Systems and Methods for Recovering Lithium from Brines Field

Abstract

Systems and methods using solar evaporation to preconcentrate lithium containing brines to at or near lithium saturation, followed by a separation processes to separate lithium from impurities. A separated impurity stream is recycled to a point in the evaporation sequence where conditions are favorable for their precipitation and removal or disposed in a separate evaporation pond or reinjected underground, while a lower impurity stream is transferred to one or more of the removal location, to a subsequent pond in the sequence, or to a lithium plant or concentration facility. Further concentration of lithium by evaporation can then take place because impurities are removed thus eliminating lithium losses due to co-precipitation and achieving significantly higher concentrations of lithium.

Claims

1. A system for efficiently extracting lithium from brines allowing significantly higher lithium recovery, concentration, and production capacity from the same ponds, the method comprising: one or more solar evaporation ponds configured to allow evaporation of brine to occur in each pond and for brine to flow from a first pond to one or more other ponds, or to a process plant for lithium separation; a conduit configured to remove at least a portion of the brine at a brine removal location at one or more of the ponds and transmit the removed brine to a separator whereby one or more impurities are separated from lithium to form a high impurity stream and a low impurity stream; wherein the high impurity stream is optionally recycled to the one or more of the evaporation ponds at a location the same as, upstream from the brine removal location, or disposed in a separate pond or reinjected underground, and the low impurity stream is fed to one or more of the ponds, or to a lithium separation plant, or to a concentration facility.

2. The system according to claim 1, wherein the high impurity stream is recycled to a pond precipitating a salt selected from the group consisting of bischofite, calcium borate, anhydrite, gypsum, carnallite, epsomite, anhydrite, kainite, Glauber's salt, halite, sylvite, sylvinite, schoenite, polyhalite, calcium borate, hexahydrite, kieserite, or others.

3. The system according to claim 1, wherein the low impurity stream is fed to a pond that is substantially free of co-precipitated Li in the form of lithium carnallite, lithium metaborate, lithium sulfate, lithium sulfate monohydrate, lithium potassium double salt, lithium schoenite, or others.

4. The system according to claim 1, wherein the portion of brine removed at the brine removal location comprises preferably 1% to 100%, 5% to 100%, 25% to 100%, or 50% to 100% of the total brine flow in the ponds.

5. The system according to claim 1, wherein the increase in lithium recovery is from about 10 to about 80% (absolute units).

6. The system according to claim 1, wherein the separator is configured to at least partially separate lithium from impurity cations and anions which have a propensity to form lithium salts that can precipitate under further brine concentration, and which impurity cations and anions are suitable for earlier precipitation with each other in a preceding evaporation pond.

7. The system according to claim 1, wherein the separator is a separation selected from the group consisting of a selective ion separation membrane, nanofiltration, ion sorption, ion exchange, solvent extraction, solvent absorption, dialysis, and electrodialysis, or other.

8. The system according to claim 1, comprising recycle of the high impurity stream to a point in one or more preceding evaporation ponds where conditions are favorable for precipitation and thus removal of one or more impurity ions without lithium co-precipitation.

9. The system according to claim 1, configured to advance the low impurity stream to a downstream pond, mechanical evaporator, or precipitation plant for further concentration or processing to lithium products.

10. The system according to claim 9, wherein the further concentration in the downstream pond, mechanical evaporator or precipitation plant occurs substantially without lithium co-precipitation and associated lithium loss.

11. The system according to claim 1, wherein the system is configured to achieve a lithium concentration increase from about 10% to about 1,000%.

12. The system according to claim 1, where the high impurity stream is fully or partially evaporated in a separate pond or re-injected underground.

13. The system according to claim 1, where the low impurity stream is fully or partially evaporated in a separate pond.

14. The system according to claim 1, wherein the precipitated salts are harvested and processed separately or with the clean concentrated lithium brine in a processing plant.

15. The system according to claim 1, further comprising: a chloride (Cl.sup.−)-sulfate (SO.sub.4.sup.2−) separator configured to separate chloride from sulfate.

16. The system according to claim 1, wherein the lithium concentration is increased to the maximum determined by LiCl solubility limit, which is around 60,000-67,000 ppm Li in solution.

17. The system according to claim 1, wherein the lithium concentration is increased 10 to 1,000 fold, or 10 to 500 fold, or 10 to 100 fold.

18. The system according to claim 1, wherein operation of a LiTAS™ separator in a moderate recovery mode results in reduction of size of the separation equipment, thereby reducing the capital cost of separation equipment per ton of lithium processed by 30-70%, or by 40-60%.

19. The system according to claim 1, wherein operation of the LiTAS™ separator in a moderate recovery mode reduces flow through the separation equipment, thereby reducing the operating cost of separation equipment per ton of lithium processed by 20-60%, or by 30-50%.

20. The system according to claim 1, wherein the system results in high concentration brines, reducing flows through the processing plant thereby also reducing processing plant capital costs by 30-70%, or 40-60%.

21. The system according to claim 1, wherein the system results in low impurity brines, reducing reagent requirements for impurity removal through the processing plant thereby also reducing processing plant capital costs by 30-70%, or by 40-60%.

22. The system according to claim 1, wherein the system results in high concentration brines, which increase processing plant per pass recovery by 30-60% as the mother liquor concentration is fixed, or by 10-30% as the mother liquor concentration is fixed.

23. The system according to claim 1, wherein for brownfield operation with existing ponds, production capacity from the same ponds can be increased by 2-fold to 50-fold by treating low concentration feed brines, or by 3-fold to 20-fold with by treating medium concentration feed brines.

24. The system according to claim 1, wherein for brownfield operation with existing ponds, production capacity from the same ponds can be increased by 4-fold to 10-fold by treating high concentration feed brines.

