Method for branch quality supplementing water in tin-lead-zinc-antimony polymetallic ore flotation

Abstract

The present application relates to the technical field of mineral processing, in particular to a method for supplementing water in flotation branches of tin-lead-zinc-antimony polymetallic ore. The filter water of the magnetic separation concentrate and lead-antimony concentrate, the overflow water after thickening of the magnetic separation tailings are used as the supplement water for wet grinding of raw ore, lead-antimony-zinc-sulfur flotation separation and foam rinsing water of lead-antimony concentrate; the flocculating agent obtained by free radical polymerization of guar gum and DMC is added during thickening of zinc-sulfur mixed flotation concentrate, and the overflow water after thickening of the zinc-sulfur mixed flotation concentrate is used as the supplement water for zinc-sulfur mixed flotation; the filter water of zinc and sulfur concentrates after zinc-sulfur separation is used as the supplement water for zinc-sulfur separation and foam rinsing water of zinc and sulfur concentrates; the filter water of table concentrator concentrate, the overflow water after thickening of table concentrator tailings, the overflow water after thickening of desulfurization flotation tailings and the filter water of tin stone flotation concentrate are used as the supplement water for table concentrator gravity separation, desulfurization flotation and tin stone flotation; the process water is recycled in sections and in quality, which avoids the influence of backwater on flotation operation and reduces the consumption of clean water and reagents.

Description

Technical Field

[0001] This invention relates to the field of mineral processing technology, and more specifically, to a method for adding water to the flotation branches of polymetallic tin-lead-zinc-antimony ore. Background Technology

[0002] In the flotation separation of tin polymetallic sulfide ores, the pulp during zinc-sulfur co-flotation is nearly neutral or weakly acidic, containing a large amount of xanthate collectors and activators. During zinc-sulfur separation, a large amount of lime is added to suppress pyrite, at which point the pulp becomes strongly alkaline, with a pH range of 12-13. However, cassiterite flotation requires a pulp that is nearly neutral or weakly acidic, and necessitates the addition of large amounts of hydroxamic acid anionic collectors and defoamers. Therefore, influenced by the different ore properties, the mixing and reuse of reflux water from different beneficiation processes increases reagent consumption during pulp acid-base adjustment. Simultaneously, the mixed enrichment of collectors, activators, and defoamers affects flotation separation, further increasing the difficulty of flotation separation.

[0003] Currently, the mixed use of reflux water from different mineral processing processes presents the following main problems:

[0004] 1. Zinc-sulfur separation slurry is strongly alkaline, while zinc-sulfur sulfide flotation slurry is weakly acidic. When the sulfide ore flotation concentrate enters the separation process, a large amount of lime needs to be added to adjust the pH value. This high lime consumption significantly increases beneficiation costs. Furthermore, the excessive use of lime easily leads to scaling on pipelines and the shaking table surface.

[0005] 2. Due to the interference of a large amount of activators and collectors in the ore dressing reflux water, the separation of lead, antimony, zinc and sulfur is difficult, and the ore dressing indicators are affected.

[0006] 3. Water recycled within the ore dressing plant that is directly used for grinding, flotation, and other processes must undergo treatment (primarily to reduce Cu content). 2+ Ca 2+ It requires the use of collectors and other agents to perform flotation operations, and the large volume of water to be treated results in high processing costs.

[0007] 4. The purification of mineral processing wastewater is a serious problem. Mineral processing plants are the main source of wastewater, which has a complex composition, containing a large amount of fine coal and clay minerals, as well as these suspended hydrophilic fine particles forming a difficult-to-treat colloidal solution. Flocculation is the most effective solution for wastewater clarification and sedimentation, and flocculants are the basic element of flocculation technology. Polyacrylamide (PAM) is the most commonly used flocculant, and various PAM derivatives have been developed. Although they have good sedimentation effects, they have long reaction times and high energy consumption. Furthermore, the residual toxic monomer acrylamide is released into the ecological environment during production and use, causing adverse effects, harming human health, and possessing potential carcinogenicity. Therefore, developing green, low-toxicity, and widely available flocculants is of great significance.

[0008] In view of this, the present invention is hereby proposed. Summary of the Invention

[0009] The purpose of this invention is to provide a method for separately adding water to the flotation process of polymetallic tin, lead, zinc, and antimony. This method collects the process water from multiple flotation stages separately and adds it in stages according to quality, effectively avoiding the impact of recycled water on the flotation operations of lead-antimony, zinc-sulfur, desulfurization, and cassiterite, ensuring the mineral processing indicators, and greatly reducing the amount of water, reagents, clean water, and wastewater carried away by the discharged slurry. It uses a new type of cationic flocculant, which has good flocculation and sedimentation effects, requires less dosage, and is energy-saving and environmentally friendly.

