CN113731627A - Pre-tailing-discarding mixed flotation method for rare earth multi-metal ore - Google Patents

Pre-tailing-discarding mixed flotation method for rare earth multi-metal ore Download PDF

Info

Publication number
CN113731627A
CN113731627A CN202111036365.6A CN202111036365A CN113731627A CN 113731627 A CN113731627 A CN 113731627A CN 202111036365 A CN202111036365 A CN 202111036365A CN 113731627 A CN113731627 A CN 113731627A
Authority
CN
China
Prior art keywords
ore
concentrate
flotation
ores
concentration
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN202111036365.6A
Other languages
Chinese (zh)
Other versions
CN113731627B (en
Inventor
李春风
刘志超
李广
张新
马嘉
强录德
唐宝彬
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Beijing Research Institute of Chemical Engineering and Metallurgy of CNNC
Original Assignee
Beijing Research Institute of Chemical Engineering and Metallurgy of CNNC
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Beijing Research Institute of Chemical Engineering and Metallurgy of CNNC filed Critical Beijing Research Institute of Chemical Engineering and Metallurgy of CNNC
Priority to CN202111036365.6A priority Critical patent/CN113731627B/en
Publication of CN113731627A publication Critical patent/CN113731627A/en
Application granted granted Critical
Publication of CN113731627B publication Critical patent/CN113731627B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • 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
    • B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
    • B03B7/00—Combinations of wet processes or apparatus with other processes or apparatus, e.g. for dressing ores or garbage
    • 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
    • B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
    • B03B9/00—General arrangement of separating plant, e.g. flow sheets
    • 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

Landscapes

  • Manufacture And Refinement Of Metals (AREA)

Abstract

The invention provides a pre-tailing-discarding mixed flotation method for rare earth polymetallic ores, and relates to the technical field of ore dressing. According to the invention, the crushed ores are subjected to particle size classification, and the pre-tailing discarding process of the ores with different particle sizes is reasonably designed by means of combining heavy medium cyclone separation, table concentrator gravity separation and desliming-centrifugal gravity separation, so that the tailing discarding and pre-enrichment of the raw ores under the condition of coarse particles are realized; then carrying out flotation to obtain high-grade bulk concentrate. The method provided by the invention can realize the high-efficiency separation between the main useful mineral aggregate and the gangue mineral in the rare earth multi-metal ore, simultaneously remarkably reduce the ore amount entering the ore grinding and flotation processes, save the cost of flotation reagents, equipment energy consumption and the like, avoid the over-grinding phenomenon caused by the existence of wear-resistant gangue mineral, and provide technical support for improving the economic benefit of the rare earth multi-metal ore and promoting the green and high-efficiency development of the ore deposit.

