CN101831544B - Method for separating manganese and silver from manganese-silver ore and purifying manganese leaching solution to extract manganese sulfate - Google Patents
Method for separating manganese and silver from manganese-silver ore and purifying manganese leaching solution to extract manganese sulfate Download PDFInfo
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Abstract
A manganese and silver separation and manganese leaching solution purification treatment method for manganese and silver ores comprises the following steps: 1) pre-degrading and saccharifying straw, shell and slag as plant by-products; 2) the product obtained in the step 1) reacts with manganese and silver raw ore or the leached manganese of the enriched bulk concentrate; 3) step 2) separating, neutralizing and adsorbing the manganese leaching solution to obtain a solution for preparing manganese sulfate and the like through further purification and crystallization; 4) the manganese leaching residue obtained in the step 3) has high reaction activity, short leaching time during silver leaching treatment and low energy consumption. The purification method is also suitable for purifying manganese leaching liquid for treating pyrolusite and ferromanganese ores by adopting reducing agents such as rice bran and the like, and the treated manganese liquid can be used for producing manganese sulfate, electrolytic manganese and the like. The method has the characteristics of wide source of separation raw materials, reasonable process route, less equipment investment, low treatment cost, stable product performance and the like, and the prepared manganese sulfate can meet the standard requirements of the industries such as chemical industry, feed, agriculture and the like.
Description
Technical field
The present invention relates to a kind of method of mineral substance separation and Extraction, purify the method for extracting manganous sulfate, be specially the method for separating and soaking manganese liquid purifying treatment to argentiferous manganese oxidized ore manganese, silver for a kind of manganese-silver ore manganese silver separates and soaks manganese liquid.What wherein, this method of soaking manganese liquid purifying treatment also was fit to adopt pyrolusite that reductive agent such as similar rice bran handles, ferrimanganic ore deposit soaks manganese liquid purifying treatment; Manganese liquid after the purification can be used for preparing manganous sulfate and electrolytic manganese etc., and the manganous sulfate of preparation can reach the requirement of different industries standards such as chemical industry, feed, agricultural.
Background technology
Manganese in the argentiferous manganese oxidized ore is mainly 4 valency manganese, and how silver is adsorbed situation with isomorph or silver with manganese exists, and manganese can not separate with beneficiation method with silver, and the manganese silver collective concentrate that can only obtain enrichment is handled in ore dressing.It is the important step that argentiferous type manganese oxidized ore is handled that manganese, silver separate, and can adopt pyrogenic process and hydrometallurgical process technology.Wherein, hydrometallurgical process technology has advantages such as manganese and silver raising recovery rate are high, facility investment is few, dust discharge is little, processing cost is low, but wet processing is if directly soak silver earlier, and silver leaching rate generally only has 20%-40%; At present treatment process that adopt are in acidic solution, 4 valency manganese to be reduced to divalent manganese with inorganic or organic type of reductive agent earlier to obtain soaking manganese liquid more; Separation is soaked manganese liquid and is obtained the argentiferous manganese slag that soaks; To soaking first manganese-back money footwork treatment process that the manganese slag soaks silver again; Can reach manganese, the effective isolating purpose of silver, can technology industrial application depend on mainly at present that the separation of manganese silver, purification and impurity removal, recovery extract the mixed economy cost of each process flow.
Wet processing manganese-silver ore technology is looked raw ore manganese, silver content can adopt direct treatment process or adopt magnetic separation to obtain the pre-concentration treatment process of manganese silver collective concentrate earlier; Reported or openly with reductive agent sulfurous gas, pyrite, xitix, polyphenol, hydrogen peroxide, glucose, starch etc. have been arranged to the manganese of argentiferous type manganese oxidized ore silver wet reducing separating technology; To obtain soaking manganese liquid adopt prior art with in lime or the lime carbonate with deironing, sulphide salt removing heavy metals, concentratedly leave standstill deliming, thermal crystalline obtains manganous sulfate after separating; Soak the manganese slag and adopt cyaniding or other method leaching-reduction to obtain thick silver powder (mud) and argentiferous behind the manganese liquid is soaked in separation, more than various reducing process all have certain defective.
