CN101927213A - Flotation separation method for molybdenite and galena - Google Patents
Flotation separation method for molybdenite and galena Download PDFInfo
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- CN101927213A CN101927213A CN2009100230943A CN200910023094A CN101927213A CN 101927213 A CN101927213 A CN 101927213A CN 2009100230943 A CN2009100230943 A CN 2009100230943A CN 200910023094 A CN200910023094 A CN 200910023094A CN 101927213 A CN101927213 A CN 101927213A
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Abstract
The invention discloses a flotation separation method for molybdenite and galena, which comprises the following steps of: 1, rough grinding; 2, rough selection and scavenging for obtaining lead-containing molybdenum rough concentrate; 3, regrinding after a certain amount of active carbon is added into the lead-containing molybdenum rough concentrate; and 4, multiple selection: selecting the reground lead-containing molybdenum rough concentrate for multiple times according to the conventional selection process, adding a galena inhibitor into the lead-containing molybdenum rough concentrate at each time of selection, and then adding a molybdenite collecting agent and a foaming agent into the lead-containing molybdenum rough concentrate as required. The method has the advantages of simple separation process, reasonable design, good separation effect and capabilities of reducing the lead content to be as minimum as possible in an ore dressing process of molybdenum, effectively improving the reclamation rate of the molybdenum and thoroughly reducing the pollution of the lead to the environment at the same time of reducing the molybdenum concentrate smelting production cost and simplifying the production process.
Description
Technical field
The invention belongs to the wulfenite floatation separation technology field, especially relate to the flotation separation method of a kind of molybdenite and galena.
Background technology
The about 3,300,000 tons of molybdenums of molybdenum in China resource reserve belong to the first in the world.In the world's four big molybdenum ores, China occupies three.Many molybdenum deposits are leaded higher, for example: and area, Luanchuan, Henan molybdenum ore, the leaded equal height of Shaanxi Jin Duicheng molybdenum ore that reserves are the first in the nation, all adopted the plumbous technology that suppresses in the molybdenum ore dressing process.Area, molybdenum ore district, Luonan, Shaanxi Huanglong shop is composed and is deposited a large amount of carbonate-type wulfenite beds, the molybdenum average grade is between 0.06%～0.078%, about 28.7 ten thousand tons of molybdenum amount, plumbous grade 0.14%～0.20%, molybdenum content is lower than lead content in the mineral deposit, as contain molybdenum 0.04～0.08%, leaded 0.12～0.3%, individual lot is leaded higher.
Plumbous in the ore dressing flotation of molybdenum, very easily be enriched in the molybdenum concntrate.Lead is the harmful element in the molybdenum concntrate, the initial oxidation roasting in smelting of high plumbous molybdenum concntrate, and lead is the oxide volatilization.Lead oxides is a severe toxicity, enters the atmosphere serious environment pollution.When molybdenum concntrate oxidizing roasting, the lead in the molybdenum concntrate easily combines with molybdenum and is converted into lead molybdate, and lead molybdate is insoluble to ammoniacal liquor, thereby causes molybdenum to enter in the ammonia leaching residue, and molybdenum recovery declines to a great extent.Plumbous height in the molybdenum concntrate can influence the quality of molybdenum trioxide briquetting, molybdenum-iron and ammonium molybdate to some extent, and these impurity in the ammonium molybdate influence the quality and the application of molybdenum powder, molybdenum bar and molybdenum sheet.
At present, to fall lead mainly be to adopt chemical method wet method leaching-out technique to molybdenum concntrate.A kind of is the villaumite direct leaching, and another kind is that heat treatment afterchlorinate thing leaches.