Description

Pre-tailing-discarding mixed flotation method for rare earth multi-metal ore
Technical Field
The invention relates to the technical field of mineral separation, in particular to a pre-tailing-discarding mixed flotation method for rare earth multi-metal ores.
Background
Compared with carbonate-type rare earth deposit, the alkaline granite-type rare earth deposit is relatively rich in heavy rare earth, has abundant key strategic metals such as uranium, niobium, zirconium, thorium, beryllium and the like besides rare earth and yttrium resources occupying 1/3 around the world, and has great economic value.
Typical alkaline granite type rare earth deposits in China include inner Mongolian Gubal's REE-Nb-U-Zr deposits, Liaoning Saima rare earth deposits, Henan Fangcheng Dazhuang niobium-rare earth deposits, Xinjiang Baochien super large REE-Nb-Ta-Zr deposits, etc. The research shows that the alkaline granite deposit has more element types, complex embedding relation, various useful minerals and fine granularity. Rare earth elements are mainly present in phosphate and silicate minerals, rare metals such as Zr, Nb, U stone, Th, and Be are mainly present in minerals such as zirconite, trogopite, niobite, bixbyite, tantalite, and thorite, and main gangue minerals are quartz, potassium feldspar, plagioclase, and the like having a small specific gravity. The alkaline granite rare earth deposit has typical rock mineralization characteristics, the ore deposit is large in scale and uniform in mineralization, but the grade of valuable elements is low, the cost for directly extracting valuable metals from raw ores by adopting a metallurgical process is high, and the ore grade enrichment is usually needed by a mineral separation process to achieve economic benefits.
As the minerals and valuable elements in the alkaline granite rare earth deposit are various, the target mineral particles are fine (0-50 mu m), and the embedding relation is complex, the target mineral is easy to argillization and loss in the fine grinding process. In the existing mineral separation process, the purpose of fully dissociating minerals is achieved by directly and finely grinding raw ores to-0.1 mm or-0.074 mm with the granularity of more than 70% (CN201811117361.9, CN201210222033.1 and CN202010333043.7), and then high-grade concentrate products are obtained by means of various separation technologies, the ore crushing and grinding and mineral separation process of the technology needs large amount of processed ores, high energy consumption and material cost, and high fine mud components can also cause the deterioration of mineral separation indexes.
Taking the inner Mongolia Gubal philosophy REE-Nb-U-Zr deposit as an example, a plurality of research units develop a large amount of mineral processing technology researches, and the current main mineral processing technology mainly comprises the following steps: (1) obtaining niobium-rare earth-zirconium mixed concentrate and zirconium concentrate by a magnetic separation-reselection process recommended by Zhengzhou of China geological academy of sciences; (2) obtaining uranium, niobium, zirconium and rare earth bulk concentrates through a magnetic separation-reselection flow proposed by the university of inner Mongolia science and technology; (3) the 'gravity separation-magnetic separation-flotation-gravity separation' and 'magnetic separation-flotation-gravity separation' processes are respectively proposed by Baotou rare earth research institute, Beijing mining and metallurgy research institute and the like, and three products of rare earth concentrate, niobium concentrate, zirconium concentrate and the like are obtained. No matter which technical scheme is adopted, raw ores are crushed and ground to the granularity of minus 0.074mm which accounts for more than 50%, even the ores are ground to the granularity of minus 0.043mm which accounts for more than 95% during flotation, all the raw ores are ground and selected, so that the ore grinding cost is high, partial valuable metals are argillized in the fine grinding process, and the ore dressing recovery rate is influenced.
Disclosure of Invention
The invention aims to provide a pre-tailing-throwing mixed flotation method for rare earth multi-metal ores, which can realize high-efficiency separation between a main useful mineral aggregate and gangue minerals in the rare earth multi-metal ores, simultaneously remarkably reduce the ore amount entering grinding and flotation processes, save the costs of flotation reagents, equipment energy consumption and the like, avoid the over-grinding phenomenon caused by the existence of wear-resistant gangue minerals, improve the recovery rate, and provide technical support for improving the economic benefit of the rare earth multi-metal ores and promoting green and high-efficiency development of the ore beds.
In order to achieve the above object, the present invention provides the following technical solutions:
the invention provides a pre-tailing-discarding mixed flotation method for rare earth multi-metal ores, which comprises the following steps of:
crushing and screening raw ores to obtain five-grade ores; the five-grade ore is +0.5mm grade ore, + 0.3-0.5 mm grade ore, + 0.15-0.3 mm grade ore, + 0.074-0.15 mm grade ore and-0.074 mm grade ore;
carrying out dense medium cyclone separation on the ore with the size fraction of +0.5mm to obtain dense medium separation concentrate;
respectively carrying out table reselection on the ore with the size fraction of + 0.3-0.5 mm, the ore with the size fraction of + 0.15-0.3 mm and the ore with the size fraction of + 0.074-0.15 mm to obtain table concentrate;
carrying out desliming-centrifugal gravity separation treatment on the ore with the size fraction of-0.074 mm to obtain ore mud concentrate;
performing flotation on the dense medium separation concentrate, the table concentrate and the slime concentrate to obtain flotation rough concentrate;
and carrying out fine concentration on the flotation rough concentrate to obtain bulk concentrate.
Preferably, the raw ore is derived from an alkaline granite-type rare earth deposit.
Preferably, the crushing and screening comprises: crushing raw ores to be less than 10mm, forming a closed system by using a high-pressure roller mill and a high-frequency vibrating screen, crushing ores with the granularity of-10 mm by using the high-pressure roller mill, passing through the high-frequency vibrating screen with the screen holes of 1-3 mm, and returning screened products to the high-pressure roller mill for reprocessing to finally obtain ores with the granularity of 1-3 mm, wherein the proportion of the-0.074 mm in granularity is not more than 15 wt%; and screening the ore with the particle size of less than 1-3 mm to obtain five-particle-size ore.
Preferably, the yield of table concentrate obtained by table reselection of the ore with the size fraction of + 0.3-0.5 mm, the ore with the size fraction of + 0.15-0.3 mm and the ore with the size fraction of + 0.074-0.15 mm is 20-60 wt% independently.
Preferably, the desliming-centrifugal gravity separation process comprises: carrying out desliming treatment on the ore with the size fraction of-0.074 mm, and separating ore mud with the size of-0.02 mm and ore sand with the size of +0.02 to-0.074 mm; carrying out centrifugal gravity separation on the sand with the granularity of plus 0.02-minus 0.074mm to obtain centrifugal concentrate; and combining the slime with the granularity of-0.02 mm and the centrifugal concentrate to obtain slime concentrate.
Preferably, the medicament for centrifugal gravity separation comprises water glass or sodium hexametaphosphate.
Preferably, the dense medium separation concentrate and the table concentrate are subjected to ore grinding and then subjected to flotation.
Preferably, flotation coarse tailings are obtained after the flotation, and the flotation method further comprises the following steps: scavenging the flotation coarse tailings to obtain scavenged concentrate; and returning the scavenging concentrate to perform flotation.
Preferably, the flotation agent comprises a primary collector and a secondary collector; the main collector comprises RA935, oxidized paraffin soap and p-tert-butyl benzene hydroxamic acid; the secondary collector comprises a dodecylamine-based bis (methylene phosphonic acid) solution.
Preferably, said beneficiation comprises a first beneficiation and a re-beneficiation carried out in sequence; the re-concentration times are more than 1; and the concentration object of the re-concentration is the concentrate obtained by the last concentration.
The invention provides a mixed flotation method for pre-discarding tails of rare earth polymetallic ores, which reasonably designs a pre-discarding tail process of ores with different grain sizes by carrying out particle size classification on crushed ores and by means of combining heavy medium cyclone separation, table concentrator gravity separation and desliming-centrifugal gravity separation, thereby realizing discarding tails and pre-enriching of raw ores under the condition of coarse grains; then carrying out flotation to obtain high-grade bulk concentrate. The method provided by the invention can realize the high-efficiency separation between the main useful mineral aggregate and the gangue mineral in the rare earth multi-metal ore, simultaneously remarkably reduce the ore amount entering the ore grinding and flotation processes, save the cost of flotation reagents, equipment energy consumption and the like, avoid the over-grinding phenomenon caused by the existence of wear-resistant gangue mineral, improve the recovery rate, and provide technical support for improving the economic benefit of the rare earth multi-metal ore and promoting the green and high-efficiency development of the ore deposit.
Drawings
FIG. 1 is a flow chart of a pre-tailing discarding mixed flotation method for rare earth multi-metal ore provided by the invention.
Detailed Description
The invention provides a pre-tailing-discarding mixed flotation method for rare earth multi-metal ores, which comprises the following steps of:
crushing and screening raw ores to obtain five-grade ores; the five-grade ore is +0.5mm grade ore, + 0.3-0.5 mm grade ore, + 0.15-0.3 mm grade ore, + 0.074-0.15 mm grade ore and-0.074 mm grade ore;
carrying out dense medium cyclone separation on the ore with the size fraction of +0.5mm to obtain dense medium separation concentrate;
respectively carrying out table reselection on the ore with the size fraction of + 0.3-0.5 mm, the ore with the size fraction of + 0.15-0.3 mm and the ore with the size fraction of + 0.074-0.15 mm to obtain table concentrate;
carrying out desliming-centrifugal gravity separation treatment on the ore with the size fraction of-0.074 mm to obtain ore mud concentrate;
performing flotation on the dense medium separation concentrate, the table concentrate and the slime concentrate to obtain flotation rough concentrate;
and carrying out fine concentration on the flotation rough concentrate to obtain bulk concentrate.
Fig. 1 is a flow chart of a method for pre-tailing discarding mixed flotation of rare earth polymetallic ores provided by the invention, and the method for pre-tailing discarding mixed flotation of rare earth polymetallic ores provided by the invention is described in detail with reference to fig. 1.
The invention carries out crushing and screening on the raw ore to obtain five-grain-size ore. In the present invention, the raw ore is preferably derived from an alkaline granite-type rare earth deposit. The invention aims at the problems of large ore treatment capacity, high ore grinding and dressing cost, low valuable metal recovery rate and the like existing in the direct crushing grinding-sorting process of raw ores of alkaline granite rare earth ore deposits, combines the characteristics of mineral types, continuous growth conditions, element occurrence forms and the like in alkaline granite ores to achieve the purpose of realizing high-efficiency pre-tailing throwing of the ores while obtaining high-recovery-rate bulk concentrates, designs a dressing technical route in a targeted manner, develops a flotation process suitable for the alkaline granite rare earth ores, and improves the dressing technical index and the economical efficiency of the resources.
In the present invention, the crushing and screening preferably comprises: crushing raw ores to be less than 10mm, forming a closed system by using a high-pressure roller mill and a high-frequency vibrating screen, crushing ores with the granularity of-10 mm by using the high-pressure roller mill, passing through the high-frequency vibrating screen with the screen holes of 1-3 mm, and returning screened products to the high-pressure roller mill for reprocessing to finally obtain ores with the granularity of 1-3 mm, wherein the proportion of the-0.074 mm in granularity is not more than 15 wt%; and screening the ore with the particle size of less than 1-3 mm to obtain five-particle-size ore. In the invention, the sieve pores of the high-frequency vibrating sieve are more preferably 1.25-2.5 mm.
In the present invention, the crushing is preferably performed using a jaw crusher. In the present invention, the sieving is preferably performed by high frequency vibration sieving.
The invention realizes the selective dissociation between useful minerals (aggregate) and gangue minerals by closed-circuit crushing, and reduces the argillization of target minerals.
