Century Lithium's updated feasibility study for the Angel Island claystone deposit in Esmeralda County, Nevada, starts at 7,500 t/d and doubles to 15,000 t/d after four years. The flowsheet was developed at the company's Amargosa Valley pilot plant.
The Updated NI 43-101 Technical Report on the Feasibility Study of the Clayton Valley Lithium Project, Esmeralda County, Nevada, was prepared for Century Lithium Corp. by Mineral Property Development, Global Resource Engineering, SRK and Century Lithium qualified persons, with an effective date of January 3, 2026. The Angel Island deposit is a flat-lying, clay-hosted body of about 25% smectite and 60% illite clays with relatively uniform lithium grade. Ore is processed by attrition scrubbing, hydrochloric acid leaching, filtration, impurity precipitation and direct lithium extraction (DLE), then lithium carbonate precipitation and drying. A chlor-alkali facility regenerates the hydrochloric acid and sodium hydroxide. Phase 1 treats 7,500 t/d (2,737,500 t a year) and makes about 35.5 t/d of lithium carbonate. Phase 2 doubles throughput to 15,000 t/d.
Critical Data
| Parameter | Value | Unit | Notes |
|---|---|---|---|
| Report effective date | January 3, 2026 | Not applicable | Updated feasibility study for Century Lithium Corp. |
| Throughput | 7,500 t/d (Years 1 to 4), then 15,000 t/d | Not applicable | 2.74 and 5.48 Mt/a |
| Feed grade | 0.113 average (ROM 0.1148, low grade 0.095) | % Li | Design basis |
| Lithium carbonate | About 35.5 to 35.6 t/d (Phase 1) | Not applicable | 71.2 t/d in Phase 2 |
| Crusher | 24 in x 48 in double roll | Not applicable | To minus 4 in |
| Attrition scrubber | 10 ft x 30 ft, 350 hp | Not applicable | Liberates 5 to 10 µm clay particles |
| Leach | Two 10 m x 10 m tanks, 4 h, 70°C in the first tank | Not applicable | pH minus 0.7 |
| HCl addition | About 96 to 110 | kg/t ore | 37% HCl |
| Leach extraction | About 90, 84 after solution losses | % Li | |
| Impurity precipitation | NaOH and air to pH 7.5, about 2 h | Not applicable | Al and Fe hydroxides removed |
| Filtration | Six plate-and-frame filters, 215 plates of 2.5 x 2.5 m | Not applicable | Membrane squeeze to 25 bar |
| DLE | ARi simulated moving bed | Not applicable | About 98% Li adsorbed |
| Chlor-alkali | About 450 t/d chlorine, 400 t/d NaOH | Not applicable | INEOS electrolyzer |
Overview
Claystone is crushed in a roll crusher and stored in a 30,000 t covered stockpile. It is slurried with high-pH process water in a horizontal attrition scrubber. The slurry is leached with hydrochloric acid at 70°C, then neutralized with sodium hydroxide and air to precipitate aluminium, iron and other impurities. Plate-and-frame filters separate the lithium-bearing solution from the solids. The solution is ultrafiltered and passed through a simulated moving bed DLE system. The eluate, at about 600 ppm Li, is concentrated by reverse osmosis and precipitated with sodium carbonate as lithium carbonate. The DLE raffinate is cleaned of calcium and magnesium and fed to the chlor-alkali plant, or recycled. Tailings and precipitates are dry stacked in a lined facility at pH 7.5.
Key Process Stages
Ore receiving and crushing. A loader feeds a 60 t hopper over the double roll crusher, which has a rock breaker. An apron feeder takes the crushed ore past a metal detector to the stacker. A reclaimer moves up to 750 t/h to the scrubber.
Attrition scrubbing. The ore is mixed with pH 11.0 process water at 33% solids. The very fine clays have almost no cohesion when wet, so the scrubber breaks them down to their 5 to 10 µm interstitial size. A 1 mm horizontal screen removes oversize, which is washed and sent to tailings.
