The Maria Dama processing plant operates at 2,000 tpd capacity with a flowsheet incorporating crushing, grinding, gravity concentration, flotation, cyanidation, Merrill-Crowe precipitation, and polymetallic sulphide recovery.
Report context
This technical report is dated effective September 30, 2023 and describes the Segovia Operations located in Antioquia, Colombia. The report documents the recovery methods employed at the historical Maria Dama processing plant, which has been continually maintained and operational since mining began at Segovia and upgraded over the years to its current capacity. The process feed includes material mined by Aris Mining and partner-mining from within the Property titles, as well as material mined by smaller groups outside of the Property titles. Approximately 43% of production is sourced from partner mining.
Processing route
Crushing
Ore from owner operated mines is crushed to 15 mm in a two stage crushing circuit consisting of a 20 inch x 36 inch 150 horsepower (hp) jaw crusher that discharges to a crushed ore bin. The primary crushed ore is screened at 15 mm on a 1.9 m x 4.7 m double deck vibrating screen, with oversize conveyed to a 4 foot 200 hp secondary cone crusher and a 200 hp tertiary cone crusher operated in closed circuit with a secondary 1.8 m x 6.0 m vibrating screen. Another crushing line is available on standby, comprised of a 150 hp primary jaw crusher, two 200 hp secondary cone crushers, and two vibratory screens. The final crushed product is produced at 80% passing 7 mm, sampled with a primary cross-cut sampler and a secondary rotary sampler as it is conveyed to the fine ore bin. Samples are assayed by the Property's analytical laboratory.
Ore from partner operated mines does not require crushing and is dumped into a receiving bin, then sampled on a primary cross-cut sampler and a secondary rotary sampler and conveyed to a separate fine ore bin. Partner ore samples are assayed by an external commercial SGS laboratory.
Grinding and gravimetric concentration
The combined crushed owner and partner ore is conveyed on a single belt to a grinding circuit comprised of a 2,000 tonne per day capacity, 12.5 foot x 23 foot 2,300 hp ball mill operated in a closed circuit cluster of four hydrocyclones (with two on standby) to produce a final grind of 80% passing 106 microns, which advances to the flotation circuit. Half of the cyclone underflow is diverted to the gravity concentration circuit comprised of two 40 hp Knelson centrifugal concentrators, operating in closed circuit with the grinding circuit. Approximately 30% of the contained gold is recovered into a primary gravity concentrate, then upgraded on a Gemini table. The grinding circuit feed is continuously weighed on a belt scale and sampled every hour.
Flotation and regrind
Cyclone overflow from the grinding circuit advances to the flotation circuit for conditioning with flotation reagents. The conditioned slurry passes through one stage of rougher flotation in a 40 cubic metre tank cell, with the overflow passing to one 30 cubic metre cleaner cell and then three stages of scavenger flotation in three 30 cubic metre flotation cells to recover the contained gold. The rougher and scavenger flotation concentrate is upgraded in one stage of cleaner flotation and combined with the rougher flotation concentrate. The combined rougher and scavenger cleaner concentrate is thickened to around 55% solids and reground in a 4 foot x 8 foot 40 hp ball mill to approximately 80% passing 38 microns, then passed to the cyanidation circuit. The regrind ball mill is operated in closed circuit with 6 inch cyclones. The flotation tailings are pumped to the tailings storage facility where they are thickened and filtered to around 15% moisture prior to dry stack placement. The thickener overflow and filtrate solutions are recycled back from the tailings storage facility to the process plant.
Cyanidation and counter current decantation
The reground flotation concentrate is thickened and processed in a cyanidation circuit comprised of four agitated leach tanks operated in series for a total leach retention time of around 96 hours. The cyanide concentration is adjusted in the first leach tank and allowed to attenuate naturally in the last leach tank. The pH of the leach slurry is maintained at around 10.5 to 11 with the addition of lime. Discharge from the last agitated leach tank flows to the counter current decantation circuit, comprised of one 24 foot diameter thickener, two 16 foot diameter thickeners, and one 42 foot diameter thickener to wash the pregnant leach solution from the leach residue. The pregnant leach solution from the first thickener overflow advances to the Merrill-Crowe recovery circuit. The tails of the leaching process are detoxified using hydrogen peroxide and iron sulphate, then passed to the polymetallic concentrate processing plant.
