Method for flotation separation of bulk concentrate containing copper and lead

Abstract

The invention provides a method for flotation separation of bulk concentrate containing copper and lead, and relates to the field of mineral separation. The method for flotation separation of the bulk concentrate containing copper and lead comprises the steps that the bulk concentrate containing copper and lead is ground, activated carbon is added in the ore grinding process, then concentration is conducted, and concentrated ore pulp is obtained; adding water into the concentrated ore pulp to obtain ore pulp containing copper and lead bulk concentrate; and an acidic material is added into the ore pulp containing the copper and lead bulk concentrate, stirring is conducted, the pH of the ore pulp is made to be 0.5-4.5, then an inhibitor and a foaming agent are added, flotation separation is conducted, and copper concentrate and lead-containing concentrate are obtained. The inhibitor, the foaming agent and the minerals can react under the acidic condition that the pH is 0.5-4.5, and separation of copper minerals and lead minerals is facilitated. By means of the method, efficient separation of copper and lead in the copper-lead-containing bulk concentrate can be achieved.

Description

Technical Field

[0001] This application relates to the field of mineral processing, and more particularly to a method for flotation separation of copper-lead mixed concentrates. Background Technology

[0002] Copper and lead, as essential metals vital to the national economy and people's livelihoods, are used in numerous fields of industrial and agricultural production. With the accelerating pace of global economic integration, the demand for copper and lead metals is constantly increasing, prompting continuous development and progress in their production. As the economy develops, copper and lead mineral resources are being exploited on a large scale, leading to increasingly scarce resources and a growing volume of difficult-to-process ores.

[0003] Copper and lead have a strong affinity for sulfur, and in the Earth's crust, they often exist as sulfides in the post-magmatic hydrothermal stage. Ores containing copper and lead sulfides are called complex sulfide ores. These ores have extremely complex mineral compositions, dense inter-mineral relationships, large fluctuations in the content of valuable components, diverse structures, and wide variations in grain size, making them difficult-to-process ores. Their mineralization conditions have a controlling influence on the beneficiation of the ore. Furthermore, since copper and lead minerals have similar natural floatability, while preferential flotation processes can easily yield qualified concentrates, they often suffer from disadvantages such as long flotation processes, long flotation times, multiple reagent types, and large reagent dosages. In contrast, copper-lead mixed flotation processes have advantages such as short flotation processes, fewer reagent types, smaller reagent dosages, and higher recovery rates. However, in copper-lead or copper-lead-zinc mixed concentrates, residual beneficiation reagents can coat the mineral surface, forming a reagent film, thus increasing the difficulty of copper-lead separation and making it difficult to obtain ideal separation indicators. If the lead and zinc content in copper concentrate is too high, it will not only affect the pricing standard of copper concentrate, but also affect the subsequent smelting process.

[0004] Currently, copper concentrate is typically smelted using pyrometallurgical processes to obtain metallic copper. During these processes, lead primarily enters the flue gas and converter dust, while zinc mainly enters the slag and flue gas. These lead and zinc resources are difficult to recover and utilize. The excessive lead and zinc content in the flue gas, converter dust, and slag not only increases the difficulty of environmental pollution control but also results in a waste of lead and zinc resources.

[0005] To this end, numerous researchers have conducted extensive studies on the flotation separation processes and reagents for copper and lead. However, most of these studies focus on alkaline conditions, with relatively few studies addressing copper-lead separation under acidic conditions. Furthermore, the pulp pH is mostly controlled within the range of 4.5-7. For example, the Webern and Fletcher concentrators, owned by St. Joe Company in the United States, use a "starch + SO2 + K2Cr2O7 method" to adjust the pH to 4.5-5 for mixed concentrates with a lead-to-copper ratio of 30:1-50:1 (10:1-100:1 in extreme cases) to inhibit the flotation of chalcopyrite from galena. However, this method uses the highly toxic K2Cr2O7. The Nakuryu concentrator in Japan, under pH 6.8, uses sulfuric acid, sulfurous acid, and starch to suppress lead-zinc flotation of copper, achieving ideal results. However, sulfurous acid is unstable, has an irritating odor, and poses significant risks to the environment and human health. Summary of the Invention

[0006] The purpose of this application is to provide a method for flotation separation of copper-lead mixed concentrates to solve the above-mentioned problems.

