A flotation method for lead-zinc sulfide pyrite

Abstract

The invention relates to a flotation method for lead-zinc-sulfide pyrite, and belongs to the flotation field in a mineral processing method. The lead-zinc-sulfide ore to be separated by flotation is ground to a particle size of less than 0.074 mm, which reaches 60-90%. The ore pulp is adjusted to a concentration of 28%-35%, and a regulator is added to make the pH value of the ore pulp 8-12. CaS in an amount of 1200-3200 g / t and butyl ether alcohol in an amount of 20-50 g / t are added to the obtained ore pulp to float the pyrite. A zinc inhibitor ZnSO4·7H2O in an amount of 500-1500 g / t is added to the obtained sulfur flotation tailings. The collector ethyl sulfide nitrogen is used in an amount of 40-80 g / t and the frother 2# oil is used in an amount of 30 g / t to prepare the slurry, and then the slurry is transported to the lead flotation system for flotation to obtain lead sulfide concentrate and lead flotation tailings; the obtained lead flotation tailings are added with a zinc sulfide activator CuSO4·5H2O in an amount of 100-400 g / t, a collector butyl xanthate is added in an amount of 100-200 g / t and the frother 2# oil is used in an amount of 30 g / t to prepare the slurry, and then the slurry is transported to the zinc flotation system for flotation to obtain zinc sulfide concentrate and flotation tailings; finally, high-quality pyrite concentrate, lead sulfide concentrate and zinc sulfide concentrate are obtained.

Description

Technical Field

[0001] The invention relates to a flotation method for lead-zinc sulfide pyrite, and belongs to the field of flotation in ore dressing methods. Background Art

[0002] Ore dressing is to separate useful minerals from useless or harmful minerals in mineral raw materials by physical or chemical methods, also known as "mineral processing". The products with enriched useful components are called concentrates, and the products with enriched useless components are called tailings. The concentrates provided by ore dressing are mainly used as raw materials for extracting metals in the smelting industry. Flotation is a method of separating minerals by using the different physical and chemical properties of the mineral surface. For the flotation separation of sulfide lead-zinc sulfide ore, the traditional process flow is to float lead first, then float zinc, and then float sulfur, or to float lead and sulfur first, then float zinc, and then separate lead and sulfur. The problem of floating lead suppressing sulfur or floating zinc suppressing sulfur is always involved. For these two methods, the main selective depressants are lime, zinc sulfate, sulfurous acid and salts, and cyanides; the main selective activators are copper sulfate and sulfuric acid; the main selective collectors are xanthate, black medicine, sulfur nitrogen, and thiamine esters, and a certain amount of frother is added at the same time. No matter which one is used, inhibitors, activators and collectors are indispensable for the entire process. Collectors are also essential when separately floating and enriching minerals such as galena, sphalerite, pyrite, etc. In the flotation separation process, lime is the most effective inhibitor of pyrite (pyrite, etc.), but lime also inhibits galena, which reduces the lead recovery rate and makes the lead content of zinc sulfide concentrate higher; when the traditional process is used to float sulfide lead-zinc-sulfur ore with a high oxidation rate, the lead ions dissolved in the slurry will activate sphalerite and pyrite (pyrite, etc.), resulting in difficulties in separating lead-zinc and lead-sulfur and zinc-sulfur, and the lead, zinc and sulfur concentrate products are seriously mixed with each other and have poor grades, resulting in low metal recovery rate; lime used in large quantities in the flotation process will cause scaling and blockage in the pipeline; when floating pyrite (pyrite, etc.) inhibited by lime, sulfuric acid, copper sulfate, etc. are needed for activation, but sulfuric acid and copper sulfate corrode iron equipment, the acid mist formed pollutes the environment and has safety hazards, and copper sulfate is expensive and used in large quantities. In short, the use of traditional processes to float lead-zinc-sulfur sulfides is generally reflected in poor production indicators, complex reagent systems, high costs, and difficult operations. Therefore, seeking scientific and effective treatment methods is the key to solving existing problems. Summary of the invention

[0003] Purpose of the invention: In order to overcome the problems existing in the existing lead-zinc sulfide pyrite treatment method, the present invention provides a flotation method for lead-zinc sulfide pyrite, which can avoid pipeline blockage and equipment corrosion, reduce production costs and improve the recovery rate of lead, zinc and sulfur.

