LU602387B1 - Method for stepwise separation of magnesium from skarn-type copper-molybdenum ore with high talc content - Google Patents

Method for stepwise separation of magnesium from skarn-type copper-molybdenum ore with high talc content

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Publication number
LU602387B1
LU602387B1 LU602387A LU602387A LU602387B1 LU 602387 B1 LU602387 B1 LU 602387B1 LU 602387 A LU602387 A LU 602387A LU 602387 A LU602387 A LU 602387A LU 602387 B1 LU602387 B1 LU 602387B1
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Luxembourg
Prior art keywords
molybdenum
copper
separation
magnesium
concentrate
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LU602387A
Other languages
German (de)
Inventor
Feng Xie
Meihua Liu
Pengkun Zhang
Sen Yan
Ruoyu Yang
Chaoxing Liu
Xiangwen Lv
Dong Yang
Jing Zhang
Haijun Wu
Shuguang Zhang
Shaodong Wang
Sheng Jian
Lin Zhang
Xin Tang
Heguo Jiang
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Kunming Metallurgical Res Institute Co Ltd
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Publication of LU602387B1 publication Critical patent/LU602387B1/en

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/02—Froth-flotation processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/001—Flotation agents
    • B03D1/004—Organic compounds
    • B03D1/008—Organic compounds containing oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/001—Flotation agents
    • B03D1/004—Organic compounds
    • B03D1/012—Organic compounds containing sulfur
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/02—Froth-flotation processes
    • B03D1/028—Control and monitoring of flotation processes; computer models therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D2201/00—Specified effects produced by the flotation agents
    • B03D2201/02—Collectors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D2201/00—Specified effects produced by the flotation agents
    • B03D2201/06—Depressants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D2203/00—Specified materials treated by the flotation agents; Specified applications
    • B03D2203/02—Ores
    • B03D2203/04—Non-sulfide ores
    • 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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  • Engineering & Computer Science (AREA)
  • General Engineering & Computer Science (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

The present disclosure discloses a method for stepwise separation of magnesium from a skarn-type copper-molybdenum ore with a high talc content. The method for stepwise separation of magnesium from a skarn-type copper-molybdenum ore with a high talc content includes pre-treatment, first separation, second separation, grinding, third separation, and fourth separation. In the present disclosure, based on the different floatability and dissemination characteristics of easily-floatable layered magnesium silicate minerals such as talc, the floatability of talc is controlled in a stepwise manner during a technological process to avoid the loss of copper and molybdenum minerals caused by the traditional pre-flotation of talc and address the problems of high agent consumption and synchronous depression of targeted metals caused by the forced depression of highly-floatable talc in the traditional process, thereby achieving the efficient beneficiation for skarn-type copper-molybdenum ores with high talc contents.

Description

DESCRIPTION
LU602387
METHOD FOR STEPWISE SEPARATION OF MAGNESIUM FROM SKARN-TYPE
COPPER-MOLYBDENUM ORE WITH HIGH TALC CONTENT
TECHNICAL FIELD
The present disclosure belongs to the technical field of metallurgy, and specifically relates to a method for stepwise separation of magnesium from a skarn-type copper-molybdenum ore with a high talc content.
BACKGROUND TECHNOLOGY
Copper and molybdenum resources are widely used in military industry, electrical industry, metallurgy, aerospace, and other fields, and serve as irreplaceable strategic metal resources for the national economic development. Skarn-type copper ores and associated molybdenum resources are crucial raw material sources. However, due to unique metallogenic processes, skarn-type copper ores often exhibit complex ore characteristics, including easily-floatable magnesium silicate minerals such as talc and serpentine. Magnesium-bearing minerals are prone to sliming during grinding, but demonstrate similar floatability to molybdenite. The efficient flotation separation for talc-type copper-molybdenum ores is a technical problem to be solved urgently in the modern beneficiation.
In talc-type copper-molybdenum ores, the major metallic minerals include chalcopyrite, chalcocite, molybdenite, and pyrite, and the gangue minerals mainly include talc, serpentine, quartz, biotite, muscovite, chlorite, tremolite, hornblende, diopside, epidote, K-feldspar, plagioclase, etc. Talc, serpentine, and biotite have layered structures, and exhibit excellent natural floatability. During a grinding-flotation process, talc, serpentine, and biotite easily cause problems such as slime coating, mechanical entrainment, and competitive adsorption with agents, which bring many adverse effects to the recovery of copper minerals. In addition, since talc and molybdenite exhibit iso-floatabilty and the quantity of easily-floatable magnesium-bearing minerals is hundreds or even thousands of times the quantity of molybdenum minerals, the conventional separation efficiency is insufficient to achieve the efficient recovery of molybdenum minerals.
When molybdenum primarily exists as the associated metal, it is almost impossible to separate an individual molybdenum concentrate product. Currently, in mines 994397 talc-bearing molybdenum ores are typically treated by the conventional beneficiation process such as "preliminary magnesium removal from raw ore + magnesium depression and molybdenum flotation" and "whole-pulp magnesium depression and molybdenum flotation of raw ore." These processes are mainly used to treat single raw molybdenum ores with relatively-high molybdenum grades. The preliminary removal of magnesium and the depression of magnesium inevitably lead to the premature loss and synchronous depression for molybdenum, resulting in low recovery efficiency of molybdenum. When copper serves as the primary metal and molybdenum serves as the associated metal, to guarantee the quality of a copper concentrate, a strong depressant such as sodium carboxymethyl cellulose is typically adopted during production to intensely interfere with talc. However, during this process, molybdenum minerals are synchronously depressed and thus can hardly be recovered, and the recovery efficiency of copper is also adversely affected. Therefore, the traditional beneficiation processes are not suitable for treating copper ores characterized by high talc contents and associated molybdenum, and exhibit some limitations. Therefore, it is very necessary to develop a method for solving the above problems.
CONTENT OF THE INVENTION
An objective of the present disclosure is to provide a method for stepwise separation of magnesium from a skarn-type copper-molybdenum ore with a high talc content.