[0007] To achieve the above objectives, this application adopts the following technical solution: This application provides a method for flotation separation of copper-lead mixed concentrate, comprising: The copper-lead mixed concentrate is ground, and activated carbon is added during the grinding process. Then it is concentrated to obtain a concentrated slurry. Water is added to the concentrated slurry to obtain a slurry containing a copper-lead mixed concentrate; An acidic substance is added to the slurry containing the copper-lead mixed concentrate, and the mixture is stirred to adjust the pH of the slurry to 0.5-4.5. Subsequently, an inhibitor and a frother are added, and flotation separation is carried out to obtain copper concentrate and lead concentrate.

[0008] According to embodiments of this application, the copper-lead mixed concentrate includes at least one of copper-lead mixed concentrate and copper-lead-zinc mixed concentrate; The copper-lead mixed concentrate contains 8-10 wt% copper and 14-30 wt% lead.

[0009] According to an embodiment of this application, the copper-lead mixed concentrate further includes zinc, and the zinc content in the copper-lead mixed concentrate is 23-25 ​​wt%.

[0010] According to embodiments of this application, the fineness of the grinding process is such that 75%-95% of the particles are of the -0.074mm size. The amount of activated carbon used is 200-1100 g / t of ore; The concentration of the slurry containing the copper-lead mixed concentrate is 10%-40%.

[0011] According to embodiments of this application, the acidic substance includes at least one of organic acid and inorganic acid; The organic acid includes at least one of acetic acid, oxalic acid, and citric acid; The inorganic acid includes at least one of hydrochloric acid, sulfuric acid, nitric acid, phosphoric acid, and silicic acid; And / or, after adding acidic substances, stir for 3-60 minutes.

[0012] According to embodiments of this application, the inhibitor includes at least one of organic acid inhibitors, cellulose inhibitors, silicate inhibitors, humic acid inhibitors, sulfur-containing inhibitors, phosphorus-containing inhibitors, starch, and dextrin. The organic acid inhibitors include at least one of oxalic acid and citric acid; The cellulose inhibitors include carboxymethyl cellulose; The silicate inhibitors include water glass; The humic acid inhibitors include at least one of humic acid and sodium humate. The sulfur-containing inhibitor includes at least one of sodium sulfide, sulfur dioxide, sulfurous acid, and sulfite; The phosphorus-containing inhibitor includes at least one of sodium pyrophosphate, sodium dithiophosphate, and sodium hexametaphosphate.

[0013] According to an embodiment of this application, the dosage of the inhibitor is 500-1500 g / t of ore feed.

[0014] According to embodiments of this application, the foaming agent includes at least one of pine oil, pine alcohol oil, camphor oil, eucalyptus oil, ether alcohol foaming agents, and ether foaming agents.

[0015] According to an embodiment of this application, the amount of the foaming agent used is 14-100 g / t of ore feed.

[0016] According to an embodiment of this application, the flotation separation includes adding 500-1500 g / t of inhibitor and 14-100 g / t of frother to a slurry with a pH of 0.5-4.5 for roughing to obtain a roughing froth product and a roughing underflow product; performing at least one cleaning operation on the roughing froth product, adding 20-150 g / t of inhibitor to the slurry in each cleaning operation, with the froth product from the final cleaning operation being copper concentrate; and performing at least one scavenging operation on the roughing underflow product, adding 4-20 g / t of frother to the scavenging operation, with the underflow product from the final scavenging operation being lead concentrate.

[0017] Compared with the prior art, the beneficial effects of this application include: This application obtains a fresh mineral surface through moderate grinding, and simultaneously reduces the impact of residual reagents in the mixed concentrate on subsequent operations through activated carbon adsorption during the grinding process. It utilizes the difference in floatability between copper and lead-zinc minerals under acidic conditions to achieve the separation of copper from lead and zinc minerals. The method of this application can achieve highly efficient separation of copper and lead in copper-lead mixed concentrates.

