Classifications

• • C—CHEMISTRY; METALLURGY
  • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
  • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
  • C25C1/00—Electrolytic production, recovery or refining of metals by electrolysis of solutions
  • C25C1/02—Electrolytic production, recovery or refining of metals by electrolysis of solutions of light metals
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
  • C22B26/10—Obtaining alkali metals
  • C22B26/12—Obtaining lithium
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
  • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
  • C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
• • C—CHEMISTRY; METALLURGY
  • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
  • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
  • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
  • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
  • C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
• • C—CHEMISTRY; METALLURGY
  • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
  • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
  • C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
  • C25C7/007—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells of cells comprising at least a movable electrode
• • C—CHEMISTRY; METALLURGY
  • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
  • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
  • C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
  • C25C7/02—Electrodes; Connections thereof
• • C—CHEMISTRY; METALLURGY
  • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
  • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
  • C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
  • C25C7/04—Diaphragms; Spacing elements

Definitions

• the present disclosure generally relates to a method for producing lithium metal. More specifically, the present disclosure relates to a method for producing lithium metal electrochemically deposited onto a substrate directly from a brine solution.
• Lithium metal and many of its alloys are currently produced via a molten salt electrolysis.
• This molten salt electrolysis process is performed with a eutectic mixture of lithium chloride and potassium chloride as the electrolyte, a graphite anode, and a stainless- steel cathode.
• KC1 is added to the electrolyte mixture to lower the melting point of the KC1- LiCl mixture to -400-420 °C compared to that of pure LiCl, which is > 600 °C.
• This electrolytic process yields molten lithium metal at the cathode of greater than 97% purity owing to the lower decomposition voltage of LiCl compared to KC1.
• the present disclosure discloses methods and apparatuses for direct lithium plating from aqueous brine solutions, which can have lithium concentrations ranging from 100 ppm to 20,000 ppm at normal ambient temperatures via a solvent extraction - electrowinning process.
• This process involves lithium selective solvent extraction using a solvent immiscible with water and electrowinning lithium from the lithium impregnated solvent before it is recycled for additional lithium extraction.
• This process is unique due to the fact that electrowinning of lithium metal in the water immiscible solvent is utilized instead of stripping of lithium-ions back into an aqueous phase. It should be noted that, unlike base metals, electrowinning of lithium from the aqueous phase is not possible due to the high reactivity of lithium metal with water.
• Electrowinning can also be used for selective extraction of a metal from a multi-component solution of a suitable solvent.
• Lithium metal deposited on the working electrode substrate in this process can be further purified for use in lithium metal electrode fabrication for primary or secondary lithium metal batteries.
• This process requires less energy and cost intensive than the current state of the art methods for commercial lithium metal production that requires a molten salt electrolysis process followed by lithium metal ingot casting and extrusion.
• this disclosure discloses a process that requires that the brine be combined with an additional water immiscible solvent with a greater affinity towards lithium salts in solution compared to the predominant salt impurities such as sodium, potassium, magnesium and calcium chloride as well as boric acid.
• the solvent benefits from having a wide electrochemical stability window.
• the added solvent must have a high solubility of lithium salts, such as LiCl, be immiscible with the brine solution, and have a wide electrochemical stability window.
• the brine solution and the additional solvent are mixed to allow for the transfer of lithium salts from the brine to the added solvent.
• the mixture is then left to separate where the added solvent, now saturated with lithium salt, and lithium salt depleted immiscible aqueous brine separate.
• the lithium salt loaded solvent is continuously overflowed or underflowed into an electrochemical cell to electroplate lithium metal onto a cathode substrate.
• the now lithium depleted water immiscible solvent phase is recycled and contacted with fresh incoming lithium salt containing brine for continuous extraction.
• the present disclosure provides a process in which solvent extraction of lithium chloride can be performed with one solvent possessing lithium salt selectivity for hydrometallurgical separation combined with the lithium brine solution.
• the brine solution and the additional solvent are mixed to allow for the transfer of lithium salts from the brine to the added solvent.
• This solvent is now contacted with a second solvent with desired characteristics for electroplating lithium and the lithium is transferred to this second solvent.
