CN109174459B - Beneficiation method for high-sulfur lead-zinc ore in high-temperature environment - Google Patents
Beneficiation method for high-sulfur lead-zinc ore in high-temperature environment Download PDFInfo
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- CN109174459B CN109174459B CN201811050953.3A CN201811050953A CN109174459B CN 109174459 B CN109174459 B CN 109174459B CN 201811050953 A CN201811050953 A CN 201811050953A CN 109174459 B CN109174459 B CN 109174459B
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Abstract
The invention discloses a beneficiation method of high-sulfur lead-zinc ore in a high-temperature environment, which comprises the steps of preparing raw ore pulp with the pH value of more than 12, performing lead roughing and lead scavenging to obtain lead rough concentrate and lead scavenging tailing pulp; adding a zinc-sulfur inhibitor into the lead rough concentrate to carry out lead concentration to obtain lead concentrate; performing zinc fast flotation, zinc roughing and zinc scavenging on the lead scavenging tailing slurry to obtain zinc fast flotation rough concentrate and zinc roughing rough concentrate; regrinding the zinc rougher concentrate, then carrying out zinc-sulfur separation rougher flotation and zinc-sulfur separation scavenging, combining the zinc fast flotation rougher concentrate and the zinc-sulfur separation rougher concentrate, adding a high-sulfur inhibitor, and carrying out zinc-sulfur separation zinc cleaner concentration, thereby obtaining the zinc concentrate. The pH of the slurry is always maintained at 13 or more in each of the flotation steps. The invention can realize the high-efficiency recovery of the high-sulfur lead-zinc ore in the high-temperature environment and effectively ensure the technical indexes of the mineral separation process of the lead and zinc ore.
Description
Technical Field
The invention relates to the technical field of beneficiation of high-sulfur lead-zinc ores, in particular to a beneficiation method of high-sulfur lead-zinc ores in a high-temperature environment (the temperature of beneficiation ore pulp is more than 40 ℃).
Background
Influenced by factors such as different regions or environments, the temperature of some regions is above 35 ℃ throughout the year, and even the temperature of some regions is higher than 40-60 ℃ for a long time in one year. Because most of the concentrating mills are built outdoors or in open spaces, the temperature change of the concentrating pulp can be directly influenced by the temperature change of the site of the concentrating mill. The temperature of the ore dressing pulp of the conventional sulfide ore is generally 15-35 ℃; when the temperature of the ore dressing pulp of the sulfide ore exceeds 40 ℃ (even reaches 60 ℃), the high-temperature environment can seriously affect the dressing index of the sulfide, and the specific expression is as follows: firstly, the selectivity of the collecting agent is deteriorated, and the phenomenon that sulfides are in the same upper part and the same lower part is caused; secondly, high-sulfur minerals (pyrite and white iron ore) are difficult to inhibit, so that the grade of the concentrate is low; desorption on the surface of the medicament mineral, low efficiency of the beneficiation medicament and low recovery rate of the target mineral.
In addition, under the influence of ore formation, most of lead-zinc ore deposits contain a large amount of high-sulfur minerals such as pyrite and white iron ore (the high-sulfur minerals refer to minerals with the sulfur content of more than 40%), the high-sulfur minerals have good floatability and relatively high content, have strong adaptability to various collectors and are very difficult to inhibit, and often accompany with the lead minerals and the zinc minerals to be enriched into final concentrate, so that the grade of the concentrate is seriously influenced; because the floatability of the high-sulfur minerals is good, when the content of the high-sulfur minerals in the ore is relatively high, the high-sulfur minerals are easy to compete with target minerals (galena and sphalerite) for adsorption and quickly float to a foam product, so that the target minerals are lost to tailings after not having time to float, and the recovery rate index is directly influenced.
Aiming at the problem of high-sulfur minerals, the beneficiation method of the high-sulfur lead-zinc ore under the normal temperature condition in the prior art adopts a selective collecting agent to realize selective collection of target minerals, and simultaneously adopts means of adding lime and the like to realize inhibition of high-sulfur minerals such as pyrite, white iron ore and the like. However, in the prior art, no beneficiation method for high-sulfur lead-zinc ore in a high-temperature environment exists, so that the beneficiation method for high-sulfur lead-zinc ore in a high-temperature environment is urgently needed to be developed to solve the problem that the high-sulfur mineral in the high-temperature environment seriously interferes with the lead and zinc flotation so as to ensure the technical indexes of the beneficiation process of lead and zinc.
Disclosure of Invention
In order to solve the problem that the high-sulfur minerals in the high-temperature environment in the prior art have serious interference on the flotation of lead and zinc, the invention provides the beneficiation method of the high-sulfur lead-zinc ore in the high-temperature environment, which can realize the high-efficiency recovery of the high-sulfur lead-zinc ore in the high-temperature environment and effectively ensure the technical indexes of the beneficiation process of the lead and zinc minerals.
