CN219252883U - Ore dressing system for efficiently recycling valuable components from low-grade zinc oxide ores - Google Patents
Ore dressing system for efficiently recycling valuable components from low-grade zinc oxide ores Download PDFInfo
- Publication number
- CN219252883U CN219252883U CN202320068492.2U CN202320068492U CN219252883U CN 219252883 U CN219252883 U CN 219252883U CN 202320068492 U CN202320068492 U CN 202320068492U CN 219252883 U CN219252883 U CN 219252883U
- Authority
- CN
- China
- Prior art keywords
- flotation
- outlet
- hydrocyclone
- scavenging
- zinc oxide
- 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.)
- Active
Links
Images
Classifications
-
- 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
Abstract
The utility model relates to a mineral separation system for efficiently recycling valuable components from low-grade zinc oxide ores, wherein a jaw crusher is connected with a vibrating screen, a discharge hole of a screen material on the vibrating screen is connected with a ball mill, the discharge hole of the ball mill is connected with a No. 2 hydrocyclone, a slurry precipitation outlet of the No. 2 hydrocyclone is connected with the ball mill, an overflow outlet of the No. 2 hydrocyclone is connected with a stirring barrel A, the stirring barrel A is connected with a pulsating high-gradient strong magnetic separator, the pulsating high-gradient strong magnetic separator is connected with a thickener, and a thick slurry discharge hole of the thickener is respectively connected with a flotation system through a stirring barrel B and a stirring barrel C; the discharge port of the vibrating screen under-screen is connected with the feed port of the spiral classifier, and the sand return outlet of the spiral classifier is connected with the ball mill; the overflow outlet of the spiral classifier is connected with a No. 1 hydrocyclone, and the overflow outlet of the No. 1 hydrocyclone is tailings; the bottom slurry precipitation outlet of the No. 1 hydrocyclone is connected with a stirring barrel A. The utility model can efficiently recycle valuable components from the low-grade zinc oxide ores.
Description
Technical Field
The utility model relates to a mineral separation system for efficiently recycling valuable components from low-grade zinc oxide ores, and belongs to the field of mineral separation.
Background
Along with the exploitation of years, the number of the zinc ores which are easy to process is smaller and smaller, the grade of the zinc ores is gradually reduced, and people begin to pay attention to the utilization of low-grade zinc oxide ores. The zinc grade of valuable components of the zinc oxide ore is mostly lower than 15%, the components are complex, the zinc oxide ore mainly exists in the siderite and the calamine, in addition, a small amount of zinc sulfide and trace zinc ferrite exist, and the gangue components in the ore are high in iron oxide, silicon oxide, calcium oxide and magnesium oxide content (about Fe respectively 2 O 3 19%~28%；SiO 2 8% -34%; 19% -33% of CaO; mgO 7% -9%), and the lack of effective processing technology for the mineral resources is not reasonably utilized due to the low-grade high impurities, so that a large amount of mineral resources become dangerous waste residues, and the potential economic value of the mineral resources is not estimated. However, due to the complex nature of the ore, the method has the characteristics of high oxidation rate, large mud content, poor quality, fine quality, impurities and the like, the method can not be reasonably and effectively developed and utilized all the time, and meanwhile, serious threat is caused to environmental protection and safety, and a certain difficulty is also increased to the environmental treatment to a certain extent. For a long time, aiming at the development and comprehensive recycling of slag resources,has been highly focused by those skilled in the art and has been inclined to have a large amount of heart blood. It is thought that the main reasons for this current situation are that, after long-term weathering, ores contain high fine-grained clay primary slime and limonite, and the ores are easy to overgrind, and the ore solubility is high, so that the beneficiation effect is greatly affected. The existing beneficiation methods of the ore are a leaching method (acid leaching-extraction method and ammonia leaching-ammonia distillation crystallization method) and a full flotation method (comprising a sulfuration-amine flotation method, a heating sulfuration flotation method, a fatty acid flotation method and a chelating N-neutral oil flotation method, and the leaching-flotation method), wherein the full flotation method is represented by the sulfuration-flotation method. The acid leaching-extraction method is to dissolve zinc oxide by sulfuric acid, then add extractant to enrich zinc in organic phase, then re-extract and enter aqueous solution, then electro-deposition, but because the content of acid-soluble substances in low-grade zinc oxide ore is large, a large amount of sulfuric acid is required to be consumed, meanwhile, the ore contains zinc sulfide, zinc silicate and other minerals which are difficult to dissolve in acid or have low dissolution speed, the zinc leaching rate is low, the production cost is high, a large amount of waste residues are generated, and the problem of environmental pollution exists, so that the ore is difficult to receive for society or enterprises; the ammonia leaching-ammonia distillation crystallization method is to use ammonia-carbon ammonia combined leaching to prepare zinc amine complex, then purify, evaporate, dry and calcine to prepare zinc oxide product, but the method is not used for low-grade zinc oxide ore treatment all the time, because raw ore contains low zinc, leaching liquid contains low zinc concentration, leaching agent consumption is high, cost is high, and enterprises cannot accept the zinc; the vulcanizing-floating method is to grind raw ore by adopting a grinding machine, then to add sodium sulfide to vulcanize the surfaces of zinc mineral particles, and then to add a collector to recycle zinc oxide by using a floating system, but because the clay mineral mud (kaolinite, chlorite and the like) and the fine-particle-grade limonite content in the ore are higher, the floating process is greatly influenced, the method is characterized by larger consumption of floating agents, larger fluctuation of flow operation, difficult control, poor production index (concentrate zinc grade and recovery rate), higher tailing water alkalinity and difficult utilization of backwater or high treatment cost. In a word, the existing beneficiation methods have the defects of poor zinc recovery index, high production cost and unacceptable enterprises, and meanwhile, the valuable component limonite is not effectively utilized. In conclusion, oxygen is generatedZinc and other valuable components in the zinc sulfide ore are effectively recycled, and meanwhile, the defects of the existing traditional method are overcome, so that the technical problem to be solved in the industry is urgent. Based on the above, the utility model provides a beneficiation system for efficiently recovering valuable components from low-grade zinc oxide ores.
