Beneficiation method for lead-zinc-sulfur separation of high-grade lead-zinc sulfide ore

Abstract

The invention relates to the technical field of lead-zinc ore flotation, in particular to a beneficiation method for lead-zinc-sulfur separation of high-grade lead-zinc sulfide ore. The method comprises the following steps: grinding high-grade lead-zinc sulfide ore, then adding an inhibitor and a collecting agent, stirring and mixing slurry, and carrying out one-roughing and three-scavenging flotation to obtain lead rough concentrate and lead flotation tailings; the lead rough concentrate is ground again, then an inhibitor and a collecting agent are added, and lead concentrate is obtained after three times of concentration; zinc flotation is conducted on the lead flotation tailings, specifically, a regulator I, an inhibitor I and a collecting agent I are added into the lead flotation tailings, stirring and size mixing are conducted, and zinc concentrate and zinc flotation tailings are obtained after one-roughing-one-concentrating-three-scavenging flotation is conducted; sulfur flotation is conducted on the zinc flotation tailings, specifically, a regulator II and a collecting agent II are added into the zinc flotation tailings, stirring and size mixing are conducted, and sulfur concentrate and tailings are obtained after roughing, concentrating and scavenging flotation is conducted; through overall separation of lead, zinc and sulfur target minerals in the high-grade lead-zinc sulfide ore, the lead and zinc recovery rate of the high-grade lead-zinc sulfide ore is improved.

Description

Technical Field

[0001] The invention relates to the technical field of lead-zinc ore flotation, and in particular to a beneficiation method for separating lead, zinc and sulfur from high-grade lead-zinc sulfide ore. Background Art

[0002] The ore structure of lead-zinc mines is generally complex, with a wide variety of useful minerals and a close relationship between the inter-associated minerals. These factors together lead to the complexity and diversity of the flotation process of lead-zinc ore beneficiation. For the flotation of sulfide lead-zinc ores, common principle processes include priority flotation, full mixed flotation, partial mixed flotation, equal flotation, asynchronous flotation and branch series flotation. The separation of lead, zinc and sulfur minerals in the lead-zinc ore dressing process is the key to affecting the quality of concentrate products and the recovery rate of lead and zinc metals. In 2023, the proven resource reserves of lead and zinc mines in China were: 24.8745 million tons of lead ore, a year-on-year increase of 13.8%; 59.9271 million tons of zinc ore, a year-on-year increase of 30.1%. The grade of lead-zinc ore is still mainly medium grade, with fewer rich ores. The rich ore reserves with a lead-zinc grade of more than 8% account for about 10% of the total reserves. Although the industry is generally faced with the current situation of mostly lean ores and focuses on improving metal recovery rates, for rich ore resources, through targeted research, the process and methods of metal recovery can be further optimized to achieve higher recovery rates and open up new ways for efficient use of resources. Therefore, exploring unique mineral processing processes and technical means suitable for rich ores can give full play to the advantages of rich ores such as high metal content, thereby achieving a higher level of metal recovery. This is of vital significance for optimizing the resource utilization structure, improving the overall benefits of the industry, and promoting sustainable development.

[0003] The main useful minerals in lead-zinc sulfide ore are galena and sphalerite, and the accessory mineral is pyrite. Pyrite is easy to oxidize and pollute the environment, so it is not suitable to be left in the tailings. Lead-zinc concentrators generally select three products: lead concentrate, zinc concentrate, and sulfur concentrate. The ore-dressing process is generally to prioritize lead-zinc-sulfur separation. The most common processes for zinc-sulfur separation are the priority zinc-reselection sulfur process and the zinc-sulfur mixed selection-reseparation process.

[0004] The traditional zinc selection first and sulfur selection second process requires a large amount of lime to suppress pyrite during zinc selection, and the pH value of the slurry is alkaline. During sulfur selection, a large amount of sulfuric acid is required to activate pyrite and adjust the pH value of the slurry to neutral. The addition of sulfuric acid causes the flotation equipment to be easily corroded, increasing the cost of equipment inspection and maintenance. There are also safety hazards during operation, and any careless operation may cause harm to the operator.

[0005] The traditional zinc-sulfur mixed selection-reseparation process requires a large amount of lime to suppress pyrite during zinc-sulfur separation. Due to the high impurity content of lime, it is very easy to clog the pipeline during the transportation of lime milk, resulting in insufficient lime usage and affecting production indicators. The sulfur concentrate produced by this zinc-sulfur separation process is of low grade and low value, and the mineral processing wastewater is alkaline, which makes wastewater treatment difficult and costly.