Leaching. Two covered, rubber-lined 10 m tanks with titanium agitators give four hours in total. The first tank is heated to 70°C with oil-filled shell-and-tube exchangers that also act as baffles. Acid vapour is captured in a water bath. About 25 to 35% of the solids dissolve, giving a leach solution of 280 to 320 ppm Li.
Precipitation and filtration. A 10 m tank holds pH 7.5 with 50% sodium hydroxide, about 2.2% of solids weight, for about two hours. Air oxidizes ferrous to ferric iron. Six membrane filters press the cake to under 30% solution, and lithium recovery at this point approaches 84%.
Clarification and DLE. A 0.5 µm ultrafiltration unit polishes the solution. Acid lowers it to pH 6.5, and 4,500 to 5,000 gpm is fed to the ARi DLE system. That system has two parallel modules of seven columns. Two columns load while the others wash, strip and rinse. The sorbent rejects over 99% of the sodium, potassium, aluminium and iron. The lithium is stripped with reverse osmosis permeate. A 1,000 psi RO unit then concentrates the eluate to 4 to 6 g/L Li.
Calcium-magnesium removal and chlor-alkali. Sodium hydroxide raises the raffinate to pH 11.7 to precipitate calcium and magnesium hydroxides. These are thickened, centrifuged and combined with tailings. The chlor-alkali plant regenerates chlorine (for hydrochloric acid) and sodium hydroxide, and its spent raffinate returns as process water.
Lithium carbonate. Sodium carbonate precipitates lithium carbonate, which is washed and dried. Conversion approaching 94% has been identified at 101°C.
Additional Interesting Data and Summary
The process design aims to make the most of the chlor-alkali plant and works within limits on water and power. The report notes that the process elements described are under patent application by the company. The neutral, non-acid-producing tailings are expected to allow the pit to be partially backfilled.
In summary, the 2026 Clayton Valley update is a claystone lithium flowsheet. It replaces conventional grinding with attrition scrubbing, uses hot hydrochloric acid leaching and simulated moving bed DLE, and closes the reagent loop through an on-site chlor-alkali plant.
Key Processes
- Double roll crushing and covered stockpiling
- Attrition scrubbing of claystone
- Hot hydrochloric acid leaching
- Sodium hydroxide precipitation of impurities
- Membrane plate-and-frame filtration
- Ultrafiltration and simulated moving bed direct lithium extraction
- Reverse osmosis concentration
- Lithium carbonate precipitation and drying
- Calcium-magnesium removal and chlor-alkali reagent regeneration
- Dry stacking of neutralized tailings
Source: Updated NI 43-101 Technical Report on the Feasibility Study of the Clayton Valley Lithium Project, Esmeralda County, Nevada, USA, prepared for Century Lithium Corp., effective date January 3, 2026.
Consolidated report summaries
The following former standalone pages about this operation were consolidated here on October 25, 2026. They are retained for source traceability; dates and figures reflect each report’s own effective date and may be superseded by the current information above.
Clayton Valley Lithium Project — 2024 Technical Report
The 2024 technical report for the Clayton Valley Lithium Project in Esmeralda County, Nevada, USA presents a feasibility-level process design for a phased lithium production plant based on hydrochloric acid leaching, direct lithium extraction, and chlor-alkali integration.
Report context
This NI 43-101 Technical Report on the Feasibility Study documents the recovery methods and process design for the Clayton Valley Lithium Project, dated 29 April 2024. The process design is based on testwork discussed in Section 13 of the report and is focused on Project Phase 2 at a nominal plant capacity of 15,000 t/d. The design incorporates a staggered start-up approach, with Project Phase 1 operating at 7,500 t/d prior to the installation of additional equipment and parallel trains for Phase 2. A Project Phase 3 expansion to 22,500 t/d was also evaluated, with additional equipment to be included as a separate plant facility.