Disclosure of Invention
Aiming at the problems, the utility model provides the beneficiation system for efficiently recycling the valuable components from the low-grade zinc oxide ores, which has the advantages of simple flow, low production cost and safe tailings discharge.
The specific technical scheme is as follows: a mineral separation system for efficiently recycling valuable components from low-grade zinc oxide ores comprises a jaw crusher, wherein a discharge port of the jaw crusher is connected with a feed port of a vibrating screen through a conveyor, a discharge port of a vibrating screen is connected with a feed port of a ball mill through a conveyor, the discharge port of the ball mill is connected with a feed port of a No. 2 hydrocyclone through a pump sump and a pulp pump, a slurry precipitation outlet at the bottom of the No. 2 hydrocyclone is connected with the feed port of the ball mill, an overflow outlet of the No. 2 hydrocyclone is connected with a feed port of a stirring barrel A, a discharge port of the stirring barrel A is connected with a feed port of a pulsating high-gradient high-intensity magnetic separator through a pulp pump, a tail ore outlet of the pulsating high-gradient high-intensity magnetic separator is connected with a feed port of a thickener, and the thick slurry discharge port of the thickener is respectively connected with a flotation system through a stirring barrel B and a stirring barrel C; the concentrate outlet of the pulsating high-gradient strong magnetic separator is brown iron concentrate; the discharge port of the vibrating screen under-screen is connected with the feed port of the spiral classifier, and the sand return outlet of the spiral classifier is connected with the feed port of the ball mill; the overflow outlet of the spiral classifier is connected with the feed inlet of the No. 1 hydrocyclone through a pump pool and a pulp pump, and the overflow outlet of the No. 1 hydrocyclone is tailings; the slurry sedimentation outlet at the bottom of the No. 1 hydrocyclone is connected with the feed inlet of the stirring barrel A.
Further, the No. 1 hydrocyclone is a phi 75 hydrocyclone; the No. 2 hydrocyclone is phi 350 hydrocyclone.
Further, the flotation system comprises a first roughing system, a first scavenging system, a second scavenging system and a first selecting system and a second selecting system; the roughing system is formed by sequentially connecting 5 flotation machines, and a feed inlet of a first flotation machine in the roughing system is connected with a discharge outlet of a stirring barrel C; the scavenging system is formed by sequentially connecting 4 flotation machines, and a tailing outlet of the last flotation machine in the roughing system is connected with a feed inlet of the first flotation machine in the scavenging system; the foam tank of the scavenging system is connected with the feed inlet of the first flotation machine in the roughing system; the scavenging two systems are formed by sequentially connecting 4 flotation machines, a tailing outlet of the last flotation machine in the scavenging two systems is connected with a feeding hole of the first flotation machine in the scavenging two systems, a foam tank of the scavenging two systems is connected with a feeding hole of the first flotation machine in the scavenging two systems, and tailings of the last flotation machine in the scavenging two systems are flotation tailings; the flotation system is composed of 4 flotation machines which are connected in reverse order, the outlet of a flotation machine foam tank of the roughing system is connected with the feed inlet of the last flotation machine in the flotation system, and the outlet of the tail ore of the first flotation machine of the flotation system is connected with the feed inlet of the first flotation machine of the roughing system; the second system of carefully choosing is composed of 3 flotation machines which are connected in reverse order, the outlet of the flotation machine foam tank of the first system of carefully choosing is connected with the feed inlet of the last flotation machine in the second system of carefully choosing, the tailing outlet of the first flotation machine in the second system of carefully choosing is connected with the feed inlet of the last flotation machine in the first system of carefully choosing, and the outlet of the flotation machine foam tank of the second system of carefully choosing is zinc oxide concentrate.
A beneficiation method for efficiently recovering valuable components from low-grade zinc oxide ores comprises the following steps: (1) Coarsely crushing the ore to be treated, conveying the ore to be treated to a crushing system, and crushing the ore to the particle size of-10 mm; (2) washing and pre-polishing waste: a. conveying the material subjected to the step (1) to a vibrating screen with a screen mesh size of 2mm for screening, and flushing with high-pressure water to obtain screened products of-10mm+2mm (2-10 mm) size and-2 mm (less than 2 mm) size; b. c, conveying the material with the particle size of-2 mm obtained in the step a to a spiral classifier for classification to obtain a product with the particle size of-2mm+0.1 mm (0.1-2 mm) and the particle size of-0.1 mm (less than 0.1 mm); c. b, conveying the material with the particle size of-0.1 mm obtained in the step b to a hydrocyclone with the diameter of 75mm for classification to obtain a product with the particle size of-0.1+0.015 (0.015-0.1 mm) mm and a product with the particle size of-0.015 mm (the product is a waste throwing material); (3) Grinding and classifying, namely merging the particle size fraction of-10 mm+2mm obtained in the step a and the particle size fraction of-2+0.1 (0.1-2 mm) obtained in the step b, and conveying the mixture into a ball mill-cyclone classification for selective grinding and classifying to obtain a material with the grinding fineness of-0.074 mm accounting for 75% and the concentration of 18% -20%; (4) B, ferric oxide magnetic separation, namely merging the materials with the grain size of-0.1+0.015 mm obtained in the step c and the grain size of-0.074 mm obtained in the step 3 and accounting for 75%, conveying the materials to a stirring barrel A for size mixing, and conveying the materials to a pulsating high-gradient strong magnetic separator for limonite magnetic separation to obtain limonite concentrate with the Fe grade of 50% -53% and magnetic separation tailings; (5) And (3) zinc oxide flotation, namely conveying the magnetic separation tailings obtained in the step (4) to a stirring tank B, adding a dispersing agent sodium hexametaphosphate, stirring and mixing uniformly, conveying the magnetic separation tailings to a stirring tank C, adding sodium sulfide, octadecylamine acetate, kerosene and No. 2 oil mixed solution, stirring and mixing uniformly, and conveying the magnetic separation tailings to a flotation system for zinc oxide flotation to obtain high-quality zinc oxide concentrate and tailings with zinc grade of 30-35%.