[0006] In the comparative document CN113262881A (Sulfide lead-zinc ore zinc selection agent composition and zinc-sulfur separation method), the invention uses ethylthiocarbamate as a collector and uses a new agent combination to achieve a process of preferential zinc selection and sulfur selection under the natural pH value of the ore pulp. The ore dressing wastewater is neutral, which reduces the cost of wastewater treatment. However, ethylthiocarbamate has a pungent odor, which may cause discomfort to the skin, eyes and respiratory tract, and is corrosive to plastic and rubber materials, which may cause equipment damage and is not suitable for industrial production. In addition, the invention cannot achieve the overall separation of lead, zinc and sulfur, and a lead flotation process must be performed first to achieve zinc-sulfur separation.

[0007] In the reference document CN109174467A (a method for flotation separation of lead-zinc sulfide minerals), the invention discloses that the frother is 2 # Oil, but 2 # Oil is only used in the lead flotation process, and no frother is added in the zinc flotation process. In addition, the invention only achieves the separation of lead and zinc in lead-zinc sulfide minerals, and cannot achieve the overall separation of lead, zinc and sulfur.

[0008] Therefore, for high-grade lead-zinc sulfide ore, a separation method that can achieve the overall separation of lead, zinc and sulfur is needed to improve the lead and zinc recovery rate of the lead-zinc sulfide ore.

[0009] The above contents are only used to assist in understanding the technical solution of the present invention and do not constitute an admission that the above contents are prior art. Summary of the invention

[0010] The main purpose of the present invention is to provide a beneficiation method for separating lead, zinc and sulfur from high-grade lead-zinc sulfide ore, aiming to solve the problem of how to achieve coordinated separation of lead, zinc and sulfur from high-grade lead-zinc sulfide ore, thereby improving the recovery rate of lead and zinc in high-grade lead-zinc sulfide ore.

[0011] To achieve the above object, the present invention provides a beneficiation method for separating lead, zinc and sulfur from high-grade lead-zinc sulfide ore, the method comprising:

[0012] S1, grinding high-grade lead-zinc sulfide ore, the grinding particle size is -200 mesh and reaches 75%;

[0013] S2, after grinding, depressants and collectors are added, the slurry is stirred and adjusted, and after one roughing and three sweeping flotation, lead rough concentrate and lead flotation tailings are obtained;

[0014] S3, re-grinding the lead concentrate, the grinding particle size is -320 mesh and reaches 75%, after grinding, inhibitors and collectors are added, and after three rounds of concentration, lead concentrate is obtained;

[0015] S4, zinc flotation of lead flotation tailings: add adjusting agent I, depressant I and collector I to the lead flotation tailings, stir and adjust the slurry, and obtain zinc concentrate and zinc flotation tailings after three flotations of one coarse and one fine;

[0016] S5, sulfur flotation of zinc flotation tailings: add adjuster II and collector II to zinc flotation tailings, stir and adjust the slurry, and obtain sulfur concentrate and tailings after coarse-fine-sweep flotation;

[0017] S6, additional explanation: the one rough and three sweep flotation processes in S2 are lead roughing, lead sweeping I, lead sweeping II, and lead sweeping III respectively; the three fine separation processes in S3 are lead fine I, lead fine II, and lead fine III respectively; the one rough and one fine three sweep flotation processes in S4 are zinc roughing, zinc fine separation, zinc sweeping I, zinc sweeping II, and zinc sweeping III respectively; the one rough, one fine, and one sweep flotation processes in S5 are sulfur roughing, sulfur fine separation, and sulfur sweeping selection respectively.

[0018] Optionally, the high-grade lead-zinc sulfide ore has a lead content of 4% to 8% and a zinc content of 15% to 22%.

[0019] Optionally, the inhibitor in S2 and S3 is zinc sulfate, the amount of crude lead used is 1000-2000 g / t, the amount of lead concentrate I is 20-60 g / t, and the amount of lead concentrate II is 20-60 g / t.

[0020] Optionally, the collector in S2 and S3 is P b The amount of crude lead used is 30-80g / t, the amount of lead concentrate I is 1-5g / t, the amount of lead concentrate II is 1-5g / t, the amount of lead concentrate III is 1-5g / t, the amount of lead sweep I is 3-8g / t, the amount of lead sweep II is 3-8g / t, and the amount of lead sweep III is 3-8g / t.

[0021] Optionally, the adjusting agent I in S4 is copper sulfate, and the crude zinc content is 500-1000 g / t.

