Process Description REV-D00

PROCESS DESCRIPTION

NICICOH.AB.GM.A29JAN

11FEB2012300

Purpose of Issue

ClientApp.Chk.Pre.

DateRev.Contractor

Nipec

National Iranian Copper Industries Company

KavoshgaranHezar Sanat

Chehel-Koureh Copper Concentration Plant Project

Page 1 of 1621

Client Number:61C12-N-P17-00-000000-0021-0304Date:24 APRIL17 SEP 201211Feb2013

Nipec Number:Rev: 03004

Stamps:

This document and the information disclosed are the property of NIPEC and are not to be used to furnish any information for making of documents or apparatus except where approved by written agreement.

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Document Title: PROCESS DESCRIPTION

Page 2 of 24Client Number: 61C12-N-P17-00-000000-001-0304002

Date: 24 APRIL201217 SEP 201211Feb2013

Nipec Number:Rev:03004

Revision Record

Page Rev.00 Rev.01 Rev.02 Rev.03 Rev.04 Page Rev.00 Rev.01 Rev.02 Rev.03 Rev.04

XXXXXXXXXXXXXXXXXXXXX

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Table of content:

1. 1- Foreword...................................................................................................................4

2- Beneficiation Process ...................................................................................................4

2-1- Various Sections.................................................................................................4

3- Process Description.......................................................................................................5

3-1-Raw ore material handling...................................................................................5

3-2-Crushing plant......................................................................................................5

3-3-Grinding...............................................................................................................7

3-4-Flotation and regrinding.......................................................................................8

3-5-Concentrate dewatering.................................................................................1217

3-6-Reagent system..............................................................................................1319

3-7-Plant utilities..................................................................................................1420

3-7-1-Water...................................................................................................1420

3-7-2- Air.......................................................................................................1521

1- Foreword

In beneficiation plant, run of mine of 300,000 t/y with 1.08% sulfide copper are charged

to plant as feed and copper concentrate of 15840 t/y with 18.55% sulfide copper is

gained as product. PLANT working days per year is 300 days , 7200 hours per year.

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2- Beneficiation Process

2-1- Various Sections

This process consists of following stages:

1- Crushing Area

2- Crushed ore storage

3- Grinding Area

4- Concentration Plant (Flotation)

5- Regrinding

6- Concentrate dewatering

3- Process Description

3-1-Raw ore material handling

Copper concentration plant shall be installed in the vicinity of Chehel Kureh underground

copper mine. The Run Of Mine ore is transferred to jaw crusher by wobblervibrating

feeder VFWF-01 and will be crushed by jaw crusher (JC-01) in the underground tunnel.

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First stage crusher, which is a double toggle jaw crusher, crushed the ore to a size of

70mm (d80) and transferred to first open stockpile by conveying system.

3-2-Crushing plant

First open stockpile will store plant feed for 7 days. Crushing plant will be working for

300 days per year and 2 shifts per day. The operating capacity of crushing plant is 71.43

t/h.

Maximum particle size of jaw crusher product is 90 mm with size distribution of

d80=70mm. The ore is loaded from open stockpile by loaders and then charged to a bin

(22-BI-01) at the top of the primary vibrating feeder (22-VF-01). There is a grizzly

(opening: 100mm) at the top of this bin and underneath is a vibratory feeder that feeds the

ore with adjustable tonnage to CRUSHING PLANT. The jaw crusher productcrusher

plant feed is transferred via belt conveyors (22-CV-01/02) to a three-deck vibrating

screen (22-VS-01), the apertures of which are 40mm ,25mm, and 8mm.The upper deck is

used to lower the force of the impact of the material hitting the screen.

Screen's under size , -8mm as crushing plant product, is transferred to crushed ore

Stockpile via a belt conveyor (22-CV-05), which has a live capacity of 3 days required

feed for flotation plant.