[0010] In order to achieve the above-mentioned objectives of the present invention, the following technical solution is adopted:

[0011] A method for adding water for the flotation of tin-lead-zinc-antimony polymetallic ores by branch separation includes the following steps:

[0012] (1) The tin-lead-zinc-antimony polymetallic ore is wet-milled and then magnetically separated. The tailings of the magnetic separation are concentrated by the first thickening device. The underflow slurry is then subjected to lead-antimony-zinc-sulfur flotation separation to obtain lead-antimony concentrate and zinc-sulfur tailings. The filter water of the magnetic separation concentrate, the filter water of the lead-antimony concentrate and the overflow water of the first thickening device are sent to the return water tank A as the wet milling water for the tin-lead-zinc-antimony polymetallic ore, the lead-antimony-zinc-sulfur flotation separation operation water and the foam washing water for the lead-antimony concentrate.

[0013] (2) The zinc-sulfur tailings are subjected to zinc-sulfur flotation operation. The zinc-sulfur flotation concentrate is fed into the second concentration unit for concentration. A flocculant is added to the second concentration unit. The flocculant is obtained by free radical polymerization of guar gum and [2-(methacryloyloxy)ethyl]trimethylammonium chloride. The overflow water of the second concentration unit is sent to the return water tank B as makeup water for the zinc-sulfur flotation operation.

[0014] (3) The underflow slurry concentrated by the second thickening device is subjected to zinc-sulfur separation operation to obtain zinc concentrate and sulfur concentrate. The filter water of the zinc concentrate and the filter water of the sulfur concentrate are sent to the return water tank C as the replenishment water for the zinc-sulfur separation operation and the foam washing water for the zinc concentrate and the sulfur concentrate.

[0015] (4) The tailings obtained from zinc-sulfur flotation in step (2) are subjected to shaking table gravity separation. The shaking table tailings are concentrated by the third thickening device and then subjected to desulfurization flotation. The desulfurization flotation tailings are concentrated by the fourth thickening device and then subjected to cassiterite flotation. The filtered water of the shaking table concentrate, the overflow water of the third thickening device, the overflow water of the fourth thickening device, and the filtered water of the cassiterite flotation concentrate are sent to the return water tank D as makeup water for the shaking table gravity separation, the desulfurization flotation, and the cassiterite flotation.

[0016] Preferably, in step (1), the pulp concentration in the lead-antimony-zinc-sulfur flotation separation operation is 30%-35%, and the pulp pH is 11-12.

[0017] Preferably, in step (2), the pH of the slurry in the zinc-sulfur flotation operation is 6-8.

[0018] Preferably, step (2) further includes a step of classifying the underflow slurry concentrated by the second thickening device. The coarse particles ≥0.074mm after classification are mixed with the replenished water in the return water tank B and then wet-milled. The wet-milled product is returned to the classification step. The fine particles -0.074mm after classification are mixed with the replenished water in the return water tank C and then enter the zinc-sulfur separation operation.

[0019] Preferably, in step (2), the amount of flocculant used in the second concentration device is 10-20 g / m³. 3 Water, with a compression layer thickness of 1-2 cm, a settling rate of 20-50 cm / min, and a light transmittance of ≥95% for the supernatant.

[0020] Preferably, in step (2), the guar gum and the [2-(methacryloyloxy)ethyl]trimethylammonium chloride are subjected to free radical polymerization under ultraviolet light initiation to obtain the flocculant.

[0021] Preferably, in step (2), the mass ratio of the guar gum to the [2-(methacryloyloxy)ethyl]trimethylammonium chloride is 1-3:3-8.

[0022] Preferably, in step (3), the pH of the slurry in the zinc-sulfur separation operation is 13-14.

[0023] Preferably, in step (4), the pH of the desulfurization flotation slurry is 6-8.

[0024] Preferably, step (4) further includes a step of wet grinding the underflow slurry concentrated by the third thickening device, using the water in the return water tank D as the replenishment water for wet grinding in step (4), and after wet grinding, the fine particles of -0.038mm are combined with the replenishment water in the return water tank D and the pH is adjusted for desulfurization flotation, and the desulfurization flotation concentrate is combined with the sulfur concentrate.

[0025] Preferably, in step (4), the pH of the cassiterite flotation slurry is 6-8.

[0026] Preferably, in step (4), the filtered water of the shaker concentrate, the overflow water of the third concentration device and the overflow water of the fourth concentration device are fed into the return water tank D through a U-shaped inclined plate. The inclined plate of the U-shaped inclined plate includes multiple U-shaped grooves, and the tangential angle of the inclined plate is 30°-45°.

[0027] Preferably, the first concentration device, the second concentration device, the third concentration device and the fourth concentration device are all thickeners.