The villaumite direct leaching is to do the oxidant intensification with alkali metal or alkaline earth metal chloride to leach.As the somewhere flotation molybdenum concentrate, account for 58% less than the 0.03mm grade, pulp density is 30%, under 110 ℃, with 5% copper chloride, 5.3% hydrochloric acid and 30% calcium chloride, the lead that leaches in the 2h molybdenum concntrate reduces to 0.01% from 0.55%; Leach 3h with 1% copper chloride, 10% ferric trichloride and 30% calcium chloride, the lead in the molybdenum concntrate reduces to 0.01% from 0.55%.Canada's Boulogne reaches the copper molybdenum and selects factory, and its output molybdenum concntrate is leaded 0.3%～1%, makes leaching agent with 1% copper chloride, 10% ferric trichloride, 3% hydrochloric acid and 30% calcium chloride, and pulp density is 35%, behind leaching 2h under 100 ℃ of conditions, and lead is lower than 0.04%.Someone has also tested with copper chloride, ferric trichloride and Klorvess Liquid, or copper chloride, ferric trichloride and magnesium chloride solution, or copper chloride, ferric trichloride and sodium chloride solution leaching molybdenum concntrate, all obtains better effects.Jin Dui city molybdenum ore has carried out molybdenum concntrate and has leached commerical test, and with 6% ferric trichloride, 2% hydrochloric acid, at 85-90 ℃ of leaching 1h, its lead reduces to 0.032% from 0.174%, and the molybdenum leaching rate is lower than 0.5%.
Heat treatment afterchlorinate thing lixiviation process is that flotation molybdenum concentrate is fully mixed with chloride (as ferric trichloride, calcium chloride, sodium chloride, magnesium chloride or ammonium chloride etc.), and muriatic consumption is according to lead in the molybdenum concntrate, copper, calcium equal size and fixed.Heat treatment 1～2h in advance under 200～350 ℃ of conditions, this moment, impurity sulphide ore particle surface such as lead was " activated ", adopt the mixture of ferric trichloride, calcium chloride, ammonium chloride and hydrochloric acid again, the pH value is not more than 4,70～90 ℃ and leaches 1～2h down, lead can be reduced to 0.05% from 0.4%.Among the patent CA1029559, under 300～325 ℃, roasting 1～2h makes lead be converted into the solubility lead dichloride to Dentro.Dan.M with molybdenum concntrate and ammonium chloride, leaches deleading through hot water again.Although this technology is effective, need high-temperature roasting, contaminated environment, and consume a large amount of ammonium chlorides.
More than two kinds of wet methods plumbous technology is fallen, be that effectively but very high to the plumbous molybdenum concntrate production cost of height, the villaumite direct leaching will consume a large amount of hydrochloric acid to low plumbous (plumbous grade is less than 1%) molybdenum concntrate, operating environment is poor; Heat treatment afterchlorinate thing lixiviation process needs high-temperature roasting, and contaminated environment consumes a large amount of ammonium chlorides.
In sum, leaded high molybdenum ore is in floatation process, galena also is enriched in the molybdenum rough concentrate with molybdenite, because galena easily mill is frangible, the back major part of regrinding is enriched in (500 orders account for 85～90%) in-500 purpose grades, and granularity is superfine, and specific area is very big, adsorbing a considerable amount of remaining floating agents: as collecting agent-kerosene, diesel oil or steam wet goods, surfactant-pine camphor wet goods.Directly cause the ore pulp thickness, galena is difficult to suppress, molybdenite and galena separation difficulty, and molybdenum recovery is low.
Summary of the invention
Technical problem to be solved by this invention is at above-mentioned deficiency of the prior art, the flotation separation method of a kind of molybdenite and galena is provided, simple, the reasonable in design and good separating effect of its separating technology, can make plumbous content in the ore dressing process of molybdenum, strive reducing to minimum, when reducing molybdenum concntrate and smelting production cost, simplify production technology, effectively improve molybdenum recovery, also can thoroughly reduce plumbous pollution to environment.