Vibrating Screen oversize, +25mm, is transferred to standard cone crusher (22-CC-01)

via a belt conveyor (22-CV-03). Product of standard cone crusher with a size of

d80=20mm transferred to conveyor (22-CV-01) by gravity. The circulating load of 2nd

stage of crushing is 20%.

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Vibrating screen middle size, +8-25mm, is transferred to short head cone crushers feed

bin (22-BI-02) via a belt conveyor (22-CV-04). Material middle size is fed to short head

cone crushers (22-CC-02/03) from bin by gravity. Product of short head cone crusher

with a size of d80=8mm transferred to conveyor (22-CV-01) by gravity. The circulating

load of 3rd stage of crushing is 20%.

Required capacity of 2nd and 3rd stage cone crushers are 60 and 62.55 t/h respectively. The

product of all crushers is transferred to three- deck vibrating screen via belt conveyors

(22-CV-01/02).

To protect downstream equipment from metal scrap, belt conveyors 22-CV-01&03&04

are equipped with fixed magnets 22-MG-01~ 3 respectively. Also, one metal detector is

used for non-magnetic metallic scrap. If metal detector detects a piece of metal, belt

conveyor 22-CV-02 will be stopped automatically and operator should be take it .

To protect downstream equipment from metal scrap, belt conveyors 22-CV-01~04 are

equipped with fixed magnets 22-MG-01~ 4 respectively. Also, one metal detector is used

for non-magnetic metallic scrap. If metal detector detects a piece of metal, chute 22-CH-

01 will be bypassed to ground and after 10s will be returned to normal position.

For feed rating control of crushing plant, vibrating feeder is equipped with a variable

speed control drive and is controlled with a belt scale installed under the conveyor belt

22-CV-01.

There is a water spray de-dusting system to remove the dust in the crushing plant. In order to prevent forming lots of dust in crushing area of the Chehel Koureh Concentrator Plant, The most effective solution is utilizing spray water system in some transferring points as well as the loading point.

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For this purpose the following points will be equipped with water spray:

Discharge point of primary feeder 22-VF-01 Transferring point from belt conveyor 22-CV-02 to vibrating screen Transferring points from vibrating feeders under stockpile into the skirt board of

the belt conveyor 32-CV-01

By spraying at these four points the proper and uniform moisture can be controlled to minimize the required moisture content in order to dust reduction and having perfect material flow in the hopper, chutes and feeders.

3-3-Grinding

Feed ore is transported to the primary ball mill (32-BM-01) via belt conveyor 32-CV-01.

Belt conveyor 32-CV-01 will be equipped with a belt scale 32-BS-01 to control the feed

ore materials discharged from the vibrating feeders (32-VF-01/02, one operating and the

other standby).

First stage grinding mill, ; which shall is a wet grinding ball mill in a closed circuit with

hydro cyclone clusters, grinds the feed to a range of -10mm to 53 microns (d80). A valve

on the inlet pipe can shut off each cyclone in cluster. There are a few cyclones in cluster

as standby.

The ore enters the ball mill through a chute. Water is added to the chute to obtain 65%

solid in the mill. Grinding media in the ball mill is steel balls. Balls, milk of lime and

other reagents are fed to ball mill via ball mill feed chute. Maximum ball size is 80mm.

Maximum ball mill volumetric load is 40%.

Basic data of primary ball mill is as follows:

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Ball mill type Over flow discharge

Motor (Kw) 10431200

Diameter(approx.) 3.7 8 m

Length(approx.) 4.645m

Speed % of critical 8075

Circulating load 250%

Bond work index 14.72 kwh/st

Discharge Solid% 65

Slurry overflow is discharged from the ball mill via the mill trommel and will be

transferred to cyclone pump box (32-PB-01) and then is pumped to cyclone by one of

cyclone pumps (32-PU-01/02). The pressure drop over the cyclones should be 1 barg.

The hydro cyclone underflow, is circulated to the ball mill through ball mill feed chute.

The hydro cyclone overflow leaves the grinding circuit for the conditioning tank (33-CT-

01) by gravity.