25. The system according to claim 1, wherein for greenfield operation, same production can be maintained by treating low concentration feed brines with 2-50% of the pond area otherwise required to reach LiCl saturation concentration, or by treating medium concentration feed brines with 5-35% of the pond area otherwise required to reach LiCl saturation concentration.

26. The system according to claim 1, wherein for greenfield operation, same production can be maintained by treating high concentration feed brines with 10-25% of the pond area otherwise required to reach LiCl saturation concentration.

27. A method for improving efficiency in extracting lithium from brines using one or more solar evaporation ponds, the method comprising: separating at least a portion of the brine at a brine removal location to obtain a removed brine; transmitting the removed brine through a separator such that one or more impurities are separated from lithium to form a high impurity stream (i.e., the impure stream) and a low impurity stream (i.e., the pure stream); recycling at least a portion of the high impurity stream to the one or more evaporation ponds at a location the same as or upstream from the brine removal location; or evaporating the high impurity stream, fully or partially, in a separate pond; or re-injecting the high impurity stream underground; and transferring the low impurity stream to one or more of the removal locations, to another pond, or to a lithium separation plant, or to a concentration facility.

28. The method according to claim 27, comprising further concentrating the low impurity stream by natural solar pond evaporation or forced mechanical-thermal evaporation, membrane distillation or other methods.

29. The method according to claim 27, wherein the separator comprises a selective monovalent-multivalent or monovalent-monovalent ion separation.

30. The method according to claim 27, wherein a lithium concentration is attained in an amount of an increase from about 10% to about 1,000%.

31. The method according to claim 27, further comprising: providing a chloride (Cl.sup.−)-sulfate (SO.sub.4.sup.2−) separator for separating chloride from sulfate.

32. The method according to claim 27, wherein the precipitated salts are harvested and processed separately or with the clean concentrated lithium brine in a processing plant.

33. The method according to claim 27, wherein the method is applicable to any salt lake, surface water, continental underground brines, geothermal brines, or other brine sources.

34. The method according to claim 27, wherein the method is applicable to brine concentrations of 10 ppm or higher, preferably 50 ppm or higher, and more preferably 100 ppm or higher.

Description

BRIEF DESCRIPTION OF FIGURES

[0025] So that the manner in which the features, advantages and objects of the invention, as well as others which may become apparent, are attained and can be understood in more detail, more particular description of the invention briefly summarized above may be had by reference to the embodiment thereof which is illustrated in the appended drawings, which drawings form a part of this specification. It is to be noted, however, that the drawings illustrate only example embodiments of the invention and is therefore not to be considered limiting of its scope as the invention may admit to other equally effective embodiments.

[0026] FIG. 1 (prior art) illustrates typical solar evaporation and concentration of lithium from brines as well as precipitations of salts at different points in the evaporation sequence. Lithium precipitation losses in such systems can be in the 40-60% range.

[0027] FIG. 2 illustrates embodiments of the present disclosure using separator applications in the evaporation pond cascade to exploit natural brine chemistry for removal of impurities and concentration of lithium without lithium co-precipitation losses. FIG. 2 (a) represents typical Chilean and Bolivian brines, (b) typical Argentinian brines, and (c) typical Bolivian and some Argentinian brines.

[0028] FIG. 3 illustrates increases in Li recovery using aspects of the presently disclosed methods and systems while attaining high lithium concentrations from a typical Bolivian brine.

[0029] FIG. 4 shows aspects of a preferred embodiment using ion separation after carnallite/bischofite ponds from a typical Chilean or Bolivian brine.

[0030] FIG. 5 illustrates an aspect of seamless integration of the presently disclosed systems in an existing operation.

[0031] FIG. 6 depicts a mass balance and simulation results of the conventional brine (Chilean Brine High Lithium, Low Sulfate) evaporation process for production of lithium.

[0032] FIG. 7 depicts a mass balance and simulation results of the brine evaporation process of FIG. 6 using preferred aspects of the present disclosure.

[0033] FIG. 8 depicts a mass balance and simulation results of another conventional brine (Bolivian Brine, Low Lithium, High Magnesium, High Sulfate) evaporation process for production of lithium.

[0034] FIG. 9 depicts a mass balance and simulation results of the brine evaporation process of FIG. 8 using preferred aspects of the present disclosure.

[0035] FIG. 10 depicts a mass balance and simulation results of another conventional brine (Argentinian Brine, Low Lithium, Low Magnesium, High Sulfate) evaporation process.

[0036] FIG. 11 depicts a mass balance and simulation results of the brine evaporation process of FIG. 10 using preferred aspects of the present disclosure.

[0037] FIG. 12 illustrates an application of Lithium Separation Technology (LiTAS™) at different points in the evaporation pond cycle. Option A represents a Pure Direct Lithium Extraction without the need for ponds. Options B and C are part of the present invention that significantly improve all aspects of the process.

DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS

[0038] The methods and systems of the present disclosure can now be described more fully hereinafter with reference to the accompanying drawings in which embodiments are shown. The methods and systems of the present disclosure may be in many different forms and should not be construed as limited to the illustrated embodiments set forth herein; rather, these embodiments are provided so that this disclosure can be thorough and complete, and can fully convey its scope to those skilled in the art. Like numbers refer to like elements throughout.

[0039] The systems and methods described herein advantageously eliminate or minimize lithium co-precipitation losses by application of a separator, preferably a selective monovalent-multivalent and/or a selective monovalent-monovalent separation process applied at a selected location in the evaporation cycle.

