RU2343987C1 - Method of floatation dressing of current tailings obtained by flushing of polymetallic or copper-zinc sulfide ores - Google Patents

Abstract

FIELD: technological processes.

SUBSTANCE: invention concerns mineral materials dressing and can be applied in tailings processing in current production of impregnated polymetallic or copper-zinc sulfide ores. Floatation dressing method for current tailings obtained by flushing of polymetallic or copper-zinc sulfide ores involves main and reference copper-lead or copper floatation in the presence of isopropylethylthiocarbamate, ammonium dibuthyldithiophosphate and methylisobuthylcarbinol foaming agent, collective concentrate desorption in the presence of sodium sulfite and activated carbon. Re-treatment cycle of foamed product after desorption resulting in obtaining collective copper-zinc or copper concentrate involves main copper-lead floatation or copper and copper-lead or copper refloatation with addition of modifying agent consisting of cyanide, zinc sulfate and carboxymethylcellulose mix at the operation ratio of 2:4÷5: 20÷30 and post-operation ratio of 3÷5:1; 3÷5:1; 3÷5:1 respectively. Also the method involves zinc cycle of chamber product in the presence of lime, liquid glass and copper sulfate to obtain commercial zinc concentrate.

EFFECT: enhanced efficiency of floatation.

3 cl, 3 dwg, 3 tbl, 5 ex

Description

The invention relates to mineral processing and can be used as in the processing of sludge from the current production of sulphide disseminated and solid polymetallic and copper-zinc ores.

The problem of the extraction of non-ferrous metals from sludges of the current production of sulfide polymetallic ores is very urgent due to the high contents of sludge fractions in the processed ores. The technical problems of processing sludge from sulphide polymetallic and copper-zinc ores are well known and include the following: non-selective aggregation, increased oxidizability, high mechanical removal into the foam product, huge specific surface area and, as a result, a multiple increase in the consumption of flotation reagents, etc. The listed features do not allow to process slimes of polymetallic and copper-zinc ores according to traditional schemes and reagent formulations.

Known methods for flotation of sulfide polymetallic ores with the suppression of sphalerite by zinc sulfate and cyanide (AS USSR No. 107921, CL. B03D 1/02, 1950); water-soluble cyanide and zinc sulfate (US patent No. 26660307, CL 209-187, 1952). However, when flotation according to known methods, the extraction of zinc into the final concentrate from sludge from sulphide polymetallic ores does not exceed 40% at its substandard content (not more than 45-50%).

The closest in technical essence and the achieved result to the proposed one is a method of flotation dressing of sludges obtained by washing sulfide polymetallic and copper-zinc ores, including the main and control flotations in the presence of isopropylethylthiocarbamate and ammonium dibutyl dithiophosphate (Kakovsky I.A. et al. 1961, No. 8).

The disadvantage of this method is that the extraction of zinc in the concentrate of the same name from the sludge of the current extraction of sulfide polymetallic or copper-zinc ores does not exceed 45-50%, and when processing sludge from mining and processing polymetallic plants, the use of this method is worsened due to increased oxidation of the material.

The technical goal of this technical solution is to increase the efficiency and selectivity of the flotation process of the current sludge obtained by washing sulphide polymetallic or copper-zinc ores by increasing the extraction of copper and lead into a collective concentrate (or copper into the same name when processing copper-zinc ores), and zinc in the concentrate of the same name with a simultaneous increase in its quality to marketable.

This goal is achieved by the fact that in the flotation enrichment method for sludges obtained by washing sulfide polymetallic or copper-zinc ores, which includes the main and control copper-lead or copper flotations in the presence of isopropylethylthiocarbamate, ammonium dibutyl dithiophosphate and a sodium nitrite blowing agent, MIB and activated carbon, recycle cycle of the foam product after desorption to obtain a collective copper-lead or copper concentrate, including the main copper-lead flotation, or copper and copper-lead, or copper doflotation with the introduction of a modifier consisting of a mixture of cyanide, zinc sulfate and carboxymethyl cellulose with an operating ratio of 2: 4 ÷ 5: 20 ÷ 30 and an operational ratio of 3 ÷ 5: 1 ; 3 ÷ 5: 1; 3 ÷ 5: 1, respectively, and the zinc cycle of the chamber product in the presence of lime, water glass and copper sulphate to produce marketable zinc concentrate.

