Adaptable processes and systems for purifying co-precipitated or independent streams of manganese, nickel, and cobalt from lithium-ion battery waste streams
Flexible processes and systems for recovering manganese (Mn), cobalt (Co), nickel (Ni) as a purified co-precipitated product or alternatively independent products, from a lithium-ion battery waste stream are provided. The process may include upstream leaching and impurity removal prior to separation in a metal recovery system that may include a manganese (Mn) recovery unit to generate a manganese (Mn)-containing product, a cobalt (Co) recovery unit to generate a cobalt (Co)-containing product or a nickel (Ni) recovery unit to generate a nickel (Ni)-containing product or alternatively and optionally may include a co-precipitator unit to form a co-precipitated product. A lithium (Li) recovery unit may further process a portion of the waste liquid stream to form a lithium (Li)-containing product.
1. A process for recovering manganese (Mn), cobalt (Co), and nickel (Ni) from a lithium-ion battery waste stream, the process comprising:
processing a waste liquid stream comprising manganese (Mn), nickel (Ni), and cobalt (Co) originating from the lithium-ion battery waste stream in a system having a first metal recovery unit and a second metal recovery unit, the second metal recovery unit including a manganese (Mn) recovery unit to recover a first product comprising manganese (Mn), a nickel (Ni) recovery unit to recover a second product comprising nickel (Ni), and a cobalt (Co) recovery unit to recover a third product comprising cobalt (Co), by either recovering a co-precipitated product comprising manganese (Mn), nickel (Ni), and cobalt (Co) in the first metal recovery unit or recovering the first product comprising manganese (Mn), the second product comprising nickel (Ni), and the third product comprising (Co) in the second metal recovery unit, wherein:
(a) the recovering the co-precipitated product in the first metal recovery unit comprises separating the manganese (Mn), nickel (Ni), and cobalt (Co) from the waste liquid stream by conducting a co-precipitation process in a reactor by increasing pH to greater than or equal to about 10 to form a precipitated solid and separating the precipitated solid from the waste liquid stream to recover the co-precipitated product comprising manganese (Mn), nickel (Ni), and cobalt (Co); or
(b) the recovering the first product comprising manganese (Mn), the second product comprising nickel (Ni), and the third product comprising (Co) in the second metal recovery unit comprises separating manganese (Mn) from the waste liquid stream to form the first product comprising manganese (Mn) by a process comprising:
(i) introducing a first oxidant to the waste liquid stream to form solid manganese dioxide (MnO 2 );
(ii) reacting the waste liquid stream with ozone (O 3 ) to form solid manganese dioxide (MnO 2 ); or
(iii) both (i) and (ii); and
separating the solid manganese dioxide (MnO 2 ) from the waste liquid stream to recover the first product comprising manganese (Mn); and
separating nickel (Ni) and cobalt (Co) from the waste liquid stream by:
(iv) adding sulfuric acid (H 2 SO 4 ) and a second oxidant to treat the waste liquid stream, followed by adjusting pH to greater than or equal to about 4, adding sodium hypochlorite (NaClO) to form cobalt oxyhydroxide (COOH), passing the waste liquid stream through a first filter to form a first retentate comprising cobalt oxyhydroxide (COOH) and a first filtrate comprising nickel (Ni) and liquid;
(v) recovering cobalt (Co) from the first retentate by purifying the cobalt oxyhydroxide (COOH) in the first retentate and adding sulfuric acid (H 2 SO 4 ) and a third oxidant to the first retentate, followed by adjusting pH to greater than or equal to about 4, then by adding NaClO and finally passing the first retentate through a second filter to form a second retentate comprising cobalt oxyhydroxide (COOH); and
(vi) recovering cobalt (Co) from the second retentate by purifying the cobalt oxyhydroxide (COOH) in the second retentate by adding sulfuric acid (H 2 SO 4 ) and a fourth oxidant to the second retentate to form cobalt sulfate (CoSO 4 ), followed by one or more of the following processes to form the third product comprising (Co):
a. removing liquid from the second retentate to recover cobalt sulfate (CoSO 4 ); and/or
b. adjusting pH of the second retentate to greater than or equal to about 9 to precipitate a cobalt hydroxide product comprising one or more of cobalt hydroxide (Co(OH) 2 ) or cobalt oxyhydroxide (COOH); and
(vii) recovering nickel (Ni) from the first filtrate as the second product comprising nickel (Ni) by one of the following processes:
a. removing liquid from the first filtrate to recover nickel sulfate (NiSO 4 ); and
b. adjusting the pH of the first filtrate to be greater than or equal to about 9 to precipitate nickel hydroxide (Ni(OH) 2 ).
