CN111804424A - Bastnaesite beneficiation device and method - Google Patents
Bastnaesite beneficiation device and method Download PDFInfo
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- CN111804424A CN111804424A CN202010733837.2A CN202010733837A CN111804424A CN 111804424 A CN111804424 A CN 111804424A CN 202010733837 A CN202010733837 A CN 202010733837A CN 111804424 A CN111804424 A CN 111804424A
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- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
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Abstract
The invention provides a bastnaesite beneficiation device and method. The device comprises a mixing device, an ore grinding device, a rare earth flotation device, a magnetic separation device and a tailing flocculation device; the mixing device is used for mixing the bastnaesite and water to prepare mixed ore pulp; the ore grinding device is used for grinding the mixed ore pulp to form ore grinding ore pulp; the rare earth flotation device is used for carrying out rare earth flotation on the ore grinding pulp in the presence of a calcium ion chelating agent to obtain flotation concentrate pulp and tailing pulp; the magnetic separation device is used for carrying out magnetic separation on the flotation concentrate pulp; the tailing flocculation device is used for lime milk flocculation on tailing pulp. The bastnaesite dressing device provided by the invention can be used for rapidly treating flotation tailing pulp on the basis of not influencing the rare earth flotation effect, return water is effectively recycled, and a large amount of water resources are saved on the basis of ensuring the production efficiency.
Description
Technical Field
The invention relates to the technical field of wet-process ore smelting, in particular to a bastnaesite ore dressing device and method.
Background
Bastnaesite is the main mineral for extracting light rare earth elements. The bastnaesite rare earth resources usually contain minerals such as fluorite, barite, quartz, chlorite, kaolin, limonite, hematite, illite and the like associated with minerals, such as bayan obo rare earth ore, yak plateau rare earth ore and the like. The rare earth in the bastnaesite is extracted mainly by a rare earth flotation method: the patent with publication numbers of CN201910703570.X, CN110449257A, CN110449258A, CN110639690A and CN109395887A discloses different rare earth beneficiation methods, and relates to rare earth beneficiation reagents or beneficiation processes. In order to improve the rare earth beneficiation index, water glass is mostly adopted as a gangue dispersing agent and an inhibitor in the patents. However, in these patents, only the reagent or process improvement is performed for the flotation effect of the rare earth, and the recycling manner of the water largely used in the flotation process, especially the water in the flotation tailings, is not involved.
Due to the use of water glass, the ore pulp of the flotation tailings is highly dispersed, so that the flotation tailings are difficult to settle, the backwater water quality of the tailings is poor, the solid content (fine particles or micro-fine particles) is high, on one hand, the tailings settle slowly, and the backwater total amount does not meet the flotation requirement; on the other hand, the backwater quality of the tailings is poor, and the negative influence is caused on the mineral dressing index. Therefore, part (or all) of the fresh water needs to be supplemented during the flotation, so that the consumption of the fresh water is increased, and the production cost of ore dressing is increased. The tailings are discharged to a tailing pond, and return to a beneficiation system after long-time sunlight exposure, aeration and natural tailing clarification, so that the production water can be satisfied under the condition of abundant water source in rainy season. However, if the rainwater is reduced and the temperature is reduced in winter, the tailing pond is not sufficient in rainwater supplement, sunlight exposure and aeration, so that the solid particles remained in the backwater are not fully settled, and the medicament is not fully degraded, and the backwater recycling requirement cannot be met. Causing the shortage of water source in the factory selection and affecting the normal production.
For the reasons, a new bastnaesite beneficiation method is needed to be provided so as to more effectively treat the rare earth flotation tailing pulp and better recycle the backwater obtained by tailing pulp treatment on the premise of not influencing the flotation effect, and the purpose of saving water resources as much as possible is achieved.
Disclosure of Invention
The invention mainly aims to provide a bastnaesite beneficiation device and method, and aims to solve the problems that tailing pulp of bastnaesite rare earth flotation is difficult to settle, return water cannot be effectively utilized or the rare earth flotation effect is influenced in the prior art.
In order to achieve the above object, according to one aspect of the present invention, there is provided an ore dressing apparatus for bastnaesite, comprising: the mixing device is provided with a bastnaesite inlet, a first water inlet and a mixed ore pulp outlet, and is used for mixing the bastnaesite and water to prepare mixed ore pulp; the ore grinding device is provided with a mixed ore pulp inlet and an ore grinding ore pulp outlet, the mixed ore pulp inlet is connected with the mixed ore pulp outlet, and the ore grinding device is used for grinding the mixed ore pulp to form ore grinding ore pulp; the rare earth flotation device is provided with an ore grinding pulp inlet, a flotation concentrate pulp outlet, a tailing pulp outlet, a backwater inlet and a flotation reagent inlet, wherein the ore grinding pulp inlet is connected with the ore grinding pulp outlet; the rare earth flotation device is used for carrying out rare earth flotation on the ore grinding pulp in the presence of a calcium ion chelating agent to obtain flotation concentrate pulp and tailing pulp; the magnetic separation device is provided with a flotation concentrate pulp inlet, a magnetic separation concentrate outlet, a magnetic separation tailing outlet and a second water inlet, the flotation concentrate pulp inlet is connected with the flotation concentrate pulp outlet, and the magnetic separation device is used for carrying out magnetic separation on the flotation concentrate pulp; the bastnaesite dressing device also comprises a lime milk supply unit, and the lime milk supply unit is connected with the flocculating agent inlet; the tailing flocculation device is used for lime milk flocculation on tailing pulp.