Processing route
Feed Handling and Size Reduction
ROM claystone will be conveyed from the mine to a covered feed material stockpile equipped with a stacker/reclaimer system. Material is passed through a roll crusher to break down large size fractions, then conveyed to two attrition scrubber units where it is mixed with neutral-pH process water and disaggregated into a slurry. The slurry is discharged onto two single deck vibrating screens with an aperture of 0.85 mm (20 mesh). Oversize and tramp material is temporarily stored and periodically transferred to the tailings disposal conveyor, while screened undersize slurry gravity flows to leaching pump boxes.
Leaching and Neutralization
The leach circuit consists of two identical trains, each with a pump box, slurry heat exchanger, and four leach tanks. Leaching is conducted at atmospheric pressure and 60°C using hydrochloric acid as the dissolution agent. The screen undersize slurry is pumped through a slurry-slurry spiral heat exchanger to recover energy from the leach discharge, pre-heating the fresh slurry to approximately 35°C. Hydrochloric acid is added to the first leach tank at a ratio of 10.4% w/w to solids. Process water is added to achieve 33% w/w solids in the slurry. The 10 m diameter × 12.5 m high leach tanks are agitated, covered, and sized to provide one hour retention per tank, four hours total per train, operating in cascade.
Leach discharge from both trains passes through spiral heat exchangers and overflows into a single agitated surge tank where sodium hydroxide adjusts the slurry to pH 7. Neutralized slurry at approximately 30% w/w solids is pumped to the tailings filtration area.
Tailings Filtration
The tailings filtration area consists of two parallel filtration trains, each with a buffer tank distributing slurry to three filter feed tanks, each feeding two filter press units. The design considers eighteen 2.5 m × 2.5 m filter press units including two standby units. Filtrate is collected as PLS in the tailings filter filtrate tanks for lithium recovery. Filtered tailings cake is combined with centrifuge residue from the impurity removal stage and transported by belt conveyors, fifteen grasshopper units, and a mobile radial stacker to the dry tailings storage facility.
Lithium Ion Exchange
PLS is pumped to the PLS surge tank which overflows to the PLS pond, providing 12-hour surge ahead of the IX circuit. Forced aeration at the PLS pond allows precipitation of ferric compounds. PLS is pumped from the surge tank to the lithium IX columns consisting of 24 trains of three columns, totalling 72 units in lead-lag arrangement. Barren solution discharges through safety screens that scavenge lost resin, and collected resin is used for start-up loading and make-up during operation. Barren solution is pumped to the centrifuge precipitation tank.
Loaded resin is eluted, with eluate passing through safety screens to scavenge lost resin before gravitating to the eluate tank and pumped through polishing filters to the softening system. Resin specified in the plant design does not require a regeneration stage.
Softening Ion Exchange
The eluate enters the softening circuit where divalent cations (Ca²⁺, Mg²⁺, Ba²⁺, Sr²⁺, Fe²⁺, Mn²⁺) are exchanged onto resin while lithium passes through. Resin regeneration is performed using a salt solution. Regeneration backwash and weak waste solutions are returned to the process. The lithium-rich softening effluent is pumped to the RO system.
Reverse Osmosis
The softening effluent is filtered and treated in a two-pass RO system to concentrate and recover lithium and ensure permeate purity. The system consists of eight 1 μm cartridge filters, eight first-pass two-stage RO skids, and eight second-pass two-stage RO skids. First-pass reject is concentrated in dissolved ions including lithium and directed to the UHP-RO system. Second-pass reject is recycled to RO feed, and second-pass permeate reports to the permeate make-up tank for reuse.
DLE Discharge Impurity Removal
Discharge solution from the lithium IX circuit is pumped to the centrifuge precipitation tank where sodium hydroxide increases pH to 12, precipitating calcium and magnesium impurities. The slurry at approximately 1.5% solids is decanted in a 12 m diameter centrifuge feed thickener. Clear solution overflows to the centrate tank, and underflow at 10% w/w solids is centrifuged. Two centrifuges produce Ca/Mg precipitates at approximately 40% w/w solids, discharging onto the tailings conveyor. Centrate combines with thickener overflow and is pumped as feed to the chlor-alkali plant.