[0004] The specific technical solution is: a flotation method for lead-zinc sulfide pyrite, comprising the following steps:

[0005] (1) Crushing, grinding, grading, slurry preparation and pH adjustment of slurry

[0006] After grinding the lead-zinc-sulfide ore to be separated by flotation to a particle size of less than 0.074 mm, the slurry is adjusted to a concentration of 28% to 35%, and a regulator is added to make the slurry pH 8 to 12;

[0007] (2) Flotation of pyrite concentrate

[0008] Adding 1200-3200 g / t of CaS and 20-50 g / t of butyl ether alcohol to the slurry obtained in the above (1) to float pyrite;

[0009] (3) Flotation of lead sulfide concentrate

[0010] The sulfur flotation tailings obtained by the above (2) are added with zinc inhibitor ZnSO4·7H2O in an amount of 500-1500 g / t, collector ethyl sulfide nitrogen in an amount of 40-80 g / t and frother 2# oil in an amount of 30 g / t to prepare the slurry, and then transported to the lead flotation system for flotation to obtain lead sulfide concentrate and lead flotation tailings;

[0011] (4) Flotation of zinc sulfide concentrate

[0012] The lead flotation tailings obtained in the above (3) are slurried by adding 100-400 g / t of zinc sulfide activator CuSO4·5H2O, 100-200 g / t of collector butyl xanthate and 30 g / t of frother 2# oil, and then transported to the zinc flotation system for flotation to obtain zinc sulfide concentrate and flotation tailings;

[0013] The regulator is sodium carbonate or sodium hydroxide.

[0014] Furthermore, the flotation pyrite concentrate operation is divided into: one roughing operation; two cleaning operations, in which the amount of CaS added in cleaning operation one is 100-300 g / t; two scavenging operations, in which the amount of CaS added in scavenging operation one is 200-600 g / t and butyl ether alcohol is 20-50 g / t, and in scavenging operation two, butyl ether alcohol is 10 g / t;

[0015] The flotation process of lead sulfide concentrate is divided into: one roughing process; two cleaning processes, in which the zinc inhibitor ZnSO4·7H2O is added at a dosage of 300~600g / t; two scavenging processes, in which 10~20g / t of ethyl sulfide and nitrogen and 10g / t of No. 2 oil are added in the first scavenging process, and 5~10g / t of ethyl sulfide and nitrogen and 10g / t of No. 2 oil are added in the second scavenging process;

[0016] The flotation operation of zinc sulfide concentrate is divided into: one roughing selection; two cleaning selections; two scavenging selections. In the first scavenging selection, 50-150 g / t of CuSO4·5H2O, 30-60 g / t of butyric acid and 10 g / t of 2# oil are added. In the second scavenging selection, 30-80 g / t of CuSO4·5H2O, 20-50 g / t of butyric acid and 10 g / t of 2# oil are added.

[0017] Beneficial effects:

[0018] (1) Preferential flotation of pyrite. In the traditional process, there is always the problem of preferential flotation of lead to suppress pyrite or preferential flotation of zinc to suppress pyrite. Generally, pyrite is always suppressed by lime under high alkaline conditions before adding activator sulfuric acid and collector for flotation. In the experiment, it was found that adding an appropriate amount of CaS and butyl ether alcohol can greatly improve the flotation of pyrite without the need for a collector, and at a certain concentration, CaS can strongly suppress galena and sphalerite. Therefore, by regulating CaS, it is possible to achieve preferential flotation of pyrite minerals to suppress lead and zinc minerals;

[0019] (2) The flotation of pyrite uses adjusting agents CaS and butyl ether alcohol instead of collectors such as butyl xanthate and black medicine, realizing the flotation of pyrite without collectors. The CaS dosage for roughing operation is 1200~3200g / t, the first cleaning operation is 100~300g, and the first scavenging operation is 200~600g / t; the butyl ether alcohol dosage for roughing operation is 40~100g / t, the first scavenging operation is 20~50g / t, and the second scavenging operation is 10g / t;

[0020] (3) Rapid flotation of pyrite at pH = 8-12 avoids the requirement of adding sulfuric acid for flotation at pH < 8 as required by traditional processes;