[0028] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0029] (1) The method of this invention is designed for polymetallic sulfide ores of tin, lead, zinc, and antimony, which involve zinc-sulfur co-flotation under acidic conditions, zinc-sulfur separation under alkaline conditions, and cassiterite flotation under acidic conditions. By adding a concentration device and a return water tank, the circulating water for multiple flotation processes can be collected and recycled separately. In particular, the zinc-sulfur co-flotation and zinc-sulfur flotation separation processes significantly reduce the amount of clean water used and the amount of lime used to adjust the pH of the slurry.

[0030] (2) In the method of the present invention, both the concentrate and tailings are concentrated by a thickening device, and the flotation process water is recycled in the corresponding process of the concentrator, which minimizes the amount of water carried away by the discharged slurry, the amount of flotation reagents added, the amount of fresh water used in the flotation process, and the amount of wastewater that needs to be treated.

[0031] (3) In this invention, the cassiterite shaking table gravity separation, flotation, and lead-antimony flotation all use their respective systems for water return or replenishment, effectively reducing the Ca2+ emissions caused by the use of large amounts of lime in the zinc-sulfur flotation process. 2+ The effects of high concentrations.

[0032] (4) In this invention, flocculant is added to the second concentration device to reduce the content of fine particles in the overflow water and avoid the fine particles circulating in the return water, which would cause high energy consumption or affect the flotation separation of polymetals. The flocculant in this invention has excellent settling effect in treating mineral processing wastewater. The flocculant uses guar gum, a natural organic flocculant, as raw material. Its flocculation performance is significantly improved compared with guar gum. Compared with the traditional flocculant polyacrylamide, the dosage is low, saving costs. Its flocculation mechanism is mainly the synergistic effect of charge neutralization, bridging and improving hydrophobicity. It solves the thorny wastewater challenge faced by industrial sustainable development and reduces environmental pollution, promoting the widespread application of guar gum-based flocculants in the field of water treatment. Attached Figure Description

[0033] To more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0034] Figure 1 This is a schematic diagram of the process flow for the flotation of polymetallic ore with tin, lead, zinc, and antimony using branch separation and water replenishment, according to an embodiment of the present invention.

[0035] Figure 2 This is a schematic diagram of the structure of the U-shaped inclined plate provided in an embodiment of the present invention. Detailed Implementation

[0036] The technical solution of the present invention will be clearly and completely described below with reference to the accompanying drawings and specific embodiments. However, those skilled in the art will understand that the embodiments described below are some embodiments of the present invention, but not all embodiments, and are only used to illustrate the present invention, and should not be regarded as limiting the scope of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention. Where specific conditions are not specified in the embodiments, conventional conditions or conditions recommended by the manufacturer shall be followed. Where the manufacturers of reagents or instruments are not specified, they are all conventional products that can be purchased commercially.

[0037] like Figure 1 As shown, an embodiment of the present invention provides a method for adding water to the flotation branch for different grades of tin-lead-zinc-antimony polymetallic ores, comprising the following steps:

[0038] (1) The tin-lead-zinc-antimony polymetallic ore is wet-milled and then magnetically separated. The tailings of the magnetic separation are concentrated by the first thickening device. The underflow slurry is then subjected to lead-antimony-zinc-sulfur flotation separation to obtain lead-antimony concentrate and zinc-sulfur tailings. The filter water of the magnetic separation concentrate, the filter water of the lead-antimony concentrate and the overflow water of the first thickening device are sent to the return water tank A as the wet milling water for the tin-lead-zinc-antimony polymetallic ore, the lead-antimony-zinc-sulfur flotation separation operation water and the foam washing water for the lead-antimony concentrate.

[0039] (2) The zinc-sulfur tailings are subjected to zinc-sulfur flotation operation. The zinc-sulfur flotation concentrate is fed into the second concentration unit for concentration. A flocculant is added to the second concentration unit. The flocculant is obtained by free radical polymerization of guar gum and [2-(methacryloyloxy)ethyl]trimethylammonium chloride. The overflow water of the second concentration unit is sent to the return water tank B as makeup water for the zinc-sulfur flotation operation.

[0040] (3) The underflow slurry concentrated by the second thickening device is subjected to zinc-sulfur separation operation to obtain zinc concentrate and sulfur concentrate. The filter water of the zinc concentrate and the filter water of the sulfur concentrate are sent to the return water tank C as replenishment water for zinc-sulfur separation operation and foam washing water for zinc concentrate and sulfur concentrate.

[0041] (4) The tailings obtained from zinc-sulfur flotation in step (2) are subjected to shaking table gravity separation. The shaking table tailings are concentrated by the third thickening device and then subjected to desulfurization flotation. The desulfurization flotation tailings are concentrated by the fourth thickening device and then subjected to cassiterite flotation. The filtered water of the shaking table concentrate, the overflow water of the third thickening device, the overflow water of the fourth thickening device, and the filtered water of the cassiterite flotation concentrate are sent to the return water tank D as makeup water for the shaking table gravity separation, the desulfurization flotation, and the cassiterite flotation.