[0040] In general, the methods comprise one or more of the following steps: solar evaporation to preconcentrate the brine to the point of lithium saturation; apply selective separation to separate lithium from the impurities at a selected location (preferably, a point such that lithium would otherwise reach saturation and co-precipitation with impurity ions); return separated impurities to a location in the evaporation sequence where conditions are favorable for their precipitation; and then further concentrate lithium by, such as evaporation, as the accompanying impurities do not favor lithium co-precipitation.

[0041] With reference to solar evaporation, to preconcentrate the brine to the point of lithium saturation, in addition to the use of solar energy for evaporation, the resulting salt precipitations are effective methods for removing undesirable impurities from the brine while concentrating the brine's lithium content. This naturally occurring process is superior to most energy intensive mechanical separations. The rejections of undesirable impurities from solar evaporation are shown in Table 2. Hence, instead of attempting to mechanically separate these impurities from the as-pumped brine, in one embodiment natural evaporation-concentration-precipitation processes are allowed to occur to, at, or near the point of lithium saturation, the “saturation point.” For example, this point may be reached after the carnallite/bischofite pond as shown in FIG. 1, or earlier with saturation of lithium sulfate monohydrate (Li.sub.2SO.sub.4.H.sub.2O). Evaporation beyond the lithium saturation point will start lithium co-precipitation and losses. Application of the systems and methods described herein after natural solar evaporation can reduce the overall volume of brine to be treated by 95-99%.

[0042] With reference to selection of advantageous location(s) for separation of lithium from impurities, we have found that the location depends on which lithium salts precipitate at what point in the evaporation sequence and also the conditions prior to this point of lithium precipitation which are favorable for precipitating other salts. Selection of locations for application of separation can also be viewed as a location for removal of a portion of the brine stream from the sequence of evaporation ponds. This location is preferably a point at which the concentration of lithium is within a range of minus 50%, minus 25%, preferably plus or minus 10%, or up to plus 50% of its saturation concentration in the brine. This point also reflects a potential limit on the location of recycle for return of impurities to the existing ponds where conditions are favorable for their precipitation and removal. The recycle location can be at the location for removal (e.g., the same pond from which removal occurred) of at least a portion of the brine stream or can be upstream of this location where conditions are favorable for precipitation of impurities without lithium co-precipitation, or a separate pond for partial or total evaporation or re-injected to the aquifer. Such recycle and precipitation of the impurities prevents them from building up in the system and altering the chemistry in the evaporation ponds.

TABLE-US-00002 TABLE 2 Rejection of ion impurities by natural evaporation and precipitation in solar evaporation processes. Ion Rejection (%) Na.sup.+ 99.5%.sup.  K.sup.+ 99.5%.sup.  Mg.sup.2+ 50% Ca.sup.2+ 50% B (ionic) 50% Cl.sup.− 80% SO.sub.4.sup.2− 95%

[0043] By way of illustration, three scenarios are shown in FIG. 2. FIG. 2a depicts a brine in which continued evaporation results in lithium co-precipitation as LiCl.MgCl.sub.2.7H.sub.2O. The previous pond in the evaporative sequence however has conditions favorable for, and thus is precipitating, MgCl.sub.2.6H.sub.2O. This is a very typical situation in Chilean and Bolivian brines as well as other high magnesium brines. Using aspects of the presently disclosed systems and methods Mg.sup.2+ is prevented from advancing forward; we have found that lithium co-precipitation as LiCl.MgCl.sub.2.7H.sub.2O will thus be prevented. Magnesium can be prevented from advancing by utilizing, for example, a suitable monovalent-divalent (Li.sup.+/Mg.sup.2+) cation selective separator. The blocked Mg′ may then be recycled to the previous pond(s) where conditions remain favorable for its precipitation as MgCl.sub.2.6H.sub.2O. The lithium passing the separator and advancing now does not have magnesium to co-precipitate and hence can be concentrated to much higher levels without incurring any lithium losses.

[0044] In the scenario of FIG. 2b, the brine is typical of Argentinian and Bolivian brines as well as other high sulfate brines, wherein the concentration of Li results in precipitation of Li.sub.2SO.sub.4.H.sub.2O. The previous pond is favorable for precipitating Na.sub.2SO.sub.4.10H.sub.2O. Using aspects of the presently disclosed systems and methods, separator blocks SO.sub.4.sup.2− from advancing, Li.sub.2SO.sub.4.H.sub.2O will not precipitate in subsequent evaporation. To block the SO.sub.4.sup.2− anion, in an embodiment of the present systems and methods an equivalent amount of cation also is blocked, to maintain electroneutrality. Na.sup.+ is preferred cation to block, as it is favored for precipitation in the previous pond to which, preferably, it is recycled. The blocked Na.sup.+ and SO.sub.4.sup.2− are thus recycled back to the previous pond where they are precipitated as additional Na.sub.2SO.sub.4.10H.sub.2O. Na.sup.+ and SO.sub.4.sup.2− can be blocked by a suitable monovalent-monovalent (Li—Na) cationic separator and a monovalent-divalent anionic separator (Cl.sup.−—SO.sub.4.sup.2−).

[0045] In FIG. 2c, as is typical of some Argentinian brines, further concentration of lithium leads to lithium schoenite (Li.sub.2SO.sub.4.K2SO.sub.4) precipitation. The previous pond precipitated K.sub.2SO.sub.4.MgSO.sub.4.CaSO.sub.4. Hence, a monovalent-monovalent separation between Li.sup.+ and K.sup.+ (which is also effective between Li.sup.+ and Mg.sup.2+, Li.sup.+ and Ca.sup.2+, and, SO.sub.4.sup.2− and Cl.sup.−) prevents the excess K.sup.+ and SO.sub.4.sup.2− from advancing and thus prevents lithium schoenite precipitation. The blocked ions are recycled to previous ponds in the sequence having conditions favorable for precipitation as K.sub.2SO.sub.4.MgSO.sub.4.CaSO.sub.4 and are thus removed from the system by solar evaporation and natural precipitation. In FIG. 2 the recycle is to the previous pond. In other aspects of this disclosure the recycle is alternatively to the first pond in the sequence where conditions are also favorable for precipitating, for example, sulfate as sodium sulfate decahydrate. Prior to application of the methods taught herein, the impurity ions co-precipitated with Li, resulting in significant Li losses.

