Process for recovery of metal values from lead-zinc ores, even those having a high carbonate content

• US 4,272,341 A
• Filed: 01/09/1980
• Issued: 06/09/1981
• Est. Priority Date: 01/09/1980
• Status: Expired due to Term

• Current Assignee: Duval Corp.
• Original Assignee: Duval Corp.
• Inventors: Lamb, Frank E.
• Primary Examiner(s): Andrews, R. L.
• Application Number:
  US06/110,569
• Time in Patent Office: 517 Days
• Field of Search: 204/98, 204/128, 204/129, 204/118, 204/117, 75/109, 423/105, 423/165, 423/544, 423/419, 423/430
• US Class Current: 205/603
• CPC Class Codes: C22B 13/04 by wet processes
• CPC Class Codes: C22B 19/22 with leaching with acids
• CPC Class Codes: C25C 1/16 of zinc, cadmium or mercury
• CPC Class Codes: C25C 1/18 of lead
• CPC Class Codes: Y02P 10/20 Recycling

Abstract

A chemical, electro-chemical process for recovering meta values from a zinc- or lead-containing material comprises:

in a solubilization stage, oxidizing the zinc- or lead-containing material by treating said material with a ferric chloride leach solution;

when solubilized lead is present, separating it from the pregnant liquor forming an essentially lead free solution;

dividing this essentially lead free solution into two portions;

passing one portion of the essentially lead free solution into the anolyte compartment of a Zn° producing electrolysis stage for use as the ferrous ion-containing anolyte thereof;

separating iron from the second portion of the essentially lead free solution, forming an essentially iron free solution;

passing the essentially iron free solution into the catholyte compartment of said Zn° producing electrolysis stage for use as the catholyte thereof;

conducting electrolysis in said Zn° producing electrolysis stage, thereby regenerating ferric chloride leach solution in the anolyte by oxidizing ferrous ions to ferric ions, and reducing zinc ions in the catholyte to Zn°; and

recovering the Zn° produced in the electrolysis stage.

In a preferred embodiment, the process is adapted to metal recovery from high-carbonate containing ores by use of a multi-step solubilization stage including an acidulation step and a carbonation stage wherein cations such as Mg and Ca are removed from the process liquor.

Claims

1. A chemical, electro-chemical process for recovering metal values from a zinc- or lead-containing material comprising:

in a solubilization stage, oxidizing the zinc- or lead-containing material by treating said material with a ferric chloride leach solution until there is substantial solubilization of the zinc or lead content of the material into said solution in the form of zinc or lead chloride, thereby also reducing ferric chloride to ferrous chloride and forming a pregnant liquor;

when solubilized lead is present, separating it from the pregnant liquor forming an essentially lead free solution and recovering the separated lead;

dividing this essentially lead free solution into two portions;

passing one portion of the essentially lead free solution into the anolyte compartment of a Zn°

producing electrolysis stage for use as the ferrous ion-containing anolyte thereof;

separating iron from the second portion of the essentially lead free solution, forming an essentially iron free solution;

passing the essentially iron free solution into the catholyte compartment of said Zn°

producing electrolysis stage for use as the catholyte thereof;

conducting electrolysis in said Zn°

producing electrolysis stage, thereby regenerating ferric chloride leach solution in the anolyte by oxidizing ferrous ions to ferric ions, and reducing zinc ions in the catholyte to Zn°

; and

recovering the Zn°

produced in the electrolysis stage.

2. The process of claim 1 which further comprises recycling the solutions emanating from the anolyte and catholyte compartments of the Zn°

producing electrolysis stage, into the oxidizing step of the solubilization stage.

3. The process of claim 1 wherein the lead is separated from the pregnant liquor by precipitation with a metal less noble than lead.

4. The process of claim 3 wherein the less noble metal precipitant is iron.

5. The process of claim 1 wherein iron is separated from the essentially lead free solution by precipitation with a metal less noble than iron.

6. The process of claim 5 wherein the less noble metal precipitant is zinc.

7. The process of claim 1 wherein the zinc- or lead-containing material is a sulfide ore thereof.

8. The chemical, electro-chemical process for recovering metal values from a zinc sulfide or lead sulfide containing material of claim 1 comprising:

(a) in a solubilization stage, oxidizing the zinc- or lead-containing material by treating said material with a ferric chloride leach solution until there is substantial solubilization of the zinc or lead content of the material into said solution in the form of zinc or lead chloride, thereby also reducing ferric chloride to ferrous chloride and forming a pregnant liquor;

(b) separating solubilized lead from the pregnant liquor as Pb°

by precipitation with metallic iron, thereby forming an essentially lead free solution;

(c) passing a portion of the essentially lead-free solution from (b) into the anolyte compartment of a Zn°

producing electrolysis stage for use as the ferrous ion-containing anolyte thereof;

(d) separating iron as Fe°

from the remainder of the essentially lead-free solution from (b) by precipitation with metallic zinc thereby forming an essentially iron free solution;

(e) passing the essentially iron free solution from (d) into the catholyte compartment of said Zn°

producing electrolysis stage for use as the catholyte thereof;

(f) conducting electrolysis in said Zn°

producing electrolysis stage, thereby regenerating ferric chloride leach solution in the anolyte by oxidizing ferrous ions to ferric ion, and reducing zinc ions in the catholyte to Zn°

;

(g) recovering the Zn°

produced in the electrolysis stage; and

(h) recycling the solutions emanating from the anolyte and catholyte compartments of the Zn°

producing electrolysis stage, into the oxidizing step of solubilization stage (a).

