A flotation system for lead-zinc sulfide ore containing pyrrhotite, a process method for the system, and a water treatment method

Abstract

The present invention discloses a flotation system for pyrrhotite-containing lead-zinc sulfide ores, a process method for the system, and a water treatment method, belonging to the fields of flotation and water treatment. The coarse concentrate of the lead-sulfur mixed flotation cell is connected to a lead-sulfur concentrator subsystem, the tailings are connected to a lead-sulfur scavenging subsystem, the lead-sulfur mixed flotation concentrate is connected to a thickener, the overflow is connected to a buffer tank, and the underflow is connected to a lead-sulfur separation flotation cell. The lead coarse concentrate is connected to the lead concentrator subsystem, the lead concentrate is connected to a filter press, and the filtrate is connected to a buffer tank. The rougher tailings are connected to the lead scavenging subsystem, the sulfur concentrate is connected to a filter press, and the filtrate is connected to a buffer tank. The lead-sulfur mixed flotation tailings are connected to a zinc flotation rougher cell, the zinc coarse concentrate is connected to the zinc concentrator subsystem, the zinc concentrate is connected to a zinc concentrate filter press, and the filtrate is connected to a buffer tank. The rougher tailings are connected to a zinc scavenging subsystem, the tailings are connected to a settling tank, and the supernatant is connected to a buffer tank. The buffer tank is connected to grinding equipment. The invention solves the problem that pyrrhotite is difficult to suppress after activation during sphalerite activation, improves the grade and recovery rate of zinc concentrate, and simplifies the water treatment process.

Description

Technical Field

[0001] The invention relates to a flotation system for lead-zinc sulfide ore containing pyrrhotite, a process method for the system, and a water treatment method for the system, belonging to the field of flotation and flotation water treatment. Background Art

[0002] Lead-zinc ore is an important non-ferrous metal mineral resource with a wide range of applications in industrial production. Due to the complex nature of the ore and the close symbiosis of lead, zinc, and sulfur minerals, the flotation separation of lead-zinc sulfide ores containing pyrrhotite presents significant technical difficulties. Traditional flotation processes for such ores often suffer from low zinc concentrate grade and recovery, high reagent consumption, and complex process flows. During the zinc-sulfur separation process, pyrrhotite is easily activated by activators and tends to float up with sphalerite, resulting in a decrease in concentrate quality. Furthermore, to suppress pyrrhotite, a large amount of inhibitors must be added, increasing production costs and the risk of environmental pollution.

[0003] Through the lead-sulfur mixed flotation and lead-sulfur separation process, the lead, zinc and sulfur minerals can be effectively separated, and the grade and recovery rate of zinc concentrate can be improved. However, due to the high concentration of Cu in the zinc concentrate flotation return water, 2+ , these remaining Cu 2+ The activation of pyrrhotite results in a decrease in the grade and recovery of zinc flotation concentrate.

[0004] According to environmental protection standards and process requirements, the water generated during the flotation process, such as the water generated by pulp concentration and the water generated by concentrate and tailings filtration, needs to be used as return water in the mineral processing system. 2+ There is a problem of activating pyrrhotite, which results in a decrease in the grade and recovery rate of lead concentrate. The main means to solve this problem is to increase the amount of inhibitor to inhibit the activation of pyrrhotite, which not only increases production costs but also increases the burden of backwater treatment. Another way to solve this problem is to increase the pH value of the reaction system to reduce the residual Cu in the zinc flotation backwater. 2+ The deposit is converted into Cu(OH)2 and separated by precipitation. Although this approach can reduce the 2+ It has no adverse effect on pyrrhotite, but makes the flotation process complicated and further increases the process cost. Summary of the Invention

[0005] The technical problem to be solved by the present invention is to provide a flotation system for lead-zinc sulfide ore containing pyrrhotite, a process method and a water treatment method of the system, which can eliminate Cu without separating copper. 2+The purpose of affecting pyrrhotite is to solve the problem that pyrrhotite is difficult to inhibit after activation during sphalerite activation, improve the grade and recovery rate of zinc concentrate, further simplify the water treatment process, and reduce the cost of reagents.

