Process for metals recovery from spent catalyst

• US 7,736,607 B2
• Filed: 12/30/2008
• Issued: 06/15/2010
• Est. Priority Date: 07/29/2005
• Status: Expired due to Fees

• Current Assignee: Chevron USA Incorporated (Chevron Corp.)
• Original Assignee: Chevron USA Incorporated (Chevron Corp.)
• Inventors: Marcantonio, Paul J.
• Primary Examiner(s): BOS, STEVEN J
• Application Number:
  US12/345,798
• Publication Number:
  US 20090110620A1
• Time in Patent Office: 532 Days
• Field of Search: 423 54- 56, 423/67, 423/68, 423/87, 423/139, 423/146, 423/306
• US Class Current: 423/54
• CPC Class Codes: C22B 23/0461 by chemical methods
• CPC Class Codes: C22B 3/26 by liquid-liquid extraction using organic compounds
• 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: Y02P 10/20 Recycling
• CPC Class Codes: Y02W 10/40 Valorisation of by-products of wastewater, sewage or sludge processing

Abstract

The process of this invention is directed to the removal of metals from an unsupported spent catalyst. The catalyst is subjected to leaching reactions. Vanadium is removed as a precipitate, while a solution comprising molybdenum and nickel is subjected to further extraction steps for the removal of these metals. Molybdenum may alternately be removed through precipitation.

Claims

1. A method for recovering vanadium, nickel and molybdenum from a spent unsupported catalyst that has been used in a hydroprocessing process, said method comprising the steps of:

a) treating said spent unsupported catalyst with an aqueous solvent and an oxidizer in a leaching zone at leaching conditions;

b) passing the effluent of step (a), which comprises liquid and solid material to a filtration zone, from which solid material is recovered as a filter cake and a liquid material is generated;

c) passing the filter cake of step (b), which comprises ammonium metavanadate to a dissolution zone, to which ammonia is added under dissolution conditions;

d) passing the effluent of step (c) to a first filtration zone for removal of coke contaminants;

e) passing the effluent of step (d) to a crystallization zone, wherein the effluent is adjusted for pH and ammonium metavanadate crystallizes as a solid;

f) passing the effluent of step (e) to a second filtration zone for the removal of ammonium metavanadate solid;

g) passing the liquid material of step (b), which comprises an aqueous phase and an organic phase, to a mixer-settler zone;

h) separating the aqueous phase of step (g), which comprises molybdenum, from the organic phase, which comprises nickel;

i) subjecting the organic phase of step (h), which remains in the mixer-settler zone, to at least one cycle of extraction, scrubbing and stripping prior to the removal of nickel sulfate solution as product;

j) removing molybdenum compounds from the aqueous phase of step (h) by solvent extraction or precipitation.

2. The method of claim 1, wherein the unsupported catalyst is washed or deoiled to remove hydrocarbon feed and product oils prior to the step of treating said catalyst with an aqueous solvent.

3. The process of claim 2, wherein the catalyst is deoiled using an organic solvent in an inert atmosphere.

4. The process of claim 3, wherein the organic solvent is selected from the group consisting of toluene, xylene and kerosene.

5. The process of claim 1, wherein the leaching zone is an autoclave, the aqueous solvent comprises ammonia, and the oxidizer comprises oxygen.

6. The process of claim 1, wherein leaching reactions occur at a temperature in the range between 20°

C. and 315°

C., a pressure in the range between 0 psig and 1200 psig, and a pH in the range from 7 to 12.

7. The process of claim 1, wherein the liquid material of step (b) is treated with a kerosene diluent for organic carbon removal prior to step (h).

8. The process of claim 1, wherein conditions of step (i) comprise a temperature in the range from about 20°

C. through about 50°

C., and a pH in the range from 7 through 12.

9. The process of claim 1, wherein the liquid material of step (b) is contacted with a lean organic solution which comprises oxime and kerosene.

10. The process of claim 9, wherein the oxime is a ketoxime.

11. The process of claim 10, wherein the ketoxime is 2-hydroxy-5-nonylacetophenone oxime.

12. The process of claim 1, wherein the liquid material of step (b) is contacted with a lean organic solution.

13. The process of claim 12, wherein the liquid material of step (b) is contacted countercurrently with a lean organic solution.

14. The process of claim 1, wherein the organic phase of step (h) is contacted currently during scrubbing and stripping in the mixer-settler zone with sulphuric acid.

15. The process of claim 1, wherein the aqueous phase of step (h) is pretreated by adjustment to a basic pH, followed by contact with magnesium sulfate in order to remove magnesium and phosphorus, prior to solvent extraction of molybdenum.

16. The process of claim 14, in which arsenic is removed as magnesium ammonia arsenic oxide and phosphorus is removed as magnesium ammonia phosphate.

17. The process of claim 1, in which the removal of molybdenum from the aqueous phase by solvent extraction further comprises:

mixing the aqueous phase with sulfuric acid in order to obtain a pH in the range from about 2 to about 7;

crystallizing ammonium molybdate solid from the aqueous phase and separating it from the remaining liquid;

contacting the remaining liquid countercurrently with a lean solution of a water soluble, saturated, straight chain amine solvent in admixture with isodecanol and kerosene, thereby creating an aqueous phase and an organic phase, the molybdenum being extracted into the organic phase;

separating the aqueous and organic phases;

contacting the organic solution countercurrently with a concentrated ammonia solution in at least one mixer settler zone; and

recovering ammonium molybdate as product.

18. The process of claim 17, where the straight chain alkyl groups of the solvent are a mixture of C₈ and C₁₀ amines, with the C₈ carbon chain predominating 2:

1.

19. The process of claim 1, in which the removal of molybdenum from the aqueous phase by precipitation further comprises:

i) passing the aqueous phase to a crystallization zone for the removal of one or more contaminants by precipitation;

ii) passing the effluent of step (a) to a filtration zone, where an aqueous solution comprising ammonium molybdate is recovered, as well as a filtrate;

iii) contacting the aqueous solution comprising ammonium molybdate with H₂S in a molybdenum precipitation zone, there by obtaining a precipitate comprising molybdenum disulfide and a liquid supernatant;

iv) passing the precipitate comprising molybdenum disulfide and the supernatant to a filtration zone, generating a supernatant and a precipitate which is removed as a solid;

v) passing the supernatant of step (iv) to an oxidation zone, where it is contacted with oxygen and ammonia;

vi) passing the effluent of step (v) to a molybdenum remix zone, where it is combined with the filtrate of step (ii), the mixture being contacted with ammonia and water to produce a product comprising ammonium molybdate.

20. The process of claim 19, wherein the contaminants are selected from the group consisting of arsenic and phosphorus and the ammonium molybdate product comprises octomolybdates.