• This second solvent with solvated lithium salts can be extracted and used in an electrochemical cell to plate lithium metal onto a cathode substrate. Both the first and second depleted solvents are recycled.
• the present disclosure provides a process in which a cation exchange membrane can be used to assist in the transfer of lithium-ions from a concentrated lithium brine solution to an alternative solvent medium to be plated as lithium metal on an electronically conductive substrate.
• Figure 1 shows schematic illustration of one embodiment of the methods disclosed to directly obtain lithium metal from lithium brine solution through a combined solvent extraction and electrowinning approach.
• Figure 2 depicts a schematic of an electrochemical cell that is used for the electrowinning process to plate lithium metal directly onto a cathode substrate from a solution consisting of a lithium salt in a solvent.
• Figure 3 depicts an optical photograph of a prototype 3-electrode cell schematized in Figure 2.
• Figure 4 shows an optical photograph of the interior of the 3-electrode cell shown in Figure 3.
• Figure 5 shows an optical photograph of the full prototype setup for proof of concept.
• the setup consists of a 3-electrode cell connected to a potentiostat to control the electrochemical parameters during the lithium electrowinning process.
• Figure 6 shows a voltammogram (or Current- Voltage curve) obtained during the electrodeposition of lithium metal onto a copper cathode in an electrochemical cell that contains IM LiPFe-DEC solution as the electrolyte.
• DEC is the solvent that dissolves the LiPFe lithium salt with low water miscibility ( ⁇ 4 wt%).
• Figure 7 shows a voltammogram of lithium metal electrodeposition at a fixed voltage and the resulting lithium metal deposited onto a copper plated platinum cathode in the electrochemical cell.
• Figure 8 depicts the electrochemical cell of Figure 3 after lithium the electrodeposition of lithium metal onto a copper substrate.
• Figure 9 shows a voltammogram (current versus voltage curve) obtained during the electrodeposition of lithium onto a copper substrate.
• the lithium salt used during this measurement was LiPFe
• the solvent was diethylene carbonate.
• the concentrate of the salt in the solvent was 1 M LiPFe in DEC. This salt in solvent solution was used for demonstrative purposes.
• Figure 10 shows a current versus time plot for another run of lithium deposition from solution where a constant potential of 4 V versus an Ag/AgCl reference electrode was applied. This voltage was chosen after observation of the plating voltage observed in the voltammogram of Figure 9.
• Figure 11 shows an optical photograph of the results of the electrodeposition experiment performed to obtain the current versus time plot of Figure 10.
• the left strip shows the copper cathode substrate prior to the experiment.
• the right strip shows lithium metal deposited onto the copper cathode substrate after the electrodeposition process was performed.
• Figure 12 shows a schematic of one of the embodiments to enable direct lithium metal deposition from brine with the assistance of a cation exchange membrane that allows for only lithium-ions to pass from the lithium brine phase to the lithium salt in solvent phase for electrodeposition onto a cathode substrate.
• Figure 13 shows a cyclic voltammogram for a lithium metal plating experiment performed in a prototype cell that was schematized in Figure 12.
• Figure 14 shows process for simultaneous lithium extraction and electroplating.
• Figures 15A & 15B shows a demonstration apparatus for the preparation of simultaneous lithium extraction and electroplating including the cell layout.
• Figure 16 shows the cell process including a sandwiched liquid membrane.
• Figure 17 shows a schematic of a processing cell for sustained continuous R2R production of lithium from aqueous brines.
• Figure 18 shows a schematic of a processing cell for deposition of lithium metal film onto a moving Cu foil from an organic solution medium.
• Figure 19 shows the design architecture of an electroplating cell.
• Direct lithium extractions (DLE) from brines are a challenging problem.
• the most abundant lithium brine resources on earth such as those in the South American “Lithium Triangle” (Argentina-Bolivia-Chile), are concentrated brines with a high level of total dissolved solids.
• These lithium brines are near-saturated mixed salt solutions containing salts of cations (primarily Li + , Na + , K + , Mg 2+ , Ca 2+ , B + and H + ) and anions (primarily Cl”, SCU 2- , and OH“).