It is further preferred that in step (3), the grinding concentration is 50% -55% and the classifying cyclone feeding concentration is 35% -40%.
It is further preferred that in step (4), the background magnetic induction is 1.1-1.2T and the magnetic medium diameter is 1.5mm; the magnetic separation concentration is 22% -26%.
It is further preferred that in step (5), the flotation system is subjected to two beneficiations, one roughing and two scavenging; the dosage of sodium sulfide is roughly 2000g/t, the first scavenging amount is 500g/t, and the second scavenging amount is 300g/t; the dosage of octadecylamine acetate is roughly 120g/t, the first scavenging amount is 60g/t, and the second scavenging amount is 40g/t; the dosage of kerosene is roughly 50g/t, the first scavenging amount is 30g/t, and the second scavenging amount is 20g/t; the consumption of the No. 2 oil is roughly selected to be 50g/t, the first scavenging amount is 30g/t, and the second scavenging amount is 20g/t; the dosage of the coarse separation dispersant sodium hexametaphosphate is 150g/t; the flotation concentration is 20% -22%.
The beneficial effects are that: the utility model provides a mineral separation system for efficiently recovering valuable components from low-grade zinc oxide ores, which solves the technical problems that the system comprises the steps of washing pre-polishing waste and high-gradient strong magnetic separation to remove a large amount of substances (including clay silicate mineral mud kaolinite, chlorite and the like, micro-fine limonite and soluble salts) interfering with the flotation of the zinc oxide ores from the low-grade zinc oxide ores, and then, the zinc oxide ores are recovered by adopting a flotation method, so that the zinc oxide mineral separation effect is improved, high-quality zinc oxide concentrate and limonite concentrate are obtained, the cost of a flotation reagent is reduced, the mineral separation economic benefit is improved, and the purposes of efficiently and comprehensively utilizing resources and reducing environmental pollution are achieved.
Compared with the prior method, the method has the advantages and positive effects that:
(1) The clay slime which accounts for 15% -20% of the total ore feeding and has great influence on the ore dressing effect is thrown out by adopting a simple water washing pre-throwing waste mode, so that the ore feeding grade of the subsequent operation is improved, and the production stability of the subsequent operation is also improved;
(2) The selective low-concentration grinding and low-concentration grading modes are skillfully adopted, so that the granularity uniformity of the ground ore product is improved, and the qualified size fraction is timely graded, so that the generation of the overgrinding size fraction is reduced, and the ore dressing effect is improved;
(3) The pulsating high-gradient strong magnetic separator is skillfully adopted to separate limonite, so that the limonite concentrate product is used for improving the content of flotation feed zinc, reducing the fine-particle-grade limonite entering a flotation system, improving the flotation effect, reducing the consumption of flotation agents, reducing the production cost and increasing the comprehensive economic benefit;
(4) The zinc oxide ore dressing index is improved, the production cost is reduced, meanwhile, valuable elements are efficiently recovered, the comprehensive economic benefit is improved, the purpose of comprehensive and efficient utilization of resources is achieved, and in addition, the hazard of environmental pollution is reduced;
(5) The adaptability is strong, the adaptability to zinc oxide ore dressing is good, and the method has wide industrial and commercial application popularization values.
Drawings
FIG. 1 is a device contact diagram of the present utility model;
wherein, 1: jaw crusher, 2: vibrating screen, 3, spiral classifier, 4, thick liquid pump pond, 5: pulp pump, 6: no. 1 hydrocyclone, 7: ball mill, 8: no. 2 hydrocyclone, 9: stirring barrel, 10: pulsating high gradient strong magnetic separator, 11: thickener, 12: a flotation system.
Detailed Description
For the purpose of better illustrating the embodiments, certain elements of the drawings may be omitted, enlarged or reduced and do not represent the actual product dimensions; it will be appreciated by those skilled in the art that certain well-known structures in the drawings and descriptions thereof may be omitted. It will be understood by those of ordinary skill in the art that the terms described above are in the specific sense of the present utility model. The technical scheme of the utility model is further described below with reference to the accompanying drawings and examples.
As shown in figure 1, the mineral separation system for efficiently recycling valuable components from low-grade zinc oxide ores comprises a jaw crusher 1, wherein a discharge port of the jaw crusher 1 is connected with a feed port of a vibrating screen 2 through a conveyor, a discharge port of a oversize material of the vibrating screen 2 is connected with a feed port of a ball mill 7 through a conveyor, a discharge port of the ball mill 7 is connected with a feed port of a No. 2 hydrocyclone 8 through a pump pond and a pulp pump, a slurry sedimentation outlet at the bottom of the No. 2 hydrocyclone 8 is connected with a feed port of the ball mill 7, an overflow outlet of the No. 2 hydrocyclone 8 is connected with a feed port of a stirring barrel A9, a discharge port of the stirring barrel A9 is connected with a feed port of a pulsating high-gradient high-intensity magnetic separator 10 through a pulp pump, a tailing outlet of the pulsating high-gradient high-intensity magnetic separator 10 is connected with a feed port of a thickener 11, and a thick slurry discharge port of the thickener 11 is respectively connected with a flotation system through a stirring barrel B and a stirring barrel C; the concentrate outlet of the pulsating high-gradient strong magnetic separator 10 is brown iron concentrate; the discharge port of the undersize material of the vibrating screen 2 is connected with the feed port of the spiral classifier 3, and the sand return outlet of the spiral classifier 3 is connected with the feed port of the ball mill 7; the overflow outlet of the spiral classifier 3 is connected with the feed inlet of the No. 1 hydrocyclone 6 through a pump pool and a pulp pump, and the overflow outlet of the No. 1 hydrocyclone 6 is tailings; the slurry sedimentation outlet at the bottom of the No. 1 hydrocyclone 6 is connected with the feed inlet of the stirring barrel A9.