[0018] Moreover, the method of this application has the advantages of cheap and readily available raw materials and simple operation. In addition, this application avoids the use of highly toxic flotation reagents such as potassium dichromate, which has the advantages of being environmentally friendly and conducive to large-scale industrial promotion. Attached Figure Description

[0019] To more clearly illustrate the technical solutions of the embodiments of this application, the accompanying drawings used in the embodiments will be briefly described below. It should be understood that the following drawings only show some embodiments of this application and should not be regarded as a limitation on the scope of this application.

[0020] Figure 1 This is a flowchart of the method for flotation separation of copper-lead mixed concentrates in this application. Detailed Implementation

[0021] As used in this article: "Prepared from" is synonymous with "comprising". The terms "comprising", "including", "having", "containing", or any other variations thereof as used herein are intended to cover non-exclusive inclusion. For example, a composition, step, method, article, or apparatus that includes the listed elements is not necessarily limited to those elements, but may include other elements not expressly listed or elements inherent to such composition, step, method, article, or apparatus.

[0022] The conjunction "composed of..." excludes any unspecified elements, steps, or components. If used in a claim, this phrase makes the claim closed, excluding materials other than those described, except for associated conventional impurities. When the phrase "composed of..." appears in a clause of the body of a claim rather than immediately following it, it limits only the elements described in that clause; other elements are not excluded from the claim as a whole.

[0023] When a quantity, concentration, or other value or parameter is expressed as a range, a preferred range, or a range defined by a series of upper and lower preferred values, this should be understood as specifically disclosing all ranges formed by any pair of any upper or preferred value with any lower or preferred value, regardless of whether the range is disclosed individually. For example, when the range “1–5” is disclosed, the described range should be interpreted as including ranges “1–4”, “1–3”, “1–2”, “1–2 and 4–5”, “1–3 and 5”, etc. When numerical ranges are described herein, unless otherwise stated, the range is intended to include its endpoints and all integers and fractions within that range.

[0024] In these embodiments, unless otherwise specified, the portions and percentages are all by weight.

[0025] "Parts by mass" refers to the basic unit of measurement that expresses the mass ratio of multiple components. One part can represent any unit mass, such as 1g or 2.689g. If we say that component A has "a" parts by mass and component B has "b" parts by mass, it means the ratio of the mass of component A to the mass of component B is a:b. Alternatively, it can mean that the mass of component A is aK and the mass of component B is bK (where K is any number representing a multiplier). It is important to understand that, unlike parts by mass, the sum of the mass parts of all components is not limited to 100 parts.

[0026] "And / or" is used to indicate that one or both of the described situations may occur, for example, A and / or B includes (A and B) and (A or B).

[0027] This application provides a method for flotation separation of copper-lead mixed concentrates, with reference to... Figure 1 ,include: The copper-lead mixed concentrate is ground, and activated carbon is added during the grinding process. Then it is concentrated to obtain a concentrated slurry. Water is added to the concentrated slurry to obtain a slurry containing a copper-lead mixed concentrate; An acidic substance is added to the slurry containing the copper-lead mixed concentrate, and the mixture is stirred to adjust the pH of the slurry to 0.5-4.5. Subsequently, an inhibitor and a frother are added, and flotation separation is carried out to obtain copper concentrate and lead concentrate.

[0028] The flotation reagents (inhibitors, frothers) of this application react with minerals under acidic conditions with a pH of 0.5-4.5, which is beneficial for the separation of copper minerals from lead and zinc minerals. If the pH value is too low, it will affect the effectiveness of subsequent beneficiation reagents; if the pH value is too high, the cleaning effect on the mineral surface will not be thorough enough. This application controls the pH value within the range of 0.5-4.5, which ensures that the subsequent beneficiation reagents can fully exert their effects and facilitates the efficient separation of minerals.

