CN103757277A - Method for re-leaching waste residue generated through leaching manganese carbonate ore with sulfuric acid - Google Patents
Method for re-leaching waste residue generated through leaching manganese carbonate ore with sulfuric acid Download PDFInfo
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- CN103757277A CN103757277A CN201310736430.5A CN201310736430A CN103757277A CN 103757277 A CN103757277 A CN 103757277A CN 201310736430 A CN201310736430 A CN 201310736430A CN 103757277 A CN103757277 A CN 103757277A
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- CN
- China
- Prior art keywords
- leaching
- waste residue
- sulfuric acid
- manganese carbonate
- carbonate ore
- Prior art date
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention discloses a method for re-leaching waste residue generated through leaching manganese carbonate ore with sulfuric acid. The method comprises the steps of grinding the waste residue which is generated through leaching the manganese carbonate ore with sulfuric acid until the particle size is not greater than 180 meshes, then, adding the ground waste residue into a reaction kettle which is resistant to pressure and the corrosion of sulfuric acid, adding a sulfuric acid solution with the pH value of 1-3, and then, carrying out reduction leaching under closed conditions while introducing industrial pure SO2.
Description
Technical field
The present invention relates to the one leaching method again of the waste residue of sulfuric acid leaching manganese carbonate ore generation.
Background technology
Manganese carbonate ore is the important source material of producing the materials such as manganese metal, manganous sulfate, Manganse Dioxide, manganous nitrate.Wet processing is to produce the main technique of above-mentioned materials, leaches the operation operation that is absolutely necessary in this technique.Producing in the wet processing of manganese metal, manganous sulfate, Manganse Dioxide, substantially adopt sulfuric acid leaching system.Owing to containing certain MnO in manganese carbonate ore
2, MnO
2be insoluble to sulfuric acid, cause while adopting sulfuric acid leaching manganese carbonate ore, the leaching yield of metal target manganese is not high, causes the wasting of resources.Sulfuric acid leaching manganese carbonate ore produces at present waste residue generation and volume of cargo in storage are all very large, and waste residue, containing manganese approximately 6%, has recovery value again.Adopt wet processing to its recycling, can rely on existing technique, the facilities and equipment of the enterprise that produces this class waste residue, than being easier to, implement, leaching operation is the requisite operation of wet processing, develops thus that leaching yield is high, leaching velocity is fast, energy consumption is low, can have larger practical value with the existing technique, the leaching method again of waste residue that sulfuric acid leaching manganese carbonate ore that facilities and equipment match produces of the enterprise that produces this class waste residue.
Summary of the invention
The recycling problem of the waste residue producing for current sulfuric acid leaching manganese carbonate ore, the object of the invention is to find that a kind of leaching yield is high, leaching velocity is fast, energy consumption is low, can with the existing technique, the leaching method again of waste residue that sulfuric acid leaching manganese carbonate ore that facilities and equipment match produces of enterprise that produces this class waste residue, it is characterized in that the waste residue that sulfuric acid leaching manganese carbonate ore is produced is milled down in the reactor that adds withstand voltage, sulfuric acid corrosion resistant after the order of particle diameter≤180.Adding pH is 1～3 sulphuric acid soln.Then pass in confined conditions technical pure SO
2gas reduces leaching.After leaching finishes, emit the slurry in reactor and carry out solid-liquid separation, obtaining required infusion solution.The leach liquor obtaining is for preparing the sulphuric acid soln that leaches manganese carbonate ore.Leached mud washes with water, and washing water are used for preparing sulphuric acid soln and leach for waste residue.Waste residue after washing send slag field to deposit.The temperature of leaching process is 50 ℃～80 ℃, and stirring velocity is 50 r/min～130 r/min.The add-on of the sulphuric acid soln of every kg waste residue is 2L～4L.Extraction time is 2h～4h.The relative pressure leaching is 0.01MPa～0.05MPa.
The object of the present invention is achieved like this: in waste residue, can leach element is mainly manganese and iron, is substantially respectively MnO
2, Mn (OH)
2and Fe (OH)
3state, mainly there is following chemical reaction in reduction leaching process:
SO
2?+?H
2O?=?H
2SO
3
H
2SO
3?+?MnO
2?=?MnSO
4
Mn(OH)
2?+?H
2SO
4?=?MnSO
4?+?H
2O
2Fe(OH)
3?+?3H
2SO4?=?Fe
2(SO
4)
3?+?6H
2O
Fe
2(SO
4)
3?+?H
2SO
3?+?H
2O?=?2FeSO
4?+?H
2SO
4
Due to SO
2reductibility stronger, MnO
2oxidisability also stronger, both are easy to occur chemical reaction, realize thus MnO
2leach more completely.
Although the acidity of the sulphuric acid soln adding is lower, be conducive to suppress Fe
3+enter leach liquor, but still have part Fe
3+enter leach liquor.Enter the Fe of leach liquor
3+by SO
2be reduced into Fe
2+, unfavorable to follow-up deironing (generally adopting neutralization precipitation method).Because the manganese content in waste residue is lower, the Mn of leach liquor
2+concentration is on the low side, and the existing purification of leaching liquor system of the direct Entry Firm of leach liquor also exists process matching problem.The leach liquor that present method is obtained leaches the required sulphuric acid soln of manganese carbonate ore for preparing, and can, according to the needs of the existing technique of enterprise, adjust flexibly the Mn of manganese carbonate ore leach liquor
2+concentration, realizes the matched well with existing technique.What is more important, contains some amount Fe in the leach liquor that the present invention obtains
2+, enter after manganese carbonate ore leaching system, there is following chemical reaction:
2FeSO
4?+?MnO
2?+?2H
2SO
4?=?Fe
2(SO
4)
3?+?MnSO
4?+?2H
2O
By above-mentioned reaction during by original sulfuric acid leaching manganese carbonate ore, the MnO that can not leach
2leach more completely, no longer produce new high Mn content waste residue.Meanwhile, Fe
2+be oxidized to Fe
3+, be conducive to follow-up purification of leaching liquor process, be equipped with completely with existing technique.