[0022] Optionally, the inhibitor I in S4 is sodium sulfite, the amount of zinc used in crude production is 200-600 g / t, and the amount of zinc used in fine production is 100-300 g / t;

[0023] Optionally, in the S4, the collector I is P2, the amount of zinc roughing is 50-100 g / t, the amount of zinc sweep I is 5-15 g / t, the amount of zinc sweep II is 5-15 g / t, and the amount of zinc sweep III is 3-8 g / t.

[0024] Optionally, the adjusting agent II in S5 is 2 #The crude amount of sulfur used in oil is 5-15g / t.

[0025] Optionally, the collector II in S5 is ethyl xanthate, the crude sulfur is used in an amount of 100-300 g / t, and the sweep sulfur is used in an amount of 50-150 g / t.

[0026] The embodiment of the present invention provides a beneficiation method for separating lead, zinc and sulfur from high-grade lead-zinc sulfide ore, which has at least the following beneficial effects:

[0027] 1. By adding inhibitors and collectors in lead flotation, adjusting agent I, inhibitor I and collector I in zinc flotation, adjusting agent II and collector II in sulfur flotation, and finely controlling the added reagents, the overall separation of lead, zinc and sulfur in high-grade lead-zinc sulfide ore can be achieved, thereby improving the recovery rate of lead and zinc in high-grade lead-zinc sulfide ore;

[0028] 2. Based on the principle of the floatability of lead-zinc minerals, a lead-zinc-sulfur priority flotation process is proposed, and this mineral processing technology plan is formulated to achieve the purpose of improving the recovery rate of lead-zinc metals and ensuring the efficient utilization of resources;

[0029] 3. Firstly, the high-grade lead-zinc sulfide ore is ground to -200 mesh 75%, and then the obtained lead rough concentrate is re-grinded, and the grinding particle size is -320 mesh 75%. The two-stage grinding is adopted to realize the stage grinding and stage flotation. The re-grinding mainly plays a grinding and stripping role on the lead rough concentrate, reduces the content of over-coarse particles or the content of intergrowths and inclusions of target minerals and non-target minerals, ensures the full monomer dissociation of lead-zinc minerals, increases the uniformity of the flotation particle size of lead concentration, and realizes the effective recovery of lead minerals;

[0030] 4. Through fine control of the entire flotation process, including: lead roughing, lead scavenging I, lead scavenging II, lead scavenging III, lead concentrate I, lead concentrate II, lead concentrate III, zinc roughing, zinc concentrate, zinc scavenging I, zinc scavenging II, zinc scavenging III, sulfur roughing, sulfur concentrate, sulfur scavenging, the step-by-step separation of lead, zinc and sulfur is achieved. The technology is mature and suitable for industrial production.

[0031] 5. Sodium sulfite is used to suppress pyrite again in zinc concentration operation, which effectively reduces the pyrite content in zinc concentrate, improves the quality of zinc concentrate leaving the factory, and increases economic benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0032] Figure 1 It is a schematic diagram of the process of the present invention.

[0033] The realization of the purpose, functional features and advantages of the present invention will be further explained in conjunction with embodiments and with reference to the accompanying drawings. DETAILED DESCRIPTION

[0034] In order to better understand the above technical solution, exemplary embodiments of the present disclosure will be described in more detail below with reference to the accompanying drawings. Although exemplary embodiments of the present disclosure are shown in the accompanying drawings, it should be understood that the present disclosure can be implemented in various forms and should not be limited by the embodiments described herein. On the contrary, these embodiments are provided to enable a more thorough understanding of the present disclosure and to fully convey the scope of the present disclosure to those skilled in the art.

[0035] Based on the above description, an embodiment of a beneficiation method for separating lead, zinc and sulfur from high-grade lead-zinc sulfide ore of the present invention is proposed.

[0036] First embodiment

[0037] In this embodiment, the lead content of the lead-zinc sulfide ore is 6.79% and the zinc content is 18.72%. Figure 1 As shown, a beneficiation method for separating lead, zinc and sulfur from high-grade lead-zinc sulfide ore, the specific steps are as follows:

[0038] (1) Grind the high-grade lead-zinc ore to a size of less than 200 mesh, which accounts for 75% of the total material. For each ton of high-grade lead-zinc sulfide ore, add 1600g of zinc sulfate, 50g of collector P and 100g of zinc sulfate to the slurry. b , and carry out lead roughing operation to obtain lead rough concentrate and lead roughing tailings; 5g of collector P is added to the lead roughing tailings. b , and carry out lead scavenging I operation to obtain lead scavenging I concentrate and lead scavenging I tailings, wherein the lead scavenging I concentrate is returned to the slurry mixing and incorporated into the lead roughing operation; 5g of collector P is added to the lead scavenging I tailings b , and carry out lead scavenging II operation to obtain lead scavenging II concentrate and lead scavenging II tailings, wherein the lead scavenging II concentrate is returned to the lead scavenging I operation; 5g of collector P is added to the lead scavenging II tailings b , and carry out lead scavenging III operation to obtain lead scavenging III concentrate and lead scavenging III tailings (lead flotation tailings), among which the lead scavenging III concentrate is returned and incorporated into the lead scavenging II operation.