[0042] This invention addresses the characteristics of polymetallic sulfide ores of tin, lead, zinc, and antimony, which involve zinc-sulfur co-flotation under weakly acidic or near-neutral conditions, zinc-sulfur separation under strongly alkaline conditions, and cassiterite flotation under weakly acidic or near-neutral conditions. By adding a thickening device and a return water tank, the invention enables the separate collection and recycling of process water for multiple flotation stages. This effectively avoids the impact of return water on lead-antimony, zinc-sulfur, desulfurization, and cassiterite flotation operations, ensuring mineral processing indicators and minimizing the amount of water carried away by the discharged slurry, the amount of reagents added, the amount of fresh water used, and the amount of wastewater.

[0043] This invention utilizes separate systems for cassiterite shaking table gravity separation, flotation, and lead-antimony flotation, all of which employ either recycled water or added clean water, effectively reducing the calcium emissions caused by the use of large amounts of lime during zinc-sulfur separation. 2+ The effects of high concentrations.

[0044] The method of this invention adds a flocculant to the second concentration unit to reduce the content of fine particles in the overflow water, avoiding the high energy consumption or the impact on the flotation separation of polymetals caused by the circulation of fine particles in the return water. The flocculant in this invention has excellent settling effect in treating mineral processing wastewater. The flocculant is made from guar gum, a natural organic flocculant, and is obtained by free radical polymerization with [2-(methacryloyloxy)ethyl]trimethylammonium chloride (DMC). It has good flocculation performance, low dosage, low cost, good hydrophobicity, and good environmental performance. Using the flocculant in this invention can improve the return water utilization rate, reduce the amount of fresh water added, and reduce mineral processing costs.

[0045] In some specific embodiments of the present invention, the intensity of the magnetic separation is 160-480 kA / m.

[0046] In some specific embodiments of the present invention, in step (1), the mass concentration of the underflow slurry concentrated by the first thickening device is 40%-50%.

[0047] In some specific embodiments of the present invention, in step (1), the pulp concentration in the lead-antimony-zinc-sulfur flotation separation operation is 30%-35%, and the pulp pH is 11-12.

[0048] In some specific embodiments of the present invention, in step (2), the pH of the slurry in the zinc-sulfur flotation operation is 6-8.

[0049] In some specific embodiments of the present invention, step (2) further includes a step of classifying the underflow slurry concentrated by the second thickening device. After classification, coarse particles ≥0.074mm are mixed with the replenished water in the return water tank B and then wet-milled. The wet-milled product is returned to the classification step. After classification, fine particles -0.074mm (less than 0.074mm) are mixed with the replenished water in the return water tank C and then enter the zinc-sulfur separation operation.

[0050] In some specific embodiments of the present invention, in step (2), the amount of flocculant used in the second concentration device is 10-20 g / m³. 3 Water, for example, 10g / m 3 12g / m 3 14g / m 3 15g / m 3 16g / m 3 18g / m 3 20g / m 3 The values ​​are any one point or any two points within the range; the thickness of the compression layer is 1-2 cm, for example, any one point or any two points within the range of 1 cm, 1.2 cm, 1.4 cm, 1.5 cm, 1.6 cm, 1.8 cm, 2 cm; the settling rate is 20-50 cm / min, for example, any one point or any two points within the range of 20 cm / min, 30 cm / min, 40 cm / min, 50 cm / min; and the transmittance of the supernatant is ≥95%.

[0051] In some specific embodiments of the present invention, in step (2), the guar gum and the [2-(methacryloyloxy)ethyl]trimethylammonium chloride are obtained by free radical polymerization under ultraviolet light initiation conditions to obtain the flocculant.

[0052] In some specific embodiments of the present invention, in step (2), the mass ratio of the guar gum and the [2-(methacryloyloxy)ethyl]trimethylammonium chloride is 1-3:3-8, for example, any one value or a range of any two values ​​from 1:3, 1:4, 1:5, 1:6, 1:7, 1:8, 2:3, 2:4, 2:5, 2:7, 3:3, 3:4, 3:5, 3:7, 3:8.

[0053] In some specific embodiments of the present invention, the method for synthesizing the flocculant includes the following steps: in a reactor with a nitrogen inlet, an aqueous solution of guar gum is purged with nitrogen, DMC is dissolved in water and mixed with an aqueous solution of guar gum, the reactor is immediately sealed, and a free radical polymerization reaction is carried out under ultraviolet light initiation. After the reaction is terminated, the flocculant is obtained by washing, filtering and drying.

[0054] This invention successfully prepared a cationic flocculant through ultraviolet light induction. The prepared flocculant has excellent sedimentation effect, and its flocculation effect is significantly improved compared with the use of guar gum or DMC alone. Compared with the traditional flocculant polyacrylamide, it requires less dosage and adds less, thus saving costs.