[0021] (4) ZnSO in the lead sulfide flotation cycle 4· 7H2O acts as both a lead sulfide activator and a zinc sulfide inhibitor. The reason may be that ZnSO 4· 7H2O precipitates the remaining S in the solution 2- Activates lead sulfide and simultaneously precipitates ZnS and ZnSO 4· 7H2O is used as a inhibitor of sphalerite. In roughing operations, ZnSO 4· 7H2O activates galena inhibited by CaS and inhibits zinc sulfide. Its ZnSO 4· 7H2O dosage is 500~1500g / t; in lead beneficiation operation ZnSO 4· 7H2O inhibits zinc sulfide, and its dosage is 200~600g / t;

[0022] (5) The preferred flotation process structure of first flotation of sulfur, then flotation of lead, and then flotation of zinc is adopted, which avoids the large-scale use of lime and sulfuric acid, avoids pipeline blockage and equipment corrosion, and improves the recovery rate of lead, zinc and sulfur.

[0023] In summary, the present invention provides a method for treating sulfided lead-zinc-pyrite ore which can avoid pipeline blockage, equipment corrosion, effective separation of lead, zinc and sulfur, high recovery rate of each metal, low reagent consumption, low cost, simple process, low equipment corrosion, and is safe and reliable. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] Figure 1 is a process flow chart of the present invention;

[0025] Figure 2 It is a device connection diagram of the present invention. DETAILED DESCRIPTION

[0026] like Figure 1 A flotation method for lead-zinc sulfide pyrite is shown, comprising the following steps:

[0027] (1) Crushing, grinding, grading, slurry preparation and pH adjustment of slurry

[0028] After grinding the lead-zinc-sulfide ore to be separated by flotation to a particle size of less than 0.074 mm, the slurry is adjusted to a concentration of 28% to 35%, and a regulator is added to make the slurry pH 8 to 12;

[0029] (2) Flotation of pyrite concentrate

[0030] Adding 1200-3200 g / t of CaS and 20-50 g / t of butyl ether alcohol to the slurry obtained in the above (1) to float pyrite;

[0031] (3) Flotation of lead sulfide concentrate

[0032] The sulfur flotation tailings obtained by the above (2) are added with zinc inhibitor ZnSO4·7H2O in an amount of 500-1500 g / t, collector ethyl sulfide nitrogen in an amount of 40-80 g / t and frother 2# oil in an amount of 30 g / t to prepare the slurry, and then transported to the lead flotation system for flotation to obtain lead sulfide concentrate and lead flotation tailings;

[0033] (4) Flotation of zinc sulfide concentrate

[0034] The lead flotation tailings obtained in the above (3) are slurried by adding 100-400 g / t of zinc sulfide activator CuSO4·5H2O, 100-200 g / t of collector butyl xanthate and 30 g / t of frother 2# oil, and then transported to the zinc flotation system for flotation to obtain zinc sulfide concentrate and flotation tailings;

[0035] The regulator is sodium carbonate or sodium hydroxide.

[0036] Furthermore, the flotation pyrite concentrate operation is divided into: one roughing operation; two cleaning operations, in which the amount of CaS added in cleaning operation one is 100-300 g / t; two scavenging operations, in which the amount of CaS added in scavenging operation one is 200-600 g / t and butyl ether alcohol is 20-50 g / t, and in scavenging operation two, butyl ether alcohol is 10 g / t;

[0037] The flotation process of lead sulfide concentrate is divided into: one roughing process; two cleaning processes, in which the zinc inhibitor ZnSO4·7H2O is added at a dosage of 300~600g / t; two scavenging processes, in which 10~20g / t of ethyl sulfide and nitrogen and 10g / t of No. 2 oil are added in the first scavenging process, and 5~10g / t of ethyl sulfide and nitrogen and 10g / t of No. 2 oil are added in the second scavenging process;

[0038] The flotation operation of zinc sulfide concentrate is divided into: one roughing selection; two cleaning selections; two scavenging selections. In the first scavenging selection, 50-150 g / t of CuSO4·5H2O, 30-60 g / t of butyric acid and 10 g / t of 2# oil are added. In the second scavenging selection, 30-80 g / t of CuSO4·5H2O, 20-50 g / t of butyric acid and 10 g / t of 2# oil are added.