[0029] In some embodiments, the pH of the slurry after adding the acidic substance is any value between 0.5, 0.7, 0.8, 1.0, 1.2, 1.4, 1.6, 1.8, 2.0, 2.2, 2.4, 2.6, 2.8, 3.0, 3.2, 3.4, 3.6, 3.8, 4.0, 4.2, 4.3, 4.5, or 0.5-4.5. The pH of the slurry after adding the acidic substance is preferably 0.8-4.5, and more preferably 0.8-4.3.

[0030] In some embodiments, the device for concentration is a thickener.

[0031] Adding activated carbon helps remove flotation reagents. After grinding, the slurry needs to be transported to a thickener for concentration and dewatering to obtain concentrated slurry and supernatant. The supernatant can be returned to the grinding process for recycling, which saves both water resources and reagents.

[0032] According to embodiments of this application, the copper-lead mixed concentrate includes at least one of copper-lead mixed concentrate and copper-lead-zinc mixed concentrate; The copper-lead mixed concentrate contains 8-10 wt% copper and 14-30 wt% lead.

[0033] For example, the copper content in a copper-lead mixed concentrate is any value between 8 wt%, 9 wt%, 10 wt%, or 8-10 wt%, and the lead content in a copper-lead mixed concentrate is any value between 14 wt%, 15 wt%, 16 wt%, 17 wt%, 18 wt%, 19 wt%, 20 wt%, 21 wt%, 22 wt%, 23 wt%, 24 wt%, 25 wt%, 26 wt%, 27 wt%, 28 wt%, 29 wt%, 30 wt%, or 14-30 wt%.

[0034] According to an embodiment of this application, the copper-lead mixed concentrate further includes zinc, and the zinc content in the copper-lead mixed concentrate is 23-25 ​​wt%.

[0035] For example, the zinc content in a copper-lead mixed concentrate is 23 wt%, 24 wt%, 25 wt%, or any value between 23 and 25 wt%.

[0036] According to an embodiment of this application, the fineness of the grinding is such that 75%-95% of the particles are of the -0.074mm size.

[0037] Grinding allows flotation reagents to come into full contact with the minerals, which is beneficial for the full progress of the reaction.

[0038] In some embodiments, the grinding equipment includes, but is not limited to, ball mills, rod mills, sand mills, etc., and the grinding media are made of, but are not limited to, stainless steel, cast iron, zirconium oxide, etc.

[0039] The amount of activated carbon used is 200-1100 g / t of ore; For example, the amount of activated carbon used is 200 g / t feed, 300 g / t feed, 400 g / t feed, 500 g / t feed, 600 g / t feed, 700 g / t feed, 800 g / t feed, 900 g / t feed, 1000 g / t feed, 1100 g / t feed, or any value between 200 and 1100 g / t feed. The concentration of the slurry containing the copper-lead mixed concentrate is 10%-40%.

[0040] For example, the concentration of the slurry containing copper-lead mixed concentrate is 10%, 15%, 20%, 25%, 30%, 35%, 40%, or any value between 10% and 40%.

[0041] In some embodiments, the concentration of the slurry containing copper-lead mixed concentrate is preferably 15%-35%, more preferably 20%-35%.

[0042] According to embodiments of this application, the acidic substance includes at least one of organic acid and inorganic acid; The organic acid includes at least one of acetic acid, oxalic acid, and citric acid; The inorganic acid includes at least one of hydrochloric acid, sulfuric acid, nitric acid, phosphoric acid, and silicic acid; And / or, after adding acidic substances, stir for 3-60 minutes. As the stirring time increases, the pH value of the slurry will increase slightly.

[0043] For example, the stirring time after adding the acidic substance can be any value between 3 min, 5 min, 10 min, 15 min, 20 min, 25 min, 30 min, 35 min, 40 min, 45 min, 50 min, 55 min, 60 min, or 3-60 min.

[0044] In some embodiments, the stirring time after adding the acidic substance is preferably 3-45 min, more preferably 3-40 min.

