Process for recovering metals from coal liquefaction residue containing spent catalysts

• US 8,628,735 B2
• Filed: 03/25/2010
• Issued: 01/14/2014
• Est. Priority Date: 03/25/2009
• Status: Active Grant

• Current Assignee: Chevron USA Incorporated (Chevron Corp.)
• Original Assignee: Chevron USA Incorporated (Chevron Corp.)
• Inventors: Bhaduri, Rahul S.
• Primary Examiner(s): Mayes, Melvin C
• Assistant Examiner(s): SWAIN, MELISSA STALDER
• Application Number:
  US12/732,136
• Publication Number:
  US 20100300250A1
• Time in Patent Office: 1,391 Days
• Field of Search: 423/53
• US Class Current: 423/53
• CPC Class Codes: C22B 3/06 in inorganic acid solutions , e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
• 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: C22B 34/225 from spent catalysts
• CPC Class Codes: C22B 34/345 from spent catalysts
• CPC Class Codes: C22B 7/006 Wet processes
• CPC Class Codes: C22B 7/009 General processes for recovering metals or metallic compounds from spent catalysts for recovering specific metals C22B11/00 - C22B61/00
• CPC Class Codes: Y02P 10/20 Recycling

Abstract

In one embodiment, this invention is directed to a method of recovering metals from a metals bearing material comprising: reducing the particle size of at least a portion of the metals bearing material; mixing the metals bearing material in an acid solution to form a first slurry containing at least alkaline earth metal compounds; separating the at least alkaline earth metal compounds from the first slurry to form a first filtrate and a metals bearing material; leaching metals from the metals bearing material to form a pressure leach solution containing transition metals; precipitating and recovering transition metals from the pressure leach solution. In another aspect, the invention relates to a method for recovering metals from a deoiled and dried coal liquefaction residue that contains spent catalyst originating from a Group VIB metal sulfide catalyst.

Claims

1. A method of recovering metals from a coal liquefaction residue containing a spent catalyst comprising:

(a) deoiling and drying the coal liquefaction residue to form an ash feed;

(b) reducing the particle size of the ash feed;

(c) mixing the ash feed in a weak acid solution to form a first slurry containing at least alkaline earth metal compounds;

(d) separating the at least alkaline earth metal compounds from the first slurry to form a first filtrate and a metals bearing material;

(e) pressure leaching metals from the metals bearing material in the presence of ammonia and air to form a pressure leach slurry containing transition metals;

(f) precipitating and recovering transition metals from the pressure leach slurry.

2. The method of claim 1 wherein step (b) comprises comminution of the ash feed to a particle size distribution wherein at least 70% of the metal bearing materials passes 200-mesh.

3. The method of claim 1 wherein a coal liquefaction residue comprises inorganic material, ash and a spent catalyst.

4. The method of claim 3 wherein the spent catalyst comprises one or more transition metals selected from the group consisting of Group VIB metals and sulfides thereof.

5. The method of claim 4 wherein the spent catalyst comprises molybdenum.

6. The method of claim 1 wherein the ash feed contains about 0.1% to 10% molybdenum by weight.

7. The method of claim 1 wherein the acid solution of step (c) is a weak acid solution selected from the group consisting of weak solutions of sulfuric acid, nitric acid, hydrochloric acid and phosphoric acid.

8. The method of claim 1, wherein the weak acid solution of step (c) is a water-soluble organic acid selected from the group consisting of formic acid, acetic acid, propionic acid, sulfamic acid and trichloro-acetic acid.

9. The method of claim 1 wherein step (c) is carried out at a temperature 35°

C. and 80°

C. for a time between about 1 to 4 hours.

10. The method of claim 9 wherein at least 70% of the at least alkaline earth metal compounds of step (c) are dissolved.

11. The method of claim 1 wherein the first filtrate of step (d) comprises solubilized alkaline earth metals and materials consisting of ash, insoluble organic matter and spent catalyst.