[0039] Its preparation system, such as Figure 2 As shown, it includes a tower mill, the lower outlet of the tower mill is provided with a pump pool through a pipeline, the pump pool is connected to the inlet of the hydrocyclone through a slurry pump, the overflow outlet of the hydrocyclone is connected to the inlet of the 1# mixing barrel through a pipeline, and the sand settling outlet of the hydrocyclone is connected to the inlet of the tower mill;

[0040] The outlet of 1# mixing barrel is connected to the inlet of 2# mixing barrel, the outlet of 2# mixing barrel is connected to the inlet of sulfur rougher, the tailings outlet of sulfur rougher is connected to the first inlet of sulfur scavenger, the tailings outlet of sulfur scavenger is connected to the second inlet of sulfur scavenger, and the tailings outlet of sulfur scavenger is connected to the 3# mixing barrel and the 4# mixing barrel in sequence;

[0041] The concentrate outlet of sulfur scavenger No. 2 is connected to the inlet of sulfur scavenger No. 1, the concentrate outlet of sulfur scavenger No. 1 is connected to the inlet of sulfur rougher, the concentrate outlet of sulfur rougher is connected to the inlet of sulfur concentrator No. 1, the concentrate outlet of sulfur concentrator No. 1 is connected to the inlet of sulfur concentrator No. 2, the tailings outlet of sulfur concentrator No. 2 is connected to the inlet of sulfur concentrator No. 1, the tailings outlet of sulfur concentrator No. 1 is connected to the inlet of sulfur rougher, and the concentrate outlet of sulfur concentrator No. 2 is pyrite concentrate;

[0042] The outlet of 4# mixing barrel is connected to the inlet of lead rougher, the tailings outlet of lead rougher is connected to the first inlet of lead scavenger, the tailings outlet of lead scavenger is connected to the second inlet of lead scavenger, and the tailings outlet of lead scavenger is connected to the 5# mixing barrel and the 6# mixing barrel in sequence;

[0043] The concentrate outlet of the second lead scavenger is connected to the inlet of the first lead scavenger, the concentrate outlet of the first lead scavenger is connected to the inlet of the lead rougher, the concentrate outlet of the lead rougher is connected to the inlet of the first lead concentrator, the concentrate outlet of the first lead concentrator is connected to the inlet of the second lead concentrator, the tailings outlet of the second lead concentrator is connected to the inlet of the first lead concentrator, the tailings outlet of the first lead concentrator is connected to the inlet of the lead rougher, and the concentrate outlet of the second lead concentrator is lead sulfide concentrate;

[0044] The outlet of 6# mixing barrel is connected to the inlet of zinc rougher, the tailings outlet of zinc rougher is connected to the inlet of zinc scavenger 1, the tailings outlet of zinc scavenger 1 is connected to the inlet of zinc scavenger 2, and the tailings outlet of zinc scavenger 2 is tailings;

[0045] The concentrate outlet of zinc scavenger 2 is connected to the inlet of zinc scavenger 1, the concentrate outlet of zinc scavenger 1 is connected to the inlet of zinc rougher, the concentrate outlet of zinc rougher is connected to the inlet of zinc concentrator 1, the concentrate outlet of zinc concentrator 1 is connected to the inlet of zinc concentrator 2, the tailings outlet of zinc concentrator 2 is connected to the inlet of zinc concentrator 1, the tailings outlet of zinc concentrator 1 is connected to the inlet of zinc rougher, and the concentrate outlet of zinc concentrator 2 is zinc sulfide concentrate.

[0046] Take a pyrite ore associated with lead, zinc and silver, the main metal minerals are galena, sphalerite, pyrite, pyrrhotite, and trace amounts of lead oxide and zinc oxide. The main gangue minerals are quartz, feldspar, garnet, kaolin, etc. The particle size of galena is generally 0.03~0.09mm, and it is closely associated with sphalerite and pyrite. The particle size of sphalerite is generally 0.02~0.25mm. The particle size of pyrite is generally 0.052~0.41. The test is carried out according to the method of the present invention, and the multi-element analysis results are shown in Table 1.