[0055] In some specific embodiments of the present invention, the mass concentration of the guar aqueous solution is 50%-80%, for example, any one value or a range of any two values ​​among 50%, 60%, 70%, and 80%.

[0056] In some specific embodiments of the present invention, the time of the free radical polymerization reaction is 30-60 min, for example, any value among 30 min, 40 min, 50 min, and 60 min, or a range of any two fixed values.

[0057] In some specific embodiments of the present invention, the reaction is terminated by introducing air after the free radical reaction is completed.

[0058] In some specific embodiments of the present invention, the solvent used for washing includes ethanol and / or water.

[0059] In some specific embodiments of the present invention, in step (3), the pH of the slurry in the zinc-sulfur separation operation is 13-14.

[0060] In some specific embodiments of the present invention, in step (4), the pH of the desulfurization flotation slurry is 6-8.

[0061] In some specific embodiments of the present invention, step (4) further includes a step of wet milling the underflow slurry concentrated by the third thickening device, using the water in the return water tank D as the replenishing water for wet milling in step (4), and the fine particles of -0.038mm (less than 0.038mm) after wet milling are combined with the replenishing water in the return water tank D and the pH is adjusted for desulfurization flotation, and the desulfurization flotation concentrate is combined with the sulfur concentrate.

[0062] In some specific embodiments of the present invention, in step (4), the pH of the cassiterite flotation slurry is 6-8.

[0063] In some specific embodiments of the present invention, in step (4), the filtered water from the shaking table concentrate, the overflow water from the third concentration device, and the overflow water from the fourth concentration device are fed into the return water tank D through a U-shaped inclined plate, as shown below. Figure 2As shown, the inclined plate of the U-shaped inclined plate includes multiple U-shaped grooves, such as two, three, four, etc., and the tangential angle of the inclined plate (the angle between the inclined plate and the horizontal plane) is 30°-45°, such as any one value or any two values ​​of 30°, 35°, 40°, 45°.

[0064] U-shaped inclined plates have excellent sedimentation effects on fine and micro-fine particles. The turbidity of the recycled water after treatment by the U-shaped inclined plates can reach 0.5-1 JTU, which reduces power consumption and the content of micro-fine particles in the recycled water, thereby improving the utilization rate of recycled water, reducing the amount of clean water to be added, and reducing the cost of mineral processing.

[0065] In some specific embodiments of the present invention, the first concentration device, the second concentration device, the third concentration device and the fourth concentration device are all thickeners, which are used to concentrate the flotation concentrate or flotation tailings of each process, so that the process water of each process can be recycled in the corresponding process, thereby reducing the amount of clean water and pH adjustment reagent used.

[0066] The following detailed description of some embodiments of the present invention is provided in conjunction with specific examples. Unless otherwise specified, all raw materials used in the embodiments are commercially available.

[0067] Example 1

[0068] a. Preparation of flocculants:

[0069] In a reactor equipped with a nitrogen inlet, guar gum was dissolved in water to prepare a 50% solution, and the mixture was purged with nitrogen for 30 min at room temperature. DMC was dissolved in 5 mL of water and mixed with the guar gum solution at a mass ratio of guar gum to DMC of 1:3. The reaction vessel was then immediately sealed and placed in a photocatalytic instrument (PL-GHX-V, Beijing Prince Technology Co., Ltd., China) for 30 min under mercury lamp irradiation (500 W, 365 nm ultraviolet light). After the reaction was complete, air was introduced to terminate the reaction. The mixture was then washed and purified with ethanol / water at a 1:1 (w / w) ratio, filtered, and dried in a convection oven at 105 °C until no further weight loss occurred. The resulting product was then ground and stored for later use.

[0070] b. Separate water replenishment process for tin-lead-zinc-antimony polymetallic ores:

[0071] (1) After adding clean water, the polymetallic sulfide ore of tin, lead, zinc and antimony is wet-milled in ball mill No. 1 to reach the qualified grinding fineness. Then, a magnetic separation operation of roughing and scavenging is carried out. The magnetic separation tailings are fed into the first thickener for concentration. Lime is added to the underflow of the first thickener to adjust the pH of the slurry to 12. The mass concentration of the underflow of the first thickener reaches 40%. The concentrated sulfide ore is transported to the separation process by slurry pump. The slurry is adjusted to a mass concentration of 30% by water in the return pool A and then the lead-antimony-zinc-sulfur flotation separation operation is carried out. The magnetic separation concentrate filtration water, lead-antimony concentrate filtration water and the overflow water of the first thickener are pumped to the high-level front return water pool A and then flow by gravity through the pipeline as the water to be added before and after the No. 1 ball mill, the water to be added for the lead-antimony-zinc-sulfur flotation separation operation and the foam washing water of the lead-antimony concentrate.