In the invention, the five-grade ore is +0.5mm grade ore, + 0.3-0.5 mm grade ore, + 0.15-0.3 mm grade ore, + 0.074-0.15 mm grade ore and-0.074 mm grade ore. In the present invention, "+ 0.3 to-0.5 mm" is taken as an example, and "+" indicates not less than; "-" indicates less than. The granularity representation method of the invention adopts the rule, and is not described in detail.
After five-grade ore is obtained, the ore with the grade of +0.5mm is subjected to dense medium cyclone separation to obtain dense medium separation concentrate. In the present invention, the heavy medium cyclone sorting preferably comprises: mixing the ore with the size fraction of +0.5mm with the heavy medium suspension to obtain ore pulp with the size fraction of +0.5 mm; adding the ore pulp with the size fraction of +0.5mm into a heavy medium cyclone for separation to obtain light component ore pulp and heavy component ore pulp; and screening the light component ore pulp and the heavy component ore pulp to obtain light component cyclone tailings with the granularity of plus 0.5mm and heavy medium separation concentrate. In the present invention, the preparation method of the dense medium suspension is preferably: mixing ferrosilicon powder with water to obtain a heavy medium suspension; the density of the dense medium suspension liquid is preferably 1.8-2.1 g/cm3More preferably 1.9 to 1.95g/cm3. In the invention, the concentration of the ore pulp with the size fraction of +0.5mm is preferably less than or equal to 30 wt%, and more preferably 10-15 wt%. In the present invention, the dense medium cyclone is preferablyIs a dense medium cyclone described in Chinese patent CN 202020302112.3. In the invention, the ore feeding pressure during the heavy medium cyclone separation is preferably 0.1-0.16 MPa, and more preferably 0.12-0.15 MPa. The invention preferably obtains the light component ore pulp from an overflow port of the heavy medium cyclone and obtains the heavy component ore pulp from a sand setting port at the bottom of the heavy medium cyclone. In the invention, the aperture of the screen mesh adopted when the light component ore pulp and the heavy component ore pulp are screened is preferably less than 0.5mm, more preferably 0.3mm, which is beneficial to improving the screening efficiency. In the present invention, the sieving is preferably performed by using a high frequency vibration sieve. In the present invention, the sieving preferably also results in undersize; and the undersize is dense medium suspension, and is returned for recycling after being settled and thickened.
The invention carries out table reselection on the ore with the size fraction of +0.3 to-0.5 mm, +0.15 to-0.3 mm and +0.074 to-0.15 mm respectively to obtain table concentrate. In the present invention, the table reselection preferably comprises: respectively adding water into the ore with the size fraction of + 0.3-0.5 mm, the ore with the size fraction of + 0.15-0.3 mm and the ore with the size fraction of + 0.074-0.15 mm to obtain ore pulp with the size fraction of + 0.3-0.5 mm, ore pulp with the size fraction of + 0.15-0.3 mm and ore pulp with the size fraction of + 0.074-0.15 mm; and respectively carrying out table reselection on the ore pulp with the size fraction of + 0.3-0.5 mm, the ore pulp with the size fraction of + 0.15-0.3 mm and the ore pulp with the size fraction of + 0.074-0.15 mm to obtain table concentrate. In the invention, the concentration of the ore pulp with the size fraction of + 0.3-0.5 mm, the ore pulp with the size fraction of + 0.15-0.3 mm and the ore pulp with the size fraction of + 0.074-0.15 mm is preferably 5-30 wt%, and more preferably 15-25 wt%. In the invention, the yield of table concentrate obtained by performing table reselection on the ore with the size fraction of + 0.3-0.5 mm, the ore with the size fraction of + 0.15-0.3 mm and the ore with the size fraction of + 0.074-0.15 mm is independently preferably 15-60 wt%, more preferably 20-50 wt% and even more preferably 25-30 wt%.
In the present invention, it is preferred that the shaker tailings are also obtained after the shaker reselection.
The ore with the size fraction of-0.074 mm is subjected to desliming-centrifugal gravity separation treatment to obtain ore mud concentrate. In the present invention, the desliming-centrifugal gravity separation treatment preferably comprises: carrying out desliming treatment on the ore with the size fraction of-0.074 mm, and separating ore mud with the size of-0.02 mm and ore sand with the size of +0.02 to-0.074 mm; carrying out centrifugal gravity separation on the sand with the granularity of plus 0.02-minus 0.074mm to obtain centrifugal concentrate; and combining the slime with the granularity of-0.02 mm and the centrifugal concentrate to obtain slime concentrate. In the present invention, the desliming treatment is preferably performed using a classification hydrocyclone, more preferably an FX Φ 20 ultrafine classification hydrocyclone. In the present invention, the feeding pressure in the desliming treatment is preferably 0.08 to 0.15MPa, and more preferably 0.09 to 0.12 MPa.
In the present invention, the centrifugal gravity separation preferably includes: mixing the sand with the granularity of plus 0.02 to minus 0.074mm with water to obtain ore pulp with the granularity of plus 0.02 to minus 0.074 mm; and then carrying out centrifugal gravity separation on the ore sand pulp with the granularity of plus 0.02 to minus 0.074mm to obtain centrifugal concentrate. In the invention, the concentration of the ore pulp with the grain size of + 0.02-0.074 mm is preferably 5-40 wt%, and more preferably 20-30 wt%. In the present invention, the agent for centrifugal gravity separation preferably includes water glass or sodium hexametaphosphate. In the present invention, the water glass or sodium hexametaphosphate is used as a dispersant. In the invention, the addition amount of the medicament relative to the sand with the grain size of + 0.02-0.074 mm is preferably 500-3000 g/t. In the present invention, the centrifugal gravity separation is preferably carried out in a nielsen centrifugal concentrator; the centrifugal reselection conditions include: the centrifugal strength is preferably 40-80G, and more preferably 50-70G; the feeding speed is preferably 0.1-2 kg/min, and more preferably 1.0-1.6 kg/min; the preferred reverse flushing water pressure is 0.03-0.05 MPa, and the more preferred reverse flushing water pressure is 0.04 MPa; the amount of the fluidizing water is preferably 1 to 4kg/min, more preferably 1.2 to 3 kg/min.
In the present invention, centrifugal tailings are preferably also obtained after the centrifugal gravity separation.
After the dense medium separation concentrate, the table concentrator concentrate and the slime concentrate are obtained, the flotation method carries out flotation on the dense medium separation concentrate, the table concentrator concentrate and the slime concentrate to obtain flotation rough concentrate. In the present invention, the dense media separation concentrate and the table concentrate are preferably subjected to flotation after grinding. In the present invention, the ore grinding preferably includes: mixing the dense medium separation concentrate, the table concentrate and water to obtain gravity concentration rough concentrate ore pulp; and grinding the gravity concentration rough concentrate pulp to obtain a ground ore powder concentrate. In the invention, the concentration of the gravity concentration rough concentrate ore pulp is preferably 20-50 wt%, and more preferably 25-40 wt%; the grinding is preferably carried out in an attritor mill; the granularity of-0.074 mm in the ground ore powder concentrate accounts for more than 90 wt%.
The invention preferably carries out flotation on the ground ore powder concentrate and the slime concentrate to obtain flotation rough concentrate. In the present invention, the flotation preferably comprises: mixing the ground ore powder concentrate and the slime concentrate, and then carrying out size mixing to obtain mixed flotation raw ore pulp; and carrying out flotation on the mixed flotation raw ore pulp to obtain flotation rough concentrate. In the invention, the concentration of the mixed flotation raw ore pulp is preferably 10-40 wt%, and more preferably 25-30 wt%; the temperature of the mixed flotation raw ore pulp is preferably 25-55 ℃, and more preferably 40-50 ℃.
In the present invention, the flotation reagent preferably comprises a primary collector and a secondary collector. In the present invention, the primary collector preferably comprises RA935, oxidized paraffin soap and p-tert-butylbenzohydroxamic acid. In the invention, the mass ratio of RA935 to oxidized paraffin soap to p-tert-butyl benzene hydroxamic acid is preferably 40-50: 30-40: 10-20, more preferably 42-45: 35-38: 12 to 20. In the invention, RA935 and oxidized paraffin soap have a strong collecting effect on bastnaesite and rare earth silicate minerals widely existing in alkaline granite, p-tert-butyl benzene hydroxamic acid has a strong collecting ability on rare earth phosphate minerals and ferrocolumbium minerals represented by monazite, the complex formulation of the RA935 and the oxidized paraffin soap is not simple mixture, and the effects are as follows: the mutual adsorption and combination of nonpolar groups among different collecting agent molecules are promoted under a high-concentration solution system, the effect of gain is achieved, and the obtained main collecting agent has good collecting capacity on rare earth minerals, niobite objects and aggregates thereof.
In the present invention, the primary collector preferably further comprises an emulsifier and an aqueous sodium hydroxide solution. In the present invention, the emulsifier is preferably triethanolamine; the emulsifier is preferably 5-30% by mass, more preferably 8-10% by mass of RA935, oxidized paraffin soap and p-tert-butyl benzene hydroxamic acid. In the present invention, the concentration of the sodium hydroxide aqueous solution is preferably 0.1 to 5 wt%, more preferably 1 to 3 wt%. In the invention, the total mass content of RA935, oxidized paraffin soap and p-tert-butyl benzene hydroxamic acid in the main collector is preferably 0.1-20 wt%, and more preferably 1-10 wt%. In the invention, the sodium hydroxide aqueous solution can saponify the fatty acid medicament RA935 and the p-tert-butyl benzene hydroxamic acid to obtain a uniform solution through saponification reaction, and simultaneously, free organic acid radical ions are obtained, thus having a dispersing function. In the invention, the addition of the emulsifier can effectively improve the dispersing capacity of the main collector.
In the invention, the addition amount of the main collector relative to the total mass of the ground ore powder concentrate and the slime concentrate is preferably 10-1500 g/t, and more preferably 400-600 g/t. In the invention, minerals such as rare earth, niobium and the like can fully react with the collecting agent, and the hydrophobicity of the surface of the minerals is enhanced so that the minerals are easy to float.
In the present invention, the secondary collector preferably comprises a dodecylamine-based bis (methylene phosphonic acid) solution. In the present invention, the method for preparing the dodecylamino bis (methylene phosphonic acid) solution preferably comprises: mixing the dodecylamino bis (methylene phosphonic acid) and the NaOH aqueous solution to obtain the dodecylamino bis (methylene phosphonic acid) solution. According to the invention, the collector solution containing organic phosphate ions is obtained by adding NaOH aqueous solution, so that the dispersing effect is achieved. In the invention, the concentration of the NaOH aqueous solution is preferably 0.5-1 wt%. In the invention, the concentration of dodecylamino bis (methylene phosphonic acid) in the dodecylamino bis (methylene phosphonic acid) solution is preferably 0.1 to 10 wt%, and more preferably 1 to 5 wt%. In the invention, the auxiliary collecting agent can improve the collecting capability of other silicate minerals such as zircon and the like, and has certain collecting capability of high valence elements such as rare earth, Ta, Nb and the like.
In the invention, the addition amount of the secondary collector relative to the total mass of the ground ore powder concentrate and the slime concentrate is preferably 0-300 g/t, and more preferably 120-200 g/t. In the invention, the auxiliary collecting agent fully reacts with the useful mineral, and the main collecting agent and the auxiliary collecting agent are jointly adsorbed on the target mineral.
In the present invention, the flotation reagent preferably further comprises a precipitant, a dispersant and a pH adjuster; the precipitating agent preferably comprises Na2CO3Or NaHCO3(ii) a The addition amount of the precipitator relative to the total mass of the ground ore powder concentrate and the slime concentrate is preferably 200-2000 g/t, and more preferably 800-1200 g/t. In the present invention, CO generated after dissolution of the precipitant3 2-With Ca in the pulp2+、Mg2+And the combination of harmful ions is inevitable, and the interference on the flotation of target minerals is eliminated.
In the present invention, the dispersant preferably includes water glass or sodium hexametaphosphate. In the invention, the addition amount of the dispersing agent relative to the total mass of the ground ore powder concentrate and the slime concentrate is preferably 500-2000 g/t, and more preferably 1200-1600 g/t. In the present invention, the dispersant functions as a fine mud particle dispersant and a gangue mineral inhibitor.