Reclaimed water is added to dilute the ball mill feed and discharge.

3-4-Flotation and Regrinding

Flotation system is designed to separate the copper mineral particles from the gangue

minerals. The final concentrate contains about 18.55% copper sulfide and a Cu sulfide

recovery of 90%.

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The cyclone overflow of ball mill cyclones are is fed to the conditioner tank. Rougher

flotation cells ( 33-RF-01/10) consist of 10 mechanical cells, each with a volume of 4.7

m3.

The pH in the rougher cells is controlled by addition of lime milk in the grinding circuit

and conditioner tank to reach around 9.50 in the circuit. The rougher concentrate with a

grade of 10.74% is transferred to the regrinding circuit by gravity. Also the tailing of

rougher cells with a grade of 0.3% copper is transported to rougher scavenger cells by

gravity.

The rougher scavenger flotation cells (33-RS-01/09) consist of 9 mechanical cells, each

with a volume of 4.7m3. The rougher scavenger concentrate with a grade of 3.62% is

transferred to the regrinding mill circuit. The tailing of rougher scavenger cells with a

grade of 0.2% copper is transported to tailing thickener via centrifugal pumps (33-PU-

0301/0402). Oxide copper minerals are recovered in the rougher/scavenger stage by

addition of PAX and NaHS reagents.

To liberate the Copper and Zinc minerals from the locked particle, the two concentrates

of rougher and rougher scavenger stages will be transferred to the regrinding area. These

concentrates in addition to the reclaim water will be mixed in the regrinding mill pump

box (33-PB-0302) and pumped to regrind hydro cyclone cluster (33-HC-01) via slurry

pumps (33-PU-0503/0604). Regrinding mill feed size is 53 microns (d80) and regrind

product size is 20 microns (d80).

The overflow of cyclones is fed to the cleaning flotation cells and the underflow materials

will be reground in ball mill (33-BM-01). The ground slurry is recycled to the hydro

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cyclones through slurry pumps (33-PU-03/04). Most of Fflotation reagents are added to

the slurry in the regrinding mill cyclone underflow.

Hydro cyclone cluster is rather flexible to the extent that the number of operating

cyclones can easily be varied. The performance of the hydro-cyclone is related to a

number of operational variables.depends on many variables. Easiest parameter in

controlling shift-to–shift operation are is the dilution of the slurry feed to cyclone and the

pressure differences over the cyclones.

Basic data of regrinding ball mill is as follows:

Ball mill type Over flow discharge

Motor (Kw) 115160

Diameter(approx.) 12.1.8 m

Length(approx.) 3.3m

Speed % of critical 75

Circulating load 280%

Bond work index 14.72 kwh/st

Discharge Solid% 50

The reground rougher and rougher scavenger concentrate is cleaned in two steps. The

cleaning stage consists of four mechanical cells, each with a volume of 2.7m3.

Concentrate of cleaner cells with a grade of 20% as total copper and max. 14.25% Zinc as

final concentrate is transferred to concentrate thickener by gravity. Also the tailing of

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cleaner cells is transferred to two mechanical cleaner/ scavenger cells, each with a

volume of 2.7m3, by gravity.

The concentrate of cleaner/scavenger cells with a grade of 6.13% copper is transferred to

regrinding mill pump box (33-PB-02) by gravity and recycled to cleaner cells with

rougher and rougher/scavenger concentrate via regrinding cyclone over flow. The tailing

of cleaner/scavenger cells with a grade of 0.25% copper is transferred to rougher

scavenger tail pump box (33-PB-01) by gravity and then transferred to tailing thickener

with rougher scavenger tail via slurry pumps (33-PU-01/02).