[0047]

[0048] Example 1

[0049] (1) The sulfide lead-zinc-sulfur ore to be separated by flotation is coarsely ground and classified by ball milling with a tower mill and a hydrocyclone, and then the sulfide lead-zinc-sulfur ore is ground to a particle size of less than 0.074 mm, reaching 60%, and the slurry is adjusted to a concentration of 28%. The grinding concentration is 70%, and the amount of Na2CO3 added is 1000g / t, so that the pH of the slurry is 8;

[0050] (2) Prioritize flotation of pyrite.

[0051] In the traditional process, there is always the problem of preferential flotation of lead to suppress pyrite or preferential flotation of zinc to suppress pyrite. Generally, pyrite is always suppressed by lime under high alkaline conditions before adding activator sulfuric acid and collector for flotation. In the experiment, it was found that adding an appropriate amount of CaS and butyl ether alcohol can greatly improve the floatation of pyrite without collectors, and at a certain concentration, CaS can strongly suppress galena and sphalerite. Therefore, by regulating CaS, it is possible to achieve preferential flotation of pyrite minerals to suppress lead and zinc minerals.

[0052] The slurry obtained by the above (1) is transported to the 1# stirring barrel, and CaS is added in an amount of 1200g / t for 4 minutes. After the pH value is controlled at 8, the slurry enters the 2# stirring barrel, and butyl ether alcohol is added in an amount of 40g / t for 3 minutes. Then, the slurry is transported to the sulfur flotation system for flotation, and the obtained products are sulfur concentrate and sulfur flotation tailings. The sulfur flotation operation is divided into: one roughing, the flotation time is 5 minutes; two cleaning, the first cleaning is to add CaS at an amount of 100g / t, the flotation time is 4 minutes for cleaning, and the second cleaning is 3 minutes; two scavenging, the first cleaning is to add CaS at an amount of 200g / t and butyl ether alcohol at an amount of 20g / t, and the second cleaning is to add butyl ether alcohol at an amount of 10g / t, and the flotation time is 4 minutes for each.

[0053] (3) Flotation of galena

[0054] The sulfur flotation tailings obtained in (2) above are transported to the 3# stirring tank and the zinc inhibitor ZnSO is added. 4· 7H2O is used at a dosage of 500g / t for 3 minutes, and then the slurry flows into the 4# mixing barrel, and the collector ethyl sulfide nitrogen is added at a dosage of 40g / t and the frother 2# oil is used at a dosage of 30g / t for 2 minutes, and then it is transported to the lead flotation system for flotation to obtain lead sulfide concentrate and lead flotation tailings. The lead flotation operation is divided into: one roughing, the flotation time is 5 minutes; two fine cleaning, the fine cleaning first adds zinc inhibitor ZnSO 4· The dosage of 7H2O is 300g / t, and the flotation time is: 4 minutes for the first selection and 3 minutes for the second selection; there are two scavengings, 10g / t of ethyl sulfide and nitrogen and 10g / t of 2# oil are added in the first scavenging, 5g / t of ethyl sulfide and nitrogen and 10g / t of 2# oil are added in the second scavenging, and the flotation time is 4 minutes for the first scavenging and 3 minutes for the second scavenging.

[0055] (4) Flotation of zinc sulfide

[0056] The lead flotation tailings obtained by the above (3) are transported to the 5# stirring barrel, and the zinc sulfide activator CuSO4·5H2O is added in an amount of 100 g / t and the slurry is mixed for 3 minutes. Then the slurry flows into the 6# stirring barrel, and the collector butyl xanthate is added in an amount of 100 g / t and the frother 2# oil is added in an amount of 30 g / t and the slurry is mixed for 2 minutes. Then, the slurry is transported to the zinc flotation system for flotation to obtain zinc sulfide concentrate and flotation tailings. Zinc flotation operation is divided into: one roughing operation with a flotation time of 5 minutes; two cleaning operations with flotation times of 4 minutes for cleaning operation one and 3 minutes for cleaning operation two; two scavenging operations, with 50g / t of CuSO4·5H2O, 30g / t of butyric acid and 10g / t of 2# oil added in scavenging operation one, and 30g / t of CuSO4·5H2O, 20g / t of butyric acid and 10g / t of 2# oil added in scavenging operation two, and the flotation time is 4 minutes respectively.