As the feedstock, current sludge obtained by washing disseminated sulfide polymetallic or copper-zinc ores processed by the collective scheme can be used.

Sludges obtained by washing solid polymetallic or copper-zinc ores processed according to a collective selective scheme can be used as feedstock.

The proposed method of flotation concentration of sludge obtained by washing sulfide polymetallic or copper-zinc ores is based on increasing flotation selectivity in the cycle of primary and control copper-lead flotation and a sharp decrease in metal loss.

Figure 1 shows a flow chart of a method of flotation concentration of sludges obtained by washing disseminated sulfide polymetallic or copper-zinc ores.

Figure 2 shows a flow diagram of a method of flotation concentration of sludges obtained by washing solid sulfide polymetallic or copper-zinc ores.

Figure 3 shows a flow chart of a method of flotation concentration of sludges obtained by washing copper-zinc ores.

The method is as follows.

The feed - slurries of the current production of sulphide disseminated polymetallic or copper-zinc ores of one of the ore dressing enterprises with a size of 90 ÷ 100% of a class of 44 μm - goes to the collective main and control flotations, which are carried out in the presence of collectors of isopropylethylthiocarbamate (15 ÷ 50 g / t ); dibutyl dithiophosphate (30 ÷ 80 g / t); MIBK blowing agent (1 ÷ 5 g / t). Foam product after desorption in the presence of sodium sulfide (0.5 ÷ 1.5 g / t) and activated carbon (2 ÷ 10 g / t) enters the main copper-lead flotation and copper-lead doflotation with the introduction of a mixture of cyanide, zinc sulfate and carboxymethyl cellulose with an operating ratio of 2: 4 ÷ 5: 20 ÷ 30 and an operational ratio of 3 ÷ 5: 1; 3 ÷ 5: 1; 3 ÷ 5: 1, respectively.

The initial feed is the sludge obtained by washing solid pyritic polymetallic ores. The processing of the rock mass is carried out according to a collective selective scheme with the removal of collective copper-lead concentrate into foam products, and the chamber product enters the standard zinc cycle with the introduction of lime, liquid glass and copper sulphate as modifiers to produce marketable zinc concentrate.

The feed is sludge obtained by washing copper-zinc ores. The processing of rock mass is carried out according to the above schemes for disseminated and solid polymetallic ores. The difference lies in the fact that the foam product does not produce a collective copper-lead concentrate, but not directly a crude copper concentrate, zinc concentrate is obtained according to the usual scheme from a chamber product of the copper cycle.

As the results showed, only such a combination of reagents and their ratio allows you to effectively depress zinc minerals while effectively isolating copper and lead minerals in the foam product. The chamber product enters the standard zinc cycle with the supply of reagents: lime, water glass and copper sulphate as modifiers to produce commercial zinc concentrate.

The method is illustrated by examples of specific implementation.

Permanent conditions:

Agitation Isopropylethylthiocarbamate 25 g / t Primary collective MIBK 1 g / t Control flotation Dibutyl dithiophosphate 100 g / t Main Zn Flotation CaO 1000 g / t CuSO ₄ 75 g / t Zh.st. 100 g / t

1. Initial feed - sulphide disseminated sludge

polymetallic ores

Example 1 (by the method of the prototype).

The feed - sludge disseminated sulfide polymetallic ores are subjected to flotation processing according to the scheme of figure 1 with a reagent regime, given under constant conditions (see above) and in the table.

Example 2 (by the proposed method).

The feed - sludge disseminated sulfide polymetallic ores are subjected to flotation processing according to the scheme of figure 1 with a reagent regime, given under constant conditions. In operations of copper-lead primary and copper-lead doflotation, a mixture of cyanide, zinc sulfate and carboxymethyl cellulose is introduced at an operating ratio of 2: 4: 20 and an operational ratio of 3: 1; 3: 1; 3: 1 respectively.