[0046] As illustrated in FIG. 2, various embodiments of separator applications at particular locations in the sequence of evaporation ponds exploit natural brine chemistry for removal of impurities and concentration of lithium without lithium co-precipitation losses.

[0047] In addition, in all the cases an optional separator configured to block the borate anion from advancing and thus recycling it back to the previous ponds where conditions are favorable for precipitation of calcium or sodium borate or boric acid al so is beneficial. Conventionally, boron is removed from the concentrated brine by expensive and environmentally undesirable methods, such as solvent extraction using organic solvents.

[0048] If however the pH is acidic, as it is in all cases with such brines and electrodialysis is used as the separation device, boron existing as molecular boric acid follow water and is essentially retained with the impurity rich stream and precipitated in the preceeding ponds. This alleviates the necessity of the boron removal step in or in between the evaporation ponds and the processing plant.

[0049] Similarly, any solvent extraction, ion exchange or ion sorption process that retains boron with the impurity rich stream will benefit from this approach as described in the preceding paragraph.

[0050] As shown in FIG. 3, increase in recovery achieved while reaching high Li concentrations for a Chilean brine with application of a LiTAS™ membrane separator.

[0051] By references to “Chilean-type,” “Bolivian-type”, and “Argentinian-type” brines herein, we mean brines having the ratios of components as shown in Table 3, plus or minus 50%, plus or minus 30%, or preferably plus or minus 15% of the following ratios.

TABLE-US-00003 TABLE 3 Classification of lithium containing brines into types based on ratio of key components. Mg.sup.+/Li.sup.+ SO.sub.4.sup.2−/Li.sup.+ Brine Type Ratio Ratio Chilean  3-10 0.1-10  Bolivian 12-50 20-50 Argentinian 1-8 10-40

[0052] It should be understood that separators useful in embodiments of the present disclosure can include any separators which can achieve separation of at least a portion of lithium from one or more impurities in the brine, and preferably targeted monovalent-monovalent and/or monovalent-multivalent separations. Examples of suitable separators utilize nanofiltration, ion sorption, or ion exchange, with preferred embodiments utilizing LiTAS™ membrane separation technology as shown in FIG. 4. By “LiTAS™” membrane separation technology, we mean lithium-ion transport and/or separation using metal organic framework (MOF) nanoparticles. MOFs have exceptionally high internal surface area and adjustable apertures that achieve separation and transport of ions while only allowing certain ions to pass through. These MOF nanoparticles are materialized like a powder, but when combined with polymer to create a tangible product, utilizing a proprietary processing method, the combined MOF and polymer create a mixed matrix membrane embedded with the nanoparticles. The MOF particles create a percolation network, or channels, that allow selected ions to pass through. When extracting lithium, the membrane is placed in a module housing. Brine is pumped through the system with one or more layers of membranes that conduct effective separation even at high salinities. While current separator technology can fall short in one area or another, LiTAS™ is particularly preferred and effective. LiTAS™ Membrane Technology U.S. Patent Application No. 62/892,439, filed Aug. 27, 2019, U.S. Patent Application No. 62/892,440, filed Aug. 27, 2019, and International Patent WO Publication Number 2019/113649A1, published Jun. 20, 2019, are hereby incorporated by reference in their entireties.

[0053] Dialysis mode is suitable for ionic separation subsystems herein as very low energy costs are incurred as the transfer of ions through the membranes relies on concentration driving forces rather than electrical or pressure driving forces. At the ultra-high salinity of the brine solutions (50-60% Total Dissolved Solids, TDS) osmotic pressures are too large to be overcome by practical or economically feasible means. A reasonable degree of selectivity, particularly monovalent-monovalent cationic selectivity (Li.sup.+—Na.sup.+,K.sup.+), is also desired along with high throughputs.

[0054] In a dialysis mode membrane operation, Li extraction is conducted in a source of fresh water or a low Li-containing water source to maintain a suitable concentration gradient across the membrane. The extractant or sweep fluid may also advantageously constitute return mother liquor from the downstream precipitation plant which is low in lithium and high in Na and Cl. High Na concentration may also enhance monovalent-monovalent selectivity between Li and Na, as the concentration driving force for Na would be lower.

[0055] A dialysis approach would slightly reduce the lithium concentration compared to the feed to the separator. This can be overcome by application of electrodialysis to selectively concentrate lithium or by reverse osmosis to reject water. The TDS of the pure stream is around 10% which can allow a small concentration using reverse osmosis before osmotic pressures become too large.

[0056] An electrodialysis mode of operation with Li-selective membranes is particularly preferred as fresh water use is minimized, and the process stream can be cleaned and concentrated simultaneously. In addition, molecular boric acid in acidic conditions remains with the impurity stream allowing its simultaneous removal with other impurities rather than needing a separate step for its removal.

[0057] Other separation technologies could be the well known solvent extraction, ion exchange or ion sorption where lithium is selectively separated from impurities and boron remains with the impurity concentrated stream.

[0058] As illustrated in FIG. 4, a preferred embodiment using impurity ion separation located after carnallite/bischofite ponds and a typical Chilean or Bolivian brine. SF, CF, UF are examples of pre-treatments that can be used on the brine before it enters any separator or LiTAS™ membrane. This also is true for traditional reverse osmosis processes. (SF=Sand Filters, CF=Carbon Filters, UF=Ultrafiltration).