Adopt sulfurous gas to make reductive agent like Chinese patent ZL93103953.3, logical sulfur dioxide gas leaches manganese in ore deposit-sulfuric acid slurries system, and the slag behind the separation manganese adopts cyaniding to soak its time of silver at 24h～40h; Obtain manganous sulfate to soaking manganese liquid with lime neutralization, purification, crystallization, manganese, silver-colored total yield reach 94.02% and 94.45% respectively.Though this sulphur dioxide reduction technology manganese, silver raising recovery rate are higher, the sulfur dioxide gas raw material of selecting for use has limitation to region and transportation, and its processing cost is also higher, has limited applying of technology.
The pyrite method is separated manganese silver and is characterized in that the reductive agent price is lower; But exist the reductive agent consumption big, go out that the quantity of slag is big, the symbiosis element in the pyrite is prone to get into and soaks manganese liquid and make later separation than complicacy etc.; Technology is fit to that the sulfuration mineral resources is arranged nearby, has the argentiferous type manganese oxidized ore processing enterprise of storing up conditions such as slag field to adopt this technology; Adopt that this method obtains soak the manganese slag again cyaniding soak silver; Time generally need 48h or longer (Zhang Suchun etc. the pyrite method is extracted the research [J] of silver from manganese-silver ore. Chinese manganese already, 1994, (5): 35-37).
Though it is higher that methods such as glucose, xitix, polyphenol, hydrogen peroxide are separated the reductive agent activity of manganese, silver; Have flow process short, soak manganese go out the quantity of slag low, when soaking silver slag active high, separate characteristics such as manganese liquid aftertreatment technology is simple; Be higher than pyrite and sulfurous gas method but comprehensively leach the manganese cost more at present, this technology also is difficult to industrial application.Though having overcome methods such as xitix, polyphenol, hydrogen peroxide, starch method leaches the manganese defect of high cost; But existing again, this method soaks manganese liquid because remaining low molecular degradation thing purifies the big problem of difficulty of removing; The manganous sulfate quality of producing is lower, generally only can reach agricultural and use standard.
And to handle the extract technology of manganese in pyrolusite, the ferrimanganic ore deposit with rice bran (or straw etc.)-sulfate reduction, be divided into full wet method, leaching-slaking method, ignite-three types of lixiviation process.If adopt full wet processing, its soak manganese liquid purify have similar separation manganese silver starch method its soak the remaining low molecular degradation thing of manganese liquid and purify the big problem of difficulty of removing, the manganous sulfate of preparation generally also only can reach agricultural and use the manganous sulfate standard; Be to improve the manganous sulfate quality, the leaching-slaking method of improvement occurred, formerly adopt sulfuric acid wet process to soak manganese after; Need after general 150 ℃～300 ℃ to soak the manganese screenings carry out slaking (Yang Ming equality, rice bran-sulfuric acid are directly soaked preparation of manganese condition research [J]. inorganic chemicals industry, 2005; (2): 30-32); To reduce the content of remaining low molecular degradation thing, further purify again and obtain high-quality manganous sulfate, the corresponding defectives such as long flow path, energy consumption height that then exist of such technology.Thereby, rice bran
(or straw etc.) though the technology report of handling pyrolusite, ferrimanganic ore deposit early, extract technology also than coal roasting reduction cost low with operational condition optimization because the manganous sulfate quality of output is lower, fail industrial application always.When being raw material system manganous sulfate with the pyrolusite; Industry mainstream applications technology is still coal/manganese ore mixing-roasting reduction-soak manganese-purification-manganous sulfate crystallization processes; Because adopt about 800 ℃ roasting reduction temperature, the coal spontaneous combustion reduction efficiency is low, there are defectives such as coal consumption is high, dust is big, facility investment is big.
Summary of the invention
The objective of the invention is to overcome above-mentioned deficiency of the prior art; One type of manganese that raw material sources are wide, separation efficiency is high, cost is low, the silver-colored separating technology that soaks manganese liquid with serial reductive agent and purifying treatment that separates have been proposed; Manganese scavenging solution after the simple process can be used for preparing manganous sulfate and electrolytic manganese etc., and the manganous sulfate of preparation can reach industry standard application requiring such as chemical industry, feed, agricultural; And adopt that this technology obtains soak the cyaniding of manganese slag when soaking silver because slag is active high; The sodium cyanide consumption is when 1.5kg/t～3.0kg/t manganese slag; Cyaniding is soaked silver and the time is merely 3h; Be the ZL93103953.3 patent introduce the sulfurous gas method soak the cyaniding of manganese slag soak silver the time 1/8～1/13, have the characteristics that silver-colored power consumption is low, efficient is high of soaking.Through verification experimental verification, the purifying treatment that manganese liquid is soaked in this similar reductive agent processing pyrolusite, ferrimanganic ore deposits such as the also suitable employing rice bran of method of soaking manganese liquid purifying treatment.