[0006] The technical solutions of the present invention are as follows:

[0007] A flotation system for pyrrhotite-containing lead-zinc sulfide ore, comprising a grinding device with an ore feeding port, a water inlet pipe and a slurry discharge pipe, the system also comprising a lead-sulfur mixed flotation tank connected to the slurry discharge pipe, wherein the coarse concentrate of the lead-sulfur mixed flotation tank is transported to a lead-sulfur concentration subsystem, and the tailings are transported to a lead-sulfur scavenging subsystem; the lead-sulfur mixed flotation concentrate produced by the lead-sulfur concentration subsystem is transported to a thickener, the overflow of the thickener is transported to a buffer water tank, and the underflow is transported to a lead-sulfur separation flotation tank; the lead coarse concentrate of the lead-sulfur separation flotation tank is transported to a lead concentration subsystem, the lead concentrate produced by the lead concentration subsystem is transported to a filter press, and the filtrate of the filter press is transported to a buffer water tank; the lead-sulfur separation flotation tank is used to separate the lead and sulfur ore. The roughing tailings from the selection tank are transported to the lead scavenging subsystem, the sulfur concentrate from the lead scavenging subsystem is transported to the filter press, and the filtrate from the filter press is transported to the buffer water tank; the lead-sulfur mixed floatation tailings from the lead-sulfur scavenging subsystem are transported to the zinc flotation roughing tank, the zinc roughing concentrate from the zinc flotation roughing tank is transported to the zinc concentration subsystem, the zinc concentrate produced by the zinc concentration subsystem is transported to the zinc concentrate filter press, and the filtrate produced by the zinc concentrate filter press is transported to the buffer water tank through the filtrate conveying pipe; the roughing tailings from the zinc flotation roughing tank are transported to the zinc scavenging subsystem, the tailings from the zinc scavenging subsystem are transported to the sedimentation tank, and the sedimentation supernatant is transported to the buffer water tank; the water in the buffer water tank is transported to the grinding equipment.

[0008] Preferably, a flow meter is installed on the filtrate delivery pipe; the filtrate delivery pipe is connected to a soluble ammonium salt solution injection mechanism; and a stirrer is installed in the filtrate collection container of the zinc concentrate filter press.

[0009] The process method of the flotation system of the lead-zinc sulfide ore containing pyrrhotite comprises the following steps:

[0010] Step 1: Grinding:

[0011] Grinding the pyrrhotite-containing lead-zinc sulfide ore; adjusting the slurry concentration to 33-37% after grinding;

[0012] Step 2: Lead-sulfur mixed floatation:

[0013] The ore pulp after grinding is transported to the lead-sulfur mixed flotation tank for lead-sulfur mixed flotation roughing; in the lead-sulfur mixed flotation roughing, zinc sulfate and sodium sulfite are respectively added to suppress sphalerite; ethyl dithiocarbamide is added as a collector; and a frother is added to obtain a coarse concentrate and tailings; the tailings enter the lead-sulfur scavenging operation to obtain lead-sulfur mixed flotation tailings; the coarse concentrate enters the lead-sulfur concentrating operation to obtain a lead-sulfur mixed flotation concentrate;

[0014] Step 3: Lead-sulfur separation and zinc flotation:

[0015] Lead-sulfur separation and zinc flotation: The lead-sulfur mixed flotation concentrate obtained in the second step is transported to a thickener for concentration to achieve a pulp mass concentration of 35%±5%. The overflow of the thickener is transported to a buffer water tank, and the underflow is transported to a lead-sulfur separation flotation tank; lime is added as a pyrite depressant; and ammonium butyl black powder is added as a collector for lead minerals to obtain lead rough concentrate and rougher tailings; the lead rough concentrate enters the lead concentration operation, during which lime is added as a depressant to obtain lead concentrate; the lead concentrate is transported to a filter press for dehydration to obtain a lead concentrate filter cake and filtrate, which is then transported to a buffer water tank; the rougher tailings enter the lead scavenging operation, during which ammonium butyl black powder is added to obtain a sulfur concentrate; the sulfur concentrate is transported to a filter press for dehydration to obtain a sulfur concentrate filter cake and filtrate, which is then transported to a buffer water tank; the lead-sulfur mixed flotation tailings from the lead-sulfur scavenging operation enter the zinc flotation rougher tank for zinc flotation operation;

[0016] Zinc flotation: First, copper sulfate is added as an activator to the zinc flotation roughing tank and stirred. Then, butyl xanthate collector and 2# oil frother are added to obtain zinc rough concentrate and roughing tailings. The zinc rough concentrate enters the zinc cleaning process to obtain zinc concentrate. The zinc concentrate is dehydrated by filter pressing to obtain zinc concentrate filter cake and filtrate. The filtrate is transported to the buffer water tank through the filtrate delivery pipe.

[0017] The water in the buffer pool is transported to the grinding equipment for use as grinding water and recycled.

[0018] Preferably, in the second step, the amount of zinc sulfate added is 300-500 g / t of raw ore; the amount of sodium sulfite added is 100-200 g / t of raw ore; the amount of ethyl sulfide and nitrogen added is 50-100 g / t of raw ore; the foaming agent is 2# oil, and the amount added is 20-30 g / t of raw ore; the lead-sulfur scavenging operation is carried out 2-3 times, and 10-20 g / t of raw ore of ethyl sulfide and nitrogen is added each time; the lead-sulfur concentration operation is carried out 2-3 times, and 300-600 g / t of raw ore of zinc inhibitor is added each time.