[0072] (2) The zinc-sulfur tailings obtained from lead-antimony-zinc-sulfur flotation separation are mixed with water added to the downstream return water tank B, and the pH of the slurry is adjusted to 7 with sulfuric acid for zinc-sulfur co-flotation. The zinc-sulfur co-flotation concentrate is fed into the second thickener, and flocculant is added to the second thickener at a dosage of 10 g / m³. 3 Water, the overflow water from the second thickener is sent to the return water tank B, and the underflow of the second thickener is classified. Coarse particles ≥0.074mm are added to the return water tank B, water is added and fed into the No. 2 ball mill for wet grinding, and the ground product is returned to the classification process.

[0073] (3) After the fine particles of -0.074mm in step (2) are classified, they are mixed with the water added to the return water tank C, and the pH is adjusted to 14 with lime. Zinc-sulfur separation is carried out to obtain zinc concentrate and sulfur concentrate. The overflow water after filtering zinc concentrate and sulfur concentrate is pumped to the high-level return water tank C as the water added to the zinc-sulfur separation operation and the foam rinsing water for zinc concentrate and sulfur concentrate.

[0074] (4) The tailings obtained from zinc-sulfur flotation are treated by a classifier and then combined with water in the return water tank D and fed into a shaking table for gravity separation. The shake table concentrate is filtered and the filtrate is returned to the return water tank D through a U-shaped inclined plate (3 U-shaped troughs). The tailings from the shaking table are concentrated by the third thickener and the overflow is returned to the return water tank D through a U-shaped inclined plate (3 U-shaped troughs). The underflow is combined with the water added to the return water tank D and fed into the No. 3 ball mill for wet grinding. After wet grinding, the fine particles of -0.038mm are combined with the water added to the return water tank D and sulfuric acid is added to adjust the pH of the slurry to 7 before desulfurization flotation. The desulfurization flotation concentrate is combined with the sulfur concentrate and the desulfurization flotation tailings are fed into the fourth thickener for concentration. The overflow of the fourth thickener is fed into the return water tank D through a U-shaped inclined plate (3 U-shaped troughs). After adjusting the pH of the slurry to 7 by adjusting the underflow of the fourth thickener, cassiterite flotation is carried out. The froth product is dewatered and the return water is returned to the return water tank D.

[0075] In the second thickener, the thickness of the compression layer is 1 cm, the settling rate is 20 cm / min, and the transmittance of the supernatant is ≥95%.

[0076] Calculations show that the process described in this embodiment requires 10m³ of clean water. 3 The lime dosage is 1000 kg / ton of raw ore. However, the traditional process (which does not use a thickening device or a return water tank to recover process water, and the product from the previous flotation step directly enters the next flotation step) involves excessive water addition during mineral processing, resulting in high mineral processing costs and energy consumption, large reagent usage, and residual reagents in the circulating water affecting the quality of the mineral processing. Specifically, the amount of clean water used is 30 m³. 3 The lime consumption is 2000 kg / ton of raw ore; compared with the traditional process, the water consumption in this embodiment is reduced by 20 m³ / ton. 3 / ton of raw ore, the amount of lime used was reduced by 1000kg / ton of raw ore.

[0077] Example 2

[0078] a. Preparation of flocculants:

[0079] In a reactor equipped with a nitrogen inlet, guar gum was dissolved in water to prepare a 50% solution, and the mixture was purged with nitrogen for 30 min at room temperature. DMC was dissolved in 5 mL of water and mixed with the guar gum solution at a mass ratio of 2:3. The reaction vessel was then immediately sealed and placed in a photocatalytic instrument (PL-GHX-V, Beijing Prince Technology Co., Ltd., China) for 30 min under mercury lamp irradiation (500 W, 365 nm ultraviolet light). After the reaction was complete, air was introduced to terminate the reaction. The mixture was then washed and purified with ethanol / water at a 1:1 (w / w) ratio, filtered, and dried in a convection oven at 105 °C until no further weight loss occurred. The resulting product was then ground and stored for later use.

[0080] b. Separate water replenishment process for tin-lead-zinc-antimony polymetallic ores:

[0081] (1) After adding water to the polymetallic sulfide ore of tin, lead, zinc and antimony, it is wet-milled in ball mill No. 1 to reach the qualified grinding fineness. Then, a magnetic separation operation of roughing and scavenging is carried out. The magnetic separation tailings are fed into the first thickener for concentration. Lime is added to the underflow of the first thickener to adjust the pH of the slurry to 11. The mass concentration of the underflow of the first thickener reaches 45%. The concentrated sulfide ore is transported to the separation process by slurry pump. The slurry is adjusted to a mass concentration of 35% by water in return water tank A and then the lead-antimony-zinc-sulfur flotation separation operation is carried out. The magnetic separation concentrate filtration water, lead-antimony concentrate filtration water and the overflow water of the first thickener are pumped to the high-level front return water tank A and then flow by gravity through pipeline as the water added before and after ball mill No. 1, the water added for lead-antimony-zinc-sulfur flotation separation operation and the foam washing water for lead-antimony concentrate.