Merrill-Crowe and refining
The solubilized gold and silver are recovered from the pregnant leach solution by clarifying the solution to remove any remaining suspended solids, de-aerating the solution to less than 1 ppm dissolved oxygen, and then precipitating the gold and silver with the addition of zinc dust. The gold and silver precipitate is recovered in three plate and frame pressure filters, then smelted with a flux in a gas fired furnace to produce the doré product. The gravity concentrate produced by the Gemini table is separately smelted with a flux in a gas fired furnace to produce a second doré product.
Polymetallic concentrate plant
A 200 tonne per day capacity polymetallic concentrate plant was constructed in 2021 to clean lead and zinc sulphides from the tailings generated by the Maria Dama processing plant. The tailings are passed to a five cubic metre conditioning tank in the lead circuit and treated with regulating reagents to depress sphalerite, pyrite, and insoluble materials. The tails proceed to a second five cubic metre conditioning tank treated with collectors that react with lead sulphides. Once conditioned, the pulp goes to a rougher stage consisting of a bank of four rougher cells with forced air that operate in parallel with a single scavenger feed cell where flotation begins. The flotation concentrates are taken to three cleaning cells with a total capacity of 1.2 cubic metres. The depleted tails then pass to the zinc circuit, and the recovered and cleaned lead concentrate from the cleaning stage is transported to the thickening area.
Zinc flotation takes place in a circuit similar to the lead flotation, starting with two stages of conditioning that activates the sphalerite depressed by the reagents in the lead circuit. Flotation begins in the rougher stage, then the flotation concentrates are taken to the cleaner and scavenger stage, and the final tails are pumped to the tailings filtration plant at the dry stack tailings facility.
The lead and zinc concentrates are pumped to separate thickeners to obtain a solids percentage of around 55 to 65%, then discharged to a lead or zinc homogenizer tank used as a pre-filtration stage, then pumped to separate hydraulic filter presses. The dried lead and zinc concentrates are separately packed in 1,000 kg capacity bags and stored in a warehouse prior to shipment to the concentrate buyer. The first concentrate was exported in December 2022.
Power, water, and process material requirements
The Property consumes a total of 100.5 GWh annually from public and private power producers. The processing plants require 47.0 litres of water per second for an annual consumption of 1.5 million cubic metres, sourced from underground dewatering and rainwater runoff stored in a surface pond near the Maria Dama processing plant. Reagent and grinding ball use includes mineral activators, frother, and collector in the flotation circuit, flocculants in the thickening circuit, sodium cyanide and lime in the cyanidation circuit, zinc dust in the Merrill-Crowe circuit, hydrogen peroxide in the cyanide detoxification circuit, a variety of fluxes in the refinery, grinding balls in the primary grinding and regrind circuit, and other standard processing chemicals.
Recommendations
An opportunity exists to increase the capacity of the Maria Dama processing plant from 2,000 to 3,000 tpd by utilizing a previously purchased ball mill already located at the Property, and by relocating and upgrading the facilities that receive material from the Segovia Operations' artisanal and small scale mining partners. This creates the potential to gradually increase annual gold production from 200,000 to 300,000 ounces of gold by filling the extra capacity by increasing mining rates. A portion of the extra capacity may be allocated to the Segovia Operations' artisanal and small scale mining partners. The addition of the ball mill to the existing circuit would enable both higher throughput and more effective use of available capacity, thereby enhancing the overall gold recovery rate for all processed materials. An upgraded receiving facility for partner mined material could also be designed to increase volumes and efficiencies. This small-scope project could be completed by early 2025 at an estimated cost of US$11.0 million.