[0039] (2) Based on each ton of high-grade lead-zinc sulfide ore, the lead concentrate obtained in step (1) is re-ground to a size below 320 mesh, which accounts for 75% of the total material. 40 g of zinc sulfate, 2.5 g of collector P are added to the slurry in sequence. b , and carry out lead concentration I operation to obtain lead concentration I concentrate and lead concentration I tailings, wherein the lead concentration I tailings are returned to the slurry for slurry mixing and incorporated into the lead roughing operation; 40g zinc sulfate and 2.5g collector P are added to the lead concentration I concentrate. b , and carry out lead concentration II operation to obtain lead concentration II concentrate and lead concentration II tailings, wherein the lead concentration II concentrate is returned to the lead concentration I operation; 2.5g collector P is added to the lead concentration II concentrate b, carry out lead concentration III operation to obtain lead concentration III concentrate (lead concentrate) and lead concentration III tailings, of which the lead concentration III tailings are returned and incorporated into the lead concentration II operation.

[0040] (3) The lead flotation tailings obtained in step (1) are added with 400 g of sodium sulfite, 700 g of copper sulfate and 80 g of collector P2 in the ore pulp per ton of high-grade lead-zinc sulfide ore, and zinc roughing operation is carried out to obtain zinc rough concentrate and zinc roughing tailings; 10 g of collector P2 is added to the zinc roughing tailings, and zinc scavenging I operation is carried out to obtain zinc scavenging I concentrate and zinc scavenging I tailings, wherein the zinc scavenging I concentrate is returned to the slurry for mixing and incorporated into the zinc roughing operation; 10 g of collector P2 is added to the zinc scavenging I tailings, and zinc scavenging I concentrate is carried out. Conduct zinc scavenging II operation to obtain zinc scavenging II concentrate and zinc scavenging II tailings, wherein the zinc scavenging II concentrate is returned to the zinc scavenging I operation; add 10g of collector P2 to the zinc scavenging II tailings, conduct zinc scavenging III operation to obtain zinc scavenging III concentrate and zinc scavenging III tailings (zinc flotation tailings), wherein the zinc scavenging III concentrate is returned to the zinc scavenging II operation; add 200g of sodium sulfite to the zinc rough concentrate, conduct zinc concentration operation to obtain zinc concentrate and zinc concentration tailings, wherein the zinc concentration tailings are returned to the slurry for mixing and incorporated into the zinc roughing operation;

[0041] (4) The zinc flotation tailings obtained in step (3) are added to the slurry in sequence, based on the amount of high-grade lead-zinc sulfide ore. # Oil, 200g of ethyl xanthate, carry out sulfur roughing operation to obtain sulfur rough concentrate and sulfur roughing tailings; add 100g of ethyl xanthate to the sulfur roughing tailings, carry out sulfur scavenging operation to obtain sulfur scavenging concentrate and sulfur scavenging tailings, wherein the sulfur scavenging concentrate is returned to the slurry mixing and incorporated into the sulfur roughing operation; the sulfur rough concentrate is directly subjected to sulfur concentrating operation to obtain sulfur concentrate and sulfur concentrating tailings, wherein the sulfur concentrating tailings is returned to the slurry mixing and incorporated into the sulfur roughing operation;

[0042] In this embodiment, the recovery rate of lead is 92.41%, and the recovery rate of zinc is 95.63%.

[0043] Second embodiment

[0044] The lead content of the lead-zinc sulfide ore in this embodiment is 7.33% and the zinc content is 20.74%. The ore dressing method is the same as that in Example 1, and the specific steps are as follows:

[0045] (1) Grind the high-grade lead-zinc ore to a size of less than 200 mesh, which accounts for 75% of the total material. For each ton of high-grade lead-zinc sulfide ore, add 1100g of zinc sulfate, 70g of collector P and 100g of zinc sulfate to the slurry. b , and carry out lead roughing operation to obtain lead rough concentrate and lead roughing tailings; 8g of collector P is added to the lead roughing tailings. b, and carry out lead scavenging I operation to obtain lead scavenging I concentrate and lead scavenging I tailings, wherein the lead scavenging I concentrate is returned to the slurry for slurry mixing and incorporated into the lead roughing operation; 8g of collector P is added to the lead scavenging I tailings b , and carry out lead scavenging II operation to obtain lead scavenging II concentrate and lead scavenging II tailings, wherein the lead scavenging II concentrate is returned to the lead scavenging I operation; 8g of collector P is added to the lead scavenging II tailings b , and carry out lead scavenging III operation to obtain lead scavenging III concentrate and lead scavenging III tailings (lead flotation tailings), among which the lead scavenging III concentrate is returned and incorporated into the lead scavenging II operation.