The purpose of the invention is realized by the following technical scheme:
a beneficiation method of high-sulfur lead-zinc ore in a high-temperature environment comprises the following steps:
step 1, wet grinding raw ore of high-sulfur lead-zinc ore, and adding a pH value regulator to prepare raw ore pulp with a pH value of more than 12;
step 3, adding a zinc-sulfur inhibitor into the lead rough concentrate, carrying out lead concentration for 2-4 times, and simultaneously adding a pH value regulator to keep the pH value of ore pulp above 13 in the lead concentration process so as to obtain lead concentrate;
step 4, adding a pH value regulator into the lead scavenging tailing slurry to enable the pH value of the lead scavenging tailing slurry to be more than 13, then adding a zinc activator, a zinc collector and a foaming agent, and performing zinc fast flotation for 1 time to obtain zinc fast flotation rough concentrate and zinc fast flotation tailing slurry;
step 6, regrinding the zinc rougher flotation rough concentrate, and simultaneously, adding a pH value regulator to keep the pH value of ore pulp above 13 in the regrinding process so as to obtain regrinding ore pulp;
step 7, adding a zinc activating agent, a zinc collecting agent and a foaming agent into the reground ore pulp, performing zinc-sulfur separation roughing and 2-4 times of zinc-sulfur separation scavenging, and simultaneously keeping the pH value of the ore pulp to be more than 13 by adding a pH value regulator in the processes of zinc-sulfur separation roughing and zinc-sulfur separation scavenging so as to obtain zinc-sulfur separation roughing zinc rough concentrate;
and 8, mixing the zinc fast flotation rough concentrate with the zinc-sulfur separation rough concentration zinc rough concentrate, adding a pH value regulator to enable the pH value of the mixed ore pulp to be more than 13, adding a high-sulfur inhibitor, a zinc activator and a zinc collector, and performing zinc-sulfur separation and concentration for 3-4 times to obtain zinc concentrate.
Preferably, in step 6, the zinc rougher coarse concentrate is mixed with the floating foam of the first zinc-sulfur separation scavenging in step 7 and the bottom flow of the first zinc-sulfur separation cleaning in step 8, and then reground, and meanwhile, the pH value of the ore pulp is kept above 13 by adding a pH value adjusting agent in the process of regrinding, so that reground ore pulp is obtained.
Preferably, in the step 1, the fraction with fineness of-0.074 mm after grinding accounts for 65-95%.
Preferably, in the step 2, at least one of ethidium chloride, aniline black powder, sodium butyl black powder and ammonium dibutyl dithiophosphate is adopted as the lead collecting agent, the using amount of the lead collecting agent in each lead roughing is 30-100 g/t of raw ore, and the using amount of the lead collecting agent in each lead scavenging is 1/4-1/2 of the lead roughing in the first lead roughing; the foaming agent is at least one of methyl isobutyl carbinol, terpineol oil and butyl ether alcohol, the dosage of the foaming agent in each lead roughing is 5-60 g/t of raw ore, and the dosage of the foaming agent in each lead scavenging is 1/4-1/2 of the lead roughing.
Preferably, in the step 3, at least one of humate, thioglycolate, sodium sulfide, zinc sulfate and sodium sulfite is adopted as the zinc-sulfur inhibitor, the dosage of the zinc-sulfur inhibitor in the first lead refining is 50-500 g/t of raw ore, and the dosage of the zinc-sulfur inhibitor in the subsequent lead refining is 0-1/2 of the first lead refining.
Preferably, in the step 4, copper sulfate is adopted as the zinc activating agent, and the using amount of the zinc activating agent in the zinc rapid flotation is 200-3000 g/t of raw ore; the zinc collector is at least one of butyl xanthate, amyl xanthate, Y89, diethyl dithiocarbamate and dibutyl dithiophosphate, and the dosage of the zinc collector in the zinc rapid flotation is 100-2000 g/t of raw ore; the foaming agent is at least one of methyl isobutyl carbinol, terpineol oil and butyl ether alcohol, and the dosage of the foaming agent in the zinc rapid flotation is 5-50 g/t of raw ore.
Preferably, in the step 5, copper sulfate is adopted as the zinc activating agent, and the dosage of the zinc activating agent in the zinc roughing is 200-3000 g/t raw ore; the zinc collector adopts at least one of butyl xanthate, amyl xanthate, Y89, diethyl dithiocarbamate and dibutyl dithiophosphate, the dosage of the zinc collector in zinc roughing is 100-2000 g/t of raw ore, and the dosage of the zinc collector in each zinc scavenging is 1/4-1/2 of the zinc roughing; the foaming agent is at least one of methyl isobutyl carbinol, terpineol oil and butyl ether alcohol, the dosage of the foaming agent in the zinc roughing is 5-50 g/t of raw ore, and the dosage of the foaming agent in each zinc scavenging is 0-1/2 of the zinc roughing.
Preferably, in step 6, the regrinding fineness is 80% of the-0.043 mm fraction to 95% of the-0.0385 mm fraction.
Preferably, in the step 7, copper sulfate is used as the zinc activator, the dosage of the zinc activator in the zinc-sulfur separation roughing is 500-5000 g/t of raw ore, and the dosage of the zinc activator in each zinc-sulfur separation scavenging is 0-1/2 of the dosage of the zinc-sulfur separation roughing; the zinc collecting agent is at least one of butyl xanthate, amyl xanthate, Y89, diethyl dithiocarbamate and dibutyl dithiophosphate, the dosage of the zinc collecting agent in the zinc-sulfur separation rough separation is 100-2000 g/t of raw ore, and the dosage of the zinc collecting agent in each zinc-sulfur separation scavenging is 0-1/2 of the zinc-sulfur separation rough separation; the foaming agent is at least one of methyl isobutyl carbinol, terpineol oil and butyl ether alcohol, the dosage of the foaming agent in the zinc-sulfur separation rough separation is 10-100 g/t of raw ore, and the dosage of the foaming agent in each zinc-sulfur separation scavenging is 0-1/2 of the zinc-sulfur separation rough separation.
