Reprocessing method of copper concentrate from foam separation of nis matte

FIELD: metallurgy.

SUBSTANCE: method includes oxidising roasting, copper cinder leaching in circulating electrolyte, compartment of leaching residual, electroextraction of copper from leaching solution. At that leaching residual in the form of thickened underflow is effected to foam separation with concentrate extraction of precious metals, and chambered product, containing in preference nonferrous materials. Chambered product is reprocessed for secondary nis matte. Electrolyte part after copper electroextraction is separated and effected to evaporation till concentration of sulfuric acid 250-300 g/l, copper vitriol is extracted from it by crystallisation, and sulfuric acid by extraction and it is returned to leaching of copper cinder. Raffinate after acid extraction, containing nickel in preference, is directed to nickel manufacturing. Concentrate of precious metals is directed to refining.

EFFECT: reduction of expenditure of energy and material cost and increasing of receiving materials extraction.

1 dwg, 1 tbl, 1 ex

 

The invention relates to the field of non-ferrous metallurgy and can be used for complex processing of copper-containing materials, in particular copper concentrate obtained from the flotation separation of copper-Nickel matte.

A method of refining copper sulfide ores and/or concentrates (Patent No. 2173726, SW 15/00, SW B1/06, publ. 20.09.2001), including their sulfamethizole firing in an inert gas environment, leaching the calcine acidic aqueous solution and the recovery of copper from solution. The ground raw material is calcined in a tubular furnace in a stream of nitrogen at a temperature of 850-950°that makes it possible to remove the sulfur from the ore and/or concentrate during firing, to increase the degree of extraction of copper by leaching.

A method of refining copper-bearing materials (Ed. the certificate №1301858, MKI SU 1/06, publ. 07.04.87, bull. No. 13), including sulfamethizole firing in an inert atmosphere mixed with sulphate of iron, with subsequent leaching of the calcine acidic aqueous solution, the recovery of copper from solution.

The disadvantage of this method is significant energy costs in the preparation of copper raw materials for subsequent leaching. In addition, significant costs are required when removing additional useful components contained in copper concentrates, primarily dragon is the R metals, Nickel or zinc.

The closest technical solution is selected as a prototype method for processing copper sulfide concentrates containing Nickel, cobalt and iron (RF Patent No. 2171856, SW 15/00, publ. 10.08.2001), including the two-stage leaching of copper concentrate. In the first stage leaching carry out a copper sulfate solution containing chlorine ion in an amount of 0.02-2.5 g/l at a temperature of at least 60°C. Before the second stage of leaching cemented subjected to desulfurization oxygen-containing gas at a temperature of 800-1300°and get refined from sulfur product, which is then dissolved at atmospheric pressure in sulfuric acid solutions or purge hydrocarbon fuel.

Moreover, when the temperature desulfurization 800-1100°get the copper oxide (calcine), which is then dissolved in sulfuric acid solutions under atmospheric pressure before the formation of sulphate of copper solution and the insoluble residue is a precious metals concentrate. When the temperature desulfurization 1150-1300°get a copper alloy, which is blown hydrocarbon fuel to the formation of the anode refined copper.

The disadvantages of this method include the following.

The organization of preliminary refining of the total volume of copper concentrate leads to great is m costs for the implementation of the process of leaching and filtration products. Conducting pre-leaching at a temperature of 60°s and 90°as shown in the examples, provides a low Nickel recovery 52% 72,5%, respectively, as well as iron 48% and 58.7%. The process under these conditions does not allow to get in the second stage leaching of the calcine concentrate precious metals without additional processing operations. A high degree of extraction of Nickel and iron, with which it is possible to obtain a rich concentrate of precious metals, can only be achieved at a temperature of 160°C. the Organization of the process under these conditions further increases the cost of the organization of the leaching process and requires expensive equipment needed to work in a hostile environment.

The present invention is directed to the development of a method for integrated processing of copper concentrate with selective extraction of non-ferrous and precious metals.

The technical result from the use of the invention is the reduction of energy and material costs and improving the extraction of the produced metals.

The essence of the invention.

A method for processing copper concentrate from the flotation separation area, including oxidative roasting of copper concentrate leaching of copper calcine in the circulating electrolyte from the bookmark residue leaching, electroextraction of copper from leaching solutions. Unlike the prototype in the inventive method, the residue leaching in the form of a thickened slurry is subjected to flotation separation with separation of precious metals concentrate chamber and a product that contains mainly non-ferrous metals, which are processed to produce secondary Feinstein; part of the electrolyte before the extraction of copper is separated and subjected to evaporation to a concentration of sulfuric acid 250-300 g/l, separated from her copper sulphate crystallization and sulfuric acid extraction and return them to the leaching of copper calcine, after extraction raffinate acid containing mainly Nickel, is directed to the production of Nickel, and precious metals concentrate sent to the refinery production.