Further, the calcium ion chelating agent supply unit is for supplying EDTA, sodium iminodisuccinate, EGTA, sodium hexametaphosphate, pyrophosphoric acid, pyrophosphates, citric acid, citrates, tartaric acid, tartrates, gluconic acid, or gluconates as the calcium ion chelating agent.
Further, bastnaesite ore dressing device still includes: a pH regulator supply unit connected to the flotation agent inlet for supplying a pH regulator; a dispersant supply unit connected to the flotation agent inlet for providing a dispersant; and the collector supply unit is connected with the flotation agent inlet and is used for supplying the collector.
Further, a pH adjuster supply unit for supplying sodium hydroxide or potassium hydroxide as a pH adjuster; the dispersant supply unit is used for providing water glass as a dispersant; the collector supply unit is used to provide hydroximic acid, fatty acid and pinitol oil as collectors.
Further, the ore grinding device is a ball mill.
Furthermore, the magnetic separation device is a wet type strong magnetic separator.
According to another aspect of the present invention, there is provided a bastnaesite beneficiation method, comprising the steps of: s1, mixing the bastnaesite and water to prepare mixed ore pulp; s2, grinding the mixed ore pulp to obtain ground ore pulp; s3, performing rare earth flotation on the ore grinding pulp to obtain flotation concentrate pulp and tailing pulp; in the rare earth flotation process, adding a calcium ion chelating agent into the system; s4, carrying out magnetic separation on the flotation concentrate ore pulp to obtain magnetic separation concentrate and magnetic separation tailings; s5, adding lime milk into the tailing pulp obtained in the step S4 for flocculation to obtain reuse water and flocculated tailings; the reuse water is returned to the step S3 to adjust the concentration of the ore grinding pulp for rare earth flotation.
Further, the calcium ion chelating agent is one or more of EDTA, sodium iminodisuccinate, EGTA, sodium hexametaphosphate, pyrophosphoric acid, pyrophosphate, citric acid, citrate, tartaric acid, tartrate, gluconic acid and gluconate.
Further, the ore grinding pulp is diluted to the concentration of 10% -45%, preferably 30% by using reuse water, and then rare earth flotation is carried out; preferably, the adding amount of the calcium ion chelating agent in the diluted ore grinding pulp is 50-500 g/t.
Further, flotation reagents adopted in the rare earth flotation process comprise a pH regulator, a dispersing agent and a collecting agent; preferably, the pH adjuster is sodium hydroxide and/or potassium hydroxide; preferably, the dispersant is water glass; preferably, the collectors are hydroximic acids, fatty acids and terpineol oils.
Further, the adding amount of the pH regulator in the diluted ore grinding pulp is 200-2000 g/t; preferably, the adding amount of the dispersing agent in the diluted ore grinding pulp is 300-3000 g/t; preferably, the addition amount of the hydroximic acid in the diluted ore grinding pulp is 200-2000 g/t, the addition amount of the fatty acid in the diluted ore grinding pulp is 200-1500 g/t, and the addition amount of the pine oil in the diluted ore grinding pulp is 20-200 g/t.
Furthermore, the adding amount of the lime milk in the tailing pulp is 500-5000 g/t calculated by lime, and the lime content of the lime milk is 15-35 wt%; preferably, the treatment time of the flocculation process is 3-90 min, preferably 20 min.
Further, step S4 includes: adjusting the concentration of flotation concentrate ore pulp to 25-35 wt%, and then carrying out magnetic separation under the magnetic field strength of 1.2-2.2T to obtain magnetic separation concentrate and magnetic separation tailings.
Further, in the step S1, the concentration of the mixed ore pulp is 35-65 wt%.
Further, in the step S2, a ball milling method is adopted in the process of grinding the mixed ore pulp, and particles with a particle size of not more than 74 μm in the ore pulp account for 65-85% of the total weight of the particles.
The invention provides a bastnaesite beneficiation device, which is mainly used for beneficiation of bastnaesite and comprises the following steps: and grinding the mixed ore pulp of the bastnaesite and the water, and subjecting the obtained ground ore pulp to rare earth flotation and magnetic separation in sequence to obtain rare earth which is fully extracted from the ore pulp. Importantly, the tailing pulp obtained by the rare earth flotation in the process can quickly flocculate and precipitate solid particles in the tailing pulp under the action of a lime milk flocculant, so that the obtained return water can be returned to the flotation step for diluting the ore grinding pulp. After lime milk is adopted for flocculation, calcium ions exist in backwater, so that in order to avoid the influence of the calcium ions on the rare earth flotation effect, the calcium ion chelating agent is added into a rare earth flotation system by utilizing the calcium ion chelating agent supply unit, and therefore the ore grinding ore pulp is subjected to rare earth flotation in the presence of the calcium ion chelating agent. Therefore, when the device provided by the invention is used for bastnaesite beneficiation, flotation tailing pulp can be quickly treated on the basis of not influencing the rare earth flotation effect, return water is effectively recycled, and a large amount of water resources are saved on the basis of ensuring the production efficiency.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the invention and, together with the description, serve to explain the invention and not to limit the invention. In the drawings:
fig. 1 shows a schematic structural view of a bastnaesite beneficiation plant according to an embodiment of the present invention.