• salts of cations primarily Li + , Na + , K + , Mg 2+ , Ca 2+ , B + and H +
• anions primarily Cl”, SCU 2- , and OH“.
• Most direct lithium extraction technologies use fresh water to either elute the lithium from the adsorbent or strip it from a lithium selective solvent.
• areas where direct lithium extraction would be practiced are extremely arid, thus making their
• lithium-ions in the brines are selectively extracted into an added solvent medium by solvent extraction or membrane-assisted solvent extraction.
• the lithium-ions are then electrochemically deposited onto an electronically conductive substrate from the final lithium impregnated organic or inorganic solvent medium in a process known as electrowinning.
• This process can also be performed with a series of solvent extraction steps prior to electrowinning lithium metal out of an organic or inorganic solvent medium onto an electronically conductive substrate.
• Lithium salts that can be used to electrodeposit lithium include, but are not limited to LiCl, LiCICU, Li2SO4, or LiPFe.
• the final purity of the deposited lithium from the full process starting from a lithium brine can range from 80 to 99.99%.
• the final thickness of the lithium metal plated from the starting concentrated brine solution can range in thickness from 1 nm to 5 mm.
• a solvent must have several key features to enable integration in the disclosed process: (1) the solvent can highly solubilize or selectively extract dissolved Li-ions/salts from aqueous brines; (2) the solvent allows the cathodic deposition of Li metal; (3) the solvent has long-term stability to resist anodic reactive degradation in the electrochemical cell during processing; and (4) the solvent must be immiscible with water. In the case of membrane- assisted solvent extraction, a membrane will provide the selective permeation of lithium from brines to an added solvent.
• the lithium metal product obtained from the above process can be further purified to serve as an anode material in a primary or secondary battery in which metallic lithium serves as at least one of the electrodes.
• metallic lithium serves as at least one of the electrodes.
• Such battery chemistries that this process might produce viable metallic lithium metal electrodes for including, but not limited to Lithium-Oxygen batteries, Lithium-sulfur batteries, rechargeable lithium metal batteries with a lithium-ion intercalating cathode, Lithium-MnCh primary batteries, and solid-state lithium metal batteries that contain a solid-state lithium-ion conductor as the electrolyte as opposed to a liquid electrolyte with a solvated lithium-ion conducting salt.
• Battery-grade lithium metal requires additional purification after the lithium metal ingot is produced from molten salt electrolysis to obtain lithium metal that is >99.8% purity needed for secondary battery operation and an additional step for electrode fabrication for lithium metal to be used in a secondary battery.
• the disclosed technology can bypass the purification step and the electrode fabrication step to directly produce battery-grade lithium metal in an electrode form.
• Lithium metal electrodes fabricated with the disclosed method can be between 1 nm and 5 mm. This process can be performed roll-to-roll to produce a full commercial scale roll of lithium metal plated on copper electrode for use in commercial fabrication of lithium metal secondary batteries, limiting the number of process steps and further reducing the cost of production for lithium metal electrodes for relevant battery chemistries.
• Figure 14 illustrates a solvo-electro-deposition process 100 for generating a lithium film.
• a solvo-electro-deposition process 100 can includes the steps of providing an aqueous brine 102, generating a pure Li-containing aqueous solution (e.g., LiCl (lithium chloride)) 104A, electrodepositing of lithium from an organic solution media 104B (e.g., membrane-assisted), and yielding a Li-metal film deposit 106 (e.g., for a battery anode).
• a pure Li-containing aqueous solution e.g., LiCl (lithium chloride)
• electrodepositing of lithium from an organic solution media 104B e.g., membrane-assisted
• yielding a Li-metal film deposit 106 e.g., for a battery anode.
• the solvo-electro-deposition process 100 can includes the steps of providing an aqueous brine 102, electrodepositing lithium directly from an organic solution media 104C (e.g., membrane-assisted), and yielding a dark greyish Li-metal film deposit 106 (e.g., for a battery anode).
• Figure 15A and 15B shows a batch-cell system 120 for use in relation to one embodiment illustrated in Figure 14.