[0057] The results show that since lime and sulfuric acid are not used, the frequency of shutdown caused by pipeline blockage and flotation equipment corrosion is reduced by about 87%, the normal start-up time is increased, and the process production is stabilized. Finally, lead concentrate with a lead grade of 65.68% and a recovery rate of 87.57%; zinc concentrate with a zinc grade of 51.45% and a recovery rate of 91.68%; and pyrite concentrate with a sulfur grade of 47.65% and a recovery rate of 86.33% were obtained.

[0058] Example 2

[0059] (1) The sulfide lead-zinc-sulfur ore to be separated by flotation is coarsely ground and graded by a combined ball mill of a tower mill and a hydrocyclone until the particle size is less than 0.074 mm, reaching 90%, and the slurry is adjusted to a concentration of 35%. The grinding concentration is 75%, and an appropriate amount of Na2CO3 is added to make the pH of the slurry 12;

[0060] (2) Prioritize flotation of pyrite.

[0061] In the traditional process, there is always the problem of preferential flotation of lead to suppress pyrite or preferential flotation of zinc to suppress pyrite. Generally, pyrite is always suppressed by lime under high alkaline conditions before adding activator sulfuric acid and collector for flotation. In the experiment, it was found that adding an appropriate amount of CaS and butyl ether alcohol can greatly improve the floatation of pyrite without collectors, and at a certain concentration, CaS can strongly suppress galena and sphalerite. Therefore, by regulating CaS, it is possible to achieve preferential flotation of pyrite minerals to suppress lead and zinc minerals.

[0062] The slurry obtained by the above (1) is transported to the 1# mixing barrel, and CaS is added in an amount of 3200g / t for 2-4 minutes. After the pH value is controlled at 12, the slurry enters the 2# mixing barrel, and butyl ether alcohol is added in an amount of 100g / t for 3 minutes. Then, it is transported to the sulfur flotation system for flotation, and the obtained products are sulfur concentrate and sulfur flotation tailings. The sulfur flotation operation is divided into: one roughing, the flotation time is 5 minutes; two fine selections, the first fine selection is added with 300g / t CaS, the flotation time is 4 minutes for fine selection, and the second fine selection is 3 minutes; two scavenging, the first scavenging is added with 600g / t CaS and 50g / t butyl ether alcohol, and the second scavenging is added with 10g / t butyl ether alcohol, and the flotation time is 4 minutes respectively.

[0063] (3) Flotation of galena

[0064] The sulfur flotation tailings obtained in (2) above are transported to the 3# stirring tank and the zinc inhibitor ZnSO is added. 4· 7H2O dosage is 1500g / t and the pulp is mixed for 3 minutes, then the pulp flows into the 4# mixing barrel, the collector ethyl sulfide nitrogen dosage is 80g / t and the frother 2# oil dosage is 30g / t and the pulp is mixed for 2 minutes, then it is transported to the lead flotation system for flotation to obtain lead sulfide concentrate and lead flotation tailings. The lead flotation operation is divided into: one roughing, the flotation time is 5 minutes; two fine cleaning, the fine cleaning first adds zinc inhibitor ZnSO 4· The dosage of 7H2O is 600g / t, and the flotation time is: 4 minutes for the first selection and 3 minutes for the second selection; there are two scavengings, 20g / t of ethyl sulfide and nitrogen and 10g / t of 2# oil are added in the first scavenging, and 10g / t of ethyl sulfide and nitrogen and 10g / t of 2# oil are added in the second scavenging. The flotation time is 4 minutes for the first scavenging and 3 minutes for the second scavenging.

[0065] (4) Flotation of zinc sulfide

[0066] The lead flotation tailings obtained by the above (3) are transported to the 5# stirring barrel, and the zinc sulfide activator CuSO4·5H2O is added in an amount of 400 g / t and the slurry is mixed for 3 minutes. Then the slurry flows into the 6# stirring barrel, and the collector butyl xanthate 200 g / t and the frother 2# oil 30 g / t are added and the slurry is mixed for 2 minutes. Then, the slurry is transported to the zinc flotation system for flotation to obtain zinc sulfide concentrate and flotation tailings. Zinc flotation operation is divided into: one roughing operation with a flotation time of 5 minutes; two cleaning operations with flotation times of 4 minutes for cleaning operation one and 3 minutes for cleaning operation two; two scavenging operations, with 150g / t of CuSO4·5H2O, 60g / t of butyric acid and 10g / t of 2# oil added in scavenging operation one, and 80g / t of CuSO4·5H2O, 50g / t of butyric acid and 10g / t of 2# oil added in scavenging operation two, and the flotation time is 4 minutes respectively.

