The principal model for gold mineralization at the Kirazli Gold Property is a high-sulphidation, epithermal gold deposit. Examples of this kind of deposit in the world are Yanacocha, Pierina and Alto Chicama in Peru. Most high-sulphidation deposits are large, low-grade bulk-tonnage systems (Yanacocha), though vein-hosted high-sulphidation deposits also occur (El Indio).

At Kirazli, gold mineralization is hosted within heterolithic phreatomagmatic/phreatic breccia bodies cutting through Miocene-age andesitic tuffs. Mineralization can generally be subdivided into two main types:

- A regional low-grade gold zone that underlies much of Kirazli, broadly enveloping the high-grade gold zones. This low-grade mineralization occurs both above and below the redox horizon. The widespread, low-grade mineralization is interpreted to be early and may be associated with the broad epithermal alteration that resulted in the chalcedonic silica (the second silica event);

- Four elongate bodies of high-grade gold mineralization occur in the advanced argillic zone overlapping slightly the bottom of the 1 km-long silica cap and the silica roots. High-grade gold mineralization also shows a strong spatial relationship with the margins of heterolithic breccia bodies. These bodies transect the redox boundaries. The subhorizontal section below the silica cap is in oxide or sometimes in transition zone while the bottom of the vertical section associated with the silica roots is in sulphide.

- The first high-grade body (A) is followed over more than 400 m in a northsouth direction from section 30650N to section 30250N. It coincides with the subvertical silica root and the phreatic breccia pipe and extends in the advanced argillic alteration mostly east of the root. Towards the top, it flares and extends subhorizontally eastward for 100 m below the silica cap end the subhorizontal eastern extension of the phreatic breccia but affects its lower portion too. The highest grade section coincides with the flat portion below the silica cap. Grades there may be spectacular as in drill hole KD-09 with 4.6 g/t Au over 38.5 m.

- The second high-grade body (B) is followed over 150 m in a north-south direction from section 30100N to section 29950N. It coincides with the advanced argillic alteration immediately west of the silica root but does not affect it. Towards the top, it extends westward for 50 m below the silica cap and affects its lower portion too.

- The third high-grade body (C) is followed over 250 m in a north-south direction from section 30100N to section 29850N. It coincides with the advanced argillic alteration immediately east of the silica root but does not affect it. Towards the top, it extends eastward for 50 m below the silica cap and affects its lower portion too. The highest grade portion coincides with the flat portion below the silica cap. Grades there may be spectacular too as in drill hole 10-KD-143 with 5.4 g/t Au over 39.5 m.

- The fourth high-grade body (D) is followed over 100 m in a north-south direction from section 29900N to section 29800N. It only affects advanced argillic altered andesites and phreatic breccias following a vertical direction until it bends to the west below the silica cap.

The Kirazli deposit will be mined by conventional open pit hard rock mining methods. Alamos Gold plans to utilize a contract mining company to move the ore and waste from the pit. The Mineral Reserve is the total of the Proven and Probable material that is planned for processing within the mine plan. Oxide and transition ore at Kirazli will be crushed, agglomerated, conveyed and stacked on to a heap leach pad where it will be cyanide leached for the recovery of gold and silver.

During pre-production, waste will be mined to construct the heap leach facility (KHLF) foundation. Any ore incurred during pre-production will be stockpiled and re-handled to the crusher once the facilities are ready for ore processing. After a six month ramp-up period, the mine is expected to produce ore at a rate of 15,000 t/d (5.25 Mt/a) for five years. Waste produced over the mine life will be used for construction of the KHLF foundation, backfilled into the pits once mining is complete or sent to the waste rock storage facility.

The following design criteria are for engineering, design and specification of the process requirements for the Kirazli Project. The process facilities encompass the following operations for 15,000 dry metric tonnes per day (dMt/d) operation:
- Primary crushing and coarse ore stockpile;
- Secondary crushing;
- Agglomeration;
- Heap leaching;
- Carbon adsorption, desorption and recovery;
- Electrowinning and refining;
- Water treatment; and
- Reagents.

ROM at nominally minus 800 mm (P100 will be 800 mm and P80 will be 64.7 mm), will be fed into the dump hopper that discharges using an apron feeder at a rate of 833 t/h. The dump hopper area is equipped with water and compressed air for dust suppression. The apron feeder will discharge into a vibratory grizzly that separates the ore at 150 mm. Undersize from the vibratory grizzly discharges onto the primary crushing discharge conveyor. Oversize from the vibratory grizzly is fed to the primary crusher. A rock breaker will be installed for breaking the occasional rocks larger than 800 mm.

The primary crusher will reduce the ore size to a P100 of 260 mm (P80 of 60 mm), at a rate of 833 t/h. Ore discharging from the primary crusher will be combined with the underflow from the vibratory grizzly and conveyed using the primary crushing discharge conveyor, to the stockpile feed conveyor. The stockpile feed conveyor is equipped with a weight scale for material balances. The coarse ore stockpile will have a live capacity of nine hours. The coarse ore stockpile will be continuously reclaimed using two of the three reclaim apron feeders (two operating, one standby).