[0019] Preferably, in the third step of lead-sulfur separation and zinc flotation, the amount of lime added is based on meeting the pulp pH of 11±0.5; the amount of butyl ammonium black medicine added is 20-30 g / t of raw ore; the lead concentration operation is carried out 2-3 times, and the amount of lime added each time is based on controlling the pH of 11±0.5; the lead scavenging operation is carried out 2-3 times, and 5-10 g / t of raw ore is added each time; in the third step of zinc flotation, the amount of copper sulfate added is 200-300 g / t of raw ore, and the stirring time is 3-5 minutes to fully activate the suppressed sphalerite; the amount of butyl xanthate added is 40-60 g / t of raw ore; the amount of 2# oil frother added is 20-30 g / t of raw ore; the zinc concentration operation is carried out 2-3 times; and the zinc inhibitor is composed of zinc sulfate and sodium sulfite in a mass ratio of 2:1.

[0020] The water treatment method of the flotation system of the lead-zinc sulfide ore containing pyrrhotite is used to detect Cu in the zinc concentrate filtrate. 2+ The concentration is adjusted, and after adding soluble ammonium salt to the filtrate collection container of the zinc concentrate filter press (7), the filtrate is pumped into the filtrate delivery pipe (8) under stirring, and discharged into the buffer water tank (12) through the filtrate delivery pipe (8) for grinding water distribution.

[0021] Preferably, the calculation formula for the amount of soluble ammonium salt added is:

[0022] ;

[0023] Where:

[0024] C-amount of soluble ammonium salt added, kg / h;

[0025] P-zinc concentrate filtrate flow rate, m 3 / h;

[0026] M-Cu in zinc concentrate filtrate 2+ Concentration, mg / L;

[0027] K-molecular weight of soluble ammonium salt;

[0028] The absolute value of the valence of the anion of N-soluble ammonium salt;

[0029] i- is determined according to the following formula: ;

[0030] Where: E- pyrrhotite molecular value as a percentage of ore mass.

[0031] Preferably, the pyrrhotite-containing lead-zinc sulfide ore is Fe 1-x Ores with S content of 0.5%-15%, galena content of 0.3%-8%, and sphalerite content of 0.4%-6%, where x=0-0.233.

[0032] The beneficial effects of the present invention are as follows:

[0033] First, the present invention eliminates the zinc flotation backwater Cu 2+ Effect on pyrrhotite: Add soluble ammonium salt to the zinc flotation return water to make the copper sulfate in the return water react with the soluble ammonium salt to eliminate Cu 2+ The specific mechanism is: copper sulfate reacts with soluble ammonium salts (such as ammonium sulfate) in the solution, and Cu²⁺ forms a stable [Cu(NH3)4]SO4 with NH3 generated by the hydrolysis of NH4⁺ through coordination bonds. [Cu(NH3)4]SO4 is a complex orthorhombic crystal and is soluble in water, but cannot activate pyrrhotite. Therefore, the present invention achieves the elimination of Cu without separating copper. 2+The purpose is to reduce the impact on pyrrhotite and further simplify the production process. Based on the above water treatment method, the flotation system of the present invention can effectively separate lead, zinc, and sulfur minerals, improving concentrate quality and recovery rate. Compared with traditional processes, the grade of zinc concentrate can be increased by 8%-25%, and the recovery rate can be increased by 1%-3%.

[0034] Furthermore, after repeated exploration and testing, the present invention proposes a method for the extraction of Cu 2+ The calculation method of elimination can be used to calculate the amount of soluble ammonium salt that needs to be added to the zinc concentrate flotation return water more accurately. If the amount of soluble ammonium salt added is insufficient, the residual Cu in the return water will be 2+ After activating pyrrhotite, the grade and recovery rate of lead concentrate decrease; if excessive soluble ammonium salt is added, not only will the cost of reagents increase, but too many ammonium ions will enter the subsequent flotation process, causing eutrophication of the water body and increased mineral processing costs.

[0035] Second, the present invention eliminates the zinc flotation return water Cu by backwater treatment. 2+ The activation effect on pyrrhotite avoids the problem that pyrrhotite cannot be suppressed after being activated during the sphalerite activation process, greatly improves the grade of zinc concentrate, and reduces the burden of return water treatment.

[0036] Third, after obtaining the lead-sulfur mixed flotation concentrate in the present invention, it is first transported to a thickener for concentration, which concentrates the slurry mass concentration from about 15% to 35%±5%. The increased slurry concentration is more conducive to improving the concentrate recovery rate. BRIEF DESCRIPTION OF THE DRAWINGS

[0037] Figure 1 It is a schematic diagram of the principle of an embodiment of the system of the present invention.