2. The process of claim 1 , wherein the recovering nickel (Ni) as the second product comprising nickel (Ni) by the (b) adjusting the pH of the first filtrate to be greater than or equal to about 9 to precipitate nickel hydroxide (Ni(OH) 2 ) further comprises adding sulfuric acid (H 2 SO 4 ) and a fifth oxidant to treat the nickel hydroxide (Ni(OH) 2 ) to form nickel sulfate (NiSO 4 ), followed by removing liquid to recover nickel sulfate (NiSO 4 ).
3. The process of claim 1 , wherein the waste liquid stream further comprises lithium (Li) and prior to the (iv) adding sulfuric acid (H 2 SO 4 ) and the second oxidant to the waste liquid stream, co-precipitating nickel (Ni) and cobalt (Co) by increasing pH of the waste liquid stream to greater than or equal to about 9 to precipitate nickel hydroxide (Ni(OH) 2 ) and cobalt hydroxide (Co(OH) 2 ), passing the waste liquid stream through a third filter to generate a third retentate that is processed during (iv) comprising nickel hydroxide (Ni(OH) 2 ) and cobalt hydroxide (Co(OH) 2 ) and a third filtrate comprising lithium (Li).
4. The process of claim 1 , wherein the first oxidant is selected from the group consisting of: potassium permanganate (KMnO 4 ), sodium permanganate (NaMnO 4 ), and combinations thereof.
5. The process of claim 4 , wherein the first oxidant comprises potassium permanganate (KMnO 4 ) and is selected to be less than or equal to about 95% of a stoichiometric amount in a reaction between the potassium permanganate (KMnO 4 ) and manganese sulfate (MnSO 4 ).
6. The process of claim 1 , wherein the second oxidant comprises hydrogen peroxide (H 2 O 2 ).
7. The process of claim 1 , wherein the separating of manganese (Mn) comprises (iii) both (i) the introducing the first oxidant to the waste liquid stream to form a first amount of manganese dioxide (MnO 2 ) and (ii) the reacting the waste liquid stream with ozone (O 3 ) to form a second amount of manganese dioxide (MnO 2 ).
8. The process of claim 7 , wherein about 95% of manganese is removed from the waste liquid stream during (i) and about 5% of manganese is removed from the waste liquid stream during (ii).
9. The process of claim 1 , wherein the separating of manganese (Mn) further comprises passing the waste liquid stream through a third filter to separate and recover manganese dioxide (MnO 2 ).
10. The process of claim 1 , wherein (i) the introducing the first oxidant to the waste liquid stream further comprises adjusting a pH of the waste liquid stream to greater than or equal to about 1.5 to less than or equal to about 3.
11. The process of claim 1 , wherein the (iv) adding sulfuric acid (H 2 SO 4 ) and the second oxidant to the waste liquid stream, followed by adjusting pH to greater than or equal to about 4, further comprises adding sodium hydroxide (NaOH) to the waste liquid stream followed by the adding the sodium hypochlorite (NaClO) and stirring for greater than or equal to about 1 hour, where the waste liquid stream has a temperature of greater than or equal to about 50° C. to less than or equal to about 60° C.
12. The process of claim 11 , wherein after the passing the first retentate through the second filter to form the second retentate, washing the second retentate with water at a temperature of greater than or equal to about 50° C. to less than or equal to about 75° C. to remove residual nickel (Ni) from the cobalt oxyhydroxide (COOH).
13. The process of claim 11 , wherein after the passing the first retentate through the second filter to form the second retentate, washing the second retentate with a sulfuric acid wash about 30 minutes to remove any residual nickel (Ni) from the cobalt oxyhydroxide (CoOOH).
14. The process of claim 1 , wherein the separating manganese (Mn) from the waste liquid stream results in the first product comprising manganese (Mn) at a purity level of greater than or equal to about 98%, the (v) recovering cobalt (Co) from the second retentate results in the second product comprising cobalt (Co) at a purity level of greater than or equal to about 98%, and the (vii) recovering nickel (Ni) from the second filtrate results in the third product comprising nickel (Ni) at a purity level of greater than or equal to about 99%.