[0067] The results show that since lime and sulfuric acid are not used, the frequency of shutdown caused by pipeline blockage and flotation equipment corrosion is reduced by about 85%, the normal start-up time is increased, and the process production is stabilized. Finally, lead concentrate with a lead grade of 68.77% and a recovery rate of 88.21% was obtained; zinc concentrate with a zinc grade of 50.83% and a recovery rate of 89.87%; and pyrite concentrate with a sulfur grade of 48.13% and a recovery rate of 87.45% were obtained.

[0068] Example 3

[0069] (1) The sulfide lead-zinc-sulfur ore to be separated by flotation is coarsely ground and graded by ball milling with a tower mill and a hydrocyclone, and then the ore is ground to a particle size of less than 0.074 mm, reaching 80%, and the ore pulp is adjusted to a concentration of 28% to 35%. The grinding concentration is 72%, and the amount of Na2CO3 added is 1000g / t, so that the pH of the ore pulp is 10;

[0070] (2) Prioritize flotation of pyrite.

[0071] In the traditional process, there is always the problem of preferential flotation of lead to suppress pyrite or preferential flotation of zinc to suppress pyrite. Generally, pyrite is always suppressed by lime under high alkaline conditions before adding activator sulfuric acid and collector for flotation. In the experiment, it was found that adding an appropriate amount of CaS and butyl ether alcohol can greatly improve the floatation of pyrite without collectors, and at a certain concentration, CaS can strongly suppress galena and sphalerite. Therefore, by regulating CaS, it is possible to achieve preferential flotation of pyrite minerals to suppress lead and zinc minerals.

[0072] The slurry obtained by the above (1) is transported to the 1# stirring barrel, and CaS is added in an amount of 3000g / t for 2-4 minutes. After the pH value is controlled at 10, the slurry enters the 2# stirring barrel, and butyl ether alcohol is added in an amount of 80g / t for 3 minutes. Then, the slurry is transported to the sulfur flotation system for flotation, and the obtained products are sulfur concentrate and sulfur flotation tailings. The sulfur flotation operation is divided into: one roughing, the flotation time is 5 minutes; two cleaning, the first cleaning is to add CaS at an amount of 200g / t, the flotation time is 4 minutes for cleaning, and the second cleaning is 3 minutes; two scavenging, the first cleaning is to add CaS at an amount of 400g / t and butyl ether alcohol at an amount of 40g / t, and the second cleaning is to add butyl ether alcohol at an amount of 10g / t, and the flotation time is 4 minutes respectively.

[0073] (3) Flotation of galena

[0074] The sulfur flotation tailings obtained in (2) above are transported to the 3# stirring tank and the zinc inhibitor ZnSO is added. 4·7H2O dosage is 1000g / t and the pulp is mixed for 3 minutes, then the pulp flows into the 4# mixing barrel, the collector ethyl sulfide nitrogen dosage is 40~80g / t and the foaming agent 2# oil dosage is 30g / t and the pulp is mixed for 2 minutes, then it is transported to the lead flotation system for flotation to obtain lead sulfide concentrate and lead flotation tailings. The lead flotation operation is divided into: one roughing, the flotation time is 5 minutes; two fine cleaning, the fine cleaning first adds zinc inhibitor ZnSO 4· The dosage of 7H2O is 400g / t, and the flotation time is: 4 minutes for the first selection and 3 minutes for the second selection; there are two scavengings, 10~20g / t of ethyl sulfide and nitrogen and 10g / t of 2# oil are added in the first scavenging, 8g / t of ethyl sulfide and nitrogen and 10g / t of 2# oil are added in the second scavenging, and the flotation time is 4 minutes for the first scavenging and 3 minutes for the second scavenging.

