that corresponding flasher produces, the fourth stage (or five, six grades) overlaps effective live steam (or steam of fine or not water self-evaporatint n. generation) heating.
The gibbsite slurry contains (is foundation with water spigot overflow product): 250～350g/l admittedly.
Final stage flash-pot dissolution fluid R
PValue: 1.22～1.44.
With vaporizing raw liquor and red mud wash liquor with diluent R
PValue is adjusted into: 1.12～1.16.
Key content of the present invention comprise following some:
(1), increase and build cover bauxite trihydrate raw material grinder preface and a sleeve preheating operation, preparation is to the qualified ore pulp of ore pulp flash-pot feed.
(2), three water aluminium raw pulies are added the 6th grade of (or the 7th grade) ore pulp flash-pot, converge, make gibbsite stripping in flash vaporization process, improve the R of dissolution fluid with the dissolved mineral slurry of diaspore
PValue.
(3), for avoiding the R of dissolution fluid
PValue improves the back and in postorder workshop section hydrolysising loss takes place, and draws the part vaporizing raw liquor in dilution trap, improves the stability of dissolution fluid.
Adopt the large-scale alumina producer of single-sleeve preheating, autoclave indirect heating, insulating and leaching technology at present, all adopt ten grades of ore pulp flash-pot pressure and temperature reducings after the insulation stripping, the 6th grade, the 7th grade flash vaporization point of ore pulp flash-pot is controlled at about 180 ℃, 167 ℃ usually in the production, according to the stripping characteristics of bauxite trihydrate, it is suitable that three water aluminium raw pulies add in this two-stage ore pulp flash-pot.
Adjust dissolution fluid R with vaporizing raw liquor
PValue mainly is to consider that the seston content of AH in the vaporizing raw liquor is low, also can substitute vaporizing raw liquor with decomposition nut liquid herein.
The invention has the beneficial effects as follows: adopt batching process after leaching of the present invention, the aluminum oxide production capacity in stripping workshop can improve more than 18%.The production capacity raising mainly reflects from two indexs, and the firstth, dissolution fluid R
PValue improves, and makes the dissolution fluid alumina concentration improve about 10g/l; The secondth, the dissolution fluid flow increases about 10%; If intrinsic one group of dissolving device production capacity 450kt/a, by adopting batching process after leaching of the present invention, same one group of dissolving device production capacity can be brought up to 530kt/a, has very big economic benefit.
Description of drawings:
Fig. 1 is a process flow diagram of the present invention.
Embodiment:
Embodiments of the invention: at first, according to the output of diaspore raw pulp, what of the three water aluminium raw pulies that determine to need add; Secondly, design and manufacturing bauxite trihydrate raw material mill, sleeve preheating and relevant device thereof; Then, the preparation apparatus of bauxite trihydrate raw pulp and the treatment facility of diaspore raw pulp are coupled together.
During work, bauxite trihydrate and circulating mother liquor adopt one section ball mill ore grinding, use hydroclone classification then, and the classification overflow is sent to the raw ore stock tank as the product of raw material grinder preface, and classification underflow returns closed circuit grinding in the ball mill.Diaspore and boehmite content in the bauxite trihydrate :≤1.5%, three water aluminium grinding finenesss :+80 orders 20～45% ,-80 orders 20～45%; The gibbsite slurry contains (is foundation with water spigot overflow product): 250～350g/l admittedly.Three water aluminium raw pulies from the raw ore stock tank are sent in the cannula primary heater of three water aluminium through slush pump, the secondary steam that sleeve preheating produces based on corresponding flasher with steam, fourth, fifth, six grade of effective live steam of cover; Through five～six grades of preheatings, preheating temperature is 160 ℃～170 ℃, sends in the 6th (or 7th) level ore pulp flash-pot of dissolving device again, converge with original water aluminium stripping slurries, and the stripping on one side of gibbsite slurry, on one side flash distillation.Final stage flash-pot dissolution fluid R
PValue is 1.22～1.24.Stripping slurries from the output of final stage ore pulp flash-pot together advance in the dilution trap with red mud wash liquor and vaporizing raw liquor (or decomposition nut liquid), adjust the R of diluent
PValue send the stripping pit to stop to remove impurity such as silicon in the solution, iron then, will dilute slip with pump after the stripping and be sent to the red-mud settlement car by pipeline and ask.