15. A process for recovering manganese (Mn), cobalt (Co), and nickel (Ni) from a lithium-ion battery waste stream, the process comprising:
purifying a waste liquid stream originating from the lithium-ion battery waste stream, wherein the waste liquid stream comprises sulfuric acid (H 2 SO 4 ), manganese (Mn), cobalt (Co), and nickel (Ni) to remove fluorine (F), phosphorous (P), and one or more impurity metals selected from the group consisting of: copper (Cu), iron (Fe), zinc (Zn), aluminum (Al), and titanium (Ti), wherein the purifying includes:
(i) removing copper (Cu), iron (Fe), and zinc (Zn) from the waste liquid stream by a solvent extraction process;
(ii) adding a source of calcium oxide and a first oxidant to the waste liquid stream to remove fluorine (F) by precipitating calcium fluoride (CaF 2 ); and
(iii) adjusting pH of the waste liquid stream to greater than or equal to about 3 to less than or equal to about 5 for a first duration and further adjusting pH of the waste liquid stream to greater than or equal to about 4.8 to less than or equal to about 7.2 to remove one or more impurity compounds comprising an element selected from the group consisting of: copper (Cu), iron (Fe), zinc (Zn), aluminum (Al), and titanium (Ti), phosphorus (P), and lead (Pb), and combinations thereof;
processing the waste liquid stream in a system having a first metal recovery unit and a second metal recovery unit, the second metal recovery unit including a manganese (Mn) recovery unit to recover a first product comprising manganese (Mn), a nickel (Ni) recovery unit to recover a second product comprising nickel (Ni), and a cobalt (Co) recovery unit to recover a third product comprising cobalt (Co), by either recovering a co-precipitated product comprising manganese (Mn), nickel (Ni), and cobalt (Co) in the first metal recovery unit or recovering the first product comprising manganese (Mn), the second product comprising nickel (Ni), and the third product comprising (Co) in the second metal recovery unit, wherein:
the recovering the co-precipitated product in the first metal recovery unit comprises separating the manganese (Mn), nickel (Ni), and cobalt (Co) from the waste liquid stream by conducting a co-precipitation process in a reactor by increasing pH to greater than or equal to about to form a precipitated solid and separating the precipitated solid from the waste liquid stream to recover the co-precipitated product comprising manganese (Mn), nickel (Ni), and cobalt (Co); or
the recovering the first product comprising manganese (Mn), the second product comprising nickel (Ni), and the third product comprising (Co) in the second metal recovery unit comprises separating manganese (Mn) from the waste liquid stream to form the first product comprising manganese (Mn) by a process comprising:
(iv) introducing a second oxidant to the waste liquid stream to form solid manganese dioxide (MnO 2 );
(v) reacting the waste liquid stream with ozone (O 3 ) to form solid manganese dioxide (MnO 2 ); or
(vi) both (iv) and (v);
removing the solid manganese dioxide (MnO 2 ) from the waste liquid stream; and
separating nickel (Ni) and cobalt (Co) from the waste liquid stream by:
(vii) adding sulfuric acid (H 2 SO 4 ) and a third oxidant to the waste liquid stream, followed by adjusting pH to greater than or equal to about 4, adding sodium hypochlorite (NaClO) to form cobalt oxyhydroxide (COOH), passing the waste liquid stream through a first filter to form a first retentate comprising cobalt oxyhydroxide (COOH) and a first filtrate comprising nickel (Ni) and liquid;
(viii) recovering cobalt (Co) from the first retentate by purifying the cobalt oxyhydroxide (COOH) in the first retentate and adding sulfuric acid (H 2 SO 4 ) and a fourth oxidant to the first retentate followed by adjusting pH to greater than or equal to about 4, passing the first retentate through a second filter to form a second retentate comprising cobalt oxyhydroxide (COOH) and a second filtrate; and
(ix) recovering cobalt (Co) from the second retentate by purifying the cobalt oxyhydroxide (COOH) in the second retentate by adding sulfuric acid (H 2 SO 4 ) and a fifth oxidant to the second retentate to form cobalt sulfate (CoSO 4 ), followed by one or more of the following processes to form the third product comprising (Co):
a. removing liquid from the second retentate to recover cobalt sulfate (CoSO 4 ); and/or
b. adjusting pH of the second retentate to greater than or equal to about 9 to precipitate a cobalt hydroxide product comprising one or more of cobalt hydroxide (Co(OH) 2 ) or cobalt oxyhydroxide (COOH);
(x) recovering nickel (Ni) from the second filtrate as the second product comprising nickel (Ni) by one of the following processes:
c. removing liquid from the second filtrate to recover nickel sulfate (NiSO 4 ); and/or
d. adjusting pH of the second filtrate to greater than or equal to about 9 to precipitate nickel hydroxide (Ni(OH) 2 ).
16. The process of claim 15 , wherein the second oxidant is selected from the group consisting of: potassium permanganate (KMnO 4 ), sodium permanganate (NaMnO 4 ), and combinations thereof and the first oxidant, the third oxidant, the fourth oxidant, and the fifth oxidant are independently selected from the group consisting of: hydrogen peroxide (H 2 O 2 ), ozone (O 3 ), sodium hypochlorite (NaClO), and combinations thereof.