• Figure 15A is a photographic representation of a laboratory-demonstrated version of the process cell (e.g., batch cell) system 120 and related solvo-electro-deposition process 100 for simultaneously extracting and electrodepositing lithium, in relation to an embodiment associated with Figure 14.
• Figure 15B is a graphic representation of the batch-cell system otherwise shown in Figure 15A.
• the batch-cell system 120 can include a cell containment unit 122 (e.g., a vessel capable of containing liquid electrolytes and carrying, e.g., electrodes and/or a membrane), a working electrode 124 (e.g., a cathode made of, for example, copper or another metal), a counter electrode 126 (e.g., an anode made, for example, of a mixed metal oxide (MMO) or platinum (Pt)), a reference electrode 128 (e.g., to aid measurement of a baseline conductivity), and a metal foil 130 (e.g., made of copper).
• a cell containment unit 122 e.g., a vessel capable of containing liquid electrolytes and carrying, e.g., electrodes and/or a membrane
• a working electrode 124 e.g., a cathode made of, for example, copper or another metal
• a counter electrode 126 e.g., an anode made, for example, of
• the process cell (e.g., batch cell) system 120 can further include a membrane 134 (for example, a CEM or a selective cation exchange membrane (sCEM)); and an anodic chamber 136 carrying a Li + -containing aqueous brine (e.g., from reservoir tanks/containers, lakes, ponds, and/or wells) and a cathodic chamber 138 carrying a Li-X (salt) solvent organic solution medium.
• a membrane 134 for example, a CEM or a selective cation exchange membrane (sCEM)
• an anodic chamber 136 carrying a Li + -containing aqueous brine (e.g., from reservoir tanks/containers, lakes, ponds, and/or wells)
• a cathodic chamber 138 carrying a Li-X (salt) solvent organic solution medium.
• the respective boundaries of the anodic chamber 136 and the cathodic chamber 138 can be defined, at least in part,
• the membrane 134 can be positioned between the working electrode 124 and the counter electrode 126.
• the counter electrode 326 and the working electrode 324 can be configured to be charged in such a manner as to drive electrodeposition of lithium onto the metal foil 330/330A extending through/into the lithium- containing organic solution (e.g., in the cathodic chamber 138).
• the process cell 120 can define a galvanic cell.
• the counter electrode 126 can contact the Li + -containing aqueous brine in the anodic chamber 136, and the working electrode 124 can contact the lithium-carrying organic solution in the cathodic chamber 138.
• the cell containment unit 122 can be defined as a housing and/or a container.
• Figure 15B illustrates a laboratory demonstration example of the batch cell process of Figure 14 that can enable the electrodeposition of a Li metal layer 132 (from an organic solvent Li-X solutions) onto a plate or foil cathode 130 (e.g., copper), while the organic solutions medium (e.g., lithium-containing organic electrolyte solution) of the cathodic chamber 138 can simultaneously extract lithium from an aqueous solution or brine of the anodic chamber 136.
• An Li+-conducting or Li+-selective membrane 134 can be placed in the middle between the organic and aqueous solutions (as seen in Figure 15B).
• This extractionelectrodeposition cell 120 can be configured with two chambers 136, 138 defined by the cell containment unit 122 and the intermediary membrane 134.
• One chamber 136 can contain the aqueous brine solution(s), and the other 138 can contain the organic solutions.
• the respective solutions can be respectively replenished from an outside reservoir tank and/or natural source (e.g., lakes, ponds, aquifers, and/or wells), as needed, with the lake 102 shown in Figure 14 being one such an example of a replenishment source.
• the process 100 of Figure 15A & 15B can be considered to be a solvo-electro extraction-electrodeposition process in a singleunit process cell 120.
• the current density for the two-electrode electrodeposition can be in the range of 0.1-100 mA per cm 2 of membrane or cathodic surface area.
• the operating voltage can go from 0 to 10 volts (which include the Li reduction potential of -3.2V relative to the Ag/AgCl (KC1) reference electrode plus the IR drops).
• FIG. 16 illustrates a derivate cell configuration, in accordance with an embodiment of the present disclosure.