[0045] According to embodiments of this application, the inhibitor includes at least one of organic acid inhibitors, cellulose inhibitors, silicate inhibitors, humic acid inhibitors, sulfur-containing inhibitors, phosphorus-containing inhibitors, starch, and dextrin. The organic acid inhibitors include at least one of oxalic acid and citric acid; The cellulose inhibitors include carboxymethyl cellulose; The silicate inhibitors include water glass; The humic acid inhibitors include at least one of humic acid and sodium humate. The sulfur-containing inhibitor includes at least one of sodium sulfide, sulfur dioxide, sulfurous acid, and sulfites; sulfites include sodium sulfite. The phosphorus-containing inhibitor includes at least one of sodium pyrophosphate, sodium dithiophosphate, and sodium hexametaphosphate.

[0046] According to an embodiment of this application, the dosage of the inhibitor is 500-1500 g / t of ore feed.

[0047] For example, the dosage of the inhibitor is 500 g / t feed, 600 g / t feed, 700 g / t feed, 800 g / t feed, 900 g / t feed, 1000 g / t feed, 1100 g / t feed, 1200 g / t feed, 1300 g / t feed, 1400 g / t feed, 1500 g / t feed, or any value between 500 and 1500 g / t feed.

[0048] According to embodiments of this application, the foaming agent includes at least one of pine oil, pine alcohol oil (also known as No. 2 oil), camphor oil, eucalyptus oil, ether alcohol foaming agents, and ether foaming agents.

[0049] According to an embodiment of this application, the amount of the foaming agent used is 14-100 g / t of ore feed.

[0050] For example, the dosage of frother is 14 g / t feed, 16 g / t feed, 18 g / t feed, 20 g / t feed, 22 g / t feed, 24 g / t feed, 26 g / t feed, 28 g / t feed, 30 g / t feed, 32 g / t feed, 34 g / t feed, 36 g / t feed, 38 g / t feed, 40 g / t feed, 42 g / t feed, 44 g / t feed, 46 g / t feed, 48 g / t feed, 50 g / t feed, 52 g / t feed, 54 g / t feed, 56 g / t feed, 58 g / t feed, 60 g / t feed, 62 g / t feed, 64 g / t feed, 68 g / t feed, 70 g / t feed, 72 g / t feed, 74 g / t feed. The feed rates are 76 g / t, 78 g / t, 80 g / t, 82 g / t, 84 g / t, 86 g / t, 88 g / t, 90 g / t, 92 g / t, 94 g / t, 96 g / t, 98 g / t, 100 g / t, or any value between 14 and 100 g / t.

[0051] According to an embodiment of this application, the flotation separation includes adding 500-1500 g / t of depressant and 14-100 g / t of frother to a slurry with a pH of 0.5-4.5 for roughing to obtain a roughing froth product and a roughing underflow product; performing at least one cleaning operation on the roughing froth product, adding 20-150 g / t of depressant to the slurry in each cleaning operation, with the froth product from the final cleaning operation being copper concentrate; performing at least one scavenging operation on the roughing underflow product, adding 4-20 g / t of frother to the scavenging operation, with the underflow product from the final scavenging operation being lead concentrate; and returning all intermediate products in the flotation separation process to the preceding flotation operation in a step-by-step return principle, forming a closed-loop flotation separation process.

[0052] In some embodiments, the inhibitors in the selection process may be the same as or different from the inhibitors in the roughing process, and independently include at least one of organic acid inhibitors, cellulose inhibitors, silicate inhibitors, humic acid inhibitors, sulfur-containing inhibitors, phosphorus-containing inhibitors, starch, and dextrin.

[0053] For example, the dosage of inhibitor in the refining operation is 20 g / t feed, 30 g / t feed, 40 g / t feed, 50 g / t feed, 60 g / t feed, 70 g / t feed, 80 g / t feed, 90 g / t feed, 100 g / t feed, 110 g / t feed, 120 g / t feed, 130 g / t feed, 140 g / t feed, 150 g / t feed, or any value between 20 and 150 g / t feed.

[0054] The frother used in the scavenging operation may be the same as or different from the frother used in the roughing operation, and may independently include at least one of pine oil, pine alcohol oil (also known as No. 2 oil), camphor oil, eucalyptus oil, ether alcohol frothers, and ether frothers.