The objective of the invention is to realize like this:
A kind of method of separating and soaking manganese liquid purification extraction manganous sulfate to manganese-silver ore manganese silver, it comprises the steps:
1) makees reductive agent with plant by-product straw, shell or fibrous residue and carry out reduction reaction with manganese; Manganese, silver element are separated; Said plant by-product straw is corn, wheat, paddy rice, Chinese sorghum, beans straw; Or plant by-product shell is wheat bran, Pericarppium arachidis hypogaeae, rice chaff shell that grain processing is discharged, or plant by-product fibrous residue is the robust fibre slag of apple, the discharging of soya bean squeezing system juice;
The powder of 0.15mm～0.50mm was processed in elder generation's fragmentation when 2) the said reductive agent of step 1) used;, sulfuric acid catalysis reacts after degrading saccharification in advance again with the manganese in the manganese-silver ore; Degradation condition is 60 ℃～95 ℃ of temperature, time 0.5h～1h in advance, and the consumption that manganese, silver separate with the plant crude fiber powder contains manganese amount of metal and pure plant powder mass ratio 1.22～2.44 by manganese-silver ore, and the sulfuric acid consumption contains manganese amount of metal and sulfuric acid amount mass ratio 0.40～0.50 by manganese-silver ore; Soak manganese reaction solution volume and manganese-silver ore total mass number than 3～4; 90 ℃～95 ℃ of manganese temperature of reaction are soaked in control, time 3h～5h obtains soaking manganese liquid, and the manganese leaching yield reaches 85%～99%, and silver is stayed and soaked in the manganese slag;
3) soak manganese liquid and adopt lime carbonate or lime to be neutralized to pH=4～5, again with the residual traces of unreacted plant degradation thing of natural mineral absorption, through further purification, crystallization obtain manganous sulfate with adsorption function;
Wherein the step 3) purifying treatment step of soaking manganese liquid is neutralization earlier, absorption again; Natural mineral is the mineral that wilkinite, zeolite, zeyssatite, kaolin, vermiculite have adsorption function, and adsorption cleaning uses the amount of natural mineral to be 2.5%～7.5% of manganese-silver ore mass ratio;
4) argentiferous behind the manganese liquid is soaked in separation and soak the manganese slag and leach, revert back cash register, obtain containing silver powder.
Described a kind of manganese-silver ore manganese silver separates and soaks the method that manganese liquid purifies the extraction manganous sulfate, and it is characterized in that: soak manganese liquid purifying treatment and use wilkinite, its smectite content is not less than 30%, and smectite content is high more, and it is few more to add consumption when purifying adsorption treatment.
The pyrolusite that purifying method also be fit to adopt similar rice bran to make reductive agent to handle, ferrimanganic ore deposit soak manganese liquid purifying treatment.
Manganese, the silver-colored separating technology that the present invention proposes has the sulfuric acid catalysis saccharification operation of degrading in advance when using with plant by-product robust fibre powder; Catalysis acid is leached needed sulfuric acid for manganese; Do not add acid, 60 ℃～95 ℃ of pure plant powder acid catalysis degraded saccharification temperatures, time 0.5h～1h; Used plant by-product staple is a crude fibre, and molecular formula is: (C
6H
10O
5)
n, reduction is soaked the main serial reaction of manganese and is:
12MnO
2+C
6H
12O
6+12H
2SO
4→12MnSO
4+6CO
2↑+18H
2O
1 molecule C
6H
12O
6Theory can transform 12 molecule MnO
2, being scaled the manganese amount of metal is 4.07 with cellulose amount Theoretical Mass ratio, actual includes other non-fibre fractionation because of other high-valency metal such as manganese-silver ore iron content and plant by-product when leaching manganese, actual amount ratio is less than last value.