• the derivative cell configuration can include a cell containment unit 222, a working electrode 224 (e.g., a cathode made of, for example, copper or another metal), a counter electrode 226 (e.g., an anode made, for example, of a mixed metal oxide (MMO) or platinum (Pt)), a reference electrode 228, a composite metal foil 230A (e.g., made of copper and coated with a lithium layer), a Li- X solvent liquid membrane 234 (e.g., including a pair of CEM’s and an intermediate solvent zone (not individually labelled)), an anodic chamber 236 carrying a Li+-containing aqueous brine, and a cathodic chamber 238 carrying Li-X solvent organic solution medium.
• a working electrode 224 e.g., a cathode made of, for example, copper or another metal
• the middle membrane 134 in the two-chamber cell 120 of Figure 15B can be replaced with a sandwiched liquid membrane or liquid chamber 234, as shown in Figure 16.
• the sandwiched liquid membrane 234 can include a Li-X solvent sandwiched with two solid Li-conducting membranes or CEMs (components not individually labelled).
• the liquid membrane 234 can provide the Li + selectivity for permeating from the aqueous solutions of the anodic chamber 236 to the organic solutions of the cathodic chamber 238.
• Figure 16 illustrates a process cell 220 for a solvo-electro extraction-electrodeposition process in a single-unit batch that utilizes a sandwiched liquid membrane 234 to enable selective transport of Li ions from the aqueous brine of the anodic chamber 236 into the organic solution medium of the cathodic chamber 238.
• the liquid membrane or chamber
• the liquid membrane can serve as a barrier to block the transport water molecules (while allowing Li transfer) from the aqueous brine chamber to the organic solution chamber. This would help sustained hours of operation in simultaneous extraction and deposition.
• Figure 17 illustrate an embodiment of a process cell 320 conducive to industrial large-scale continuous production of Li metal film deposit on a substrate foil (e.g., a copper foil or other metal film or web) while extracting lithium from an aqueous brine, for example, using a roll-to-roll (R2R) arrangement.
• a substrate foil e.g., a copper foil or other metal film or web
• R2R roll-to-roll
• the process cell 320 can include a cell containment unit 322 (e.g., a vessel capable of containing liquid electrolytes and carrying, e.g., electrodes and/or a membrane), a working electrode 324 (e.g., a cathode made of, for example, copper or another metal), a counter electrode 326 (e.g., an anode made, for example, of a mixed metal oxide (MMO) or platinum (Pt)), a reference electrode 328 (e.g., usually positioned close (within a few millimeters) to the cathode surface), a metal foil 330 (e.g., copper foil), a composite metal foil 330A (e.g., made of copper upon coating with a lithium layer), a membrane 334 (e.g., a CEM or sCEM), an anodic chamber 336 carrying a Li + - containing aqueous brine, a brine source 336A (e.g.
• the membrane 334 can be positioned between the working electrode 324 and the counter electrode 326.
• the counter electrode 326 and the working electrode 324 can be configured to be charged in such a manner as to drive electrodeposition of lithium onto the metal foil 330/330A extending through the lithium - containing organic solution.
• the process cell 320 can further include connective conduits and/or one or more additional intermediate rollers (such as shown but not labeled), as needed, to facilitate fluid movement/replenishment and/or foil movement.
• the roll-to-roll process cell 320 of Figure 17 can facilitate a continuous, multiplestep deposition process.
• an aqueous brine solution in the anodic chamber 336 can be replenished as necessary to continuously provide Li + from an outside source or reservoir 336A.
• Li + can be continuously transferred from aqueous phase into organic phase, via the membrane 334.
• electrodeposition of Li metal onto the moving copper cathode 324 e.g., in the form of a copper foil 330 supplied from the feed foil roll 340A
• the cathodic e.g., organic solution
• the water content level of the organic phase can be controlled by a dewatering column 344 and the related recirculation loop.
• the product roll 340B of a Li metal-Cu foil web 330A can be preserved and/or stored in an inert gas chamber 342, provided with an argon (Ar) gas atmosphere or another suitably inert gas therein along with any hardware needed to facilitate the collection of the product roll 340B.