[0055] For example, the amount of frother used in scavenging operations is 4 g / t feed, 5 g / t feed, 6 g / t feed, 7 g / t feed, 8 g / t feed, 9 g / t feed, 10 g / t feed, 11 g / t feed, 12 g / t feed, 13 g / t feed, 14 g / t feed, 15 g / t feed, 16 g / t feed, 17 g / t feed, 18 g / t feed, 19 g / t feed, 20 g / t feed, or any value between 4 and 20 g / t feed.

[0056] The implementation schemes of this application will be described in detail below with reference to specific embodiments. However, those skilled in the art will understand that the following embodiments are only for illustrating this application and should not be regarded as limiting the scope of this application. Unless otherwise specified in the embodiments, conventional conditions or conditions recommended by the manufacturer shall apply. Reagents or instruments used without specified manufacturers are all conventional products that can be purchased commercially.

[0057] Example 1 The lead-zinc mixed concentrate used in Example 1 originated from a copper-lead-zinc sulfide ore with extremely fine intercalated grains. The copper-lead-zinc mixed concentrate in Example 1 contained 9.5% copper, 15% lead, and 25% zinc. Multiple institutions have verified that even when ground to a fineness of -325 mesh (90%), effective separation of copper, lead, and zinc is still difficult; industrially, only a mixed concentrate can be produced. This example uses the mixed concentrate produced under these industrial conditions as raw material for subsequent processing.

[0058] Add activated carbon to the copper-lead-zinc mixed concentrate at a rate of 500 g / t feed, and then grind for 5 minutes; the fineness of the ore is -0.074 mm, accounting for 91%. Subsequently, concentrate and dewater the slurry to a concentration of 50%. Add fresh water to bring the slurry concentration to 20%. Add sulfuric acid to adjust the slurry pH to 1.8 ± 0.1, and stir for 10 minutes. As the stirring time increases, the slurry pH rises to 3.5 ± 0.2. Then add 400 g / t sodium humate and 1000 g / t sodium sulfite as inhibitors. The feed ore and frother No. 2 oil (14g / t) are used for roughing to obtain roughing froth and roughing underflow products. The roughing froth product undergoes two cleaning operations, with 20g / t sodium humate and 50g / t sodium sulfite added in batches during each operation. The froth product from the second cleaning operation is copper concentrate. The roughing underflow product undergoes two scavenging operations, with 6g / t frother No. 2 oil added in batches during each scavenging operation. The underflow product from the second scavenging operation is a lead-zinc mixed concentrate. Intermediate products from the flotation separation process are returned to the preceding flotation operations in a sequential manner, forming a closed-loop flotation separation process. The copper concentrate contains 22.28% copper, 9.61% lead, and 9.87% zinc, with a copper recovery rate of 85.32%. The lead-zinc mixed concentrate contains 2.19% copper, 18.08% lead, and 33.65% zinc, with lead and zinc recovery rates of 76.69% and 85.64%, respectively.

[0059] Example 2 In the copper-lead-zinc mixed concentrate of Example 2, the copper content was 9.1%, the lead content was 14.3%, and the zinc content was 24.2%.

[0060] Copper-lead-zinc mixed concentrate was added to activated carbon at a rate of 1100 g / t feed, and then ground for 3 minutes to achieve a fineness of -0.074 mm (78%). The concentrate was then concentrated and dewatered to a pulp concentration of 50%. Fresh water was added to bring the pulp concentration to 35%. Sulfuric acid was added to adjust the pulp pH to 1.5 ± 0.1, and the mixture was stirred for 10 minutes. As the stirring time increased, the pulp pH also increased, eventually reaching 3.7 ± 0.1. Finally, sodium humate (1300 g / t feed) was added as an inhibitor. Frothing agent No. 2 oil (20g / t) was used for roughing to obtain roughing froth and roughing underflow products. The roughing froth product underwent three cleaning operations, with 100g / t of sodium humate inhibitor and 50g / t of sodium hexametaphosphate added in batches during each cleaning operation. The froth product from the third cleaning operation was copper concentrate. The roughing underflow product underwent two scavenging operations, with 10g / t of frother No. 2 oil added in batches during each scavenging operation. The underflow product from the second scavenging operation was a lead-zinc mixed concentrate. The copper concentrate contained 21.65% copper, 10.12% lead, and 10.2% zinc, with a copper recovery rate of 90.74%. The lead-zinc mixed concentrate contained 1.36% copper, 16.88% lead, and 32.83% zinc, with lead and zinc recoveries of 73.01% and 83.92%, respectively.