Three types of reagents are added to the flotation system. These are as follows:

- Collectors

These reagents produce a hydrophobic layer on the mineral surface, which enables the

mineral to be captured and attached to an air bubble. The collectors utilized in the

flotation area are AP3894 and PAX. Characterizations of these reagents are as follow:

AP3894Name AERO 3894 PromoterChemical Family ThionocarbamateSynonyms NoneMolecular Formula MixtureMolecular WGT MixtureAppearance Pale yellow to reddish mobile liquidOdor PungentMelting Point Not applicableVapor Pressure Not applicableSpecific Gravity 1.004Vapor Density >1; (air=1)%Volatile(By WT) 100pH Not applicable

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Saturation in air(%By Vol) Not applicableEvaporation rate Not applicableFlash point 120F; 49°CDecomposition temp 392 F; 200°CSolubility in water NegligibleStability StablePolymerization Will not occurIncompatible material Strong oxidizing agentsFlammable properties Flammable LiquidFlammable limits(% By Vol) Not available

Potassium Amyl Xantate (PAX)Chemical Name Potassium Amyl Xantate Chemical Family Xanthates; Carbonodithioic acid saltSynonyms Potassium amyl xanthate; PAX; Carbonodithioic acid, 0-

pentyl ester, potassium salt; Potassium pentyl xanthate, Pot. Amyl Xanthogenate; Pot. O-Amyl Dithiocarbamate

Appearance Grey/yellow hygroscopic pelletsFormula C6H11KOS2Odor Unpleasant sulphurous odourMelting Point 255-288 °CSolubility in water Soluble completelySpecific Gravity 0.94(warwe=1)Flash Point Closed Cup 12-13 °CpH Not applicable

Chemical StabilityProduct is stable if stored and handled under recommended conditions. Hazardous polymerization will not occur.

Vapor pressure (mm Hg) Not applicableProportion(%) >90Flammability Flammable

Conditions to avoid

Strong oxidizers can cause fire or explosions. Acids will accelerate the hydrolysis of xanthates. Incompatible with cooper, brass, bronze. Avoid high temperatures and moisture

Hazardous decomposition products carbon disulfide, trithiocarbonate, amyl alcohol

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Handling

Avoid contact with eyes. Use only in well ventilated area. Wash thoroughly after handling. Avoid prolonged or repeated skin contact. Ground containers when transferring material from one to another. Use caution opening containers with xanthates of unknown age for any CS2 vapor accumulation.

Storage

Keep containers tightly closed in a dry, cool and well-ventilated place. Keep away from heat and sources of ignition. Store containers out of direct sunlight at moderate temperatures. Properly ground storage containers.

- Frothers

These reagents modify the surface tension of the liquid. This affects the bubble size and

helps to form a stable froth on the slurry surface, which is capable of carrying the mineral

particles until they are removed from the cell. The utilized frother in the flotation area is

MIBC. Characterizations of this reagent are as follow:

Methyl Isobutyl CarbinolMaterial Formal Name 4-methylpentan-2-ol

Synonyms1,3-dimethyl 1-butanolMIBCMethyl Amyl Alcohol

Appearance Clear. Liquid.Odor Sweet.Boiling point 130 - 133 °C / 266 - 271 °FFlash point 41 °C / 106 °F (IP 170)Explosion / Flammability limits in air 1 - 5.5 %(V)Auto-ignition temperature 305 °C / 581 °F (ASTM E-659)Vapor pressure 420 Pa at 20 °C / 68 °FSpecific gravity 0.81-0.9 at 20 °C / 68 °FDensity 806 - 808 kg/m3 at 20 °C / 68 °F (ASTM D-4052)Water solubility 16 g/l at 20 °C / 68 °FVapor density (air=1) 3.5Volatile organic carbon content 70.6 % (EC/1999/13)

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Evaporation rate (nBuAc=1) 0.3 (ASTM D 3539, nBuAc=1)

Stability Stable under normal conditions of use. Reacts with strong oxidising agents. Reacts with strong acids.

Conditions to AvoidAvoid heat, sparks, open flames and other ignition sources.

Materials to Avoid Strong oxidising agents. Strong acids.