Key reported parameters
| Parameter | Value | Units | Basis |
|---|---|---|---|
| Maria Dama plant capacity | 2,000 | tpd | Historical operating |
| Crushed product size | 80% passing 7 | mm | Design |
| Grind size (primary) | 80% passing 106 | microns | Design |
| Regrind size | 80% passing 38 | microns | Design |
| Ball mill power (primary) | 2,300 | hp | Design |
| Ball mill dimensions (primary) | 12.5 x 23 | foot | Design |
| Gravity gold recovery | 30 | % | Historical operating |
| Leach retention time | 96 | hours | Design |
| Leach pH | 10.5 to 11 | , | Design |
| Polymetallic plant capacity | 200 | tpd | Design |
| Concentrate solids (polymetallic) | 55 to 65 | % | Design |
| Tailings moisture (dry stack) | 15 | % | Design |
| Annual power consumption | 100.5 | GWh | Historical operating |
| Water consumption | 47.0 | litres/second | Historical operating |
| Annual water consumption | 1.5 | million cubic metres | Historical operating |
| Partner mining production share | 43 | % | Historical operating |
| Proposed capacity expansion | 3,000 | tpd | Proposed design |
| Proposed annual gold production increase | 200,000 to 300,000 | ounces | Proposed design |
| Expansion estimated cost | US$11.0 | million | Proposed design |
| Expansion completion target | Early 2025 | , | Proposed design |
Project website: https://aris-mining.com/operation/segovia/
Project website: https://digbee.com/organisation/401-bay-street-suite-2400-po-box-15-toronto-on-m5h-2y4/overview
Technical qualifications
The technical report specifies that the qualified person responsible for Section 17 (Recovery Methods) recommends implementing the small-scope capacity expansion project. The report does not provide testwork results for the proposed expansion, nor does it include detailed mass balances, metallurgical recoveries, or equipment sizing calculations for the upgraded circuit. The historical operating data for the Maria Dama plant is presented as descriptive information without supporting testwork or performance data for individual unit operations. The polymetallic concentrate plant is described as constructed in 2021, with the first concentrate exported in December 2022, but no operational performance data or metallurgical testwork results are provided for this circuit.
Source: NI 43-101 Technical Report for the Segovia Operations, Antioquia, Colombia, effective September 30, 2023, Section 17 Recovery methods.
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.
Segovia Prefeasibility Study — 2020 Technical Report
This prefeasibility-level technical report for the Segovia Project presents mineral resource and reserve estimates, process plant operating data, and metallurgical testwork for the Carla orebody.
Report context
This NI 43-101 Technical Report was prepared by SRK Consulting (U.S.), Inc. for Gran Colombia Gold Corp. on the Segovia Project, which comprises the Providencia, El Silencio, and Sandra K mines, and the Carla Project. The effective date of the report is December 31, 2019. The report provides Mineral Resource and Mineral Reserve estimates prepared in accordance with CIM Definition Standards (2014). Mineral Resources are reported inclusive of Mineral Reserves. The quality of information, conclusions, and estimates contained herein are consistent with the level of effort involved in SRK’s services, based on information available at the time of preparation, data supplied by outside sources, and the assumptions, conditions, and qualifications set forth in this report.
Processing route
Maria Dama process plant flowsheet
GCG ore is processed through the Maria Dama process plant utilizing a process flowsheet that includes crushing, grinding, gravity concentration, gold flotation, concentrate regrinding, concentrate cyanidation, Merrill-Crowe zinc precipitation and refining of both the zinc precipitate and gravity concentrate to produce a final gold/silver doré product. The Maria Dama plant has a capacity of 1,500 t/d.
Historical plant performance
Plant production for the period 2017 to 2019 increased from 293,395 t of ore at an average gold grade of 16.85 g/t Au in 2017 to 451,450 t at an average gold grade of 15.48 g/t Au during 2019. Overall gold recovery has ranged from 93.8 to 95.9% over the period 2017 to 2019. During the period 2017 to 2019 gold production increased from 149,037 to 214,036 ounces. Silver recovery is not monitored but is a relatively minor contributor to overall Project economics. Process plant cash operating costs decreased from US$29.51/t ore processed in 2017 to US$24.42/t in 2019.
Testwork on Carla ore
GCG is planning to mine and process ore from the Carla vein and has conducted metallurgical testwork at SGS Canada on a single test composite that was formulated from selected drill holes and intervals from the Carla vein. The metallurgical program included rougher flotation followed by cyanidation of the reground rougher concentrate using process conditions currently practiced at GCG’s Maria Dama process plant. In addition, whole-ore cyanidation and Bond ball mill work index tests were conducted. The results of this testwork demonstrated that the gold contained in ore from the Carla vein is highly recoverable using the process conditions currently in use at the Maria Dama process plant. Gold and silver recoveries were reported at about 95% and 77%, respectively. SRK has reduced the reported laboratory recoveries by 2% in order to account for inherent plant inefficiencies. As such, overall gold and silver recoveries from Carla ore are projected at 93% and 75%, respectively.