Wherein the figures include the following reference numerals:
100. a mixing device; 101. a bastnaesite inlet; 102. a first water inlet; 103. a mixed pulp outlet; 200. a grinding device; 201. a mixed pulp inlet; 202. an ore pulp grinding outlet; 300. a rare earth flotation device; 301. an ore pulp grinding inlet; 302. an ore pulp outlet of flotation concentrate; 303. a tailing pulp outlet; 304. a return water inlet; 305. a flotation reagent inlet; 400. a magnetic separation device; 401. a flotation concentrate pulp inlet; 402. a magnetic concentrate outlet; 403. a magnetic separation tailing outlet; 404. a second water inlet; 500. a tailing flocculation device; 501. a tailing pulp inlet; 502. a flocculant inlet; 503. a flocculated tailing outlet; 504. and a backwater outlet.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.
As described in the background art, in the prior art, the tailing pulp of bastnaesite rare earth flotation is difficult to settle, so that the return water after the tailing pulp is treated cannot be effectively utilized or the rare earth flotation effect is influenced after the return water is recycled.
In order to solve the above problems, the present invention provides a bastnaesite dressing apparatus, as shown in fig. 1, the apparatus includes a mixing apparatus 100, an ore grinding apparatus 200, a rare earth flotation apparatus 300, a magnetic separation apparatus 400, and a tailing flocculation apparatus 500; the mixing device 100 is provided with a bastnaesite inlet 101, a first water inlet 102 and a mixed pulp outlet 103, and the mixing device 100 is used for mixing the bastnaesite and water to prepare mixed pulp; the ore grinding device 200 is provided with a mixed ore pulp inlet 201 and an ore grinding ore pulp outlet 202, the mixed ore pulp inlet 201 is connected with the mixed ore pulp outlet 103, and the ore grinding device 200 is used for grinding the mixed ore pulp to form ore grinding ore pulp; the rare earth flotation device 300 is provided with an ore grinding pulp inlet 301, a flotation concentrate pulp outlet 302, a tailing pulp outlet 303, a backwater inlet 304 and a flotation reagent inlet 305, wherein the ore grinding pulp inlet 301 is connected with the ore grinding pulp outlet 202, the bastnaesite flotation device further comprises a calcium ion chelating agent supply unit, and the chelating agent supply unit is connected with the flotation reagent inlet 305; the rare earth flotation device 300 is used for performing rare earth flotation on the ore grinding pulp in the presence of a calcium ion chelating agent to obtain flotation concentrate pulp and tailing pulp; the magnetic separation device 400 is provided with a flotation concentrate ore pulp inlet 401, a magnetic separation concentrate outlet 402, a magnetic separation tailing outlet 403 and a second water inlet 404, the flotation concentrate ore pulp inlet 401 is connected with the flotation concentrate ore pulp outlet 302, and the magnetic separation device 400 is used for carrying out magnetic separation on flotation concentrate ore pulp; the tailing flocculation device 500 is provided with a tailing pulp inlet 501, a flocculating agent inlet 502, a flocculated tailing outlet 503 and a backwater outlet 504, the tailing pulp inlet 501 is connected with the tailing pulp outlet 303, the backwater outlet 504 is connected with the backwater inlet 304, the bastnaesite beneficiation device further comprises a lime milk supply unit, and the lime milk supply unit is connected with the flocculating agent inlet 502; the tailing flocculation device 500 is used for lime milk flocculation of tailing pulp.
The main route for mineral separation of bastnaesite by adopting the device is as follows: and grinding the mixed ore pulp of the bastnaesite and the water, and subjecting the obtained ground ore pulp to rare earth flotation and magnetic separation in sequence to obtain rare earth which is fully extracted from the ore pulp. Importantly, the tailing pulp obtained by the rare earth flotation in the process can quickly flocculate and precipitate solid particles in the tailing pulp under the action of a lime milk flocculant, so that the obtained return water can be returned to the flotation step for diluting the ore grinding pulp. After lime milk is adopted for flocculation, calcium ions exist in backwater, so that in order to avoid the influence of the calcium ions on the rare earth flotation effect, the calcium ion chelating agent is added into a rare earth flotation system by utilizing the calcium ion chelating agent supply unit, and therefore the ore grinding ore pulp is subjected to rare earth flotation in the presence of the calcium ion chelating agent. Therefore, when the device provided by the invention is used for bastnaesite beneficiation, flotation tailing pulp can be quickly treated on the basis of not influencing the rare earth flotation effect, return water is effectively recycled, and a large amount of water resources are saved on the basis of ensuring the production efficiency. The method makes full use of the rare earth beneficiation wastewater, and has the advantages of simple wastewater treatment process, stable effect, low cost, convenience for large-scale industrial application and the like.
