At Agbaou, the target deposit type being explored for is the mesothermal auriferous sulphide (pyrite + pyrrhotite) and quartz vein style mineralization. The gold mineralization within Agbaou deposit is hosted within a specific quartz vein type that occurs along a broad area and can be characterized by a wide range of quartz-vein types, brecciation, boudinage, sericitic and carbonate alteration.

The lateritic cover is generally between five and ten metres thick with a very well developed weathering profile is over much of the area.

Mineralization at Agbaou can be broadly separated into two categories: laterite cap (generally >0.5g/t Au) and primary (free gold and sulphide hosted). The laterite cap, which covers the entire deposit area, is of variable thickness (1 to 5m) and represents secondary (re-mobilized) mineralization. The primary mineralization is associated with a system of gold bearing quartz-veins hosted by tightly folded Birimian-age sedimentary and volcanic rocks. The quartz veins can occur within either meta-volcanic or meta-sedimentary rocks, but the host rock is typically strongly sheared. The primary mineralized envelope is broad (60 to 100m), consisting of a number (up to seven zones in Agbaou Main) of mineralized zones that generally follow the limb of the regional fold. Particulate gold mineralization is located within quartz veins and along wall rock-quartz vein boundaries.

The mineralized quartz veins at Agbaou have a visually distinctive texture that has been described as “mottled”. Gold mineralization is also associated with variable amounts of sulphides, mainly pyrrhotite and pyrite. These veins are easily identifiable in the diamond drilling core intersections from the fresh rock below the saprolite/fresh rock boundary. The deposits are aligned along a northeast trending, steeply southeast dipping structure that marks the axial plane of the large-scale, regional fold.

Contractor-based mining was the preferred option for Agbaou and BCM was the selected mining contractor. BCM is responsible for the site preparation (including removal of vegetation) haul road construction, excavation and haulage of ore to the Run of Mine (“ROM”) pad and waste to the waste dumps, oversize breakage and equipment maintenance.

The mining operations are based on the use of hydraulic excavators and haul truck fleet engaged in conventional open pit mining techniques. The excavators load the free-dug or blasted material into the haul trucks, with the ore being transported to the processing area and the waste to the designated local waste dumps. Access roads will be developed as required for access into new areas. Where necessary, the main arterial roads outside of the pits, will be constructed to a minimum 30m width, including berms and drainage areas.

Topsoil in mining areas will be recovered during the pit preparation phase and stockpiled for future use with progressive waste dumps and possible pit rehabilitation.

The majority of the gold mineralized material will be transported to the ROM area, and discharged directly into the feed hopper.

The in-situ materials in hard and semi-hard rock will require drilling and blasting to assist fragmentation and subsequent loading. The oxide portion of the ore body is free digging or may be in need of light blasting in certain areas.

The process plant is designed to treat either 1.6Mt per annum of saprolite ore or 1.34Mt of bedrock ore, or a combination of the two ore types if required.

The proposed process design criteria consist of crushing, ore stockpiling, milling and classification, gravity and in-line leach reactor (“ILR”), CIL, cyanide detoxification, tailings disposal, acid wash, elution, electrowinning and gold room, carbon regeneration, consumables, oxygen and air services; and water services.

The crushing plant will treat both saprolite and bedrock ore at a rate of approximately 300 wet tonnes per hour to deliver a product size of 100% passing 150mm through a primary jaw crushing circuit. Design availability is for 80% utilization for the crushing circuit.

ROM ore is trucked and either placed on the ROM pad or tipped directly into a 200 tonne ROM bin fitted with a 1000mm x 800mm inclined static grizzly to scalp off any oversize material. Ore is transferred from the bin by a mechanical apron feeder that discharges crusher feed onto a vibrating grizzly feeder with 120mm spacing. The vibrating grizzly feed undersize material is pre-scalped to provide cushioning and conveyor belt protection from the oversize material which is discharged into and through a single toggle Jaw Crusher that reduces the ore size to 100% passing 150mm.

Crushed ore reclaimed from the surge bin and is conveyed to the SAG mill. Dilution water is added to the SAG mill to achieve the required 50% w/w solids density for saprolite material and 70% for bedrock in the SAG mill discharge for optimum grinding efficiency.

A portion of the cyclone underflow feed stream reports onto a gravity scalping screen to remove the +2.5mm coarse material. Dilution water will be added to the scalping screen feed box to decrease the concentrator feed solids density to 55% for saprolite ore and 50% for bedrock ore. The screen oversize returns to the ball mill feed stream to be re-ground and re classified while the screen undersize is fed to a gravity concentrator to recover the free gold. Concentrator tails gravitate back to the common mill discharge sump.

The leaching of gravity concentrates is a batch recovery and treat process using an ILR. The leach solution is prepared by first adding caustic to water for pH adjustment and then sodium cyanide to a 2% concentration. The leaching of gold is effected by circulating the 2% cyanide solution through a rotating reactor drum. Oxygen is added to the circulating leach solution during the step process stage to increase the gold leaching rate.

The pregnant eluate in the gravity pregnant tank is re-circulated through a dedicated electrowinning cell for the recovery of gold. Loaded cathodes are periodically removed from the electrowinning cell where the gold sludge is pressure washed off the stainless steel cathodes using highpressure guerney. Gold sludge is decanted, vacuum filtered and transferred to a calcining oven for drying prior to fluxing and Smelting for bullion production.

The screened leach feed slurry (cyclone overflow) is sampled for metallurgical accounting before gravitating into the CIL tanks, where pressure swing absorption oxygen plant (“PSA”) (Enriched) oxygen is added down shaft on the tank agitators to increase the gold leaching rate.

The CIL circuit consists of six tanks, each with a live volume of 2000m³, resulting in a total retention time of 25.6 hours for saprolite ore and 36.8 hours for bedrock ore. Each of the six CIL tanks are equipped with dual impeller agitators to keep the slurry and carbon particles in suspension during the leach process.

Regenerated, eluted or virgin carbon is added to the last CIL tank. Recessed impeller vertical spindle pumps are installed in the CIL tanks to periodically transfer carbon upstream from CIL tank 6 to CIL tank 1. Loaded carbon in CIL tank 1 is periodically pumped onto a vibrating loaded carbon screen for downstream acid washing and elution purposes. The slurry is returned to CIL tank 1. High pressure water is sprayed on the screen to ensure that clean carbon reports as screen oversize to the acid wash column. The tails slurry leaving the last CIL tank gravitates to a carbon safety screen where carbon is recovered as oversize and slurry reports to the cyanide detoxification circuit.

Loaded carbon recovered from CIL tank 1 is discharged from the loaded carbon screen into a dedicated acid wash column. The acid wash column is sized to accommodate 6 tonnes of loaded carbon. During the acid wash cycle dilute hydrochloric acid solution (3% HCl) is circulated from the acid wash tank through the acid wash column. The solution exiting the column returns to the acid wash tank via the external strainers that prevent any carryover of carbon from the column to the acid wash tank.

The elution of gold from loaded carbon is done using the Split Anglo American Research Laboratories method (“AARL”).

The pregnant eluate from the elution column is directed to fill the pregnant tank. When the electrowinning circuit is available, the pregnant solution is re-circulated through the CIL electro-winning cell.