For solving the problems of the technologies described above, the technical solution used in the present invention is: the flotation separation method of a kind of molybdenite and galena is characterized in that this method may further comprise the steps:
Step 1, corase grind: according to conventional FLOTATION SEPARATION corase grind technology, adopting ball mill is that raw ore is roughly ground to molybdenum ore, and mog accounts for 65～70% for-200 orders;
Step 2, roughly select and scan: adopt conventional molybdenum floating agent that the molybdenum ore after corase grind is roughly selected and scanned, obtain leaded molybdenum rough concentrate;
Step 3, regrind:, adopt ball mill that described leaded molybdenum rough concentrate is regrinded, and mog accounts for 80～90% for-400 orders according to conventional FLOTATION SEPARATION regrinding process;
Step 4, repeatedly selected: according to conventional dressing process, carry out selected to the leaded molybdenum rough concentrate after regrinding several times, all in described leaded molybdenum rough concentrate, add the galena inhibitor in each refining process earlier, in described leaded molybdenum rough concentrate, add the collecting agent and the foaming agent of molybdenite afterwards more as required; The total consumption that repeatedly adds the galena inhibitor in the refining process by 300～1200 gram/ton raw ores and the consumption of adding galena inhibitor reduce one by one; And repeatedly in the refining process, in described leaded molybdenum rough concentrate add the collecting agent of molybdenite and total consumption of foaming agent is respectively 10～30 gram/ton raw ores and 5～10 gram/ton raw ores.
Before the regrinding described in the above-mentioned steps three, in described leaded molybdenum rough concentrate, add granularity by 200 ± 50 purpose active carbons and the consumption of adding active carbon be 100～200 gram/ton raw ores.
Galena inhibitor described in the above-mentioned steps four is the phosphorus nox.
When collecting agent that adds molybdenite in described leaded molybdenum rough concentrate described in the above-mentioned steps four and foaming agent, the collecting agent of the molybdenite that is added and the consumption of foaming agent reduce one by one, and in the end do not add the collecting agent and the foaming agent of molybdenite in 1～4 time.
The leaded molybdenum rough concentrate to after regrinding described in the above-mentioned steps four carries out repeatedly when selected, and selected number of times is at least 7 times.
Raw ore described in the above-mentioned steps one is the molybdenum ore of leaded＞0.1wt%.
The present invention compared with prior art has the following advantages:
1, separating technology is simple and separation costs is low.
2, reasonable in design and good separating effect, when the FLOTATION SEPARATION wulfenite, specifically be when in ball mill, regrinding, add a certain amount of active carbon, one of its purpose is to make molybdenite and galena obtain abundant monomer dissociation, another purpose is the floating agent of the adsorbable galena particle surface absorption of active carbon in process of lapping, as collecting agent kerosene, foaming agent terpenic oil.After said process was handled, ore pulp viscosity declined to a great extent, and the remaining medicament of mineral surfaces significantly reduces, and the galena mineral produce unsalted surface, in brief, at first make the galena surface remove remaining floating agent with active carbon, produce unsalted surface.Afterwards, adopt the phosphorus nox that fresh galena surface is fully suppressed again, the collecting agent and the foaming agent that add an amount of molybdenite then, make fresh molybdenite surface absorption, thereby increased the floatability gap of molybdenite and galena, realized that molybdenite effectively separates with galena, and improved the rate of recovery of molybdenite.
3, practical value height, easily industrialization.
In sum, simple, the reasonable in design and good separating effect of separating technology of the present invention, it adopts reagent removal by active carbon and phosphorus nox to suppress plumbous integrated processes, molybdenite is effectively separated with galena, simultaneously help improving the rate of recovery of molybdenum again, can make plumbous content in the ore dressing process of molybdenum, strive reducing to minimum, when reducing molybdenum concntrate and smelting production cost, simplify production technology, effectively improve molybdenum recovery, also can thoroughly reduce plumbous pollution environment.
Below by drawings and Examples, technical scheme of the present invention is described in further detail.
Description of drawings
Fig. 1 is a flow chart of the present invention.
The specific embodiment
Embodiment 1
As shown in Figure 1, the flotation separation method of molybdenite of the present invention and galena may further comprise the steps:
Step 1, corase grind: according to conventional FLOTATION SEPARATION corase grind technology, adopting ball mill is that raw ore is roughly ground to molybdenum ore, and mog accounts for 65～70% for-200 orders.Before the corase grind, in described raw ore, add conventional molybdenum floating agent and acidity-basicity regulator as required.Described raw ore is the molybdenum ore of leaded＞0.1wt%.