Example 3 (by the proposed method).

The feed - sludge disseminated sulfide polymetallic ores are subjected to flotation processing according to the scheme of figure 1 with a reagent regime, given under constant conditions. In operations of copper-lead basic and copper-lead doflotation, a mixture of cyanide, zinc sulfate and carboxymethyl cellulose is introduced at an operating ratio of 2: 5: 20 and an operational ratio of 3: 1; 3: 1; 4: 1 respectively.

Example 4 (by the proposed method).

The feed - sludge disseminated sulfide polymetallic ores are subjected to flotation processing according to the scheme of figure 1 with a reagent regime, given under constant conditions. In operations of copper-lead primary and copper-lead doflotation, a mixture of cyanide, zinc sulfate and carboxymethyl cellulose is introduced at an operating ratio of 1: 5: 30 and an operational ratio of 5: 1; 5: 1; 5: 1 respectively.

II. Initial nutrition - sludges of continuous sulfide polymetallic ores

Example 1 (by the method of the prototype).

The feed - sludges of continuous sulfide polymetallic ores are subjected to flotation processing according to the scheme of figure 2 with a reagent regime shown in constant conditions and in table.2.

Example 2 (by the proposed method).

The feed - sludge solid sulfide polymetallic ores are subjected to flotation processing according to the scheme of figure 2 with a reagent regime, given under constant conditions. In operations of copper-lead primary and copper-lead doflotation, a mixture of cyanide, zinc sulfate and carboxymethyl cellulose is introduced at an operating ratio of 2: 4: 25 and an operational ratio of 4: 1; 4: 1; 4: 1 respectively.

Example 3 (by the proposed method).

The feed - sludge solid sulfide polymetallic ores are subjected to flotation processing according to the scheme of figure 2 with a reagent regime, given under constant conditions. In operations of copper-lead basic and copper-lead doflotation, a mixture of cyanide, zinc sulfate and carboxymethyl cellulose is introduced at an operating ratio of 2: 5: 20 and an operational ratio of 3: 1; 3: 1; 4: 1 respectively.

Example 4 (by the proposed method).

The feed - sludge solid sulfide polymetallic ores are subjected to flotation processing according to the scheme of figure 2 with a reagent regime, given under constant conditions. In operations of copper-lead primary and copper-lead doflotation, a mixture of cyanide, zinc sulfate and carboxymethyl cellulose is introduced at an operating ratio of 1: 5: 30 and an operational ratio of 2: 1; 3: 1; 4: 1 respectively.

Example 5 (by the proposed method).

The feed - sludge solid sulfide polymetallic ores are subjected to flotation processing according to the scheme of figure 2 with a reagent regime, given under constant conditions. In operations of copper-lead primary and copper-lead doflotation, a mixture of cyanide, zinc sulfate and carboxymethyl cellulose is introduced at an operating ratio of 2: 4: 20 and an operational ratio of 5: 1; 3: 1; 3: 1 respectively.

III. The original feed is the slime of copper-zinc ores

Sludges of copper-zinc ores are subjected to flotation processing according to the scheme of Fig. 3 with a reagent regime given under constant conditions.

Example 1 (by the method of the prototype).

The feed - sludges of copper-zinc ores are subjected to flotation processing according to the scheme of figure 3 with a reagent regime shown in constant conditions and in table.3.

Example 2 (by the proposed method).

The feed - the slime of copper-zinc ores is subjected to flotation processing according to the scheme of figure 3 with a reagent regime, given in constant conditions. In copper operations, a mixture of cyanide, zinc sulfate and carboxymethyl cellulose is introduced at an operating ratio of 2: 4: 30 and an operational ratio of 3: 1; 3: 1; 4: 1 respectively.

Example 3 (by the proposed method).

The feed - the slime of copper-zinc ores is subjected to flotation processing according to the scheme of figure 3 with a reagent regime, given in constant conditions. In copper flotation operations, a mixture of cyanide, zinc sulfate and carboxymethyl cellulose is introduced at an operating ratio of 1: 5: 20 and an operational ratio of 5: 1; 4: 1; 4: 1 respectively.

Example 4 (by the proposed method).