9. The process of claim 8 wherein the solubilization stage is conducted by counterflow of the zinc sulfide or lead sulfide containing material and the ferric chloride leach solution.

10. The process of claim 1 wherein the leaching in the solubilization stage is conducted at ambient temperature using stirred reactors.

11. The process of claim 8 wherein the precipitation of iron by zinc is conducted at the atmospheric boiling point of the essentially lead-free solution.

12. The process of claim 1 wherein the zinc electrolysis stage is conducted in a diaphragm equipped electrolysis cell in which the cathode member upon which the metallic zinc deposits is a circular rotating plate equipped with mechanical scrapers for removal of the zinc deposits.

13. The process of claim 1 wherein the temperature in the solubilization stage is approximately at the atmospheric boiling point of the leached solution.

14. The process of claim 1 wherein the solubilization stage is conducted at a temperature greater than the atmospheric boiling point of the leach solution and the stage is conducted in a sealed reactor at elevated pressure.

15. The process of claim 14 wherein the temperature is approximately 140°

C. and the pressure is about 40-50 psi.

16. The process of claim 8 wherein the metallic iron used to precipitate lead in step b is obtained from the iron which is precipitated in iron removal step d;

and the zinc used to precipitate iron in step d is obtained from the zinc recovered in the electrolysis stage of step g.

17. The process of claim 3 wherein the material from which the metal values are recovered further comprises minor metals other than zinc or lead which metals are more noble than the precipitant used to precipitate lead in the lead removal step, whereby these minor metals are also precipitated.

18. The process of claim 8 wherein the zinc sulfide or lead sulfide containing material further comprises minor metals of cadmium, copper, silver, arsenic or antimony and the minor metal content is removed from the pregnant liquor by precipitation with metallic iron.

19. The process of claim 18 wherein at least one of said minor metals is removed by precipitation with iron prior to the lead removal step b.

20. The process of claim 4 in which the iron precipitant is finely divided iron powder.

21. The process of claim 8 wherein the portion of the essentially lead-free solution to be passed into the anolyte compartment is subjected to a sulfate removal step by reaction with an oxygen-containing gas at a temperature of 85°

-120°

C., thereby forming a sulfate-containing solid;

the thus-formed solid is removed from the liquor; and

the sulfate-depleted liquor is then passed into the anolyte compartment.

22. The process of claim 21 wherein the oxygen-containing gas is air.

23. The process of claim 8 wherein, prior to recycling of the depleted catholyte solution per step h, a portion of the catholyte solution is treated with an alkali metal carbonate, thereby precipitating zinc carbonate;

the separated zinc carbonate is resolubilized by treatment with hydrochloric acid; and

the solution containing the resolubilized zinc is added to the catholyte solution being recycled to the oxidizing step of solubilization stage a.

24. The process of claim 23 wherein the alkali metal carbonate is sodium carbonate.

25. The process of claim 7 wherein the ore is a pre-concentrated ore.

26. The process of claim 1 wherein the zinc or lead-containing material further comprises carbonates of calcium or magnesium and said process comprises

(a) in a multi-step solubilization stage, (i) oxidizing the zinc- or lead-containing material by treating said material with a ferric chloride leach solution until there is substantial solubilization of the zinc or lead content of the material into said solution in the form of zinc or lead chloride, thereby also reducing ferric chloride to ferrous chloride and forming a pregnant liquor, and simultaneously also solubilizng said calcium and magnesium carbonates into said solution, thereby forming soluble calcium and magnesium chlorides and insoluble hydrated ferric oxide solid;

(ii) separating the latter solid from the resultant solution;

(iii) solubilizng the separated solid by treating it with acid thereby forming a ferric ion-containing solution and insoluble solids; and

(iv) using the ferric ion solution from (iii) as at least part of the leach solution in (i);

(b) separating solubilized lead from the pregnant liquor, thereby forming an essentially lead-free solution;

(c) passing a portion of the essentially lead-free solution from (b) into the anolyte compartment of a Zn°

producing electrolysis stage for use as the ferrous ion-containing anolyte thereof;

(d) separating iron from the remainder of the essentially lead-free solution from (b) thereby forming an essentially iron-free solution;

(e) selectively separating zinc from the essentially iron free solution by treating it with an alkali metal carbonate thereby precipitating zinc as a zinc carbonate solid and forming an essentially zinc-free solution;

(f) separating the zinc carbonate solid from said essentially zinc-free solution;

(g) resolubilizing the zinc carbonate by treatment with hydrochloric acid forming a zinc chloride containing solution;

(h) passing the latter zinc chloride-containing solution into the catholyte compartment of said Zn°

producing electrolysis stage for use as the catholyte thereof;

(i) conducting electrolysis in said Zn°

producing electrolysis stage, thereby regenerating ferric chloride leach solution in the anolyte by oxidizing ferrous ions to ferric ion, and reducing zinc ions in the catholyte to Zn°

;

(j) recovering the Zn°

produced in the electrolysis stage; and

(k) separating calcium and magnesium from the zinc-free solution formed in (e) by treating it with an alkali metal carbonate thereby forming insoluble calcium and magnesium carbonates and an essentially calcium-, magnesium- and zinc-free solution; and

(l) recycling the calcium-, magnesium- and zinc-free solution back to the solubilization stage (a).