In the present embodiment, described raw ore is to contain 25 kilograms of the molybdenum ore of molybdenum 0.082wt%, leaded 0.2wt% and quality.The conventional molybdenum floating agent that is added is a collecting agent, is specially kerosene; Described acidity-basicity regulator is a lime.Before the corase grind, in raw ore, add kerosene and lime and the consumption of the two respectively and be respectively 200 gram/ton raw ores (being to add 200g kerosene in the raw ore per ton) and 500 gram/ton raw ores (being to add 500g lime in the raw ore per ton); And mog accounts for 65～70% for-200 orders, and promptly corase grind back particle diameter accounts for 65～70% less than 200 purpose particles.
Step 2, roughly select and scan: adopt conventional molybdenum floating agent that the molybdenum ore after corase grind is roughly selected and scanned, obtain leaded molybdenum rough concentrate.
In the present embodiment, roughly select and scan in the process, the conventional molybdenum floating agent that is added is collecting agent and foaming agent, and collecting agent is specially kerosene and foaming agent is a terpenic oil, roughly selects and the time of scanning is respectively 5min and 4min.In the rougher process, add kerosene and terpenic oil consumption be respectively 54 gram/ton raw ores and 40 gram/ton raw ores.Scan in the process, add kerosene and terpenic oil consumption be respectively 45 gram/ton raw ores and 20 gram/ton raw ores.After roughly selecting and scanning, obtain to contain the rough concentrate about molybdenum 1.5～2.5wt%, leaded 4wt%.
Step 3, regrind: according to conventional FLOTATION SEPARATION regrinding process, adopt ball mill that described leaded molybdenum rough concentrate is regrinded, and the corase grind fineness accounts for 80～90% for-400 orders.In the present embodiment, time consuming is 25min again.
Step 4, repeatedly selected: according to conventional dressing process, carry out selected to the leaded molybdenum rough concentrate after regrinding several times, all in described leaded molybdenum rough concentrate, add the galena inhibitor in each refining process earlier, in described leaded molybdenum rough concentrate, add the collecting agent and the foaming agent of molybdenite afterwards more as required; The total consumption that repeatedly adds the galena inhibitor in the refining process by 300～1200 gram/ton raw ores and the consumption of adding galena inhibitor reduce one by one; And repeatedly in the refining process, in described leaded molybdenum rough concentrate add the collecting agent of molybdenite and total consumption of foaming agent is respectively 10～30 gram/ton raw ores and 5～10 gram/ton raw ores.Described galena inhibitor is the phosphorus nox.
In this step, several times the leaded molybdenum rough concentrate after regrinding is carried out when selected, selected number of times is at least 7 times.At least divide and carry out for 7 times, generally speaking, selected number of times is 7～12 times.Simultaneously, when adding the collecting agent of molybdenite and foaming agent in described leaded molybdenum rough concentrate, the collecting agent of the molybdenite that is added and the consumption of foaming agent reduce one by one, and in the end do not add the collecting agent and the foaming agent of molybdenite in 1～4 time; In addition, each time flotation time is that 1～10min and flotation time reduce one by one.Simultaneously, in the refining process, in described leaded molybdenum rough concentrate, add the gangue mineral inhibitor as required, be specially waterglass.
In the present embodiment, selected number of times is 8 times.First and third, five and seven time selected in, adding waterglass and consumption respectively is 200 gram/ton raw ores, 60 gram/ton raw ores, 60 gram/ton raw ores and 60 gram/ton raw ores.The total consumption that repeatedly adds the phosphorus nox in the refining process is 300 gram/ton raw ores.Described collecting agent and foaming agent are specially kerosene and terpenic oil, and repeatedly in the refining process add the collecting agent of molybdenite and total consumption of foaming agent is respectively 25.4 gram/ton raw ores and 8.7 gram/ton raw ores.In addition, the 6th, seven and eight time selected in, add and do not add kerosene and terpenic oil.
In the present embodiment, roughly grind, roughly select and scan, regrind and 8 each workshop sections such as selected in, the processing time of each workshop section and to add the consumption of kerosene, terpenic oil, waterglass and lime as shown in table 1:
Table 1 molybdenum plumbum floatation separation process parameters and regime of agent
In sum, through 8 times selected after, obtain molybdenum concntrate.