[0059] As shown and discussed above, the separators advance lithium forward and recycle the impurities to the preceding ponds. The return location of the impurities is preferred to be the same pond from which the feed to the separator is drawn. This can however also be recycled to earlier stages of evaporation if the chemistry is favorable for ion impurity precipitation is such ponds. The impurities could also be evaporated partially or completely in a separate pond or injected to the aquifer. The lithium advance stream could be concentrated during separation such as with electrodialysis or other separation methods and advance directly to the downstream processing plant.

[0060] Referring to FIG. 5, the systems and methods taught herein can be integrated seamlessly in existing operations. In conventional processes, the brine advances from one pond to the next in sequence. With this disclosure, the advancing brine instead passes through a separator at a selected location based on brine chemistry and lithium saturation at that point. Part of the brine with reduced impurities then advances to the next pond in the series, and the other part with higher impurities is recycled to the pond feeding the separator or optionally to one or more previous ponds in the sequence. The recycle feed pond precipitates the excess impurities recycled by the separator, thus keeping the advancing brine composition substantially constant.

[0061] New ponds and evaporation concentration systems can also be designed to incorporate aspects of the presently disclosed systems and methods in new operations. The impurities-depleted brine from the separator can advance normally to the next pond in the series where lithium concentration can increase significantly without co-precipitation as double salts with impurities.

[0062] These and further aspects of the systems and methods are described below in relation to exemplary embodiments which include examples that both illustrate the use of the systems and methods and provide corresponding characterization data relating to ions removed and Li recovery efficiency. Having described currently preferred embodiments of systems and methods, and having shown illustrative details of particular embodiments, it will be understood that the specific examples given below are employed in a descriptive sense only and are not for the purpose of limitation. Various modifications to the embodiments may be made without departing from the spirit and scope of the present invention which is limited only by the appended claims.

EXAMPLES

[0063] The currently preferred systems and methods were modelled using simulation software through the entire evaporation sequence of the ponds. An Extended UNIQUAC thermodynamic modelling approach was used to predict thermodynamic equilibrium. This model has been validated previously in lithium and non-lithium aqueous chemistry applications from a variety of sources. The model provided brine compositions through the progressive evaporation stages precipitating different phases of salts. Modelling was conducted at a steady state at a fixed temperature of either 5° C. (Argentinian type brines) or 10° C. (Chilean and Bolivian type brines).

[0064] As evaporation proceeds, the first salt to precipitate is halite followed by sylvinite (mixture of halite and sylvite), kainite, calcium borate and gypsum. Further evaporation precipitates carnallite, bischofite, kainite, sylvinite, gypsum, kieserite and boric acid. The precipitation of salts varies and is dependent on the starting brine compositions and evaporation conditions. This proceeds until a lithium concentration of about 0.5-2% is reached. Further evaporation from this level starts precipitation of lithium sulfate monohydrate, lithium carnallite or lithium schoenite, again dependent on the brine composition, potentially resulting in significant lithium losses from prior systems.

[0065] Equilibrium concentrations of all ionic species were obtained from the thermodynamic model and used in a mass balance simulation. The equilibrium concentrations controlled the precipitation of different salts in this model and advanced the brine from one stage to the next. Separator selectivities as shown in Table 4 were programmed into the model to generate pure and impure streams from the separator. In Examples A and B, the impure stream was returned to the pond from which the separator feed was drawn. In Example C, the impure stream was returned to the first pond in the evaporation sequence. The model was iterated until a steady state was obtained in the ponds and the separator. Under the new steady-state brine chemistry of the ponds, equilibrium parameters were recalculated and the model re-iterated. The pure stream from the separator was concentrated in the next pond in a similar fashion. The result was a full profile of brine and precipitated solids compositions and flow across the entire evaporation sequence of the Examples.

TABLE-US-00004 TABLE 4 Exemplary LiTAS ™ separator ionic selectivity ratios, used for modelling separator performance in lithium brine evaporation pond sequences in Examples A and B. Example A is a single stage separation while Example B utilizes two stage separation. Selectivity Ratio Selectivity Ratio (per stage)/B Recovery Ion Example A Example B Li.sup.+:Na.sup.+ 1.25 1 Li.sup.+:K.sup.+ 1.1 1 Li.sup.+:Mg.sup.2+ 10 100 Li.sup.+:Ca.sup.2+ 10 100 Li.sup.+:B (ionic) 1.25 5% Recovery

[0066] These simulations were conducted for three known brine sources from Chile, Bolivia and Argentina. Single pass transfer to the pure stream was set at 10% in Example A, 90% in Example B and 84% for Example C. Example B also utilized a two stage separation where the lithium rich stream after the first stage undergoes another separation step to further clean that stream in a second stage. Example A represents monovalent selective membrane dialysis, Example B monovalent selective membrane electrodialysis and Example C a lithium selective membrane dialysis process. These variations between the examples have been shown to demonstrate the applicability of the method taught here to any such appropriate technology or separation. Results are presented in the three examples below. Simulations were conducted both for the conventional brine evaporation process and the process incorporating a preferred system and method as taught in this disclosure. Simulation results of Examples A and C represent existing or proposed operations. The results for the conventional process as practiced match closely with actual operations. This also confirms the validity of our modelling and simulation approach for these and other applications and examples.

Example A: Chilean Brine (High Li, Low Sulfate)

[0067] FIG. 6 represents the conventional brine evaporation process simplified to four pond stages. The starting brine composition is indicated by Stream 1 composition and the final concentrated brine by Stream 11 compositions. All streams are numbered and the flow rates in tons per hour are indicated. The salt species precipitating in each pond are also indicated with their amounts in tons per hour.

