Process for recovery of lithium from brine

1. A process for recovery of lithium ions from a lithium-bearing brine, the process comprising:

contacting the lithium-bearing brine with a lithium ion sieve in a first reactor to form a lithium ion complex with the lithium ion sieve;

separating the lithium ion complex with the lithium ion sieve from the brine with a solid/liquid separation device;

contacting the lithium ion complex with the lithium ion sieve with water before decomplexing in a second reactor; and

decomplexing lithium ions from the lithium ion sieve in the second reactor to form an acidic lithium salt eluate solution separated from the lithium ion sieve;

separating the lithium ion sieve from the acidic lithium salt eluate solution with a solid/liquid separation device;

contacting the lithium ion sieve with water after decomplexing in the second reactor to obtain a regenerated lithium ion sieve and a dilute acid water wash;

wherein the lithium ion sieve comprises an oxide of titanium or niobium;

wherein a pH of the first reactor is maintained at a constant value through addition of an alkali comprising anhydrous ammonia or ammonium hydroxide;

wherein the decomplexing is performed by elution using an acid;

wherein an average contact time of the lithium ion complex with the lithium ion sieve and the acid is less than 1 hour;

wherein a concentration of the acid is maintained at a constant value through additions of said acid; and

wherein the concentration of the acid is less than 0.1 M.

2. The process of claim 1 , wherein the pH of the acid is greater than 1 and less than 3.

3. The process of claim 1 , wherein the pH of the acid is approximately 2.

4. The process of claim 1 , wherein the pH is maintained at the constant value of greater than 4 and less than 9.

5. The process of claim 1 , wherein the pH in the first reactor is greater than 6 and less than 8.

6. The process of claim 1 , wherein more than 90% of the lithium ion sieves have an average particle diameter of less than 40 μm and more than 90% of the lithium ion sieves have an average particle diameter of greater than 0.4 μm.

7. The process of claim 6 , further comprising removing lithium ion sieves having an average particle diameter of less than 1 μm before contacting the lithium-bearing brine with the lithium ion sieve.

8. The process of claim 1 , wherein more than 90% by volume of particles of the lithium ion sieve are less than 100 μm in diameter and greater than 0.5 μm in diameter.

9. The process of claim 1 , wherein more than 90% by volume of particles of the lithium ion sieve are greater than 0.5 μm in diameter.

10. The process of claim 1 , wherein the lithium ion sieve comprises metatitanic acid.

11. The process of claim 1 , further comprising:

adding the regenerated lithium ion sieve to the first reactor.

12. The process of claim 11 , further comprising adding the dilute acid water wash and additional concentrated acid to the second reactor.

13. The process of claim 11 , further comprising dewatering the lithium ion complex with the lithium ion sieve to a moisture content of less than 90% by weight before decomplexing the lithium ion from the lithium ion sieve in the second reactor.

14. The process of claim 11 , further comprising dewatering the regenerated lithium ion sieve before being added to the first reactor.

15. The process of claim 11 , wherein contacting the lithium ion sieve with water comprises contacting the lithium ion sieve with sufficient water such that more than 50% of the lithium ion that has been decomplexed from the lithium ion sieve is washed from the lithium ion sieve prior to adding the regenerated lithium ion sieve to the first reactor.

16. The process of claim 15 , wherein contacting the lithium ion sieve with water comprises contacting the lithium ion sieve with water in more than one counter-current stage such that more than 50% of the lithium ion that has been decomplexed from the lithium ion sieve is washed from the lithium ion sieve prior to adding the regenerated lithium ion sieve to the first stirred reactor.

17. The process of claim 1 , wherein the first reactor comprises ultrafiltration or microfiltration membranes.

18. The process of claim 17 , wherein air is used to agitate contents of the first reactor.

19. The process of claim 17 , wherein a flux rate through the ultrafiltration membrane or the microfiltration membrane is greater than 30 LMH at transmembrane pressures of less than 30 kPa.

20. The process of claim 1 , wherein a concentration of the lithium ion sieve is greater than 50 g/L.

21. The process of claim 1 , wherein the alkali further comprises sodium hydroxide, potassium hydroxide, sodium carbonate, magnesium hydroxide, or calcium hydroxide.

22. The process of claim 1 , wherein the acid comprises hydrochloric acid or sulfuric acid.

23. The process of claim 1 , wherein a concentration of the lithium ion sieve is greater than 100 g/L.

24. A process for recovery of lithium ions from a lithium-bearing brine, the process comprising:

contacting the lithium-bearing brine with a lithium ion sieve in a first reactor to form a lithium ion complex with the lithium ion sieve;

separating the lithium ion complex with the lithium ion sieve from the brine with a solid/liquid separation device;

contacting the lithium ion complex with the lithium ion sieve with water before decomplexing in a second reactor; and

decomplexing lithium ions from the lithium ion sieve in the second reactor to form an acidic lithium salt eluate solution separated from the lithium ion sieve;

separating the lithium ion sieve from the acidic lithium salt eluate solution with a solid/liquid separation device;

contacting the lithium ion sieve with water after decomplexing in the second reactor to obtain a regenerated lithium ion sieve and a dilute acid water wash;

wherein the lithium ion sieve comprises an oxide of titanium or niobium;

wherein a pH of the first reactor is maintained at a constant value through addition of an alkali comprising sodium hydroxide at a concentration of 4% to 8% w/w;

wherein a concentration of the acid is maintained at a constant value through additions of said acid; and

wherein the concentration of the acid is less than 0.1 M.