CN103130256A - Dissolving self-evaporation process - Google Patents
Dissolving self-evaporation process Download PDFInfo
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- CN103130256A CN103130256A CN2011103966689A CN201110396668A CN103130256A CN 103130256 A CN103130256 A CN 103130256A CN 2011103966689 A CN2011103966689 A CN 2011103966689A CN 201110396668 A CN201110396668 A CN 201110396668A CN 103130256 A CN103130256 A CN 103130256A
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Abstract
The invention discloses dissolving self-evaporation process. After alumina sand and alkali liquid are prepared into qualified ore pulp, the ore pulp is fed into a high-pressure dissolving system through a high-pressure pump and dissolved at a high temperature from 260 DEG C to 280 DEG C, and dissolved pulp is obtained. The temperature of the dissolved pulp is reduced to about 130 DEG C to 120 DEG C after the temperature of the dissolved pulp and pressure of the dissolved pulp are reduced stage by stage through multi-stage self-evaporation, and then the dissolved pulp is conveyed into a dilution tank, diluted through one-time washing liquid from a red mud settling and washing work section and conveyed to a red mud separating and washing work section through a pump. During the multi-stage self-evaporation process, the one-time washing liquid of the red mud settling and washing work section is injected in a plurality of stages of back self-evaporators of multi-stage self-evaporators. The dissolving self-evaporation process achieves the aim of reducing concentration of sodium carbonate, meets requirements of normal washing balance, enables dilution concentration to be guaranteed, does not increase energy consumption of an evaporation work section, meets environment-protection requirements due to discharging of red mud, and has multipurpose effects.
Description
Technical field
The present invention relates to the stripping evaporation technology flow process in a kind of aluminum oxide production process.
Background technology
In alumina producing, after bauxite and alkali lye are prepared into qualified raw pulp, send into pressure digestion system with high-pressure pump, the dissolved mineral slurry that obtains after at high temperature (approximately 260 ~ 280 ℃) stripping of raw pulp, through multistage self-evaporatint n. step by step after pressure and temperature reducing temperature be down to approximately 130 ~ 120 ℃, send into again dilution trap, after the next primary wash liquor dilution of red-mud settlement washing room, with the past red mud separating, washing of pumping workshop section.
The self-evaporating process of stripping is a concentration process, the sodium salt that contains in dissolved mineral slurry---sodium carbonate (Na
2O
3), can be along with Enrichment reaches capacity and separates out in self-evaporating process, the crystallize sodium carbonate of separating out can be attached on the tube wall of ore pulp pipe, and blocking pipe gradually, causes the interruption of stripping normal flow.For fear of separating out of crystallize sodium carbonate when the self-evaporatint n., the method that usually adopts is water filling in higher what flash-pot of end of concentration, and the concentration of sodium carbonate is reduced to below saturation concentration, and it is not separated out.This is comparatively effective means of a kind of reduction concentration of sodium carbonate, but the problem of bringing is: a large amount of water has entered in dissolved mineral slurry, makes ore pulp be diluted rear alkali concn and reduces.Because the dilution of dissolved mineral slurry is that primary wash liquor with red mud separating, washing workshop section is as diluent, the weaker concn of ore pulp has requirement, if just add a large amount of water when stripping self-evaporatint n., for guaranteeing the dilution pulp density, only have the add-on that reduces primary wash liquor, the required normal wash water add-on of red mud separating, washing is reduced, the washing balance is upset, the washing effect of red mud descends, and effluxes red mud and does not reach environmental requirement.If guarantee the washing effect of red mud, leaching requirement with normal need washs red mud, and the concentration of stripping dilution does not just reach the normal value requirement, can cause like this steaming water yield increase of subsequent evaporation workshop section, steam consumption increases, and the energy consumption of alumina producing increases.Stripping flash-pot water filling flow process is seen Figure of description 1.
Summary of the invention
The technical problem to be solved in the present invention is, a kind of stripping self-evaporatint n. technique is provided, and with the water filling in the higher final stage flash-pot of concentration that overcomes that prior art exists, thereby causes ore pulp to be diluted the deficiencies such as rear alkali concn reduction.
In order to solve described technical problem, the present invention is by the following technical solutions: after bauxite and alkali lye are prepared into qualified raw pulp, send into pressure digestion system with high-pressure pump, raw pulp is obtaining dissolved mineral slurry after stripping under the high temperature of 260 ~ 280 ℃, dissolved mineral slurry through multistage self-evaporatint n. step by step after pressure and temperature reducing temperature be down to approximately 130 ~ 120 ℃, send into again dilution trap, after the next primary wash liquor dilution of red-mud settlement washing room, with the past red mud separating, washing of pumping workshop section; In described multistage self-evaporatint n. flow process, the primary wash liquor of employing red-mud settlement washing injects the rear some grades of flash-pots that lean on of multistage flash-pot.
The pressure of the primary wash liquor of the red-mud settlement washing of adopting will be higher than the pressure in the flash-pot that injects.
The primary wash liquor pressure of delivering to dilution trap when the washing of original red-mud settlement is enough high, namely adopts from then on primary wash liquor pipe top set, and primary wash liquor is injected flash-pot.
The present invention is directed to stripping self-evaporatint n. needs water filling to reduce concentration of sodium carbonate, and then causes large water gaging to enter the dilution flow process, and the wash water of red-mud settlement washing can not be added, and has disturbed normal laterite washing balance; Or cause weaker concn to reduce, evaporization process steams the water yield and increases, the situation that the energy consumption of alumina producing increases, employing will change the mode of annotating primary wash liquor into toward the flash-pot water filling, both reached the purpose that reduces concentration of sodium carbonate, satisfy again the requirement of normal washing balance, weaker concn is guaranteed, and does not increase the energy consumption of evaporation section.