Oxidative roasting of copper concentrate provides the minimum transition in a solution of iron and Nickel in the leach process of circulating the electrolyte, while undesirable impurities, primarily iron, remain in the residue of the leaching.

Flotation separation of the thickened pulp leaching provides selective isolation from the rest of the leaching of precious metals concentrate suitable for further processing. In this chamber the product flotation contains mainly the oxides of Nickel and iron and insignificant the number of copper and precious metals. Pyrometallurgical processing chamber product of sulfide copper-Nickel raw material melting at Stein with its subsequent conversion allows you to effectively separate the iron and get sulfide copper-Nickel matte is the feedstock for the production of cathode Nickel and copper.

The cut-off part of the electrolyte and the special processing is performed with the purpose of the output generated in the circuit electroextraction Nickel and impurities. Due to the cutoff part of the electrolyte provides optimal composition according to the content of trace contaminants that allows electroextraction copper with the lowest cost of electricity. Evaporation of part of the electrolyte and crystallization of copper sulphate gives a return of the principal amount of copper from the electrolyte compartment in the scheme of primary copper production. Evaporation is conducted until the concentration of sulfuric acid 250-300 g/L. the Specified interval is optimal for obtaining the sulphate of satisfactory quality with a minimum content of Nickel and iron. In the process of evaporation of the electrolyte to the acid concentration of less than 250 g/l extract copper sulphate significantly reduced, which makes it difficult to use this process for removing copper from a shut-off solution. When the degree of evaporation of the solution more than 300 g/l increases izvicinaties in sulphate, which leads to the need to increase the cutoff of the electrolyte and increase the cost of its processing.

Extraction the extraction of sulfuric acid from the mother liquor and its use in the leaching of copper calcine will reduce the amount of sulfuric acid. Extraction of the acid get Nickel raffinate with a slight acid content, which allows processing it on the post production of cathode Nickel.

Schematic diagram of processing of copper concentrate from the separation area is shown in the drawing.

The implementation of the invention.

Copper concentrate from the flotation separation area containing 69% copper, 21.5 percent sulfur and 0.02% silver (the rest is Nickel, cobalt, iron, and others), is burned in a furnace of the fluidized bed area of 1.6 m2when the temperature in the firing material layer 900-950°With, to a residual content of sulfur in the calcine ˜0,1%, sulphur dioxide formed during the firing, used for the production of sulfuric acid. The resulting calcine composition: Nickel - 4%, copper - 68%, cobalt - 0,2%>, iron 4.5 percent, is directed to the leaching.

Leaching of the calcine is carried out in a circulating electrolyte electroextraction copper, consisting of: sulfuric acid 80-120 g/l, copper 35-40 g/l, Nickel 15-20 g/l, iron - up to 2.5 g/l, for 30-50 minutes at a temperature of 5-75° C. Next, the slurry leaching sent to the thickener. The clarified overflow thickener after final filtration is mixed with the main volume of electrolyte and sent to electroextraction copper.

Electroextraction copper is carried out in electrolytic baths with insoluble lead anodes. Food tubs provide electrolyte having a copper concentration of 40-50 g/l and the concentration of acids 105-115 g/l, obesogenic electrolyte contains 35-37 g/l copper and 115-125 acid. Options electroextraction copper the following: a current density of 250-270 a/m, the current output 86-89%, energy consumption 1850-1950 kWh/t of copper.

Of the poor electrolyte electroextraction of copper in 0.5-1 m3/t electrolytic copper output in the scheme of special processing. Shut the electrolyte evaporated 2-3 times until the concentration of sulfuric acid 250-300 g/l and then cooled to the crystallization of copper sulfate. Sulphate is separated from the mother liquor and transmit scheme leaching of the calcine.

Sulfuric acid from the mother liquor, from extraction of copper sulphate is extracted by the methods of solvent extraction. Extraction of the acid carry out a number of extractants such as tributyl phosphate, tertiary amines, higher alcohols, and mixtures thereof.

Reextraction acid is carried out with water, the resulting aqueous acid solution used for the leaching of the calcine pax is with the circulating electrolyte. The raffinate of extraction, containing dissolved during leaching of Nickel calcine, Refine the technology of production of Nickel. Below is an example in the table shows the results of tests carried out on the extraction of sulfuric acid from the mother solution after crystallization of copper sulfate.