[0038] Explanation of the accompanying symbols: 1. Grinding equipment; 2. Lead-sulfur mixed flotation cell; 3. Lead-sulfur scavenging subsystem; 4. Zinc flotation roughing cell; 5. Zinc scavenging subsystem; 6. Zinc concentration subsystem; 7. Zinc concentrate filter press; 8. Filtrate conveying pipe; 9. Lead scavenging subsystem; 10. Lead-sulfur separation flotation cell; 11. Lead concentration subsystem; 12. Buffer water tank; 13. Lead-sulfur concentration subsystem; 14. Thickener. DETAILED DESCRIPTION

[0039] The present invention is further described below in conjunction with examples and experimental data.

[0040] The pyrrhotite-containing lead-zinc sulfide ore of the present invention generally refers to Fe 1-x Ores with S (x=0-0.233) content of 0.5%-15%, galena content of 0.3%-8%, and sphalerite content of 0.4%-6%.

[0041] Example 1: Flotation system for lead-zinc sulfide ore containing pyrrhotite

[0042] like Figure 1 An embodiment of a flotation system for a pyrrhotite-containing lead-zinc sulfide ore includes a grinding device 1 having an ore feeding port, a water inlet pipe, and a slurry discharge pipe.

[0043] The system of this embodiment also includes a lead-sulfur mixed flotation cell 2 for rough selection of the grinding slurry. The feed end of the lead-sulfur mixed flotation cell 2 is connected to the slurry discharge pipe. The coarse concentrate of the lead-sulfur mixed flotation cell 2 is transported to the lead-sulfur concentration subsystem 13, and the tailings of the lead-sulfur mixed flotation cell 2 are transported to the lead-sulfur scavenging subsystem 3.

[0044] The lead-sulfur mixed flotation concentrate produced by the lead-sulfur concentration subsystem 13 is transported to a thickener 14. The supernatant overflowing from the thickener 14 is transported to a buffer water tank 12. The slurry from the underflow of the thickener 14 is transported to a lead-sulfur separation flotation cell 10 for rough lead-sulfur separation. The rough lead concentrate from the lead-sulfur separation flotation cell 10 is transported to a lead concentration subsystem 11. The lead concentrate produced by the lead concentration subsystem 11 is transported to a filter press (omitted in the accompanying drawings), and the filtrate produced by the filter press is transported to the buffer water tank 12. The rougher tailings from the lead-sulfur separation flotation cell 10 are transported to a lead scavenging subsystem 9. The sulfur concentrate produced by the lead scavenging subsystem 9 is transported to a filter press (omitted in the accompanying drawings), and the filtrate produced by the filter press is transported to the buffer water tank 12.

[0045] The lead-sulfur mixed float tailings from the lead-sulfur scavenging subsystem 3 are transported to the zinc flotation rougher 4 used for zinc flotation roughing. The zinc rough concentrate from the zinc flotation rougher 4 is transported to the zinc concentrator subsystem 6. The zinc concentrate produced by the zinc concentrator subsystem 6 is transported to the zinc concentrate filter press 7. The filtrate produced by the zinc concentrate filter press 7 is transported to the buffer water tank 12 via the filtrate conveying pipe 8. The rougher tailings from the zinc flotation rougher 4 are transported to the zinc scavenging subsystem 5. The tailings produced by the zinc scavenging subsystem 5 are transported to the sedimentation tank (the sedimentation tank is omitted in the drawings), and the sedimentation supernatant is transported to the buffer water tank 12.

[0046] The water in the buffer water tank 12 is transported to the grinding equipment 1 through the water inlet pipe.

[0047] Specifically, the lead-sulfur concentration subsystem 13 includes lead-sulfur concentration I and lead-sulfur concentration II. The coarse concentrate of the lead-sulfur mixed flotation tank 2 is transported to the lead-sulfur concentration I, the middlings of the lead-sulfur concentration I are returned to the lead-sulfur mixed flotation tank 2, the middlings of the lead-sulfur concentration II are returned to the lead-sulfur concentration I, and the lead-sulfur mixed flotation concentrate produced by the lead-sulfur concentration II is transported to the thickener 14.

[0048] The lead concentration subsystem 11 includes lead concentration I and lead concentration II. The lead coarse concentrate from the lead-sulfur separation flotation cell 10 is transported to lead concentration I, the middlings from lead concentration I are returned to the lead-sulfur separation flotation cell 10, the middlings from lead concentration II are returned to lead concentration I, and the lead concentrate produced by lead concentration II is transported to a filter press.

[0049] The lead scavenging subsystem 9 includes lead scavenging I and lead scavenging II. The rougher tailings of the lead-sulfur separation flotation cell 10 are transported to the lead scavenging I, the middlings of the lead scavenging I are returned to the lead-sulfur separation flotation cell 10, the middlings of the lead scavenging II are returned to the lead scavenging I, and the sulfur concentrate produced by the lead scavenging II is transported to the filter press.