[0046] (2) Based on each ton of high-grade lead-zinc sulfide ore, the lead concentrate obtained in step (1) is re-ground to a size below 320 mesh, which accounts for 75% of the total material. 25 g of zinc sulfate, 3 g of collector P and 1 g of slurry are added to the slurry in sequence. b , and carry out lead concentration I operation to obtain lead concentration I concentrate and lead concentration I tailings, of which the lead concentration I tailings are returned to the slurry for slurry mixing and incorporated into the lead roughing operation; 25g zinc sulfate and 3g collector P are added to the lead concentration I concentrate. b , and carry out lead concentration II operation to obtain lead concentration II concentrate and lead concentration II tailings, wherein the lead concentration II concentrate is returned to the lead concentration I operation; 3g of collector P is added to the lead concentration II concentrate b , carry out lead concentration III operation to obtain lead concentration III concentrate (lead concentrate) and lead concentration III tailings, of which the lead concentration III tailings are returned and incorporated into the lead concentration II operation.

[0047] (3) The lead flotation tailings obtained in step (1) are added with 200 g of sodium sulfite, 600 g of copper sulfate and 70 g of collector P2 in the ore pulp per ton of high-grade lead-zinc sulfide ore, and zinc roughing operation is carried out to obtain zinc roughing concentrate and zinc roughing tailings; 10 g of collector P2 is added to the zinc roughing tailings, and zinc scavenging I operation is carried out to obtain zinc scavenging I concentrate and zinc scavenging I tailings, wherein the zinc scavenging I concentrate is returned to the slurry for mixing and incorporated into the zinc roughing operation; 10 g of collector P2 is added to the zinc scavenging I tailings, and zinc scavenging I concentrate is carried out. Conduct zinc scavenging II operation to obtain zinc scavenging II concentrate and zinc scavenging II tailings, wherein the zinc scavenging II concentrate is returned to the zinc scavenging I operation; add 10g of collector P2 to the zinc scavenging II tailings, conduct zinc scavenging III operation to obtain zinc scavenging III concentrate and zinc scavenging III tailings (zinc flotation tailings), wherein the zinc scavenging III concentrate is returned to the zinc scavenging II operation; add 100g of sodium sulfite to the zinc rough concentrate, conduct zinc concentration operation to obtain zinc concentrate and zinc concentration tailings, wherein the zinc concentration tailings are returned to the slurry mixing and incorporated into the zinc roughing operation;

[0048] (4) The zinc flotation tailings obtained in step (3) are added to the slurry in sequence, based on the amount of high-grade lead-zinc sulfide ore. #Oil, 100g of ethyl xanthate, carry out sulfur roughing operation to obtain sulfur rough concentrate and sulfur roughing tailings; add 50g of ethyl xanthate to the sulfur roughing tailings, carry out sulfur scavenging operation to obtain sulfur scavenging concentrate and sulfur scavenging tailings, wherein the sulfur scavenging concentrate is returned to the slurry mixing and incorporated into the sulfur roughing operation; the sulfur rough concentrate is directly subjected to sulfur concentrating operation to obtain sulfur concentrate and sulfur concentrating tailings, wherein the sulfur concentrating tailings is returned to the slurry mixing and incorporated into the sulfur roughing operation;

[0049] In this embodiment, the recovery rate of lead is 92.15%, and the recovery rate of zinc is 96.95%.