Preferably, in the step 8, at least one of humate, thioglycolate and sodium sulfite is adopted as the high-sulfur inhibitor, the dosage of the high-sulfur inhibitor in the first zinc-sulfur separation concentration is 50-500 g/t of raw ore, and the dosage of the high-sulfur inhibitor in the subsequent zinc-sulfur separation concentration is 0-1/2 of the dosage of the high-sulfur inhibitor in the first zinc-sulfur separation concentration; the zinc activator adopts copper sulfate, the dosage of the zinc activator in the first zinc-sulfur separation and concentration is 100-5000 g/t of raw ore, and the dosage of the zinc activator in the subsequent zinc-sulfur separation and concentration is 0-1/2 of the dosage of the first zinc-sulfur separation and concentration; the zinc collecting agent is at least one of butyl xanthate, amyl xanthate, Y89, diethyl dithiocarbamate and dibutyl dithiophosphate, the dosage of the zinc collecting agent in the first zinc-sulfur separation and concentration process is 100-1000 g/t of raw ore, and the dosage of the zinc collecting agent in the subsequent zinc-sulfur separation and concentration process is 0-1/2 of the first zinc-sulfur separation and concentration process.
According to the technical scheme provided by the invention, the beneficiation method of the high-sulfur lead-zinc ore under the high-temperature environment effectively solves the problems of high activity, difficult inhibition and serious interference on the recovery index of the lead-zinc ore concentrate of the sulfur-containing ore in the high-temperature ore pulp by controlling the whole flotation process to be basically carried out under the high-alkali condition, adding the zinc-sulfur inhibitor during lead concentration to highly enhance and inhibit the high-sulfur minerals such as the white iron ore, the pyrite and the like, and carrying out enhanced collection with the high-selectivity collecting agent, zinc fast flotation, zinc ore regrinding and enhanced dissociation and the like, so that the high-sulfur lead-zinc ore under the high-temperature environment is effectively developed and utilized, and the grade and the recovery rate of the lead-zinc ore concentrate; meanwhile, the invention also has the advantages of simple operation, stable flow, convenient field management, strong adaptability to ore properties, high efficiency and stability of the dressing and smelting process and the like.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the description of the embodiments are briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings based on the drawings without creative efforts.
Fig. 1 is a schematic flow chart of a beneficiation method of high-sulfur lead-zinc ore in a high-temperature environment according to an embodiment of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention are clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments of the present invention without making any creative effort, shall fall within the protection scope of the present invention.
The ore dressing method for high-sulfur lead-zinc ore under high-temperature environment provided by the invention is described in detail below. Details which are not described in detail in the embodiments of the invention belong to the prior art which is known to the person skilled in the art.
As shown in fig. 1, a beneficiation method of high-sulfur lead-zinc ore in a high-temperature environment includes the following steps:
step 1, wet grinding is carried out on the raw ore of the high-sulfur lead-zinc ore, and a pH value regulator is added, so that raw ore pulp with the pH value of more than 12 is prepared.
And 2, adding a lead collecting agent and a foaming agent into the raw ore pulp, performing lead roughing for 1-2 times and lead scavenging for 1-3 times, and simultaneously adding a pH value regulator to keep the pH value of the ore pulp above 12 in the processes of lead roughing and lead scavenging, so as to obtain lead rough concentrate and lead scavenging tailing pulp.
And 3, adding a zinc-sulfur inhibitor (namely an inhibitor for inhibiting zinc minerals, pyrite and pyrite) into the lead rough concentrate, carrying out lead concentration for 2-4 times, and simultaneously adding a pH value regulator to keep the pH value of the ore pulp above 13 in the lead concentration process so as to obtain the lead concentrate.
And 4, adding a pH value regulator into the lead scavenging tailing slurry to enable the pH value of the lead scavenging tailing slurry to be more than 13, then adding a zinc activating agent, a zinc collecting agent and a foaming agent, and performing zinc rapid flotation for 1 time to obtain zinc rapid flotation rough concentrate and zinc rapid flotation tailing slurry.
And 5, adding a pH value regulator into the zinc rapid flotation tailing slurry to enable the pH value of the zinc rapid flotation tailing slurry to be more than 13, then adding a zinc activating agent, a zinc collecting agent and a foaming agent, performing zinc roughing for 1-2 times and zinc scavenging for 2-4 times, and simultaneously keeping the pH value of the ore slurry to be more than 13 by adding the pH value regulator in the zinc roughing and zinc scavenging processes, thereby obtaining zinc roughing rough concentrate.
And 6, regrinding the zinc rougher flotation rough concentrate, and simultaneously, adding a pH value regulator to keep the pH value of the ore pulp above 13 in the regrinding process so as to obtain regrinding ore pulp.
And 7, adding a zinc activating agent, a zinc collecting agent and a foaming agent into the reground ore pulp, performing zinc-sulfur separation roughing and 2-4 times of zinc-sulfur separation scavenging, and simultaneously keeping the pH value of the ore pulp to be more than 13 by adding a pH value regulator in the processes of zinc-sulfur separation roughing and zinc-sulfur separation scavenging so as to obtain zinc-sulfur separation roughing zinc rough concentrate.
And 8, mixing the zinc fast flotation rough concentrate with the zinc-sulfur separation rough concentration zinc rough concentrate, adding a pH value regulator to enable the pH value of the mixed ore pulp to be more than 13, adding a high-sulfur inhibitor, a zinc activator and a zinc collector, and performing zinc-sulfur separation and concentration for 3-4 times to obtain zinc concentrate.
Specifically, the beneficiation method for the high-sulfur lead-zinc ore in the high-temperature environment comprises the following steps:
(1) in step 1, the grinding fineness is preferably 65-95% of-0.074 mm size fraction. The pH value regulator is preferably lime; when the lime consumption reaches 3000-30000 g/t of raw ore (in the field, "3000-30000 g/t of raw ore" means 3000-30000 g/t of raw ore per ton of raw ore; in this document, the dosage of the medicament in this form represents the meaning, and only the numerical value is different), the pH value of the prepared raw ore pulp is more than 12.