[0082] (2) The zinc-sulfur tailings obtained from lead-antimony-zinc-sulfur flotation separation are mixed with water added to the downstream return water tank B, and the pH of the slurry is adjusted to 6 with sulfuric acid for zinc-sulfur co-flotation. The zinc-sulfur co-flotation concentrate is fed into the second thickener, and flocculant is added to the second thickener at a dosage of 20 g / m³. 3 Water, the overflow water from the second thickener is sent to the return water tank B, and the underflow of the second thickener is classified. Coarse particles ≥0.074mm are added to the return water tank B, water is added and fed into the No. 2 ball mill for wet grinding, and the ground product is returned to the classification process.

[0083] (3) After the fine particles of -0.074mm in step (2) are classified, they are mixed with the water added to the return water tank C, and the pH is adjusted to 13 with lime. Zinc-sulfur separation is carried out to obtain zinc concentrate and sulfur concentrate. The overflow water after filtering zinc concentrate and sulfur concentrate is pumped to the high-level return water tank C as the water added to the zinc-sulfur separation operation and the foam rinsing water for zinc concentrate and sulfur concentrate.

[0084] (4) The tailings obtained from zinc-sulfur flotation are treated by a classifier and then combined with water in the return water tank D and fed into a shaking table for gravity separation. The shake table concentrate is filtered and the filtrate is returned to the return water tank D through a U-shaped inclined plate (3 U-shaped troughs). The shake table tailings are concentrated by the third thickener and the overflow is returned to the return water tank D through a U-shaped inclined plate (3 U-shaped troughs). The underflow is combined with the water added to the return water tank D and fed into the No. 3 ball mill for wet grinding. After wet grinding, the fine particles of -0.038mm are combined with the water added to the return water tank D and sulfuric acid is added to adjust the pH of the slurry to 6 before desulfurization flotation. The desulfurization flotation concentrate is combined with the sulfur concentrate and the desulfurization flotation tailings are fed into the fourth thickener for concentration. The overflow of the fourth thickener is fed into the return water tank D through a U-shaped inclined plate (3 U-shaped troughs). The underflow of the fourth thickener is adjusted to adjust the pH of the slurry to 6 before cassiterite flotation. The froth product is dewatered and the return water is returned to the return water tank D.

[0085] In the second thickener, the thickness of the compression layer is 1.5 cm, the settling rate is 30 cm / min, and the transmittance of the supernatant is ≥95%.

[0086] Calculations show that the process described in this embodiment requires 15m³ of clean water. 3 The lime consumption is 1500 kg / ton of raw ore. However, the traditional process (which does not use a thickening device or a return water tank to recover process water, and the product from the previous flotation step directly enters the next flotation step) involves excessive water addition during mineral processing, resulting in high costs, energy consumption, and reagent usage. Furthermore, residual reagents in the circulating water can affect the quality of the mineral processing. Specifically, the amount of clean water used is 30 m³. 3 The lime consumption is 2000 kg / ton of raw ore; compared with the traditional process, the water consumption in this embodiment is reduced by 15m³. 3 / ton of raw ore, the amount of lime used was reduced by 500kg / ton of raw ore.

[0087] Comparative Example 1

[0088] The difference between Comparative Example 1 and Example 2 is that the flocculant used is polyacrylamide, and the dosage is 20 g / m³. 3 Water, and other conditions are the same as in Example 2.

[0089] Calculations show that the amount of clean water used in Comparative Example 1 is 18m³. 3 The lime consumption is 1850 kg / ton of raw ore.

[0090] Although the present invention has been illustrated and described with specific embodiments, it should be understood that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them; those skilled in the art should understand that modifications can be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features therein, without departing from the spirit and scope of the present invention; and these modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention; therefore, this means that all such substitutions and modifications that fall within the scope of the present invention are included in the appended claims.