[0050] The first comparison

[0051] In this embodiment, the lead content of the lead-zinc sulfide ore is 6.79% and the zinc content is 18.72%. A beneficiation method with only one stage of grinding is adopted, and the specific steps are as follows:

[0052] (1) Grind the high-grade lead-zinc ore to a size of less than 200 mesh, which accounts for 75% of the total material. For each ton of high-grade lead-zinc sulfide ore, add 1600g of zinc sulfate, 50g of collector P, b , add 10g collector P to lead scavenging I, lead scavenging II and lead scavenging III respectively b , carry out lead roughing and lead scavenging operations to obtain lead rough concentrate and lead scavenging tailings;

[0053] (2) without regrinding the lead crude concentrate obtained in step (1), 3 g of collector Pb is added to lead concentration I, 60 g of zinc sulfate and 3 g of collector Pb are added to lead concentration II, and 3 g of collector Pb is added to lead concentration III, based on each ton of high-grade lead-zinc sulfide ore, to carry out lead concentration operations to obtain lead concentrate;

[0054] (3) flotation of the lead scavenging tailings obtained in step (1), adding 600 g of copper sulfate and 70 g of collector P2 to the zinc roughing, and adding 10 g of collector P2 to the zinc scavenging I and zinc scavenging II, respectively, per ton of high-grade lead-zinc sulfide ore, and performing zinc flotation operation to obtain zinc concentrate and zinc scavenging tailings;

[0055] (4) flotation of the zinc scavenging tailings obtained in step (3), adding 60g of ethyl xanthate and 10g of 2# oil to the sulfur roughing, and adding 20g of ethyl xanthate to the sulfur scavenging, and performing sulfur flotation to obtain sulfur concentrate and tailings;

[0056] The difference from Example 1 is that only one stage of grinding is used and the reagent system is optimized.

[0057] In this embodiment, the recovery rate of lead is 89.01%, and the recovery rate of zinc is 94.91%.

[0058] In Example 1, the recovery rate of lead is 92.41%, and the recovery rate of zinc is 95.63%. By comparing the two, it can be seen that the present invention adopts two-stage grinding to achieve stage grinding and stage flotation, and the regrinding mainly plays a grinding and stripping role on the lead coarse concentrate, reduces the content of over-coarse particles or the content of intergrowths and inclusions between target minerals and non-target minerals, ensures sufficient monomer dissociation of lead and zinc minerals, increases the uniformity of flotation particle size of lead concentration, and realizes effective recovery of lead minerals. Among them, the two-stage grinding has a greater impact on the recovery rate of lead, and the recovery rate is more significantly improved.

[0059] The second comparison

[0060] The lead content of the lead-zinc sulfide ore in this comparative example is 6.21%, and the zinc content is 19.39%. The conventional flotation process is used for separation. The specific steps are as follows:

[0061] (1) The high-grade lead-zinc ore was ground to a size of less than 200 mesh, accounting for 69.04% of the total material, and flotation was performed. For each ton of high-grade sulfide lead-zinc ore, 1333 g of zinc sulfate, 200 g of ethyl xanthate, 6.7 g of 2 # Oil, 1067g zinc sulfate and 133g ethyl xanthate are added to lead-sulfur roughing II, and 33g ethyl xanthate is added to lead-sulfur scavenging I and lead-sulfur scavenging II respectively, and lead-sulfur mixed selection is carried out to obtain lead-sulfur roughing concentrate and lead-sulfur scavenging tailings;

[0062] (2) The lead-sulfur roughing concentrate obtained in step (1) is re-grinded, and the material ground to less than 320 mesh accounts for 70% of the total material for flotation. Based on each ton of high-grade lead-zinc sulfide ore, 40g of ethyl sulfide nitrogen is added to the lead separation, 13.3g of ethyl sulfide nitrogen is added to the lead scavenging I, and 6.7g of ethyl sulfide nitrogen is added to the lead scavenging II, respectively, to perform lead-sulfur separation operations to obtain lead concentrate and lead scavenging tailings;

[0063] (3) The lead scavenging tailings obtained in step (2) are subjected to flotation. Per ton of high-grade lead-zinc sulfide ore, 1333 g of lime, 267 g of copper sulfate, 67 g of butyl xanthate, 6.7 g of 2 # Oil, add 13g of butyl xanthate to zinc II scavenging I, scavenging II and scavenging III respectively, carry out zinc-sulfur separation operation, and obtain zinc II concentrate and sulfur concentrate;

[0064] (4) The lead-sulfur scavenging tailings obtained in step (1) are subjected to flotation. Based on each ton of high-grade lead-zinc sulfide ore, 467 g of copper sulfate, 133 g of butyl xanthate, 6.7 g of 2 # Oil, add 27g of butyl xanthate to zinc roughing II and zinc I scavenging I respectively, add 13g of butyl xanthate to zinc I scavenging II and zinc I scavenging III respectively, carry out zinc-sulfur mixed selection operation to obtain zinc I concentrate and tailings.

[0065] The difference between this comparative example and Example 1 is that a different mineral processing process from that of Example 1 is adopted, in which lead-sulfur mixed selection is first performed, and then lead-sulfur separation is performed, and the obtained lead scavenging tailings are then subjected to zinc-sulfur mixed selection. Compared with the step-by-step coordinated separation of lead, zinc and sulfur in the present invention, the process is more lengthy and the lead and zinc recovery steps are more complicated.

