SU1027211A1 - Method for processing iron-based material containing non-ferrous metals - Google Patents

Description

The invention relates to hydrometallurgy of non-ferrous metals and can be used in the processing of oxidized nickel ores, ocean nodules for a metallized iron-based product. There is a method of processing materials based on iron., Containing non-ferrous metals 1. The disadvantage of this method is that in the leaching process, the oxygen supplied to oxidize the iron forms explosive mixtures with evolving hydrogen. The closest to the invention according to the technical essence and the achieved result is the method of processing materials based on iron containing non-ferrous metals, including their stadial leaching. acid solution in the presence of oxygen with simultaneous or subsequent precipitation of iron from solutions and extraction of non-ferrous metals G 2 C from them. The disadvantages of this method are; hydrogen evolution during the leaching of oxygen into the atmosphere with the formation of explosive mixtures; the use of two reagents — acids of the genus and alkali metal salt of sodium sulfate) for oxidizing iron in leaching solutions from the two to the trivalent state and precipitating it from solutions in the form of rozite Ma-ez (HAL; (HE environmental pollution of sulfate. m sodium discharged from the liquid phase slurry in the tailing dump; inapplicability of the method to the processing of poor ferronickel requiring large amounts of sodium sulfate to bind all the iron into sodium rosit. The aim of the invention is to prevent the formation of explosive hydrogen-oxygen gas mixture in the leaching process and reducing the consumption of reagents for iron deposition. The goal is achieved by the method of treating iron-based materials containing nonferrous metals, including their stadial acidification in the presence of oxygen in the presence of oxygen with simultaneous or subsequent precipitation iron from solutions and extracting non-ferrous metals from them; leaching the alloy; in the first stage, lead with sulfuric acid or its mixture with sulfuric acid with sulfuric acid acid in solution in the amount of G20- t of the total acid consumption, and the process is carried out to a constant pH value, and then in the second stage leaching is continued at 80-1 and the initial oxygen pressure is 315 atido dissolution of non-ferrous metals and iron deposition. The proposed method as a source of raw materials used magnetic concentrate of the following chemical composition, wt.%: Fe 75,2; N1 6.8; Co 0.71; Fe ° 73.3; Mi6,8; Co ° 0.68. The size of the concentrate is (-) O, 16 mm, 1001. The loading of the magnetic concentrate into the apparatus is 500 g, the acid solution is 2.0 tons. The total amount of acid fed into the apparatus was calculated as a 2-3 fold excess from the stoichiometry to dissolve metals. The first leaching stage must be carried out at 20-100 ° C until the total amount of the introduced acid is completely neutralized, i.e. to a constant pH. At this leaching stage, the acid is mainly consumed to dissolve the iron. Non-ferrous metals are transferred to the solution in an insignificant amount. At this leaching stage, the dissolution of iron in the presence of sulfurous acid is not accompanied by the evolution of hydrogen into the gas phase. It can be assumed that the dissolution of iron with a mixture of acids will be accompanied by the formation of iron thiosulfate, which reacts with sulfuric acid to form iron sulfate and elemental sulfur. Elemental sulfur is then combined with atomic hydrogen to form hydrogen sulfide which precipitates sulfate iron in the form of sulfide. In this case, the evolution of hydrogen into the gas phase also does not occur. Then, the pulp from the first stage enters the second one and its leaching is continued at 80–150 0 in the presence of oxygen (or oxygen) with a partial pressure of oxygen of 3–15 atm. In the second stage, iron is oxidized and thermally hydrolyzed, while non-ferrous metals go into solution. With such a leaching process, hydrogen in the gas phase is released in small quantities in the second leaching stage (Tables 1, 3, and k). After the leaching is completed, the solid is separated from the liquid by the known technology. PRI me R 1. The optimum ratio of sulfuric and sulfuric acid in the two-stage leaching. Mode 1 leaching stage: temperature 90 ° C, duration 1 h. Mode And stage leaching: temperature, oxygen partial pressure of 7 MPa, gas phase discharge rate 2, D l / min. Leaching the metallized product with a mixture of sulfuric acid and sulfuric acid is not accompanied by the formation of an explosive hydrogen-oxygen mixture of gases with a content of at least 20% sulfuric acid of the total amount of acids (less than 7 ° Hx). Leaching of metallized products with a mixture of acids should be carried out in technological schemes with the regeneration of sulfuric acid during electrolytic separation of metal from solutions. In this case, the loss of acid in the circuit can be compensated by feeding on the leaching of sulfuric acid. PRI me R 2. The temperature range and duration of stage 1 of the leaching of a metallized product with a mixture of sulfuric and sulphurous acids. Leaching mode: initial concentration of sulfuric acid is + 6.7 g / l, initial concentration of sulfuric acid is 40.5 g / l. In tab. Figure 2 shows the change in the acidity of the solution in stage I of the leaching of the metallized product. In experiment No. 2, in the first minutes of mixing the pulp, the temperature spontaneously increased from 20 to 0 ° due to the heat of chemical reactions. In the future, it was maintained at this level by heating the pulp. The process of neutralization of the mixture of acids at stage 1 of leaching proceeds rapidly and ends at 114 for 10 minutes, at a higher temperature during the heating of the pulp without oxygen supply. Neutralization of the mixture of acids is not accompanied by evolution of hydrogen into the gas phase. PRI me R 3. The temperature range of the leaching process of the magnetic concentrate with sulfuric acid in two stages without the formation of an explosive hydrogen-oxygen gas phase. Stage 1 leaching was performed while the pulp was heated to the required temperature in the absence of oxygen. The stage II leaching regime: the oxygen partial pressure is 5 MPa, the initial concentration of sulfurous acid is 58.3 g / l, the rate of gas phase bleeding is 2.0 l / min. In tab. Figure 3 shows the change in the composition of the gas phase in the P stage of the leaching of a magnetic concentrate with sulphurous acid at different temperatures. In this temperature range, the use of sulfurous acid with its preliminary neutralization before leaching in the absence of oxygen allows the leaching of metallized products without the formation of an explosive gas mixture. The temperature increase is leached from 80 to accelerates the process of dissolution of metals and the rate of hydrolysis of iron. At 80 ° C, the maximum extraction of metals into the solution — nickel 96%, cobalt — is achieved within four hours of leaching the magnetic concentrate, with — within two hours, at 150 ° C — within 0.5 h. The limits of the partial pressure of oxygen, providing a non-explosive gas phase in a two-stage leaching of a magnetic concentrate with sulfuric acid. Stage 1 leaching was performed without oxygen during the heating of the pulp to 100 ° C. Leaching stage II mode: temperature 100 ° С, gas phase straviguring rate 2.0 l / min.