- Modifiers

a. pHPh modifiers, which are used to control the alkalinity/acidity of the slurry final

concentrate before thickening to give the optimum collector actionsedimentation of

particles. pH will be adjusted with by lime that. I t should be 9.5011up to 10-11 in the

rougher stage while in other stagesthickener concentrate thickener feed. Lime isn’t added

to the flotation circuit. it will operate at normal condition without lime addition.

Characterizations of this reagent are is as follow:

LimeAppearance White or grayish-white lumps or powderOdor ODOURLESSChemical Name Calcium OxideChemical Formula CaOConc.(%) 65-90Physical State SolidBoiling Point (°C/°F) N.A.Melting Point (°C/°F) 1345 / 2453Specific Gravity (Apparent) g/cc:1.6-2.8Vapor Pressure (mm Hg) N.A.Vapor Density N.A.Evaporation Rate N.A.

Solubility in WaterReacts with water to produce Ca(OH)2 and large amounts of heat.

pH (25°C/77°F) 12.4Flammability NON FLAMMABLE

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b. Resurfacing agents, which are commonly used to depress or reactive particular

minerals in selective flotation. The zinc lead depressant that is used in this system is

SMBS ( sSodium mMeta be bisulfide) and reactive agent that is utilized for oxide copper

is NaHS. Characterizations of these reagents are as follow:

Sodium Metabisulfite(SMBS)

Trade Names Sodium Metabisulfite, Anhydrous Sodium Bisulfite, ABS, Disodium Pyrosulfite, Sodium Pyrosulfite, SMBS

Chemical Formula (Na2S2O5)Appearance White to yellowish, fine crystalline powderODOUR PungentBoiling point Decomposes above 302°F (150°C)Melting Point °C About 150 (Decomposition) °C Molecular weight 190.11Content ( As Na2S2O5) % MIN 97Vapor density (Air = 1) Not applicableSolubility in water 100% by weightSolubility (g/100gH2O@20°C) 65Concentration(%M) (5% aqueous soluti on)he actual concentration of SMBS contained in the storage solution

0-1%

Specific gravity 1.48Melting point >302°FEvaporation rate Not applicable

Water reactiveYes, increases the natural rate of yield of sulfur dioxide gas.

pH 4.3-4.5 (1% solution)

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Flash point Not applicable – non-combustible solidFlammability limits in air % by volume Not applicableStability Stable under normal conditions of use.Condition avoid Heating can release hazardous gases.Material to avoid Oxidising agents. Acids.Hazardous decom. Products Thermal decomposition may release oxides of sulphur (SOx).

Usage Precautions

Product should be used in accordance with good industrial principles for handling and storing of hazardous chemicals. Minimize creation of air-borne dust by application of good occupational hygiene principles, appropriate control measures and extraction techniques.

Storage PrecautionsStore in closed original container at temperatures between 15°C and 25°C. Store away from direct sunlight and moisture Store separated from: Acids.

Sodium Hydrosulfide SolutionChemical Family Inorganic salt solution

Synonyms KI-300, sodium hydrogen sulfide, sodium sulfhydrate’ sodium bisulfide, sodium mercaptan

Formula NaHSChemical Ingredients (% by wt.)Sodium hydrosulfide 20-45%Sodium sulfide <1.0% (Typical)Sodium Carbonate <3.0% (Typical)Water 55-80%Appearance May be yellow to red, to dark green to black liquid.

Odour Strong hydrogen sulfide (rotten egg) odor, hydrocarbon (mercaptan) odor.

Boiling point 253 °F(122.8 °C) - 269 °F (131.7 °C)Vapor pressure 17 mm Hg @ 68 °F (20 °C)Vapor density 1.17 (Air = 1.0)Solubility in water CompleteSpecific Gravity 1.152 - 1.303 (9.6 - 10.9 lbs/gal)

Freezing point0° F (-17.8° C) - 20%56º F (13.3º C) - 45%

pH 11.5 - 12.5

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Volatile Not applicableStability This is a stable materialFlammable properties Flash point: Not flammable

Handling

Wear proper protective equipment . Avoid breathing product vapors. Avoid contact with skin and eyes. Use only in a well ventilated area. Dilute product only in enclosed containers. Wash thoroughly after handling.