[0050] The lead-sulfur scavenging subsystem 3 includes lead-sulfur scavenging I and lead-sulfur scavenging II. The tailings of the lead-sulfur mixed flotation cell 2 are transported to the lead-sulfur scavenging I, the middlings of the lead-sulfur scavenging I are returned to the lead-sulfur mixed flotation cell 2, the middlings of the lead-sulfur scavenging II are returned to the lead-sulfur scavenging I, and the lead-sulfur mixed flotation tailings produced by the lead-sulfur scavenging II are transported to the zinc flotation roughing cell 4.

[0051] The zinc concentration subsystem 6 includes zinc concentration I and zinc concentration II. The zinc rough concentrate from the zinc flotation roughing tank 4 is transported to zinc concentration I, the middlings from zinc concentration I are returned to the zinc flotation roughing tank 4, the middlings from zinc concentration II are returned to zinc concentration I, and the zinc concentrate produced by zinc concentration II is transported to the zinc concentrate filter press 7.

[0052] The zinc scavenging subsystem 5 includes zinc scavenging I and zinc scavenging II. The rougher tailings of the zinc flotation rougher tank 4 are transported to the zinc scavenging I, the middlings of the zinc scavenging I are returned to the zinc flotation rougher tank 4, the middlings of the zinc scavenging II are returned to the zinc scavenging I, and the tailings produced by the zinc scavenging II are transported to the sedimentation tank.

[0053] Furthermore, a flow meter is installed on the filtrate delivery pipe 8 to measure the flow rate of the zinc concentrate filtrate in the filtrate delivery pipe 8; the filtrate delivery pipe 8 is connected to a soluble ammonium salt solution injection mechanism. A stirrer is installed in the filtrate collection container of the zinc concentrate filter press 7.

[0054] Specifically, the soluble ammonium salt solution injection mechanism includes a liquid pump with a metering device, the liquid inlet end of the liquid pump is connected to the filtrate collection container of the zinc concentrate filter press 7 through a pipeline, and the liquid discharge end is connected to the filtrate delivery pipe 8 through a pipeline.

[0055] Example 2: Process Example of a Flotation System for Pyrrhotite-Containing Lead-Zinc Sulfide Ore

[0056] The flotation ore in this embodiment belongs to the pyrrhotite-containing lead-zinc sulfide ore, in which Fe 1-x S (x = 0.10) content (9.64%), galena content (2.99%), sphalerite (2.76%). After analysis, the specific main components are shown in Table 1.

[0057] Table 1

[0058]

[0059] The first step, grinding: the above-mentioned pyrrhotite-containing lead-zinc sulfide ore, i.e. Figure 1 The "sample" in the sample is ground. The optimal grinding fineness is determined through testing based on the ore properties to ensure smooth subsequent flotation operations. In this example, the ore is ground to a -200 mesh content of 70%. The slurry concentration is adjusted to 35%.

[0060] Step 2, Lead-Sulfur Flotation: The milled slurry is transferred to the lead-sulfur flotation tank 2 for roughing. During this roughing operation, zinc sulfate and sodium sulfite are added to suppress sphalerite. The zinc sulfate and sodium sulfite dosages are 400g / t of ore and 150g / t of ore, respectively. Ethyl thiocyanate is added as a collector at a rate of 75g / t of ore, and #2 oil is added as a frother at a rate of 25g / t of ore. A single roughing operation is performed for 8 minutes, yielding rougher tailings and a lead-sulfur flotation concentrate.

[0061] The rougher tailings enter the lead-sulfur scavenging subsystem 3, where they are scavenged twice, with 10g of ethyl sulfide and nitrogen added per ton of ore for each scavenging operation. Each scavenging operation lasts 3 minutes, resulting in lead-sulfur mixed float tailings. The middlings obtained from the scavenging are returned to the previous operation in sequence.

[0062] The lead-sulfur mixed flotation coarse concentrate enters the lead-sulfur concentrator subsystem 13, where it undergoes two concentrating operations. During each concentrating process, an appropriate amount of zinc depressant is added (400g / t zinc sulfate and 200g / t sodium sulfite in lead concentrator I; 200g / t zinc sulfate and 100g / t sodium sulfite in lead concentrator II). The concentrating times are 3 minutes and 2 minutes, respectively, to produce a lead-sulfur mixed flotation concentrate. The middlings obtained from the concentrating operations are returned to the previous level.