[0068] As seen in this example, the starting lithium brine concentration is high at 0.19%. The Mg/Li ratio is moderately low at 6.6. Sulfate is low at 0.2%. Upon evaporation in Pond I, the major precipitate is halite (NaCl). Pond II precipitates NaCl and KCl (sylvinite) in major amounts. In Pond III, conditions are favorable for precipitation of magnesium as bischofite (MgCl.sub.2.6H.sub.2O) and carnallite (KCl.MgCl.sub.2.6H.sub.2O). These conditions are exploited in this Example to recycle additional magnesium and precipitate the same. Lithium concentration after this pond reaches 1.65%. This point was determined such that any concentration beyond this will result in lithium co-precipitation. As seen, by comparison, further evaporation starts to precipitate lithium and magnesium together as lithium carnallite (LiCl.MgCl.sub.2.7H.sub.2O) resulting in large lithium losses.

[0069] Hence, the point of application for the separator was determined. The separator would be applied after Pond III and before Pond IV as lithium precipitation and losses do not occur in Pond III but start in Pond IV. The co-precipitating element of interest is also now determined to be Mg as lithium co-precipitates with magnesium in Pond IV. A suitable location to remove this magnesium is also now known to be Pond III where conditions are favorable to precipitation of magnesium but not lithium.

[0070] As shown in FIG. 6 for Example A, a mass balance and simulation results of the conventional brine evaporation process for production of lithium. Composition numbers do not add to 100% due to rounding and ignoring trace levels of elements.

[0071] The mass balance and simulation results after application of the separator at the selected location is shown in FIG. 7. The separator takes feed from Pond III. It partially separates lithium from magnesium. The lower magnesium pure stream is advanced to Pond IV for further evaporation and concentration while the higher magnesium impure stream is recycled to Pond III, where the excess incoming magnesium is precipitated and removed.

[0072] As shown in FIG. 7 for Example A, a mass balance and simulation results of the brine evaporation process for production of lithium using the invention. Composition numbers do not add to 100% due to rounding and ignoring trace levels of elements. Comparison of FIGS. 6 and 7 indicates information listed below. [0073] 1) The composition of Stream 8 in both cases remains unchanged with the only difference being the flow rate. This is because the composition is determined by the solid-liquid equilibrium conditions in Pond III. The excess magnesium in Stream 12 returning from the separator is removed in the precipitate as additional bischofite. [0074] 2) The lithium content in the final concentrated stream with the application of a preferred method according to the present disclosure is more than doubled, as lithium losses do not occur in Pond IV due to now low levels of magnesium there. The lithium concentration then advantageously proceeds from 1.65% to 6% without any lithium precipitation losses in Pond IV. [0075] 3) There is no precipitation observed in Pond IV, indicating that lithium concentration can proceed further to the point where lithium precipitation initiates. [0076] 4) Stream 16 in FIG. 7 shows any water addition that may be required by the separator operation. It could be zero where the separator does not require it without impacting the method. This additional water, if any, can be evaporated in the preceding pond where the impurity enriched stream is recycled.

Example B: Bolivian Brine (Low Li, High Magnesium, High Sulfate)

[0077] FIG. 8 represents the conventional brine evaporation process simplified to four pond stages for a Bolivian brine. The starting brine composition is indicated by Stream 1 composition, and the final concentrated brine by Stream 11 composition. All streams are numbered and the flow rates in tons per hour are indicated. The salt species precipitating in each pond are also indicated with their amounts in tons per hour.

[0078] As seen in this example, the starting lithium brine concentration is very low at 0.07%. The Mg/Li ratio is very high at 19. Sulfate/Li ratio is also very high at 29. Upon evaporation in Pond I, the major precipitate is halite (NaCl) and polyhalite (K.sub.2SO.sub.4.MgSO.sub.4.2CaSO.sub.4.2H.sub.2O). Pond II precipitates NaCl+KCl (Sylvinite) and minor amounts of polyhalite. In Pond III, halite, sylvinite, kainite (KCl.MgSO.sub.4.3H.sub.2O) and carnallite (KCl.MgCl.sub.2.6H.sub.2O) precipitate. Here, Li concentration reaches 0.49%. Further evaporation in Pond IV starts lithium sulfate monohydrate precipitation along with increasing amounts of carnallite and other salts.

[0079] The preferred point of application for the separator is thus selected. The separator would be applied after Pond III and before Pond IV as lithium precipitation and losses do not occur in Pond III but start in Pond IV. The co-precipitating ion of interest is also now determined to be sulfate as lithium precipitates as Li.sub.2SO.sub.4.H.sub.2O in Pond IV. The separation used here grossly separates all impurities from Li. A suitable location to remove this sulfate ion is also now known to be Pond III as it is already precipitating Mg, K and sulfate as carnallite and kainite and boric acid, but not lithium. Magnesium is the counter-ion to sulfate that is selected in this Example as sulfate precipitates with magnesium in the preceding ponds.

[0080] Simulation and modeling of this new flowsheet as shown in FIG. 9 indicates that all recirculating impurities, mainly Mg, sulfate and boric acid are precipitated in Pond III. The recirculation and the change in concentration changes the form in which they precipitate. In addition to carnallite and boric acid, magnesium and sulfate now precipitate as kieserite (MgSO.sub.4.H.sub.2O) and hexahydrite (MgSO.sub.4.6H.sub.2O).

[0081] With the application of the preferred method, the recoverable lithium would almost quadruple as seen by comparing Streams 13 in FIGS. 8 and 9. Note that this current operation harvests the precipitated lithium sulfate monohydrate as feed to the processing plant (FIG. 8, Stream 13). The Li-rich advancing stream (FIG. 9, Stream 11) is now much lower in impurities compared to the Pond III overflow from the base case flowsheet (FIG. 8, Stream 8). This allows further evaporative concentration of FIG. 9, Stream 11 to nearly 4.2% Li concentration without any precipitation of any salt. This is a 10 fold increase in Li concentration compared to the base case (FIG. 8) without incurring any Li loss. Simulation and modeling indicates that concentration beyond 4.2% Li in this case will again result in initiation of lithium sulfate monohydrate precipitation.