Tailings management
The El Chocho tailings storage facility has been designed as a dry stack TSF. The tailings production rate is currently around 1,500 t/d and may ultimately be increased to 1,600 t/d with a total estimated volume of current tailings storage at 1.28 Mt and future storage of 2.3 Mt to meet the life-of-mine requirements. The current operation features a filter plant with a single plate and frame filter press and three dehydration cells capable of treating the full tailings load of 1,500 t/d of dry solids. There is an emergency pond adjacent to the filter plant for temporary slurry tailings storage when the filter press is down for maintenance. A second filter press is planned for construction in 2021 with the goal of eliminating down time for maintenance and reaching a filtering rate of 1,600 t/d.
The current storage facility consists of existing Phases 1B and 1A and new Phase 1C, which finished construction in February 2020. There is a future Phase 2A planned for construction downstream of Phase 1C. Phase 1B was the first tailings storage facility built and was designed to accept slurry tailings. Phase 1A was designed as interim containment measure while Phase 1C was being constructed. Phase 1C and future Phase 2A were designed by Wood. Filtered tailings are transported from the filter press by haul trucks and spread with a track dozer and compacted with vibratory smooth drum compactor to a specified lift thickness and minimum relative density. The outer 40 m of each tailings lift is compacted to a higher relative density to improve mass and erosional stability of the placed tailings.
Flotation tailings from the Maria Dama process plant are pumped directly to the TSF for filtration and dry stacking. A smaller secondary stream of cyanide tailings is first detoxified using H2O2 and FeSO4, then pumped to one of several settling/holding ponds for temporary storage. The detoxified and dewatered tailings from the four settling ponds will eventually be treated through a polymetallic plant (cleaning plant) to remove lead and zinc before being transferred to the El Chocho TSF. The cleaning plant is currently under construction and should be operational by the end of 2020.
Key reported parameters
| Parameter | Value | Units | Basis |
|---|---|---|---|
| Plant capacity | 1,500 | t/d | Design |
| Plant throughput (2019) | 451,450 | t | Actual |
| Overall gold recovery (2017-2019) | 93.8 – 95.9 | % | Actual |
| Gold recovery – Carla ore (testwork) | 95 | % | Testwork (reported lab) |
| Gold recovery – Carla ore (projected) | 93 | % | Testwork (reduced for plant inefficiencies) |
| Silver recovery – Carla ore (testwork) | 77 | % | Testwork (reported lab) |
| Silver recovery – Carla ore (projected) | 75 | % | Testwork (reduced for plant inefficiencies) |
| Gold recovery assumed for Mineral Resources | 90.5 | % | Assumption based on plant performance |
| Plant feed gold grade (2017) | 16.85 | g/t | Actual |
| Plant feed gold grade (2019) | 15.48 | g/t | Actual |
| Gold production (2017) | 149,037 | oz | Actual |
| Gold production (2019) | 214,036 | oz | Actual |
| Process plant cash cost (2017) | 29.51 | US$/t | Actual |
| Process plant cash cost (2019) | 24.42 | US$/t | Actual |
| Tailings production rate | 1,500 | t/d | Design |
| Future tailings rate (planned) | 1,600 | t/d | Design |
| Current tailings storage volume | 1.28 | Mt | Actual |
| Future tailings storage volume | 2.3 | Mt | Design |
Project website: https://www.scribd.com/document/721346409/GCM-Segovia-PFS-Update-NI43-101-Dated-20220506-Final
Technical qualifications
The report was prepared as a prefeasibility-level study. SRK reviewed all geotechnical data acquired by Geomecanica del Peru Consulting and determined that data from the field geotechnical investigation is appropriate for supporting a PFS based on field observations and the work conducted by GCG. The data collection process is adequate and consistent with international standards for a PFS. More data will need to be incorporated into the PFS geotechnical model to move forward to a feasibility study.
SRK has not updated the Mineral Resource models for the Carla and Las Verticales areas as no new information is currently available and therefore the last estimate remains valid.
A requirement for long-term post-closure water treatment would add significant cost to closure estimates. Detailed geochemical characterization is needed to more accurately understand the potential for mining wastes to generate poor quality contact water that might persist into closure and post closure.
The Mineral Reserve estimates are based on a mine design, mine plan, and economic model. The cut-off grade calculation assumes a $1,350/oz Au price, 90.5% metallurgical recovery, $6/oz smelting and refining charges, $25/t G&A, $26/t processing cost, and mining costs ranging from $76 to $115/t. Costs and prices used for cut-off grade calculation may be somewhat different than those in the final economic model due to the need to make assumptions early on for mine planning prior to finalizing other items and using long term forecasts for the life of mine plan.