The feed - the slime of copper-zinc ores is subjected to flotation processing according to the scheme of figure 3 with a reagent regime, given in constant conditions. In copper flotation operations, a mixture of cyanide, zinc sulfate and carboxymethyl cellulose is introduced at an operating ratio of 2: 4: 20 and an operational ratio of 3: 1; 3: 1; 5: 1 respectively.

Example 5 (by the proposed method).

The feed - the slime of copper-zinc ores is subjected to flotation processing according to the scheme of figure 3 with a reagent regime, given in constant conditions. In copper flotation operations, a mixture of cyanide, zinc sulfate and carboxymethyl cellulose is introduced at an operating ratio of 2: 4: 25 and an operational ratio of 4: 1; 4: 1; 5: 1 respectively.

As the studies showed, only such a combination of flotation operations and the corresponding reagent modes allows the selection of copper and zinc minerals. When processing according to these schemes, rough zinc concentrates with a zinc content of at least 40% and a copper concentrate suitable for attaching to the technological products of the ordinary ore processing scheme are obtained.

Thus, in order to increase the efficiency and selectivity of the flotation processing of sludge from the current extraction of copper-zinc ores from mining and processing enterprises, it is necessary to simultaneously use flotation processing units: basic copper-lead and doflotation in optimal conditions with the introduction of a mixture of cyanide, zinc sulfate and carboxymethyl cellulose at an operating ratio 2: 4 ÷ 5: 20 ÷ 30 and the operational ratio of 3 ÷ 5: 1; 3 ÷ 5: 1; 3 ÷ 5: 1, respectively.

Summary indicators of flotation processing of sludge from the current production of sulfide polymetallic or copper-zinc ores clearly showed that the use of the proposed method in comparison with the prototype allows you to:

- increase the extraction of zinc in the concentrate of the same name by 10 ÷ 15%, while the quality of the obtained zinc concentrate is not lower than 53%, i.e. to the quality of commodity concentrate;

- to obtain a collective copper-lead concentrate with copper extraction from 80 to 92%, suitable for joining the washed ore ore flotation scheme to technological products;

- to increase the efficiency and selectivity of the flotation process of current sludge obtained by washing sulfide polymetallic or copper-zinc ores.

Table 1 The results of experiments on a collective scheme for processing sludges of the current production of disseminated sulfide polymetallic ore No pp Product Name Exit, % Cu Pb Zn Test conditions * β ε β ε β ε one Collective Cu-Pb con-t 4.11 3,50 38.91 8.60 41.62 7.10 9.97 According to the prototype
Consumption of butyl xanthonate 200 g / t
Soda 6000 g / t
MIBK 160 g / t
1: 30 ratio: 0.8 Zn concentrate 4.80 1.80 23.34 1.80 10.16 47.20 77.29 Tails 91.09 0.10 37.75 0.45 48.22 0.41 12.75 Source 100.00 0.37 100.00 0.85 100.00 2.93 100.00 2 Collective Cu-Pb con-t 3.63 8.80 77.94 12.09 56.28 4.60 5.64 According to the proposed method (example 1) cyanide: ZnSO ₄ : carboxymethyl cellulose in the operation ratio of 2: 4: 20 and the operational ratio of 3: 1; 3: 1; 3: 1 respectively Zn concentrate 4.66 0.90 10.23 1,61 9.62 53.83 84.75 Tails 91.71 0.09 11.83 0.29 34.10 0.31 9.60 Source 100.00 0.41 100.00 0.78 100.00 2.96 100.00 3 Collective Cu-Pb con-t 3.61 8.65 74.37 11.59 51.04 4.40 5.18 According to the proposed method (example 2) cyanide: ZnSO ₄ : carboxymethyl cellulose in operation, the ratio of 2: 5: 20, the operational ratio of 3: 1; 3: 1; 4: 1 respectively Zn concentrate 4.91 1.65 19.30 2.40 14.38 53.10 84,99 Tails 91.48 0.09 6.33 0.31 34.58 0.33 9.83 Source one hundred 0.42 one hundred 0.82 one hundred 3.07 one hundred four Collective Cu-Pb con-t 2.82 10.30 67.52 14.02 48.19 5.20 4.92 According to the proposed method (example 3) cyanide: ZnSO ₄ : carboxymethyl cellulose in operation, the ratio of 1: 5: 30, the operational ratio of 5: 1; 5: 1; 5: 1 respectively Zn concentrate 4,55 1.36 14.40 2.21 12.27 55.31 84.51 Tails 92.63 0.05 18.08 0.35 39.54 0.34 10.57 Source one hundred 0.43 one hundred 0.82 one hundred 2.98 one hundred 5 Collective Cu-Pb con-t 3.20 9.20 65.51 13.87 53.55 5.43 5.90 According to the proposed method (example 4) cyanide: ZnSO ₄ : carboxymethyl cellulose in the operation ratio of 1: 2: 30; operational ratio 5: 1; 5: 1; 5: 1 respectively Zn concentrate 4,59 0.10 1,02 1.97 10.90 54.01 84.10 Tails 92.20 0.08 33.47 0.32 35.55 0.32 10.00 Source 100.00 0.45 100.00 0.83 100.00 2.95 100.00