Lithium Concentration and Precipitation
The RO concentrate at an estimated 2.4 g/L Li undergoes further concentration via UHP-RO at 120 bar, reaching up to 130,000 mg/L TDS on a sodium chloride basis. The UHP-RO system consists of two skids/trains with high pressure and centrifugal pumps. Permeate is reused and reports to the RO permeate make-up tank.
The UHP-RO reject, at an estimated 4.1 g/L Li, is concentrated with the mechanical vapour recompression evaporator, consisting of three skids with three vessels each, total evaporation capacity 3,100 m³/d. The refined stream is pH-adjusted to 5 with HCl before evaporation. Distillate is reused as RO water.
The concentrated liquor at 9.7 g/L Li passes through final polishing to remove residual calcium and magnesium hardness. The liquor enters the CIX circuit at approximately 84 m³/h, distributed to three softening vessels with 7.4 m³ resin capacity each. The CIX circuit is designed to provide discharge concentrations below 1 mg/L calcium and magnesium within a 2.8-hour cycle time. Hydrochloric acid, sodium hydroxide, and RO water regenerate and rinse the resin. Weak waste solution is recycled to the RO raw water system, and high strength waste returns to the surge tank.
Lithium Carbonate Production
Effluent from the CIX circuit reports to a series of stirred lithium carbonation refining reactors where lithium is precipitated as lithium carbonate using 28% w/w soda ash solution. Four 7.6 m³ refining reactors are distributed in two modules with a capacity of 930 m³/d per module. Precipitation occurs at 80°C, maintained by direct steam injection. The reactors are highly automated to ensure high yield and quality.
The resulting lithium carbonate slurry at an estimated 3% w/w solids undergoes dewatering and washing through a single-stage peeler centrifuge to reduce water content to approximately 20% w/w. Blowdown solution from the centrifuge contains important lithium levels and reports to the mother liquor storage tank before recycling to the PLS surge tank. Centrifuge rinsing solution containing soda ash and lithium is recycled to the soda ash solution preparation tank. Two operational and one standby peeler centrifuge units with a capacity of 1.8 t/h each are considered in the design.
Lithium Carbonate Drying and Loadout
The washed lithium carbonate filter cake is conveyed by screw conveyor to an indirect electric rotary dryer with a capacity of 4 t/h. Dried lithium carbonate is discharged at 160°C to a blower, which pneumatically transports the material to a transfer bin feeding a magnetic detector and cage mill. The cage mill breaks up agglomerates formed in the dryer. Dust generated is captured in a baghouse and discharged into the transfer bin. Fine lithium carbonate is stored in a silo, packaged into 1 m³ bags, and loaded into intermodal shipping containers.
Chlor-alkali Plant
The chlor-alkali unit consists of two parallel trains. Process discharge from the lithium IX is mixed with depleted solution and concentrated to 300 g/L sodium chloride. The concentrated salt solution is purified through filtration, precipitation, and ion exchange steps to remove magnesium, calcium, lithium, boron, and aluminium. Purified salt solution passes through a heat exchanger before feeding electrolysers.
Each cell is divided into anode and cathode sides separated by an ion exchange membrane. Salt solution and 30% w/w caustic are fed to the anode and cathode chambers respectively. Hydrogen and chlorine gas feeds hydrochloric acid synthesis to produce 35–36% w/w HCl solution. Caustic is diluted and recycled to the electrolyser with excess used in the process plant.
Hydrochloric acid at 36% purity is produced at the chlor-alkali plant and pumped to storage tanks providing five days capacity. During start-up, HCl arrives by bulk tanker truck. Sodium hydroxide at 32% purity is produced and stored in two tanks with five days capacity. During start-up, NaOH arrives by bulk tanker truck.