The No. 1 hydrocyclone is a phi 75 hydrocyclone; the No. 2 hydrocyclone is phi 350 hydrocyclone.
Further, the flotation system comprises a first roughing system, a first scavenging system, a second scavenging system and a first selecting system and a second selecting system; the roughing system is formed by sequentially connecting 5 flotation machines from left to right, and a feed inlet of a first flotation machine in the roughing system is connected with a discharge outlet of a stirring barrel C; the scavenging system is formed by sequentially connecting 4 flotation machines from left to right, and a tailing outlet of the last flotation machine in the roughing system is connected with a feed inlet of the first flotation machine in the scavenging system; the foam tank of the scavenging system is connected with the feed inlet of the first flotation machine in the roughing system; the scavenging two systems are formed by sequentially connecting 4 flotation machines from left to right, a tailing outlet of the last flotation machine in the scavenging two systems is connected with a feeding hole of the first flotation machine in the scavenging two systems, a foam tank of the scavenging two systems is connected with a feeding hole of the first flotation machine in the scavenging two systems, and tailings of the last flotation machine in the scavenging two systems are flotation tailings; the flotation system is composed of 4 flotation machines which are connected in reverse order (from right to left), the outlet of a flotation machine foam tank of the roughing system is connected with the feed inlet of the last flotation machine in the flotation system, and the outlet of the first flotation machine tail ore of the flotation system is connected with the feed inlet of the first flotation machine of the roughing system; the second system of carefully choosing is composed of 3 flotation machines which are connected in reverse order (from right to left), the outlet of the flotation machine foam tank of the first system of carefully choosing is connected with the feed inlet of the last flotation machine of the second system of carefully choosing, the tailing outlet of the first flotation machine of the second system of carefully choosing is connected with the feed inlet of the last flotation machine of the first system of carefully choosing, and the outlet of the flotation machine foam tank of the second system of carefully choosing is zinc oxide concentrate. The first flotation machine is the sequence number from left to right, and the last flotation machine is the sequence number from left to right.
The concrete beneficiation method comprises the following steps: the method comprises the following steps: (1) Coarsely crushing the ore to be treated, conveying the ore to be treated to a crushing system, and crushing the ore to the particle size of-10 mm; (2) washing and pre-polishing waste: a. conveying the material subjected to the step (1) to a vibrating screen with a screen mesh size of 2mm for screening, and flushing with high-pressure water to obtain screened products of-10mm+2mm size and-2 mm size; b. c, conveying the material with the particle size of-2 mm obtained in the step a to a spiral classifier for classification to obtain a product with the particle size of-2mm+0.1mm and the particle size of-0.1 mm; c. b, conveying the material with the particle size of-0.1 mm obtained in the step b to a hydrocyclone with the diameter of 75mm for classification to obtain a product with the particle size of-0.1+0.015 mm and a product with the particle size of-0.015 mm (the product is a waste throwing material); (3) Grinding and classifying, namely merging the particle fraction of-10 mm+2mm obtained in the step a and the particle fraction of-2+0.1 mm obtained in the step b, and conveying the mixture into a ball mill-cyclone classification for selective grinding and classifying to obtain a material with the grinding fineness of-0.074 mm accounting for 75% and the concentration of 18% -20%; (4) B, ferric oxide magnetic separation, namely merging the materials with the grain size of-0.1+0.015 mm obtained in the step c and the grain size of-0.074 mm obtained in the step 3 and accounting for 75%, conveying the materials to a stirring barrel A for size mixing, and conveying the materials to a pulsating high-gradient strong magnetic separator for limonite magnetic separation to obtain limonite concentrate with the Fe grade of 50% -53% and magnetic separation tailings; (5) And (3) zinc oxide flotation, namely conveying the magnetic separation tailings obtained in the step (4) to a stirring tank B, adding a dispersing agent sodium hexametaphosphate, stirring and mixing uniformly, conveying the magnetic separation tailings to a stirring tank C, adding sodium sulfide, octadecylamine acetate, kerosene and No. 2 oil mixed solution, stirring and mixing uniformly, and conveying the magnetic separation tailings to a flotation system for zinc oxide flotation to obtain high-quality zinc oxide concentrate and tailings with zinc grade of 30-35%.
It is further preferred that in step (3), the grinding concentration is 50% -55% and the classifying cyclone feeding concentration is 35% -40%.
It is further preferred that in step (4), the background magnetic induction is 1.1-1.2T and the magnetic medium diameter is 1.5mm; the magnetic separation concentration is 22% -26%.
It is further preferred that in step (5), the flotation system is subjected to two beneficiations, one roughing and two scavenging; the dosage of sodium sulfide is roughly 2000g/t, the first scavenging amount is 500g/t, and the second scavenging amount is 300g/t; the dosage of octadecylamine acetate is roughly 120g/t, the first scavenging amount is 60g/t, and the second scavenging amount is 40g/t; the dosage of kerosene is roughly 50g/t, the first scavenging amount is 30g/t, and the second scavenging amount is 20g/t; the consumption of the No. 2 oil is roughly selected to be 50g/t, the first scavenging amount is 30g/t, and the second scavenging amount is 20g/t; the dosage of the coarse separation dispersant sodium hexametaphosphate is 150g/t; the flotation concentration is 20% -22%.
