Process for reduced alkali consumption in the recovery of silver

• US 8,252,254 B2
• Filed: 06/11/2007
• Issued: 08/28/2012
• Est. Priority Date: 06/15/2006
• Status: Active Grant

• Current Assignee: Barrick Gold Corporation
• Original Assignee: Barrick Gold Corporation
• Inventors: Choi, Yeonuk, Kondos, Peter D., McMullen, Jacques
• Primary Examiner(s): Mayes, Melvin C
• Assistant Examiner(s): DARJI, PRITESH D
• Application Number:
  US11/761,103
• Publication Number:
  US 20070292326A1
• Time in Patent Office: 1,905 Days
• Field of Search: 423/24, 423/45, 423/146, 423/147, 423/166, 757/44, 757/33
• US Class Current: 423/45
• CPC Class Codes: C22B 1/00 Preliminary treatment of ores or scrap
• CPC Class Codes: C22B 1/11 Removing sulfur, phosphorus or arsenic other than by roasting
• 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: Y02P 10/20 Recycling

Abstract

The present invention is directed to a precious metal recovery process in which basic ferric sulphates and/or jarosites are controlled by hot curing of the autoclave discharge slurry followed by decomposition of argentojarosite using strong acid consumers.

Claims

1. A process for the enhanced recovery of silver from autoclave discharge, comprising:

oxidizing an aqueous feed slurry in an autoclave to form an aqueous discharge slurry, the feed slurry comprising a silver-containing material and sulphide sulphur, wherein at least most of the sulphide sulphur is oxidized in the autoclave to sulphate sulphur and wherein at least a portion of the sulphate sulphur is in the form of a solid-phase reactive sulphate, the solid-phase reactive sulphate comprising iron and silver;

removing, from the autoclave, the aqueous discharge slurry comprising discharge solids and aqueous discharge liquid, the discharge solids comprising silver and at least most of the solid-phase reactive sulphate and wherein a liquid phase of the aqueous discharge slurry comprises an acid;

hot curing the aqueous discharge slurry to allow at least most of the iron-containing solid-phase reactive sulphates in the discharge solids to react with the acid in the aqueous discharge slurry to form liquid-phase iron-containing reactive sulphate, wherein, after the hot curing step, at least a portion of the solid-phase reactive sulphate comprises silver and the discharge solids have a total solid-phase reactive sulphate content of no more than about 2 wt %;

after the hot curing step, contacting the discharge solids with a strong acid consumer while maintaining a temperature of the discharge solids to greater than about 80°

C. to convert at least most of the remaining iron-containing solid-phase reactive sulphate to a nonreactive iron-containing species and to decompose at least most of the silver-containing solid-phase reactive sulphate to a soluble form of silver, wherein an amount of the strong acid consumer used is no more than about 100 kg/tonne of the discharge solids, and wherein after the contacting step no more than about 25% of the iron in the discharge solids is in the form of solid-phase reactive sulphate; and

thereafter recovering at least most of the silver from the discharge solids.

2. The process of claim 1, wherein the solid-phase reactive sulphate comprises basic ferric sulphate, the liquid-phase reactive sulphate comprises dissolved ferric sulphate, the nonreactive iron-containing species comprises iron hydroxide, and the acid comprises sulphuric acid, wherein, in the hot curing step, the temperature of the aqueous discharge slurry is maintained at greater than 60 degrees Celsius, and wherein, in the hot curing step, the aqueous discharge slurry is held in a stirred vessel and further comprising:

after the hot curing step and before the thereafter recovering step, separating at least a portion of the liquid phase of the aqueous discharge slurry from the discharge solids, wherein the solid-phase reactive sulphate comprises basic ferric sulphates and wherein, in the thereafter recovering step, at least most of the basic ferric sulphates are converted into dissolved ferric sulphate according to the following equation;

2Fe(SO₄)(OH)+H₂SO₄=Fe₂(SO₄)₃+2H₂O.