(2) In the step 2, at least one of ethidium, aniline black powder, sodium butyl black powder and dibutyl ammonium dithiophosphate is adopted as the lead collecting agent, the using amount of the lead collecting agent in each lead roughing is 30-100 g/t of raw ore, and the using amount of the lead collecting agent in each lead scavenging is 1/4-1/2 of the lead roughing; the foaming agent is at least one of methyl isobutyl carbinol, terpineol oil and butyl ether alcohol, the dosage of the foaming agent in each lead roughing is 5-60 g/t of raw ore, and the dosage of the foaming agent in each lead scavenging is 1/4-1/2 of the lead roughing. The pH value regulator is preferably lime; in the lead roughing and lead scavenging processes, the dosage of lime is usually controlled to be 300-1000 g/t of raw ore, so that the pH value of ore pulp can be kept above 12.
(3) In the step 3, at least one of humate, thioglycolate, sodium sulfide, zinc sulfate and sodium sulfite is adopted as the zinc-sulfur inhibitor, the dosage of the zinc-sulfur inhibitor in the first lead refining is 50-500 g/t of raw ore, and the dosage of the zinc-sulfur inhibitor in the subsequent lead refining is 0-1/2 of the dosage of the zinc-sulfur inhibitor in the first lead refining. The pH value regulator is preferably lime; in each lead dressing process, the dosage of lime is usually controlled to be 500-10000 g/t of raw ore, namely the pH value of ore pulp is kept above 13.
(4) In the step 4, copper sulfate is adopted as the zinc activating agent, and the dosage of the zinc activating agent in the zinc rapid flotation is 200-3000 g/t of raw ore; the zinc collector is at least one of butyl xanthate, amyl xanthate, Y89, diethyl dithiocarbamate and dibutyl dithiophosphate, and the dosage of the zinc collector in the zinc rapid flotation is 100-2000 g/t of raw ore; the foaming agent is at least one of methyl isobutyl carbinol, terpineol oil and butyl ether alcohol, and the dosage of the foaming agent in the zinc rapid flotation is 5-50 g/t of raw ore. The pH value regulator is preferably lime; the using amount of lime is generally controlled to be 500-10000 g/t of raw ore, so that the pH value of the lead flotation tailing pulp is more than 13.
(5) In the step 5, copper sulfate is adopted as the zinc activating agent, and the dosage of the zinc activating agent in the zinc roughing is 200-3000 g/t raw ore; the zinc collector adopts at least one of butyl xanthate, amyl xanthate, Y89, diethyl dithiocarbamate and dibutyl dithiophosphate, the dosage of the zinc collector in zinc roughing is 100-2000 g/t of raw ore, and the dosage of the zinc collector in each zinc scavenging is 1/4-1/2 of the zinc roughing; the foaming agent is at least one of methyl isobutyl carbinol, terpineol oil and butyl ether alcohol, the dosage of the foaming agent in the zinc roughing is 5-50 g/t of raw ore, and the dosage of the foaming agent in each zinc scavenging is 0-1/2 of the zinc roughing. The pH value regulator is preferably lime; the using amount of lime is generally controlled to be 500-5000 g/t of raw ore, so that the pH value of the zinc rapid flotation tailing pulp is more than 13.
(6) In step 6, the zinc rougher concentrate is preferably mixed with the floating foam scavenged by the first zinc-sulfur separation in step 7 and the bottom flow of the first zinc-sulfur separation and concentration in step 8, and then reground, wherein the regrind degree is preferably 80% of-0.043 mm to 95% of-0.0385 mm, and the pH value of the ore pulp is kept above 13 by adding a pH value regulator during the regrinding process, so as to obtain reground ore pulp. The using amount of lime is usually controlled to be 1000-5000 g/t of raw ore, so that the pH value of the zinc rough concentration is more than 13.
(7) In the step 7, copper sulfate is adopted as the zinc activator, the dosage of the zinc activator in the zinc-sulfur separation roughing is 500-5000 g/t of raw ore, and the dosage of the zinc activator in each zinc-sulfur separation sweep is 0-1/2 of the dosage of the zinc-sulfur separation roughing; the zinc collecting agent is at least one of butyl xanthate, amyl xanthate, Y89, diethyl dithiocarbamate and dibutyl dithiophosphate, the dosage of the zinc collecting agent in the zinc-sulfur separation rough separation is 100-2000 g/t of raw ore, and the dosage of the zinc collecting agent in each zinc-sulfur separation scavenging is 0-1/2 of the zinc-sulfur separation rough separation; the foaming agent is at least one of methyl isobutyl carbinol, terpineol oil and butyl ether alcohol, the dosage of the foaming agent in the zinc-sulfur separation rough separation is 10-100 g/t of raw ore, and the dosage of the foaming agent in each zinc-sulfur separation scavenging is 0-1/2 of the zinc-sulfur separation rough separation. In the processes of zinc-sulfur separation roughing and zinc-sulfur separation scavenging, the use amount of lime is usually controlled to be 300-10000 g/t of raw ore, namely the pH value of ore pulp can be kept above 13.