[0061] Example 3 In Example 3, the copper-lead mixed concentrate contained 8.22% copper and 28.87% lead.

[0062] Activated carbon was added to a copper-lead mixed concentrate slurry with a slurry concentration of 30%, with an activated carbon content of 200 g / t of feed. The slurry was then ground for 5 minutes, and the fineness of the slurry was 83% of the particles being -0.074 mm. The pulp was then concentrated and dehydrated, resulting in a pulp concentration of 53%. Fresh water was added to bring the pulp concentration to 34%, and the pH was adjusted to 0.8±0.1. The pulp was stirred for 30 minutes, and as the stirring time increased, the pulp pH rose to 4.2±0.2. Then, 400 g / t of sodium sulfite inhibitor, 100 g / t of sodium pyrophosphate, and 16 g / t of No. 2 frother were added to the pulp for roughing, yielding roughing froth product and roughing underflow product. The roughing froth product underwent two cleaning operations, with 40 g / t of sodium sulfite inhibitor and 10 g / t of sodium pyrophosphate added in batches during each cleaning operation. The froth product from the second cleaning operation was copper concentrate. The roughing underflow product underwent one scavenging operation, with 4 g / t of No. 2 frother added in each scavenging operation. The underflow product from the scavenging operation was lead concentrate. The copper concentrate contains 23.02% copper and 7.69% lead, with a copper recovery rate of 90.36%; the lead concentrate contains 1.17% copper and 38.96% lead, with a lead recovery rate of 91.41%.

[0063] Comparative Example 1 The difference between Comparative Example 1 and Example 1 is that sulfuric acid was added to adjust the pH of the slurry to 0.4 ± 0.1, and the mixture was stirred for 10 minutes. As the stirring time increased, the pH of the slurry rose to 2.5 ± 0.2. Everything else was the same as in Example 1.

[0064] In Comparative Example 1, the copper concentrate contained 23.43% copper, 9.12% lead, and 9.65% zinc, with a copper recovery rate of 67.25%. The lead-zinc mixed concentrate contained 4.28% copper, 17.20% lead, and 30.75% zinc, with lead and zinc recoveries of 83.42% and 89.47%, respectively.

[0065] The copper recovery rate of Comparative Example 1 was significantly lower than that of Examples 1-3, which may be due to the low pH of the slurry in Comparative Example 1 before stirring.

[0066] Comparative Example 2 The difference between Comparative Example 2 and Example 1 is that sulfuric acid was added to adjust the pH of the slurry to 4.5 ± 0.1, and the mixture was stirred for 10 minutes. As the stirring time increased, the pH of the slurry rose to 6.6 ± 0.2. Everything else was the same as in Example 1.

[0067] In Comparative Example 2, the copper concentrate contained 19.53% copper, 10.97% lead, and 10.97% zinc, with a copper recovery rate of 86.73%; the lead-zinc mixed concentrate contained 1.88% copper, 17.79% lead, and 35.65% zinc, with lead and zinc recoveries of 67.40% and 81.06%, respectively.

[0068] The lead recovery rate of Comparative Example 2 was significantly lower than that of Examples 1-3, and the zinc recovery rate of Comparative Example 2 was significantly lower than that of Examples 1-2. This may be due to the excessively high pH of the slurry after stirring in Comparative Example 2.

[0069] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of this application, and are not intended to limit them. Although this application has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still 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. Such 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 this application.

[0070] Furthermore, those skilled in the art will understand that although some embodiments herein include certain features included in other embodiments but not others, combinations of features from different embodiments are intended to be within the scope of this application and form different embodiments. For example, in the foregoing claims, any of the claimed embodiments can be used in any combination. The information disclosed in this background section is intended only to enhance the understanding of the general background of this application and should not be construed as an admission or in any way implying that such information constitutes prior art known to those skilled in the art.

