Process for enhanced acid leaching of laterite ores

A technology for leaching and ore, which is applied in the field of leaching nickel-containing laterite ore, can solve the problems of negative environmental impact, slowness, high acid consumption, etc., and achieve the effect of reducing demand, providing economic benefits, reducing or eliminating the release of acid

Inactive Publication Date: 2013-10-16
BHP BILLITON SSM TECH PTY LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0010] However, discharging iron as jarosite leads to high acid consumption, since it is known that 1.5 moles of sulfuric acid are required to dissolve 1 mole of ferric iron, and only 1 mole of sulfuric acid is released during jarosite precipitation to help leach saprolite part
Jarosite is not a stable compound and slowly releases acid as it weathers, negatively impacting the environment

Method used

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  • Process for enhanced acid leaching of laterite ores
  • Process for enhanced acid leaching of laterite ores
  • Process for enhanced acid leaching of laterite ores

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0056] Example 1: Ore Treatment, Chemical Analysis and Mineralogical Research

[0057] The three limonite samples were stirred in tap water for 2 hours and passed through a 1 mm sieve. Put any too large substance in Na, K and NH 4 Water with low ion content is ground to less than 1 mm with a rod mill. The two saprolite samples were subjected to Na, K and NH 4 Grinding with a rod mill in water with low ion content to P 80 100 <650μm. The slurries of limonite and saprolite were adjusted to solids concentrations of 30% w / w and 25% w / w, respectively. The SG and true PSD (particle size distribution) of the ore were measured with a Malvern Instrument, see Table 1.

[0058] Table 1: SG and PSD of Feed Ore

[0059]

[0060] The chemical analysis results of the ore samples are listed in Table 2.

[0061] Table 2: Chemical analysis of laterite samples

[0062]

[0063] The results of the mineralogical studies of the ore samples are briefly summarized in Table 3.

[0064] ...

Embodiment 2

[0066] Example 2: Continuous pressure leaching of limonite 1 containing 4.9% magnesium and normal pressure leaching of saprolite 2

[0067] 914 g of a 30.3% w / w limonite 1 slurry (as in Example 1) and 118 g of 98% H 2 SO 4 Added to a 2 liter titanium autoclave. In a stirred autoclave, pressurized leaching was continued for 1 hour at 250 °C and 48 bar (heating time removed). Simultaneously, 1101 g of 25.2% w / w saprolite 2 slurry (as shown in Example 1) and 159 g of 98% H 2 SO4 Mixed in a 3 liter stirred glass reactor and leached for 30 minutes at 95°-104°C and atmospheric pressure. The saprolite was heated to 60°C before adding the acid. The acidities of the final solutions obtained by pressure leaching of limonite and atmospheric pressure leaching of saprolite were 38.3g / L and 15.7g / L, respectively. The pressure leach slurry was transferred to the glass reactor while hot (~90°C) and mixed with the saprolite leach slurry, and atmospheric leaching and precipitation of iron ...

Embodiment 3

[0072] Example 3: Continuous pressure leaching of limonite 2 containing 2.7% magnesium and normal pressure leaching of saprolite 2

[0073] 914 g of 30.5% w / w Limonite 2 slurry (as shown in Example 1) and 104 g of 98% H 2 SO 4 Mixed in a 2 liter stirred titanium autoclave. In the autoclave, pressure leaching was continued for 1 hour at 250°C and 48 bar (heating time excluded). Simultaneously, 1101 g of 25.2% w / w saprolite 2 slurry (as shown in Example 1) and 181 g of 98% H 2 SO 4 Mixed in a 3 liter stirred glass reactor and leached for 30 minutes at 95°-104°C and atmospheric pressure. The saprolite was heated to 60°C before adding the acid. The acidities of the final solutions obtained by pressure leaching of limonite and atmospheric pressure leaching of saprolite were 46.1g / L and 22.6g / L, respectively. The pressure leaching slurry was transferred to the glass reactor while it was hot (~90°C) and mixed with the saprolite leaching slurry, and the atmospheric leaching and ...

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Abstract

A process is described for the recovery of nickel and cobalt from a nickeliferous laterite ore including the steps of: a) providing a nickeliferous laterite ore and separating that ore into its low magnesium limonite fraction and high magnesium saprolite fraction; b) treating the limonite fraction in acid solution in a primary high pressure leach step to produce a primary leach slurry; c) adding the saprolite fraction to the primary leach slurry to initiate precipitation of iron as goethite and / or hematite, while simultaneously releasing further acid from the iron precipitation, to effect a secondary atmospheric leach step, producing a secondary leach slurry; wherein all water used to prepare the ore slurries and / or acid solutions has an ionic composition that substantially avoids jarosite formation.

Description

field of invention [0001] The present invention relates to a process for the leaching of nickel-bearing laterite ores by hydrometallurgically treating the "limonite" and "saprolite" fractions of the ore in a continuous manner to recover nickel and cobalt. In particular, the present invention relates to a method of combining high pressure acid leaching of the limonite ore fraction of laterites in a medium with atmospheric pressure acid leaching of the saprolite fraction of the laterite ores, essentially This avoids the precipitation of iron as jarosite and discards the iron as solid goethite and / or hematite while recovering nickel and cobalt. Background of the invention [0002] Laterite ore bodies are oxidized ores, and laterite ore bodies generally consist of a limonite upper layer (of the ore profile) and a saprolite lower layer. Geological studies have shown that the main nickel-bearing mineral in the upper layer of laterite is limonite with low magnesium content, and th...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C22B3/08C22B3/44C22B23/00
CPCC22B23/043C22B23/0461C22B3/08C22B3/10C22B23/00
Inventor 刘后元达米安·加利·伊格内修斯·柯雷布斯
Owner BHP BILLITON SSM TECH PTY LTD
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