[0063] Step 3: Lead-sulfur separation and zinc flotation:

[0064] Lead-sulfur separation and zinc flotation: The lead-sulfur mixed flotation concentrate obtained in the second step was measured to have a pulp concentration of 15%. The concentrate was first conveyed to a thickener 14 for concentration, bringing the pulp concentration to 35% ± 5%. The overflow supernatant from the thickener 14 was conveyed to a buffer tank 12, and the underflow of the lead-sulfur mixed flotation concentrate from the thickener 14 was conveyed to a lead-sulfur separation flotation cell 10 for lead-sulfur separation.

[0065] During the lead-sulfur separation roughing operation, lime is added as a depressant to suppress pyrite, and the slurry pH is controlled at 11 ± 0.5 (the amount of lime added is based on the required slurry pH; based on experiments, 1000g of lime per ton of raw ore is sufficient to meet the required slurry pH). Butyl ammonium chloride is also added as a collector for lead minerals at a rate of 20g per ton of raw ore. A single roughing operation is performed for 4 minutes to produce a lead concentrate and roughing tailings.

[0066] The crude lead concentrate enters the lead concentrator subsystem 11, where it undergoes two concentrating operations. During each concentrating process, lime is added as a depressant, preferably to control the pH at 11 ± 0.5 (based on experiments, 500 g / t of lime is sufficient to meet the required slurry pH). The concentrating times are 3 minutes and 2 minutes, respectively, to produce lead concentrate. The resulting middlings are then returned to the previous level.

[0067] The lead concentrate is transported to a filter press for dehydration to obtain a lead concentrate filter cake and a filtrate, and the filtrate is transported to a buffer water tank 12 .

[0068] The rougher tailings enter the lead scavenging subsystem 9, where they are scavenged twice, with 5g of ammonium butyl black powder added per ton of raw ore for 3 minutes each time, to produce sulfur concentrate. The middlings obtained from the scavenging are returned to the previous operation in sequence.

[0069] The sulfur concentrate is transported to a filter press for dehydration to obtain a sulfur concentrate filter cake and a filtrate, and the filtrate is transported to a buffer water tank 12 .

[0070] Zinc flotation: The lead-sulfur mixed flotation tailings from the lead-sulfur scavenging subsystem 3 enter the zinc flotation roughing tank 4 for zinc flotation operation.

[0071] First, copper sulfate was added to zinc flotation rougher tank 4 as an activator at a rate of 200 g / t of ore, with stirring for 3 minutes to fully activate the suppressed sphalerite. Then, butyl xanthate was added as a collector at a rate of 40 g / t of ore, and 2# oil was added as a frother at a rate of 30 g / t of ore. A single roughing operation was performed for 5 minutes to produce a zinc concentrate and rougher tailings.

[0072] The zinc concentrate enters the zinc concentrator subsystem 6, where it undergoes two concentrating operations, each lasting 3 minutes, to produce zinc concentrate. The middlings obtained from the concentrating are returned to the previous operation in sequence.

[0073] After the zinc concentrate is dehydrated by filter pressing, a zinc concentrate filter cake and a filtrate are obtained, and the filtrate is transported to the buffer water tank 12 through the filtrate transport pipe 8.

[0074] The water in the buffer water tank 12 is transported to the grinding equipment 1 for use as grinding water and is recycled. The above liquid transportation is usually carried out by means of a water pump or by gravity transportation by means of liquid level difference.

[0075] Example 3: Water treatment example of flotation system for lead-zinc sulfide ore containing pyrrhotite

[0076] Based on Example 2, the Cu content in the zinc concentrate filtrate was detected. 2+ concentration, and add ammonium sulfate as a soluble ammonium salt to the filtrate collection container of the zinc concentrate filter press 7, pump it into the filtrate delivery pipe 8 under stirring, and discharge it into the buffer water tank 12 through the filtrate delivery pipe 8 for mixing with the sample for grinding.

[0077] Furthermore, the calculation formula for the amount of soluble ammonium salt added is:

[0078] ;

[0079] Where:

[0080] C-amount of soluble ammonium salt added, kg / h;

[0081] P-zinc concentrate filtrate flow rate, m 3 / h;

[0082] M-Cu in zinc concentrate filtrate 2+ Concentration, mg / L;

[0083] K-molecular weight of soluble ammonium salt;

[0084] The absolute value of the valence of the anion of N-soluble ammonium salt;

[0085] i- is determined according to the following formula: ;

[0086] Where: E- pyrrhotite molecular value as a percentage of ore mass.

[0087] Ammonium sulfate is used as the soluble ammonium salt and the flow rate of zinc concentrate filtrate is 5m 3 / h, Cu in zinc concentrate filtrate 2+ Concentration 12mg / L, Fe 1-x Taking the S(x=0.1) content of 9.64% (E=9.64, i=1.63) as an example, the above formula is used to calculate the amount of ammonium sulfate added to be 0.40kg / h.