[0082] As shown in FIG. 9 for Example B, a mass balance and simulation results of the brine evaporation process for production of lithium using the invention. Composition numbers do not add to 100% due to rounding and ignoring trace levels of elements.

Example C: Argentinian Brine (Low Li, Low Magnesium, High Sulfate)

[0083] The brines in this Example are Argentinian type brines which are characterized by low Li and Mg contents but high sulfate. FIG. 10 represents the conventional brine evaporation process simplified to four pond stages. The starting brine composition is indicated by Stream 1 composition and the final concentrated brine by Stream 11 composition.

[0084] As seen in this Example, the starting lithium brine concentration is very low at 0.07%. The Mg/Li ratio is also very low at ˜3. Sulfate/Li ratio is however very high at 20. Upon evaporation in Pond I, the major precipitate is halite (NaCl) along with Glauber's salt (Na.sub.2SO.sub.4.10H.sub.2O). Pond II continues to precipitate halite. Pond III precipitates halite and sylvite (Sylvinite, NaCl+KCl). These ponds also precipitate minor amounts of syngenite (K.sub.2SO.sub.4.CaSO.sub.4.H.sub.2O). Hence it can be seen that the major sink to remove the high levels of sulfate in this brine type is in Pond I.

[0085] Pond III reaches a lithium concentration of 0.69%. Further concentration beyond this in Pond IV results in lithium co-precipitation losses as lithium potassium double salt (lithium schoenite, Li.sub.2SO.sub.4.K.sub.2SO.sub.4). Hence, the selected location for the separator application would be after Pond III. It is also now determined that reducing sulfate levels along with an associated counter-ion such as K or Na would prevent lithium co-precipitation losses in Pond IV. A suitable sink for sulfate was already determined to be Pond I. Hence, recirculating the impure sulfate concentrated stream from the separator to Pond I, would remove the excess sulfate. A separator was modelled at the selected location, achieving monovalent-monovalent and monovalent-multivalent separation with selectivities as shown in Table 5.

[0086] As shown in FIG. 10 for Example C, a mass balance and simulation results of the conventional brine evaporation process for production of lithium. Composition numbers do not add to 100% due to rounding and ignoring trace levels of elements.

TABLE-US-00005 TABLE 5 Separator ionic selectivity ratios used for modelling monovalent- monovalent and monovalent-multivalent separator performance in lithium brine evaporation pond sequence of Example C. Ion Selectivity Ratio Li.sup.+:Na.sup.+ 4.4 Li.sup.+:K.sup.+ 6.3 Li.sup.+:Mg.sup.2+ 10.6 Li.sup.+:Ca.sup.2+ 20.0 Li.sup.+:Cl.sup.− 2.8 Li.sup.+:SO.sub.4.sup.2− 11.3 Cl.sup.−:SO.sub.4.sup.2− 4.0 Li.sup.+:B (ionic) 4.0

[0087] FIG. 11 shows the steady-state mass balance of the entire pond sequence after introduction of the separator and recycle of the separator impure stream to Pond I. Some of the excess sulfate recycled by the separator would be precipitated in Pond I as Na.sub.2SO.sub.4.10H.sub.2O, which can be seen to be an increase from the conventional case. The excess recycling sulfates alters the chemistry of the pond sequence resulting in different solid-liquid equilibrium conditions in the ponds. Due to the high levels of recirculating sulfates, conditions become favorable for the precipitation of epsomite (MgSO.sub.4.7H.sub.2O) in Pond III. This is where the major proportion of remaining excess sulfate would be removed.

[0088] The pure stream from the separator proceeds normally to Pond IV. Here, evaporation can proceed without any co-precipitation of lithium due to the low levels of sulfate. Lithium concentration can now reach 1.95% before co-precipitation of lithium would begin. In the conventional case, lithium concentration without co-precipitation losses would only reach 0.69%.

[0089] As shown in FIG. 11 for Example C, a mass balance and simulation results of the brine evaporation process for production of lithium using the invention. Composition numbers do not add to 100% due to rounding and ignoring trace levels of elements.

Concentration Improvement Example

[0090] In another embodiment of this invention, a separator can be used in conjunction with one or more evaporation ponds in different arrangements as shown in FIG. 12. Option A represents a Pure Direct Lithium Extraction without the need for ponds. It is seen that the separator can achieve a high recovery but realizes only a moderate concentration of lithium typically between 1000-7000 ppm Li. This lithium concentration brine can be fed to the precipitation plant but involves large volumes and hence large process equipment. In addition, removal of impurities is difficult from dilute solutions. High energy input is required for precipitation and the precipitation yield is low as it is limited by the difference between the feed concentration and the solubility limit for lithium carbonate which is fixed. Options B and C utilize one or more ponds in combination with a lithium separator to improve the process economics in all respects by achieving a higher concentration of lithium and achieving a cleaner lithium product. Option B incorporates recycle which allows a reduction in capital cost of the separator by almost 50% as high recoveries are not desired as lithium does not exit the system. Capital cost is further reduced as a smaller volume if post-evaporated brine is treated. Final brine concentration is increased almost another 10-fold to LiCl saturation at 60,000-67,000 ppm Li. This makes the processing plant smaller and more efficient. Option C allows a major capacity expansion opportunity. Here, well brine is processed through the separator which increases lithium concentration nearly 10-fold. For brownfield operation, enough pond capacity is freed to increase capacity of the operation 10-fold without the need to construct additional pond capacity. Even for a greenfield project, only 10% of the pond capacity is required. High Li recoveries are still achieved in these options.