27. The process of claim 26 wherein the multi-step solubilization stage (a) comprises an oxidizing step (i) which, in turn, comprises at least two leaching steps, the first one of which solubilizes primarily lead;

and which further comprises, after acidulation step (iii), separating the ferric ion-containing solution from the insoluble solids formed in step (iii) and washing the separated solids with the solutions recycled from step (1), thereby forming a solution which is recycled to step a(i) or a(iii), of the solubilization stage, and a waste solid.

28. The process of claim 26 wherein the acidulation step (iii) of the solubilization stage (a) is effected using hydrochloric acid.

29. The process of claim 26 wherein lead is separated from the pregnant liquor in step (b) by precipitation therefrom using metallic iron as the precipitant.

30. The process of claim 26 wherein iron is separated from the lead-free solution in step (d) by precipitation therefrom using metallic zinc as the precipitant.

31. The process of claim 26 wherein the alkali metal carbonate precipitant is sodium carbonate.

32. The process of claim 26 wherein calcium and magnesium carbonates are coprecipitated in step (k).

33. The process of claim 26 wherein calcium is selectively precipitated in the form of calcium carbonate prior to the precipitation of magnesium, in the form of magnesium carbonate in step (k).

34. The process of claim 28 wherein a caustic chlorine electrolysis stage is incorporated to provide a source of HCl and alkali metal hydroxide, the HCl being utilized in the acidulation step of solubilization stage (a) and in zinc carbonate resolubilization step (g), and the alkaline metal hydroxide subsequently being reacted with carbon dioxide to form the souce of the alkali metal carbonate utilized in carbonate precipitation steps (e) and (k).

35. The process of claim 34 wherein the electrolyte formed in the caustic chlorine electrolysis salt is provided by recycling a portion of the zinc-, calcium- and magnesium-free solution from step (k), said solution containing alkali metal chloride;

and the process further comprising conducting electrolysis in the caustic chlorine cell, thereby producing chlorine gas at the anode and alkali metal hydroxide and hydrogen gas at the cathode, which latter products are produced by reaction of water with the alkali metal formed at the cathode by reduction of the alkali metal cation;

reacting the hydrogen and chlorine gases so produced in a hydrogen chloride reactor to produce HCl;

recycling the depleted zinc cell catholyte back into the catholyte and adding to the recycled catholyte a portion of the HCl gas produced in the HCl unit, thereby forming hydrochloric acid;

adding the zinc carbonate from step (f) to the recycling hydrochloric acid-containing catholyte, thereby resolubilizing the zinc carbonate per step (g);

adding the remaining portion of the HCl gas from the HCl reactor to step (iii) of solubilization stage (a), thereby forming hydrochloric acid used to resolublize the hydrated ferric oxide solid;

reacting the alkali metal hydroxide formed in the caustic chlorine cell with carbon dioxide, thereby forming an alkali metal carbonate-containing solution;

and adding a portion of this alkali metal carbonate-containing solution to the iron-free solution in step (e) in order to selectively separate zinc; and

recycling the remaining portion of the alkali metal carbonate-containing solution to calcium and magnesium carbonate precipitation step (k).

36. The process of claim 35 wherein the alkali metal is sodium.

37. The process of claim 29 wherein the material from which the metal values are recovered further comprises minor metals other than zinc or lead which metals are more noble than the precipitant used to precipitate lead in the lead removal step, whereby these minor metals are also precipitated.

38. The process of claim 35 wherein the carbon dioxide reactant is derived from fossil fuel.

39. The process of claim 26 wherein the zinc- or lead-containing material is a sulfide ore of zinc and lead.

40. The process of claim 26 wherein the portion of the essentially lead-free solution to be passed into the anolyte compartment is subjected to a sulfate removal step by reaction with an oxygen-containing gas at a temperature of 85°

-120°

C., thereby forming a sulfate-containing solid;

the thus-formed solid is removed from the liquor; and

the sulfate-depleted liquor is then passed into the anolyte compartment.

41. The process of claim 1 wherein the oxidizing reaction in the solubilization stage is conducted for a period of time sufficiently short that substantial solubilization of the lead content of the treated material is accomplished and, simultaneously, only minimal solubilization of the zinc content thereof occurs.

42. The process of claim 1, wherein iron is separated from said second portion of the essentially lead free solution by introducing the latter into an electrolysis cell where metallic iron is recovered and ferric chloride is regenerated in said solution by electrolysis of the ferrous chloride-containing electrolyte;

and wherein said solution is then passed into the catholyte compartment of said Zn°

producing electrolysis stage.