Claims (2)
1. batching process after leaching in alumina production is characterized in that: at first, a hydraulic alum clay stone raw pulp enters preheating according to the production technique of routine and stripping equipment carries out temperature raising and stripping; Secondly, a cover bauxite trihydrate raw material grinder preface and a sleeve preheating operation is set, bauxite trihydrate and circulating mother liquor while charging feed mill are carried out ore grinding, three water aluminium raw pulies behind the ore grinding enter the temperature raising of sleeve preheating equipment; The 3rd, three water aluminium raw pulies after the temperature raising are added the 6th grade or the 7th grade of ore pulp flash-pot, converge with the dissolved mineral slurry of diaspore, make gibbsite stripping in flash vaporization process, improve the RP value of dissolution fluid; The 4th, dissolved mineral slurry comes out to enter diluent facilities from the ore pulp flash-pot, and enters the stripping pit behind the red mud wash liquor mixed diluting that adds simultaneously; At last, the stripping slurry of discharging from the stripping pit is sent to the sedimentation operation.
2. batching process after leaching according to claim 1 is characterized in that: draw the part vaporizing raw liquor in dilution trap in the dilution operation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2005102002892A CN1865145B (en) | 2005-05-19 | 2005-05-19 | Mine adding process after leaching in alumina production |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2005102002892A CN1865145B (en) | 2005-05-19 | 2005-05-19 | Mine adding process after leaching in alumina production |
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| CN1865145A CN1865145A (en) | 2006-11-22 |
| CN1865145B true CN1865145B (en) | 2010-04-07 |
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| CN2005102002892A Expired - Fee Related CN1865145B (en) | 2005-05-19 | 2005-05-19 | Mine adding process after leaching in alumina production |
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Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100532262C (en) * | 2007-07-12 | 2009-08-26 | 中国铝业股份有限公司 | Method for producing aluminium oxide by middle-low grade alumyte |
| CN102009991A (en) * | 2010-12-30 | 2011-04-13 | 中国铝业股份有限公司 | Method for producing aluminum oxide by Bayer process |
| CN102491386A (en) * | 2011-11-22 | 2012-06-13 | 中国铝业股份有限公司 | Method for improving silica modulus of purified liquid obtained by Bayer process |
| CN112684772B (en) * | 2020-12-31 | 2024-05-03 | 贵阳振兴铝镁科技产业发展有限公司 | Heat balance control system and method for aluminum oxide dissolution |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4614641A (en) * | 1985-06-19 | 1986-09-30 | Aluminum Company Of America | Parallel purification of alumina with physical pretreatment |
| CN1528669A (en) * | 2003-09-26 | 2004-09-15 | 中国铝业股份有限公司 | Flash evaporator water injection method of digesting system for alumina high-pressure pan |
| CN1597524A (en) * | 2004-07-23 | 2005-03-23 | 山东铝业股份有限公司 | Bauxite low temperature continuous dissolving out technology |
-
2005
- 2005-05-19 CN CN2005102002892A patent/CN1865145B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4614641A (en) * | 1985-06-19 | 1986-09-30 | Aluminum Company Of America | Parallel purification of alumina with physical pretreatment |
| CN1528669A (en) * | 2003-09-26 | 2004-09-15 | 中国铝业股份有限公司 | Flash evaporator water injection method of digesting system for alumina high-pressure pan |
| CN1597524A (en) * | 2004-07-23 | 2005-03-23 | 山东铝业股份有限公司 | Bauxite low temperature continuous dissolving out technology |
Non-Patent Citations (2)
| Title |
|---|
| 赵清杰.一水硬铝石溶出新工艺.轻金属 1.2000,(1),17-21. |
| 赵清杰.一水硬铝石溶出新工艺.轻金属 1.2000,(1),17-21. * |
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| CN1865145A (en) | 2006-11-22 |
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Address after: 550081 Guiyang Province, Jinyang New District, Zhu Zhu Road, No. 2 Patentee after: Guiyang Aluminum & Magnesium Design Institute Co., Ltd. Address before: 550004 No. 208, Beijing Road, Guiyang, Guizhou Patentee before: Guiyang Aluminium and Magnesium Design Inst. |
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