Storage

Store in well ventilated areas. Do not store combustibles in the area of storage vessels. Keep away from any sources of heat or flame. Store tote and smaller containers out of direct sunlight at moderate temperatures [<80º F (27º C)].

C. c. Dispersant

Sodium silicate is used as dispersant and depressant of silicates minerals in the flotation

area. Characterizations of this reagent are as follow:

SODIUM SILICATE LIQUIDAppearance VISCOUS CLEAR TO LIGHT YELLOW LIQUIDPhysical State Liquid and corrosive Odour ODOURLESSpH 12.8 (1% Solution) (Approximately)VapourVapor Pressure 24 mm Hg @ 20°CVapourVapor Density NOT AVAILABLEBoiling Point 100°C (Approximately)Melting Point < 0°CEvaporation Rate AS FOR WATERSolubility (Water) SOLUBLESpecific Gravity 1.3 - 1.56% Volatiles > 60 % (Water)Flammability NON FLAMMABLEFlash Point NOT RELEVANTUpper Explosion Limit NOT RELEVANTLower Explosion Limit NOT RELEVANT

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COMPOSITIONWATER(H2O) Content: >60%SODIUM SILICATE(Na4SiO4) Content: 20-40%

3-5-Concentrate Dewatering

a. Thickener (34-TH-01)

Dewatering process consists of two stages, Cu concentrate thickening and filtering.

The purpose of the copper concentrate thickening is to increase the density of the copper

concentrate slurry before filtering process.

The copper concentrate is transferred to concentrate thickener feed well. The copper

concentrate solids are settled to the bottom of the thickener, while water flows via the

over-flow launder to the process water reservoir. Flocculants are added to concentrate

thickener to increase the particle settling rate. Under-flow product will be pumped to the

distribution box 34-DB-01 by variable speed slurry pumps (34-PU-01/02).in normally

condition , thickener under flow product should be transferred to pressure filter buffer

tank. There are two discharging pipes at the bottom of thickener to prevent any stoppage

in case of blockage of the operating pipe.

b. Pressure filter

The purpose of the filtering is to increase the density of the copper concentrate to 90%

solid. Feed to the pressure filter buffer tank is regulated by the density of the concentrate

thickener underflow. When the density is within the set point range the filter buffer tank

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valve is opened and when the density is outside the set point range or the level of buffer

tank is greater than the High alarm set point , the thickener re-circulation valve in the 34-

DB-01 is opened. Buffer filter tank is equipped with a mixer. There are two pressure

filters (34-PF-01/02) in dewatering area, one filter is operating and the other is standby.

Concentrate slurry is transferred to pressure filter via slurry pumps (34-PU-03/04).

Filtrate is transferred to process water reservoir and Final final concentrate is discharged

to concentrate storage by gravity.

3-6-Reagents System

The reagents are used in the process to achieve optimal result in the flotation area. The

reagents for flotation area are prepared in preparation tanks ( except MIBC and Sodium

silicate and AP3894 that are in form of liquid) and then transferred to daily tanks by

gravity. To prepare and reserve of lime, used a tank. Reagent materials from daily tanks

are pumped to the consumption points by metering pumps except lime that will be

transfertransferred to cleaner concentrate launder by gravity from preparation tank. One

set of each reagent pump is considered to operate and another as standby. Five reagent

dosage systems should be considered to supply the reagents by dosing pumps ,

(centrifugal pump will be used for lime milk distribution), that are distribute the

reagents to the following consumption points:

a. Lime milk :primary ball mill cyclone under-flow , conditioning tank and

cleaner conc. launder

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b. MIBC and sodium silicate: primary ball mill cyclone under flow, conditioning