[0088] Ammonium chloride is used as the soluble ammonium salt and the flow rate of zinc concentrate filtrate is 5m 3 / h, Cu in zinc concentrate filtrate 2+ Taking the concentration of 12 mg / L as an example, the above formula is used to calculate the amount of ammonium chloride added to be 0.33 kg / h.

[0089] Comparative Example

[0090] The difference between this embodiment and the third embodiment is that the zinc concentrate is dehydrated by filtration to obtain a zinc concentrate filter cake. The filtrate is directly pumped into the buffer water tank 12 without treatment to be mixed with the sample for grinding.

[0091] The comparative data of the experimental results of Example 3 and the comparative example are shown in Table 2.

[0092] Table 2

[0093]

[0094] As shown in Table 2, the zinc concentrate grade of Example 3 is 42.39%, and the recovery rate is 84.71%. The zinc concentrate grade of the comparative example is 22.35%, and the recovery rate is 83.53%. The zinc concentrate grade and recovery rate of Example 3 are 20.04% and 1.18% higher than those of the comparative example, respectively.

Claims

1. A flotation system for lead-zinc sulfide ore containing pyrrhotite, comprising a grinding device (1) having an ore feeding port, a water inlet pipe and a slurry discharge pipe, characterized in that: The system further comprises a lead-sulfur mixed flotation cell (2) connected to a slurry discharge pipe, wherein the coarse concentrate of the lead-sulfur mixed flotation cell (2) is transported to a lead-sulfur concentration subsystem (13), and the tailings are transported to a lead-sulfur scavenging subsystem (3); the lead-sulfur mixed flotation concentrate produced by the lead-sulfur concentration subsystem (13) is transported to a thickener (14), the overflow of the thickener (14) is transported to a buffer water tank (12), and the underflow is transported to a lead-sulfur separation flotation cell (10); the lead coarse concentrate of the lead-sulfur separation flotation cell (10) is transported to a lead concentration subsystem (11), the lead concentrate produced by the lead concentration subsystem (11) is transported to a filter press, and the filtrate of the filter press is transported to a buffer water tank (12); the coarse tailings of the lead-sulfur separation flotation cell (10) are transported to a lead scavenging subsystem (9), and the lead scavenging subsystem (9) is transported to a lead concentration subsystem (11). The sulfur concentrate of the subsystem (9) is transported to the filter press, and the filtrate of the filter press is transported to the buffer water tank (12); the lead-sulfur mixed float tailings of the lead-sulfur scavenging subsystem (3) are transported to the zinc flotation roughing tank (4), the zinc rough concentrate of the zinc flotation roughing tank (4) is transported to the zinc concentration subsystem (6), the zinc concentrate produced by the zinc concentration subsystem (6) is transported to the zinc concentrate filter press (7), and the filtrate produced by the zinc concentrate filter press (7) is transported to the buffer water tank (12) through the filtrate transport pipe (8); the roughing tailings of the zinc flotation roughing tank (4) are transported to the zinc scavenging subsystem (5), the tailings of the zinc scavenging subsystem (5) are transported to the sedimentation tank, and the sedimentation supernatant is transported to the buffer water tank (12); the water in the buffer water tank (12) is transported to the grinding equipment (1).

2. The flotation system according to claim 1, characterized in that: A flow meter is installed on the filtrate delivery pipe (8); the filtrate delivery pipe (8) is connected to a soluble ammonium salt solution injection mechanism; and a stirrer is installed in the filtrate collection container of the zinc concentrate filter press (7).

3. The flotation system according to claim 1 or 2, characterized in that: The lead-zinc sulfide ore containing pyrrhotite refers to Fe 1-x Ores with S content of 0.5%-15%, galena content of 0.3%-8%, and sphalerite content of 0.4%-6%, where x=0-0.

233.