In the present invention, the pH adjustor preferably includes H2SO4Solutions or NaOH solutions. The pH value of the mixed flotation raw ore pulp is adjusted to 8.0-9.5 by adopting a pH regulator, and more preferably 8.8-9.1.
In the present invention, the flotation method preferably comprises: and sequentially adding a regulator, a dispersant, a pH regulator, a main collector and an auxiliary collector into the mixed flotation raw ore pulp for flotation. In the invention, the stirring system is preferably selected for 1-10 min after the regulator is added; after the dispersing agent is added, preferably selecting a stirring system for 1-10 min; after the pH regulator is added, the pH value of the system is adjusted to 8.0-9.5; adding a main collector and then preferably selecting a stirring system for 1-10 min; and preferably stirring the system for 1-10 min after adding the auxiliary collecting agent.
In the flotation process, a large amount of bubbles are generated in the flotation tank, and the bubbles are scraped out after floating to the surface of ore pulp to obtain flotation rough concentrate. In the invention, the time for flotation is preferably 1-10 min, and more preferably 5 min.
In the present invention, the post-flotation preferably also obtains flotation coarse tailings, and the post-flotation preferably further comprises: scavenging the flotation coarse tailings to obtain scavenged concentrate; and returning the scavenging concentrate to perform flotation. In the present invention, the scavenging agent preferably comprises a primary collector and a secondary collector; the composition of the primary collector and the secondary collector is the same as the flotation reagent, and the details are not repeated. In the invention, when the scavenging is carried out, the addition amount of the main collector relative to the flotation coarse tailings is preferably 0-300 g/t, and more preferably 200-250 g/t; the addition amount of the secondary collector relative to the flotation coarse tailings is preferably 0-150 g/t, and more preferably 50-100 g/t.
In the present invention, the scavenging preferably includes: adding a main collector into the flotation coarse tailings, and stirring for 1-10 min; adding a secondary collecting agent, and stirring for 1-10 min; and (4) aerating and scavenging for 1-10 min to obtain scavenging concentrate.
In the present invention, flotation tailings are preferably also obtained after the scavenging.
After flotation rough concentrate is obtained, the invention carries out concentration on the flotation rough concentrate to obtain bulk concentrate. In the present invention, the concentration preferably includes a first concentration and a re-concentration which are performed in this order; the number of re-concentration is preferably 1 or more; and the concentration object of the re-concentration is the concentrate obtained by the last concentration. In the present invention, the selected agent is preferably water glass; the addition amount of the water glass relative to the flotation rough concentrate is preferably 0-300 g/t, and more preferably 50-200 g/t. In the specific embodiment of the invention, the flotation rough concentrate is poured into a flotation machine, water glass is added, stirring is carried out for 1-10 min, then air flotation is carried out for 1-10 min, and first concentration is completed; and pouring the concentrate subjected to the first concentration into a flotation machine, stirring for 0-5 min, and then performing air flotation for 1-10 min to finish the second concentration to obtain bulk concentrate.
In the invention, the tailings of the first concentration are returned to be floated; and returning the tailings subjected to the re-concentration to carry out the last concentration.
In the invention, the light component cyclone tailings with the granularity of plus 0.5mm, the table tailings, the centrifugal tailings and the flotation tailings are combined to obtain the total tailings.
The invention aims at the high cost of ore grinding and ore dressing when the raw ore of the alkaline granite rare earth ore is directly crushed, ground and sortedAnd the like, and by combining the characteristics of large specific gravity difference and low grade of main gangue minerals and useful minerals in the ores, the ore dressing process suitable for coarse grain tailing discarding of the alkaline granite rare earth ores is developed. Preferably, the invention aims at obtaining high-recovery and high-grade bulk concentrates, adopts the technical scheme of coarse grinding, tailing discarding and fine grinding flotation, after primary crushing of raw ores, adopts a high-pressure roller mill to finely crush the raw ores to below 1-3 mm, relieves the mud phenomenon of target minerals such as bastnaesite, xingan stone and the like in a mode of interlayer extrusion crushing of the high-pressure roller mill, divides the finely crushed ores into a plurality of granularities through a vibrating screen and a cyclone, and respectively carries out dense medium cyclone separation, table concentrator separation and centrifugal ore dressing on ores with different granularity: and (3) quickly separating light ore particles and heavy ore particles of ore with the size fraction of +0.5mm under a high-strength separation force field of a heavy medium cyclone, classifying the ore with the size fraction of 0.074-0.5 mm by using a table concentrator for fine separation, and strengthening the separation speed and effect of the ore particles with different specific gravities of the ore with the size fraction of 0.02-0.074 mm through a centrifugal and gravity composite force field. 53.76 percent of gangue minerals can be abandoned before the mixed flotation through discarding tailings in advance, the obtained gravity concentration rough concentrate coarse granularity (more than 0.074 mm) is further finely ground and dissociated, and the mixed flotation is carried out after the gravity concentration rough concentrate coarse granularity and the gravity concentration rough concentrate fine granularity are combined to obtain Rare Earth Oxide (REO) and ZrO2、Nb2O5And bulk concentrate of U. In a specific embodiment of the invention, the REO, ZrO2、Nb2O5And the grades of U are 17.065-18.122%, 24.36-48.90%, 6.21-7.73% and 0.259-0.753 respectively, and the recovery rates are 77.71-81.59%, 70.20-83.77%, 75.99-79.87% and 72.66-82.86% respectively.
The invention carries out discarding tailings in advance under the condition of coarse grain crushing and grinding to obtain coarse concentrate with high recovery rate, and then carries out flotation and deep separation on useful mineral aggregate and gangue mineral after selective dissociation to obtain high-grade bulk concentrate. The invention has the advantages of obviously reducing the grinding amount of ores, avoiding over grinding, saving the cost of grinding and flotation and the like. The technology can provide technical support for improving the economic benefit of the alkaline granite rare earth ore and promoting the green and efficient development of the ore deposit.
The technical solution of the present invention will be clearly and completely described below with reference to the embodiments of the present invention. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
The rare earth multi-metal ore (801 ore) is a typical alkaline granite rare earth ore deposit, the grades of main valuable elements REO, U, Nb and Zr in shallow ores (0-50 m) of the ore deposit are 0.995%, 0.016%, 0.37% and 3.02%, and main ore minerals are dahurian angelica stone, bastnaesite, monazite, zinc leucite, niobite, zircon, ilmenite and the like; the gangue minerals are quartz, albite, potash feldspar, natrii sulfas, calcite, etc. Useful minerals are usually in a fine particle shape (0.002-0.050 mm) and are embedded among gangue minerals with coarse particles (0.1-5 mm), hydrothermal alternating and alteration phenomena such as sodium feldspar, silicification and neon are serious during ore formation, the ore suffers from long-term weathering, the hardness of the ore is low, and the ore is easy to argillization in a fine grinding process.
The above-mentioned alkaline granite type rare earth ores, each weighing 20kg in weight, were taken and subjected to a test under the process flow shown in fig. 1.
(1) Crushing and grinding ores: firstly, crushing raw ore to be less than 10mm by a jaw crusher, crushing and grinding the ore with the particle size of-10 mm by a high-pressure roller mill, then passing through a high-frequency vibrating screen with the screen hole of 1.25mm, returning the product on the screen to the high-pressure roller mill for further treatment, and finally obtaining the ore with the particle size of-1.25 mm and the particle size of-0.074 mm accounting for 13 wt%.
(2) Grading the granularity of ore: the crushed and ground ore is sieved by high-frequency vibration to respectively obtain five particle sizes of +0.5mm, + 0.3-0.5 mm, + 0.15-0.3 mm, + 0.074-0.15 mm and-0.074 mm.
(3) Desliming of fine fraction ore:
adopting an FX phi 20 superfine classification hydrocyclone to desliming ore with the size of-0.074 mm under the condition that the feeding pressure is 0.1MPa, and separating ore mud with the size of-0.02 mm and ore sand with the size of +0.02 to-0.074 mm.
(4) +0.5mm size fraction ore dense medium cyclone separation
Preparing a dense medium suspension: and mixing the ferrosilicon powder with water and quickly stirring the mixture in a stirring tank until the mixture is suspended to obtain a suspension with the density of 1.90.
Preparation of separation ore pulp: adding the ore into the heavy medium suspension to obtain ore pulp with the ore concentration of about 15 wt%.
Heavy medium cyclone separation: and adding the ore pulp into an FX phi 250 heavy medium cyclone through a sand pump, adjusting the ore feeding pressure to be 0.12MPa, obtaining light component ore pulp from an overflow port of the heavy medium cyclone after the operation is stable, and obtaining heavy component ore pulp from a sand setting port at the bottom of the heavy medium cyclone.
Medium removal and screening: and (3) screening the light component ore pulp and the heavy component ore pulp by using a high-frequency vibrating screen with the aperture of 0.3mm respectively, wherein oversize products are light component cyclone tailings with the granularity of +0.5mm and heavy medium separation concentrate, and undersize products are heavy medium suspension liquid, and returning the heavy medium suspension liquid for recycling after sedimentation and thickening.
The radioactivity of the light component cyclone tailings with the granularity of plus 0.5mm is qualified through inspection, and the light component cyclone tailings can be used for building sand; the dense medium separation concentrate is tailing discarding rough concentrate, and high-grade concentrate can be obtained through further fine grinding separation.
(5) And the table concentrator reselection of + 0.074-0.5 mm size fraction ore:
adding water into ore with the grain size of + 0.3-0.5 mm to obtain ore pulp with the concentration of 20 wt%, uniformly stirring, pouring into a feeding end of a shaking table, adjusting the inclination angle and water flow of a bed surface to obtain shaking table concentrate and shaking table tailings, and controlling the yield of the concentrate to be 50 wt%.
Adding water into ore with the grain size of plus 0.15-minus 0.3mm to obtain ore pulp with the mass concentration of 25%, uniformly stirring, pouring the ore pulp into a feeding end of a shaking table, adjusting the inclination angle and water flow of a bed surface to obtain shaking table concentrate and shaking table tailings, and controlling the yield of the concentrate to be 40 wt%.
Adding water into ore with the grain size of plus 0.074-minus 0.15mm to obtain ore pulp with the mass concentration of 20%, uniformly stirring, pouring the ore pulp into a feeding end of a shaking table, adjusting the inclination angle and water flow of a bed surface to obtain shaking table concentrate and shaking table tailings, and controlling the yield of the concentrate to be 25 wt%.
(6) And the centrifugal gravity separation of ore with the size fraction of +0.02 to-0.074 mm:
mixing the ore sand with the granularity of plus 0.02-minus 0.074mm obtained in the step (3) with proper amount of water to obtain ore pulp with the concentration of 20 wt%, adding 1000G/t of water glass as a dispersing agent, uniformly feeding the ore pulp into a feeding funnel of a Nielsen centrifugal concentrator, adjusting the centrifugal strength to 60G, the feeding speed to be 1.2kg/min, the reverse flushing water pressure to be 0.04MPa and the fluidization water amount to be 1.5kg/min to obtain centrifugal concentrate and centrifugal tailings.
(7) Product combination: and (3) combining all the concentrates in the steps (4) and (5) to obtain gravity coarse concentrate, combining the centrifugal concentrate in the step (6) and the slime with the granularity of-0.02 mm in the step (3) to obtain slime concentrate, and combining the tailings in the steps (4), (5) and (6) to obtain gravity tailings.
(8) Re-grinding the gravity-separated rough concentrate: and adding water into the gravity-selected rough concentrate in the previous step to prepare ore pulp with the concentration of 25 wt%, and regrinding the ore pulp by adopting an attritor mill until the granularity of-0.074 mm accounts for 90 wt% to obtain the ore powder concentrate.
