Process for controlling acid in sulfide pressure oxidation processes

• US 8,262,770 B2
• Filed: 09/12/2008
• Issued: 09/11/2012
• Est. Priority Date: 09/18/2007
• Status: Active Grant

• Current Assignee: Barrick Gold Corporation
• Original Assignee: Barrick Gold Corporation
• Inventors: Hillier, Daniel, Choi, Yeonuk, Ahern, Noelene
• Primary Examiner(s): Yang, Jie
• Application Number:
  US12/209,939
• Publication Number:
  US 20090071296A1
• Time in Patent Office: 1,460 Days
• Field of Search: 757/44, 757/11
• US Class Current: 75/744
• CPC Class Codes: C22B 1/00 Preliminary treatment of ores or scrap
• CPC Class Codes: C22B 11/00 Obtaining noble metals
• CPC Class Codes: C22B 11/04 by wet processes extraction of metal compounds by leaching in organic solutions C22B3/16; treatment or purification of solutions by liquid-liquid extraction C22B3/26
• CPC Class Codes: C22B 11/08 by cyaniding
• CPC Class Codes: C22B 3/08 Sulfuric acid , other sulfurated acids or salts thereof
• CPC Class Codes: C22B 3/20 Treatment or purification of solutions, e.g. obtained by leaching C22B3/18 takes precedence
• CPC Class Codes: C22B 3/44 by chemical processes treatment or purification of solutions by liquid-liquid extraction C22B3/26, by ion-exchange extraction C22B3/42
• CPC Class Codes: Y02P 10/20 Recycling

Abstract

The present invention is directed to flotation of refractory gold sulfide ores and to pressure oxidized residue neutralization using flotation tailings that have been contacted with an off gas of pressure oxidation.

Claims

1. A method, comprising:

(a) providing a precious metal-bearing material, the precious metal-bearing material comprising acid consumers;

(b) floating the material to form a first fraction comprising at least most of the precious metal in the precious metal-bearing material and a second fraction comprising at least some of the acid consumers in the precious metal-bearing material;

(c) pressure oxidizing at least portions of the first fraction but not the second fraction to form a pressure oxidized slurry comprising pressure oxidized residue and reactive sulfates and an off gas, wherein the pressure oxidized residue comprises at least most of the precious metal in the preciuos metal-bearing material;

(d) contacting the off gas with at least a portion of the second fraction to cool the off gas and heat the at least a portion of the second fraction;

(e) contacting the heated at least a portion of the second fraction with at least a portion of the pressure oxidized slurry to neutralize, at least partially, reactive sulfates in the at least a portion of the pressure oxidized slurry;

(f) contacting the pressure oxidized residue with an alkaline lixiviant to dissolve at least most of a selected precious metal in a pregnant leach solution; and

(g) thereafter recovering the dissolved selected precious metal from the pregnant leach solution.

2. The method of claim 1, wherein the selected precious metal is at least one of gold and silver and wherein step (e) comprises the sub-steps:

(e1) first contacting the pressure oxidized slurry with a wash solution in one or more first decantation units to form a dilute slurry and an overflow component, the overflow component having a temperature less than a temperature of the pressure oxidized slurry;

(e2) second contacting the heated at least a portion of the second fraction with at least a portion of the overflow component to neutralize at least partially reactive sulfates in the overflow component; and

(e3) thereafter contacting the overflow component with lime to consume reactive sulfates remaining from step (e2) to form the neutralized overflow component.

3. The method of claim 2, wherein an amount of lime required to yield a selected pH in the absence of heating the at least a portion of the second fraction is greater than an amount of limestone and/or lime required to yield the selected pH when the at least a portion of the second fraction is heated.

4. The method of claim 2, wherein an amount of limestone and/or lime required to consume the reactive sulfates when the second fraction is contacted with the off gas is no more than about 50% of an amount of lime required to consume the reactive sulfates when the second fraction is not contacted with the off-gas.

5. The method of claim 1, wherein the feed material comprises from about 0.1 to about 30 wt. % inorganic carbon and from about 0.3 to about 10 wt. % organic carbonaceous material.

6. The method of claim 1, wherein the at least a portion of the slurry is a liquid component and further comprising:

hot curing the pressure oxidized slurry, following pressure oxidation, to convert substantially solid-phase reactive sulfates into liquid-phase reactive sulfates; and

separating the hot cured slurry into a solid component and the liquid component, the solid component comprising the pressure oxidized residue and the liquid phase comprising the liquid-phase reactive sulfates.

7. The method of claim 1, wherein the first fraction is a concentrate and the second fraction is tails, wherein the heated at least a portion of the flotation tails has a temperature ranging from about 25 to about 80 degrees Celsius, wherein the at least a portion of the pressure oxidized slurry, immediately prior to step (e) has a temperature of no more than about 50 degrees Celsius, and wherein, during contacting step (e), the pressure oxidized slurry is heated, by the flotation tails, to a temperature of at least about 55 degrees Celsius.

8. The method of claim 1, wherein the second fraction comprises at least most of the acid consumers in the feed material.

9. The method of claim 1, wherein the precious metal is at least one of gold and silver and wherein an amount of lime required to consume the reactive sulfates when the tails are contacted with the off gas is no more than about 50% of an amount of lime required to consume the reactive sulfates when the tails are not contacted with the off-gas.