The objective of the present disclosure is achieved as follows: The method for stepwise separation of magnesium from a skarn-type copper-molybdenum ore with a high talc content includes pre-treatment, first separation, second separation, grinding, third separation, and fourth separation, and specifically includes:
A, the pre-treatment. adding a lime to a crushed skarn-type copper-molybdenum ore with a high talc content, and grinding until 50% to 60% of resulting particles have a particle size of less than 74 um to produce a material a;
B, the first separation: adding a copper-molybdenum collector and a first frother all at once to the material a, and conducting roughing once to produce a 602987 copper-molybdenum mixed rougher concentrate b and a copper-molybdenum mixed rougher tailing c; and adding the copper-molybdenum collector and the first frother to the copper-molybdenum mixed rougher tailing c, and conducting scavenging twice, where froths from the scavenging are returned step by step;
C, the second separation: adding the lime, a talc depressant, and the copper-molybdenum collector successively to the copper-molybdenum mixed rougher concentrate b, and conducting cleaning to produce a copper-molybdenum mixed cleaner concentrate d and a copper-molybdenum mixed cleaner tailing e; adding the copper-molybdenum collector to the copper-molybdenum mixed cleaner tailing e, and conducting cleaner scavenging to produce a copper-molybdenum mixed cleaner scavenger concentrate f and a tailing g; and returning the copper-molybdenum mixed cleaner scavenger concentrate f to the cleaning, where the tailing g is a final tailing 2;
D, the grinding: adding the lime and the talc depressant successively to the copper-molybdenum mixed cleaner tailing e, and grinding until 80% to 90% of resulting particles have a particle size of less than 74 um to produce a material h;
E, the third separation: adding the copper-molybdenum collector and the first frother successively to the material h, and conducting first cleaning and second cleaning and cleaner scavenging once to produce a copper-molybdenum concentrate i; and
F, the fourth separation: subjecting the copper-molybdenum concentrate i to agent removal, copper-molybdenum/magnesium separation, high-grade molybdenum-magnesium separation, and low-grade molybdenum-magnesium separation to produce a low-grade molybdenum concentrate product, where the fourth separation is specifically as follows: 1) the agent removal: adding clean water to the copper-molybdenum concentrate |, conducting cleaning, and concentrating for the agent removal to produce a material j; 2) the copper-molybdenum/magnesium separation: adding a copper depressant, a neutral oil, and the first frother successively to the material j, and conducting roughing, scavenging once, and first cleaning and second cleaning sequentially, where intermediates are returned step by step, a tailing from the scavenging is a final copper concentrate product, and a froth from the second cleaning is a crude molybdenum-magnesium concentrate product k;
3) the high-grade molybdenum-magnesium separation: adding a molybdenum depressant, the neutral oil, and a second frother successively to the crude 1006987 molybdenum-magnesium concentrate product k, and conducting roughing to produce a high-grade molybdenum-magnesium separation rougher concentrate | and a high-grade molybdenum-magnesium separation rougher tailing m; adding a molybdenum depressant, the neutral oil, and the second frother successively to the high-grade molybdenum-magnesium separation rougher tailing m, and conducting scavenging to produce a high-grade molybdenum-magnesium separation scavenger concentrate n and a high-grade molybdenum-magnesium separation scavenger tailing; and returning the high-grade molybdenum-magnesium separation scavenger concentrate n to the high-grade molybdenum-magnesium separation roughing step, where the high-grade molybdenum-magnesium separation scavenger tailing is a final high-grade molybdenum concentrate product o; and 4) the low-grade molybdenum-magnesium separation: adding a molybdenum depressant and the second frother successively to the high-grade molybdenum-magnesium separation rougher concentrate |, and conducting roughing, scavenging once, and cleaning once sequentially, where intermediates are returned step by step, a froth from the cleaning is talc, and a tailing from the scavenging is the low-grade molybdenum concentrate product.
The method includes the following specific steps:
A, first grinding: adding a lime to a crushed ore, and conducting the first grinding until 50% to 60% of resulting particles have a particle size of less than 74 um;
B, copper-molybdenum mixed roughing, namely, first separation of copper and molybdenum from talc: adding the copper-molybdenum collector and the first frother successively to a slurry obtained in the step A, and conducting roughing and scavenging twice, where froths from the scavenging are returned step by step;
C, cleaning, namely, second separation of copper and molybdenum from talc: adding the lime, a talc depressant, and the copper-molybdenum collector to a froth product obtained in the step B, and conducting mixed cleaning once and mixed cleaner scavenging once, where a froth from the mixed cleaner scavenging is returned to the mixed cleaning step;
D, second grinding: adding the lime and the talc depressant successively to a froth product obtained in the step C, and conducting the second grinding until 80% to 90% of resulting particles have a particle size of less than 74 um;
E, cleaning, namely, third separation of copper and molybdenum from talc: adding the copper-molybdenum collector and the first frother successively to a slurry obtained 1006987 in the step D, and conducting first cleaning and second cleaning and cleaner scavenging, where a lime is added to a froth from the first cleaning, and then the second cleaning is conducted; a tailing from the cleaner scavenging is returned to the step C; and intermediates are returned step by step);
F, agent removal before cleaner separation of copper, molybdenum, and magnesium: adding clean water to a froth product obtained in the step E, and concentrating to produce a concentrate with a concentration of 50% to 60% and overflow water; recycling the overflow water for an upstream operation; and feeding the concentrate into a stirring mill, and scrubbing to produce a product in which 80% to 85% of resulting particles have a particle size of less than 45 um;
G, copper-molybdenum/magnesium separation: adding a copper depressant, the neutral oil, and the first frother successively to the product obtained in the step F, and conducting roughing once, scavenging once, and first cleaning and second cleaning, where intermediates are returned step by step, a tailing from the scavenging is a final copper concentrate product, and a froth from the second cleaning is a crude molybdenum-magnesium concentrate product;
H, high-grade molybdenum-magnesium separation: adding a molybdenum depressant, the neutral oil, and a second frother successively to the crude molybdenum-magnesium concentrate product obtained in the step G, and conducting roughing once and scavenging once, where a tailing from the scavenging is a final high-grade molybdenum concentrate product; and
I, low-grade molybdenum-magnesium separation: adding a molybdenum depressant and the second frother successively to a rougher froth obtained in the step
H, and conducting roughing once, scavenging once, and cleaning once, where intermediates are returned step by step, a froth from the cleaning is talc, and a tailing from the scavenging is a final low-grade molybdenum concentrate product. The steps F,
G, H, and | are four stages of separation of copper and molybdenum from talc, respectively.
Further, in the step A, the first grinding is conducted under the following process conditions: the lime is added at 1,000 g/t to 1500 g/t, a pH of a slurry is 9.0 to 9.5, and the first grinding is conducted until 50% to 60% of resulting particles have a particle size of less than 74 um.
Further, in the step B, during the copper-molybdenum mixed roughing, namely, the first separation of copper and molybdenum from talc: The roughing is conducted under 992987 the following process conditions: the copper-molybdenum collector is added at 20 g/t to 30 g/t, and then stirring is conducted for 2 min to 3 min; and the first frother is added at g/t to 25 g/t, and then stirring is conducted for 2 min to 3 min. First scavenging is conducted under the following process conditions: the copper-molybdenum collector is added at 8 g/t to 12 git, and then stirring is conducted for 2 min to 3 min; and the first frother is added at 5 g/t to 8 g/t, and then stirring is conducted for 2 min to 3 min.
Second scavenging is conducted under the following process conditions: the copper-molybdenum collector is added at 4 g/t to 6 g/t, and then stirring is conducted for 2 min to 3 min; and the first frother is added at 2 g/t to 4 g/t, and then stirring is conducted for 2 min to 3 min.
Further, in the step C, during the cleaning, namely, the second separation of copper and molybdenum from talc. The mixed cleaning is conducted under the following process conditions: the lime is added at 200 g/t to 400 g/t, and then stirring is conducted for 3 min to 5 min; the talc depressant is added at 50 g/t to 100 g/t, and then stirring is conducted for 3 min to 5 min; and the copper-molybdenum collector is added at 4 g/t to 6 g/t, and then stirring is conducted for 2 min to 3 min. The mixed cleaner scavenging is conducted under the following process conditions: the copper-molybdenum collector is added at 2 g/t to 3 g/t, and then stirring is conducted for 2 min to 3 min.
Further, in the step D, the second grinding is conducted under the following process conditions: the lime is added at 100 g/t to 200 g/t, the talc depressant is added at 10 g/t to 30 g/t, and the second grinding is conducted until 80% to 90% of resulting particles have a particle size of less than 74 um.