(9) Mixing, floating and size mixing: and (3) combining the ground ore powder concentrate obtained in the step (8) and the slime concentrate obtained in the step (7) to obtain mixed flotation raw ore, wherein the ore granularity of the mixed flotation raw ore is-0.074 mm, the ore pulp concentration is adjusted to 30 wt% by adding water, the mixture is placed in a flotation machine and stirred uniformly, and the ore pulp temperature is adjusted to 50 ℃.
(10) Preparing a main collector:
firstly, mixing RA935, oxidized paraffin soap and p-tert-butyl benzene hydroxamic acid in parts by weight of 45: 35: 20 to obtain the main material.
Adding triethanolamine serving as an emulsifier into the main material, wherein the mass of the triethanolamine is 10% of that of the main material, and then continuously adding 1 wt% of NaOH aqueous solution to obtain the main collector with the main material content of 5 wt%.
(11) Preparing a secondary collecting agent: dissolving dodecyl amino bis (methylene phosphonic acid) by using 1 wt% of NaOH aqueous solution to obtain the secondary collector with the concentration of 5 wt%.
(12) Adding a regulator:
adding Na into the mixed flotation raw ore pulp2CO3The total amount of the mixed flotation raw ore is 1000g/t, and the mixed flotation raw ore is stirred for 2 min.
Adding water glass into the ore pulp after the last step, wherein the using amount of the added water glass is 1600g/t relative to the mixed flotation raw ore, and stirring for 2 min.
After the last step with H2SO4The pH value of the ore pulp is adjusted to 8.8 by the solution and NaOH solution.
(13) Adding a main collector: and (3) adding the main collector in the step (10), and stirring for 3min for fully reacting the minerals such as rare earth, niobium, zirconium and the like with the collector, wherein the using amount of the main collector is 400g/t relative to that of the mixed flotation raw ore.
(14) Adding a secondary collector: and (3) adding the auxiliary collecting agent in the step (11), and stirring for 3min, wherein the using amount of the auxiliary collecting agent is 200g/t relative to that of the mixed flotation raw ore, so that the auxiliary collecting agent and the useful mineral are fully reacted, and the main collecting agent and the auxiliary collecting agent are jointly adsorbed on the target mineral.
(15) Flotation of useful minerals: and opening an air inlet valve, generating a large amount of bubbles in the flotation tank, floating to the surface of the ore pulp, scraping out the bubbles, and performing flotation for 5min to obtain flotation rough concentrate and flotation rough tailings.
(16) Useful minerals are scavenged: adding the main collector in the step (10) into the flotation coarse tailings, wherein the using amount is 200g/t, and stirring for 3 min; adding 100g/t of the auxiliary collecting agent in the step (11), and stirring for 3 min; and (4) aerating and scavenging for 4min to obtain scavenged concentrate and flotation tailings, and returning the scavenged concentrate to the flotation process.
(17) And (3) concentrating useful minerals: pouring the flotation rough concentrate obtained in the step (15) into a flotation machine, adding 200g/t of water glass, stirring for 2min, and then performing air flotation for 4min to finish first concentration; and returning the tailings of the first concentration to the flotation process, pouring the concentrate of the first concentration into a flotation machine, stirring for 1min, performing aerated flotation for 4min to finish the second concentration, and returning the tailings of the second concentration to the first concentration process.
(18) Product treatment: and (3) combining the concentrate of the second concentration in the last step into final mixed concentrate, and combining the gravity tailings in the step (7) and the flotation tailings in the step (16) to obtain total tailings.
Example 1 the results of the test are shown in table 1.
Table 1 test results of example 1
Figure BDA0003247117630000141
Comparative example 1
The effect of direct mixed flotation of the internal Mongolian Gubal hucho alkaline granite rare earth ore which is taken by a plurality of parts with the weight of 20kg in the example 1 is different from that of the comparison raw ore in the example 1.
(1) Crushing raw ore to below 10mm by using a jaw crusher, crushing and grinding the ore with the size of-10 mm by using a high-pressure roller mill, passing through a high-frequency vibrating screen with the screen hole of 1.25mm, and returning the product on the screen to the high-pressure roller mill for reprocessing to finally obtain the ore with the size of-1.25 mm.
(2) The ore is directly reground by a vertical ball mill without size classification until the fineness is the same as that of the mixed flotation raw ore (9) in the example 1, namely, the-0.074 mm particle size accounts for 95 wt%. Adding water to adjust the concentration of the ore pulp to 30 wt%, placing the ore pulp into a flotation machine, uniformly stirring, and adjusting the temperature of the ore pulp to 50 ℃.
The other conditions were the same as in (10) to (17) in example 1, and flotation bulk concentrate and total tailings were obtained, and the test results of comparative example 1 are shown in table 2.
Table 2 test results of comparative example 1
Figure BDA0003247117630000151
Example 2
The inner Mongolia copal taimen uranium rare earth multi-metal ore (801 ore) is a typical alkaline granite rare earth ore deposit, the average grade of main valuable elements REO, U, Nb and Zr in deep ores (50-100 m) of the ore deposit is 0.762%, 0.013%, 0.28% and 2.95%, and main ore minerals are Xingan stone, bastnaesite, monazite, zinc solar garnet, niobite, zircon, ilmenite and the like; the gangue minerals are quartz, albite, potash feldspar, natrii sulfas, calcite, etc. Useful minerals are usually in a fine particle shape (0.002-0.050 mm) and are embedded among gangue minerals with coarse particles (0.1-5 mm), the weathering degree of the ores is weak, but due to the serious hydrothermal alternation phenomena such as sodermanization, silicification and neon during the mineralization, the hardness of the ores is low, and the useful minerals are easy to be over-grinded into mud.
The above-mentioned alkaline granite type rare earth ores, each weighing 20kg in weight, were taken and subjected to a test under the process flow shown in fig. 1.
(1) Crushing and grinding ores: firstly, crushing raw ore to be less than 10mm by a jaw crusher, crushing and grinding the ore with the particle size of-10 mm by a high-pressure roller mill, then passing through a high-frequency vibrating screen with the screen hole of 2.0mm, returning the product on the screen to the high-pressure roller mill for further treatment, and finally obtaining the ore with the particle size of-0.074 mm, wherein the particle size accounts for 9 wt%.
(2) Grading the granularity of ore: the crushed and ground ore is sieved by high-frequency vibration to respectively obtain five particle sizes of +0.5mm, + 0.3-0.5 mm, + 0.15-0.3 mm, + 0.074-0.15 mm and-0.074 mm.
(3) Desliming of fine fraction ore:
adopting an FX phi 20 superfine classification hydrocyclone to desliming ore with the size of-0.074 mm under the condition that the feeding pressure is 0.12MPa, and separating ore mud with the size of-0.02 mm and ore sand with the size of +0.02 to-0.074 mm.
(4) +0.5mm size fraction ore dense medium cyclone separation
Preparing a dense medium suspension: and mixing the ferrosilicon powder with water and quickly stirring the mixture in a stirring tank until the mixture is suspended to obtain a suspension with the density of 1.95.
Preparation of separation ore pulp: adding the ore into the heavy medium suspension to obtain ore pulp with the concentration of about 10 wt%.
Heavy medium cyclone separation: and adding the ore pulp into an FX phi 250 heavy medium cyclone through a sand pump, adjusting the ore feeding pressure to be 0.14MPa, obtaining light component ore pulp from an overflow port of the heavy medium cyclone after the operation is stable, and obtaining heavy component ore pulp from a sand setting port at the bottom of the heavy medium cyclone.
Medium removal and screening: and (3) screening the light component ore pulp and the heavy component ore pulp by using a high-frequency vibrating screen with the aperture of 0.3mm respectively, wherein oversize products are light component cyclone tailings with the granularity of +0.5mm and heavy medium separation concentrate, and undersize products are heavy medium suspension liquid, and returning the heavy medium suspension liquid for recycling after sedimentation and thickening.
The radioactivity of the light component cyclone tailings with the granularity of plus 0.5mm is qualified through inspection, and the light component cyclone tailings can be used for building sand; the dense medium separation concentrate is tailing discarding rough concentrate, and high-grade concentrate can be obtained through further fine grinding separation.
(5) And the table concentrator reselection of + 0.074-0.5 mm size fraction ore:
adding water into ore with the grain size of plus 0.3-minus 0.5mm to obtain ore pulp with the concentration of 15 wt%, uniformly stirring, pouring the ore pulp into a table concentrator feeding end, adjusting the inclination angle and water flow of a bed surface to obtain table concentrator concentrate and table concentrator tailings, and controlling the yield of the concentrate to be 25 wt%.
Adding water into ore with the grain size of plus 0.15-minus 0.3mm to obtain ore pulp with the concentration of 25 wt%, uniformly stirring, pouring the ore pulp into a feeding end of a shaking table, adjusting the inclination angle and water flow of a bed surface to obtain shaking table concentrate and shaking table tailings, and controlling the yield of the concentrate to be 23 wt%.
Adding water into ore with the grain size of plus 0.074-minus 0.15mm to obtain ore pulp with the concentration of 20 wt%, uniformly stirring, pouring the ore pulp into a feeding end of a shaking table, adjusting the inclination angle and water flow of a bed surface to obtain shaking table concentrate and shaking table tailings, and controlling the yield of the concentrate to be 20 wt%.
(6) And the centrifugal gravity separation of ore with the size fraction of +0.02 to-0.074 mm:
mixing the ore sand with the granularity of plus 0.02-minus 0.074mm obtained in the step (3) with proper amount of water to obtain ore pulp with the concentration of 30 wt%, adding 1500G/t of sodium hexametaphosphate as a dispersing agent, uniformly feeding the ore pulp into a feeding funnel of a Nielsen centrifugal concentrator, adjusting the centrifugal strength to be 50G, the feeding speed to be 1.0kg/min, the reverse flushing water pressure to be 0.03MPa and the fluidization water amount to be 1.2kg/min to obtain centrifugal concentrate and centrifugal tailings.
(7) Product combination: and (3) combining all the concentrates in the steps (4) and (5) to obtain gravity coarse concentrate, combining the centrifugal concentrate in the step (6) and the slime with the granularity of-0.02 mm in the step (3) to obtain slime concentrate, and combining the tailings in the steps (4), (5) and (6) to obtain gravity tailings.
(8) Re-grinding the gravity-separated rough concentrate: and adding water into the gravity concentration rough concentrate in the previous step to prepare ore pulp with the concentration of 30 wt%, and regrinding the ore pulp by adopting an upright ball mill until the granularity of-0.074 mm accounts for 92 wt% to obtain the ground ore concentrate.
(9) Mixing, floating and size mixing: and (3) merging the ground ore powder concentrate obtained in the step (8) and the slime concentrate obtained in the step (7) to obtain a mixed flotation raw ore, wherein the ore granularity of the mixed flotation raw ore is-0.074 mm and accounts for 98 wt%, the concentration of the ore pulp is adjusted to 25 wt%, the mixed flotation raw ore is placed in a flotation machine and is uniformly stirred, and the temperature of the ore pulp is adjusted to 40 ℃.
(10) Preparing a main collector:
mixing RA935, oxidized paraffin soap and p-tert-butyl benzene hydroxamic acid according to the mass portion ratio of 50:38:12 to obtain a main material.
Adding triethanolamine serving as an emulsifier into the main material, wherein the mass of the triethanolamine is 5% of that of the main material, and then continuously adding 2 wt% of NaOH aqueous solution to obtain the main collector with the main material content of 1 wt%.
(11) Preparing a secondary collecting agent: dissolving dodecyl amino bis (methylene phosphonic acid) by using 1 wt% of NaOH aqueous solution to obtain the 1 wt% of auxiliary collector.
(12) Adding a regulator:
adding Na into the mixed flotation raw ore pulp2CO3The total amount of the mixed flotation crude ore is 800g/t, and the mixed flotation crude ore is stirred for 2 min.
Adding sodium hexametaphosphate into the ore pulp after the last step, wherein the using amount of the sodium hexametaphosphate is 1200g/t relative to the mixed flotation raw ore, and stirring for 2 min.
After the last step with H2SO4The pH value of the ore pulp is adjusted to 8.9 by the solution and NaOH solution.