Compared with other flocculating agents such as polyacrylamide and the like, the lime milk flocculating agent is adopted to flocculate the rare earth flotation tailing pulp, so that the lime milk flocculating agent has a good flocculation effect on one hand, and the reuse water is matched with the calcium ion chelating agent for use on the other hand, so that the influence of flocculating agent residue on the rare earth recovery rate in the ore dressing process is avoided. And the calcium ion sequestrant is used to treat calcium introduced in the test or calcium ions originally present in the pulp, but may also have an effect on metal ions such as magnesium, iron, etc. if present in the pulp.
In order to further enhance the chelating effect of calcium ions to prevent them from affecting the effect of rare earth flotation, in a preferred embodiment, the calcium ion chelating agent supply unit is used to supply, but not limited to, EDTA (ethylenediaminetetraacetic acid, formula C)10H16N2O8) Imino disuccinic acidSodium peroxodisulfate, EGTA (ethylene glycol bis (2-aminoethyl ether) tetraacetic acid, formula C14H24N2O10) Sodium hexametaphosphate, pyrophosphoric acid, pyrophosphates (such as sodium pyrophosphate and potassium pyrophosphate), citric acid, citrates (such as sodium citrate and potassium citrate), tartaric acid, tartrates (such as sodium tartrate and potassium tartrate), gluconic acid or gluconates (such as sodium gluconate and potassium gluconate) as calcium ion chelators. The calcium ion chelating agents have better calcium ion chelating effect, and simultaneously do not cause adverse effect on rare earth components in ore grinding pulp, thereby better promoting rare earth flotation.
The flotation reagent in the rare earth flotation process can be a type commonly used in the field, and in a preferred embodiment, the carbon-cerium ore beneficiation device further comprises: a pH adjuster supply unit connected to the flotation agent inlet 305 for supplying a pH adjuster; a dispersant supply unit connected to the flotation agent inlet 305 for supplying a dispersant; a collector supply unit connected to the flotation agent inlet 305 for providing a collector. More preferably, the pH adjuster supply unit is for supplying sodium hydroxide or potassium hydroxide as the pH adjuster; the dispersant supply unit is used for providing water glass as a dispersant; the collector supply unit is used to provide hydroximic acid, fatty acid and pinitol oil as collectors.
In a preferred embodiment, the milling apparatus 200 is a ball mill. The ball mill is adopted for ore grinding, so that the ore grinding efficiency is higher, the ore grinding particle size is smaller, and the subsequent rare earth flotation and magnetic separation are facilitated. More preferably, the magnetic separation device 400 is a wet strong magnetic separator.
According to another aspect of the present invention, there is also provided a bastnaesite beneficiation method, which includes the steps of: s1, mixing the bastnaesite and water to prepare mixed ore pulp; s2, grinding the mixed ore pulp to obtain ground ore pulp; s3, performing rare earth flotation on the ore grinding pulp to obtain flotation concentrate pulp and tailing pulp; in the rare earth flotation process, adding a calcium ion chelating agent into the system; s4, carrying out magnetic separation on the flotation concentrate ore pulp to obtain magnetic separation concentrate and magnetic separation tailings; s5, adding lime milk into the tailing pulp obtained in the step S4 for flocculation to obtain reuse water and flocculated tailings; the reuse water is returned to the step S3 to adjust the concentration of the ore grinding pulp for rare earth flotation.
As mentioned above, the bastnaesite is subjected to ore dressing by the method, and the tailing pulp obtained by rare earth flotation rapidly flocculates and precipitates solid particles in the tailing pulp under the action of the lime milk flocculant, so that the obtained return water can be returned to the flotation step for diluting the ore grinding pulp. After lime milk is adopted for flocculation, calcium ions exist in backwater, so that in order to avoid the influence of the calcium ions on the rare earth flotation effect, the calcium ion chelating agent is added into a rare earth flotation system by utilizing the calcium ion chelating agent supply unit, and therefore the ore grinding ore pulp is subjected to rare earth flotation in the presence of the calcium ion chelating agent. Therefore, when the method provided by the invention is used for bastnaesite beneficiation, flotation tailing pulp can be quickly treated on the basis of not influencing the rare earth flotation effect, return water is effectively recycled, and a large amount of water resources are saved on the basis of ensuring the production efficiency.
In a preferred embodiment, the calcium ion chelating agent includes, but is not limited to, EDTA (ethylenediaminetetraacetic acid, formula C)10H16N2O8) Sodium iminodisuccinate, EGTA (ethylene glycol bis (2-aminoethyl ether) tetraacetic acid, formula C14H24N2O10) Sodium hexametaphosphate, pyrophosphoric acid, pyrophosphates (e.g., sodium pyrophosphate, potassium pyrophosphate, etc.), citric acid, citrates (e.g., sodium citrate, potassium citrate, etc.), tartaric acid, tartrates (e.g., sodium tartrate, potassium tartrate, etc.), gluconic acid, or gluconates (e.g., sodium gluconate, potassium gluconate, etc.). The calcium ion chelating agents have better calcium ion chelating effect, and simultaneously do not cause adverse effect on rare earth components in ore grinding pulp, thereby better promoting rare earth flotation.