17. The process of claim 15 , wherein during the introducing the second oxidant to the waste liquid stream, a pH of the waste liquid stream is adjusted to be greater than or equal to about 1.5 to less than or equal to about 3.
18. The process of claim 15 , wherein the removing the solid manganese dioxide (MnO 2 ) from the waste liquid stream further comprises passing the waste liquid stream through a third filter to separate and recover the solid manganese dioxide (MnO 2 ).
19. The process of claim 15 , wherein the waste liquid stream further comprises lithium (Li), wherein prior to (vii) adding sulfuric acid (H 2 SO 4 ) and a second oxidant to the waste liquid stream, co-precipitating nickel (Ni) and cobalt (Co) by increasing pH of the waste liquid stream to greater than or equal to about 9 to precipitate nickel hydroxide (Ni(OH) 2 ) and cobalt hydroxide (Co(OH) 2 ), passing the waste liquid stream through a third filter to generate a third retentate comprising nickel hydroxide (Ni(OH) 2 ) and cobalt hydroxide (Co(OH) 2 ) that is processed during (vii) and a third filtrate comprising lithium (Li).
20. The process of claim 19 , wherein the co-precipitating nickel (Ni) and cobalt (Co) occurs in an inert atmosphere.
21. The process of claim 19 , further comprising recovering lithium (Li) by further processing the third filtrate to form at least one compound comprising lithium (Li) by concentrating lithium (Li) and adding sodium carbonate (Na 2 CO 3 ) to precipitate lithium carbonate (Li 2 CO 3 ).
22. The process of claim 15 , wherein the (vii) adding sulfuric acid (H 2 SO 4 ) and the third oxidant to the waste liquid stream, followed by the adjusting pH to greater than or equal to about 4, further comprises adding sodium hydroxide (NaOH) followed by adding the sodium hypochlorite (NaClO) and stirring for greater than or equal to about 1 hour where the waste liquid stream has a temperature of greater than or equal to about 50° C. to less than or equal to about 60° C.
23. The process of claim 22 , wherein after the passing the waste liquid stream through the first filter to form the first retentate comprising cobalt oxyhydroxide (CoOOH), conducting at least one of: washing the first retentate with water to remove residual nickel (Ni) at a temperature of greater than or equal to about 50° C. to less than or equal to about 75° C.; or washing the second retentate with a sulfuric acid wash for greater than or equal to about 30 minutes to remove any residual nickel (Ni).
24. The process of claim 15 , wherein the solvent extraction process further comprises first mixing the waste liquid stream with a first extractant and a first organic phase to remove copper (Cu) and then mixing the waste liquid stream with a second extractant and a second organic phase to remove at least iron (Fe) and zinc (Zn).
25. The process of claim 24 , wherein the first extractant comprises 2-hydroxy-5-nonylbenzaldehyde oxime, the second extractant comprises bis-(2-ethylhexyl) phosphoric acid and the first organic phase and the second organic phase are independently selected from the group consisting of: kerosene, sulfonated kerosene, hexane, and combinations thereof.
26. The process of claim 15 , wherein the separating manganese (Mn) from the waste liquid stream results in the first product comprising manganese (Mn) at a purity level of greater than or equal to about 98%, the recovering cobalt (Co) from the second retentate results in the second product comprising cobalt (Co) at a purity level of greater than or equal to about 98%, and the recovering nickel (Ni) from the second filtrate results in the third product comprising nickel (Ni) at a purity level of greater than or equal to about 99% and a separation efficiency for each of copper (Cu), iron (Fe), and zinc (Zn) is respectively greater than or equal to about 98% and a separation efficiency for fluorine is greater than or equal to about 99%.
27. The process of claim 15 , wherein the purifying the lithium-ion battery waste liquid stream further comprises after the (iii) adjusting pH of the waste liquid stream to greater than or equal to about 3 to less than or equal to about 5, the purifying further comprises adjusting the pH to be less than or equal to about 2.5 and conducting a deep impurity removal process to remove additional amounts of one or more of: copper (Cu), iron (Fe), zinc (Zn), and aluminum (Al) from the waste liquid stream by solvent extraction.
28. The process of claim 15 , wherein the purifying the lithium-ion battery waste liquid stream further comprises prior to the (i) removing copper (Cu), iron (Fe), and zinc (Zn) from the waste liquid stream by the solvent extraction process, removing an initial amount of aluminum (Al) by increasing a pH of the waste liquid stream to precipitate an aluminum compound and separating the aluminum compound from the waste liquid stream.