Embodiment one:
The zinc oxide ore is implemented by adopting the process, and the technical steps comprise:
(1) The ore to be treated is coarsely crushed. Conveying the ore to be processed to a crushing system, and crushing the ore to the size of-10 mm;
(2) And (5) washing and pre-polishing waste. The method comprises the following specific steps:
a. conveying the material subjected to the step (1) to a vibrating screen with a screen mesh size of 2mm for screening, and flushing with high-pressure water to obtain screened products of-10mm+2mm size and-2 mm size;
b. c, conveying the material with the particle size of-2 mm obtained in the step a to a spiral classifier for classification to obtain a product with the particle size of-2mm+0.1mm and the particle size of-0.1 mm;
c. the-0.1 mm fraction obtained after completion of step b above was sent to a hydrocyclone of 75mm diameter for classification to obtain-0.1+0.015 mm fraction and-0.015 mm fraction (this fraction is a waste-disposal material).
(3) Selective milling-classification. And c, combining the particle size fraction of-10mm+2mm obtained in the step a and the particle size fraction of-2+0.1 mm obtained in the step b, and conveying to a ball mill-cyclone classification system for selective grinding and classification to obtain a material with the grinding fineness of-0.074 mm, wherein the particle size fraction accounts for 75% and the concentration is 18% -20%. In the process, the ore grinding concentration is 50% -55%, and the ore feeding concentration of the classifying cyclone is 35% -40%.
(4) And (3) carrying out iron oxide magnetic separation, namely merging the materials with the grain size of-0.1+0.015 mm obtained in the step (c) and the grain size of-0.074 mm obtained in the step (3) accounting for 75%, conveying the materials to a stirring barrel A for size mixing, and conveying the materials to a pulsating high-gradient strong magnetic separator for limonite magnetic separation to obtain limonite concentrate with the Fe grade of 50% -53% and magnetic separation tailings (the tailings enter a thickener for concentration). In the process, the background magnetic induction intensity is 1.1-1.2T, and the diameter of the magnetic medium is 1.5mm; the magnetic separation concentration is 22% -26%.
(5) And (3) zinc oxide flotation. And (3) conveying the magnetic separation tailings obtained in the step (4) to a stirring tank B, adding a dispersing agent sodium hexametaphosphate, stirring for 3 minutes, conveying to the stirring tank C, adding a mixed solution of sodium sulfide, octadecylamine acetate, kerosene and No. 2 oil, stirring for 3 minutes, and conveying to a flotation system for zinc oxide flotation to obtain high-quality zinc oxide concentrate and tailings with zinc grade of 30-35%. In the process, two carefully selecting, one rough selecting and two scavenging are carried out; the dosage of sodium sulfide is roughly 2000g/t, the first scavenging amount is 500g/t, and the second scavenging amount is 300g/t; the dosage of octadecylamine acetate is roughly 120g/t, the first scavenging amount is 60g/t, and the second scavenging amount is 40g/t; the dosage of kerosene is roughly 50g/t, the first scavenging amount is 30g/t, and the second scavenging amount is 20g/t; the consumption of the No. 2 oil is roughly selected to be 50g/t, the first scavenging amount is 30g/t, and the second scavenging amount is 20g/t; the dosage of the coarse separation dispersant sodium hexametaphosphate is 150g/t; the concentration of rougher flotation is 20% -22%.
The test results were obtained: zinc oxide concentrate zinc grade 32.45%, recovery 81.37%, limonite concentrate iron grade 50.21%, recovery 42.66%.
Embodiment two:
the raw material No. 2 is a certain zinc oxide ore, and the chemical components are as follows: zn10.73%, fe17.61%, siO 2 18.31 、AL 2 O 3 9.13% 、 CaO 9.78%, wherein the zinc phase components are 8.36% of wurtzite, 1.33% of zinc silicate, 0.61% of zinc sulfide and 0.45% of zinc ferrite, and the iron phase components are as follows: magnetite 1.91%, siderite 0.38%, hematite/limonite 13.89%, ferric silicate 0.86%, ferric sulfide 0.57%.
The zinc oxide ore is implemented by adopting the process, and the technical steps comprise:
(1) The ore to be treated is coarsely crushed. Conveying the ore to be processed to a crushing system, and crushing the ore to the size of-10 mm;
(2) And (5) washing and pre-polishing waste. The method comprises the following specific steps:
a. conveying the material subjected to the step (1) to a vibrating screen with a screen mesh size of 2mm for screening, and flushing with high-pressure water to obtain screened products of-10mm+2mm size and-2 mm size;
b. c, conveying the material with the particle size of-2 mm obtained in the step a to a spiral classifier for classification to obtain a product with the particle size of-2mm+0.1mm and the particle size of-0.1 mm;
c. the-0.1 mm fraction obtained after completion of step b above was sent to a hydrocyclone of 75mm diameter for classification to obtain-0.1+0.015 mm fraction and-0.015 mm fraction (this fraction is a waste-disposal material).
(3) Selective milling-classification. And c, combining the particle size fraction of-10mm+2mm obtained in the step a and the particle size fraction of-2+0.1 mm obtained in the step b, and conveying to a ball mill-cyclone classification system for selective grinding and classification to obtain a material with the grinding fineness of-0.074 mm, wherein the particle size fraction accounts for 75% and the concentration is 18% -20%. In the process, the ore grinding concentration is 50% -55%, and the ore feeding concentration of the classifying cyclone is 35% -40%.