(8) In step 8, at least one of humate, thioglycolate and sodium sulfite is adopted as the high-sulfur inhibitor, the dosage of the high-sulfur inhibitor in the first zinc-sulfur separation concentration is 50-500 g/t of raw ore, and the dosage of the high-sulfur inhibitor in the subsequent zinc-sulfur separation concentration is 0-1/2 of that in the first zinc-sulfur separation concentration. The zinc activator adopts copper sulfate, the dosage of the zinc activator in the first zinc-sulfur separation and concentration is 100-5000 g/t of raw ore, and the dosage of the zinc activator in the subsequent zinc-sulfur separation and concentration is 0-1/2 of the dosage of the first zinc-sulfur separation and concentration; the zinc collecting agent is at least one of butyl xanthate, amyl xanthate, Y89, diethyl dithiocarbamate and dibutyl dithiophosphate, the dosage of the zinc collecting agent in the first zinc-sulfur separation and fine separation is 100-1000 g/t of raw ore, the dosage of the zinc collecting agent in the other zinc-sulfur separation and fine separation is 1/4-1/2 of the first zinc-sulfur separation and fine separation, and the zinc collecting agent can be omitted. In the process of separating and concentrating zinc and sulfur, the dosage of lime is usually controlled to be 1000-20000 g/t of raw ore, and the pH value of ore pulp can be kept above 13.
Furthermore, the beneficiation method of the high-sulfur lead-zinc ore in the high-temperature environment controls the whole flotation process to be basically carried out under the high-alkali condition, so that high-sulfur minerals such as white iron ore, pyrite and the like in high-temperature ore pulp are effectively inhibited, the serious interference of the high-sulfur minerals on the recovery of the lead-zinc concentrate is overcome to a great extent, and favorable conditions are created for obtaining qualified lead concentrate and zinc concentrate; meanwhile, when lead concentration is carried out, the zinc-sulfur inhibitor is added to effectively inhibit high-sulfur minerals such as white iron ore, pyrite and the like in the high-temperature lead rough concentrate pulp, so that the problems that the sulfur-containing minerals in the high-temperature pulp are high in activity and difficult to inhibit and lead flotation is seriously interfered are effectively solved, the problem that the stability and the selectivity of the lead collecting agent are poor in the high-temperature environment is solved, the grade and the recovery rate index of the lead minerals in the high-temperature environment are considered, and the high lead concentrate grade and the high lead recovery rate can be obtained; in addition, the method adopts measures such as zinc mineral reinforced collection, reinforced inhibition, zinc rapid flotation, regrinding into fine-grained zinc mineral reinforced dissociation and the like, thereby effectively solving the problems of high activity, difficult inhibition and serious interference on zinc flotation of sulfur-containing minerals in high-temperature ore pulp, overcoming the trouble that the collecting force of the zinc collector is poor in high-temperature environment, considering the grade and recovery rate indexes of the zinc mineral in the high-temperature environment, and ensuring that higher zinc concentrate grade and lead recovery rate can be obtained. Therefore, the method can realize effective development and utilization of the high-sulfur lead-zinc ore (especially the high-sulfur lead-zinc ore containing the Bainite type) in a high-temperature environment, fully considers the grade and recovery rate indexes of the lead concentrate and the zinc concentrate, has better technical indexes of the mineral separation process, and has the advantages of simple operation, stable flow, convenient field management, strong adaptability to ore properties, high efficiency and stability of the mineral separation and smelting process and the like.
In conclusion, the embodiment of the invention can realize the high-efficiency recovery of the high-sulfur lead-zinc ore in the high-temperature environment, and effectively ensure the technical indexes of the mineral separation process of the lead and zinc ore.
In order to more clearly show the technical scheme and the technical effects provided by the present invention, the following detailed description is given to the ore dressing method for high-sulfur lead-zinc ore under high-temperature environment provided by the embodiment of the present invention with specific examples.
Example 1
The perennial air temperature of a certain high-sulfur lead-zinc ore area is above 35 ℃, and the air temperature of part of months is above 45 ℃; influenced by factors such as heat dissipation of a grinding machine, heat dissipation of a flotation machine, heat dissipation of a sand pump and the like, the temperature of ore pulp entering flotation after grinding is 45-57 ℃. The raw ore of the high-sulfur lead-zinc ore contains 1.72 percent of lead, 8.42 percent of zinc and 22.54 percent of sulfur. The process mineralogy research of the high-sulfur lead-zinc ore shows that: the lead-containing minerals in the ore are mainly galena and then are a small amount of white lead ore; the zinc-containing mineral mainly comprises sphalerite, and also contains a small amount of sphalerite, calamine and the like; the sulfur-containing minerals mainly comprise white iron ore and pyrite, wherein the white iron ore accounts for 28% of the total mineral composition; the gangue minerals mainly comprise quartz, calcite, mica, kaolin, feldspar, etc.; is a typical high-temperature environment pyrite-containing high-sulfur lead-zinc ore.
As shown in fig. 1, a beneficiation method of high-sulfur lead-zinc ore in a high-temperature environment, which is used for performing flotation on the high-sulfur lead-zinc ore, may specifically include the following steps:
step A1, carrying out wet grinding on the raw ore of the high-sulfur lead-zinc ore, wherein the grinding fineness is 85% of minus 0.074mm, and adding lime to adjust the pH value of ore pulp, wherein the use amount of the lime is 20kg/t of the raw ore, so as to prepare the raw ore pulp with the pH value of more than 12.
Step A2, taking ethionine and sodium butyrate black powder as lead collecting agents, taking pinitol oil as a foaming agent, sequentially adding ethionine, sodium butyrate black powder and pinitol oil into the raw ore pulp, and performing 2 times of lead roughing and 1 time of lead scavenging under the condition of aeration; in the first lead coarse selection, the dosage of ethidium and nitrogen is 50g/t of raw ore, the dosage of sodium butyrate and black powder is 20g/t of raw ore, and the dosage of pinitol oil is 35g/t of raw ore; in the second lead roughing and lead sweeping, the dosage of each medicament is 1/3 of the first lead roughing; when the second lead roughing is carried out, lime is added into the ore pulp, the using amount of the lime is 1kg/t of raw ore, and the pH value of the ore pulp is kept above 12; when lead scavenging is carried out, lime is added into ore pulp, the using amount of the lime is 800g/t of raw ore, and the pH value of the ore pulp is kept above 12; thereby obtaining lead rough concentrate and lead scavenging tailing slurry.