In order to further improve the flotation effect and improve the recovery rate of rare earth, in a preferred embodiment, the grinding ore pulp is diluted to the concentration of 10% -45%, preferably 30% by using reuse water, and then rare earth flotation is carried out; more preferably, the adding amount of the calcium ion chelating agent in the diluted ore grinding pulp is 50-500 g/t. The addition amount of the calcium ion chelating agent is controlled within the range, so that the calcium ion chelating effect is further improved, and the rare earth flotation has a better flotation effect.
The flotation agent in the rare earth flotation process can be a type commonly used in the field, and in a preferred embodiment, the flotation agent adopted in the rare earth flotation process comprises a pH regulator, a dispersant and a collector; preferably, the pH adjuster is sodium hydroxide and/or potassium hydroxide; preferably, the dispersant is water glass; preferably, the collectors are hydroximic acids, fatty acids and terpineol oils.
In order to further improve the flotation effect and improve the recovery rate of rare earth, in a preferred embodiment, the adding amount of the pH regulator in the diluted ore grinding pulp is 200-2000 g/t; preferably, the adding amount of the dispersing agent in the diluted ore grinding pulp is 300-3000 g/t; preferably, the addition amount of the hydroximic acid in the diluted ore grinding pulp is 200-2000 g/t, the addition amount of the fatty acid in the diluted ore grinding pulp is 200-1500 g/t, and the addition amount of the pine oil in the diluted ore grinding pulp is 20-200 g/t.
In a preferred embodiment, the addition amount of the lime milk in the tailing pulp is 500-5000 g/t calculated by lime, and the lime content of the lime milk is 15-35 wt%; preferably, the treatment time of the flocculation process is 3-90 min, preferably 20 min. This enables faster and more complete flocculation of the solid particles in the tailings slurry, while minimizing calcium ion residues in the backwater.
The magnetic separation process is used for removing nonmagnetic impurities in the rare earth flotation concentrate pulp so as to further refine the rare earth. In a preferred embodiment, the step S4 includes: adjusting the concentration of flotation concentrate ore pulp to 25-35 wt%, and then carrying out magnetic separation under the magnetic field strength of 1.2-2.2T to obtain magnetic separation concentrate and magnetic separation tailings. The magnetic separation is performed under such conditions, and the recovery effect of rare earth can be further improved. In the actual operation process, the magnetic separation process preferably includes concentration and scavenging, which can be adjusted by those skilled in the art according to the actual situation and will not be described herein.
In a preferred embodiment, in the step S1, the concentration of the mixed ore pulp is 35-65 wt%. More preferably, in step S2, a ball milling method is adopted in the process of grinding the mixed pulp, and particles with a particle size of not more than 74 μm in the ground pulp account for 65-85% of the total weight of the particles. The condition is more beneficial to the subsequent rare earth flotation and magnetic separation.
The present application is described in further detail below with reference to specific examples, which should not be construed as limiting the scope of the invention as claimed.
Example 1
Rare earth ore in Sichuan contains REO 2.93%, the main rare earth minerals are bastnaesite and bastnaesite, and the gangue minerals mainly comprise quartz, fluorite, barite, calcite, muscovite, chlorite, kaolin, limonite, hematite, illite and the like.
The rare earth ore is mixed with water to obtain mixed ore pulp with the mass concentration of 50 percent, and the mixed ore pulp is sent to a ball mill for grinding to obtain the ore pulp with the grain diameter not more than 74um accounting for 80 percent. The concentration of ore grinding pulp is adjusted to 30 wt% by using backwater (the source is detailed in the following), and then 600 g of sodium hydroxide, 500g of water glass, 400 g of hydroximic acid, 500g of fatty acid, 200g of EDTA and 80 g of pine oil are added into each ton of ore pulp. And sequentially adding the agents into the ore pulp, stirring for 3min after the last agent is added, performing flotation for 4min to obtain rare earth flotation rough concentrate, and performing fine concentration on the flotation rough concentrate for 3 times to obtain rare earth flotation concentrate. Adjusting the concentration of the ore pulp of the rare earth flotation concentrate to 30 wt% by using water, and carrying out strong magnetic separation under the condition that the magnetic field intensity is 1.5T to obtain magnetic separation rough concentrate 1 and magnetic separation tailings 1. And (3) carrying out scavenging on the magnetic separation tailings 1 to obtain magnetic separation concentrates 2 and magnetic separation tailings 2, and throwing the magnetic separation tailings 2 to tailings. And combining the magnetic concentrate 1 and the magnetic concentrate 2, and then carrying out concentration for 1-3 times to obtain the final concentrate. Lime milk flocculation is carried out on tailing pulp subjected to rare earth ore flotation, and the method specifically comprises the following steps: adding flocculating agent lime milk (the lime content is 10%) into the tailing pulp, wherein the addition amount is 1000 g of the dry weight of lime added into each ton of ore, settling for 20min to obtain backwater, and returning the backwater to adjust the concentration of the ore grinding pulp.