• Figure 18 illustrates a roll-to-roll (R2R) cathodic deposition process for depositing a lithium (Li) metal film onto a moving metal (e.g., copper) foil web via an organic solution, in accordance with an embodiment of the present disclosure.
• the R2R cathodic deposition process can be achieved using a roll-to-roll (R2R) process cell 420.
• the R2R process cell 420 can include a cell containment unit 422, a working electrode 424 (e.g., a cathode made of, for example, copper or another metal), a counter electrode 426 (e.g., an anode made, for example, of a mixed metal oxide (MMO) or platinum (Pt)), a metal foil 430 (e.g., copper foil), a composite metal foil 430A (e.g., made of copper upon coating with a lithium layer), a cathodic chamber 438 carrying a Li-X solvent organic solution medium, an input/feed foil roll 440 A, a product foil roll 440B (e.g., lithium-coated copper foil), an argon (Ar) gas-filled holding tank 442 (e.g., in which product foil roll 440B can be retained), and a dewatering column 444.
• the counter electrode 426 e.g., anode
• the working electrode 424 e.g., cathode
• the R2R process cell 420 may, for example, not incorporate a separate anodic chamber and/or a membrane, as an organic Li-carrying solution serves as the Li source, instead of a brine.
• both the anode 426 and the cathode 428 can be included in the same chamber (e.g., 438), thereby simplifying the construction relative to the system 320 of Figure 16.
• the fixed anode 426 can be placed outside the organic solution and/or the anode 426 can be modified with one or more coating materials (such as LFP (lithium iron phosphate)).
• other additives such as ionic liquids
• an ionic liquid organic phase
• Q iq/vw Equation 1 where Q is the total charge passed therethrough.
• Q is related to the quantity of lithium metal deposited on the cathode surface. For example, for lithium with a single positive charge, each charge corresponds to a single lithium atom.
• the thickness range equivalent can be considered to be proportional to the thickness produced, given that each charge corresponds to a single lithium atom.
• the electrodeposition time can be calculated using Equations 1 & 2.
• the total deposition time converts to 500 hours.
• the deposition time may range, for example, from 1.25 to 500 hours, based on the parameters chosen and the thickness/thickness equivalent desired.
• a design with an increase to the overlap of the cathode and anode can enable a large electroplating time while still allowing for a reasonable linear production speed. It is to be understood that various design architectures can be employed to achieve the electroplating conditions.
• Figure 19 displays one such design for electroplating, with the design featuring extended overlap surface areas for the two electrodes.
• the intermediate transport rolls 540C can be configured to facilitate the definition of a plurality of foil sections (e.g., two of which, 530A and 530B, are labeled), and a given foil section can be defined between a proximate pair of intermediate transport rolls 540C.
• the foil sections can together define a plurality of adjacent foil sections, for example, 530A and 530B.
• a given counter electrode 526 can be considered to be an anode and may include/define a plurality of anode extensions, one of which is labeled as 526A (i.e., defining a multi-prong anode 526).
• Each anode extension can extend between an accompanying pair of adjacent foil sections (e.g., anode extension 526A between foil sections 530A and 530B), together defining a given electroplating zone Z, of which a plurality of such electroplating zones Z can be defined by the R2R process cell 520.
• the electrode surface overlap area A can facilitate an increase in the plated quantity and/or can allow for a faster linear speed v in Equation 2.
• the R2R electroplating process facilitated by the R2R process cell 520 can enable a lithium electroplating reaction time ranging, for example, from 0.5 to 1000 hours, 5-400 hours, or 20-300 hours.
• the large surface area overlap A associated with the R2R process cell 520 may be extended to a mass transport window, where ion transport in the electrolyte is driven by the multi-prong anode 526.
• the processing cell configuration is necessarily not limited to the illustrative designs shown in the above-described figures. Besides the variation in organic solution engineering, the electrode design and material type can be easily modified for better performances, and such modifications are considered to be within the scope of the present disclosure. Further, unless otherwise expressly excluded, it is to be understood that components described with respect to the various embodiments may be mixed and/or matched with respect to one another. Additionally, while copper has been discussed as a candidate material upon which to electro-deposit lithium, it is to be understood that other conductive metals or metal alloys may serve as appropriate substrates upon which to deposit the lithium.