The residue leaching, having the chemical composition: 24% Ni; 9,5% Cu, 35% Fe; 0,12% Ag; 1,7% S, Rasulova circulating electrolyte to the solid content ˜ 305 g/l, sulfuric acid ˜50 g/l and is directed to the separation of photomachine * rotor type (8 cameras, Iaboutby.=1,5m3). Aeration of the pulp produced by the air, for intensification of use flotation flotation reagents blowing agents, collectors, in particular potassium butyl xanthate. When the total time of flotation ˜40 minutes got the foam product of the following composition in %: Ni - 8; copper - 40; iron - 8; silver - 26. Removing the concentrate was %; Ag-94; Cu-22; S-74. In the froth product collectives to -90% precious metals contained mainly in the sulfide phase. In the pulp chamber of the product, basically, remove the iron oxide phase. The residual content of silver in the chamber product ˜0,01% indicates a full selection of silver in the precious metals concentrate.

Foam product (to Central precious metals) are sent to the refinery production, and chamber the product is separated from the solution by filtration and recycle fuse together with the sulfide copper-Nickel concentrates on Stein. A subsequent operation, the iron is transferred to the slag and produce copper-Nickel matte, which is the feedstock for production of electrolytic Nickel and copper.

Example.

Tests on the extraction of sulfuric acid from the mother solution after crystallization of copper sulfate composition in g/l: H2SO4- 305-370; Cu - 15-17; Ni - 40-42; Fe - 2.2-2.4, was performed on the pilot extraction cascade mixer settlers extractors. As extractant used a mixture containing in%: 30 - triallylamine (TAA) and 70 ISO-oktilovom alcohol (Di-2-ethylhexanol).

Extraction of acid from one stripped off and the filtered solutions was carried out at the following costs: water phase ˜350 l/h, organics ˜1200 l/h are Given in table the results clearly show a decrease in the quantity of sulfuric acid in Nickel solutions.

Thus, implementation of the proposed method of processing copper concentrate provides comprehensive extraction of non-ferrous and precious metals while reducing energy and material costs and provides better extraction of the produced metals.

The degree of extraction in the reextract, %
Table
Name solutionThe content of components in g/l
H2SO4CuNiFe
The original solution374.012.236.82.2
The raffinate174.09.729.01.8
The reextract180.01.04.40.26
The degree of extraction in the reextract, %58.211.211.812.2
The original solution398.011.533.82.3
The raffinate153.79.628.22.0
The reextract172.61.43.80.22
The degree of extraction in the reextract, %65.312.111.211.0
The original solution382.012.233.81.90
The raffinate167.09.728.51.86
The reextract1441.13.00.32
60.711.38.917.0
The original solution328.013.339.22.6
The raffinate157.011.432.52.0
The reextract131.31.44.20.14
The degree of extraction in the reextract, %57.010.510.75.4
The original solution37013.137.22.60
The raffinate16711.637.12.56
The reextract135.00.932.80.14
The degree of extraction in the reextract, %59.48.07.55.6

A method of processing copper concentrate from the flotation separation area, including oxidative roasting of copper concentrate leaching of copper calcine in the circulating electrolyte, separating the residue leaching, electroextraction of copper from leaching solutions, characterized in that the residue leaching in the form of a thickened slurry is subjected to flotation section is of emitting precious metals concentrate chamber and the product, containing mainly non-ferrous metals, which are processed to produce secondary Feinstein; part of the electrolyte after electroextraction copper is separated and subjected to evaporation to a concentration of sulfuric acid 250-300 g/l, separated from her copper sulphate crystallization and sulfuric acid extraction and return them to the leaching of copper calcine, after extraction raffinate acid containing mainly Nickel, is directed to the production of Nickel, and precious metals concentrate sent to the refinery production.



 

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6 cl, 6 tbl, 5 ex

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10 cl, 2 ex

FIELD: non-iron metallurgy, in particular reprocessing of copper containing sulfide materials.

SUBSTANCE: invention relates to reprocessing of copper containing materials to produce solutions useful for copper recovering. Method includes two-step autoclave leaching with sulfuric acid. The first step is carried out with limited copper converting into solution. On the second step precipitate is fully leached with fresh sulfuric acid solution while maintaining specific ratio of liquid and solid phases. Method of present invention makes in possible to produce in both leaching steps copper containing solutions of desired composition.

EFFECT: improved method for copper recovering, reduced capacity of autoclave equipment.

23 ex, 1 tbl

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