Step A3, adding humate, sodium sulfide and lime into the lead rough concentrate by using humate and sodium sulfide as zinc-sulfur inhibitors, and carrying out lead concentration for 4 times after stirring; in the first lead refining, the dosage of humate is 50g/t of raw ore, the dosage of sodium sulfide is 30g/t of raw ore, and the dosage of lime is 800g/t of raw ore, so that the pH value of ore pulp is kept above 13; the second lead concentration, the third lead concentration and the fourth lead concentration are carried out, the dosage of humate and sodium sulfide is 1/3 of the dosage of the first lead concentration, the dosage of lime is 500g/t of raw ore, and the pH value of ore pulp is kept above 13; thereby obtaining lead concentrate.
Step A4, copper sulfate is used as a zinc activator, Y89 and amyl xanthate are used as zinc collectors, and pine oil is used as a foaming agent; adding lime into the lead scavenging tailing slurry, wherein the using amount of the lime is 5kg/t of raw ore, so that the pH value of the lead scavenging tailing slurry is more than 13; and then adding copper sulfate, wherein the dosage of the copper sulfate is 2kg/t of raw ore, stirring for 2-3 min, sequentially adding Y89, pentylxanthate and terpineol, wherein the dosage of Y89 is 300g/t of raw ore, the dosage of pentylxanthate is 300g/t of raw ore, and the dosage of terpineol is 25g/t of raw ore, and performing zinc fast flotation for 1 time to obtain zinc fast flotation rough concentrate and zinc fast flotation tailing pulp.
Step A5, adding lime into the zinc fast flotation tailing slurry by using copper sulfate as a zinc activator, using Y89 and amyl xanthate as zinc collectors and using pine alcohol oil as a foaming agent, wherein the lime is used in an amount of 5kg/t of raw ore, so that the pH value of the zinc fast flotation tailing slurry is more than 13, then adding copper sulfate, the copper sulfate is used in an amount of 1kg/t of raw ore, stirring for 2-3 min, sequentially adding Y89, amyl xanthate and pine alcohol oil, and performing zinc roughing for 2 times and zinc scavenging for 4 times; in the first zinc coarse screening, the dosage of Y89 is 800g/t of raw ore, the dosage of amyl xanthate is 800g/t of raw ore, and the dosage of pinitol oil is 25g/t of raw ore; 1/3 of the copper sulfate, the zinc collecting agent and the foaming agent in the second zinc roughing and each zinc scavenging; and during the zinc roughing and zinc scavenging processes, lime is added to keep the pH value of the ore pulp above 13, so that the zinc roughing rough concentrate is obtained.
Step A6, mixing the zinc roughing rough concentrate with the floating foam scavenged by the first zinc-sulfur separation in the step A7 and the bottom flow of the first zinc-sulfur separation and concentration in the step A8, then regrinding, wherein the regrinding fineness is-0.038 mm and accounts for 85%, and simultaneously adding lime to adjust the pH value of ore pulp, wherein the use amount of the lime is 5kg/t of raw ore, so that the pH value of the ore pulp is kept above 13, and thus reground ore pulp is obtained.
Step A7, copper sulfate is used as a zinc activator, Y89 and amyl xanthate are used as zinc collectors, terpineol oil is used as a foaming agent, copper sulfate, Y89, amyl xanthate and terpineol oil are sequentially added into the regrind ore pulp, and zinc-sulfur separation roughing and 2-4 times of zinc-sulfur separation scavenging are carried out; in the zinc-sulfur separation coarse selection, the dosage of copper sulfate is 1000g/t of raw ore, the dosage of Y89 is 400g/t of raw ore, the dosage of amyl xanthate is 400g/t of raw ore, and the dosage of pine oil is 15g/t of raw ore; the dosage of copper sulfate in the first zinc-sulfur separation scavenging is 100g/t of raw ore, and copper sulfate is not added in other zinc-sulfur separation scavenging; the zinc collector in each zinc-sulfur separation scavenging is 1/3 of the crude separation of zinc and sulfur without adding foaming agent; lime is added in the zinc-sulfur separation roughing and each zinc-sulfur separation scavenging, the dosage of each lime is 1000g/t of raw ore, the pH value of ore pulp is kept above 13, and thus the sulfur separation roughing zinc rough concentrate is obtained.
Step A8, adopting humate and thioglycolate as high-sulfur inhibitors, adopting copper sulfate as a zinc activator, and adopting Y89 and pentylxanthate as zinc collectors; mixing the zinc fast flotation rough concentrate and the zinc-sulfur separation rough concentration together, adding lime, wherein the using amount of lime is 1000g/t of raw ore each time, keeping the pH value of ore pulp at more than 13, then sequentially adding humate, thioglycolate, copper sulfate, Y89 and pentylxanthate, and carrying out zinc-sulfur separation and fine concentration for 3-4 times, thereby obtaining zinc concentrate. In the first zinc-sulfur separation and fine selection, the dosage of humate is 60g/t of raw ore, the dosage of thioglycolate is 60g/t of raw ore, the dosage of copper sulfate is 300g/t of raw ore, the dosage of Y89 is 200g/t of raw ore, and the dosage of pentylxanthate is 200g/t of raw ore; in the second zinc-sulfur separation and fine selection, the dosage of humate and thioglycolate is 1/2 of the dosage of the first zinc-sulfur separation and fine selection, the dosage of copper sulfate is 1/4 of the dosage of the first zinc-sulfur separation and fine selection, and the dosage of Y89 and the dosage of pentylxanthate are 1/2 of the dosage of the first zinc-sulfur separation and fine selection; in the other zinc-sulfur separation and fine selection, the dosage of humate and thioglycolate is 1/2 of the dosage of the first zinc-sulfur separation and fine selection, and copper sulfate, Y89 and pentylxanthate are not added.