[0075] (4) Flotation of zinc sulfide

[0076] The lead flotation tailings obtained by the above (3) are transported to the 5# stirring barrel, and the zinc sulfide activator CuSO4·5H2O is added in an amount of 300 g / t and the slurry is mixed for 3 minutes. Then the slurry flows into the 6# stirring barrel, and the collector butyl xanthate is added in an amount of 150 g / t and the frother 2# oil is added in an amount of 30 g / t and the slurry is mixed for 2 minutes. Then, the slurry is transported to the zinc flotation system for flotation to obtain zinc sulfide concentrate and flotation tailings. Zinc flotation operation is divided into: one roughing operation with a flotation time of 5 minutes; two cleaning operations with flotation times of 4 minutes for cleaning operation one and 3 minutes for cleaning operation two; two scavenging operations, with 100g / t of CuSO4·5H2O, 40g / t of butyric acid and 10g / t of 2# oil added in scavenging operation one, and 60g / t of CuSO4·5H2O, 40g / t of butyric acid and 10g / t of 2# oil added in scavenging operation two, and the flotation time is 4 minutes respectively.

[0077] The results show that since lime and sulfuric acid are not used, the frequency of shutdown caused by pipeline blockage and flotation equipment corrosion is reduced by about 84%, the normal start-up time is increased, and the process production is stabilized. Finally, lead concentrate with a lead grade of 63.89% and a recovery rate of 85.98%; zinc concentrate with a zinc grade of 51.76% and a recovery rate of 90.78%; and pyrite concentrate with a sulfur grade of 46.55% and a recovery rate of 85.69% were obtained.

Claims

1. A flotation method for lead-zinc sulfide pyrite, characterized in that: The following steps are involved: (1) Crushing, grinding, grading, slurry preparation and pH adjustment of slurry After grinding the lead-zinc-sulfide ore to be separated by flotation to a particle size of less than 0.074 mm, the slurry is adjusted to a concentration of 28% to 35%, and a regulator is added to make the slurry pH 8 to 12; (2) Flotation of pyrite concentrate Adding 1200-3200 g / t of CaS and 20-50 g / t of butyl ether alcohol to the slurry obtained in the above (1), and then transporting the slurry to the sulfur flotation system for sulfur flotation; (3) Flotation of lead sulfide concentrate The sulfur flotation tailings obtained by the above (2) are added with a zinc inhibitor ZnSO4·7H2O in an amount of 500-1500 g / t, a collector ethyl sulfide nitrogen in an amount of 40-80 g / t, and a frother 2# oil in an amount of 30 g / t to prepare a slurry, and then transported to a lead flotation system for lead flotation operation to obtain lead sulfide concentrate and lead flotation tailings; (4) Flotation of zinc sulfide concentrate The lead flotation tailings obtained in the above (3) are slurried by adding 100-400 g / t of zinc sulfide activator CuSO4·5H2O, 100-200 g / t of collector butyl xanthate and 30 g / t of frother 2# oil, and then transported to the zinc flotation system for zinc flotation operation to obtain zinc sulfide concentrate and flotation tailings; The adjusting agent is sodium carbonate or sodium hydroxide.

2. A flotation method for lead-zinc sulfide pyrite according to claim 1, characterized in that: Sulfur flotation operation is divided into: one roughing; two cleaning, cleaning first adding CaS dosage of 100~300g / t; two scavenging, scavenging first adding CaS dosage of 200~600g / t and butyl ether alcohol of 20~50g / t, scavenging second adding butyl ether alcohol of 10g / t; Lead flotation operation is divided into: one roughing; two cleaning, cleaning first adding zinc inhibitor ZnSO4·7H2O dosage of 300~600g / t; two scavenging, scavenging first adding ethyl sulfide nitrogen dosage of 10~20g / t and frother 2# oil dosage of 10g / t, scavenging second adding ethyl sulfide nitrogen dosage of 5~10g / t and frother 2# oil dosage of 10g / t; Zinc flotation operation is divided into: one roughing; two cleaning; two scavenging, scavenging and adding The dosage is 50~150g / t, the dosage of butyl yellow medicine is 30~60g / t and the dosage of foaming agent 2# oil is 10g / t, and the two are added The dosage is 30~80g / t, the dosage of butyl yellow medicine is 20~50g / t and the dosage of foaming agent 2# oil is 10g / t.

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