By adopting the process, the grade of the finally obtained rare earth concentrate is 66.32 percent of the grade of the finally obtained rare earth concentrate, and the recovery rate of the rare earth is 86.25 percent. Water consumption: the backwater consumption accounts for 80 percent of the total water consumption.
Example 2
The difference from the embodiment 1 is that: the amount of EDTA added was 50 g/t. The grade of the finally obtained rare earth concentrate is 62.33 percent of the grade of the finally obtained rare earth concentrate, and the recovery rate of the rare earth is 80.72 percent. Water consumption: the backwater consumption accounts for 80 percent of the total water consumption.
Example 3
The difference from the embodiment 1 is that: the amount of EDTA added was 100 g/t. The grade of the finally obtained rare earth concentrate is 63.19 percent of the grade of the finally obtained rare earth concentrate, and the recovery rate of the rare earth is 82.96 percent. Water consumption: the backwater consumption accounts for 80 percent of the total water consumption.
Example 4
The difference from the embodiment 1 is that: the amount of EDTA added was 300 g/t. The grade of the finally obtained rare earth concentrate is 65.52% of the grade of the finally obtained rare earth concentrate, and the recovery rate of the rare earth is 85.29%. Water consumption: the backwater consumption accounts for 80 percent of the total water consumption.
Example 5
The difference from the embodiment 1 is that: the amount of EDTA added was 500 g/t. The grade of the finally obtained rare earth concentrate is 64.08% of the grade of the finally obtained rare earth concentrate, and the recovery rate of the rare earth is 87.33%. Water consumption: the backwater consumption accounts for 80 percent of the total water consumption.
Example 6
The difference from the embodiment 1 is that: the calcium ion chelating agent is different in species, is sodium iminodisuccinate and is used in an amount of 100 g/t. The grade of the finally obtained rare earth concentrate is 61.36 percent of the grade of the finally obtained rare earth concentrate, and the recovery rate of the rare earth is 80.62 percent. Water consumption: the backwater consumption accounts for 80 percent of the total water consumption.
Example 7
The difference from the embodiment 1 is that: the calcium ion chelating agent is sodium citrate with different types, and the dosage is 100 g/t. The grade of the finally obtained rare earth concentrate is 62.55 percent of the grade of the finally obtained rare earth concentrate, and the recovery rate of the rare earth is 82.18 percent. Water consumption: the backwater consumption accounts for 80 percent of the total water consumption.
Example 8
The difference from the embodiment 1 is that: the calcium ion chelating agent is EGTA. The grade of the finally obtained rare earth concentrate is 58.66% of the grade of the finally obtained rare earth concentrate, and the recovery rate of the rare earth is 79.42%. Water consumption: the backwater consumption accounts for 80 percent of the total water consumption.
Example 9
The difference from the embodiment 1 is that:
the rare earth ore is mixed with water to obtain mixed ore pulp with the mass concentration of 35 percent, and the mixed ore pulp is sent to a ball mill for grinding to obtain the ore pulp with the grain diameter not more than 74um accounting for 60 percent. The concentration of ore grinding pulp is adjusted to 25 wt% by using backwater (the source is detailed below), and then 200g of sodium hydroxide, 800 g of water glass, 200g of hydroximic acid, 200g of fatty acid, 200g of EDTA and 20 g of pine oil are added into each ton of the ore pulp. And sequentially adding the agents into the ore pulp, stirring for 3min after the last agent is added, performing flotation for 4min to obtain rare earth flotation rough concentrate, and performing fine concentration on the flotation rough concentrate for 3 times to obtain rare earth flotation concentrate. Adjusting the concentration of the ore pulp of the rare earth flotation concentrate to 30 wt% by using water, and carrying out strong magnetic separation under the condition that the magnetic field intensity is 1.5T to obtain magnetic separation rough concentrate 1 and magnetic separation tailings 1. And (3) carrying out scavenging on the magnetic separation tailings 1 to obtain magnetic separation concentrates 2 and magnetic separation tailings 2, and throwing the magnetic separation tailings 2 to tailings. And combining the magnetic concentrate 1 and the magnetic concentrate 2, and then carrying out concentration for 1-3 times to obtain the final concentrate. Lime milk flocculation is carried out on tailing pulp subjected to rare earth ore flotation, and the method specifically comprises the following steps: adding flocculating agent lime milk (the lime content is 10%) into the tailing pulp, wherein the addition amount is 1000 g of the dry weight of lime added into each ton of ore, settling for 20min to obtain backwater, and returning the backwater to adjust the concentration of the ore grinding pulp.
By adopting the process, the grade of the finally obtained rare earth concentrate is 64.22% of the grade of the finally obtained rare earth concentrate, and the recovery rate of the rare earth is 80.59%. Water consumption: the backwater consumption accounts for 80 percent of the total water consumption.