Crushed ore from the secondary discharge conveyor feeds the overland conveyor at a rate of 833 t/h. Overland conveyor will also receive Portland cement at a rate of 2.5 kg/t of ore from the cement silo prior to discharging into the agglomeration drum. Barren solution will be added to the agglomeration drum to bring the ore moisture content to 7.5%. The agglomerated ore is discharged onto the heap feed conveyor where concentrated sodium cyanide solution is dripped onto the ore at a rate of 1 L/hr using the leach activator pump.

A design for 833 t/h of agglomerated ore from the heap feed conveyor is transferred to the heap leach pad through a series of conveyors.

The heap leach will be built by placing the ore in 10 m lifts using the radial stacker.

The leach pad will be built using multiple-lifts with a capacity for approximately 35M dry tonnes. The leach cycle is designed for 90 days of ore leaching, where dilute sodium cyanide solution is applied using drip emitters and sprinklers at a rate of 10 L/h/m².

Barren solution from the adsorption-desorption-recovery (ADR) circuit will be pumped into the barren solution tank which will have an approximate one hour residence time of 850 m³. Barren solution will be pumped onto the heap, using vertical turbine pumps, at a rate of 844 m³/h. Concentrated NaCN solution will be added to the barren solution tank and antiscalant will be added to the suction side of the barren solution pumps using metering pumps.

As the cyanide solution migrates through the ore, it leaches the gold, silver and any cyanide soluble metals. The pregnant solution is collected at base of the heap pad on the geomembrane liner. Drainage pipes throughout the heap pad will drain the pregnant solution into the pregnant solution sump at a rate of 841 m³/h.

A single event pond will be included to handle storm events, power outages or pump/piping failures. The event pond will have the capacity to receive excess solution from the pregnant solution pond. The event pond can also be pumped to enhanced evaporation. The pregnant solution pond will be capable of transferring solution to the event pond, the pregnant solution sump or to the barren solution tank.

The adsorption circuit will process 841 m³/h of pregnant solution from the pregnant solution pond. The adsorption circuit consists five carbon columns that hold 10.6 t of 6 x 12 mesh activated carbon each. Each column is equipped with internal diaphragms with bubble caps. The columns have flared tops to allow for excess solution, or turn-up, due to a storm event. The carbon columns are arranged in cascading fashion. Pregnant solution will first flow over a trash screen into a head tank. The pregnant solution in the head tank gravity feeds the first carbon column. The solution flows from column to column by gravity and the flowrate is controlled by dart valves. Solution leaving the fifth column is discharged over a carbon safety screen and collected in the barren surge tank.

Carbon is transferred from tank to tank by use of a single carbon transfer pump. Carbon is pumped countercurrent to the flow of the pregnant solution and is discharged from the first column. Loaded carbon will be transferred in 5.3 t batches to the loaded carbon holding tank.

The carbon desorption circuit consists of two mild steel vessels sized to hold 5.3 t of loaded carbon each. 5.3 t of loaded carbon is pumped from the carbon holding tank to one of the strip columns. The remaining carbon from the absorption circuit will be pumped into the other strip column.

Barren solution from the electrowinning cell, combined with sodium hydroxide and cyanide solution, is pumped through a plate and frame heat exchanger. Additional sodium hydroxide and cyanide solution will be supplied from the reagent area. The solution will be further heated to 143°C and 297 kPa by an electric boiler circulating through a primary heat exchanger, heat recovery exchanger, and a cooling heat exchanger. The heated solution is then fed through the bed of loaded carbon in the strip vessels where the metals are extracted into solution.

Pregnant solution will be pumped from strip column through the cooling heat exchanger and into the electrowinning feed tank. The solution from the feed tank is pumped into four, 100 ft3 (2.83 m3 ), high efficiency sludge type electrowinning cells. Gold, silver and other potential metals will be plated onto stainless steel cathodes.

The barren solution is recycled back to the strip vessel, with sodium hydroxide and cyanide makeup, for further stripping. After approximately every third strip cycle, the strip solution will be discharged to the barren solution tank and new strip solution will be prepared.

Once the carbon is stripped, the carbon will be pumped to the acid wash circuit. The acid wash circuit will also be piped in a fashion that acid washing can preformed prior to stripping as well.

Carbon will be pumped into the acid wash vessel and then pre-rinsed with fresh water to remove any residual cyanide solution. The rinse water will discharged to the barren solution tank. Concentrated hydrochloric acid is added to fresh water in the dilute acid tank to achieve a pH of between 1.0 and 2.0. The acid wash solution is pumped into the bottom of the acid wash vessel to remove any scale or inorganic contamination. The solution is recirculated in the vessel until a pH of 2.0 is discharged. The spent acid solution is discharged to the acid neutralization tank, where the pH is brought up to 10.5 using sodium hydroxide. The neutralization solution is then pumped to the barren solution tank. Process water is then pumped through the acid washed carbon to remove any residual chlorides. The rinse solution will also be transferred to the barren solution tank.