4. The process of the flotation system of the pyrrhotite-containing lead-zinc sulfide ore according to claim 1, 2 or 3, characterized in that The following steps are involved: Step 1: Grinding: Grinding the pyrrhotite-containing lead-zinc sulfide ore; adjusting the slurry concentration to 33-37% after grinding; Step 2: Lead-sulfur mixed floatation: The ore pulp after grinding is transported to the lead-sulfur mixed flotation tank for lead-sulfur mixed flotation roughing; in the lead-sulfur mixed flotation roughing, zinc sulfate and sodium sulfite are respectively added to suppress sphalerite; ethyl dithiocarbamide is added as a collector; and a frother is added to obtain a coarse concentrate and tailings; the tailings enter the lead-sulfur scavenging operation to obtain lead-sulfur mixed flotation tailings; the coarse concentrate enters the lead-sulfur concentrating operation to obtain a lead-sulfur mixed flotation concentrate; Step 3: Lead-sulfur separation and zinc flotation: Lead-sulfur separation and zinc flotation: The lead-sulfur mixed flotation concentrate obtained in the second step is transported to a thickener for concentration to achieve a pulp mass concentration of 35%±5%. The overflow of the thickener is transported to a buffer water tank, and the underflow is transported to a lead-sulfur separation flotation tank; lime is added as a pyrite depressant; and ammonium butyl black powder is added as a collector for lead minerals to obtain lead rough concentrate and rougher tailings; the lead rough concentrate enters the lead concentration operation, during which lime is added as a depressant to obtain lead concentrate; the lead concentrate is transported to a filter press for dehydration to obtain a lead concentrate filter cake and filtrate, which is then transported to a buffer water tank; the rougher tailings enter the lead scavenging operation, during which ammonium butyl black powder is added to obtain a sulfur concentrate; the sulfur concentrate is transported to a filter press for dehydration to obtain a sulfur concentrate filter cake and filtrate, which is then transported to a buffer water tank; the lead-sulfur mixed flotation tailings from the lead-sulfur scavenging operation enter the zinc flotation rougher tank for zinc flotation operation; Zinc flotation: First, copper sulfate is added as an activator to the zinc flotation roughing tank and stirred. Then, butyl xanthate collector and 2# oil frother are added to obtain zinc rough concentrate and roughing tailings. The zinc rough concentrate enters the zinc cleaning process to obtain zinc concentrate. The zinc concentrate is dehydrated by filter pressing to obtain zinc concentrate filter cake and filtrate. The filtrate is transported to the buffer water tank through the filtrate delivery pipe. The water in the buffer pool is transported to the grinding equipment for use as grinding water and recycled.

5. The process according to claim 4, characterized in that: In the second step, the amount of zinc sulfate added is 300-500g / t of raw ore; the amount of sodium sulfite added is 100-200g / t of raw ore; the amount of ethyl sulfide and nitrogen added is 50-100g / t of raw ore; the foaming agent is 2# oil, and the amount added is 20-30g / t of raw ore; the lead-sulfur scavenging operation is carried out 2-3 times, and 10-20g / t of raw ore of ethyl sulfide and nitrogen is added each time; the lead-sulfur concentration operation is carried out 2-3 times, and 300-600g / t of raw ore of zinc inhibitor is added each time.

6. The process according to claim 4, characterized in that: In the third step of lead-sulfur separation and zinc flotation, the amount of lime added is based on the pH of the ore pulp of 11±0.

5. The amount of butyl ammonium chloride added is 20-30g / t of the raw ore. The lead beneficiation operation is carried out 2-3 times, and the amount of lime added each time is based on the pH of 11±0.

5. The lead scavenging operation is carried out 2-3 times, and 5-10g / t of the raw ore is added each time. In the third step of zinc flotation, the amount of copper sulfate added is 200-300g / t of the raw ore, and the stirring time is 3-5 minutes to fully activate the suppressed sphalerite. The amount of butyl xanthate added is 40-60g / t of the raw ore. The amount of 2# oil frother added is 20-30g / t of the raw ore. The zinc beneficiation operation is carried out 2-3 times. The zinc depressant consists of zinc sulfate and sodium sulfite in a mass ratio of 2:

1.

7. The process according to claim 4, 5 or 6, characterized in that: The lead-zinc sulfide ore containing pyrrhotite refers to Fe 1-x Ores with S content of 0.5%-15%, galena content of 0.3%-8%, and sphalerite content of 0.4%-6%, where x=0-0.

233.

8. The water treatment method of the flotation system of the pyrrhotite-containing lead-zinc sulfide ore according to claim 1, 2 or 3, characterized in that: Detection of Cu in zinc concentrate filtrate 2+ The concentration is adjusted, and after adding soluble ammonium salt to the filtrate collection container of the zinc concentrate filter press (7), the filtrate is pumped into the filtrate delivery pipe (8) under stirring, and discharged into the buffer water tank (12) through the filtrate delivery pipe (8) for grinding water distribution.

9. The water treatment method according to claim 8, characterized in that The calculation formula for the amount of soluble ammonium salt added is: ； Where: C-soluble ammonium salt addition amount, kg / h; P-zinc concentrate filtrate flow rate, m 3 / h; M-Cu in zinc concentrate filtrate 2+ Concentration, mg / L; K-molecular weight of soluble ammonium salt; The absolute value of the valence of the anion of N-soluble ammonium salt; i- is determined according to the following formula: ; Where: E- pyrrhotite molecular value as a percentage of ore mass.

10. The water treatment method according to claim 8 or 9, characterized in that: The lead-zinc sulfide ore containing pyrrhotite refers to Fe 1-x Ores with S content of 0.5%-15%, galena content of 0.3%-8%, and sphalerite content of 0.4%-6%, where x=0-0.233.

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