Antiscalant is dosed at 5 mg/L to the RO feed water from drums using peristaltic pumps.
Water System
The water system consists of two separate circuits: make-up water and process water. Raw water is supplied from a new well to the raw water tank, then filtered and treated in an RO system. RO permeate is stored in the RO/fire water tank. Primary RO water usage is as permeate make-up for elution at the lithium IX system and reagent dilution in the IX, softening, and CIX systems. Raw water requirement has been estimated at 221 m³/h.
The plant design contemplates two process water circuits. A neutral-pH process water (PW1) circuit and a high pH (~12 pH) process water (PW2) circuit. PW2 is generated from the chlor-alkali plant and tailings filtrate. Excess PW2 is neutralized with hydrochloric acid and combined with raw water RO and process water RO reject streams to generate PW1. PW1 is used in the chlor-alkali plant, leaching tanks, and wash water in the tailings filters.
Excess neutralized water is treated in a process water ultrafiltration and RO system consisting of six UF filters and six two-pass/two-stage RO skids, recycling excess water back to the system.
Steam, Air, and Power
Steam is supplied from an electric steam boiler for process heating, primarily for the leaching circuit and lithium carbonation tanks. Two dedicated process air compressor systems provide high pressure compressed air for air squeeze on pressure filters and blowdown air on IX columns. Instrument air is used throughout the plant.
Power for processing facilities will be supplied via power lines from the electrical grid. Total power requirements are 113.75 MWh for Project Phase 1 and 174.69 MWh for Project Phase 2, with the chlor-alkali plant representing the largest consumer at 78.0 MWh and 120.0 MWh respectively.
Key reported parameters
| Design Parameter | Units | Project Phase 1 | Project Phase 2 |
|---|---|---|---|
| Nominal processing rate | t/d | 7,500 | 15,000 |
| Annual processing rate | t/y | 2,737,500 | 5,475,000 |
| Plant availability | % | 92 | 92 |
| ROM feed moisture | % | 20 | 20 |
| Processing plant feed rate (dry) | t/h | 340 | 680 |
| Leach temperature | °C | 60 | 60 |
| Leach retention time | h | 4 | 4 |
| Leach tanks/trains | units | 4 / 1 | 4 / 2 |
| Acid consumption | t/t feed | 0.104 | 0.104 |
| Filtration filters | units | 9 | 18 |
| Filtrate cake water content | wt % | 35 | 35 |
| PLS to lithium recovery | m³/h | 1,041 | 2,083 |
| Lithium solution feed to RO | m³/h | 99 | 198 |
| Solution feed to chlor-alkali plant | m³/h | 1,130 | 2,260 |
| Lithium carbonate production | t/d | 35.6 | 71.2 |
| Average lithium grade in feed | % | 0.113 | 0.113 |
| Lithium leach recovery | % | 80.2 | 80.2 |
| Overall lithium recovery | % | 78 | 78 |
| Total make-up water | m³/h | , | 221 |
| Chlorine production | t/d | , | 1,234 |
| Hydrogen production | Nm³/h | , | 16,607 |
| NaOH 100% production | t/d | , | 1,387 |
| HCl concentration (min) | % w/w | , | 36 |
| Electrolyser units | , | , | 24 |
| Cell elements per electrolyser | , | , | 86 |
| Salt storage | d | , | 5 |
Project website: https://noramlithiumcorp.com/resource/clayton-valley/
Project website: https://www.centurylithium.com/news/2021/cypress-development-provides-update-on-clayton-valley-lithium-projects-pilot-plant-status
Technical qualifications
This report presents a feasibility-level process design; it does not constitute a pre-feasibility or definitive feasibility study. Several elements of the process description are protected under patent application by the company, and the generalized descriptions of the DLE processes are proprietary to the company and its intellectual property license. The process design is based on testwork discussed in Section 13 of the source report, and the design parameters show design criteria rather than demonstrated operating performance. Power requirements are presented as design basis values in MWh, the unit used in the source table, and may be subject to refinement.