Beneficial effect
The coarse-fibred plant by-product class reductive agent that is rich in that adopts the present invention to propose separates manganese-silver ore; Can not only overcome the deficiency of existing manganese-silver ore manganese, silver-colored separating technology; Make manganese silver reach the higher separation and the recovery; And the reductive agent that adopts is inexpensive regenerated resource in a large number, do not have the limitation of region and resource application.The purification process technique that proposes to this separating technology is fit to not only that it soaks the purification of manganese liquid with manganese-silver ore; And be fit to adopt the pyrolusite that reductive agent such as similar rice bran handles, the purifying treatment of soaking manganese liquid in ferrimanganic ore deposit; Manganese liquid after the purification can be used for preparing manganous sulfate and electrolytic manganese etc., and the manganous sulfate of preparation can reach the requirement of different industries standards such as chemical industry, feed, agricultural.It soaked the purifying treatment difficult problem of manganese liquid when the present invention technology purification process technique can solve reduction such as the rice bran processing pyrolusite that exists for many years, ferrimanganic ore deposit.
Description of drawings
Fig. 1 is a process flow sheet of the present invention;
Embodiment
Below in conjunction with process flow sheet of the present invention, the present invention is further described:
Embodiment 1
(1) corn straw is broken to the powder that particle diameter is about 0.15mm in advance, the 1kg powder is added to W (H
2SO
4In the 3kg sulfuric acid of)=95%, the 5.3kg water pre-blended solution, stir, be heated to 95 ℃ of in advance degraded saccharification 0.5h, add content W (Mn)=30.5%, silver-colored 640g/t, W (Fe)=11.5% granularity-0.075mm and be 90% mn-ag concentrate powder 4kg; Moisturizing 5kg; Stir, be incubated 90 ℃～95 ℃ and leach manganese reaction 5h, isolate the undissolved manganese slag that soaks, the manganese slag is soaked in water 12kg washing; The manganese leaching yield is 92.5%, and silver-colored solubility rate is less than 2%;
(2) manganese leach liquor and washings are merged, the limit adds 0.85kg lime carbonate limit stirring heating and is warming up to 90 ℃ and be incubated 1h, and the pH value of neutralization back solution is 5, adds 0.2kg wilkinite insulation reaction 0.5h again, isolates except that scum;
(3) purifying and removing of heavy metal and crystallization system manganous sulfate operation adopts existing current techique, obtains sulfuric acid monohydrate manganese product 3.1Kg, first grade manganous sulfate 1.8Kg wherein, its W (Mn)=31.93%, W (Fe)≤0.004%;
(4) step (1) is soaked the manganese slag and add water 10kg dispersion slurrying, adding the lime adjust pH is 11, adds the 7.8g sodium cyanide and soaks silver-colored 3h with the cyaniding leaching machine, silver leaching rate 92.67%;
(5), step (4) soaked silvering solution adopt general zinc powder reduction technology to reclaim silver, obtain the silver powder 128g of argentiferous W (Ag)=1.8%, silver raising recovery rate about 99%.
(6), respectively go on foot manganese, silver adds up to total yield to be respectively 90.65%, 89.91%.
Embodiment 2
(1) wheat bran is broken to the powder that particle diameter is about 0.15mm in advance, the 0.8kg powder is added to W (H
2SO
4In the 3kg sulfuric acid of)=95%, the 5.3kg water pre-blended solution, stir, be heated to 60 ℃ of in advance degraded saccharification 1h, add content W (Mn)=30.5%, silver-colored 640g/t, W (Fe)=11.5% granularity-0.075mm and be 90% mn-ag concentrate powder 4kg; Moisturizing 5kg; Stirring heats up 90 ℃～95 ℃ leaches manganese reaction 4h, isolates the undissolved manganese slag that soaks, and the manganese slag is soaked in water 12kg washing; The manganese leaching yield is 93.10%, and silver-colored solubility rate is less than 2%;
(2) manganese leach liquor and washings are merged, the limit adds 0.85kg lime carbonate limit stirring heating and rises steady temperature to 90 ℃, and the pH value of neutralization back solution is 5, adds 0.1kg natural zeolite powder insulation reaction 0.5h, isolates except that scum;
(3) the existing current techique of purifying and removing of heavy metal and crystallization system manganous sulfate process using, the manganese sulfate product 3.15Kg that obtains, first grade manganous sulfate 1.75Kg wherein, its W (Mn)=32.10%, W (Fe)≤0.004%;
(4) step (1) is soaked the manganese slag and add water 10kg dispersion slurrying, adding the lime adjust pH is 11, adds the 7.8g sodium cyanide and soaks silver-colored 3h with the cyaniding leaching machine, silver leaching rate 92.85%;
(5), step (4) soaked silvering solution adopt general zinc powder reduction technology to reclaim silver, obtain the silver powder 129g of argentiferous W (Ag)=1.78%, silver raising recovery rate about 99%.