five

In tab. Given the change in the composition of the gas phase at the II stage of the leaching of a magnetic concentrate with sulfurous acid at different partial pressures of oxygen.

The leaching of a metallized product with sulfuric acid prevents the formation of explosive; hydrogen-oxygen gas mixture

(, H, j, 7%) with a partial pressure of oxygen of at least 3.0 MPa.

With a lower partial pressure of oxygen, the rate of oxidation of iron and its precipitation from leaching solutions drastically decrease, and hydrogen is released into the gas phase more, 1%.

The leaching process with oxygen partial pressure is greater

272116

Athe pressure occurs without the formation of an explosive gas phase, but the rate of alkalization increases slightly, so it is not economically feasible to increase the pressure.

Thus, the proposed method of hydrometallurgical processing of metallized iron-based smelt allows;

obtain a non-explosive hydrogen-oxygen mixture in the leaching process; reduce reagent consumption due to the fact that iron precipitation is carried out without using sodium sulfate; to engage in processing poor alloys on the content of non-ferrous metals.

Table 1

3

96.1

1 92.0

2 82.3 12.2 9.5

12.9

3 77.6 16.2 93, i

17.3

, 2 38,759,6

72,826.3

99.0O

99.2O

99.2O 96.7 9.9

2.5

55, 8

88,813,6

99.2O

99, O

99.2O

99.2O ,, 94.6 9.4

2.1

5 7,24,3

96,52,6

99.2Oi 72.0 18.1 90.1 20.1 10 kS, 10 5 tt8.7 0.5 89.2 1005 6 O 58.0 58.0

eight

Continued table. 1 60 80 20 40 60 In 20 40 Bo In 20 i40 60 In 100

Table2 O99 / O O99, 93.1 93.5 2.5 1,096,02.3 0,997,01,9 O99,2O O99,3O O99.2O 9.5 90.9 0.8 1.496.61, D 1,196, 02.65 О99.8О О99.2О О99.8О 96.7 95.7 2.6 2, 80.6 1.2E3.03.8. 0,895,02,5 0,696,32,3 0,193,72,7 O96,52, B 93,3 89,1 0,6

About 0.5

ABOUT

0.16

0.50

1.0

2.0 o

0.5

1.0

ABOUT

0.5

1.0

Table3

9b, 0

0.7

0.6 96.5 98.0 1.0 98.0 1.0 3.1 95.2

99.0

about

about

99.5 99.0

0.0 0.5

99.0 0.5 99.0 1.0

97.5 98.2 1.5 99.0 0.5

Table4

n

12

1027211

Continued table. BUT

Claims (1)

METHOD FOR PROCESSING IRON-BASED MATERIALS CONTAINING NON-FERROUS METALS, including stage-by-stage leaching of them with an acid solution in the presence of oxygen with simultaneous or subsequent precipitation of iron from solutions and extraction of non-ferrous metals from them, characterized in that, in order to prevent the formation of an explosive oxygen-hydrogen mixture in the process of leaching and reducing the consumption of reagents for the deposition of iron, leaching. the alloy in the first stage is carried out with sulfuric acid or a mixture of it with sulfuric acid in the amount of sulfuric acid in the solution in an amount of 20-100% of the total acid consumption, and the process is carried out to a constant pH value, and then in the second stage leaching continues at 80- 100 ° C and a partial pressure of oxygen of 3'15 ati until the dissolution of non-ferrous metals and the deposition of iron. SU,. „1027211