• one or more embodiments of the present disclosure can result in (1) a roll-to-roll Li metal film (battery anode) production technology; and/or a lithium-metal production and lithium-ion extraction technology from either aqueous solutions or from organic solutions.
• the integrated hybrid solvo-electro-processing can enable the simultaneous lithium extraction and metal production in a single-stage batch or continuous operation.
• the “solvo-processing” can take advantage of the organic solutions as a Li + -transporting medium suitable for electrodeposition or as a solvent(s) for selective extraction of lithium from aqueous brines.
• a Li + -selective membrane (solid CEM or liquid) between the aqueous phase and organic phase can add Li + -transporting selectivity for DLE (direct lithium extraction) from the source brine.
• the “electro-processing” of the present disclosure can utilize the electrically enhanced rate of electrodialysis (for lithium extraction and transporting mobility) and/or electrodeposition (for Li metal film production).
• the Aqueous-Organic biphase electrodialysis can be uniquely implemented in extracting/transporting lithium from aqueous brines/solutions into an organic solution medium.
• the present technology can provide (1) lower cost option for Li metal film production as battery anode ( ⁇ 20 pm thick); and/or (2) simultaneous DLE from aqueous brine and Li metal film electrodeposition in a single integrated process.
• the present technology can manifest itself in one or more features.
• the technology can allow combined Li extraction (from aqueous brine) and Li metal (battery anode) production simultaneously in a continuous process, which needs no processing water.
• the process can be operated in either a roll-to-roll (R2R) or batch mode for Li metal production (via electrodeposition of Li from an organic phase) and/or continuous lithium extraction from aqueous brines.
• the technology can implement an organic phase as an electrodeposition medium that can be either lithium salt-soluble or lithium ion-selective (like those organic solutions obtained from solvent extraction).
• the system can feature a dewatering method that can control the water content of the organic phase, thus allowing sustained electrodeposition of Li metal with better current efficiency and/or better quality of Li metal fil deposit.
• the method associated herewith can yield a faster direct lithium extraction (DLE) rate from aqueous brines because of the larger Li + concentration gradient between an aqueous and organic phase driven by electrodeposition phenomenon.
• the integrated process can take advantage of an electrodialysis-like phenomenon for faster ion mobility and/or transport from an aqueous phase into an organic phase.
• the present system can allow for lower temperature (e.g., room temperature and/or ambient), lower cost processing than molten-salt electrowinning.
• a R2R version of the present system and method can be used to directly produce a thin film deposit of Li metal on copper foil web, which can be used, for example, as a suitable platform for a Li battery anode.
• a Li battery anode a Li battery anode.
• Example 1 Lithium deposition from an organic solvent with LiPFe as an ionically conducting salt.
• FIG. ! shows a schematic of the three-electrode electrochemical cell that was used for the electrodeposition of lithium metal, which consists of a Working Electrode (cathode, such as copper, copper plated platinum, or another electronically conductive substrate), a Reference Electrode (such as Ag/AgCl), and a Counter Electrode (Anode).
• a Working Electrode cathode, such as copper, copper plated platinum, or another electronically conductive substrate
• Reference Electrode such as Ag/AgCl
• Counter Electrode Anode
• the electrochemical cell uses a cathode copper rod as the working electrode that is electrically insulated on the side such that only the well-defined circular flat surface (0.5 cm 2 ) at the bottom end is exposed to the electrolyte solution.
• a glass encapsulated reference electrode (Ag/AgCl (IM KC1)) faces ( ⁇ l-mm gap) is used as the reference electrode.
• a platinum foil ring anode is placed concentrically at the bottom part of the electrodeposition cell to serve as the counter electrode.
• the above specified components are shown in Figure 4 for clarity. Note that the electrochemical cell design and electrode choices (in shape, material type, and dimension) are not limited to this example in geometrical shape, physical dimension, or material composition.