[0066] In this comparative example, the recovery rate of lead is 89.47%, and the recovery rate of zinc is 94.92%.

[0067] In Example 1, the recovery rate of lead is 92.41%, and the recovery rate of zinc is 95.63%. By comparison, it can be seen that the present invention realizes the step-by-step separation of lead, zinc and sulfur by finely controlling the entire flotation process, including: lead roughing, lead sweeping I, lead sweeping II, lead sweeping III, lead refinement I, lead refinement II, lead refinement III, zinc roughing, zinc refinement, zinc sweeping I, zinc sweeping II, zinc sweeping III, sulfur roughing, sulfur refinement and sulfur sweeping, and the technology is mature and suitable for industrial production.

[0068] The third comparison

[0069] The lead content of the lead-zinc sulfide ore in this comparative example is 6.25% and the zinc content is 18.51%. Other processes are used for separation. The specific steps are as follows:

[0070] (1) grinding high-grade lead-zinc ore to a size of less than 200 meshes, and performing flotation on 80% of the total material. For each ton of high-grade sulfide lead-zinc ore, 1200 g of zinc sulfate, 500 g of sodium sulfite, 35 g of BK906, and 4 g of BK204 are added to lead roughing I, 15 g of BK906 is added to lead roughing II, 600 g of zinc sulfate, 250 g of sodium sulfite, and 10 g of BK906 are added to lead scavenging I, and 5 g of BK906 is added to lead scavenging II. The lead roughing and lead scavenging operations are performed to obtain lead roughing concentrate and lead scavenging tailings;

[0071] (2) The lead roughing concentrate obtained in step (1) is re-grinded, and the material ground to less than 320 mesh accounts for 85% of the total material for flotation. Based on each ton of high-grade lead-zinc sulfide ore, 500g of zinc sulfate is added to lead concentration I, 300g of ethyl thiocyanate is added to lead concentration II, and 150g of ethyl thiocyanate is added to lead concentration III to carry out lead concentration operations to obtain lead concentrate and lead scavenging tailings;

[0072] (3) flotation of the lead scavenging tailings obtained in step (2), and adding 500g of zinc sulfate, 50g of ethyl thiocyanate, 30g of ethyl xanthate, and 8g of BK204 to the sulfur-zinc roughing, and adding 20g of ethyl thiocyanate and 4g of BK204 to the sulfur-zinc scavenging, to obtain a sulfur-zinc roughing concentrate and a sulfur-zinc scavenging tailings;

[0073] (4) flotation of the sulfur-zinc rougher concentrate obtained in step (3), and adding 1200 g lime, 50 g BK526, 50 g copper sulfate, and 15 g butyl xanthate to zinc-sulfur separation, 100 g lime and 10 g BK526 to zinc concentration II, 20 g copper sulfate and 10 g butyl xanthate to zinc scavenging I, and 10 g copper sulfate and 5 g butyl xanthate to zinc scavenging II, respectively, per ton of high-grade lead-zinc sulfide ore, to carry out zinc-sulfur separation to obtain zinc concentrate 2 and sulfur concentrate;

[0074] (5) flotation of the sulfur-zinc scavenging tailings obtained in step (3), and adding 300 g of copper sulfate, 200 g of butyl xanthate, and 16 g of BK204 to zinc roughing I, 100 g of copper sulfate, 100 g of butyl xanthate, and 4 g of BK204 to zinc roughing II, and 25 g of copper sulfate, 25 g of butyl xanthate, and 4 g of BK204 to zinc scavenging, to obtain zinc concentrate 1 and tailings;

[0075] The difference between this comparative example and Example 1 is that a different mineral processing process from that of Example 1 is adopted, namely, lead separation is performed first, sulfur-zinc mixed separation is performed, and finally zinc-sulfur separation is performed.

[0076] In this comparative example, the recovery rate of lead is 87.52%, and the recovery rate of zinc is 95.24%.

[0077] In Example 1, the recovery rate of lead is 92.41%, and the recovery rate of zinc is 95.63%. By comparison of the two, it can be seen that the present invention adopts a new mineral processing process, adds inhibitors and collectors in lead flotation, adds adjusting agent I, inhibitor I and collector I in the zinc flotation stage, adds adjusting agent II and collector II in the sulfur flotation stage, and realizes fine control of the added reagents, thereby realizing the coordinated separation of lead, zinc and sulfur in high-grade lead-zinc sulfide ore, and improving the recovery rates of lead and zinc in high-grade lead-zinc sulfide ore.