table 2 The results of experiments on a collective scheme for processing slurries of the current extraction of solid pyritic polymetallic ore No pp Product Name Exit, % Cu Pb Zn Test conditions β ε β ε β ε one Collective Cu-Pb con-t 24.9 14.03 92.1 18.11 91.4 14.23 28.8 According to the prototype
Consumption of butyl, xanthonate 200 g / t
Soda 6000 g / t
MIBK 160 g / t
1: 30 ratio: 0.8 Zn concentrate 14.7 0.41 1,6 0.16 0.7 56.2 67.9 Tails 60,4 0.40 6.36 0.46 3.25 0.65 7.93 Source 100.0 3.82 100.0 3.53 100.0 12.14 100.0 2 Collective Cu-Pb con-t 18.88 18.5 90.5 17.3 91.5 8.2 12.7 According to the proposed method (example 1) cyanide: ZnSO ₄ : carboxymethyl cellulose in the operation ratio of 2: 4: 25; operational ratio 4: 1; 4: 1; 4: 1 respectively Zn concentrate 19.29 0.62 3,1 0.23 1,2 53.20 84.0 Tails 61.83 0.43 6.41 0.42 3.29 0.67 7.26 Source 100.0 3.86 100.0 3.57 100.0 12.21 100.0 3 Collective Cu-Pb con-t 15.65 21.9 90.2 19.0 84.0 6.5 8.4 According to the proposed method (example 2) cyanide: ZnSO ₄ : carboxymethyl cellulose in operation ratio of 1: 5: 30; operational ratio 3: 1; 4: 1; 5: 1 respectively Zn concentrate 17.46 0.6 2,8 0.48 2,4 60.8 88.0 Tails 66.88 0.40 7.04 0.65 13.63 0.72 3.60 Source 100.0 3.78 100.0 3.56 100.0 12.07 100.0 four Collective Cu-Pb con-t 14.72 22.5 87.1 21,4 84.8 5,0 6.1 According to the proposed method (example 3) cyanide: ZnSO ₄ : carboxymethyl cellulose in the operation ratio of 1: 6: 20; operational ratio 3: 1; 3: 1; 4: 1 respectively Zn concentrate 18,42 1.20 5.8 1.3 6.8 59.60 90,4 Tails 66.86 0.40 7.1 0.45 8.42 0.65 3,58 Source 100.0 3.80 100.0 3,54 100.0 12.15 100.0 5 Collective Cu-Pb con-t 25.66 13.00 87.8 12.00 88.2 13,2 27.9 According to the proposed method (example 4) cyanide: ZnSO ₄ : carboxymethyl cellulose in the operation ratio of 2: 4: 20; an operational ratio of 5: 1; 3: 1; 3: 1 respectively Zn concentrate 16.72 1.40 6.2 1,57 7.2 50.06 69.0 Tails 57.63 0.40 6.07 0.65 4,59 0.28 3.09 Source 100.0 3.80 100.0 3.49 100.0 12.12 100.0