tank, 5th rougher cell, regrind mill cyclone under flow, first rougher/scavenger

cell

c. AP3894 and MIBC and sodium silicate: primary ball mill cyclone under flow,

conditioning tank, 5th rougher cell, regrind mill cyclone under flow, first

rougher/scavenger cell

d. SMBS: primary ball mill feedConditioner tank and first cleaner cell as dry by

vibrating feeder

e. PAX and NaHS: first rougher/scavenger cell, 1ST and 4th rougher scavenger

cellsconditioner tank, fourth rougher/scavenger cell and regrind mill cyclone

under flow

f. NaHS: conditioner tank, regrind mill cyclone under flow

3-7-Plant Utilities:

3-7-1-Water

The required fresh water for the plant is estimated to be about 43.11m3 /h overall.

The clarified water, which is returned from the tailing thickener and concentrate

thickener as over-flow, will be collected in the process water reservoir and used as

returned water in different points of the plant.

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Process water consumption in PLANT:

PW to ball mill feed chute 20.87 m3 /h

PW to ball mill discharge pump box 67.85 m3 /h

PW to conditioner tank 17.54 m3 /h

PW to rougher conc. launder 4.8 m3 /h

PW to rougher/scavenger conc. launder 1.7 m3 /h

PW to cleaner conc. launder 5 m3 /h

PW to cleaner/scavenger conc. launder 1 m3 /h

PW to lime milk preparation 0.189 m3 /h

PW for floor washing 3 m3 /h

TOTAL 121.95 m3 /h

Fresh water consumption in PLANT:

FW for reagents preparation 0.35 m3 /h

FW to pump sealing 1 m3 /h (approx.)

FW to miscellaneous 7.5 m3 /h

FW to process water reservoir 34.26 m3 /h

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TOTAL 8.8543.11 m3 /h

Return water in the PLANT:

RW from tailing thickener 60.77 m3 /h

RW from concentrate thickener 24.96 m3 /h

RW from pressure filter 1.96 m3 /h

TOTAL 87.69 m3 /h

The required fresh water for the plant is estimated to be about 43.11m3/h overall.

The clarified water, which is returned from the tailing thickener and concentrate thickener

as over-flow, will be collected in the process water reservoir and used as returned water

in different points of the plant.

Process water consumption in PLANT:

PW to ball mill feed chute 20.87 m3/h

PW to ball mill discharge pump box 67.85 m3/h

PW to conditioner tank 17.54 m3/h

PW to rougher conc. launder 4.8 m3/h

PW to rougher/scavenger conc. launder 1.7 m3/h

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PW to cleaner conc. launder 5 m3/h

PW to cleaner/scavenger conc. launder 1 m3/h

PW to lime milk preparation 0.189 m3/h

PW for floor washing 3 m3/h

TOTAL 121.95 m3/h

Fresh water consumption in PLANT:

FW for process 34.26 m3 /h

FW for reagents preparation 0.35 m3/h

FW to pump sealing 1 m3/h (approx.)

FW to miscellaneous 7.5 m3/h

TOTAL 8.8543.11 m3/h

Return water in the PLANT:

RW from tailing thickener 60.7760.77 m3/h

RW from concentrate thickener 24.96 m3/h

RW from pressure filter 1.96 m3/h

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TOTAL 87.6987.69 m3/h

3-7-2- Air

The required air for the process will be supplied from two blowers (41-BL-01/02) and

two compressors (41-CM-01/02).

Required air for all of flotation cells is supplied by two blowers, one blower is operating

and another one is as standby. The maximum required capacity of air for flotation cells is

1087m3/min with a maximum pressure 17kpa.

Two compressors, each with a pressure of 7.5 barg with a capacity of 80nm3/h, will be

installed to supply the required instrument and plant air. The produced compressed air

after getting through water trap and filter and being storing in the receiver tank with a

1000 liter capacity, will be dried in a dryer and filtered in final filter to achieve the

required quality. The air will then be distributed for instrument air consumers.

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Process Description REV-D00

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