Further, in the step E, during the cleaning, namely, the third separation of copper and molybdenum from talc: The first cleaning is conducted under the following process conditions: the copper-molybdenum collector is added at 2 g/t to 3 g/t, and then stirring is conducted for 2 min to 3 min; and the first frother is added at 1 g/t to 3 g/t, and then stirring is conducted for 2 min to 3 min. The second cleaning is conducted under the following process conditions: the lime is added at 50 g/t to 100 g/t, and then stirring is conducted for 3 min to 5 min. The cleaner scavenging is conducted under the following process conditions: the copper-molybdenum collector is added at 1 g/t to 2 g/t, and then stirring is conducted for 2 min to 3 min; and the first frother is added at 1 g/t to 2 g/t, and then stirring is conducted for 2 min to 3 min.
Further, in the step G, during the copper-molybdenum/magnesium separation: The roughing is conducted under the following process conditions: the copper depressant is 092987 added at 200 g/t to 400 g/t, and then stirring is conducted for 3 min to 5 min; the neutral oil is added at 2 g/t to 3 g/t, and then stirring is conducted for 2 min to 3 min; and the first frother is added at 1 g/t to 2 g/t, and then stirring is conducted for 2 min to 3 min.
The scavenging is conducted under the following process conditions: the copper depressant is added at 50 g/t to 100 g/t, and then stirring is conducted for 3 min to 5 min; the neutral oil is added at 1 g/t to 2 g/t, and then stirring is conducted for 2 min to 3 min; and the first frother is added at 1 g/t to 2 g/t, and then stirring is conducted for 2 min to 3 min. First cleaning is conducted under the following process conditions: the copper depressant is added at 50 g/t to 80 g/t, and then stirring is conducted for 3 min to 5 min; and the first frother is added at 1 g/t to 2 g/t, and then stirring is conducted for 2 min to 3 min. The second cleaning is conducted under the following process conditions: the copper depressant is added at 20 g/t to 30 g/t, and then stirring is conducted for 3 min to 5 min.
Further, in the step H, during the high-grade molybdenum-magnesium separation:
The roughing is conducted under the following process conditions: the molybdenum depressant is added at 10 g/t to 15 g/t, and then stirring is conducted for 3 min to 5 min; the neutral oil is added at 3 g/t to 5 g/t, and then stirring is conducted for 2 min to 3 min; and the second frother is added at 5 g/t to 8 g/t, and then stirring is conducted for 2 min to 3 min. The scavenging is conducted under the following process conditions: the molybdenum depressant is added at 5 g/t to 10 g/t, and then stirring is conducted for 3 min to 5 min; the neutral oil is added at 2 g/t to 4 g/t, and then stirring is conducted for 2 min to 3 min; and the second frother is added at 3 g/t to 6 g/t, and then stirring is conducted for 2 min to 3 min.
Further, in the step |, during the low-grade molybdenum-magnesium separation:
The roughing is conducted under the following process conditions: the molybdenum depressant is added at 5 g/t to 10 g/t, and then stirring is conducted for 3 min to 5 min; and the second frother is added at 3 g/t to 6 g/t, and then stirring is conducted for 2 min to 3 min. The scavenging is conducted under the following process conditions: the molybdenum depressant is added at 3 g/t to 6 g/t, and then stirring is conducted for 3 min to 5 min; and the second frother is added at 2 g/t to 4 g/t, and then stirring is conducted for 2 min to 3 min.
The cleaning is conducted under the following process conditions: the molybdenum depressant is added at 3 g/t to 6 g/t, and then stirring is conducted for 3 min to 5 min: 992587 and the second frother is added at 2 g/t to 4 g/t, and then stirring is conducted for 2 min to 3 min.
Further, the copper-molybdenum collector in the steps B, C, and E is TF1#.
Further, the first frother in the steps B, E, and G is methyl isobutyl carbinol.
Further, the talc depressant in the steps C and D is a fructan.
Further, the copper depressant in the step G is one or two of sodium sulfide or sodium hydrosulfide.
Further, the neutral oil in the steps G, H, and | is one or two of emulsions of kerosene and diesel.
Further, the second frother in the steps H and | is propylene glycol ether alcohol.
Further, the molybdenum depressant in the steps H and | is TD-3.
Further, a main component of the copper-molybdenum collector TF1# in the steps
B, C, and E is a mixture of isopropylthiourea, ethylene glycol chloroformate, and pyridine, including 30% to 50% of the isopropylthiourea, 40% to 50% of the ethylene glycol chloroformate, and 5% to 10% of the pyridine.
Further, a main component of each of the molybdenum depressants TD-3 in the steps H and | is a mixture of dextrin, sodium cellulose xanthate, and octylphenol ethoxylate, including 30% to 40% of the dextrin, 40% to 60% of the sodium cellulose xanthate, and 5% to 10% of the octylphenol ethoxylate.
Compared with the prior art, the present disclosure has the following advantages: 1. During the copper-molybdenum mixed flotation process of the present disclosure, no talc depressant is added, and only the copper-molybdenum collector TF1# with relatively weak collection performance for pyrite and talc is adopted instead, which promotes the early separation of copper-molybdenum from a part of talc and a large amount of pyrite. The early separation can alleviate the depression burden of talc and pyrite subsequently, and can also avoid the losses of copper and molybdenum minerals caused by the overuse of a talc depressant and a lime while reducing the consumption of depressants. 2. In the present disclosure, a flotation desliming process is added before a regrinding operation, and a selective talc depressant with mild depression performance is adopted to control the flotation of talc.
As a result, the regrinding capacity can be reduced, and the problems such as slime coating, mechanical entrainment, and competitive adsorption with agents during a 7902987 cleaning process caused by the sliming of talc and other magnesium-bearing gangue in large quantities can be avoided.
Moreover, the moderately-floatable coarse-grained talc with sufficient liberation can be fully intercepted.
3. In the present disclosure, after the regrinding, the newly-liberated fine-grained talc with medium floatability is selectively depressed to achieve the maximum interception of whole-grained moderately-floatable magnesium-bearing gangue such as talc before the separation of target minerals.
Consequently, the later reverse flotation separation of talc is guaranteed, and it is fully adaptable to the complex dissemination characteristics of talc and other magnesium-bearing gangue minerals.
4. During the copper-molybdenum mixed flotation process of the present disclosure, the selective collection and depression is adopted.
Compared with the traditional "forced promotion-forced depression" xanthate agent system, the selective collection and depression is conducive to the removal of adsorption agents before the separation of a copper-molybdenum-magnesium mixed concentrate, reduces the separation difficulty, and involves a relatively-short copper separation process.
5. In the present disclosure, before the separation of copper, molybdenum, and magnesium, a weak depression flotation environment is created to avoid the premature loss of copper minerals and increase the probability of copper minerals with complex dissemination characteristics to enter the grinding and scrubbing operation, thereby improving the recovery efficiency of copper.
Moreover, the full separation of copper minerals from magnesium-bearing minerals (such as talc and fluorine-containing mica) is significantly advantageous for enhancing the copper grade of a copper concentrate and reducing the harmful impurities such as magnesium and fluorine, which enables the acquisition of a high-quality copper concentrate.
6. In the present disclosure, the floatability of talc is screened through an early process to control the separation of magnesium-bearing gangue minerals with the optimal floatability such as talc within a later copper/molybdenum/magnesium separation process, which facilitates the cleaner separation of talc from copper and molybdenum metallic minerals.