• the full experimental setup for the electrochemical cell and the lithium metal electrowinning process is shown in Figure 5.
• Figure 6 shows a voltammogram obtained during an initial linear sweep voltammetry experiment to determine the plating voltage of lithium metal onto the copper current collector in the experimental setup portrayed in Figure 5 with the experimental cell shown in Figure 3.
• the electrolyte solution for this demonstration was IM LiPFe in diethyl carbonate (DEC).
• DEC diethyl carbonate
• a reduction-oxidation (redox) reaction is observed to occur around -2.8V versus the Ag/AgCl reference electrode, which is denoted by the drastic increase in the absolute value of the measured current of the electrochemical cell.
• This initial onset of current increase is attributed to the breakdown of the DEC solvent, which is known to have a limited electrochemical stability window.
• a secondary redox reaction begins at roughly 3.2V versus Ag/AgCl which is attributed to the onset of electrochemical plating of lithium.
• This agreement between the experimentally observed potential and the thermodynamically predicted potential is a preliminary indication that lithium metal can be electrowon from solution.
• the relevant standard reduction reactions and corresponding potentials relative to the standard hydrogen electrode (SHE) are provided.
• This final equation can be used to regulate the deposition rate during the process in the method described in this invention to obtain a lithium metal electrode of a desired thickness for use in primary or secondary lithium metal batteries.
• Example 2 Scalability demonstration for electrowinning of lithium metal for commercial lithium metal electrode production.
• the copper rod cathode surface in the previous example had a limited surface area for lithium deposition (0.5 cm 2 ).
• a long strip of copper was used as the working electrode as opposed to a single end-face of a copper rod.
• This copper strip had an electrochemically active surface area that was over 10 times greater than the face of the copper rod that was used in the original lithium electrowinning experiments.
• This enlargement of the working electrode demonstrates the scalability of this approach towards commercial applications, which require lithium to be deposited on a copper substrate up to three meters wide on a roll-to-roll basis.
• the electrochemical cell for electrowinning lithium metal from a solvent medium consisted of an Ag/AgCl reference electrode, a platinum counter electrode and IM LiPFe in DEC as the electrolyte.
• Visual confirmation of lithium metal deposition onto the larger copper working electrode is provided in Figure 11 where the copper substrate is shown before and after the electrowinning process.
• the disclosed method for lithium metal production from brine may be easily modified to utilize existing commercial electroplating or electrowinning equipment or components.
• the electrowinning cell can take advantage of the roll-to-roll cathodic deposition for scalable, large surface area deposition of lithium metal onto a substrate surface that is submerged and pulled through the platting electrolyte medium.
• An example of this embodiment can include rolling copper foil through a liquid lithium electrolyte medium to plate lithium metal on the copper foil substrate.
• Some existing commercial electrodeposition cells, such as industrial electrowinning or electroplating cells may be modified and adapted for this roomtemperature hybrid solvent extraction and electrowinning process.
• Example 3 Membrane-assisted lithium metal production from concentrated lithium brine.
• One embodiment of the enclosed methods allows for the use of a cation exchange membrane to assist in the separation of lithium-ions from concentrated lithium brine into an alternative solvent media that lithium metal may then be plated from.
• An electrochemical cell that may be used in this process is schematized in Figure 12. In this cell, lithium-ions are electrochemically driven from the concentrated lithium brine, through the lithium-ion selective cation exchange membrane, into a solvent medium, and then finally plated onto a metallic substrate that is used as the cathode in the cell. A cyclic voltammogram is provided in Figure 13 for such an electrochemical cell.
• the electrochemical cell used for this experiment consisted of a copper substrate cathode, a platinum anode, concentrated lithium brine as the anolyte, a lithium conducting salt solvated in a solvent as the catholyte, and a cation exchange membrane as the separator between the compartments that contained the two different electrolyte media.
• this experiment indicates the reversibility of the process, in actuality the concentrated lithium brine would continuously be refreshed to provide a constant source of lithium-ions to drive the operation of the cell.
• this process can be modified to be a continuous roll-to-roll process.
• 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.

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• 2023
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