Source: NI 43-101 Technical Report – Segovia Prefeasibility Study, SRK Consulting (U.S.), Inc., March 2020, Sections 1.4, 1.5, 1.6, 1.8, 1.9, 1.10, 1.11, 2, 16.
Segovia 2021 PFS Update NI 43-101 Technical Report
This technical report details the processing methods, plant expansion plans, and historical operating performance for the Maria Dama process plant at the Segovia project.
Report context
This NI 43-101 Technical Report, dated May 2022, provides an update to the 2021 Pre-Feasibility Study for the Segovia project, which is operated by Gran Colombia Gold (GCM). The report describes the existing 1,500 t/d Maria Dama process plant and a planned expansion to 2,000 tpd capacity by July 2022.
Processing route
Crushing Circuit
Run-of-mine ore from GCM’s mining operations is crushed to -15 mm in a two-stage crushing circuit. The circuit includes a 20 inch x 36-inch primary jaw crusher that discharges to a RoM ore bin. Primary crushed ore is screened at 15 mm on a 1.9 m x 4.7 m double-deck screen (1 ½ inch top deck and ¾ inch bottom deck). Screen oversize is conveyed to a 4 ft secondary cone crusher (CH-440 Sandvik) operated in closed circuit with a secondary vibrating screen (1.8 m x 6 m). The final 15 mm crushed product is sampled with a primary cross-cut sampler and a secondary rotary sampler as it is conveyed to the fine ore bin. Two Sandvik CH-430 cone crushers serve as backup when the CH-440 crusher is down for maintenance.
Ore delivered by mining contractors is already crushed before arrival and is dumped into a receiving bin. Contractor ore is sampled with both a primary cross-cut sampler and a secondary rotary sampler as it is conveyed from the receiving bin to a separate fine ore bin, with samples assayed by an outside commercial laboratory (SGS). GCM ore samples are assayed by the on-site analytical laboratory.
Grinding Circuit
GCM’s and the contractor’s ore are conveyed to a single conveyor belt feeding the grinding circuit. The circuit consists of a 12.5 ft x 23 ft ball mill operated in a closed circuit with a cluster of Cavex 250 cyclones to produce a final grind of 80% passing 150 µm in the cyclone overflow, which advances to the flotation circuit. A portion of the cyclone underflow is diverted to the gravity concentration circuit, which consists of a single QS-40 Knelson centrifugal concentrator operated in closed circuit with the grinding circuit. Approximately 30% of the contained gold is recovered into a primary gravity concentrate, which is further upgraded in the refinery on a Gemini table. Feed to the grinding circuit is continuously weighed on a belt-scale and hand-sampled every hour.
Flotation and Regrind Circuit
Cyclone overflow from the grinding circuit advances to the flotation circuit where it is first conditioned with flotation reagents. Conditioned slurry is then subjected to one stage of rougher flotation in a 40 m³ tank cell manufactured by Prominer, three stages of scavenger flotation in a bank of three 30 m³ WEMCO flotation cells, and finally one cleaner cell. Rougher/scavenger flotation concentrate is upgraded in one stage of cleaner flotation and combined with the rougher flotation concentrate. The combined rougher/scavenger cleaner concentrate, representing about 7 wt% of the plant feed, is thickened to about 55% solids (w/w) and reground in a 4 ft x 8 ft ball mill to approximately 80% passing 45 µm prior to the cyanidation circuit. The regrind ball mill is operated in closed circuit with 6-inch Krebs cyclones.
Cyanidation and Counter-Current-Decantation Circuit
The reground flotation concentrate is thickened and then processed through a conventional cyanidation circuit consisting of four agitated leach tanks operated in series to provide a total leach retention time of about 96 hours. The cyanide concentration is adjusted to 450 ppm NaCN in the first leach tank and is allowed to naturally attenuate to about 200 ppm NaCN in the last leach tank. The pH of the leach slurry is maintained at about 10.5 to 11 with lime.
Discharge from the fourth agitated leach tank flows to the CCD circuit, which consists of two 24 ft diameter thickeners and one 42 ft diameter thickener and serves to wash the pregnant leach solution (PLS) from the leach residue. The PLS from the first thickener overflow advances to the Merrill Crowe gold recovery circuit, and the thickener underflow from the third thickener is discharged to the TSF.