Example 10
The difference from the embodiment 1 is that:
the rare earth ore is mixed with water to obtain mixed ore pulp with the mass concentration of 55%, and the mixed ore pulp is sent to a ball mill for grinding to obtain ore pulp with the particle size not more than 74um accounting for 80%. The concentration of ore grinding pulp is adjusted to 35 wt% by using backwater (the source is detailed in the following), and then 2000g of sodium hydroxide, 3000g of water glass, 2000g of hydroximic acid, 1500g of fatty acid, 200g of EDTA and 200g of pine oil are added into each ton of ore pulp. And sequentially adding the agents into the ore pulp, stirring for 5min after the last agent is added, performing flotation for 5min to obtain rare earth flotation rough concentrate, and performing fine concentration on the flotation rough concentrate for 3 times to obtain rare earth flotation concentrate. Adjusting the concentration of the ore pulp of the rare earth flotation concentrate to 30 wt% by using water, and carrying out strong magnetic separation under the condition that the magnetic field intensity is 1.5T to obtain magnetic separation rough concentrate 1 and magnetic separation tailings 1. And (3) carrying out scavenging on the magnetic separation tailings 1 to obtain magnetic separation concentrates 2 and magnetic separation tailings 2, and throwing the magnetic separation tailings 2 to tailings. And combining the magnetic concentrate 1 and the magnetic concentrate 2, and then carrying out concentration for 1-3 times to obtain the final concentrate. Lime milk flocculation is carried out on tailing pulp subjected to rare earth ore flotation, and the method specifically comprises the following steps: adding flocculating agent lime milk (the lime content is 10%) into the tailing pulp, wherein the addition amount is 1000 g of the dry weight of lime added into each ton of ore, settling for 20min to obtain backwater, and returning the backwater to adjust the concentration of the ore grinding pulp.
By adopting the process, the grade of the finally obtained rare earth concentrate is 62.36% of the grade of the finally obtained rare earth concentrate, and the recovery rate of the rare earth is 87.96%. Water consumption: the backwater consumption accounts for 80 percent of the total water consumption.
Comparative example 1
The difference from the embodiment 1 is that: and (3) returning water is adopted, and when no chelating agent is added, the grade of the finally obtained rare earth concentrate is 46.77% of the grade of the finally obtained rare earth concentrate, and the recovery rate of the rare earth is 70.89%. Water consumption: the backwater consumption accounts for 80 percent of the total water consumption.
Comparative example 2
The difference from the embodiment 1 is that: and clear water is adopted, so that the grade of the finally obtained rare earth concentrate is 69.18% of the grade of the finally obtained rare earth concentrate, and the recovery rate of the rare earth is 90.43%. Water consumption: the clear water accounts for 100% of the total water consumption.
In a word, the invention applies the backwater of the rare earth flotation tailings to the rare earth flotation, obtains better effect and realizes the recycling of the backwater of the flotation. Specifically, compared with the method without adding the flocculating agent, the method has the advantages that the solid content of the backwater is reduced after the flocculating agent lime is added, and the influence of water glass on tailing sedimentation is eliminated. Compared with the condition that no flocculating agent is added, the tailing sedimentation speed is high after the flocculating agent lime is added. After the chelating agent is added, the influence of the agent on the flotation index is reduced. The gangue minerals mixed in the flotation concentrate can be removed through magnetic separation operation, so that the grade of the rare earth concentrate is improved.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (15)
1. A bastnaesite ore dressing device, characterized by comprising:
a mixing device (100) having a bastnaesite inlet (101), a first water inlet (102) and a mixed pulp outlet (103), the mixing device (100) being for mixing bastnaesite and water to formulate a mixed pulp;
the ore grinding device (200) is provided with a mixed ore pulp inlet (201) and an ore grinding ore pulp outlet (202), the mixed ore pulp inlet (201) is connected with the mixed ore pulp outlet (103), and the ore grinding device (200) is used for grinding the mixed ore pulp to form ore grinding ore pulp;
the rare earth flotation device (300) is provided with an ore grinding ore pulp inlet (301), a flotation concentrate ore pulp outlet (302), a tailing ore pulp outlet (303), a water return inlet (304) and a flotation reagent inlet (305), wherein the ore grinding ore pulp inlet (301) is connected with the ore grinding ore pulp outlet (202), the bastnaesite beneficiation device further comprises a calcium ion chelating agent supply unit, and the chelating agent supply unit is connected with the flotation reagent inlet (305); the rare earth flotation device (300) is used for carrying out rare earth flotation on the ore grinding ore pulp in the presence of a calcium ion chelating agent to obtain flotation concentrate ore pulp and tailing ore pulp;
a magnetic separation device (400) having a flotation concentrate pulp inlet (401), a magnetic separation concentrate outlet (402), a magnetic separation tailings outlet (403) and a second water inlet (404), the flotation concentrate pulp inlet (401) being connected to the flotation concentrate pulp outlet (302), the magnetic separation device (400) being configured to magnetically separate the flotation concentrate pulp;
the tailing flocculation device (500) is provided with a tailing pulp inlet (501), a flocculating agent inlet (502), a flocculated tailing outlet (503) and a backwater outlet (504), the tailing pulp inlet (501) is connected with the tailing pulp outlet (303), the backwater outlet (504) is connected with the backwater inlet (304), the bastnaesite beneficiation device further comprises a lime milk supply unit, and the lime milk supply unit is connected with the flocculating agent inlet (502); the tailing flocculation device (500) is used for lime milk flocculation on tailing pulp.