(4) And (3) carrying out iron oxide magnetic separation, namely merging the materials with the grain size of-0.1+0.015 mm obtained in the step (c) and the grain size of-0.074 mm obtained in the step (3) accounting for 75%, conveying the materials to a stirring barrel A for size mixing, and conveying the materials to a pulsating high-gradient strong magnetic separator for limonite magnetic separation to obtain limonite concentrate with the Fe grade of 50% -53% and magnetic separation tailings (the tailings enter a thickener for concentration). In the process, the background magnetic induction intensity is 1.1-1.2T, and the diameter of the magnetic medium is 1.5mm; the magnetic separation concentration is 22% -26%.
(5) And (3) zinc oxide flotation. And (3) conveying the magnetic separation tailings obtained in the step (4) to a stirring tank B, adding a dispersing agent sodium hexametaphosphate, stirring for 3 minutes, conveying to the stirring tank C, adding a mixed solution of sodium sulfide, octadecylamine acetate, kerosene and No. 2 oil, stirring for 3 minutes, and conveying to a flotation system for zinc oxide flotation to obtain high-quality zinc oxide concentrate and tailings with zinc grade of 30-35%. In the process, two carefully selecting, one rough selecting and two scavenging are carried out; the dosage of sodium sulfide is roughly 2000g/t, the first scavenging amount is 500g/t, and the second scavenging amount is 300g/t; the dosage of octadecylamine acetate is roughly 120g/t, the first scavenging amount is 60g/t, and the second scavenging amount is 40g/t; the dosage of kerosene is roughly 50g/t, the first scavenging amount is 30g/t, and the second scavenging amount is 20g/t; the consumption of the No. 2 oil is roughly selected to be 50g/t, the first scavenging amount is 30g/t, and the second scavenging amount is 20g/t; the dosage of the coarse separation dispersant sodium hexametaphosphate is 150g/t; the concentration of rougher flotation is 20% -22%.
The test results were obtained: zinc oxide concentrate zinc grade 31.31%, recovery rate 78.36%, limonite concentrate iron grade 50.65%, recovery rate 41.78%.
Embodiment III:
raw material 3#: some zinc oxide ore comprises the following chemical components: 12.77% of Zn, 18.83% of Fe and SiO 2 23.48% 、AL 2 O 3 9.86% 、 12.71% of CaO, wherein the zinc phase components of the CaO are 10.96% of wurtzite, 1.21% of zinc silicate, 0.76% of zinc sulfide and 0.67% of zinc ferrite, and the iron phase components are as follows: magnetite 1.76%, siderite 0.77%, hematite/limonite 14.82%, ferric silicate 1.12% and ferric sulfide 0.36%.
The zinc oxide ore is implemented by adopting the process, and the technical steps comprise:
(1) The ore to be treated is coarsely crushed. Conveying the ore to be processed to a crushing system, and crushing the ore to the size of-10 mm;
(2) And (5) washing and pre-polishing waste. The method comprises the following specific steps:
a. conveying the material subjected to the step (1) to a vibrating screen with a screen mesh size of 2mm for screening, and flushing with high-pressure water to obtain screened products of-10mm+2mm size and-2 mm size;
b. c, conveying the material with the particle size of-2 mm obtained in the step a to a spiral classifier for classification to obtain a product with the particle size of-2mm+0.1mm and the particle size of-0.1 mm;
c. the-0.1 mm fraction obtained after completion of step b above was sent to a hydrocyclone of 75mm diameter for classification to obtain-0.1+0.015 mm fraction and-0.015 mm fraction (this fraction is a waste-disposal material).
(3) Selective milling-classification. And c, combining the particle size fraction of-10mm+2mm obtained in the step a and the particle size fraction of-2+0.1 mm obtained in the step b, and conveying to a ball mill-cyclone classification system for selective grinding and classification to obtain a material with the grinding fineness of-0.074 mm, wherein the particle size fraction accounts for 75% and the concentration is 18% -20%. In the process, the ore grinding concentration is 50% -55%, and the ore feeding concentration of the classifying cyclone is 35% -40%.
(4) And (3) carrying out iron oxide magnetic separation, namely merging the materials with the grain size of-0.1+0.015 mm obtained in the step (c) and the grain size of-0.074 mm obtained in the step (3) accounting for 75%, conveying the materials to a stirring barrel A for size mixing, and conveying the materials to a pulsating high-gradient strong magnetic separator for limonite magnetic separation to obtain limonite concentrate with the Fe grade of 50% -53% and magnetic separation tailings (the tailings enter a thickener for concentration). In the process, the background magnetic induction intensity is 1.1-1.2T, and the diameter of the magnetic medium is 1.5mm; the magnetic separation concentration is 22% -26%.
(5) And (3) zinc oxide flotation. And (3) conveying the magnetic separation tailings obtained in the step (4) to a stirring tank B, adding a dispersing agent sodium hexametaphosphate, stirring for 3 minutes, conveying to the stirring tank C, adding a mixed solution of sodium sulfide, octadecylamine acetate, kerosene and No. 2 oil, stirring for 3 minutes, and conveying to a flotation system for zinc oxide flotation to obtain high-quality zinc oxide concentrate and tailings with zinc grade of 30-35%. In the process, two carefully selecting, one rough selecting and two scavenging are carried out; the dosage of sodium sulfide is roughly 2000g/t, the first scavenging amount is 500g/t, and the second scavenging amount is 300g/t; the dosage of octadecylamine acetate is roughly 120g/t, the first scavenging amount is 60g/t, and the second scavenging amount is 40g/t; the dosage of kerosene is roughly 50g/t, the first scavenging amount is 30g/t, and the second scavenging amount is 20g/t; the consumption of the No. 2 oil is roughly selected to be 50g/t, the first scavenging amount is 30g/t, and the second scavenging amount is 20g/t; the dosage of the coarse separation dispersant sodium hexametaphosphate is 150g/t; the concentration of rougher flotation is 20% -22%.
The test results were obtained: zinc oxide concentrate zinc grade 30.97%, recovery rate 79.61%, limonite concentrate iron grade 52.11% and recovery rate 42.23%.