3. The process of claim 1, wherein the solid-phase reactive sulphate comprises basic iron sulphate, the liquid-phase reactive sulphate comprises ferric sulphate, the nonreactive iron-containing species comprises iron hydroxide, and the acid comprises sulphuric acid, wherein the strong acid consumer used in the contacting step is predominantly lime, wherein, in the hot curing step, greater than about 90% of the solid-phase reactive sulphate is converted into liquid-phase reactive sulphate, and wherein, in the contacting step, a pH of the discharge solids is increased to a pH in the range of from about pH 9.0 to about pH 12.0, and further comprising:

contacting dissolved ferric sulphate in the aqueous discharge slurry with a second acid consumer different from the strong acid consumer used in the contacting step to convert at least most of the dissolved ferric sulphate to ferric hydroxide.

4. The process of claim 1, wherein, after the hot curing step, the aqueous discharge slurry comprises from about 50 to about 150 g/l liquid-phase reactive sulphate, no more than about 5 wt. % solid-phase reactive sulphate, and from about 10 to 140 g/l sulphuric acid, and wherein the aqueous discharge slurry comprises no more than about 0.5 wt. % basic ferric sulphate.

5. The process of claim 1, wherein in the contacting step the strong acid consumer is lime and an amount of lime contacted with the discharge solids is no more than about 60 kg/tonne, wherein greater than about 10 % of the solid-phase reactive sulphates present before the contacting step is in the form of argentojarosite.

6. The process of claim 1, further comprising after the hot curing step and before the contacting step:

separating at least most of the discharge liquid phase from the discharge solids, the discharge liquid comprising most of the liquid-phase reactive sulphate and acid and the discharge solids comprising most of the solid-phase reactive sulphate;

contacting the discharge liquid with an acid consumer to neutralize the liquid-phase reactive sulphate and the acid; and

washing, by a wash solution, the discharge solids, wherein the wash solution comprises an acid consumer to neutralize most of any remaining liquid-phase reactive sulphate and acid, wherein a total amount of acid consumer contacted, in the contacting step, with the discharge solids ranges from about 20 to about 60 kg/tonne of the discharge solids.

7. The process of claim 6, wherein a total amount of lime equivalent acid consumer contacted, in the contacting step, with the discharge solids ranges from about 20 to about 60 kg/tonne of the discharge solids after the hot curing step and before the contacting step, wherein the silver-containing material comprises gold and wherein the thereafter recovering step comprises the substeps:

contacting the discharge solids with a lixiviant to dissolve, in a pregnant leach solution, at least most of the silver and gold in the discharge solids; and

recovering at least most of the dissolved silver and gold from the pregnant leach solution.

8. The process of claim 1, wherein, in the contacting step, the discharge solids are in a slurry having a pH of at least about pH 10 and a temperature of at least about 90°

C., and wherein the amount of lime equivalent acid consumer contacted with the discharge solids ranges from about 20 kg/tonne to about 60 kg/tonne.

9. The process of claim 6, wherein, in the separating and liquid phase contacting steps, the discharge solids are maintained at a temperature greater than about 60°

C.

10. The process of claim 6, further comprising before the oxidizing step:

contacting at least a portion of the separated aqueous discharge liquid with the silver-containing material, wherein the at least a portion of the separated aqueous discharge liquid comprises liquid-phase reactive sulphate and free sulphuric acid to partially oxidize sulphide sulphur in the material prior to the oxidizing step.

24. The method of claim 1, wherein the autoclave is operated under conditions favoring the formation of basic ferric sulphate and disfavoring the formation of hematite.

27. The method of claim 1, wherein, in the contacting step, greater than about 75% of the solid-phase reactive sulphate is converted to the nonreactive iron-containing species, wherein greater than about 90% of the solid-phrase reactive sulphate is in the form of jarosites.

30. The method of claim 1, wherein, in the contacting step, the discharge solids are in a slurry having a pH of at least about pH 7 and a temperature of at least about 80°

C.

11. A process for the enhanced recovery of silver from autoclave discharge, comprising:

oxidizing, in an autoclave, sulphide sulphur in an aqueous feed slurry, to form an aqueous discharge slurry, the aqueous feed slurry comprising a precious metal-containing material, wherein at least most of the sulphide sulphur is oxidized to sulphate sulphur, wherein the precious metal comprises silver and gold, and wherein at least a portion of the sulphate sulphur is in the form of a solid-phase reactive sulphate, the solid-phase reactive sulphate comprising iron as basic ferric sulphate and silver as argentojarosite;

removing, from the autoclave, the aqueous discharge slurry comprising discharge solids and aqueous discharge liquid, the discharge solids comprising at least a portion of the precious metal and at least most of the solid-phase reactive sulphate, and wherein a liquid phase of the aqueous discharge slurry comprises sulphuric acid;

hot curing the aqueous discharge slurry to allow greater than about 90% of the basic ferric sulphate in the discharge solids to react with the sulphuric acid to form ferric sulphate dissolved in the aqueous discharge liquid, the discharge solids having, after the hot curing step, a total solid-phase reactive sulphate content of no more than about 2 wt %;

thereafter separating the aqueous discharge liquid from the discharge solids, wherein at least most of the dissolved ferric sulphate and remaining acid are in the separated aqueous discharge liquid;

contacting the separated discharge solids with a strong acid consumer to decompose the remaining basic ferric sulphate to an iron oxide, and to decompose the argentojarosite, wherein a total amount of lime equivalent acid consumer contacted, in the contacting step, with the discharge solids ranges from about 20 to about 60 kg/tonne of the discharge solids and wherein after the contacting step no more than about 25 % of the iron in the discharge solids is in the form of solid-phase reactive sulphate;

thereafter contacting a lixiviant, at a pH greater than about pH 7.0, with the discharge solids to dissolve at least most of the silver and gold in the discharge solids; and

recovering the dissolved silver and gold.

12. The process of claim 11, wherein the strong acid consumer comprises lime, and wherein, in the separating step, the discharge solids are maintained at a temperature of greater than about 80°

C. and in a liquid phase having a pH of greater about pH 9, and wherein, in the hot curing step, the temperature of the aqueous discharge slurry is maintained at or greater than 60 degrees Celsius.

13. The process of claim 11, wherein the strong acid consumer is lime and wherein no more than about 60 kg/tonne of acid consumer is contacted with the discharge solids in the contacting step and further comprising:

contacting dissolved ferric sulphate in the aqueous discharge liquid with lime and/or limestone to convert at least most of the dissolved ferric sulphate to ferric hydroxide.

14. The process of claim 11, wherein, in the separating step, the discharge solids are maintained at a temperature of greater than about 60°

C., wherein, after the hot curing step, the aqueous discharge slurry comprises from about 50 to about 150 g/L dissolved ferric sulphate, no more than about 1 wt % solid-phase reactive sulphate, no more than about 0.5 wt. % basic ferric sulphate, from about 10 to about 50 g/L ferric ion, and from about 10 g/L to about 40 g/L sulphuric acid, wherein the aqueous discharge liquid comprises greater than about 80% of the dissolved ferric iron in the aqueous discharge slurry after the hot curing step, wherein the separated aqueous discharge liquid comprises no more than about 1 wt % solids, and wherein the separated aqueous discharge solids comprise no more than about 70 wt % liquid.

25. The method of claim 11, wherein the autoclave is operated under conditions favoring the formation of basic ferric sulphate and disfavoring the formation of hematite.

31. The method of claim 11, wherein, in the contacting step, the discharge solids are in a slurry having a pH of greater than about pH 9 and a temperature of at least about 90°

C.

15. A process for the enhanced recovery of silver from autoclave discharge, comprising:

oxidizing sulphide sulphur in an aqueous feed slurry in an autoclave to form an aqueous discharge slurry, the aqueous feed slurry comprising a silver-containing material, wherein at least most of the sulphide sulphur is oxidized to sulphate sulphur and wherein at least a portion of the sulphate sulphur is in the form of a solid-phase reactive sulphate, the solid-phase reactive sulphate comprising iron as basic sulphate and silver as argentojarosite;

removing, from the autoclave, the aqueous discharge slurry comprising discharge solids and aqueous discharge liquid, the discharge solids comprising at least most of the solid-phase reactive sulphate, and wherein a liquid phase of the aqueous discharge slurry comprises sulphuric acid;

hot curing the aqueous discharge slurry to allow greater than about 85% of the iron-containing solid-phase reactive sulphate in the discharge solids to react with the sulphuric acid to form liquid-phase reactive sulphate as dissolved ferric sulphate in the aqueous discharge liquid, the discharge solids after the hot curing step having a total solid-phase reactive sulphate content of no more than about 2 wt %;

thereafter separating the aqueous discharge liquid from the discharge solids, wherein at least most of the liquid-phase reactive sulphate and remaining acid are in the separated aqueous discharge liquid;

contacting the separated discharge solids with lime to decompose at least most of the silver containing argentojarosite, wherein an amount of the lime used is no more than about 100 kg/tonne of the discharge solids, and wherein after the contacting step no more than about 25% of the iron in the discharge solids is in the form of solid-phase reactive sulphate;

thereafter contacting a lixiviant, at a pH greater than about pH 7.0, with the discharge solids to dissolve at least most of the silver in the solids; and

recovering the dissolved silver.

16. The process of claim 15, wherein, in the contacting step, the discharge solids are maintained at a temperature of greater than about 80°

C. and in a liquid phase having a pH of greater than about pH 9, and wherein, in the separating step, the temperature of the discharge slurry is maintained at or greater than 60 degrees Celsius.

17. The process of claim 15, wherein no more than about 60 kg/tonne of lime is contacted with the discharge solids in the contacting step and further comprising:

contacting liquid-phase reactive sulphate in the aqueous discharge liquid with lime and/or limestone to convert at least most of the dissolved ferric sulphate to ferric hydroxide.

18. The process of claim 15, wherein, in the separating step, the discharge solids are maintained at a temperature of greater than about 85°

C. and wherein, after the hot curing step, the aqueous discharge slurry comprises from about 50 to about 150 g/L liquid-phase reactive sulphate, no more than about 1 wt % solid-phase reactive sulphate, and from about 10 g/L to about 40 g/L sulphuric acid.

19. The process of claim 15, wherein during the separating step, a second acid consumer other than lime is contacted with the discharge solids and wherein a total amount of lime-equivalent acid consumer contacted, in the contacting step, with the discharge solids ranges from about 20 to about 60 kg/tonne of the discharge solids.

20. The process of claim 19, wherein the second acid consumer is limestone.

21. The process of claim 15, further comprising before the oxidizing step:

contacting at least a portion of the separated aqueous discharge liquid with unoxidized precious metal-containing material, wherein the separated aqueous discharge liquid comprises liquid-phase reactive sulphate and free sulphuric acid to partially oxidize sulphide sulphur in the unoxidized material.

22. The process of claim 15, wherein the duration of the hot curing step is greater than about 6 hours and wherein a total amount of lime-equivalent acid consumer contacted, in the contacting step, with the discharge solids ranges from about 20 to about 60 kg/tonne of the discharge solids.

23. The process of claim 15, wherein the duration of the hot curing step is greater than about 12 hours and wherein a total amount of lime-equivalent acid consumer contacted, in the contacting step, with the discharge solids ranges from about 20 to about 60 kg/tonne of the discharge solids.

26. The method of claim 15, wherein the autoclave is operated under conditions favoring the formation of basic ferric sulphate and disfavoring the formation of hematite.

28. The method of claim 15, wherein, in the hot curing step, an amount of lime required to decompose at least most of the argentojarosite is substantially lower than an amount of lime required to decompose at least most of the argentojarosite using conventional lime boiling techniques.

29. The method of claim 15, wherein the aqueous discharge slurry, after the hot curing step comprises dissolved ferric iron and metal sulphates, wherein the separated aqueous discharge liquid includes greater than about 90% of the dissolved ferric iron, wherein the separated discharge solids comprise no more than about 10% of the dissolved metal sulphates and free sulphuric acid and at least most of the silver in the aqueous discharge slurry, after the hot curing step.

32. The method of claim 15, wherein, in the contacting step, the discharge solids are in a slurry having a pH of from about pH 10 to about pH 12 and a temperature from about 80°

C. to about 100°

C.