Embodiment 2
In the present embodiment, as different from Example 1: before the regrinding described in the step 3, in described leaded molybdenum rough concentrate, adding granularity is 100～200 gram/ton raw ores by the consumption of 200 ± 50 purpose active carbons and institute's adding active carbon, the consumption that specifically adds active carbon by 150 gram/ton raw ores and repeatedly in the refining process total consumption of adding phosphorus nox be 800 gram/ton raw ores.In the present embodiment, all the other separating steps are all identical with embodiment 1.
In addition, for relatively convenient, adopt a cover floatation separation process that raw ore is carried out FLOTATION SEPARATION, promptly do not add in step 3 and do not add galena inhibitor-phosphorus nox in active carbon and the step 4, all the other steps are all identical with embodiment 1.
Below, the molybdenum concntrate that embodiment 1, embodiment 2 are separated with above-mentioned conventional floatation separation process is that molybdenum plumbum floatation separating resulting compares, its comparative result is as shown in table 2:
Table 2 molybdenum plumbum floatation separating resulting
The above; it only is preferred embodiment of the present invention; be not that the present invention is imposed any restrictions, everyly any simple modification that above embodiment did, change and equivalent structure changed, all still belong in the protection domain of technical solution of the present invention according to the technology of the present invention essence.
Claims (6)
1. the flotation separation method of molybdenite and galena is characterized in that this method may further comprise the steps:
Step 1, corase grind: according to conventional FLOTATION SEPARATION corase grind technology, adopting ball mill is that raw ore is roughly ground to molybdenum ore, and mog accounts for 65～70% for-200 orders;
Step 2, roughly select and scan: adopt conventional molybdenum floating agent that the molybdenum ore after corase grind is roughly selected and scanned, obtain leaded molybdenum rough concentrate;
Step 3, regrind:, adopt ball mill that described leaded molybdenum rough concentrate is regrinded, and mog accounts for 80～90% for-400 orders according to conventional FLOTATION SEPARATION regrinding process;
Step 4, repeatedly selected: according to conventional dressing process, carry out selected to the leaded molybdenum rough concentrate after regrinding several times, all in described leaded molybdenum rough concentrate, add the galena inhibitor in each refining process earlier, in described leaded molybdenum rough concentrate, add the collecting agent and the foaming agent of molybdenite afterwards more as required; The total consumption that repeatedly adds the galena inhibitor in the refining process is 300～1200 gram/ton raw ores, and add the galena inhibitor consumption reduce one by one; And repeatedly in the refining process, in described leaded molybdenum rough concentrate add the collecting agent of molybdenite and total consumption of foaming agent is respectively 10～30 gram/ton raw ores and 5～10 gram/ton raw ores.
2. according to the flotation separation method of described a kind of molybdenite of claim 1 and galena, it is characterized in that: before the regrinding described in the step 3, in described leaded molybdenum rough concentrate, adding granularity is 200 ± 50 purpose active carbons, and add active carbon consumption be 100～200 gram/ton raw ores.
3. according to the flotation separation method of claim 1 or 2 described a kind of molybdenites and galena, it is characterized in that: the galena inhibitor described in the step 4 is the phosphorus nox.
4. according to the flotation separation method of claim 1 or 2 described a kind of molybdenites and galena, it is characterized in that: when collecting agent that in described leaded molybdenum rough concentrate, adds molybdenite described in the step 4 and foaming agent, the collecting agent of the molybdenite that is added and the consumption of foaming agent reduce one by one, and in the end do not add the collecting agent and the foaming agent of molybdenite in 1～4 time.
5. according to the flotation separation method of claim 1 or 2 described a kind of molybdenites and galena, it is characterized in that: the leaded molybdenum rough concentrate to after regrinding described in the step 4 carries out repeatedly when selected, and selected number of times is at least 7 times.
6. according to the flotation separation method of claim 1 or 2 described a kind of molybdenites and galena, it is characterized in that: the raw ore described in the step 1 is the molybdenum ore of leaded＞0.1wt%.