Embodiment four:
raw material 4#: some zinc oxide ore comprises the following chemical components: zn9.89%, fe19.21%, siO 2 20.44% 、AL 2 O 3 9.39% 、 15.27% of CaO, wherein the zinc phase components of the CaO are 7.43% of wurtzite, 1.08% of zinc silicate, 0.65% of zinc sulfide and 0.82% of zinc ferrite, and the iron phase components are as follows: magnetite 2.02%, siderite 0.67%, red/brown iron ore 15.25%, ferric silicate 0.82% and ferric sulfide 0.45%.
The zinc oxide ore is implemented by adopting the process, and the technical steps comprise:
(1) The ore to be treated is coarsely crushed. Conveying the ore to be processed to a crushing system, and crushing the ore to the size of-10 mm;
(2) And (5) washing and pre-polishing waste. The method comprises the following specific steps:
a. conveying the material subjected to the step (1) to a vibrating screen with a screen mesh size of 2mm for screening, and flushing with high-pressure water to obtain screened products of-10mm+2mm size and-2 mm size;
b. c, conveying the material with the particle size of-2 mm obtained in the step a to a spiral classifier for classification to obtain a product with the particle size of-2mm+0.1mm and the particle size of-0.1 mm;
c. the-0.1 mm fraction obtained after completion of step b above was sent to a hydrocyclone of 75mm diameter for classification to obtain-0.1+0.015 mm fraction and-0.015 mm fraction (this fraction is a waste-disposal material).
(3) Selective milling-classification. And c, combining the particle size fraction of-10mm+2mm obtained in the step a and the particle size fraction of-2+0.1 mm obtained in the step b, and conveying to a ball mill-cyclone classification system for selective grinding and classification to obtain a material with the grinding fineness of-0.074 mm, wherein the particle size fraction accounts for 75% and the concentration is 18% -20%. In the process, the ore grinding concentration is 50% -55%, and the ore feeding concentration of the classifying cyclone is 35% -40%.
(4) And (3) carrying out iron oxide magnetic separation, namely merging the materials with the grain size of-0.1+0.015 mm obtained in the step (c) and the grain size of-0.074 mm obtained in the step (3) accounting for 75%, conveying the materials to a stirring barrel A for size mixing, and conveying the materials to a pulsating high-gradient strong magnetic separator for limonite magnetic separation to obtain limonite concentrate with the Fe grade of 50% -53% and magnetic separation tailings (the tailings enter a thickener for concentration). In the process, the background magnetic induction intensity is 1.1-1.2T, and the diameter of the magnetic medium is 1.5mm; the magnetic separation concentration is 22% -26%.
(5) And (3) zinc oxide flotation. And (3) conveying the magnetic separation tailings obtained in the step (4) to a stirring tank B, adding a dispersing agent sodium hexametaphosphate, stirring for 3 minutes, conveying to the stirring tank C, adding a mixed solution of sodium sulfide, octadecylamine acetate, kerosene and No. 2 oil, stirring for 3 minutes, and conveying to a flotation system for zinc oxide flotation to obtain high-quality zinc oxide concentrate and tailings with zinc grade of 30-35%. In the process, two carefully selecting, one rough selecting and two scavenging are carried out; the dosage of sodium sulfide is roughly 2000g/t, the first scavenging amount is 500g/t, and the second scavenging amount is 300g/t; the dosage of octadecylamine acetate is roughly 120g/t, the first scavenging amount is 60g/t, and the second scavenging amount is 40g/t; the dosage of kerosene is roughly 50g/t, the first scavenging amount is 30g/t, and the second scavenging amount is 20g/t; the consumption of the No. 2 oil is roughly selected to be 50g/t, the first scavenging amount is 30g/t, and the second scavenging amount is 20g/t; the dosage of the coarse separation dispersant sodium hexametaphosphate is 150g/t; the concentration of rougher flotation is 20% -22%.
The test results were obtained: zinc oxide concentrate zinc grade 30.06%, recovery rate 79.78%, limonite concentrate iron grade 51.35% and recovery rate 45.72%.
In conclusion, the process is implemented on the zinc oxide ore to obtain high-quality zinc oxide concentrate with zinc grade more than 30% and brown iron concentrate with iron grade more than 50%, and the zinc recovery rate is more than 78% and the iron recovery rate is more than 41%, so that the process has better adaptability to the zinc oxide ore, is simple and stable, has relatively low production cost, can obtain better economic benefit, can effectively and comprehensively utilize mineral resources, is safe and reliable in waste residue emission, and has wide industrial and commercial application popularization values.
Claims (4)
1. A mineral separation system for efficiently recycling valuable components from low-grade zinc oxide ores is characterized by comprising a jaw crusher (1), wherein a discharge port of the jaw crusher (1) is connected with a feed port of a vibrating screen (2) through a conveyor, a discharge port of a screen upper material of the vibrating screen (2) is connected with a feed port of a ball mill (7) through the conveyor, a discharge port of the ball mill (7) is connected with a feed port of a No. 2 hydrocyclone (8) through a pump tank and a pulp pump, a slurry settling outlet at the bottom of the No. 2 hydrocyclone (8) is connected with a feed port of the ball mill (7), an overflow outlet of the No. 2 hydrocyclone (8) is connected with a feed port of a stirring barrel A (9), a discharge port of the stirring barrel A (9) is connected with a feed port of a pulsating high-gradient strong magnetic separator (10) through a pulp pump, a tailing outlet of the pulsating high-gradient strong magnetic separator (10) is connected with a feed port of a thickener (11), and a thick slurry discharge port of the thickener (11) is respectively connected with a flotation system through a stirring barrel B and a stirring barrel C; the concentrate outlet of the pulsating high-gradient strong magnetic separator (10) is brown iron concentrate;
the discharge port of the vibrating screen (2) for the undersize is connected with the feed port of the spiral classifier (3), and the sand return outlet of the spiral classifier (3) is connected with the feed port of the ball mill (7);
the overflow outlet of the spiral classifier (3) is connected with the feed inlet of the No. 1 hydrocyclone (6) through a pump pool and a pulp pump, and the overflow outlet of the No. 1 hydrocyclone (6) is tailings;
the bottom slurry sedimentation outlet of the No. 1 hydrocyclone (6) is connected with the feed inlet of the stirring barrel A (9).