[0091] The term “brownfield” or brownfield operation as used herein refers to a lithium brine project that has at least one equipment installed at the facility or an evaporation pond-based lithium or lithium compounds production process. The term “greenfield” or greenfield operation as used herein refers to a lithium brine project that does not have any equipment installed at the facility. The term “moderate recovery” as used herein refers to lithium recovery of about 30-70%. The term “low feed concentration” as used herein refers to 30-100 ppm Li, the term “medium feed concentration” refers to 100-400 ppm Li, and “high feed concentration” refers to 400 ppm Li or higher.

[0092] The systems and methods described above are configured to achieve a lithium concentration increase from about 10% to about 1,000%. In one embodiment, the lithium concentration is increased to the maximum determined by LiCl solubility limit, which is around 60,000-67,000 ppm Li in solution. In another embodiment, the lithium concentration is increased 10 to 1,000 fold, or 10 to 500 fold, or 10 to 100 fold. In another embodiment, operation of a LiTAS™ separator in a moderate recovery mode results in reduction of size of the separation equipment, thereby reducing the capital cost of separation equipment per ton of lithium processed by 30-70%, or by 40-60%. In another embodiment, operation of the LiTAS™ separator in a moderate recovery mode reduces flow through the separation equipment, thereby reducing the operating cost of separation equipment per ton of lithium processed by 20-60%, or by 30-50%. In another embodiment, the systems and methods result in high concentration brines, reducing flows through the processing plant thereby also reducing processing plant capital costs by 30-70%, or 40-60%. In another embodiment, the systems and methods result in low impurity brines, reducing reagent requirements for impurity removal through the processing plant thereby also reducing processing plant capital costs by 30-70%, or by 40-60%. In another embodiment, the systems and methods result in high concentration brines, which increase processing plant per pass recovery by 30-60% as the mother liquor concentration is fixed, or by 10-30% as the mother liquor concentration is fixed.

[0093] In one example, for brownfield operation with existing ponds, production capacity from the same ponds can be increased by 2-fold to 50-fold by treating low concentration feed brines, or by 3-fold to 20-fold with by treating medium concentration feed brines. In another example, for brownfield operation with existing ponds, production capacity from the same ponds can be increased by 4-fold to 10-fold by treating high concentration feed brines.

[0094] In one example for greenfield operation, same production can be maintained by treating low concentration feed brines with 2-50% of the pond area otherwise required to reach LiCl saturation concentration, or by treating medium concentration feed brines with 5-35% of the pond area otherwise required to reach LiCl saturation concentration. In one example, for a greenfield operation, same production can be maintained by treating high concentration feed brines with 10-25% of the pond area otherwise required to reach LiCl saturation concentration.

[0095] The systems and methods disclosed above are applicable to any salt lake, surface water, continental underground brines, geothermal brines, or other brine sources. The systems and methods are also applicable to brine concentrations of 10 ppm or higher, preferably 50 ppm or higher, and more preferably 100 ppm or higher. In one aspect of the systems and methods herein the portion of brine removed at the brine removal location is preferably 1% to 100%, 5% to 100%, 25% to 100%, or 50% to 100% of the total brine flow in the ponds. In another aspect, the increase in lithium recovery is from about 10 to about 80% (absolute units).

[0096] The Specification, which includes the Summary, Brief Description of the Drawings and the Detailed Description, and the appended Claims refer to particular features (including process or method steps) of the disclosure. Those of skill in the art understand that the invention includes all possible combinations and uses of particular features described in the Specification. Those of skill in the art understand that the disclosure is not limited to or by the description of embodiments given in the Specification.

[0097] Those of skill in the art also understand that the terminology used for describing particular embodiments does not limit the scope or breadth of the disclosure. In interpreting the Specification and appended Claims, all terms should be interpreted in the broadest possible manner consistent with the context of each term. All technical and scientific terms used in the Specification and appended Claims have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs unless defined otherwise.

[0098] As used in the Specification and appended Claims, the singular forms “a,” “an,” and “the” include plural references unless the context clearly indicates otherwise. The verb “comprises” and its conjugated forms should be interpreted as referring to elements, components or steps in a non-exclusive manner. The referenced elements, components or steps may be present, utilized or combined with other elements, components or steps not expressly referenced. The verb “operatively connecting” and its conjugated forms means to complete any type of required junction, including electrical, mechanical or fluid, to form a connection between two or more previously non-joined objects. If a first component is operatively connected to a second component, the connection can occur either directly or through a common connector. “Optionally” and its various forms means that the subsequently described event or circumstance may or may not occur. The description includes instances where the event or circumstance occurs and instances where it does not occur.

[0099] Conditional language, such as, among others, “can,” “could,” “might,” or “may,” unless specifically stated otherwise, or otherwise understood within the context as used, is generally intended to convey that some implementations could include, while other implementations do not include, certain features, elements, and/or operations. Thus, such conditional language generally is not intended to imply that features, elements, and/or operations are in any way required for one or more implementations or that one or more implementations necessarily include logic for deciding, with or without user input or prompting, whether these features, elements, and/or operations are included or are to be performed in any particular implementation.

[0100] The systems and methods described herein, therefore, are well adapted to carry out the objects and attain the ends and advantages mentioned, as well as others inherent therein. While example embodiments of the system and method have been given for purposes of disclosure, numerous changes exist in the details of procedures for accomplishing the desired results. These and other similar modifications may readily suggest themselves to those skilled in the art, and are intended to be encompassed within the spirit of the system and method disclosed herein and the scope of the appended claims.