Claims

1. A method for flotation separation of copper-lead mixed concentrate, characterized in that, include: The copper-lead mixed concentrate is ground, and activated carbon is added during the grinding process. Then it is concentrated to obtain a concentrated slurry. Water is added to the concentrated slurry to obtain a slurry containing a copper-lead mixed concentrate; An acidic substance is added to the slurry containing the copper-lead mixed concentrate, and the mixture is stirred to adjust the pH of the slurry to 0.5-4.

5. Subsequently, an inhibitor and a frother are added, and flotation separation is carried out to obtain copper concentrate and lead concentrate.

2. The method for flotation separation of copper-lead mixed concentrate according to claim 1, characterized in that, The copper-lead mixed concentrate includes at least one of copper-lead mixed concentrate and copper-lead-zinc mixed concentrate; The copper-lead mixed concentrate contains 8-10 wt% copper and 14-30 wt% lead.

3. The method for flotation separation of copper-lead mixed concentrate according to claim 2, characterized in that, The copper-lead mixed concentrate also includes zinc, and the zinc content in the copper-lead mixed concentrate is 23-25 ​​wt%.

4. The method for flotation separation of copper-lead mixed concentrate according to claim 1, characterized in that, The fineness of the grinding process is such that 75%-95% of the particles are of -0.074mm size. The amount of activated carbon used is 200-1100 g / t of ore; The concentration of the slurry containing the copper-lead mixed concentrate is 10%-40%.

5. The method for flotation separation of copper-lead mixed concentrate according to claim 1, characterized in that, The acidic substance includes at least one organic acid and an inorganic acid; The organic acid includes at least one of acetic acid, oxalic acid, and citric acid; The inorganic acid includes at least one of hydrochloric acid, sulfuric acid, nitric acid, phosphoric acid, and silicic acid; And / or, after adding acidic substances, stir for 3-60 minutes.

6. The method for flotation separation of copper-lead mixed concentrate according to claim 1, characterized in that, The inhibitors include at least one of the following: organic acid inhibitors, cellulose inhibitors, silicate inhibitors, humic acid inhibitors, sulfur-containing inhibitors, phosphorus-containing inhibitors, starch, and dextrin. The organic acid inhibitors include at least one of oxalic acid and citric acid; The cellulose inhibitors include carboxymethyl cellulose; The silicate inhibitors include water glass; The humic acid inhibitors include at least one of humic acid and sodium humate. The sulfur-containing inhibitor includes at least one of sodium sulfide, sulfur dioxide, sulfurous acid, and sulfite; The phosphorus-containing inhibitor includes at least one of sodium pyrophosphate, sodium dithiophosphate, and sodium hexametaphosphate.

7. The method for flotation separation of copper-lead mixed concentrate according to claim 6, characterized in that, The dosage of the inhibitor is 500-1500 g / t of ore feed.

8. The method for flotation separation of copper-lead mixed concentrate according to claim 1, characterized in that, The foaming agent includes at least one of pine oil, pine alcohol oil, camphor oil, eucalyptus oil, ether alcohol foaming agents, and ether foaming agents.

9. The method for flotation separation of copper-lead mixed concentrate according to claim 8, characterized in that, The amount of the foaming agent used is 14-100g / t of feed.

10. The method for flotation separation of copper-lead mixed concentrate according to any one of claims 1-9, characterized in that, The flotation separation includes adding 500-1500 g / t of depressant and 14-100 g / t of frother to a slurry with a pH of 0.5-4.5 for roughing to obtain a roughing froth product and a roughing underflow product; performing at least one cleaning operation on the roughing froth product, adding 20-150 g / t of depressant to the slurry in each cleaning operation, with the froth product from the final cleaning operation being copper concentrate; and performing at least one scavenging operation on the roughing underflow product, adding 4-20 g / t of frother to the scavenging operation, with the underflow product from the final scavenging operation being lead concentrate.

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