7. In the present disclosure, TD-1# is employed to depress molybdenite, two molybdenum concentrate outlets are arranged, and the amount of TD-1# is controlled to allow the stepwise depression of molybdenum and the reverse flotation for magnesium removal.
Thus, the mechanical entrainment caused by "depression of the less and flotation of the more" (less molybdenite and more talc) is avoided. In addition, the recovery 992387 efficiency of molybdenum is maximized, and the partially locked molybdenum is separated from the fully liberated molybdenum to achieve the quality control for a molybdenum concentrate based on a grade. 8. The agents adopted in the present disclosure all are conventional flotation agents, which are eco-friendly. 9. In the present disclosure, based on the different floatability and dissemination characteristics of easily-floatable layered magnesium silicate minerals such as talc, the floatability of talc is controlled in a stepwise manner during a technological process to avoid the loss of copper and molybdenum minerals caused by the traditional pre-flotation of talc and address the problems of high agent consumption and synchronous depression of targeted metals caused by the forced depression of highly-floatable talc in the traditional process, thereby achieving the efficient beneficiation for skarn-type copper-molybdenum ores with high talc contents.
DESCRIPTION OF THE DRAWING
FIG. 1 is a schematic flow chart of the method of the present disclosure.
SPECIFIC IMPLEMENTATIONS
The present disclosure is further described below in conjunction with embodiments, but is not limited thereto in any way. The embodiments of the present disclosure are merely descriptions of the preferred experimental methods of the present disclosure, and do not limit the concept and scope of the present disclosure. Any variation and improvement made based on the teachings of the present disclosure without departing from the design spirit of the present disclosure shall fall within the protection scope of the present disclosure.
The present disclosure provides a method for stepwise separation of magnesium from a skarn-type copper-molybdenum ore with a high talc content, including pre-treatment, first separation, second separation, grinding, third separation, and fourth separation, and specifically including:
A. Pre-treatment: A lime is added to a crushed skarn-type copper-molybdenum ore with a high talc content, and grinding is conducted until 50% to 60% of resulting‘ 095987 particles have a particle size of less than 74 um to produce a material a.
B. First separation: A copper-molybdenum collector and a first frother are added all at once to the material a, and roughing is conducted once to produce a copper-molybdenum mixed rougher concentrate b and a copper-molybdenum mixed rougher tailing c. The copper-molybdenum collector and the first frother are added to the copper-molybdenum mixed rougher tailing c, and scavenging is conducted twice.
Froths from the scavenging are returned step by step.
C. Second separation: The lime, a talc depressant, and the copper-molybdenum collector are added successively to the copper-molybdenum mixed rougher concentrate b, and cleaning is conducted to produce a copper-molybdenum mixed cleaner concentrate d and a copper-molybdenum mixed cleaner tailing e. The copper-molybdenum collector is added to the copper-molybdenum mixed cleaner tailing e, and cleaner scavenging is conducted to produce a copper-molybdenum mixed cleaner scavenger concentrate f and a tailing g. The copper-molybdenum mixed cleaner scavenger concentrate f is returned to the cleaning. The tailing g is a final tailing 2.
D. Grinding: The lime and the talc depressant are added successively to the copper-molybdenum mixed cleaner tailing e, and grinding is conducted until 80% to 90% of resulting particles have a particle size of less than 74 um to produce a material h.
E. Third separation: The copper-molybdenum collector and the first frother are added successively to the material h, and two times of cleaning and cleaner scavenging are conducted to produce a copper-molybdenum concentrate i.
F. Fourth separation: The copper-molybdenum concentrate i is subjected to agent removal, copper-molybdenum/magnesium separation, high-grade molybdenum-magnesium separation, and low-grade molybdenum-magnesium separation to produce a low-grade molybdenum concentrate product.
The fourth separation is specifically as follows: 1) Agent removal: Clean water is added to the copper-molybdenum concentrate |, cleaning is allowed, and concentration is conducted for the agent removal to produce a material |.
2) Copper-molybdenum/magnesium separation: A copper depressant, a neutral oil, and the first frother are added successively to the material j, and roughing, scavenging. 994987 and two times of cleaning are conducted sequentially. Intermediates are returned step by step, a tailing from the scavenging is a final copper concentrate product, and a froth from the second cleaning is a crude molybdenum-magnesium concentrate product k. 3) High-grade molybdenum-magnesium separation: A molybdenum depressant, the neutral oil, and a second frother are added successively to the crude molybdenum-magnesium concentrate product k, and roughing is conducted to produce a high-grade molybdenum-magnesium separation rougher concentrate | and a high-grade molybdenum-magnesium separation rougher tailing m. A molybdenum depressant, the neutral oil, and the second frother are added successively to the high-grade molybdenum-magnesium separation rougher tailing m, and scavenging is conducted to produce a high-grade molybdenum-magnesium separation scavenger concentrate n and a high-grade molybdenum-magnesium separation scavenger tailing.
The high-grade molybdenum-magnesium separation scavenger concentrate n is returned to the high-grade molybdenum-magnesium separation roughing step. The high-grade molybdenum-magnesium separation scavenger tailing is a final high-grade molybdenum concentrate product o. 4) Low-grade molybdenum-magnesium separation: A molybdenum depressant and the second frother are added successively to the high-grade molybdenum-magnesium separation rougher concentrate |, and roughing, scavenging, and cleaning are conducted sequentially. Intermediates are returned step by step, a froth from the cleaning is talc, and a tailing from the scavenging is the final low-grade molybdenum concentrate product.
The two times of scavenging in the step B are conducted as follows: The copper-molybdenum collector and the first frother are added to the copper-molybdenum mixed rougher tailing c, and first scavenging is conducted to produce a copper-molybdenum mixed first-scavenger concentrate and a copper-molybdenum mixed first-scavenger tailing. The copper-molybdenum mixed first-scavenger concentrate is returned to the copper-molybdenum mixed roughing step. The copper-molybdenum collector and the first frother are added to the copper-molybdenum mixed first-scavenger tailing, and second scavenging is conducted to produce a copper-molybdenum mixed second-scavenger concentrate and a final tailing 1. The copper-molybdenum mixed second-scavenger concentrate is returned to the first scavenging.
The two times of cleaning and the cleaner scavenging in the step E are conducted as follows: The copper-molybdenum collector and the first frother are added to the 1006987 material h, and first cleaning is conducted to produce a first copper-molybdenum cleaner concentrate and a first copper-molybdenum cleaner tailing. À lime is added to the first copper-molybdenum cleaner concentrate, and second cleaning is conducted to produce the copper-molybdenum concentrate i and a second copper-molybdenum cleaner tailing. The copper-molybdenum collector and the first frother are added to the first copper-molybdenum cleaner tailing, and the cleaner scavenging is conducted to produce a copper-molybdenum cleaner scavenger concentrate and a copper-molybdenum cleaner scavenger tailing. The copper-molybdenum cleaner scavenger tailing is returned to the cleaning. The copper-molybdenum cleaner scavenger concentrate and the second copper-molybdenum cleaner tailing are combined and returned to the first cleaning.
The copper-molybdenum collector in the steps B, C, and E includes isopropylthiourea, ethylene glycol chloroformate, and pyridine.
The isopropylthiourea, the ethylene glycol chloroformate, and the pyridine are in a mass ratio of (2-6):(3-6):(0.3-1.2).
The molybdenum depressant in the step F includes dextrin, sodium cellulose xanthate, and octylphenol ethoxylate.
The dextrin, the sodium cellulose xanthate, and the octylphenol ethoxylate are in a mass ratio of (2-5):(3-7):(0.3-1.2).
The first frother in the step B, the step E, and the step 2) of F is methyl isobutyl carbinol, and the second frother in the step 3) of F and the step 4) of F is propylene glycol ether alcohol.
The talc depressant is a fructan.
The copper depressant is sodium sulfide and/or sodium hydrosulfide, and the neutral oil is an emulsion of kerosene and/or diesel.
The present disclosure is further described below with reference to specific examples.
Example 1
An ore sample from a concentrator in Henan province, China was adopted. The ore sample had a copper content of 0.49%, a molybdenum content of 0.028%, a magnesium oxide content of 13.21%, and an iron content of 12.42%. In the ore sample, the major metallic minerals were chalcopyrite, covellite, molybdenite, and pyrite, and the main easily-floatable magnesium silicate minerals were talc and serpentine.
The ore sample was treated through the following process steps:
A. First grinding: A lime was added at 1,200 g/t to a crushed ore, and the first 200 grinding was conducted until 60% of resulting particles had a particle size of less than 74 um.
B. Copper-molybdenum mixed roughing, namely, first separation of copper and molybdenum from talc: A slurry obtained in the step A was subjected to roughing once and scavenging twice. The roughing was conducted under the following process conditions: a copper-molybdenum collector TF1# was added at 30 g/t, and then stirring was conducted for 3 min. A frother methyl isobutyl carbinol was added at 20 g/t, and then stirring was conducted for 3 min. First scavenging was conducted under the following process conditions: The copper-molybdenum collector TF1# was added at 10 g/t, and then stirring was conducted for 3 min. The frother methyl isobutyl carbinol was added at 6 g/t, and then stirring was conducted for 3 min. Second scavenging was conducted under the following process conditions: The copper-molybdenum collector
TF1# was added at 5 g/t, and then stirring was conducted for 3 min. The frother methyl isobutyl carbinol was added at 3 g/t, and then stirring was conducted for 3 min.
C. Copper-molybdenum mixed cleaning, namely, second separation of copper and molybdenum from talc: A froth product obtained in the step B was subjected to mixed cleaning once and mixed cleaner scavenging once. The cleaning was conducted under the following process conditions: A lime was added at 400 g/t, and then stirring was conducted for 4 min. A fructan as a talc depressant was added at 100 g/t, and then stirring was conducted for 5 min. TF1# was added at 5 g/t, and then stirring was conducted for 3 min. The mixed cleaner scavenging was conducted under the following process conditions: The copper-molybdenum collector TF1# was added at 3 g/t, and then stirring was conducted for 3 min.
D. Second grinding: À lime at 150 g/t and a fructan as a talc depressant at 20 g/t were added successively to a froth product obtained in the step C, and the second grinding was conducted until 85% of resulting particles had a particle size of less than 74 um.
E. Cleaning, namely, third separation of copper and molybdenum from talc: À slurry obtained in the step D was subjected to first cleaning and second cleaning and cleaner scavenging. First cleaning was conducted under the following process conditions: A copper-molybdenum collector TF1# was added at 2 g/t, and then stirring was conducted for 3 min. A frother methyl isobutyl carbinol was added at 2 g/t, and then stirring was conducted for 3 min.
Second cleaning was conducted under the following process conditions: A lime was added at 100 g/t, and then stirring was conducted for 4 min. The cleaner scavenging 994587 was conducted under the following process conditions: The copper-molybdenum collector TF1# was added at 2 g/t, and then stirring was conducted for 3 min. The frother methyl isobutyl carbinol was added at 2 g/t, and then stirring was conducted for 3 min.
F. Agent removal before cleaner separation of copper, molybdenum, and magnesium: Clean water was added to a froth product obtained in the step E, cleaning was allowed, and concentration was conducted to produce a concentrate with a concentration of 55% and overflow water. The overflow water was recycled for an upstream operation. The concentrate was fed into a stirring mill, and scrubbed to produce a product in which 85% of resulting particles had a particle size of less than 45 pm.
G. Copper-molybdenum/magnesium separation: The product obtained in the step F was subjected to roughing, scavenging, and first cleaning and second cleaning. The roughing was conducted under the following process conditions: Sodium sulfide was added at 350 g/t, and then stirring was conducted for 5 min. Emulsified kerosene was added at 2 g/t, and then stirring was conducted for 2 min. A frother methyl isobutyl carbinol was added at 2 g/t, and then stirring was conducted for 2 min. The scavenging was conducted under the following process conditions: The sodium sulfide was added at 80 g/t, and then stirring was conducted for 5 min. The emulsified kerosene was added at 1 g/t, and then stirring was conducted for 2. The frother methyl isobutyl carbinol was added at 1 g/t, and then stirring was conducted for 2 min. First cleaning was conducted under the following process conditions: The sodium sulfide was added at 60 g/t, and then stirring was conducted for 2 min. The frother methyl isobutyl carbinol was added at 1 g/t, and then stirring was conducted for 2 min. The second cleaning was conducted under the following process conditions: The sodium sulfide was added at 30 g/t, and then stirring was conducted for 5 min. Intermediates were returned step by step, a tailing from the scavenging was a final copper concentrate product, and a froth from the second cleaning was a crude molybdenum-magnesium concentrate product.
H. High-grade molybdenum-magnesium separation: The crude molybdenum-magnesium concentrate product obtained in the step G was subjected to roughing once and scavenging once. The roughing was conducted under the following process conditions: A molybdenum depressant TD-3 was added at 15 g/t, and then stirring was conducted for 3 min.
Emulsified kerosene was added at 5 g/t, and then stirring was conducted for 2 min.
A frother propylene glycol ether alcohol was added at 5 g/t, and then stirring was 1006987 conducted for 2 min. The scavenging was conducted under the following process conditions: The molybdenum depressant TD-3 was added at 10 g/t, and then stirring was conducted for 3 min. The emulsified kerosene was added at 2 g/t, and then stirring was conducted for 2 min. The frother propylene glycol ether alcohol was added at 3 g/t, and then stirring was conducted for 2 min. A tailing from the scavenging was a final high-grade molybdenum concentrate product. . Low-grade molybdenum-magnesium separation: A rougher froth obtained in the step H was subjected to roughing once, scavenging once, and cleaning once. The roughing was conducted under the following process conditions: A molybdenum depressant TD-3 was added at 8 g/t, and then stirring was conducted for 3 min. A frother propylene glycol ether alcohol was added at 5 g/t, and then stirring was conducted for 2 min. The scavenging was conducted under the following process conditions: The molybdenum depressant TD-3 was added at 6 g/t, and then stirring was conducted for 3 min. The frother propylene glycol ether alcohol was added at 3 g/t, and then stirring was conducted for 2 min to 3 min. The cleaning was conducted under the following process conditions: The molybdenum depressant TD-3 was added at 4 git, and then stirring was conducted for 3 min. The frother propylene glycol ether alcohol was added at 2 g/t, and then stirring was conducted for 2 min. Intermediates were returned step by step, a froth from the cleaning was talc, and a tailing from the scavenging was a final low-grade molybdenum concentrate product.
When the ore was treated by the above process, a copper concentrate with a Cu grade of 26.19% and a Cu recovery rate of 86.54%, a high-grade molybdenum concentrate with a Mo grade of 45.37% and a Mo recovery rate of 65.24%, and a low-grade molybdenum concentrate with a Mo grade of 22.33% and a Mo recovery rate of 11.24% could be produced. It can be seen that the process can improve the comprehensive utilization of difficult-to-select mineral resources.
Example 2
An ore sample from a concentrator in Yunnan province, China was adopted. The 7994987 ore sample had a copper content of 0.56%, a molybdenum content of 0.018%, a magnesium oxide content of 10.49%, and an iron content of 14.12%. In the ore sample, the major metallic minerals were chalcopyrite, molybdenite, and pyrite, and the main easily-floatable magnesium silicate mineral was talc. The ore sample was treated through the following process steps:
A. First grinding: A lime was added at 1500 g/t to a crushed ore, and the first grinding was conducted until 55% of resulting particles had a particle size of less than 74 um.
B. Copper-molybdenum mixed roughing, namely, first separation of copper and molybdenum from talc: A slurry obtained in the step A was subjected to roughing once and scavenging twice. The roughing was conducted under the following process conditions: a copper-molybdenum collector TF1# was added at 30 g/t, and then stirring was conducted for 3 min. A frother methyl isobutyl carbinol was added at 25 g/t, and then stirring was conducted for 3 min. First scavenging was conducted under the following process conditions: The copper-molybdenum collector TF1# was added at 12 g/t, and then stirring was conducted for 3 min. The frother methyl isobutyl carbinol was added at 8 g/t, and then stirring was conducted for 3 min. Second scavenging was conducted under the following process conditions: The copper-molybdenum collector
TF1# was added at 6 g/t, and then stirring was conducted for 3 min. The frother methyl isobutyl carbinol was added at 4 g/t, and then stirring was conducted for 3 min.
C. Copper-molybdenum mixed cleaning, namely, second separation of copper and molybdenum from talc: À froth product obtained in the step B was subjected to mixed cleaning once and mixed cleaner scavenging once. The cleaning was conducted under the following process conditions: À lime was added at 400 g/t, and then stirring was conducted for 4 min. À fructan as a talc depressant was added at 80 g/t, and then stirring was conducted for 5 min. TF1# was added at 5 g/t, and then stirring was conducted for 3 min. The mixed cleaner scavenging was conducted under the following process conditions: The copper-molybdenum collector TF1# was added at 3 g/t, and then stirring was conducted for 3 min.
D. Second grinding: À lime at 200 g/t and a fructan as a talc depressant at 15 g/t were added successively to a froth product obtained in the step C, and the second grinding was conducted until 90% of resulting particles had a particle size of less than 74 um.
E. Cleaning, namely, third separation of copper and molybdenum from talc: A slurry obtained in the step D was subjected to first cleaning and second cleaning and cleaner 997987 scavenging. First cleaning was conducted under the following process conditions: A copper-molybdenum collector TF1# was added at 3 g/t, and then stirring was conducted for 3 min. A frother methyl isobutyl carbinol was added at 2 g/t, and then stirring was conducted for 3 min. Second cleaning was conducted under the following process conditions: A lime was added at 80 g/t, and then stirring was conducted for 4 min. The cleaner scavenging was conducted under the following process conditions:
The copper-molybdenum collector TF1# was added at 2 g/t, and then stirring was conducted for 3 min. The frother methyl isobutyl carbinol was added at 2 g/t, and then stirring was conducted for 3 min.
F. Agent removal before cleaner separation of copper, molybdenum, and magnesium: Clean water was added to a froth product obtained in the step E, cleaning was allowed, and concentration was conducted to produce a concentrate with a concentration of 50% and overflow water. The overflow water was recycled for an upstream operation. The concentrate was fed into a stirring mill, and scrubbed to produce a product in which 85% of resulting particles had a particle size of less than 45 pm.
G. Copper-molybdenum/magnesium separation: The product obtained in the step F was subjected to roughing, scavenging, and first cleaning and second cleaning. The roughing was conducted under the following process conditions: Sodium sulfide was added at 400 g/t, and then stirring was conducted for 5 min. Emulsified kerosene was added at 2 g/t, and then stirring was conducted for 2 min. A frother methyl isobutyl carbinol was added at 2 g/t, and then stirring was conducted for 2 min. The scavenging was conducted under the following process conditions: The sodium sulfide was added at 80 g/t, and then stirring was conducted for 5 min. The emulsified kerosene was added at 1 g/t, and then stirring was conducted for 2. The frother methyl isobutyl carbinol was added at 1 g/t, and then stirring was conducted for 2 min. First cleaning was conducted under the following process conditions: The sodium sulfide was added at 50 g/t, and then stirring was conducted for 2 min. The frother methyl isobutyl carbinol was added at 1 g/t, and then stirring was conducted for 2 min. The second cleaning was conducted under the following process conditions: The sodium sulfide was added at 30 g/t, and then stirring was conducted for 5 min. Intermediates were returned step by step, a tailing from the scavenging was a final copper concentrate product, and a froth from the second cleaning was a crude molybdenum-magnesium concentrate product.
H. High-grade molybdenum-magnesium separation: The crude molybdenum-magnesium concentrate product obtained in the step G was subjected to 7602987 roughing once and scavenging once. The roughing was conducted under the following process conditions: A molybdenum depressant TD-3 was added at 10 g/t, and then stirring was conducted for 3 min. Emulsified kerosene was added at 4 g/t, and then stirring was conducted for 2 min. A frother propylene glycol ether alcohol was added at g/t, and then stirring was conducted for 2 min. The scavenging was conducted under the following process conditions: The molybdenum depressant TD-3 was added at 6 gh, and then stirring was conducted for 3 min. The emulsified kerosene was added at 2 gf, and then stirring was conducted for 2 min. The frother propylene glycol ether alcohol was added at 3 g/t, and then stirring was conducted for 2 min. A tailing from the scavenging was a final high-grade molybdenum concentrate product. . Low-grade molybdenum-magnesium separation: A rougher froth obtained in the step H was subjected to roughing once, scavenging once, and cleaning once. The roughing was conducted under the following process conditions: A molybdenum depressant TD-3 was added at 7 g/t, and then stirring was conducted for 3 min. A frother propylene glycol ether alcohol was added at 5 g/t, and then stirring was conducted for 2 min. The scavenging was conducted under the following process conditions: The molybdenum depressant TD-3 was added at 5 g/t, and then stirring was conducted for 3 min. The frother propylene glycol ether alcohol was added at 3 g/t, and then stirring was conducted for 2 min to 3 min. The cleaning was conducted under the following process conditions: The molybdenum depressant TD-3 was added at 3 git, and then stirring was conducted for 3 min. The frother propylene glycol ether alcohol was added at 2 g/t, and then stirring was conducted for 2 min. Intermediates were returned step by step, a froth from the cleaning was talc, and a tailing from the scavenging was a final low-grade molybdenum concentrate product.
When the ore was treated by the above process, a copper concentrate with a Cu grade of 25.73% and a Cu recovery rate of 87.93%, a high-grade molybdenum concentrate with a Mo grade of 46.15% and a Mo recovery rate of 60.88%, and a low-grade molybdenum concentrate with a Mo grade of 19.57% and a Mo recovery rate of 12.91% could be produced. It can be seen that the process can improve the comprehensive utilization of difficult-to-select mineral resources.
Example 3
An ore sample from a concentrator in Yunnan province, China was adopted. The 7994987 ore sample had a copper content of 0.48%, a molybdenum content of 0.019%, a magnesium oxide content of 8.33%, and an iron content of 13.39%. In the ore sample, the major metallic minerals were chalcopyrite, chalcocite, molybdenite, and pyrite, and the main easily-floatable magnesium silicate minerals were talc and chlorite. The ore sample was treated through the following process steps:
A. First grinding: A lime was added at 1300 g/t to a crushed ore, and the first grinding was conducted until 60% of resulting particles had a particle size of less than 74 um.
B. Copper-molybdenum mixed roughing, namely, first separation of copper and molybdenum from talc: A slurry obtained in the step A was subjected to roughing once and scavenging twice. The roughing was conducted under the following process conditions: a copper-molybdenum collector TF1# was added at 25 g/t, and then stirring was conducted for 3 min. A frother methyl isobutyl carbinol was added at 20 g/t, and then stirring was conducted for 3 min. First scavenging was conducted under the following process conditions: The copper-molybdenum collector TF1# was added at 9 g/t, and then stirring was conducted for 3 min. The frother methyl isobutyl carbinol was added at 6 g/t, and then stirring was conducted for 3 min. Second scavenging was conducted under the following process conditions: The copper-molybdenum collector
TF1# was added at 5 g/t, and then stirring was conducted for 3 min. The frother methyl isobutyl carbinol was added at 3 g/t, and then stirring was conducted for 3 min.
C. Copper-molybdenum mixed cleaning, namely, second separation of copper and molybdenum from talc: À froth product obtained in the step B was subjected to mixed cleaning once and mixed cleaner scavenging once. The cleaning was conducted under the following process conditions: À lime was added at 300 g/t, and then stirring was conducted for 4 min. À fructan as a talc depressant was added at 75 g/t, and then stirring was conducted for 5 min. TF1# was added at 4 g/t, and then stirring was conducted for 3 min. The mixed cleaner scavenging was conducted under the following process conditions: The copper-molybdenum collector TF1# was added at 2 g/t, and then stirring was conducted for 3 min.
D. Second grinding: À lime at 180 g/t and a fructan as a talc depressant at 20 g/t were added successively to a froth product obtained in the step C, and the second grinding was conducted until 90% of resulting particles had a particle size of less than 74 um.
E. Cleaning, namely, third separation of copper and molybdenum from talc: A slurry obtained in the step D was subjected to first cleaning and second cleaning and cleaner 997987 scavenging. First cleaning was conducted under the following process conditions: A copper-molybdenum collector TF1# was added at 2 g/t, and then stirring was conducted for 3 min. A frother methyl isobutyl carbinol was added at 1 g/t, and then stirring was conducted for 3 min. Second cleaning was conducted under the following process conditions: A lime was added at 90 g/t, and then stirring was conducted for 4 min. The cleaner scavenging was conducted under the following process conditions:
The copper-molybdenum collector TF1# was added at 1 g/t, and then stirring was conducted for 3 min. The frother methyl isobutyl carbinol was added at 1 g/t, and then stirring was conducted for 3 min.
F. Agent removal before cleaner separation of copper, molybdenum, and magnesium: Clean water was added to a froth product obtained in the step E, cleaning was allowed, and concentration was conducted to produce a concentrate with a concentration of 55% and overflow water. The overflow water was recycled for an upstream operation. The concentrate was fed into a stirring mill, and scrubbed to produce a product in which 85% of resulting particles had a particle size of less than 45 pm.
G. Copper-molybdenum/magnesium separation: The product obtained in the step F was subjected to roughing, scavenging, and first cleaning and second cleaning. The roughing was conducted under the following process conditions: Sodium sulfide was added at 280 g/t, and then stirring was conducted for 5 min. Emulsified kerosene was added at 2 g/t, and then stirring was conducted for 2 min. A frother methyl isobutyl carbinol was added at 1 g/t, and then stirring was conducted for 2 min. The scavenging was conducted under the following process conditions: The sodium sulfide was added at 70 g/t, and then stirring was conducted for 5 min. The emulsified kerosene was added at 1 g/t, and then stirring was conducted for 2. The frother methyl isobutyl carbinol was added at 1 g/t, and then stirring was conducted for 2 min. First cleaning was conducted under the following process conditions: The sodium sulfide was added at 60 g/t, and then stirring was conducted for 2 min. The frother methyl isobutyl carbinol was added at 1 g/t, and then stirring was conducted for 2 min. The second cleaning was conducted under the following process conditions: The sodium sulfide was added at 30 g/t, and then stirring was conducted for 5 min. Intermediates were returned step by step, a tailing from the scavenging was a final copper concentrate product, and a froth from the second cleaning was a crude molybdenum-magnesium concentrate product.
H. High-grade molybdenum-magnesium separation: The crude molybdenum-magnesium concentrate product obtained in the step G was subjected to 7602987 roughing once and scavenging once. The roughing was conducted under the following process conditions: A molybdenum depressant TD-3 was added at 12 g/t, and then stirring was conducted for 3 min. Emulsified kerosene was added at 3 g/t, and then stirring was conducted for 2 min. A frother propylene glycol ether alcohol was added at g/t, and then stirring was conducted for 2 min. The scavenging was conducted under the following process conditions: The molybdenum depressant TD-3 was added at 5 gh, and then stirring was conducted for 3 min. The emulsified kerosene was added at 2 gf, and then stirring was conducted for 2 min. The frother propylene glycol ether alcohol was added at 3 g/t, and then stirring was conducted for 2 min. A tailing from the scavenging was a final high-grade molybdenum concentrate product. . Low-grade molybdenum-magnesium separation: A rougher froth obtained in the step H was subjected to roughing once, scavenging once, and cleaning once. The roughing was conducted under the following process conditions: A molybdenum depressant TD-3 was added at 8 g/t, and then stirring was conducted for 3 min. A frother propylene glycol ether alcohol was added at 5 g/t, and then stirring was conducted for 2 min. The scavenging was conducted under the following process conditions: The molybdenum depressant TD-3 was added at 4 g/t, and then stirring was conducted for 3 min. The frother propylene glycol ether alcohol was added at 3 g/t, and then stirring was conducted for 2 min to 3 min. The cleaning was conducted under the following process conditions: The molybdenum depressant TD-3 was added at 3 git, and then stirring was conducted for 3 min. The frother propylene glycol ether alcohol was added at 2 g/t, and then stirring was conducted for 2 min. Intermediates were returned step by step, a froth from the cleaning was talc, and a tailing from the scavenging was a final low-grade molybdenum concentrate product.
When the ore was treated by the above process, a copper concentrate with a Cu grade of 27.33% and a Cu recovery rate of 84.07%, a high-grade molybdenum concentrate with a Mo grade of 45.03% and a Mo recovery rate of 62.03%, and a low-grade molybdenum concentrate with a Mo grade of 20.16% and a Mo recovery rate of 10.68% could be produced. It can be seen that the process can improve the comprehensive utilization of difficult-to-select mineral resources.