10. A method, comprising:

(a) providing a precious metal-bearing material, the precious metal-bearing material comprising acid consumers;

(b) floating the precious metal-bearing material to form a concentrate comprising at least most of the precious metal in the precious metal-bearing material and tailings comprising at least most of the acid consumers in the precious metal-bearing material;

(c) pressure oxidizing a slurry comprising the concentrate to form a pressure oxidized slurry, the pressure oxidized slurry comprising pressure oxidized residue and reactive sulfates and an off gas, wherein the pressure oxidized residue comprises at least most of the precious metal in the precious metal-bearing material;

(d) thereafter hot curing the pressure oxidized slurry to convert solid-phase reactive sulfates into liquid-phase reactive sulfates;

(e) separating the hot cured slurry into a solid component and a liquid component, the solid component comprising the pressure oxidized residue and the liquid component comprising the liquid-phase sulfates;

(f) contacting the off gas with at least a portion of the tailings and not the concentrate to cool the off gas and heat the at least a portion of the tailings;

(g) contacting the heated at least a portion of the tailings with the liquid component of the hot cured slurry to neutralize, at least partially, liquid-phase reactive sulfates; and

(h) thereafter recovering the precious metal from the solid component of the hot cured slurry.

11. The method of claim 10, wherein the precious metal is at least one of gold and silver and wherein the feed material comprises from about 0.1 to about 30 wt. % inorganic carbon and from about 0.3 to about 10 wt. % organic carbonaceous material.

12. The method of claim 10, wherein the heated at least a portion of the flotation tails has a temperature ranging from about 25 to about 80 degrees Celsius, wherein the at least a portion of the pressure oxidized slurry, immediately prior to step (h) has a temperature of no more than about 50 degrees Celsius, and wherein, during contacting step (h), the pressure oxidized slurry is heated, by the flotation tails, to a temperature of at least about 55 degrees Celsius.

13. The method of claim 10, wherein an amount of lime required to consume the reactive sulfates when the tails are contacted with the off gas is no more than about 50% of an amount of limestone and/or lime required to consume the reactive sulfates when the tails are not contacted with the off-gas.

14. A method, comprising:

(a) floating a precious metal-bearing material, the precious metal-bearing material comprising acid consumers, to form a concentrate comprising at least some of the precious metal in the precious metal-bearing material and tailings comprising at least some of the acid consumers in the precious metal-bearing material;

(b) contacting the concentrate with an acid-containing wash solution to consume, at least partially, acid consumers in the concentrate and form a pre-treated slurry comprising the concentrate;

(c) washing the pre-treated slurry to form a washed slurry and a liquid overflow, the liquid overflow comprising acid;

(d) pressure oxidizing the pre-treated slurry to form a pressure oxidized slurry, the pressure oxidized slurry comprising a pressure oxidized concentrate and reactive sulfates and an off gas, wherein the pressure oxidized concentrate comprises at least most of the precious metal in the precious metal-bearing material;

(e) separating the pressure oxidized slurry into a solid component and a liquid component, the solid component comprising the pressure oxidized residue and the liquid component comprising the liquid-phase sulfates;

(f) contacting the off gas with at least a portion of the tailings and not the concentrate to cool the off gas and heat the at least a portion of the tailings;

(g) contacting the heated at least a portion of the tailings with at least one of the liquid component of the pressure oxidized slurry and liquid overflow to neutralize, at least partially, liquid-phase reactive sulfates; and

(h) thereafter recovering the precious metal from the solid component of the pressure oxidized slurry.

15. The method of claim 14 wherein the feed material comprises from about 0.1 to about 30 wt. % inorganic carbon and from about 0.3 to about 10 wt. % organic carbonaceous material.

16. The method of claim 14, wherein the heated at least a portion of the flotation tails has a temperature ranging from about 25 to about 80 degrees Celsius, wherein the at least a portion of the pressure oxidized slurry, immediately prior to step (h) has a temperature of no more than about 50 degrees Celsius, and wherein, during contacting step (h), the pressure oxidized slurry is heated, by the flotation tails, to a temperature of at least about 55 degrees Celsius.

17. The method of claim 14, wherein the tails comprise most of the acid consumers in the feed material.

18. The method of claim 14, further comprising after step (d) and before step (e):

hot curing the pressure oxidized slurry to convert substantially solid-phase reactive sulfates into liquid-phase reactive sulfates.

19. A method, comprising:

(a) providing a refractory precious metal-bearing sulfidic material;

(b) providing a slurry stream comprising acid consumers;

(c) oxidizing the refractory precious metal-bearing sulfidic material to form an oxidized slurry comprising oxidized residue and reactive sulfates and waste heat, wherein the pressure oxidized residue comprises at least most of the precious metal in the preciuos metal-bearing material;

(d) contacting the slurry stream with the waste heat to heat the slurry stream and not the refractory sulfidic precious metal-bearing material; and

(e) contacting the heated slurry stream with the liquor component of the oxidized slurry to neutralize, at least partially, reactive sulfates in the oxidized slurry;

(f) thereafter contacting the oxidized residue with an alkaline lixiviant to dissolve at least most of a selected precious metal in a pregnant leach solution; and

(g) thereafter recovering the selected precious metal from the pregnant leach solution.

20. The method of claim 19, wherein the slurry stream comprises flotation tails, wherein the oxidizing step is pressure oxidation, wherein the waste heat is in an off-gas from pressure oxidation, and wherein, in the contacting step (d), the slurry stream is contacted physically with the off-gas.