The report notes the process plant design is based on maximizing the use of the chlor-alkali plant and infrastructure limitations related to water and power availability. The process water RO system includes six UF filters and six two-pass/two-stage RO skids; the number of RO skids in the main concentration section is eight first-pass and eight second-pass units. Water balances include unquantified elements in certain circuits. The raw water requirement is described as estimated at 221 m³/h.
Source: Clayton Valley Lithium Project, Esmeralda County, Nevada, USA, NI 43-101 Technical Report on the Feasibility Study, Project No.: 252456, 29 April 2024, Recovery Methods, Section 17.
Century Lithium’s Clayton Valley: DLE & Carbonate Recovery Process
Century Lithium’s Clayton Valley: DLE & Carbonate Recovery Process
Source: Century Lithium Corp (2026)
Website: https://www.centurylithium.com/news/2024/century-lithium-announces-positive-feasibility-study-for-the-clayton-valley-lithium-project-nevada
Critical Data
| Parameter | Value | Unit | Notes |
|---|---|---|---|
| Throughput | 7,500 | t/d | Phase 1; Phase 2 increases to 15,000 t/d |
| Mill Power | Not specified as total; attrition scrubber motor is 350 hp | ||
| Target Grind Size | 5–10 | μm | Interstitial particle size after attrition scrubbing |
| Head Grade | 0.113 | % | Average lithium grade in feed material |
| Recovery % | 84 | % | Overall lithium recovery from feed to final product |
| Processing Capacity | 7,500 | t/d | Nominal dry feed rate for Phase 1; 92% plant availability |
| Energy Consumption | Not provided in source; chlor-alkali plant produces 450 t/d NaOH, 400 t/d Cl₂ | ||
| Water Consumption | 36.3 | m³/h | Total make-up water for Phase 1 (73.2 m³/h for Phase 2) |
| Operating Hours | 22.08 | hours/day | Based on 92% plant availability |
Overview
Century Lithium Corp. operates the Clayton Valley Lithium Project in Esmeralda County, Nevada, USA, a flat-lying clay-hosted lithium deposit at the Angel Island deposit. The feasibility study, effective January 3, 2026, details a comprehensive recovery methods flowsheet designed to produce high-purity lithium carbonate from fine-grained claystone. The process is significant for its innovative integration of attrition scrubbing for comminution, hydrochloric acid leaching, selective direct lithium extraction (DLE), and a chlor-alkali circuit that regenerates hydrochloric acid and sodium hydroxide for on-site reuse. This closed-loop approach minimizes chemical trucking and enhances sustainability. The plant initially processes 7,500 tonnes per day (t/d) in Phase 1, expanding to 15,000 t/d in Phase 2, achieving an overall lithium recovery of 84% from a feed grade averaging 0.113% Li. The flowsheet was developed and refined through pilot-scale operations at the Amargosa Valley Pilot Plant, validating key parameters such as leach extraction of 95% and DLE recovery of 98%. By combining attrition scrubbing, pH-controlled precipitation, ultrafiltration, and simulated moving bed DLE technology, Century Lithium demonstrates a technically viable and economically sound approach to unlocking the value of claystone lithium resources.
Key Process Stages
- Stage 1: Ore Receiving and Crushing – ROM claystone ore is trucked to a 30,000-ton covered stockpile. A 60-t feed hopper feeds a 24-in × 48-in double roll crusher, reducing ore to minus 4 inches. A variable-speed 4-ft × 25-ft McLanahan apron feeder and a stacker/reclaimer with 750 t/h capacity convey crushed ore to an attrition scrubber. Dust control via hood and baghouse ensures environmental compliance.