2. A beneficiation system for efficiently recovering valuable components from low grade zinc oxide ores according to claim 1, wherein the No. 1 hydrocyclone is a phi 75 hydrocyclone.
3. A beneficiation system for efficiently recovering valuable components from low grade zinc oxide ores according to claim 2, wherein the No. 2 hydrocyclone is a phi 350 hydrocyclone.
4. A beneficiation system for efficiently recovering valuable components from low grade zinc oxide ores according to claim 3, wherein the flotation system comprises a rougher, a scavenger and a beneficiation system;
the roughing system is formed by sequentially connecting 5 flotation machines, and a feed inlet of a first flotation machine in the roughing system is connected with a discharge outlet of a stirring barrel C;
the scavenging system is formed by sequentially connecting 4 flotation machines, and a tailing outlet of the last flotation machine in the roughing system is connected with a feed inlet of the first flotation machine in the scavenging system; the foam tank of the scavenging system is connected with the feed inlet of the first flotation machine in the roughing system;
the scavenging two systems are formed by sequentially connecting 4 flotation machines, a tailing outlet of the last flotation machine in the scavenging two systems is connected with a feeding hole of the first flotation machine in the scavenging two systems, a foam tank of the scavenging two systems is connected with a feeding hole of the first flotation machine in the scavenging two systems, and tailings of the last flotation machine in the scavenging two systems are flotation tailings;
the flotation system is composed of 4 flotation machines which are connected in reverse order, the outlet of a flotation machine foam tank of the roughing system is connected with the feed inlet of the last flotation machine in the flotation system, and the outlet of the tail ore of the first flotation machine of the flotation system is connected with the feed inlet of the first flotation machine of the roughing system;
the second system of carefully choosing is composed of 3 flotation machines which are connected in reverse order, the outlet of the flotation machine foam tank of the first system of carefully choosing is connected with the feed inlet of the last flotation machine in the second system of carefully choosing, the tailing outlet of the first flotation machine in the second system of carefully choosing is connected with the feed inlet of the last flotation machine in the first system of carefully choosing, and the outlet of the flotation machine foam tank of the second system of carefully choosing is zinc oxide concentrate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320068492.2U CN219252883U (en) | 2023-01-10 | 2023-01-10 | Ore dressing system for efficiently recycling valuable components from low-grade zinc oxide ores |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320068492.2U CN219252883U (en) | 2023-01-10 | 2023-01-10 | Ore dressing system for efficiently recycling valuable components from low-grade zinc oxide ores |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219252883U true CN219252883U (en) | 2023-06-27 |
Family
ID=86854314
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320068492.2U Active CN219252883U (en) | 2023-01-10 | 2023-01-10 | Ore dressing system for efficiently recycling valuable components from low-grade zinc oxide ores |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219252883U (en) |
-
2023
- 2023-01-10 CN CN202320068492.2U patent/CN219252883U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108993766B (en) | Ore dressing treatment method for weathered ilmenite | |
| CN101428248B (en) | Beneficiation method for recycling specularite | |
| CN101733190B (en) | Benefication method for sulphur-containing composite iron tailing | |
| WO2021073162A1 (en) | Method for intensive recovery of valuable components from rare earth tailings | |
| CN104888958B (en) | Micro-fine particle red magnetic mixed iron ore sorting process | |
| CN102430473A (en) | Pre-selecting and tailings discarding process of lean magnetite ores | |
| CN100558467C (en) | A kind of beneficiation method that improves brown iron ore grade | |
| CN111686925B (en) | Mineral processing technology for recovering rare earth, fluorite and barite from low-grade rare earth ore | |
| CN105057089A (en) | Beneficiation technology for rock-type primary ilmenite | |
| CN113731628B (en) | Method for efficiently recovering cassiterite from fine-grain dip-dyed type tin polymetallic ore | |
| CN101537394A (en) | Chemical-adding scrubbing beneficiation and enrichment method suitable for clay vanadium ore | |
| CN110575904A (en) | Spodumene grading-grade dual medium-flotation beneficiation method | |
| CN112206919A (en) | Beneficiation method for obtaining blocky manganese concentrate | |
| CN112024120A (en) | Beneficiation method for micro-fine-particle-grade hematite and limonite | |
| CN108212504A (en) | A kind of method that pre-selection-roasting-magnetic floats technique recycling magnetic tailing | |
| CN114247559A (en) | Tailing-free ore dressing method for lithium ore recovery | |
| WO2024045687A2 (en) | Method for pre-selection and discarding and reducing over-grinding of gold ores | |
| CN219252883U (en) | Ore dressing system for efficiently recycling valuable components from low-grade zinc oxide ores | |
| CN116116568B (en) | Beneficiation method for efficiently recycling valuable components from low-grade zinc oxide ores | |
| CN110773327A (en) | Method for flotation recovery of fine cassiterite of oxidized vein tin ore | |
| CN102886301B (en) | Hematite beneficiation method | |
| CN112718231B (en) | Mineral separation method of molybdenite of magnesium-rich mineral | |
| CN112295725A (en) | Solid waste treatment method | |
| CN219252881U (en) | Complex zinc oxide ore recovery system with multiple zinc occurrence states | |
| CN217491212U (en) | Mineral processing system for recovering strong magnetic iron ore from tailings generated in gold extraction by carbon slurry method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |