Reduction of lime consumption when treating refractory gold ores or concentrates

• US 8,029,751 B2
• Filed: 10/13/2009
• Issued: 10/04/2011
• Est. Priority Date: 12/22/2004
• Status: Active Grant

• Current Assignee: Placer Dome Technical Services Limited
• Original Assignee: Placer Dome Technical Services Limited
• Inventors: Ferron, Cesare Giosue, King, James A., Ji, Jinxing, Fleming, Christopher Andrew
• Primary Examiner(s): Mayes; Melvin C
• Assistant Examiner(s): DAVIS, SHENG HAN
• Application Number:
  US12/578,330
• Publication Number:
  US 20100024603A1
• Time in Patent Office: 721 Days
• Field of Search: None
• US Class Current: 423/23
• 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 3/08 Sulfuric acid , other sulfurated acids or salts thereof
• 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 a precious metal recovery process in which basic ferric sulphates and/or jarosites are controlled by a number of mechanisms, including control of the oxidation reaction conditions in the first autoclave compartment, hot curing of the autoclave discharge slurry, and/or contacting of the autoclave feed slurry with the hot cured discharge liquid.

Claims

1. A precious metal recovery process, comprising:

inputting a precious metal-containing feed slurry into a first compartment of a multi-compartment autoclave, the precious metal-containing feed slurry comprising a precious metal-containing material comprising sulphide sulphur in the form of one or more of pyrite, realgar, orpiment, chalcopyrite, and arsenopyrite;

providing, in the first compartment, a slurry temperature that is at least about 5°

C. less than a slurry temperature in a second compartment of the autoclave, the second compartment being adjacent to and downstream of the first compartment, whereby an acid level in the first compartment favors the formation of insoluble hematite from iron compounded with the sulphide sulphur;

removing, from the autoclave, an aqueous discharge slurry comprising discharge solids and aqueous discharge liquid, the discharge solids comprising at least a portion of the precious metal and basic iron sulphate, wherein at least most of the sulphide sulphur in the precious metal-containing material is oxidized to sulphate sulphur, wherein the aqueous discharge slurry comprises sulphuric acid and a dissolved metal sulphate, and wherein the discharge slurry comprises less than 10 wt. % (dry basis) of the basic iron sulphate;

contacting the discharge solids with an acid consumer to consume at least a portion of the sulphuric acid and the dissolved metal sulphates; and

contacting a lixiviant, at a pH above about pH 7.0, with the discharge solids to solubilize at least most of the precious metal; and

recovering the solubilized precious metal.

2. The process of claim 1, wherein at least most of the iron in the discharge slurry is in the form of hematite and wherein an acid level in the second compartment favors formation of basic iron sulphate and/or jarosite.

3. The process of claim 1, wherein the discharge solids comprise basic ferric sulphate, wherein at least most of the basic iron sulphate in the aqueous discharge solids is basic ferric sulphate, and further comprising before the lixiviant contacting step:

prior to contact of an acid consumer other than the basic ferric sulphate, allowing at least most of the basic ferric sulphate in the aqueous discharge solids to react at a temperature of at least about 60°

C., with at least most of the sulphuric acid in the aqueous discharge liquid to form ferric sulphate solubilized in the aqueous discharge liquid; and

separating at least most of the aqueous discharge liquid from the discharge solids, wherein at least most of the solubilized ferric sulphate is in the separated aqueous discharge liquid and wherein the separated aqueous discharge solids comprise sulphuric acid; and

contacting the separated discharge solids with an acid consumer to consume at least most of the sulphuric acid and the dissolved metal sulphates.

4. The process of claim 1, wherein the slurry temperature in the first compartment is at least about 10°

C. less than the slurry temperature in the second compartment, wherein the slurry temperature in the first compartment ranges from about 160 to about 220°

C., and wherein an acid level in the first compartment ranges from about 5 to about 30 g/L.

5. The process of claim 1, wherein the slurry temperature in the first compartment ranges from about 5 to about 30°

C. less than the slurry temperature in the second compartment, wherein the slurry temperature in the first compartment ranges from about 160 to about 220°

C., wherein the slurry temperature in the second compartment ranges from about 180 to about 230°

C., and wherein an acid level in the first compartment ranges from about 5 to about 30 g/L.

6. The process of claim 1, wherein laterite is contacted with the feed slurry prior to or during sulphide oxidation in the first autoclave compartment and wherein a molar ratio of acid consumers (as equivalent CaO₃) in the laterite to sulphides in the precious metal-containing material ranges from about 0.05 to about 0.90.

7. The process of claim 1, further comprising before the inputting step:

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

8. The process of claim 1, wherein acid consumers are added in the first compartment, wherein an acid concentration in the first compartment is at least about 5 g/L less than an acid concentration in the second compartment, and wherein the molar ratio of total acid consumers (as equivalent CO₃) to sulphides in the first compartment is no more than about 0.26.

9. The process of claim 8, wherein the molar ratio ranges from about 0.1 to about 0.225.

22. The process of claim 1, wherein a molecular oxygen mass transfer rate in the first compartment is less than a molecular oxygen mass transfer rate in the second compartment.

23. The process of claim 1, wherein a shear in the first compartment is less than a shear in the second compartment and wherein a pulp density of the precious metal-containing feed slurry in the first compartment ranges from about 30 to about 49% (w/w).

10. A precious metal recovery process, comprising:

(a) inputting a precious metal-containing feed slurry into a first compartment of a multi-compartment autoclave, the precious metal-containing feed slurry comprising a precious metal-containing material comprising sulphide sulphur;

(b) operating the first compartment under conditions favoring hematite formation and a second compartment of the multi-compartment autoclave under conditions favoring formation of basic ferric sulphate and/or jarosite;

(c) removing, from the autoclave, an aqueous discharge slurry comprising discharge solids and aqueous discharge liquid, the discharge solids comprising at least a portion of the precious metal and basic iron sulphate, wherein at least most of the sulphide sulphur in the precious metal-containing material is oxidized to sulphate sulphur, wherein the aqueous discharge slurry comprises sulphuric acid and a dissolved metal sulphate, and wherein the discharge slurry comprises less than 10 wt. % (dry basis) basic iron sulphate;

(d) contacting the discharge solids with an acid consumer to consume at least a portion of the sulphuric acid and dissolved metal sulphates; and

(e) contacting a lixiviant, at a pH above about pH 7.0, with the discharge solids to solubilize at least most of the precious metal; and

(f) recovering the solubilized precious metal.

11. The process of claim 10, wherein, in the operating step, the first compartment has a slurry temperature that is at least about 5°

C. less than a slurry temperature in the second compartment and wherein at least most of the iron in the discharge slurry is in the form of hematite.

12. The process of claim 10, wherein the first compartment is the initial compartment in the autoclave and wherein, in the operating step, no more than about 70% of the sulphide sulphur in the first compartment is oxidized, wherein a slurry temperature in the first compartment is at least about 10°

C. less than a slurry temperature in the second compartment, wherein the slurry temperature in the first compartment ranges from about 160 to about 220°

C., and wherein an acid level in the first compartment ranges from about 5 to about 30 g/L.

13. The process of claim 10, wherein the first compartment is the initial compartment in the autoclave, wherein an acid concentration in the first compartment is at least about 5 g/L less than an acid concentration in the second compartment, and wherein, in the operating step, a total acid concentration in the first compartment ranges from about 5 to about 30 g/l.

14. The process of claim 10, wherein acid consumers are added to the first but not the second compartments, wherein an acid concentration in the first compartment is at least about 5 g/L less than an acid concentration in the second compartment, and wherein a molar ratio of total acid consumers to sulphides in the first compartment ranges from about 0.10 to about 0.225.

15. The process of claim 10, wherein at least most of the iron in the discharge slurry is in the form of hematite and wherein at least most of the basic iron sulphate in the aqueous discharge solids is basic ferric sulphate and further comprising before the lixiviant contacting step:

(g) allowing at least most of the basic ferric sulphate in the aqueous discharge solids to react with the sulphuric acid to form ferric sulphate solubilized in the aqueous discharge liquid; and

(h) separating at least most of the aqueous discharge liquid from the discharge solids, wherein at least most of the solubilized ferric sulphate is in the separated aqueous discharge liquid and wherein the separated aqueous discharge solids comprise sulphuric acid; and

(i) contacting the separated discharge solids with an acid consumer to consume at least most of the sulphuric acid and the dissolved metal sulphates.

16. The process of claim 11, wherein the slurry temperature in the first compartment is at least about 10°

C. less than the slurry temperature in the second compartment.

17. The process of claim 11, wherein the slurry temperature in the first compartment ranges from about 5 to about 30°

C. less than the slurry temperature in the second compartment.

18. The process of claim 10, wherein laterite is contacted with the feed slurry prior to or during sulphide oxidation in the first autoclave compartment and wherein a molar ratio of acid consumers (as equivalent CaO₃) in the laterite to sulphides in the precious metal-containing material ranges from about 0.05 to about 0.90.

19. The process of claim 10, further comprising before step (a):

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

20. The process of claim 10, wherein acid consumers are added in the first compartment and wherein the molar ratio of total acid consumers (as equivalent CO₃) to sulphides in the first compartment is no more than about 0.26.

21. The process of claim 10, wherein the first compartment is the initial compartment in the autoclave and wherein, in the operating step, a total acid concentration in the first compartment is at least about 5 g/l less than a total acid concentration in a last downstream autoclave compartment.

24. The process of claim 14, wherein an acid consumer is added to the first compartment and wherein, in the first compartment, a molar ratio of total acid consumers (as equivalent CO₃) to sulphide sulphur is no more than about 0.26.

25. The process of claim 14, wherein the aqueous discharge slurry has a free acid concentration of from about 20 to about 50 g/L and a dissolved iron concentration of at least about 1 g/L and wherein the acid consumer is a base.

26. The process of claim 25, wherein, in the aqueous discharge slurry, at least about 50% of the iron is in the form of hematite and no more than about 50% is in the form of basic ferric sulphate and wherein the aqueous discharge slurry comprises less than 10 wt. % (dry basis) basic ferric sulphate.

27. The process of claim 16, wherein, after the allowing step, the aqueous discharge liquid comprises from about 10 to about 140 g/L dissolved ferric sulphate (as Fe₂(SO₄)₃), no more than about 3% wt basic ferric sulphates in a solid phase, no more than about 1% wt jarosites in the solid phase, and from about 10 to about 40 g/L sulphuric acid, wherein, after the allowing step, at least about 80% of the iron in the aqueous discharge liquid is in the form of dissolved ferric sulphate, and wherein, after the allowing step, no more than about 20% of the iron is in the form of basic ferric sulphate.

28. The process of claim 10, wherein at least most of the iron sulphate in the discharge solids is basic ferric sulphate, and further comprising before the lixiviant contacting step:

(g) prior to contact of an acid consumer other than the basic ferric sulphate, allowing at least most of the basic ferric sulphate in the aqueous discharge solids to react, at a temperature of at least about 60°

C., with at least most of the basic sulphuric acid in the aqueous discharge liquid to form ferric sulphate solubilized in the aqueous discharge liquid;

(h) separating at least most of the aqueous discharge liquid from the discharge solids, wherein at least most of the solubilized ferric sulphate is in the separated aqueous discharge liquid and wherein the separated aqueous discharge solids comprise sulphuric acid; and

(i) contacting the separated discharge solids with an acid consumer to consume at least most of the sulphuric acid and dissolved metal sulphates.

29. The process of claim 10, wherein a molecular oxygen mass transfer rate in the first compartment is less than a molecular oxygen mass transfer rate in the second compartment.

30. The process of claim 10, wherein a shear in the first compartment is less than a shear in the second compartment and wherein a pulp density of the precious metal-containing feed slurry in the first compartment ranges from about 30 to about 49% (w/w).

31. The process of claim 10, wherein an acid consumer is added to the first compartment and wherein, in the first compartment, a molar ratio of total acid consumers (as equivalent CO₃) to sulphide sulphur is no more than about 0.26.

32. The process of claim 10, wherein the aqueous discharge slurry has a free acid concentration of from about 20 to about 50 g/L and a dissolved iron concentration of at least about 1 g/L and wherein the acid consumer is a base.

33. The process of claim 32, wherein, in the aqueous discharge slurry, at least about 50% of the iron is in the form of hematite and no more than about 50% is in the form of basic ferric sulphate and wherein the aqueous discharge slurry comprises less than 10 wt. % (dry basis) basic ferric sulphate.

34. The process of claim 28, wherein, after the allowing step, the aqueous discharge liquid comprises from about 10 to about 140 g/L dissolved ferric sulphate (as Fe₂(SO₄)₃), no more than about 3% wt basic ferric sulphates in a solid phase, no more than about 1% wt jarosites in the solid phase, and from about 10 to about 40 g/L sulphuric acid, wherein, after the allowing step, at least about 80% of the iron in the aqueous discharge liquid is in the form of dissolved ferric sulphate, and wherein, after the allowing step, no more than about 20% of the iron is in the form of basic ferric sulphate.

35. A process, comprising:

(a) inputting a precious metal-containing feed slurry into a first compartment of a multi-compartment autoclave, the precious metal-containing feed slurry comprising a precious metal-containing material comprising sulphide sulphur;

(b) operating the first compartment under conditions favoring hematite formation and a second compartment of the multi-compartment autoclave under conditions favoring formation of basic ferric sulphate and/or jarosite;

(c) removing, from the autoclave, an aqueous discharge slurry comprising discharge solids and aqueous discharge liquid, the discharge solids comprising at least a portion of the precious metal and basic iron sulphate, wherein at least most of the sulphide sulphur in the precious metal-containing material is oxidized to sulphate sulphur, wherein the aqueous discharge slurry comprises sulphuric acid and a dissolved metal sulphate, and wherein the discharge slurry comprises less than 10 wt. % (dry basis) basic iron sulphate;

(d) contacting the discharge solids with an acid consumer to consume at least a portion of the sulphuric acid and dissolved metal sulphate; and

(e) contacting a lixiviant, at a pH above about pH 7.0, with the discharge solids to solubilize at least most of the precious metal;

(f) prior to contact of an acid consumer other than the basic ferric sulphate, allowing at least most of the basic ferric sulphate in the aqueous discharge solids to react, at a temperature of at least about 60°

C., with at least most of the basic sulphuric acid in the aqueous discharge liquid to form ferric sulphate solubilized in the aqueous discharge liquid;

(g) separating at least most of the aqueous discharge liquid from the discharge solids, wherein at least most of the solubilized ferric sulphate is in the separated aqueous discharge liquid and wherein the separated aqueous discharge solids comprise sulphuric acid;

(h) contacting the separated discharge solids with an acid consumer to consume at least most of the sulphuric acid and dissolved metal sulphate; and

recovering the solubilized precious metal.