2. The bastnaesite beneficiation apparatus according to claim 1, wherein the calcium ion chelating agent supply unit is configured to supply EDTA, sodium iminodisuccinate, EGTA, sodium hexametaphosphate, pyrophosphoric acid, pyrophosphates, citric acid, citrates, tartaric acid, tartrates, gluconic acid, or gluconates as the calcium ion chelating agent.
3. The bastnaesite beneficiation apparatus according to claim 1 or 2, further comprising:
a pH adjuster supply unit connected to the flotation agent inlet (305) for supplying a pH adjuster;
a dispersant supply unit connected to the flotation agent inlet (305) for providing a dispersant;
a collector supply unit connected to the flotation agent inlet (305) for providing a collector.
4. The bastnaesite beneficiation apparatus according to claim 3, wherein the pH adjuster supply unit is configured to supply sodium hydroxide or potassium hydroxide as the pH adjuster; the dispersant supply unit is used for providing water glass as the dispersant; the collector supply unit is used to provide hydroximic acid, fatty acid and pinitol oil as the collector.
5. The bastnaesite beneficiation plant according to claim 1 or 2, wherein the ore grinding device (200) is a ball mill.
6. The bastnaesite beneficiation device according to claim 1 or 2, wherein the magnetic separation device (400) is a wet type strong magnetic separator.
7. The bastnaesite beneficiation method is characterized by comprising the following steps of:
s1, mixing the bastnaesite and water to prepare mixed ore pulp;
s2, grinding the mixed ore pulp to obtain ground ore pulp;
s3, performing rare earth flotation on the ore grinding pulp to obtain flotation concentrate pulp and tailing pulp; adding a calcium ion chelating agent into the system in the rare earth flotation process;
s4, carrying out magnetic separation on the flotation concentrate ore pulp to obtain magnetic separation concentrate and magnetic separation tailings;
s5, adding lime milk into the tailing pulp obtained in the step S4 for flocculation to obtain reuse water and flocculated tailings; returning the reuse water to the step S3 to adjust the concentration of the ore grinding slurry for the rare earth flotation.
8. The bastnaesite beneficiation method according to claim 7, wherein the calcium ion chelating agent is one or more of EDTA, sodium iminodisuccinate, EGTA, sodium hexametaphosphate, pyrophosphoric acid, pyrophosphates, citric acid, citrates, tartaric acid, tartrates, gluconic acid, gluconates.
9. The bastnaesite beneficiation method according to claim 7 or 8, wherein the ore grinding slurry is diluted to a concentration of 10% to 45%, preferably 30%, with the reuse water, and then the rare earth flotation is performed;
preferably, the adding amount of the calcium ion chelating agent in the diluted ore grinding pulp is 50-500 g/t.
10. The bastnaesite beneficiation method according to claim 9, wherein the flotation reagents used in the rare earth flotation process include a pH adjuster, a dispersant, and a collector;
preferably, the pH adjuster is sodium hydroxide and/or potassium hydroxide;
preferably, the dispersant is water glass;
preferably, the collectors are hydroximic acids, fatty acids and pinitol oils.
11. The bastnaesite beneficiation method according to claim 10, wherein the amount of the pH adjuster added to the diluted ore grinding slurry is 200 to 2000 g/t; preferably, the adding amount of the dispersing agent in the diluted ore grinding pulp is 300-3000 g/t; preferably, the addition amount of the hydroximic acid in the diluted ore grinding pulp is 200-2000 g/t, the addition amount of the fatty acid in the diluted ore grinding pulp is 200-1500 g/t, and the addition amount of the pine oil in the diluted ore grinding pulp is 20-200 g/t.
12. The bastnaesite beneficiation method according to any one of claims 7 to 11, wherein the lime milk is added to the tailing pulp in an amount of 500 to 5000g/t in terms of lime, and the lime content of the lime milk is 15 to 35 wt%; preferably, the treatment time of the flocculation process is 3-90 min, preferably 20 min.
13. The bastnaesite beneficiation method according to any one of claims 7 to 11, wherein the step S4 includes: adjusting the concentration of the flotation concentrate ore pulp to 25-35 wt%, and then carrying out magnetic separation under the magnetic field strength of 1.2-2.2T to obtain the magnetic separation concentrate and the magnetic separation tailings.
14. The bastnaesite beneficiation method according to any one of claims 7 to 11, wherein in the step S1, the mixed pulp has a concentration of 35 to 65 wt%.
15. The bastnaesite beneficiation method according to claim 14, wherein in the step S2, a ball milling method is adopted in the ore grinding process of the mixed ore pulp, and particles with a particle size of not more than 74 μm in the ore grinding ore pulp account for 65-85% of the total particle weight.
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