Outstanding advantages of the present invention is: through above-mentioned series reaction, the Mn in the waste residue that final sulfuric acid leaching manganese carbonate ore produces leaches substantially completely, reduces the wasting of resources, also to subsequent solution, does not purify and brings difficulty; Due to SO
2be easy to and MnO
2reaction, so reduction leaching process speed is fast; Process is carried out in confined conditions, has avoided SO
2effusion produce environmental pollution.
specific implementation method
embodiment 1: it is in the lining titanium pressure reaction still of 5L that the waste residue (containing manganese 6.2%, iron 15.1%, particle diameter 180 orders) that 2000g sulfuric acid leaching manganese carbonate ore is produced adds volume, adding pH is 3 sulphuric acid soln 4L, then closes vent valve, and opens SO
2intake valve passes into SO
2, at 60～70 ℃, stirring (stirring velocity 80r/min) and leach 2h, in reactor, relative pressure is 0.01MPa.After finishing, leaching carries out the washing of liquid-solid separation and leached mud.According to the assay result of the leached mud after cleaning, the leaching yield of manganese is 96.2%.
Embodiment 2: it is in the lining titanium pressure reaction still of 100L that the waste residue (containing manganese 6.2%, iron 15.1%, particle diameter 180 orders) that 20kg sulfuric acid leaching manganese carbonate ore is produced adds volume, adding pH is 1 sulphuric acid soln 80L, then closes vent valve, and opens SO
2intake valve passes into SO
2, at 50～60 ℃, stir (stirring velocity 70r/min) and leach 3h.In reactor, relative pressure is 0.05MPa.After finishing, leaching carries out the washing of liquid-solid separation and leached mud.According to the assay result of the leached mud after cleaning, the leaching yield of manganese is 99.3%.
Claims (2)
1. the one leaching method again of the waste residue of a sulfuric acid leaching manganese carbonate ore generation, it is characterized in that the waste residue that sulfuric acid leaching manganese carbonate ore is produced is milled down in the reactor that adds withstand voltage, sulfuric acid corrosion resistant after the order of particle diameter≤180, adding pH is 1～3 sulphuric acid soln, then passes in confined conditions technical pure SO
2gas reduces leaching, after leaching and finishing, emits the slurry in reactor and carries out solid-liquid separation, obtain required infusion solution, the leach liquor obtaining is for preparing the sulphuric acid soln that leaches manganese carbonate ore, and leached mud washes with water, and washing water are used for preparing sulphuric acid soln and leach for waste residue.
2. the waste residue after washing send slag field to deposit, the temperature of leaching process is 50 ℃～80 ℃, and stirring velocity is 50 r/min～130 r/min, and the add-on of the sulphuric acid soln of every kg waste residue is 2L～4L, extraction time is 2h～4h, and the relative pressure of leaching is 0.01MPa～0.05MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310736430.5A CN103757277A (en) | 2013-12-29 | 2013-12-29 | Method for re-leaching waste residue generated through leaching manganese carbonate ore with sulfuric acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310736430.5A CN103757277A (en) | 2013-12-29 | 2013-12-29 | Method for re-leaching waste residue generated through leaching manganese carbonate ore with sulfuric acid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103757277A true CN103757277A (en) | 2014-04-30 |
Family
ID=50524591
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310736430.5A Pending CN103757277A (en) | 2013-12-29 | 2013-12-29 | Method for re-leaching waste residue generated through leaching manganese carbonate ore with sulfuric acid |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1121049A (en) * | 1994-10-18 | 1996-04-24 | 冶金工业部长沙矿冶研究院 | Method for producing high-purity manganese carbonate by using pyrolusite |
| CN101456597A (en) * | 2009-01-08 | 2009-06-17 | 四川大学 | Method for preparing manganese sulfate solution by using sulphur dioxide gas leach manganese dioxide ore |
| CN102030375A (en) * | 2010-10-29 | 2011-04-27 | 北京矿冶研究总院 | Method for preparing lithium cobaltate by directly using failed lithium ion battery |
-
2013
- 2013-12-29 CN CN201310736430.5A patent/CN103757277A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1121049A (en) * | 1994-10-18 | 1996-04-24 | 冶金工业部长沙矿冶研究院 | Method for producing high-purity manganese carbonate by using pyrolusite |
| CN101456597A (en) * | 2009-01-08 | 2009-06-17 | 四川大学 | Method for preparing manganese sulfate solution by using sulphur dioxide gas leach manganese dioxide ore |
| CN102030375A (en) * | 2010-10-29 | 2011-04-27 | 北京矿冶研究总院 | Method for preparing lithium cobaltate by directly using failed lithium ion battery |
Non-Patent Citations (2)
| Title |
|---|
| 杨明平等: "二氧化硫浸锰制备高纯碳酸锰", 《无机盐工业》, vol. 36, no. 5, 30 September 2004 (2004-09-30), pages 42 - 44 * |
| 阳启华等: "SO2浸出软锰矿过程中抑制连二硫酸锰生成的研究", 《湿法冶金》, vol. 31, no. 3, 30 June 2012 (2012-06-30), pages 144 - 148 * |
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Application publication date: 20140430 |