Specifically, by adopting the beneficiation method of the high-sulfur lead-zinc ore in the high-temperature environment provided by the embodiment 1 of the invention, most of the white iron ore is effectively inhibited, so that qualified lead concentrate and zinc concentrate are obtained; meanwhile, the problem of uneven thickness and distribution of zinc minerals in raw ores is considered, the monomer zinc minerals are quickly floated, and the loss caused by over-grinding of zinc is avoided; the regrinding operation is carried out on the fine-grain embedded zinc mineral, so that the full dissociation of the zinc mineral is realized, and the grade and the recovery rate of zinc are ensured. Finally, the grade of the obtained lead concentrate is 51.82 percent, and the grade of the obtained zinc concentrate is 47.46 percent; the lead recovery rate was 79.53% and the zinc recovery rate was 89.36%.
In conclusion, the embodiment of the invention can realize the high-efficiency recovery of the high-sulfur lead-zinc ore in the high-temperature environment, and effectively ensure the technical indexes of the mineral separation process of the lead and zinc ore.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are included in the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (10)
1. The beneficiation method of the high-sulfur lead-zinc ore in the high-temperature environment is characterized by comprising the following steps of:
step 1, wet grinding raw ore of high-sulfur lead-zinc ore, and adding a pH value regulator to prepare raw ore pulp with a pH value of more than 12;
step 2, adding a lead collecting agent and a foaming agent into the raw ore pulp, performing lead roughing for 1-2 times and lead scavenging for 1-3 times, and simultaneously adding a pH value regulator to keep the pH value of the ore pulp above 12 in the processes of lead roughing and lead scavenging so as to obtain lead rough concentrate and lead scavenging tailing pulp;
step 3, adding a zinc-sulfur inhibitor into the lead rough concentrate, carrying out lead concentration for 2-4 times, and simultaneously adding a pH value regulator to keep the pH value of ore pulp above 13 in the lead concentration process so as to obtain lead concentrate;
step 4, adding a pH value regulator into the lead scavenging tailing slurry to enable the pH value of the lead scavenging tailing slurry to be more than 13, then adding a zinc activator, a zinc collector and a foaming agent, and performing zinc fast flotation for 1 time to obtain zinc fast flotation rough concentrate and zinc fast flotation tailing slurry;
step 5, adding a pH value regulator into the zinc rapid flotation tailing slurry to enable the pH value of the zinc rapid flotation tailing slurry to be more than 13, then adding a zinc activating agent, a zinc collecting agent and a foaming agent, performing zinc roughing for 2 times and zinc scavenging for 2-4 times, and simultaneously keeping the pH value of the ore slurry to be more than 13 by adding the pH value regulator in the zinc roughing and zinc scavenging processes to obtain zinc roughing rough concentrate;
step 6, regrinding the zinc rougher flotation rough concentrate, and simultaneously, adding a pH value regulator to keep the pH value of ore pulp above 13 in the regrinding process so as to obtain regrinding ore pulp;
step 7, adding a zinc activating agent, a zinc collecting agent and a foaming agent into the reground ore pulp, performing zinc-sulfur separation roughing and 2-4 times of zinc-sulfur separation scavenging, and simultaneously keeping the pH value of the ore pulp to be more than 13 by adding a pH value regulator in the processes of zinc-sulfur separation roughing and zinc-sulfur separation scavenging so as to obtain zinc-sulfur separation roughing zinc rough concentrate;
and 8, mixing the zinc fast flotation rough concentrate with the zinc-sulfur separation rough concentration zinc rough concentrate, adding a pH value regulator to enable the pH value of the mixed ore pulp to be more than 13, adding a high-sulfur inhibitor, a zinc activator and a zinc collector, and performing zinc-sulfur separation and concentration for 3-4 times to obtain zinc concentrate.
2. The beneficiation method for high-sulfur lead-zinc ore under high temperature environment according to claim 1, characterized in that, in step 6, the zinc rougher coarse concentrate is mixed with the floating foam of the first zinc-sulfur separation scavenging in step 7 and the bottom flow of the first zinc-sulfur separation concentration in step 8, and then reground, and meanwhile, the pH value of the ore pulp is kept above 13 by adding a pH value regulator during the regrinding process, so as to obtain reground ore pulp.
3. The beneficiation method for high-sulfur lead-zinc ore under high-temperature environment according to claim 1 or 2, wherein in the step 1, the fraction of the ore ground with fineness of-0.074 mm accounts for 65-95%.
4. The beneficiation method for the high-sulfur lead-zinc ore under the high-temperature environment according to the claim 1 or 2, characterized in that in the step 2, at least one of ethidium nitrogen, aniline black, sodium butyl black and dibutyl ammonium dithiophosphate is adopted as the lead collecting agent, the using amount of the lead collecting agent in each lead roughing is 30-100 g/t of raw ore, and the using amount of the lead collecting agent in each lead scavenging is 1/4-1/2 of the lead roughing in the first lead roughing; the foaming agent is at least one of methyl isobutyl carbinol, terpineol oil and butyl ether alcohol, the dosage of the foaming agent in each lead roughing is 5-60 g/t of raw ore, and the dosage of the foaming agent in each lead scavenging is 1/4-1/2 of the lead roughing.