(13) Adding a main collector: and (3) adding the main collector in the step (10) after the last step, and stirring for 3min, wherein the dosage of the main collector is 600g/t relative to the dosage of the mixed flotation raw ore.
(14) Adding a secondary collector: and adding the secondary collector after the last step, and stirring for 3min, wherein the dosage of the secondary collector is 200g/t relative to the dosage of the mixed flotation raw ore.
(15) Flotation of useful minerals: and opening an air inlet valve, generating a large amount of bubbles in the flotation tank, floating to the surface of the ore pulp, scraping out the bubbles, and performing flotation for 5min to obtain flotation rough concentrate and flotation rough tailings.
(16) Useful minerals are scavenged: adding the main collector in the step (10) into the flotation coarse tailings, wherein the using amount is 300g/t, and stirring for 3 min; adding 50g/t of the auxiliary collecting agent in the step (11), and stirring for 3 min; and (4) aerating and scavenging for 4min to obtain scavenged concentrate and flotation tailings, and returning the scavenged concentrate to the flotation process.
(17) And (3) concentrating useful minerals: pouring the flotation rough concentrate obtained in the step (15) into a flotation machine, adding water glass at 300g/t, stirring for 2min, and then performing air flotation for 4min to finish first concentration; and returning the tailings of the first concentration to the flotation process, pouring the concentrate of the first concentration into a flotation machine, stirring for 2min, performing aerated flotation for 4min to finish the second concentration, and returning the tailings of the second concentration to the first concentration process.
(18) Product treatment: and (3) combining the concentrate of the second concentration in the last step into final mixed concentrate, and combining the gravity tailings in the step (7) and the flotation tailings in the step (16) to obtain total tailings.
The test results of example 2 are shown in table 3.
Table 3 test results of example 2
Figure BDA0003247117630000181
Example 3
The Xinjiang Behcet cumin super-large REE-Nb-Ta-Zr deposit is a super-large alkaline granite rare earth deposit, the main valuable elements in the deposit are REO (0.124%), Nb (0.056%), Ta (0.005%) and Zr (0.16%), and the ore is in a sparse dip-dyed structure and occasionally has a fine vein dip-dyed structure. The ore minerals (3-4%) are mainly pyrochlore, secondarily zircon, monazite, xenotime, thorite, silicocalcinatrite and the like, the gangue minerals (97-96%) are mainly albite, microcline and quartz, and a small amount of neon, ulnar, a small amount of ilmenite, magnetite, apatite and the like.
Several parts of alkaline granite rare earth ore, 40kg in weight, were taken separately and tested under the process flow shown in fig. 1.
(1) Crushing and grinding ores: firstly, crushing blocky raw ores to be less than 10mm by a jaw crusher, then forming a closed system by using a high-pressure roller mill and a high-frequency vibrating screen, crushing and grinding the ores with the particle size of-10 mm by the high-pressure roller mill, then passing through the high-frequency vibrating screen with the screen hole of 2.5mm, returning the products on the screen to the high-pressure roller mill for reprocessing, and finally obtaining the ores with the particle size of-0.074 mm accounting for 10 wt%, and realizing selective dissociation between useful minerals (aggregates) and gangue minerals and simultaneously reducing argillization by closed circuit grinding.
(2) Grading the granularity of ore: the crushed and ground ore is sieved by high-frequency vibration to respectively obtain five particle sizes of +0.5mm, + 0.3-0.5 mm, + 0.15-0.3 mm, + 0.074-0.15 mm and-0.074 mm.
(3) Desliming of fine fraction ore:
and (2) adopting an FX phi 20 superfine classification hydrocyclone to desliming-0.074 mm size fraction ore under the condition that the feeding pressure is 0.09MPa, so as to obtain-0.02 mm size ore mud and 0.02-0.074 mm size ore sand.
(4) +0.5mm size fraction ore dense medium cyclone separation
Preparing a dense medium suspension: mixing ferrosilicon powder with water and quickly stirring in a stirring tank until the ferrosilicon powder is suspended to obtain a suspension with the density of 1.95;
preparation of separation ore pulp: adding the ore into the heavy medium suspension to obtain ore pulp with the concentration of about 10 wt%.
Heavy medium cyclone separation: and feeding the ore pulp into an FX phi 250 heavy medium cyclone through a sand pump, adjusting the feeding pressure to be 0.15MPa, obtaining light component ore pulp from an overflow port of the heavy medium cyclone after the operation is stable, and obtaining heavy component ore pulp from a sand setting port at the bottom of the heavy medium cyclone.
Medium removal and screening: and respectively sieving the light component ore pulp and the heavy component ore pulp through a high-frequency vibrating screen with the aperture of 0.3mm, wherein oversize products are light component cyclone tailings with the granularity of +0.5mm and heavy medium separation concentrate, and undersize products are heavy medium suspension liquid, and returning for recycling after sedimentation and thickening.
(5) And the table concentrator reselection of + 0.074-0.5 mm size fraction ore:
adding water into ore with the grain size of plus 0.3-minus 0.5mm to obtain ore pulp with the concentration of 15 wt%, uniformly stirring, pouring the ore pulp into a feeding end of a shaking table, adjusting the inclination angle and water flow of a bed surface to obtain shaking table concentrate and shaking table tailings, and controlling the yield of the concentrate to be 30 wt%.
Adding water into ore with the grain size of + 0.15-0.3 mm to obtain ore pulp with the concentration of 20 wt%, uniformly stirring, pouring the ore pulp into a feeding end of a shaking table, adjusting the inclination angle and water flow of a bed surface to obtain shaking table concentrate and shaking table tailings, and controlling the yield of the concentrate to be 20 wt%.
Adding water into ore with the grain size of plus 0.074-minus 0.15mm to obtain ore pulp with the concentration of 20 wt%, uniformly stirring, pouring the ore pulp into a table concentrator feeding end, adjusting the inclination angle and water flow of a bed surface to obtain table concentrator concentrate and table concentrator tailings, and controlling the yield of the concentrate to be 15 wt%.
(6) And the centrifugal gravity separation of ore with the size fraction of +0.02 to-0.074 mm:
mixing the ore sand with the granularity of plus 0.02-minus 0.074mm obtained in the step (3) with proper amount of water to obtain ore pulp with the concentration of 20 wt%, adding 800G/t of water glass as a dispersing agent, uniformly feeding the ore pulp into a feeding funnel of a Nielsen centrifugal concentrator, adjusting the centrifugal strength to 70G, the feeding speed to be 1.6kg/min, the reverse flushing water pressure to be 0.05MPa and the fluidization water amount to be 3kg/min, and obtaining centrifugal concentrate and centrifugal tailings.
(7) Product combination: and (3) combining all the concentrates in the steps (4) and (5) to obtain gravity coarse concentrate, combining the centrifugal concentrate in the step (6) and the slime with the granularity of-0.02 mm in the step (3) to obtain slime concentrate, and combining the tailings in the steps (4), (5) and (6) to obtain gravity tailings.
(8) Re-grinding the gravity-separated rough concentrate: and adding water into the gravity concentration rough concentrate in the previous step to prepare ore pulp with the concentration of 40 wt%, and regrinding the ore pulp by adopting an upright ball mill until the granularity of-0.074 mm accounts for 95 wt% to obtain the ground ore powder concentrate.
(9) Mixing, floating and size mixing: and (3) merging the ground ore powder concentrate in the step (8) and the slime concentrate in the step (7) to obtain a mixed flotation raw ore, wherein the ore granularity of the mixed flotation raw ore is-0.074 mm, the ratio is 98.5 wt%, the concentration of the ore pulp is adjusted to 25 wt%, the mixed flotation raw ore is placed in a flotation machine and is uniformly stirred, and the temperature of the ore pulp is adjusted to 45 ℃.
(10) Preparing a main collector:
mixing RA935, oxidized paraffin soap and p-tert-butyl benzene hydroxamic acid according to the mass ratio of 42:38:20 to obtain a main material.
Adding an emulsifier triethanolamine into the main material, wherein the mass of the triethanolamine is 8% of that of the main material, and then continuously adding 3 wt% of NaOH aqueous solution to obtain a main collector solution with the main material content of 10 wt%.
(11) Preparing a secondary collecting agent: and dissolving dodecyl amino bis (methylene phosphonic acid) by using 0.5 wt% of NaOH aqueous solution to obtain the secondary collector with the concentration of 5 wt%.
(12) Adding a regulator:
adding NaHCO into the mixed flotation raw ore pulp3The total amount of the coarse ore is 1200g/t, and the mixture is stirred for 3 min.
Adding sodium hexametaphosphate into the ore pulp after the last step, wherein the using amount of the sodium hexametaphosphate is 1400g/t relative to the raw ore for flotation, and stirring for 3 min.
After the last step with H2SO4The solution and NaOH solution adjust the pH value of the ore pulp to 9.1.
(13) Adding a main collector: and (3) adding the main collector in the step (10) after the previous step, and stirring for 4min, wherein the dosage of the main collector is 500g/t relative to the dosage of the mixed flotation raw ore.
(14) Adding a secondary collector: and adding a secondary collector after the last step, and stirring for 4min, wherein the dosage of the secondary collector is 120g/t relative to the dosage of the mixed flotation raw ore.
(15) And (3) air flotation: and opening an air inlet valve, generating a large amount of bubbles in the flotation tank, floating to the surface of the ore pulp, scraping out the bubbles, and performing flotation for 6min to obtain flotation rough concentrate and flotation rough tailings.
(16) Useful minerals are scavenged: adding the main collector in the step (10) into the flotation coarse tailings, wherein the dosage is 250g/t, and stirring for 4 min; adding 50g/t of the auxiliary collecting agent in the step (11), and stirring for 4 min; and (4) aerating and scavenging for 4min to obtain scavenged concentrate and flotation tailings, and returning the scavenged concentrate to the flotation process.
(17) And (3) concentrating useful minerals: pouring the flotation rough concentrate obtained in the step (15) into a flotation machine, adding 50g/t of water glass, stirring for 3min, and then performing air flotation for 4min to finish first concentration; and returning the tailings of the first concentration to the flotation process, pouring the concentrate of the first concentration into a flotation machine, stirring for 2min, performing aerated flotation for 4min to finish the second concentration, and returning the tailings of the second concentration to the first concentration process.
(18) Product treatment: and (3) combining the concentrate of the second concentration in the last step into final mixed concentrate, and combining the gravity tailings in the step (7) and the flotation tailings in the step (16) to obtain total tailings.
The test results of example 3 are shown in Table 4.
Table 4 test results of example 3
Figure BDA0003247117630000211
It can be seen from the above examples and comparative examples that the invention has developed a process suitable for coarse grain gravity separation tailing discarding and gravity separation coarse concentrate regrinding flotation of alkaline granite type rare earth ore. Through the technical scheme of 'coarse grinding, tailing discarding and fine grinding and flotation', raw ores are crushed by a jaw crusher and finely crushed by a high-pressure roller mill, the ores are divided into a plurality of granularities, and the advanced tailing discarding of ores with the granularity of +0.5mm, + 0.074-/-0.5 mm and + 0.02-/-0.074 mm is realized by a heavy medium cyclone, a shaking table and a centrifugal concentrator respectively, so that the advanced tailing discarding with almost full granularity under the condition of coarse grinding is realized, and 53.76 percent of gangue minerals are discarded before mixed flotation. After the coarse particle size (more than 0.074 mm) of gravity concentration rough concentrate is further finely ground, the deep separation between useful mineral aggregate and gangue mineral is realized through flotation, and Rare Earth Oxide (REO) and ZrO are obtained2、Nb2O5And bulk concentrate of U. In a specific embodiment of the invention, the REO, ZrO2、Nb2O5And the grades of U are 17.065-18.122%, 24.36-48.90%, 6.21-7.73% and 0.259-0.753 respectively, and the recovery rates are 77.71-81.59%, 70.20-83.77%, 75.99-79.87% and 72.66-82.86% respectively. Compared with the prior art of direct fine grinding and sorting, the method has the advantages of remarkably reducing the ore amount entering the grinding and subsequent ore dressing processes, saving the cost of grinding, ore dressing, equipment energy consumption and the like, avoiding over-grinding argillization, having better mixed concentrate sorting indexes and providing technical support for improving the economic benefit of the alkaline granite rare earth ore.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.