[0078] In summary, through the repeated experiments of Example 1 and Example 2 and the comparative experiments of Comparative Examples 1, 2 and 3, it can be shown that the present invention has significant advantages in the treatment of high-grade lead-zinc ores. Through specific process flow and innovative technical means, the present invention can effectively realize the flotation separation of pyrite, sphalerite and pyrite in high-grade lead-zinc ores, so that each mineral can be targeted for recycling and treatment, greatly improving the recycling efficiency of resources, so that the recovery rate of lead can be increased to more than 92%, and the recovery rate of zinc can be increased to more than 95%.

[0079] It should be noted that, although the preferred embodiments of the present invention have been described, those skilled in the art may make additional changes and modifications to these embodiments once they have learned the basic creative concept. Therefore, the appended claims are intended to be interpreted as including the preferred embodiments and all changes and modifications that fall within the scope of the present invention.

[0080] Obviously, those skilled in the art can make various changes and modifications to the present invention without departing from the spirit and scope of the present invention. Thus, if these modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include these modifications and variations.

Claims

1. A method for separating lead, zinc and sulfur from high-grade lead-zinc sulfide ore, characterized in that: The method comprises the following steps: S1, grinding high-grade lead-zinc sulfide ore, the grinding particle size is -200 mesh and reaches 75%; S2, after grinding, depressants and collectors are added, the slurry is stirred and adjusted, and after one roughing and three sweeping flotation, lead rough concentrate and lead flotation tailings are obtained; S3, re-grinding the lead concentrate, the grinding particle size is -320 mesh and reaches 75%, after grinding, inhibitors and collectors are added, and after three rounds of concentration, lead concentrate is obtained; S4, zinc flotation of lead flotation tailings: add adjusting agent I, depressant I and collector I to the lead flotation tailings, stir and adjust the slurry, and obtain zinc concentrate and zinc flotation tailings after three flotations of one coarse and one fine; S5, sulfur flotation of zinc flotation tailings: add adjuster II and collector II to zinc flotation tailings, stir and adjust the slurry, and obtain sulfur concentrate and tailings after coarse-fine-sweep flotation; S6, additional explanation: the one rough and three sweep flotation processes in S2 are lead roughing, lead sweeping I, lead sweeping II, and lead sweeping III respectively; the three fine separation processes in S3 are lead fine I, lead fine II, and lead fine III respectively; the one rough and one fine three sweep flotation processes in S4 are zinc roughing, zinc fine separation, zinc sweeping I, zinc sweeping II, and zinc sweeping III respectively; the one rough, one fine, and one sweep flotation processes in S5 are sulfur roughing, sulfur fine separation, and sulfur sweeping selection respectively.

2. The method according to claim 1, characterized in that the high-grade lead-zinc sulfide ore has a lead content of 4% to 8% and a zinc content of 15% to 22%.

3. The method according to claim 1, characterized in that the inhibitor in S2 and S3 is zinc sulfate, the amount of crude lead used is 1000-2000 g / t, the amount of lead concentrate I is 20-60 g / t, and the amount of lead concentrate II is 20-60 g / t.

4. The method according to claim 1, wherein the collector in S2 and S3 is P b The amount of crude lead used is 30-80g / t, the amount of lead concentrate I is 1-5g / t, the amount of lead concentrate II is 1-5g / t, the amount of lead concentrate III is 1-5g / t, the amount of lead sweep I is 3-8g / t, the amount of lead sweep II is 3-8g / t, and the amount of lead sweep III is 3-8g / t.

5. The method according to claim 1, characterized in that the adjusting agent I in S4 is copper sulfate and the amount of zinc crude used is 500-1000g / t.

6. The method according to claim 1, characterized in that the inhibitor I in S4 is sodium sulfite, the amount of zinc used in crude production is 200-600 g / t, and the amount of zinc used in fine production is 100-300 g / t.

7. The method according to claim 1, characterized in that the collector I in S4 is P2, the amount of zinc roughing is 50-100 g / t, the amount of zinc sweep I is 5-15 g / t, the amount of zinc sweep II is 5-15 g / t, and the amount of zinc sweep III is 3-8 g / t.

8. The method according to claim 1, characterized in that the adjusting agent II in S5 is 2 # The crude amount of sulfur used in oil is 5-15g / t.

9. The method according to claim 1, characterized in that the collector II in S5 is ethyl xanthate, the crude sulfur is used in an amount of 100-300 g / t, and the sweep sulfur is used in an amount of 50-150 g / t.

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