Table 3 The results of experiments on a collective scheme for processing sludges of the current extraction of copper-zinc ore No pp Product Name Exit, % Pb Cu Zn Test conditions * β ε β ε β ε one Cu con 33.31 1.33 85.19 14.20 84.45 8.30 42.40 According to the prototype
Consumption of butyl, xanthonate 200 g / t
Soda 6000 g / t
MIBK 160 g / t
1: 30 ratio: 0.8 Zn concentrate 10.21 0.42 8.24 4.60 8.38 33,20 51.97 Tails 56.49 0.26 6.57 0.71 7.16 0.65 5.63 Source 100.00 0.52 100.00 5.60 100.00 6.52 100.00 2 Cu con 30.70 1,50 85.26 16.70 89.93 6.40 30.89 According to the proposed method (example 1) cyanide: ZnSO ₄ : carboxymethyl cellulose in the operation ratio of 2: 4: 30; operational ratio 3: 1; 3: 1; 4: 1 respectively Zn concentrate 10.10 0.42 7.85 2.40 4.25 40.30 63,99 Tails 59.21 0.21 6.88 0.56 5.82 0.55 5.12 Source 100.00 0.54 100.00 5.70 100.00 6.36 100.00 3 Cu con 28.41 1.45 74.90 17.10 91.31 7.90 35.97 According to the proposed method (example 2) cyanide: ZnSO ₄ : carboxymethyl cellulose in operation, the ratio of 1: 5: 20; operational ratio 5: 1; 4: 1; 4: 1 respectively Zn concentrate 8.71 0.48 7.61 2.20 3.60 42.10 58.79 Tails 62.88 0.22 17.50 0.43 5.08 0.52 5.24 Source 100.00 0.55 100.00 5.32 100.00 6.24 100.00 four Cu con 29.87 1.12 63.13 17.00 90.69 8.50 38.95 According to the proposed method (example 3) cyanide: ZnSO ₄ : carboxymethyl cellulose in operation, the ratio of 2: 4: 20, the operational ratio of 3: 1; 3: 1; 5: 1 respectively Zn concentrate 8.47 0.42 6.71 2,30 3.48 42,20 54.81 Tails 61.66 0.19 30.16 0.53 5.84 0.66 6.24 Source 100.00 0.53 100.00 5.60 100.00 6.52 100.00 5 Cu con 29.06 1.18 64.71 17.50 90.82 7.30 33.57 According to the proposed method (example 4) cyanide: ZnSO ₄ : carboxymethyl cellulose in the operation ratio of 2: 4: 25; operational ratio 4: 1; 4: 1; 4: 1 respectively Zn concentrate 8.45 0.53 8.45 2.90 4.38 45.00 60,20 Tails 62.48 0.20 26.84 0.43 4.80 0.63 6.23 Source 100.00 0.53 100.00 5.60 100.00 6.32 100.00

Claims (3)

1. A method of flotation concentration of current sludge obtained by washing sulphide polymetallic or copper-zinc ores, including the main and control copper-lead or copper flotation in the presence of isopropylethylthiocarbamate, ammonium dibutyl dithiophosphate and MIBK blowing agent, collective sulfur desorption and collective sulfur desorption after-desorption foam product cycle to produce a collective copper-lead or copper concentrate, including a basic copper-lead flotation or copper and copper-lead or copper doflotation with the introduction of a modifier consisting of a mixture of cyanide, zinc sulfate and carboxymethyl cellulose with an operating ratio of 2: 4 ÷ 5: 20 ÷ 30 and an operational ratio of 3 ÷ 5: 1; 3 ÷ 5: 1; 3 ÷ 5: 1, respectively, and the zinc cycle of the chamber product, in the presence of lime, water glass and copper sulphate to produce marketable zinc concentrate. 2. The method according to claim 1, characterized in that the current sludge obtained by washing the disseminated sulfide polymetallic or copper-zinc ores processed by the collective scheme is used as the feedstock. 3. The method according to claim 1, characterized in that the current sludge obtained by washing solid sulphide polymetallic or copper-zinc ores processed according to the collective ore scheme is used as feedstock.

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