Claims (10)

1. A pre-tailing-discarding mixed flotation method for rare earth multi-metal ores comprises the following steps:
crushing and screening raw ores to obtain five-grade ores; the five-grade ore is +0.5mm grade ore, + 0.3-0.5 mm grade ore, + 0.15-0.3 mm grade ore, + 0.074-0.15 mm grade ore and-0.074 mm grade ore;
carrying out dense medium cyclone separation on the ore with the size fraction of +0.5mm to obtain dense medium separation concentrate;
respectively carrying out table reselection on the ore with the size fraction of + 0.3-0.5 mm, the ore with the size fraction of + 0.15-0.3 mm and the ore with the size fraction of + 0.074-0.15 mm to obtain table concentrate;
carrying out desliming-centrifugal gravity separation treatment on the ore with the size fraction of-0.074 mm to obtain ore mud concentrate;
performing flotation on the dense medium separation concentrate, the table concentrate and the slime concentrate to obtain flotation rough concentrate;
and carrying out fine concentration on the flotation rough concentrate to obtain bulk concentrate.
2. The method according to claim 1, characterized in that the raw ore is derived from alkaline granite-type rare earth deposits.
3. The method of claim 1 or 2, wherein the crushing and screening comprises: crushing raw ores to be less than 10mm, forming a closed system by using a high-pressure roller mill and a high-frequency vibrating screen, crushing ores with the granularity of-10 mm by using the high-pressure roller mill, passing through the high-frequency vibrating screen with the screen holes of 1-3 mm, and returning screened products to the high-pressure roller mill for reprocessing to finally obtain ores with the granularity of 1-3 mm, wherein the proportion of the-0.074 mm in granularity is not more than 15 wt%; and screening the ore with the particle size of less than 1-3 mm to obtain five-particle-size ore.
4. The method of claim 1, wherein the table concentrate yields obtained from table reselection of +0.3 to-0.5 mm size fraction ore, +0.15 to-0.3 mm size fraction ore and +0.074 to-0.15 mm size fraction ore are independently 20 to 60 wt%.
5. The method of claim 1, wherein the desliming-centrifugal gravity separation process comprises: carrying out desliming treatment on the ore with the size fraction of-0.074 mm, and separating ore mud with the size of-0.02 mm and ore sand with the size of +0.02 to-0.074 mm; carrying out centrifugal gravity separation on the sand with the granularity of plus 0.02-minus 0.074mm to obtain centrifugal concentrate; and combining the slime with the granularity of-0.02 mm and the centrifugal concentrate to obtain slime concentrate.
6. The method of claim 5, wherein the agent of centrifugal gravity separation comprises water glass or sodium hexametaphosphate.
7. The method of claim 1, wherein the dense media sort concentrate and the table concentrate are ground and then floated.
8. The method according to claim 1 or 7, wherein flotation coarse tailings are also obtained after the flotation, and the method further comprises the following steps: scavenging the flotation coarse tailings to obtain scavenged concentrate; and returning the scavenging concentrate to perform flotation.
9. The method of claim 1, wherein the flotation reagent comprises a primary collector and a secondary collector; the main collector comprises RA935, oxidized paraffin soap and p-tert-butyl benzene hydroxamic acid; the secondary collector comprises a dodecylamine-based bis (methylene phosphonic acid) solution.
10. The method according to claim 1, characterized in that said beneficiation comprises a first beneficiation and a re-beneficiation carried out in sequence; the re-concentration times are more than 1; and the concentration object of the re-concentration is the concentrate obtained by the last concentration.
CN202111036365.6A 2021-09-06 2021-09-06 Pre-tailing-throwing mixed flotation method for rare earth multi-metal ore Active CN113731627B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202111036365.6A CN113731627B (en) 2021-09-06 2021-09-06 Pre-tailing-throwing mixed flotation method for rare earth multi-metal ore