Claims (10)

CLAIMS LU602387
1. A method for stepwise separation of magnesium from a skarn-type copper-molybdenum ore with a high talc content, comprising pre-treatment, first separation, second separation, grinding, third separation, and fourth separation, and specifically comprising: A, the pre-treatment: adding a lime to a crushed skarn-type copper-molybdenum ore with a high talc content, and grinding until 50% to 60% of resulting particles have a particle size of less than 74 um to produce a material a; B, the first separation: adding a copper-molybdenum collector and a first frother all at once to the material a, and conducting roughing to produce a copper-molybdenum mixed rougher concentrate b and a copper-molybdenum mixed rougher tailing c; and adding the copper-molybdenum collector and the first frother to the copper-molybdenum mixed rougher tailing c, and conducting scavenging twice, wherein froths from the scavenging are returned step by step; C, the second separation: adding the lime, a talc depressant, and the copper-molybdenum collector successively to the copper-molybdenum mixed rougher concentrate b, and conducting cleaning to produce a copper-molybdenum mixed cleaner concentrate d and a copper-molybdenum mixed cleaner tailing e; adding the copper-molybdenum collector to the copper-molybdenum mixed cleaner tailing e, and conducting cleaner scavenging to produce a copper-molybdenum mixed cleaner scavenger concentrate f and a tailing g; and returning the copper-molybdenum mixed cleaner scavenger concentrate f to the cleaning, wherein the tailing g is a final tailing 2; D, the grinding: adding the lime and the talc depressant successively to the copper-molybdenum mixed cleaner tailing e, and grinding until 80% to 90% of resulting particles have a particle size of less than 74 um to produce a material h; E, the third separation: adding the copper-molybdenum collector and the first frother successively to the material h, and conducting first cleaning and second cleaning and cleaner scavenging to produce a copper-molybdenum concentrate i; and F, the fourth separation: subjecting the copper-molybdenum concentrate i to agent removal, copper-molybdenum/magnesium separation, high-grade molybdenum-magnesium separation, and low-grade molybdenum-magnesium separation to produce a low-grade molybdenum concentrate product, wherein the fourth separation is specifically as follows: 1) the agent removal: adding clean water to the copper-molybdenum concentrate i,
conducting cleaning, and concentrating for the agent removal to produce a material j;
2) the copper-molybdenum/magnesium separation: adding a copper depressant, a 7902987 neutral oil, and the first frother successively to the material j, and conducting roughing, scavenging, and first cleaning and second cleaning sequentially, wherein intermediates are returned step by step, a tailing from the scavenging is a final copper concentrate product, and a froth from the second cleaning is a crude molybdenum-magnesium concentrate product k;
3) the high-grade molybdenum-magnesium separation: adding a molybdenum depressant, the neutral oil, and a second frother successively to the crude molybdenum-magnesium concentrate product k, and conducting roughing to produce a high-grade molybdenum-magnesium separation rougher concentrate | and a high-grade molybdenum-magnesium separation rougher tailing m; adding the molybdenum depressant, the neutral oil, and the second frother successively to the high-grade molybdenum-magnesium separation rougher tailing m, and conducting scavenging to produce a high-grade molybdenum-magnesium separation scavenger concentrate n and a high-grade molybdenum-magnesium separation scavenger tailing; and returning the high-grade molybdenum-magnesium separation scavenger concentrate n to the high-grade molybdenum-magnesium separation roughing step, wherein the high-grade molybdenum-magnesium separation scavenger tailing is a final high-grade molybdenum concentrate product o; and
4) the low-grade molybdenum-magnesium separation: adding the molybdenum depressant and the second frother successively to the high-grade molybdenum-magnesium separation rougher concentrate |, and conducting roughing, scavenging once, and cleaning once sequentially, wherein intermediates are returned step by step, a froth from the cleaning is talc, and a tailing from the scavenging is the low-grade molybdenum concentrate product.
2. The method for the stepwise separation of the magnesium from the skarn-type copper-molybdenum ore with the high talc content according to claim 1, wherein the 692987 conducting scavenging twice in the step B is as follows: adding the copper-molybdenum collector and the first frother to the copper-molybdenum mixed rougher tailing c, and conducting first scavenging to produce a copper-molybdenum mixed first-scavenger concentrate and a copper-molybdenum mixed first-scavenger tailing; returning the copper-molybdenum mixed first-scavenger concentrate to the copper-molybdenum mixed roughing step; adding the copper-molybdenum collector and the first frother to the copper-molybdenum mixed first-scavenger tailing, and conducting second scavenging to produce a copper-molybdenum mixed second-scavenger concentrate and a final tailing 1; and returning the copper-molybdenum mixed second-scavenger concentrate to the first scavenging.
3. The method for the stepwise separation of the magnesium from the skarn-type copper-molybdenum ore with the high talc content according to claim 1, wherein the conducting first cleaning and second cleaning and cleaner scavenging once in the step E is as follows: adding the copper-molybdenum collector and the first frother to the material h, and conducting the first cleaning to produce a first copper-molybdenum cleaner concentrate and a first copper-molybdenum cleaner tailing; adding the lime to the first copper-molybdenum cleaner concentrate, and conducting the second cleaning to produce the copper-molybdenum concentrate i and a second copper-molybdenum cleaner tailing; adding the copper-molybdenum collector and the first frother to the first copper-molybdenum cleaner tailing, and conducting the cleaner scavenging to produce a copper-molybdenum cleaner scavenger concentrate and a copper-molybdenum cleaner scavenger tailing; returning the copper-molybdenum cleaner scavenger tailing to the cleaning; and combining the copper-molybdenum cleaner scavenger concentrate with the second copper-molybdenum cleaner tailing, and returning a combined material to the first cleaning.
4. The method for the stepwise separation of the magnesium from the skarn-type copper-molybdenum ore with the high talc content according to claim 1, wherein the copper-molybdenum collector in the steps B, C, and E comprises isopropylthiourea, ethylene glycol chloroformate, and pyridine.
5. The method for the stepwise separation of the magnesium from the skarn-type LU602387 copper-molybdenum ore with the high talc content according to claim 4, wherein the isopropylthiourea, the ethylene glycol chloroformate, and the pyridine are in a mass ratio of (2-6):(3-6):(0.3-1.2).
6. The method for the stepwise separation of the magnesium from the skarn-type copper-molybdenum ore with the high talc content according to claim 1, wherein the molybdenum depressant in the step F comprises dextrin, sodium cellulose xanthate, and octylphenol ethoxylate.
7. The method for the stepwise separation of the magnesium from the skarn-type copper-molybdenum ore with the high talc content according to claim 6, wherein the dextrin, the sodium cellulose xanthate, and the octylphenol ethoxylate are in a mass ratio of (2-5):(3-7):(0.3-1.2).
8. The method for the stepwise separation of the magnesium from the skarn-type copper-molybdenum ore with the high talc content according to claim 1, wherein the first frother in the step B, the step E, and the step 2) of F is methyl isobutyl carbinol; and the second frother in the step 3) of F and the step 4) of F is propylene glycol ether alcohol.
9. The method for the stepwise separation of the magnesium from the skarn-type copper-molybdenum ore with the high talc content according to claim 1, wherein the talc depressant is a fructan.
10. The method for the stepwise separation of the magnesium from the skarn-type copper-molybdenum ore with the high talc content according to claim 1, wherein the copper depressant is sodium sulfide and/or sodium hydrosulfide; and the neutral oil is an emulsion of kerosene and/or diesel.
LU602387A 2024-06-12 2025-01-24 Method for stepwise separation of magnesium from skarn-type copper-molybdenum ore with high talc content LU602387B1 (en)

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