5. The beneficiation method for the high-sulfur lead-zinc ore under the high-temperature environment according to claim 1 or 2, wherein in the step 3, the zinc-sulfur inhibitor is at least one of humate, thioglycolate, sodium sulfide, zinc sulfate and sodium sulfite, the dosage of the zinc-sulfur inhibitor in the first lead refining is 50-500 g/t of raw ore, and the dosage of the zinc-sulfur inhibitor in the subsequent lead refining is 0-1/2 of that in the first lead refining.
6. The beneficiation method for the high-sulfur lead-zinc ore under the high-temperature environment according to claim 1 or 2, wherein in the step 4, copper sulfate is adopted as the zinc activating agent, and the using amount of the zinc activating agent in the zinc fast flotation is 200-3000 g/t of raw ore; the zinc collector is at least one of butyl xanthate, amyl xanthate, Y89, diethyl dithiocarbamate and dibutyl dithiophosphate, and the dosage of the zinc collector in the zinc rapid flotation is 100-2000 g/t of raw ore; the foaming agent is at least one of methyl isobutyl carbinol, terpineol oil and butyl ether alcohol, and the dosage of the foaming agent in the zinc rapid flotation is 5-50 g/t of raw ore.
7. The beneficiation method for the high-sulfur lead-zinc ore under the high-temperature environment according to claim 1 or 2, wherein in the step 5, copper sulfate is adopted as the zinc activating agent, and the dosage of the zinc activating agent in zinc roughing is 200-3000 g/t raw ore; the zinc collector adopts at least one of butyl xanthate, amyl xanthate, Y89, diethyl dithiocarbamate and dibutyl dithiophosphate, the dosage of the zinc collector in zinc roughing is 100-2000 g/t of raw ore, and the dosage of the zinc collector in each zinc scavenging is 1/4-1/2 of the zinc roughing; the foaming agent is at least one of methyl isobutyl carbinol, terpineol oil and butyl ether alcohol, the dosage of the foaming agent in the zinc roughing is 5-50 g/t of raw ore, and the dosage of the foaming agent in each zinc scavenging is 0-1/2 of the zinc roughing.
8. The beneficiation method for high-sulfur lead-zinc ore under high-temperature environment according to claim 1 or 2, wherein in step 6, the regrinding fineness is-0.043 mm in size fraction of 80% to-0.0385 mm in size fraction of 95%.
9. The beneficiation method for the high-sulfur lead-zinc ore under the high-temperature environment according to claim 1 or 2, wherein in the step 7, copper sulfate is adopted as the zinc activator, the dosage of the zinc activator in the zinc-sulfur separation roughing is 500-5000 g/t of raw ore, and the dosage of the zinc activator in each zinc-sulfur separation scavenging is 0-1/2 of the dosage of the zinc-sulfur separation roughing; the zinc collecting agent is at least one of butyl xanthate, amyl xanthate, Y89, diethyl dithiocarbamate and dibutyl dithiophosphate, the dosage of the zinc collecting agent in the zinc-sulfur separation rough separation is 100-2000 g/t of raw ore, and the dosage of the zinc collecting agent in each zinc-sulfur separation scavenging is 0-1/2 of the zinc-sulfur separation rough separation; the foaming agent is at least one of methyl isobutyl carbinol, terpineol oil and butyl ether alcohol, the dosage of the foaming agent in the zinc-sulfur separation rough separation is 10-100 g/t of raw ore, and the dosage of the foaming agent in each zinc-sulfur separation scavenging is 0-1/2 of the zinc-sulfur separation rough separation.
10. The beneficiation method for high-sulfur lead-zinc ore under high-temperature environment according to claim 1 or 2, characterized in that in step 8, at least one of humate, thioglycolate and sodium sulfite is adopted as the high-sulfur inhibitor, the amount of the high-sulfur inhibitor used in the first zinc-sulfur separation beneficiation is 50-500 g/t of raw ore, and the amount of the high-sulfur inhibitor used in the subsequent zinc-sulfur separation beneficiation is 0-1/2 of the first zinc-sulfur separation beneficiation; the zinc activator adopts copper sulfate, the dosage of the zinc activator in the first zinc-sulfur separation and concentration is 100-5000 g/t of raw ore, and the dosage of the zinc activator in the subsequent zinc-sulfur separation and concentration is 0-1/2 of the dosage of the first zinc-sulfur separation and concentration; the zinc collecting agent is at least one of butyl xanthate, amyl xanthate, Y89, diethyl dithiocarbamate and dibutyl dithiophosphate, the dosage of the zinc collecting agent in the first zinc-sulfur separation and concentration process is 100-1000 g/t of raw ore, and the dosage of the zinc collecting agent in the subsequent zinc-sulfur separation and concentration process is 0-1/2 of the first zinc-sulfur separation and concentration process.
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| CN115646658B (en) * | 2022-09-13 | 2023-05-23 | 彝良驰宏矿业有限公司 | Beneficiation method for high-sulfur lead zinc ore |
| CN115870099B (en) * | 2022-11-28 | 2024-06-14 | 昆明理工大学 | Method for recycling zinc from micro-fine zinc-containing high-sulfur tailings |
| CN117772405B (en) * | 2024-02-27 | 2024-05-31 | 矿冶科技集团有限公司 | Beneficiation method for difficultly-separated mixed lead-zinc ore |
| CN117772404B (en) * | 2024-02-27 | 2024-06-04 | 矿冶科技集团有限公司 | Beneficiation method for high-grade lead-zinc-sulfur ore |
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