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| CN102266822A (en) * | 2011-07-13 | 2011-12-07 | 金堆城钼业股份有限公司 | Molybdenite flotation collector |
| CN102277481A (en) * | 2011-07-27 | 2011-12-14 | 西部鑫兴金属材料有限公司 | Method for reducing lead and protecting rhenium for high-lead rhenium and molybdenum containing concentrate |
| CN102732713A (en) * | 2012-06-26 | 2012-10-17 | 西部鑫兴金属材料有限公司 | Method for separating and recovering sediments after processing rhenium molybdenum concentrate-containing high lead |
| CN102773152A (en) * | 2012-07-13 | 2012-11-14 | 四川领航石墨制品有限公司 | Fine flaky-cryptocrystalline mixed graphite separation technique |
| CN103878069A (en) * | 2012-12-19 | 2014-06-25 | 沈阳有色金属研究院 | Molybdenite separation method |
| CN104941789A (en) * | 2015-06-26 | 2015-09-30 | 湖南有色金属研究院 | Beneficiation method for molybdenum-sulfur bulk concentrate |
| CN105149103A (en) * | 2015-08-21 | 2015-12-16 | 西北矿冶研究院 | Separation and beneficiation method for molybdenite and galena |
| CN105597945A (en) * | 2015-12-31 | 2016-05-25 | 金堆城钼业股份有限公司 | Process for separating molybdenum from lead in high-lead molybdenum ore |
| CN107042162A (en) * | 2017-04-06 | 2017-08-15 | 新疆紫金锌业有限公司 | A kind of beneficiation method of low-grade vulcanized lead ore deposit |
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| CN113333174A (en) * | 2021-05-13 | 2021-09-03 | 西北矿冶研究院 | Beneficiation reagent for flotation of tantalum and niobium in tantalum-niobium ore and preparation method thereof |
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102266822A (en) * | 2011-07-13 | 2011-12-07 | 金堆城钼业股份有限公司 | Molybdenite flotation collector |
| CN102277481A (en) * | 2011-07-27 | 2011-12-14 | 西部鑫兴金属材料有限公司 | Method for reducing lead and protecting rhenium for high-lead rhenium and molybdenum containing concentrate |
| CN102732713A (en) * | 2012-06-26 | 2012-10-17 | 西部鑫兴金属材料有限公司 | Method for separating and recovering sediments after processing rhenium molybdenum concentrate-containing high lead |
| CN102773152A (en) * | 2012-07-13 | 2012-11-14 | 四川领航石墨制品有限公司 | Fine flaky-cryptocrystalline mixed graphite separation technique |
| CN103878069A (en) * | 2012-12-19 | 2014-06-25 | 沈阳有色金属研究院 | Molybdenite separation method |
| CN104941789A (en) * | 2015-06-26 | 2015-09-30 | 湖南有色金属研究院 | Beneficiation method for molybdenum-sulfur bulk concentrate |
| CN105149103A (en) * | 2015-08-21 | 2015-12-16 | 西北矿冶研究院 | Separation and beneficiation method for molybdenite and galena |
| CN105597945A (en) * | 2015-12-31 | 2016-05-25 | 金堆城钼业股份有限公司 | Process for separating molybdenum from lead in high-lead molybdenum ore |
| CN107042162A (en) * | 2017-04-06 | 2017-08-15 | 新疆紫金锌业有限公司 | A kind of beneficiation method of low-grade vulcanized lead ore deposit |
| CN111841898A (en) * | 2020-07-17 | 2020-10-30 | 矿冶科技集团有限公司 | Combined inhibitor for refractory fine-grained molybdenum-lead bulk concentrate and application thereof |
| CN111841898B (en) * | 2020-07-17 | 2022-06-10 | 矿冶科技集团有限公司 | Combined inhibitor for refractory fine-grained molybdenum-lead bulk concentrate and application thereof |
| CN113333174A (en) * | 2021-05-13 | 2021-09-03 | 西北矿冶研究院 | Beneficiation reagent for flotation of tantalum and niobium in tantalum-niobium ore and preparation method thereof |
| CN113333174B (en) * | 2021-05-13 | 2022-05-31 | 西北矿冶研究院 | Beneficiation reagent for flotation of tantalum and niobium in tantalum-niobium ore and preparation method thereof |
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