Description of drawings
Fig. 1 is the schematic diagram of prior art;
Fig. 2 is schematic diagram of the present invention.
Embodiment
Embodiments of the invention: its technical process is: after bauxite and alkali lye are prepared into qualified raw pulp, send into pressure digestion system with high-pressure pump, raw pulp is obtaining dissolved mineral slurry after stripping under the high temperature of 260 ~ 280 ℃, dissolved mineral slurry through multistage self-evaporatint n. step by step after pressure and temperature reducing temperature be down to approximately 130 ~ 120 ℃, send into again dilution trap, after the next primary wash liquor dilution of red-mud settlement washing room, with the past red mud separating, washing of pumping workshop section.In described multistage self-evaporatint n. flow process, the primary wash liquor of employing red-mud settlement washing injects the rear some grades of flash-pots that lean on of multistage flash-pot.
Fig. 2 is the flow process that high pressure digestion ore pulp flash-pot is annotated primary wash liquor, which grade flash-pot to annotate washing lotion for, and when needing according to alumina producer self-evaporatint n., the particular case of concentration of sodium carbonate is fixed.Owing in the stripping flash-pot, pressure being arranged, pressure from the primary wash liquor of red-mud settlement washing will can inject flash-pot smoothly higher than the pressure guarantee washing lotion in that grade flash-pot that injects, if the primary wash liquor pressure that dilution trap is delivered in original red-mud settlement washing is enough high, also can adopt from then on primary wash liquor pipe top set, primary wash liquor is injected flash-pot.
Claims (3)
1. stripping self-evaporatint n. technique, after bauxite and alkali lye are prepared into qualified raw pulp, send into pressure digestion system with high-pressure pump, raw pulp is obtaining dissolved mineral slurry after stripping under the high temperature of 260 ~ 280 ℃, dissolved mineral slurry through multistage self-evaporatint n. step by step after pressure and temperature reducing temperature be down to approximately 130 ~ 120 ℃, send into again dilution trap, after the next primary wash liquor dilution of red-mud settlement washing room, with the past red mud separating, washing of pumping workshop section; It is characterized in that: in described multistage self-evaporatint n. flow process, the primary wash liquor of employing red-mud settlement washing injects the rear some grades of flash-pots that lean on of multistage flash-pot.
2. a kind of stripping self-evaporatint n. technique according to claim 1 is characterized in that: the pressure of the primary wash liquor of the red-mud settlement washing of adopting will be higher than the pressure in the flash-pot that injects.
3. a kind of stripping self-evaporatint n. technique according to claim 1 and 2 is characterized in that: the primary wash liquor pressure of delivering to dilution trap when original red-mud settlement washing is enough high, namely adopts from then on primary wash liquor pipe top set, and primary wash liquor is injected flash-pot.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011103966689A CN103130256A (en) | 2011-12-05 | 2011-12-05 | Dissolving self-evaporation process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011103966689A CN103130256A (en) | 2011-12-05 | 2011-12-05 | Dissolving self-evaporation process |
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|---|---|
| CN103130256A true CN103130256A (en) | 2013-06-05 |
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| CN2011103966689A Pending CN103130256A (en) | 2011-12-05 | 2011-12-05 | Dissolving self-evaporation process |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104436716A (en) * | 2013-09-17 | 2015-03-25 | 贵阳铝镁设计研究院有限公司 | Ore pulp spontaneous-evaporation steam-liquid separation device |
| CN110040752A (en) * | 2019-04-29 | 2019-07-23 | 贵州大学 | A method of improving digesting efficiency of alumina in high titanium bauxite |
| CN111960440A (en) * | 2020-09-02 | 2020-11-20 | 陶予敏 | Process for producing soda ash and building insulating brick from red mud |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1221706A (en) * | 1998-09-09 | 1999-07-07 | 贵州铝厂 | Tech. for avoiding separating out of soda crystal in evaporiator |
| 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 |
| CN101234771A (en) * | 2007-01-31 | 2008-08-06 | 中国铝业股份有限公司 | Mother liquid evaporation desalting technique in aluminum oxide production |
| CN101671042A (en) * | 2008-09-09 | 2010-03-17 | 中铝国际技术发展有限公司 | Alumina melting method |
| CN102107897A (en) * | 2009-12-23 | 2011-06-29 | 中国铝业股份有限公司 | Method for controlling precipitation of crystal alkali in evaporator |
-
2011
- 2011-12-05 CN CN2011103966689A patent/CN103130256A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1221706A (en) * | 1998-09-09 | 1999-07-07 | 贵州铝厂 | Tech. for avoiding separating out of soda crystal in evaporiator |
| 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 |
| CN101234771A (en) * | 2007-01-31 | 2008-08-06 | 中国铝业股份有限公司 | Mother liquid evaporation desalting technique in aluminum oxide production |
| CN101671042A (en) * | 2008-09-09 | 2010-03-17 | 中铝国际技术发展有限公司 | Alumina melting method |
| CN102107897A (en) * | 2009-12-23 | 2011-06-29 | 中国铝业股份有限公司 | Method for controlling precipitation of crystal alkali in evaporator |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104436716A (en) * | 2013-09-17 | 2015-03-25 | 贵阳铝镁设计研究院有限公司 | Ore pulp spontaneous-evaporation steam-liquid separation device |
| CN110040752A (en) * | 2019-04-29 | 2019-07-23 | 贵州大学 | A method of improving digesting efficiency of alumina in high titanium bauxite |
| CN111960440A (en) * | 2020-09-02 | 2020-11-20 | 陶予敏 | Process for producing soda ash and building insulating brick from red mud |
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Application publication date: 20130605 |