Claims

1. A method for adding water to the flotation of tin-lead-zinc-antimony polymetallic ores, characterized in that, Includes the following steps: (1) The tin-lead-zinc-antimony polymetallic ore is wet-milled and then magnetically separated. The tailings of the magnetic separation are concentrated by the first thickening device. The underflow slurry is then subjected to lead-antimony-zinc-sulfur flotation separation to obtain lead-antimony concentrate and zinc-sulfur tailings. The filter water of the magnetic separation concentrate, the filter water of the lead-antimony concentrate and the overflow water of the first thickening device are sent to the return water tank A as the wet milling water for the tin-lead-zinc-antimony polymetallic ore, the lead-antimony-zinc-sulfur flotation separation operation water and the foam washing water for the lead-antimony concentrate. (2) The zinc-sulfur tailings are subjected to zinc-sulfur flotation operation. The zinc-sulfur flotation concentrate is fed into the second concentration unit for concentration. A flocculant is added to the second concentration unit. The flocculant is obtained by free radical polymerization of guar gum and [2-(methacryloyloxy)ethyl]trimethylammonium chloride. The overflow water of the second concentration unit is sent to the return water tank B as makeup water for the zinc-sulfur flotation operation. (3) The underflow slurry concentrated by the second thickening device is subjected to zinc-sulfur separation operation to obtain zinc concentrate and sulfur concentrate. The filter water of the zinc concentrate and the filter water of the sulfur concentrate are sent to the return water tank C as the replenishment water for the zinc-sulfur separation operation and the foam washing water for the zinc concentrate and the sulfur concentrate. (4) The tailings obtained from zinc-sulfur flotation in step (2) are subjected to shaking table gravity separation. The shaking table tailings are concentrated by the third thickening device and then subjected to desulfurization flotation. The desulfurization flotation tailings are concentrated by the fourth thickening device and then subjected to cassiterite flotation. The filtered water of the shaking table concentrate, the overflow water of the third thickening device, the overflow water of the fourth thickening device, and the filtered water of the cassiterite flotation concentrate are sent to the return water tank D as makeup water for the shaking table gravity separation, the desulfurization flotation, and the cassiterite flotation.

2. The method for adding water to the flotation branch of a polymetallic ore (tin-lead-zinc-antimony) according to claim 1, characterized in that, In step (1), the pulp concentration in the lead-antimony-zinc-sulfur flotation separation operation is 30%-35%, and the pulp pH is 11-12.

3. The method for adding water for the flotation of tin-lead-zinc-antimony polymetallic ores according to claim 1, characterized in that, In step (2), the pH of the slurry in the zinc-sulfur flotation operation is 6-8.

4. The method for adding water for flotation of tin-lead-zinc-antimony polymetallic ores according to claim 1, characterized in that, Step (2) also includes a step of classifying the underflow slurry concentrated by the second thickening device. After classification, coarse particles ≥0.074mm are mixed with the replenished water in the return water tank B and then wet-milled. The wet-milled product is returned to the classification operation. After classification, fine particles -0.074mm are mixed with the replenished water in the return water tank C and then enter the zinc-sulfur separation operation.

5. The method for adding water for flotation of tin-lead-zinc-antimony polymetallic ores according to claim 1, characterized in that, In step (2), the amount of flocculant used in the second concentration device is 10-20 g / m³. 3 Water, with a compression layer thickness of 1-2 cm, a settling rate of 20-50 cm / min, and a light transmittance of ≥95% for the supernatant.

6. The method for adding water for flotation of tin-lead-zinc-antimony polymetallic ores according to claim 1, characterized in that, In step (2), the guar gum and the [2-(methacryloyloxy)ethyl]trimethylammonium chloride are subjected to free radical polymerization under ultraviolet light initiation to obtain the flocculant.

7. The method for adding water for flotation of tin-lead-zinc-antimony polymetallic ores according to claim 1, characterized in that, In step (2), the mass ratio of the guar gum to the [2-(methacryloyloxy)ethyl]trimethylammonium chloride is 1-3:3-8.

8. The method for adding water for flotation of tin-lead-zinc-antimony polymetallic ores according to claim 1, characterized in that, In step (3), the pH of the slurry in the zinc-sulfur separation operation is 13-14.

9. The method for adding water for flotation of tin-lead-zinc-antimony polymetallic ores according to claim 1, characterized in that, In step (4), at least one of the following features (1)-(4) is included: (1) The pH of the desulfurization flotation slurry is 6-8; (2) It also includes a step of wet grinding the underflow slurry after the third thickening device is concentrated, using the water in the return water tank D as the replenishing water for wet grinding in step (4), and after wet grinding, the fine particles of -0.038mm are combined with the replenishing water in the return water tank D and the pH is adjusted for desulfurization flotation, and the desulfurization flotation concentrate is combined with the sulfur concentrate. (3) The pH of the cassiterite flotation pulp is 6-8; (4) The filtered water of the shaker concentrate, the overflow water of the third concentration device and the overflow water of the fourth concentration device are fed into the return water tank D through the U-shaped inclined plate. The inclined plate of the U-shaped inclined plate includes multiple U-shaped grooves and the tangent of the inclined plate is 30°-45°.

10. The method for adding water for the flotation of tin-lead-zinc-antimony polymetallic ores according to claim 1, characterized in that, The first concentration device, the second concentration device, the third concentration device and the fourth concentration device are all thickeners.

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