- Stage 2: Attrition Scrubbing – Crushed ore is mixed with high-pH process water at 33% solids in a 10-ft diameter × 30-ft long McLanahan horizontal attrition scrubber (350 hp). The scrubber breaks particles down to their interstitial size of 5–10 microns, liberating the clay crystalline structure. The slurry passes a 1-mm screen; oversize is conveyed to tailings while the undersize feeds the leach circuit.
- Stage 3: Leaching – The sized slurry enters two covered, rubber-lined leach tanks (10-m tall × 10-m diameter) with titanium agitators at 300 rpm. Leaching occurs at 70°C and pH -0.7 using 37% hydrochloric acid at ~4.8% of solids weight (96–110 kg HCl per tonne ore). Combined tank volume provides a 4-hour residence time. Lithium leach extraction reaches 90%, with overall extraction accounting for solution losses at 84%.
- Stage 4: Precipitation and Tailings Filtration – Leach slurry flows to a baffled precipitation tank (10-m × 10-m) where 50% sodium hydroxide raises pH to 7.5 for 2 hours, precipitating Al, Fe, and other deleterious elements as hydroxides. Air oxidizes ferrous to ferric iron. The slurry then feeds six plate-and-frame filters (215 plates each, 2.5-m × 2.5-m, membrane squeeze to 25 bar) achieving <30% cake moisture. The filtrate (direct lithium extractant, DLE) is polished through a 0.5-micron ultrafiltration unit.
- Stage 5: Direct Lithium Extraction and Elution – Clarified DLE solution (250–350 ppm Li, pH adjusted to 6.5) flows to a simulated moving bed DLE system from ARi using two parallel trains of seven columns (7–14-ft diameter × 9-ft high). Lithium adsorbs onto a proprietary aluminum hydroxide sorbent with 98% recovery. Stripping with reverse osmosis permeate produces an eluate of ~600 ppm Li, which is further concentrated to 4–6 g/L Li via a secondary RO unit. Raffinate is sent to Ca/Mg removal and then to the chlor-alkali circuit for chemical regeneration.
Additional Interesting Data and Summary
The Clayton Valley Lithium Project recovery system is underpinned by extensive pilot-scale testing and a robust process design basis. Key technical metrics include a leach temperature of 70°C with a 4-hour retention time, acid consumption of 6% by solution weight, and a lithium leach extraction of 95%. The DLE circuit achieves 98% lithium recovery while rejecting over 99% of Al, Fe, and Mg, and >95% of Ca, producing a high-grade eluate at 6.8 g/L Li after RO concentration. Lithium carbonate precipitation uses sodium carbonate at 1.1× stoichiometric ratio at 101°C, achieving 94% conversion rates. The chlor-alkali plant, designed with INEOS electrolyzers, produces 450 t/d of 32% sodium hydroxide and 400 t/d of chlorine (as 37% HCl), enabling closed-loop recycling of key reagents. Environmental considerations are integral: the tailings are non-acid producing (ABA testing confirmed), dry-stacked in a lined facility at pH 7.5, with the pit partially backfilled. Water recycling is emphasized; total make-up water is only 36.3 m³/h for Phase 1, minimizing freshwater demand. Sustainability initiatives include on-site chemical regeneration that reduces truck transport of HCl and NaOH, and the use of a hydrogen electrolyzer to manage by-product gases. Economically, the project produces 35.6 t/d of lithium carbonate in Phase 1 (71.2 t/d in Phase 2) at an average feed grade of 0.113% Li. The flowsheet is designed for modular expansion, with DLE and chlor-alkali units easily scalable. Future optimization is expected as the project advances, but the current feasibility study confirms technical viability. This integrated approach positions Century Lithium Corp. as a leader in sustainable claystone lithium processing, combining innovative DLE technology with chemical regeneration to achieve high recoveries with minimal environmental footprint. The plant’s 84% overall lithium recovery, low water consumption, and non-acid generating tailings underscore its potential as a benchmark for responsible lithium production in the Nevada basin.
Key Processes: Gravity Separation, Crushing
Target Commodities: Lithium