(6), respectively go on foot manganese, silver adds up to total yield to be respectively 91.24%, 90.08%.
Embodiment 3
(1) fibrous residue with apple squeezing system juice is broken to the powder that particle diameter is about 0.50mm in advance, and the 0.5kg powder is added to W (H
2SO
4In the 3kg sulfuric acid of)=95%, the 5.3kg water pre-blended solution, stir, be heated to 95 ℃ of in advance degraded saccharification 0.5h, add content W (Mn)=30.5%, silver-colored 640g/t, W (Fe)=11.5% granularity-0.075mm and be 90% mn-ag concentrate powder 4kg; Moisturizing 9kg; Stirring heats up 90 ℃～95 ℃ leaches manganese reaction 3h, isolates the undissolved manganese slag that soaks, and the manganese slag is soaked in water 12kg washing; The manganese leaching yield is 93.50%, and silver-colored solubility rate is less than 2%;
(2) manganese leach liquor and washings are merged, the limit adds 0.70kg lime carbonate limit stirring heating and rises steady temperature to 90 ℃, and the pH value of neutralization back solution is 5, adds 0.3kg diatomite in powder insulation reaction 0.5h, isolates except that scum;
(3) the existing current techique of purifying and removing of heavy metal and crystallization system manganous sulfate process using obtains sulfuric acid monohydrate manganese product 3.05Kg, first grade manganous sulfate 1.70Kg wherein, its W (Mn)=32.05%, W (Fe)≤0.004%;
(4) step (1) is soaked the manganese slag and add water 10kg dispersion slurrying, adding the lime adjust pH is 11, adds the 7.8g sodium cyanide and soaks silver-colored 3h with the cyaniding leaching machine, silver leaching rate 93.01%;
(5), step (4) soaked silvering solution adopt general zinc powder reduction technology to reclaim silver, obtain the silver powder 131g of argentiferous W (Ag)=1.75%, silver raising recovery rate about 99%.
(6), respectively go on foot manganese, silver adds up to total yield to be respectively 91.63%, 90.24%.
The coarse-fibred plant by-product class reductive agent that is rich in that adopts the present invention to propose separates manganese-silver ore; Can not only overcome the deficiency of existing manganese-silver ore manganese, silver-colored separating technology; Make manganese silver reach the higher separation and the recovery; And the reductive agent that adopts is inexpensive regenerated resource in a large number, do not have the limitation of region and resource application.The purification process technique that proposes to this separating technology is fit to not only that it soaks the purification of manganese liquid with manganese-silver ore; And be fit to adopt the pyrolusite that reductive agent such as similar rice bran handles, the purifying treatment of soaking manganese liquid in ferrimanganic ore deposit; Manganese liquid after the purification can be used for preparing manganous sulfate and electrolytic manganese etc., and the manganous sulfate of preparation can reach the requirement of different industries standards such as chemical industry, feed, agricultural.It soaked the purifying treatment difficult problem of manganese liquid when the present invention technology purification process technique can solve reduction such as the rice bran processing pyrolusite that exists for many years, ferrimanganic ore deposit.
Above embodiment only is used to explain preferred implementation of the present invention; But the present invention is not limited to above-mentioned embodiment; In the ken that said field those of ordinary skill is possessed; Any modification of being done within spirit of the present invention and the principle, be equal to and substitute and improvement etc., it all should be encompassed within the technical scheme scope that the present invention asks for protection.