29. The process of claim 15 , wherein the waste liquid stream further comprises carbon-based compounds and the purifying the lithium-ion battery waste liquid stream further comprises prior to the (i) removing copper (Cu), iron (Fe), and zinc (Zn) from the waste liquid stream by the solvent extraction process, removing the carbon-based compounds by adding sulfuric acid (H 2 SO 4 ) and a sixth oxidant to the waste liquid stream, followed by passing the waste liquid stream through a third filter to remove the carbon-based compounds from the waste liquid stream by forming a third filtrate that comprises the waste liquid stream and a third retentate comprising the carbon-based compounds.
30. A system for recovering manganese (Mn), cobalt (Co), and nickel (Ni) from a lithium-ion battery waste stream, the system comprising:
a first metal recovery unit configured to recover a co-precipitated product comprising manganese (Mn), nickel (Ni), and cobalt (Co) from a waste liquid stream originating from the lithium-ion battery waste stream comprising manganese (Mn), nickel (Ni), and cobalt (Co), the first metal recovery unit comprising:
a co-precipitation reactor that comprises:
a plurality of co-precipitation reactor inlets that receive the waste liquid stream, a chelating agent, and sodium hydroxide (NaOH);
a co-precipitation reactor agitator; and
at least one co-precipitation reactor outlet, wherein the co-precipitation reactor is in thermal communication with a heat source and is configured to generate a co-precipitated product comprising manganese (Mn), nickel (Ni), and cobalt (Co);
a second metal recovery unit configured to recover a first product comprising manganese (Mn) in a manganese (Mn) recovery unit, a second product comprising nickel (Ni) in a nickel (Ni) recovery unit, and a third product comprising cobalt (Co) in a cobalt (Co) recovery unit, wherein:
the manganese (Mn) recovery unit comprises at least one first reactor, a source of a first oxidant selected from the group consisting of: potassium permanganate (KMnO 4 ), sodium permanganate (NaMnO 4 ), and combinations thereof, a source of ozone (O 3 ), a first filter downstream of the at least one first reactor, wherein the at least one first reactor has a plurality of first inlets receiving the first oxidant, the ozone (O 3 ), and the waste liquid stream, a first agitator, and a first outlet through which the waste liquid stream exits to enter the first filter for separation into a first filtrate and a first retentate comprising manganese dioxide (MnO 2 );
a separation unit that receives the first filtrate, the separation unit having a separation reactor, a second filter downstream of the separation reactor, a source of a first base, a source of a first acid, a source of a second oxidant, and a source of sodium hypochlorite (NaClO), wherein the separation reactor has a plurality of second inlets receiving the first base, the first acid, the second oxidant, the sodium hypochlorite (NaClO), and the first filtrate, a second agitator, and a second outlet through which the first filtrate exits to enter a second filter for separation into a second filtrate and a second retentate comprising cobalt oxyhydroxide (COOH);
a cobalt (Co) recovery unit downstream of the separation unit that receives the second retentate comprising cobalt oxyhydroxide (COOH), the cobalt (Co) recovery unit comprising:
a source of at least a second acid,
a source of a third oxidant,
at least a third reactor having a plurality of third inlets receiving the second acid, the third oxidant, and the second retentate, a third agitator, and a third outlet through which the second retentate exits,
one or more cobalt (Co) processing units downstream from the at least a third reactor selected from:
(i) one or more chromatographic columns for separating nickel (Ni) from cobalt (Co);
(ii) a first evaporator or crystallizer to form cobalt sulfate (CoSO 4 ); and/or
(iii) a first precipitator to form a cobalt hydroxide product comprising one or more of cobalt hydroxide (Co(OH) 2 ) or cobalt oxyhydroxide (COOH); and
a nickel (Ni) recovery unit downstream of the separation unit that receives the second filtrate, the nickel (Ni) recovery unit comprising one or more of:
a second evaporator/crystallizer to form nickel sulfate (NiSO 4 );
a precipitator reactor to form nickel hydroxide (Ni(OH) 2 ); and/or
at least a fourth reactor to form nickel sulfate (NiSO 4 ) having a plurality of fourth inlets receiving Ni(OH) 2 , a third acid, and a fourth oxidant, a fourth agitator, and a fourth outlet through which a stream comprising nickel sulfate (NiSO 4 ) exits;
a fluid conduit system for establishing fluid communication within the first metal recovery unit including the co-precipitation reactor and the second metal recovery unit including the manganese (Mn) recovery unit, the separation unit, the cobalt (Co) recovery unit, and the nickel (Ni) recovery unit; and at least one pump for circulating fluids within the fluid conduit system.