12. The method of claim 11 wherein the solubilized alkaline earth metals are precipitated from the first filtrate by contacting the first filtrate, in the presence of air, with a phosphate at a pH of about neutral.

13. The method of claim 12 wherein the phosphate is selected from the group consisting of ammonium phosphate, potassium phosphate and sodium phosphate.

14. The method of claim 13 the phosphate strength ranges from about 0.5 to 5.0 normal.

15. The method of claim 1 wherein the coal liquefaction residue comprises 0.1 to 10% Mo by weight.

16. The method of claim 15 wherein the coal liquefaction residue comprises 40 to 60% by weight insoluble organic matter and is 40 to 60% by weight ash.

17. The method of claim 16 wherein the ash comprises between 1-5 wt. % Al, 1-3 wt. % Ba, 2-10 wt. % Ca, 1-5 wt. % Fe, 1-5 wt. % Na, 3-10 wt. % Si and 40-60 wt. % C.

18. The method of claim 1 wherein step (e) further comprises forming the pressure leach solution in an autoclave in the presence of ammonia and air, at a pressure and a temperature sufficient to produce leaching reactions and forming soluble complexes of Group VIB transition metals.

19. The method of claim 18 wherein step (e) wherein at least 70% of the Group VIB transition metals are leached into solution.

20. The method of claim 19 wherein the Group VIB transition metal is molybdenum and wherein at least 75 wt. % of said molybdenum is leached into solution in the form of ammonium molybdate.

21. The method of claim 18 wherein the pressure and the temperature within the autoclave respectively range between 120°

C. to 250°

C. and from 0 psig to 1200 psig.

22. The method of claim 21 wherein the pressure and the temperature within the autoclave respectively range between 135°

C. to 225°

C. and from 100 psig to 1000 psig.

23. The method of claim 21 or claim 22 further comprising a leaching time between 60 minutes to 360 minutes.

24. The method of claim 1 wherein step (e) further comprises passing the pressure leach slurry to a liquid solids separation step selected from the group consisting of settling, centrifugation, decantation and filtration to form a pressure leach residue comprising ash and insoluble organic matter and a pressure leach filtrate comprising Group VIB metal complexes and ammonium sulfate.

25. The method of claim 24 wherein the liquid solids separation step comprises filtration by a method selected from the group consisting of vertical centrifugation, vacuum filter, plate and frame filter and pressure belt filter.

26. The method of claim 24 wherein the pressure leach filtrate is passed to an acid precipitation step wherein a strong mineral acid is added to the pressure leach filtrate to achieve a preselected pH to effect precipitation of at least 90% of the Group VIB metals to form a Group VIB metal slurry.

27. The method of claim 26 wherein the preselected pH is 3.5 to effect precipitation of at least 90% of a molybdenum complex contained in said pressure leach filtrate.

28. The method of claim 26 wherein the Group VIB metal precipitated is tungsten and the preselected pH ranges from 1.0 to about 2.0 to effect precipitation of at least 95% of the soluble tungsten complexes.

29. The method of claim 26 wherein the strong mineral acid is selected from the group consisting of sulfuric acid, hydrochloric acid, phosphoric acid and nitric acid.

30. The method of claim 26 wherein the Group VIB metal slurry is passed to a solid liquid separation step selected from the group consisting of settling, filtration, decantation, centrifugation, and combinations thereof to form a Group VIB metals precipitate and an ammonium sulfate filtrate.

31. A method of claim 30 wherein the Group VIB metals precipitate comprises 50 to 80 wt. % molybdenum, not more than one wt. % vanadium, less than 20 wt. % ammonium sulfate and 1 to 10 wt. % sulfur.

32. The method of claim 30 wherein the ammonium sulfate filtrate is substantially free of Group VIB metal complexes.

33. The method of claim 30 wherein the ammonium sulfate filtrate comprises from 0.1 to 3% of the Group VIB metals contained in the metals bearing materials.