Claims (2)
1. manganese-silver ore manganese silver separates and soaks manganese liquid and purifies the method for extracting manganous sulfate, and it comprises the steps:
1) makees reductive agent with plant by-product straw, shell or fibrous residue and carry out reduction reaction with manganese; Manganese, silver element are separated; Said plant by-product straw is corn, wheat, paddy rice, Chinese sorghum, beans straw; Or plant by-product shell is wheat bran, Pericarppium arachidis hypogaeae, rice chaff shell that grain processing is discharged, or plant by-product fibrous residue is the robust fibre slag of apple, the discharging of soya bean squeezing system juice;
The powder of 0.15mm～0.50mm was processed in elder generation's fragmentation when 2) the said reductive agent of step 1) used;, sulfuric acid catalysis reacts after degrading saccharification in advance again with the manganese in the manganese-silver ore; Degradation condition is 60 ℃～95 ℃ of temperature, time 0.5h～1h in advance, and the consumption that manganese, silver separate with the plant crude fiber powder contains manganese amount of metal and pure plant powder mass ratio 1.22～2.44 by manganese-silver ore, and the sulfuric acid consumption contains manganese amount of metal and sulfuric acid amount mass ratio 0.40～0.50 by manganese-silver ore; Soak manganese reaction solution volume and manganese-silver ore total mass number than 3～4; 90 ℃～95 ℃ of manganese temperature of reaction are soaked in control, time 3h～5h obtains soaking manganese liquid, and the manganese leaching yield reaches 85%～99%, and silver is stayed and soaked in the manganese slag;
3) soak manganese liquid and adopt lime carbonate or lime to be neutralized to pH=4～5, again with the residual traces of unreacted plant degradation thing of natural mineral absorption, through further purification, crystallization obtain manganous sulfate with adsorption function;
Wherein the step 3) purifying treatment step of soaking manganese liquid is neutralization earlier, absorption again; Natural mineral is the mineral that wilkinite, zeolite, zeyssatite, kaolin, vermiculite have adsorption function, and adsorption cleaning uses the amount of natural mineral to be 2.5%～7.5% of manganese-silver ore mass ratio;
4) argentiferous behind the manganese liquid is soaked in separation and soak the manganese slag and leach, revert back cash register, obtain containing silver powder.
2. a kind of manganese-silver ore manganese silver according to claim 1 separates and soaks the method for manganese liquid purification extraction manganous sulfate; It is characterized in that: soak manganese liquid purifying treatment and use wilkinite; Its smectite content is not less than 30%, and smectite content is high more, and it is few more to add consumption when purifying adsorption treatment.
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| CN114457241B (en) * | 2022-01-05 | 2024-01-30 | 重庆大学 | Method for reducing soluble manganese and water content of electrolytic manganese slag |
| CN114457240A (en) * | 2022-01-05 | 2022-05-10 | 重庆大学 | Method for harmlessly treating electrolytic manganese slag leachate |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1079258A (en) * | 1993-04-07 | 1993-12-08 | 核工业中南地质勘探局230研究所 | Produce manganous sulfate and extract silver-colored method from manganese-silver ore |
| CN1186866A (en) * | 1997-11-27 | 1998-07-08 | 夏新民 | Wet silver extracting process from silver ore with high manganese, sulphur and iron content |
| CN1632143A (en) * | 2004-12-30 | 2005-06-29 | 周国宪 | Method for chloridizing roasting and ammonia extraction of silver and manganese products for manganese silver finished ore |
-
2010
- 2010-05-18 CN CN2010101742674A patent/CN101831544B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1079258A (en) * | 1993-04-07 | 1993-12-08 | 核工业中南地质勘探局230研究所 | Produce manganous sulfate and extract silver-colored method from manganese-silver ore |
| CN1186866A (en) * | 1997-11-27 | 1998-07-08 | 夏新民 | Wet silver extracting process from silver ore with high manganese, sulphur and iron content |
| CN1632143A (en) * | 2004-12-30 | 2005-06-29 | 周国宪 | Method for chloridizing roasting and ammonia extraction of silver and manganese products for manganese silver finished ore |
Non-Patent Citations (2)
| Title |
|---|
| 孙亚光等.低分子碳氢化合物分离锰银氧化矿工艺研究.《矿业工程》.2008,第28卷(第2期),66-71. * |
| 杨明平等.酒糟- 硫酸浸取锰矿尾矿中锰制备硫酸锰工艺.《无机盐工业》.2006,第38卷(第11期),50-52. * |
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| CN101831544A (en) | 2010-09-15 |
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