Merrill-Crowe and Refining
The PLS is processed in the Merrill Crowe circuit to recover solubilized gold and silver values from solution. This is accomplished by clarifying the PLS to remove any remaining suspended solids, de-aerating the solution to less than 1 ppm dissolved oxygen, and then precipitating the gold and silver values by the addition of zinc dust. The resulting gold and silver precipitate is recovered in three plate and frame pressure filters. The gold and silver precipitate is smelted using a flux composed of borax (40%), sodium nitrate (30%), soda ash (15%), and silica (3%). Approximately 650 kg of flux is blended with 600 kg of precipitate and smelted in a gas-fired furnace to produce a final doré product.
The gravity concentrate produced from the Gemini table located in the refinery is directly smelted using a flux formula in which flux is added in the ratio of two parts flux to one-part gravity concentrate. The flux composition includes borax (40%), sodium nitrate (30 to 33%), soda ash (7.5%), and silica (6%).
Tailings
Final leached tailings from the CCD circuit are detoxified with hydrogen peroxide and then pumped to lined dewatering cells identified as Bascula, Bolivia-1, Bolivia-2 and Bolivia-3. Effluent from the dewatering cells is then recycled back to the process plant. Flotation tailings are pumped to the El Chocho TSF where they are thickened and filtered to about 15% moisture prior to dry stack placement at the TSF. Thickener overflow and filtrate solutions are recycled back from the TSF to the process plant.
Proposed Plant Expansion
GCM is expanding the capacity of the Maria Dama process plant and expects to be able to process ore at the rate of 2,000 tpd by July 2022. The plant expansion includes the following components:
- Expansion of the ore stockpile area and upgrades to the crushing circuit designed to increase crushing capacity from 70 to 150 t/h.
- Installation of a new 40 m³ tank flotation cell to the rougher flotation circuit.
- Installation of a new Merrill-Crowe circuit for recovery of gold from the leach solution using conventional zinc precipitation technology.
- Replacement of the old thickeners in the CCD circuit with new thickeners.
- Upgrading the process water distribution system.
- Installation of a second tailings pressure filter at the El Chocho dry stack TSF.
The plant expansion is budgeted at a cost of US$9.57 million, allocated as follows: second tailings pressure filter (US$4.16 million), ore stockpile and crusher upgrade (US$3.96 million), new Merrill-Crowe circuit (US$0.24 million), process water distribution (US$0.14 million), new thickeners (US$0.76 million), and new rougher flotation tank cell (US$0.31 million).
Key reported parameters
| Parameter | Design / Proposed | Historical Actual | Basis |
|---|---|---|---|
| Plant capacity | 2,000 tpd (proposed) | 1,500 t/d (existing); 1,524 t/d average in 2021 | Proposed expansion target; 2021 operating data |
| Crushing capacity | 150 t/h (proposed) | 70 t/h (existing) | Design upgrade target |
| Final grind size | Not specified | 80% passing 150 µm | Operating data |
| Regrind size | Not specified | 80% passing 45 µm | Operating data |
| Flotation concentrate mass pull | Not specified | ~7 wt% of plant feed | Operating data |
| Leach retention time | Not specified | ~96 hours | Operating data |
| Cyanide concentration | Not specified | 450 ppm NaCN (first tank); ~200 ppm (last tank) | Operating data |
| Leach pH | Not specified | 10.5 to 11 | Operating data |
| Gold recovery | Not specified | 94.7% to 95.6% (2019-2021) | Actual production data |
| Gold production | Not specified | 206,693 oz (2021) | Actual production data |
| Plant operating cost | Not specified | US$25.30/t; US$68.09/Au oz (2021) | Actual cost data |
| Plant expansion budget | US$9.57 million | Not applicable | Design estimate |
Technical qualifications
This report is based on the original technical report titled "Segovia 2021 PFS Update NI 43-101 Technical Report" dated May 2022. The processing methods described show the existing Maria Dama process plant and proposed expansion as designed by GCM. Historical production data covers the period from 2002 to 2021, with detailed operating data from 2019 to 2021. The report notes that although silver occurs in the ore, silver recovery is not monitored. Reagent consumption data and operating costs are provided from actual plant operations for 2018 through 2021. The flowsheet figures and general arrangement drawings referenced in the original report (Figures 17-1 and 17-2) are not reproduced here. Equipment specifications are based on the major equipment list provided by GCM in 2022.
Source: Segovia 2021 PFS Update NI 43-101 Technical Report, May 2022, Section 17 Recovery Methods