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202111036365.6A CN113731627B (en) 2021-09-06 2021-09-06 Pre-tailing-throwing mixed flotation method for rare earth multi-metal ore

Publications (2)

Publication Number Publication Date
CN113731627A true CN113731627A (en) 2021-12-03
CN113731627B CN113731627B (en) 2023-06-09

Family

ID=78735743

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202111036365.6A Active CN113731627B (en) 2021-09-06 2021-09-06 Pre-tailing-throwing mixed flotation method for rare earth multi-metal ore

Country Status (1)

Country Link
CN (1) CN113731627B (en)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114618649A (en) * 2022-03-21 2022-06-14 中南大学 Method for selecting ore enrichment platinum group metal from spent automobile catalyst
CN115069400A (en) * 2022-06-28 2022-09-20 中国铝业股份有限公司 Treatment method of gibbsite type bauxite
CN115254398A (en) * 2022-09-01 2022-11-01 山东黄金矿业科技有限公司选冶实验室分公司 Method for pre-selecting and discarding gold ores and reducing excessive grinding
CN115254398B (en) * 2022-09-01 2024-06-07 山东黄金矿业科技有限公司选冶实验室分公司 Method for pre-dressing waste disposal and overgrinding reduction of gold ore

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103962232A (en) * 2014-05-08 2014-08-06 广东省工业技术研究院(广州有色金属研究院) Rare earth ore beneficiation method
CN110639690A (en) * 2019-10-14 2020-01-03 广东省资源综合利用研究所 Beneficiation method for high-mud micro-fine particle rare earth minerals
CN110976096A (en) * 2019-11-15 2020-04-10 南华大学 Beneficiation method for rare earth ore
CN111530620A (en) * 2020-04-24 2020-08-14 核工业北京化工冶金研究院 Beneficiation, separation and enrichment method for complex multi-metal rare earth ore
CN111530634A (en) * 2020-04-24 2020-08-14 核工业北京化工冶金研究院 Flotation method of alkaline granite type rare earth ore
CN112156884A (en) * 2020-08-07 2021-01-01 核工业北京化工冶金研究院 Pretreatment method for high-acid-consumption difficult-leaching volcanic-type uranium ore
CN112958270A (en) * 2021-02-01 2021-06-15 核工业北京化工冶金研究院 Comprehensive recovery method of uranium-containing low-grade polymetallic ore
CN113333181A (en) * 2021-06-18 2021-09-03 核工业北京化工冶金研究院 Flotation method for severely weathered rare earth ore
CN113333155A (en) * 2021-06-18 2021-09-03 核工业北京化工冶金研究院 Beneficiation method for recycling uranium from rare earth ore

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103962232A (en) * 2014-05-08 2014-08-06 广东省工业技术研究院(广州有色金属研究院) Rare earth ore beneficiation method
CN110639690A (en) * 2019-10-14 2020-01-03 广东省资源综合利用研究所 Beneficiation method for high-mud micro-fine particle rare earth minerals
CN110976096A (en) * 2019-11-15 2020-04-10 南华大学 Beneficiation method for rare earth ore
CN111530620A (en) * 2020-04-24 2020-08-14 核工业北京化工冶金研究院 Beneficiation, separation and enrichment method for complex multi-metal rare earth ore
CN111530634A (en) * 2020-04-24 2020-08-14 核工业北京化工冶金研究院 Flotation method of alkaline granite type rare earth ore
CN112156884A (en) * 2020-08-07 2021-01-01 核工业北京化工冶金研究院 Pretreatment method for high-acid-consumption difficult-leaching volcanic-type uranium ore
CN112958270A (en) * 2021-02-01 2021-06-15 核工业北京化工冶金研究院 Comprehensive recovery method of uranium-containing low-grade polymetallic ore
CN113333181A (en) * 2021-06-18 2021-09-03 核工业北京化工冶金研究院 Flotation method for severely weathered rare earth ore
CN113333155A (en) * 2021-06-18 2021-09-03 核工业北京化工冶金研究院 Beneficiation method for recycling uranium from rare earth ore

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
张金山等: "我国稀土选矿联合工艺的发展现状", 《中国矿业》 *
熊述清: "四川某地稀土矿重浮联合选矿试验研究", 《矿产综合利用》 *

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114618649A (en) * 2022-03-21 2022-06-14 中南大学 Method for selecting ore enrichment platinum group metal from spent automobile catalyst
CN115069400A (en) * 2022-06-28 2022-09-20 中国铝业股份有限公司 Treatment method of gibbsite type bauxite
CN115254398A (en) * 2022-09-01 2022-11-01 山东黄金矿业科技有限公司选冶实验室分公司 Method for pre-selecting and discarding gold ores and reducing excessive grinding
CN115254398B (en) * 2022-09-01 2024-06-07 山东黄金矿业科技有限公司选冶实验室分公司 Method for pre-dressing waste disposal and overgrinding reduction of gold ore

Also Published As

Publication number Publication date
CN113731627B (en) 2023-06-09

Similar Documents

Publication Publication Date Title
CN102500462B (en) Rutile roughing technology consisting of selective ore grinding, coarse particle gravity separation and fine particle floatation
CN108787158B (en) Recovery beneficiation method for micro-fine particle ore in uranium-containing polymetallic ore
CN109604048B (en) Method for stepwise recovering metallic copper, copper sulfide and iron minerals in copper converter slag
CN101733194B (en) Ore dressing method of low-grade manganese carbonate ore
CN101693222A (en) Method for separating oolitic hematite
CN113731627A (en) Pre-tailing-discarding mixed flotation method for rare earth multi-metal ore
CN103263977B (en) Process for recovering iron and rare earth in baotite low-intensity magnetic separation tailings
CN102357400A (en) Method for processing low-grade kaolinite ore
CN105944825B (en) A kind of ore dressing and desiliconizing enrichment method of Fine Hematite Ore
CN111715399B (en) Pretreatment method of high-calcium high-magnesium fine-particle embedded scheelite
CN111389598B (en) Method for recovering mica and feldspar quartz from rare metal ore dressing tailings
CN109453891A (en) A kind of high sesquialter collophane spiral chute floats process integration again
CN113333155B (en) Beneficiation method for recycling uranium from rare earth ore
CN106964480B (en) A kind of fine grinding sorted suitable for micro fine particle magnetite stone-hierarchical composition new process
CN109647616B (en) Method for comprehensively recovering magnetite and copper minerals from copper slag flotation tailings
CN109894256A (en) Low-grade iron ore powder mentions iron and drops miscellaneous beneficiation method
CN115178363B (en) Ultra-high purity quartz powder prepared from mudstone-containing quartz rock and comprehensive utilization process
CN103272698A (en) Mineral separation process for recycling iron and rare earth in baotite magnetite flotation tailings
CN110961244B (en) Method for pre-enriching vanadium-containing minerals in medium-fine scale graphite ores
CN106269212A (en) A kind of magnetic separation grading system is for the method for extraction of superpure concentrate of magnetite
CN112024120A (en) Beneficiation method for micro-fine-particle-grade hematite and limonite
CN108580022B (en) Mineral processing technology for producing chemical-grade chromite concentrate
CN109261372A (en) A kind of method of substep recycling fluorite and barite
CN108144743B (en) Using the low-grade uranium ferro-boron associated minerals ore-dressing technique method of high-pressure roller mill
CN107913802A (en) It is a kind of from the method for selecting the recycling fluorite of flotation in tin tailings

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant