Criterios de Diseño

Sociedad Min era Cerro Cerro Verde Verde S.A.A.

Prima rim ary Sulfide ulf ide Proj Proje ect Project No. PSP108

Process ro cess De Design si gn Criteri Cri teria a Docu Doc u m ent No. C-DCC-DC-25 25-0 -001 01 Rev. 1 27 January Januar y 2006 2006

F:\103\109 ENGDOC\109.3 CRIT_DC\PROCESS CRIT_DC\PROCESS\C-DC-25-001\C-DC-25 \C-DC-25-001\C-DC-25-001_PROCDESC -001_PROCDESCRIT_REV1.DOC RIT_REV1.DOC

Client Name: Project Name: Name: Proj ect Numb er:

Socied ad Minera Cerro Verde S.A.A. Primary Sulfide Project PSP108 PSP108

Docu ment C-DC-25-00 C-DC-25-001 1 Page 1 of 64 Rev. 1

FLUOR

Mining & Minerals

PROCESS DESIGN CRITERIA

This document has been revised as indicated below. Changes after revision 0 are identified by vertical bars at the right side of the page, with additions being underlined. Please replace all pages of this document and destroy the superceded copies. Rev No. C 0 1



Originator (name/initials) Ken Wood Ken Wood Ken Wood

Rev Date 24Nov04 11Feb05 27Jan06

Revision Revision Descripti Descripti on Issued for Approval Issued for Design Issued for Design



New Issue

APPROVAL S

Entire Document Re-issued

ORIGINAL SIGNED BY FLUOR

DATE

CLIENT

DATE

Brad Matthews

04Feb06

Jim Vanderbeek

04Feb06

Area Project Engineer:

Ken Wood

04Feb06

Lead Discipline Engineer:

Ken Wood

04Feb06

Project Manager: Engineering Manager:

Process Approval:

F:\103\109 ENGDOC\109.3 CRIT_DC\PROCESS CRIT_DC\PROCESS\C-DC-25-001\C-DC-25-0 \C-DC-25-001\C-DC-25-001_PROCDESC 01_PROCDESCRIT_REV1.DOC RIT_REV1.DOC

PROCESS

Client Name: Project Name: Name: Proj ect Numb er:

Socied ad Minera Cerro Verde S.A.A. Primary Sulfide Project PSP108 PSP108

Docu ment C-DC-25-00 C-DC-25-001 1 Page 1 of 64 Rev. 1

FLUOR

Mining & Minerals

PROCESS DESIGN CRITERIA

This document has been revised as indicated below. Changes after revision 0 are identified by vertical bars at the right side of the page, with additions being underlined. Please replace all pages of this document and destroy the superceded copies. Rev No. C 0 1



Originator (name/initials) Ken Wood Ken Wood Ken Wood

Rev Date 24Nov04 11Feb05 27Jan06

Revision Revision Descripti Descripti on Issued for Approval Issued for Design Issued for Design



New Issue

APPROVAL S

Entire Document Re-issued

ORIGINAL SIGNED BY FLUOR

DATE

CLIENT

DATE

Brad Matthews

04Feb06

Jim Vanderbeek

04Feb06

Area Project Engineer:

Ken Wood

04Feb06

Lead Discipline Engineer:

Ken Wood

04Feb06

Project Manager: Engineering Manager:

Process Approval:

F:\103\109 ENGDOC\109.3 CRIT_DC\PROCESS CRIT_DC\PROCESS\C-DC-25-001\C-DC-25-0 \C-DC-25-001\C-DC-25-001_PROCDESC 01_PROCDESCRIT_REV1.DOC RIT_REV1.DOC

PROCESS

Sociedad Minera Cerro Verde S.A.A. Primary Sulfide Project Project No. PSP108

Document C-DC-25-001_Rev 1

0.01 PROCESS DESIGN CRITERIA- INDEX Se c t i o n

WB S No .

0.01

3000

0.02

Des c r i p t i o n

Rev

By

Dat e

In d ex

1

PR

27-J an -06

3000

Un i t s an d A b b r ev i at i o n s

1

PR

27-J an -06

0.03

3000

So u r c e Co d es

1

PR

27-J an -06

0.04

3000

Pr o c es s Des i g n B as i s

1

PR

27-J an -06

0.05

3000

Si t e Co n d i t i o n s

1

PR

27-J an -06

0.06

3000

Gen er al

1

PR

27-J an -06

0.07

3000

Or e Var i ab i l i t y

1

PR

27-J an -06

0.08

3000

B l o c k Fl o w Di ag r am

1

PR

27-J an -06

1.01

3110

Pr i m ar y Cr u s h i n g

1

PR

27-J an -06

1.02

3120

Co ar s e Or e St o c k p i l e

1

PR

27-J an -06

1.03

3210

St o c k p i l e Rec l ai m Feed er s

1

PR

27-J an -06

2.01

3220

Sec o n d ar y Cr u s h i n g an d Sc r een i n g

1

PR

27-J an -06

2.02

3230

Ter t i ar y Cr u s h i n g an d Sc r een i n g

1

PR

27-J an -06

2.05

3300

B al l Mi l l i n g

1

PR

27-J an -06

2.06

3320

B al l Mal l B al l Han d l i n g Fac i l i t y

1

PR

27-J an -06

2.07

3330

B al l Mi l l Di s c h ar g e Pu m p /Su m p

1

PR

27-J an -06

2.08

3330

Pr i m ar y Mi l l i n g Cl as s i f i c at i o n

1

PR

27-J an -06

4.01

3410

Ro u g h er Fl o t at i o n

1

PR

27-J an -06

4.02

3410

Sc av en g er Fl o t at i o n

1

PR

27-J an -06

4.03

3420

Ro u g h er Co n c en t r at e Po l i s h i n g

1

PR

27-J an -06

4.04

3420

Sc av en g er Co n c en t r at e Reg r i n d

1

PR

27-J an -06

4.05

3420

Reg r i n d Ci r c u i t Cl as s i f i c at i o n

1

PR

27-J an -06

4.06

3440

Cl ean er Fl o t at i o n - Fi r s t Cl ean er Cel l s

1

PR

27-J an -06

4.07

3440

Cl ean er Fl o t at i o n - Cl ean er /Sc av en g er Cel l s

1

PR

27-J an -06

4.08

3430

Cl ean er Fl o t at i o n - Fi n al Co l u m n Cel l s

1

PR

27-J an -06

4.09

3510

Co p p er Mo l y Co n c en t r at e Th i c k en i n g

1

PR

27-J an -06

5.01

3520

Mo l y Ro u g h er -Sc av Fl o t at i o n

1

PR

27-J an -06

5.02

3520

Mo l y Cl ean er Fl o t at i o n

1

PR

27-J an -06

5.03

3530

Mo l y Th i c k en i n g /Dew at er i n g & Dr y i n g

1

PR

27-J an -06

5.04

3540

Reagents - Lime / NaHS / Nitrogen

1

PR

27-J an -06

5.05

3540

Reag en t s - Mo l y Pl an t

1

PR

27-J an -06

6.01

3610

Co p p er Co n c en t r at e Th i c k en i n g

1

PR

27-J an -06

6.02

3620

Co n c en t r at e Sl u r r y St o r ag e an d Dew at er i n g

1

PR

27-J an -06

6.03

3630

Co n c en t r at e Dr y St o r ag e an d L o ad i n g

1

PR

27-J an -06

7.01

3700

Tai l i n g Th i c k en i n g

1

PR

27-J an -06

8.01

3800

Tai l i n g Co l l ec t i o n an d Di s p o s al

1

AG

27-J an -06

8.02

4000

Tai l i n g Dam & Seep ag e Co l l ec t i o n

1

AG

27-J an -06

9.01

3910

Reag en t s - Co l l ec t o r

1

PR

27-J an -06

9.02

3910

Reag en t s - Fr o t h er / Mo l y Co l l ec t o r

1

PR

27-J an -06

9.03

3910

Reag en t s - Fl o c c u l an t s

1

PR

27-J an -06

9.04

3910

Reag en t s - L i m e

1

KW

27-J an -06

9.04 9.05

3900/5100

Pr o c es s / Fr es h Wat er Sy s t em s

1

AG

27-J an -06

9.06

3930/3960

Reag en t s - Wat er Tr eat m en t

1

KW

27-Jan-06

9.07

5100

Fr es h Wat er Tr eat m en t

1

KW

27-Jan-06

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Co m m en t s

|

| | | |

2 of 64

Sociedad Min era Cerro Verde S.A.A. Primary Sulfide Project Project No PSP108


Process Design Criteria Section:

0.02 Units and Abbreviations

Initial Revision

C-DC-25-901 HPGR Rev. D

Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Ab br evi ati on s:

Abbreviation °C o

' " . a A Bq C cd d D80 dB F F80 g/t Gy h H Hz J K kg kW L lm lx m M min µm mo mol MW N N/A O/F P80 Pa rad s

Meaning degree Celsius degree of arc minute of arc second of arc decimal separator thousands separator (space, not comma) year ampere 1 s-1 becquerel 1 Bq = coulomb 1C = 1 A.s candela day Size which 80% of the material passes a square mesh screen of the same opening decibels farad 1F = 1 C/V Feed size of which 80% passes a square mesh screen of the same opening grams per metric tonne, = parts per million (weight) gray 1 Gy = 1 J / kg hour henry 1H = 1 V.s/A (or Wb/A) 1 s-1 hertz 1 Hz = joule 1J kelvin kilogram kilowatt liter lumen 1 lm lux 1 lx meter 6 Prefix for 10 , or million

=

1 N.m

= =

1 cd.sr 1 lm/m2

Note 2: Note 2:

minute micron (micrometer) month mole Megawatt newton 1N = 1 kg.m/s2 not applicable Overflow Product size of which 80% passes a square mesh screen of the same opening pascal 1 Pa = 1 N/m2 radian second


3 of 64




0.02 Units and Abbreviations

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Ab br evi ati on s:

Abbreviation S sr Sv t T T80 TBA, TBD U/F V VSD W Wb  (Omega)

Meaning siemens 1S = 1 A/V steradian sievert 1 Sv = J / kg metric tonne 1 t = 1000 kg tesla 1T = 1 Wb/m2 Transfer product size of which 80% passes a square mesh screen of the same opening To be announced, to be determined Underflow volt 1V = 1 W/A Variable speed drive watt 1W = 1 J/s weber 1 Wb = 1 V.s 1 ohm = 1 V/A

N/A oz troy ounce 1 oz = 31.1035 g lb pound (avoirdupois) = 453.59 g Note 2: It is preferable that the words lumen and lux be spelled out.

(for use with metal prices only)

Definition o f design value terms:

Annual rate Operating days Availability Nominal capacity

Flowsheet balance

Design values

Flow rate per 365 calendar days Number of plant operating days per year is 365 days The time actually operated as a percentage of total available time For the grinding and flotation sections of the plant, availability is 93% The overall average capacity of the plant is 108,000 t/d. On an hourly basis the nominal flow includes the availability, for example: 108,000 t/d = 4,839 t/h 24 h/d x 93% availability This is the same mass rate as shown on the flowsheets/mass balance The values in the flowsheet balance represent the steady state average rate during the design utilization time (availability) per operating day for any facility or equipment as calculated above. Design values are the nominal hourly or average (flowsheet ) flows multiplied by the appropriate design factors for the specific process section or equipment. They include availability Design values are the instantaneous values that take into account variability in process parameters, f lows that operate for less than 24 h in an operating day, or where additional capacity is required to allow for maintenance or catch-up capability. Design values do not relate to annual production nor are they cumulative to represent a metallurgical balance. Design values are individual rates used to size equipment While actual flows might be forced to exceed the design values, performance would be degraded. For example grind could be coarser, recovery reduced, etc.


4 of 64

Soci edad Minera Cerro Verde S.A.A. Primary Sulfide Project Project No. PSP108



0.03 Source Codes

Initial Revision *


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

CODE

DESCRIPTION

A

Basic design criteria set by and/or agreed with SMCV

B

Primary Sulfide Prefeasibility Study

C

Derived from SMCV testwork program data

D

Derived from design calculations

E

Engineering handbook data

F

Fluor data based on experience from other projects

G

Normal industry practice

H

Assumed values--represents best estimate from available data

I

Manufacturer/Vendor-originated data

J

Criteria from Technology supplier

K

Preliminary information --requires further evaluation and confirmation

L

Data from existing operation

REV

*Note: Current design criteria Revision A is taken as Revision D of specification C-DC-25-901 HPGR.


5 of 64

Sociedad Min era Cerro Verde S.A.A. Primary Sulfide Project Project No. PSP108



0.04 Process Design Basis

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revisio n

P.Rosario

Date:

27-Jan-06

Rev

1

•

•

•

•

•

• •

•

•

Sociedad Minera Cerro Verde S.A.A. (SMCV) currently operates a mining/leaching SX/EW facility which produces copper cathodes. It is located near the city of Arequipa in Southern Peru, at an elevation approaching 2,800 m. The climate is generally temperate and dry, but with limited precipitation in January through March. Minimum temperatures are above freezing. The current project involves the installation of a new concentrator to treat primary sulfide ores which are becoming available as the existing oxide ore is removed from the Cerro Verde and Santa Rosa open pit mines. The primary product will be a copper sulfide concentrate of approximately 28% Cu grade, as well as a limited amount of byproduct molybdenum concentrate. Concentrate will nominally be shipped overseas through the Pacific Ocean port of Matarani, Peru, approximately 95 km from the mine site. The mineral resource is relatively low grade at an average of 0.64% Cu for the first ten years. The project viability is enhanced by the low mine waste stripping requirements as a result of oxide mining activities. The nominal treatment rate will be 108,000 t/d. There will be no provision made for future expansion and mine life will be in excess of 25 years. The approach to design of the facilities will be to design for low capital cost while still aiming at an operating cost limit of $0.60/lb copper or less. Design plant capacity will be as close as practicable to nameplate capacity to help limit capital costs. Operating schedule will be 24 h/d, 365 days per year The plant will be designed for safe and efficient operation and maintenance but with as compact a layout as is compatible with safety and efficiency. Overall plant design will be on the basis of complying with current North American standards of health, safety and environmental control, specifically OSHA, MSHA and EPA standards. Peruvian standards will be met where they are more stringent than the North American ones. The basic circuit will include: single primary gyratory crusher, with overland conveyor to a coarse ore stockpile. a secondary crushing circuit consisting of cone crushers operating in closed circuit with screens. a tertiary crushing circuit consisting of high pressure grinding rolls (HPGR) operating in closed circuit with ball mill feed screens. four grinding lines each consisting of a feed bin, two ball mill feed screens, a ball mill, and a cyclone classification system. flotation of a bulk Cu-Mo concentrate in one row of cells per ball mill; concentrate regrind in vertical stirred mills followed by upgrading in a combination of mechanical and column flotation cells. concentrate thickening. molybdenum separation, dewatering and packaging. copper concentrate dewatering by thickening and pressure filtration. Tailing will be thickened at the concentrator site, with overflow water recycled to the process water system. Tailing will be diluted and cycloned at or near the tailing embankment to provide sand for construction of the embankment itself, beyond the engineered starter dam. Specific equipment sizes, quantities and details will be developed in the Equipment List. Copper concentrate will be transported off site to the port of Matarani. Molybdenum concentrate will be packaged in drums or bulk bags for shipping to destination. • • •

•

• •

• • • •

| |

•

• •


6 of 64





Initial Revision


Date:

15-Mar-04

Rev

A

Last Revisio n

P.Rosario

Date:

27-Jan-06

Rev

1

•

Intermediate storage will be provided at several points in the process to accommodate different operating availabilities for different areas. Limited storage will be provided by the mine for stockpiling run of mine ore ahead of the primary crusher. This material will require rehandling by front end loader. Coarse ore stockpile will provide 10 h live storage and nominally 4-5 d total storage with bulldozing. This will provide adequate capacity to allow primary crusher maintenance without disrupting downstream operations. Approximately ½ h surge capacity will be provided ahead of HPGRs while over 2 h storage will be provided between the HPGR and ball mill circuits. Concentrate slurry storage for 24 h operation will be provided ahead of the filtration system to allow for a lower availability in the filter operation. Filtered concentrate storage will be provided for a total of 10 d operation, to allow for possible disruptions or delays to concentrate transport to the port. Storage will consist of 24 h capacity for direct loading, with the balance on an emergency storage pad. Concentrate loading and moving will be by front end loader. Storage for 30 d concentrate production will be provided at the port to allow for accumulation of shipload lots of concentrate as well as having capacity to accommodate delays in ship arrivals. Plant layout will be such as to maximize gravity flow of the major process streams, consistent with capital constraints of site preparation costs. Tailing flow to the tailing impoundment area will be by gravity. Spares will largely be uninstalled to constrain capital costs and to simplify installation and operation. The plant will have an advanced level of automation to help in achieving the target grinding circuit availability of 93% and the key metallurgical targets of 28% copper concentrate at 90% recovery. Design factors used in equipment sizing will be kept as low as practicable while still being able to achieve the design throughput and metallurgical performance on a yearly basis. They will be stated clearly and will be specific for each section of the process rather than applied overall. There will be no discipline design factors applied on top of the process design factors, other than required safety factors. Design Factors: For primary crushing and coarse ore conveying, a design factor of 1.111 will be used. This will meet the grinding circuit feed requirements while also allowing a reasonable margin to replenish the stockpile after crusher shutdowns. Catch-up capacity will be provided by operating at greater than the design availability on a short term basis. From coarse ore reclaim through crushing, grinding, bulk rougher-scavenger flotation, and final plant tailing, design flow will be 111.1% of nominal or balance flow, on a mass basis. This is to compensate for variability in the grindability of the ore, to ensure that over the course of a year, the daily average production can be achieved. From rougher-scavenger concentrate through regrind and cleaner circuits the design will allow for a maximum head grade of 1% Cu at nominal throughput, or 0.8% Cu head grade at the maximum throughput. This factor allows the equipment to be sized to handle the tonnage variations expected from the grinding circuit as well as the range of concentrate production resulting from variability of the copper head grade. These design factors do not relate to the defined annual production nor do they add up to result in a metallurgical or mass balance. They are used for sizing equipment. •

•

•

•

•

•

•

• •

•

•

•

•

•

•


7 of 64





Initial Revision


Date:

15-Mar-04

Rev

A

Last Revisio n

P.Rosario

Date:

27-Jan-06

Rev

1

•

The design froth factors are as follows: Copper rougher concentrates froth factor - 1.5 Copper cleaner concentrates froth factor - 3.0 Molybdenum rougher and rougher/scavenger concentrates froth factor – 3.0 Molybdenum 1st cleaner concentrates – 3.0 Molybdenum 2nd and 3rd cleaner concentrates – 3.5 Molybdenum 4th, 5th, and 6th cleaner concentrates – 4.0 These froth factors are used for sizing equipment as follows: For gravity lines (Rougher/Scavenger/Polishing/Regrind/Final Cleaners/Moly) the flow will equal the design maximum slurry flow multiplied by the froth factor. The pipes or launders will be assumed to be 50% full. For pump boxes, the live volume will equal the design maximum slurry flow multiplied by the froth factor, divided by the retention time. The retention time will be a minimum of 1 minute, as limited by available space. The freeboard above the overflow centerline will be 0.5 m and the freeboard below the overflow centerline and operating level will also be 0.5 m, leading to an operating level of 1 m below the top of the pump box. For sumps, the live volume will equal the slurry drain flow multiplied by the froth factor divided by the retention time. The volume will be determined by fl oor area and sump slopes. Floor area is a function of layout and segregation of spillage products by process characteristics. Low level will be determined by the minimum operating level of the sump pump. High level, or the sump floor high point and the sump pump base plate elevation will be 150 mm below the top of the sump opening. Sumps will have a retention time of 5 minutes, space permitting. Pumps process flow will equal the design maximum slurry flow multiplied by the froth factor. The pump vendor flow will equal the design maximum slurry flow multiplied by the adjusted froth factor by pump vendor. Pressure lines flow will equal the design maximum slurry flow. Distributor boxes live volume will equal the design maximum slurry flow multiplied by the froth factor divided by the retention time. Retention times will be a minimum of 30 seconds as limited by available space. The operating level will equal the driving head required through dart valves (if applicable), nozzle, elbow (if applicable) at the design maximum slurry flow. The freeboard above the overflow centerline will be 0.5 m and the freeboard below the overflow centerline and the operating level will be 0.5 m. The flow through samplers will equal the design maximum slurry flow multiplied by the froth factor.

• • • • • • •

•

•

•

•

• •

|

•

• •

All reagent storage facilities will require secondary containment facilities as necessary. The study will use SI (International System of Units) metric units, except for piping, which will be in Imperial units.


8 of 64




0.05 Site Conditions

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revisio n

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Data

Source Rev

Reference

1. Project Location

Mine location Project elevation: Project latitude: Project longitude:

masl deg/min deg/min

16 km ESE of Arequipa, Peru 2,700 m (8,860 ft) 16° 32’ south 71° 37’ west

L L L

A A A A

Spec C-DC-10-002 Spec C-DC-10-002 Spec C-DC-10-002

L L L L

A A A A

Spec C-DC-10-002 Spec C-DC-10-002 Spec C-DC-10-002 Spec C-DC-10-002

L L L H H

A A A A A

Spec C-DC-10-002 Spec C-DC-10-002 Spec C-DC-10-002 Spec C-DC-10-002 Spec C-DC-10-002

H L L

A A

Spec C-DC-10-002 Spec C-DC-10-002

L H

0 0

Spec C-DC-10-002 Spec C-DC-10-002

L

A

Spec C-DC-10-002

L L

0 A

Spec C-DC-10-002 2000-2002 data

L L

A A

2000-2002 data 2000-2002 data

L L

0 A

EIS data 2000-2002 data

2. Site Acc ess

Road distances to: Arequipa Pacific port of Matarani Lima, the country’s capital San Jose, railway access

km km km km

26 100 1,100 12

3. Climatic Conditi ons

A. Air Temperatures Average annual maximum °C 24.7 Average annual minimum °C 3.7 Average daily variation °C 16.6 Design maximum °C 30 Design minimum °C 0 (Short occurrences only) B. Wind Maximum gust km/h 100 Prevailing winds direction Southwesterly Winds are frequently laden with fine volcanic ash. C. Precipitation Average annual precipitation mm/a 40.7 Maximum 24 hour rainfall mm 81.5 D. Evaporation Average daily evaporation mm/d 6.1 E. Solar Radiation Average daily radiation W/m2 6,270 Range W/m2 4,230-7,850 F. Barometric Pressure Average annual mm Hg 555 Range mm Hg 551-559 G. Relative Humidity Average annual % 56.1 Range 8-100


9 of 64




0.06

General

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev. Reference

*If different than the nominal Ore type Ore specific gravity Ore moisture content Ore moisture content

nominal range

Nominal annual capacity Concentrator availability Instantaneous surge factor, throughput Concentrator treatment rate Concentrator treatment rate Operating schedule

% % t/a %

Porphyry Copper 2.75 1.7 1-5

B A L

A A

A D B D A A A A A

A

B-p.183

A

t/h t/d d/a h/d shifts/d h/shift

39,420,000 93.0 1.111 4,839 108,000 365 24 3 8

Ore head grade, years 1-10 Cu, average Mo, average Ag, average

% % g/t

0.64 0.019 1.54

B C C

1 A A

|

Metal recoveries, years 1-10 Cu, average Ag, average, to copper conc Mo, average, to Cu-Mo concentrate Mo, average, Mo concentrator

% % % %

91.4 61 71.6 90

C,D C C,H C,H

1 A 1 2

|

Concentrate grades, years 1-10 Cu, average Ag, average, in Cu concentrate Mo, average, in Cu-Mo concentrate Mo, average, in Mo concentrate

% g/t % %

29.4 47 0.677 55

C,D C,D C,D C,D

1 1 1 1

| | | |

C,D D

1 1

Des. Calc @ max feed rate & max gra

| |

C,D C,D C,D

1 1 1

Calc @ ave feed rate & ave grade

| | |

Copper concentrate production rate (dry), years 1-10 Average t/d Yearly production (nominal) t/a

2,149 784,000

Metal production, years 1-10 Cu, average Cu, maximum Mo, average

231,000 266,000 4,800

t/a t/a t/a

5,376 120,000

2,812


C C A C

Dynamic simulation

A A A A

| |

Calc @ ave feed rate & max grade Calc @ ave feed rate & ave grade

10 of 64




0.07 Ore Variability

Initial Revision


Date:

15-Mar-03

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Ore Variability by Year 108,000 t/d

Variable SPI BWI Production rate Grind size P80 Ball mill specific power Head grade Copper Head grade Molybdenum Recovery of copper Concentrate grade Concentrate grade Concentrate production

Units min. kWh/t t/h µm kWh/t % Cu % Mo % % Mo % Cu t/d

Sou rc e Rev Reference Years 1-10 Years 11-29 Average Minimum Maximum Average Minimum Maximum 146 122 160 141 121 159 15.2 14.4 15.6 15.1 14.4 15.7 4,839 5,376 4,839 5,376 125 125 8.25 7.90 8.48 8.22 7.82 8.49 0.64 0.54 0.74 0.49 0.37 0.69 0.019 0.016 0.026 0.012 0.001 0.022 91.4 90.9 91.7 90.0 85.0 91.0 55.0 55.0 29.4 27.9 30.1 27.7 27.3 31.3 2,149 2,812 1,719 2,503

Ore Lithology and Alteration Characteristics on page 2 of 3 of this spec. JK Drop Test and breakage data on page 2 of 3 of this spec. Metallurgical parameters by lithology and alteration type on page 2 of 3 of this spec. and flotation model. SPI and BWI distribution curves for LOM orebody on page 3 of 3 of this spec.


C

C

C,D C,D C,D C,D C,D C,D C,D C,D C,D C,D C,D

A A C A A A A 1 1 1 1

C C C

A A 1

C

A

Mine Plan VO2 Rev10

From material balance.

| | | | | | | | | | |

| |

11 of 64

ORE VARIABILITY BY LITHOLOGY / ALTERATION TYP

GN1- Gneiss YGD 2- Yarabamba Granodiorite

Lithology Codes

DMP 4- Dacite Monzonite Porphyry SBx 6-Silica Breccia

QTBX 8YGDBx 1 YGD Breccia DMPBx 9- DMP Breccia Document C-DC-25-001_Rev 1

Cerro Verde Sulfide Project Metallurgical Test Program Ore Type Distribution and Proposed Ore Variation Ass essment Sampling Requirements

Model 10A Al ter ati on Type Al ter ati on Al ter ati on Code Code %

Propylitic External Argillic Phyllic Potassic Silicic Propylitic (Sil) Silicic Propylitic (QS) Quartz Sericite

PE 1 A 2 PHY 3 K-S 4 SIL 5 PI-SIL 6 PI-QS 7

7.48 0.76 37.62 19.65 9.18 18.92 6.37 99.98

Totals

GN 1 % Samples

0.00 0.00 0.61 2.53 0.85 4.35 1.74 10.08

0 0 1 3 2 6 3 15

YGD 2 % Samples

6.76 0.74 27.08 8.93 4.33 8.79 2.50 59.13

9 2 37 12 6 12 3 81

Lithology SBx 6 % Samples

DMP 4 % Samples

0.71 0.02 7.60 8.01 2.86 4.56 1.79 25.55

2 0 10 11 4 6 3 36

0.01 0.00 0.21 0.01 0.18 0.39 0.18 0.98

QTBX 8 % Samples

0 0 0 0 0 0 0 0

0.00 0.00 0.92 0.06 0.36 0.32 0.00 1.66

% Samples

0 0 1 0 0 0 0 1

0.00 0.10 0.03 0.33 0.30 0.05 0.81

0 0 0 0 0 0 0 0

YGDBx 10 % Samples

0.00 0.00 1.10 0.08 0.27 0.21 0.11 1.77

0 0 2 0 0 0 0 2

Cerro Verde Drop Test Summary Lithology Code

Alteration Hazen Code Number

2 2 4 2 4 2 4 1 2 4

3 3 3 4 4 5 5 6 6 6

1 2 3 4 5 6 7 8 9 10

A

Drop Test Parameters b Axb

66.25 60.10 57.79 57.90 63.96 62.00 62.34 73.52 69.66 53.57

0.82 1.23 0.75 0.62 0.44 0.81 0.91 0.42 0.53 1.16

54.33 73.92 43.34 35.90 28.14 50.22 56.73 30.88 36.92 62.14

SPI/BWI Data Ta

0.52 0.89 0.41 0.52 0.21 0.53 0.52 0.40 0.42 0.80

SG

2.85 2.86 2.87 2.92 2.86 2.79 2.84 2.86 2.86 2.89

No. SPI/BWI

SPI Ave

37 37 10 12 11 6 4 6 12 6

101 101 104 173 180 97 107 164 149 179

Min

Max

44 44 58 83 127 48 33 98 95 154

SD

161 161 186 242 232 146 152 297 192 233

Ave

34 34 50 52 32 39 49 69 26 32

14.9 14.9 14.0 15.4 16.2 12.9 15.4 15.6 15.4 15.3

BWI (kwh/mt) Min Max

13.2 13.2 12.5 12.8 13.4 10.8 13.7 13.4 12.7 14.5

SD

16.5 16.5 16.0 17.3 18.2 15.0 17.2 17.5 19.7 16.3

Distrib ution of Metallurgi cal Ore Type Parameter (MET01) From L OM Plan Lithology Alteration MET01 Number % of Cu Mo Cu Conc of B loc ks Tot al Rec ov er y Recov er y Grade 51 1-4-6-8-9-10 1-2-7 13,121 19.0 90.1 51.4 28.4 52 2 1 3,960 5.7 82.8 51.4 26.1 53 2 2 488 0.7 90.1 53.1 28.4 54 2 3 18,037 26.1 85.0 49.1 24.8 55 2 4 6,600 9.5 88.1 51.6 30.9 56 2 5 3,078 4.5 90.0 50.1 27.4 57 2 6 5,634 8.2 91.4 56.2 29.1 58 2 7 1,509 2.2 88.7 53.8 25.5 59 4 3 5,388 7.8 88.0 48.0 30.1 60 4 4 5,770 8.3 92.7 52.9 29.8 61 4 5-6 5,171 7.5 93.2 55.3 29.8 0 365 0.5

Total

69,121

100.0


12 of 64


Document C-DC-25-001 Rev 0



Initial Revision


Date:

15-Mar-03

Rev A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

So ur ce Rev Reference C

Cerro Verde SAG Performance Index Distribution 100% 90% 80% 70%

%

60%

A

2.4 2.4 1.2 1.4 1.5 1.7 1.9 1.5 1.9 0.7


Document C-DC-25-001 Rev 0



Initial Revision


Date:

15-Mar-03

Rev A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

So ur ce Rev Reference C

A

C

A

Cerro Verde SAG Performance Index Distribution 100% 90% 80% 70%

% e 60% v i t a 50% l u m 40% u C 30% 20% 10% 0% 0

25

50

75

100

125

150

175

200

225

250

275

300

SAG Performance Index (minu tes)

Cerro Verde Bond Work Index Distributi on 100% 90% t 80% n e 70% c r e P 60% e v 50% i t a 40% l u m 30% u C 20% 10% 0% 10

11

12

13

14

15

16

17

18

19

20

Bond Work Index (kWh/t)


13 of 64




0.08 Block Flow Diagram

Initial Revision


Date:

15-Mar-03

Rev A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

Units

Data

1

Source Rev Reference

108,000 t/d HPGR case:

See drawing no. PSP108-C-0000-25I-001 Rev 4


C

1

|

14 of 64




1.01

Primary Crushing

Initial Revision


Date:

15-Mar-04

Rev A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

Units

Nominal

Size (mm) 2,000 1,200 600 200 100 50 25 12 6 mm t/a t/h t/h t/h mm mm days/year shifts/day hours/shift % h/d 3 t/m

Cum % passing 100 99 95 70 50 30 25 15 8 380 39,420,000 6,429 6,429 6,540 200 165 365 3 8 70% 16.8 1.6

Design*

Source

1 Rev

Reference

* If different than the nominal Run of mine feed size: Top size

Nominal run of mine 80%passing Crusher annual production (dry) Crushing rate (dry) Disch. conveyor capacity average Coarse ore conveyor capacity (wet) Open side setting recommended Product size 80% passing Operating schedule

Availability (crusher & disch. conv.) Bulk density (dry) vol. calcs - design Bulk density (dry) wt. calcs - design Abrasion index, average/range Crushing work index (low energy) av/range Ore UCS, Average/max Crusher type No of crushers Crusher size Crusher dump pocket capacity Crusher surge pocket capacity Truck dump points Dust suppression method Moisture content, nominal/range Dump pocket cleanout method Mine haul truck capacity, design Maximum conveyor inclination Maximum inclination at loading point Minimum chute slopes Dynamic surcharge angle of material on belt Angle of repose Angle of withdrawal

3

t/m Bond kWh/t MPa _ in t t units % t degrees degrees degrees degrees degrees degrees

7,200 7,200 7,300

1.92 0.24/0.2 to 0.3 13/7-19 140/250 Gyratory 1 60-113 500 500 2 Water spray and ADS spray 1.7/1-5 Backhoe 238 15 10 70 25 max 37 65


H H H H H H H H H H A D D D I I A A A G G H

A A A A A A A A A A C C C C A A A A A A A A

H H C H A,G D I G G A G H G A F F F F B E

A A C A A A C A A A 0 A A A A A A A A A

Maximum Maximum

Dawson tests

15 of 64




1.02 Coarse Ore Stockpile

Initial Revision


Date:

15-Mar-04

Rev A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

Units

Stockpile live capacity (dry) Stockpile live capacity (dry) Stockpile diameter Stockpile height Stockpile capacity total without pushing Stockpile capacity total with bulldozing Stockpile capacity total Material angle of repose Draw down angle Moisture content Bulk density (dry) vol. calcs - design Bulk density (dry) wt. calcs - design

t h m m t t d degrees degrees % 3 t/m 3 t/m

Nominal

Design*

50,000 10 115 44 250,000 400,000 4 37 65 1-5 1.6 1.92


Source

F D C C F A F A F L F F

1 Rev

Reference

* If different than the nominal C-7606-3100-59-SK102 A C A A A A A A A A A A

16 of 64




1.03

Stockpile Reclaim Feeders

Initial Revision


Date:

15-Mar-04

Rev A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

Units 3

t/m Bulk density (dry) vol. calcs - design 3 t/m Bulk density (dry) wt. calcs - design Nominal feed top size mm Number of lines Feed moisture, nominal % Total feed rate, nominal (dry), design (wet) t/h Number of feeders Normal no. feeders operating Feed rate/feeder (dry) - nominal, (wet) - max t/h Feeder type Feeder control VSD/Fixed Feeder drive type Coarse ore reclaim conveyor capacity wet t/h width mm Coarse ore reclaim dust control Coarse ore surge bin capacity time min tonnage, per line t Availability %

Nominal

Design*

1.6 1.92 280 1 2.4 5,056 4 3 1,685 Apron VSD VFD 11,500 2,400 ADS sprays 17 800 89


6,000

2,000

Source

A A E A L D F F D F G G D D G K D G

1 Rev

Reference

* If different than the nominal A A A A 0 C A A C A A A 0 A A A A 1

|

17 of 64




2.01 Secondary Crushing & Screening

Initial Revision


Date:

15-Mar-04

Rev A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev 1

Units

Nominal

Design* Source Rev Reference

* If different than the nominal Coarse ore screens

Purpose Number of screens Feed to screening section New feed, nominal (dry), design (wet) Recirculated, nominal, design (wet) Total, nominal (dry), design (wet) Feed rate per screen, nominal (dry), design (wet) Screen feed size 100 % passing 80% passing % passing 75 mm % passing 40 mm % passing 20 mm Screen size and type To deck o enin Efficiency Bottom deck opening Efficiency Screen oversize (combined TD + BD) per screen Screen undersize product (-40 mm) per screen

Ref. Bruno CVHPGR24r

G D

A C

A D D D L D D D D D D D D D D A

1 1 0 C 0 C C C C 0 C C C C 1 1

4 750 45 70 74 Closed, C.O. Screens type ADS 40 t/10 t overhead crane % 85

D I D I D I,A G F G

A A A A A A A A 1

t/h

D

0

Scalp secondary crusher feed 4 t/h t/h t/h t/h mm mm % % % m mm % mm % t/h t/h

5,056 5,800 5,056 6,300 10,112 11,500 2,528 3,200 280 103 73 46 24 3.66 x 7.93 DD Banana 76 90 49 90 1,264 1,700 1,264 1,500

Utilization 89% ** *

| | |

*** ***

| |

Secondary crushin g

Number of crushers Crusher size Closed side setting Product percent passing css Product percent passing 47 mm Open or closed circuit Secondary crushing & screening dust control Secondary crushing maintenance crane Crusher Normal Operating Loading Factor

No. kW mm % %

|

Crusher Feed

Screen oversize (combined TD + BD)

1,264

1,700

|

CVHPGR 24n

| | |

*Maximum new feed rate and maximum recirculation do not coincide **Design value calculated assuming 2 crushers@100% load and 2@normal 85% load ***Design value calculated with crusher@85% load


18 of 64




2.02 Tertiary Crushing & Screening

Initial Revision


Date:

15-Mar-04

Rev A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Rev

Reference

Units

Nominal

Design*

Source

* If different than the nominal Tertiary crushi ng

Surge bin capacity, per unit Number of crushers Section availability Crusher type, size Installed power per unit Specific throughput rate Specific energy Specific press force Feed topsize Circulating load Feed rate per crusher, dry Feed moisture Product size P80 Tertiary product bulk density Tertiary product bulk density Expected wear rate Expected roll life Tertiary crushing dust control

time tonnage installed operating

range range range range range range % -5 mm Flake Loose range

min t

31 1,200 4 4 % 91% HPGR 24/17-8 kW 2 x2,500 ts/hm3 200-256 256 kWh/t 1.7-2.0 2.0 N/mm2 3.5-4 4.0 mm 46 50 % 20-75 75 t/h 2,349 2,630 % 3-6% 5% mm 4-10.8 10.8 % 65 t/m3 2.3 t/m3 1.4 g/t ore 0.75 h 5,700-6,700 6,000 Dust collection, wet scrubber

Ball mill screening

Total feed rate to screens Section availability Surge bin capacity, per unit

t/h % h t

9,396 93% time 2.1 tonnage 5,000 Number of screens 8 Feed rate per screen t/h 1,149 Number of feeders per screen 1 Capacity per feeder t/h 1,149 2,100 Wet or dry screening Wet Screen feed arrangement Pulping box ahead of screen; water sprays both decks Screen size, type m 3 X 7.3 DD Banana 12 Top deck opening mm Efficiency % 88 Bottom deck opening mm 6 Efficiency % 91 Oversize product moisture range % 5-10% 10% Circulating load to HPGR circ, total dry t/h 4,355 wet t/h 4,839 range % 20-90 75 Undersize product, total dry t/h 4,840 Undersize product, size P80 mm 2.8 3.5


F D I,A I A I I I I I I I D H I I C C C I G

C A A A C 0 0 A A A C A A C A A C 1 A A A

G D A D D D D F D A,G F D D D D D H D D I D D

A 0 C 0 A C C C C A A 0 C C C C A C C C C 1

Dynamic Simulation Dynamic Simulation

1.6 is used for bin sizing Krupp-Polysius "

|

Ref Bruno CVHPGR25

Ref. Sim HPGR PSDs

19 of 64

|




2.05 Ball Mill Grinding

Initial Revision


Date:

15-Mar-04

Rev A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Rev

Reference

Units

Nominal

Design*

Source

* If different than the nominal Ball Milling

Section availability Number of mills Feed rate per mill - dry Feed rate total - dry Solids S.G. design basis Feed size - T80 Product size P80 - range

% t/h t/h _ µm µm

93% 4 1,211 4,843 2.75 2,800 115-150

1,350 5,400

125

A D D D C D C

C A 1 1 A C C

C C C,A

A A A

C,D

A A C

C,D C,D C,D

C C C

F

A

| |

Mill feed characteristics

Reduction in ball mill feed work index "soft" % 11.9 "hard" % 6.3 Assumed for design % 10 * Open circuit test. Reduction expected to be less for closed circuit product test. Work Index, maximum annual average (reduced basi metric 14.1 metric Work Index, annual average range (reduced) 13.0 - 14.1 Nominal New feed size distribution Size Cumulative mm % Passing 5.6 99.7 5 98.7 2.8 80.0 1 57.0 0.5 44.0 0.31 37.0 0.2 32.0 0.125 27.0 0.09 24.0 D99 mm 5.6 New feed D80 mm 2.8 D50 mm 0.7 Circuit configuration

Screen undersize product discharges to ball mill discharge/cyclone feed sump and is cycloned before reaching ball mill feed


Krupp Krupp Krupp

20 of 64




2.05 Ball Mill Grinding

Initial Revision


Date:

15-Mar-04

Rev A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Rev

Reference

Units

Mill drive type Mill motor Design factor for grinding and downstream Ball mill operating point Ball load (nominal) Charge volume Percent of critical speed Ball mill drive design conditions Ball load (drive design point) Charge volume Percent of critical speed Ball mill structural design point Ball load Total charge Mill diameter inside shell Mill effective grinding length Critical speed Operating speed, nominal Mill rotation direction Trommel installed Liner material Liner wear rate Maximum ball size Estimated ball consumption Slurry percent solids by mass Lime addition Pulp pH Circulating load - design basis (UF:OF)

type kW

Nominal

Gearless 12 000 1.11

Design*

Source

* If different than the nominal B 0 B 0 C

% by vol % by vol %

35 35 75

B F B

C A C

% by vol % by vol %

38 38 75

B I B

A A C

% by vol 40 % by vol 40 m (ft) 7.300 (24) m (ft) 11.000 (36) rpm 15.9 % critical 75

F I B B D B

A 0 0 C C

Clockwise, viewed from feed end Yes/no No type Steel g/t ore 22 mm 75 kg/t ore 0.35 % 72 yes/no yes pH 9.5-10 % 250

I F G B B B A C B G

0 A A A A A A A A A


21 of 64




2.06 Ball Mill Ball Handling

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units Ball delivery method Ball delivery mass per load Ball size, normal Ball specification Ball consumption rate Ball consumption Ball storage capacity Ball storage capacity, total mass Ball loading to long term storage Ball recovery method from feed hopper

Ball feeding/metering system Manual/automatic/continuous operation Feeders Ball feed rate Feeder operating time, design Ball transfer to ball feeding conveyor Feed selection to specific ball mill Ball addition measurement method Emergency ball addition method Emergency ball addition point Emergency ball bucket capacity

t mm kg/t ore t/d d t

Nominal

Design*

Truck 35 75 Forged 0.35 38 31 1,200 Rear dump truck Gravity fed chute

53

Metering feeder to ball conveyor Automatic number 1 t/h 6.6 16.8 h/d 24 High angle conveyor Diverter gates on ball distribution conveyor Belt weightometer Ball bucket by crane Feed point on each ball mill feed chute t 4


Source Rev Reference * If different than the nominal G A K A B A G A B A D 1 A 1 D A G A G A

F A G A A F F F F F F

| |

A A A A A A A 0 A A A

22 of 64




2.07 Ball Mill Discharge Sump/Pump

Initial Revisio n


Date:

15-Mar-04

Rev

A

Last Revisio n

P.Rosario

Date:

27-Jan-06

Rev

1

Units Per Ball Mill Grinding Line

New feed mass, design maximum Ball mill circulating load (UF:OF) Total cyclone feed, including circulating load Solids specific gravity Cyclone feed density Cyclone feed slurry specific gravity Number of cyclone clusters per ball mill Feed volume per cyclone cluster Number of operating pumps, total Number of installed standby pumps Number of uninstalled standby pumps Pressure drop across cyclones Pump type Pump size Pump liner material Pump impeller material Pump drive Sump retention time, minimum Sump volume Sump shape

Nominal Design* Source Rev Reference

* If different than the nominal 1,211 1,350 A 1 250% G A 4,238 4,700 D 1 2.75 B A % wt. 50% 60% K A 1.46 1.6 D A 1 G A m /h 5,832 6500 D 1 Design value calc @ 50% wt. mm 1 A A 0 A A 1 A A per 2 operating pumps kPa 69 I 0 Horizontal centrifugal slurry pump G A 28x26 D A Metal G A Metal G A VFD A C min 1.95 1.75 G 1 m 190 D 1 Sides sloped at 60 deg from horiz.(lower part) A t/h % t/h

Estimated cycl one feed size distributi on

100 % passing size F100 80% passing size F80 % passing 75 µm

µm µm

%

6,000 550 28-35


H H H

C C C

23 of 64

| | |

|

| |




2.08 Primary Milling Classification

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revisio n

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal Design* Source Rev Reference

Total Grinding Circuit:

* If different than the nominal 5,400 A 1 G A 18,900 D 1 60% G A A A

Total new feed mass t/h 4,843 Ball mill circulating load (U/F:O/F) % 250% Total classification feed t/h 16,951 Cyclone feed density % wt. 50% Number of cyclone clusters (1 per ball mill) 4 Per ball mill/cyclone cluster m3/h Feed volume per cyclone cluster 5,832 6,500 m µ Split size D50 Overflow: Product solids mass t/h 1,211 1,350 µm Product P80 size 125 125-149 Product density, weight % solids % wt. 28% m3/h Product slurry volume 3,554 3,950 Underflow Product solids, mass t/h 3,027 3,370 µm Product D80 size 2,000 Product density, weight % solids % wt. 72% Product specific gravity 1.85 m3/h Product slurry volume, nominal 2,278 2,540 Cyclone Clusters Cyclone size mm 840 Cyclone type High efficiency design Number of operating cyclones per cluster 6 Total number of cyclones per cluster 8 Vortex finder diameter mm 350 Vortex finder material ceramic Apex diameter 163 Apex fixed/adjustable fixed Apex material ceramic Pressure drop across cyclones kPa 69 Distributor type Bottom feed radial manifold Cyclone installation angle, degrees from vertical degrees 11 Cyclone isolation Full flow knife gate valves w/rubber sealing Cyclone valve operation Automated, air actuated Feed manifold lining Rubber Underflow launder lining Rubber Overflow launder lining Rubber Estimated size distributions Size Feed (nom) Underflow Overflow Cum % Cum % Cum % passing passing passing µm 12,500 100.0 100.0 100.0 9,500 99.7 94.6 100.0 4,750 97.8 88.2 100.0 3,350 96.6 84.7 100.0 2,000 92.7 79.8 100.0 850 86.2 70.5 100.0 600 81.7 64.5 99.9 300 66.1 44.9 96.9 212 57.1 35.2 90.7 150 47.5 25.7 83.0 106 38.6 17.4 75.3 75 32.9 15.0 68.0 F:\103\109 EngDoc\109.3 CRIT_DC\Process\C-DC-25-001\C-DC-25-001_ProcDesCrit_Rev1.xls

| |

D

1 A

|

D A C D

1 C A 1

|

D D A D D

1 A A A 1

|

I G I I D G D G G I G I G G G G G

0 A 0 0 0 A 0 A A 0 A 0 A A A A 0

I

A

|

|

|

Candelaria

24 of 64




Initial Revision Last Revision

4:01

Rougher Flotation

C-DC-25-901 HPGR Rev. D P.Rosario

Date:

15-Mar-04

Rev

A

Date:

27-Jan-06

Rev

1

Units

Nominal

minutes t/h t/h m3/h m3/h % % Yes/No

0 4,843 4,480 14,215 13,120 28 25 - 32 Yes 10-11 125

Design*

Source

Rev

F

1 0 C 0 C A A A 1 A

Reference * If different than the nominal

Conditioning time Feed rate Feed rate - Minimum Pulp flow rate Pulp flow rate - Minimum % Solids by mass % Solids by mass - Range Lime addition Slurry pH P80 feed Cell type Cell Volume Effective Cell volume No of rows of cells No. of cells/row Residence time basis Effective Volume Air Holdup Pulp residence time - 1st cell Pulp residence time - 2nd cell Concentrate collection lip length Lip loading factor - 1st cell Lip loading factor - 2nd cell Froth factor for concentrate design Flotation air Air volume/cell Air pressure Air temperature Feed grade Stage recovery - 1st cell Stage recovery - 2 cells combined Tailing grade - 1st cell Tailing grade - 2nd cell Conc grade - 1st cell Conc grade - 2nd cell Weight floated % of plant feed - 1st cell Weight floated % of plant feed - 2nd cell Concentrate rate - solids only - 1st cell Concentrate % solids - 1st cell Concentrate P80 microns Concentrate solids S.G. - 1st cell

µm

5,400 15,800

C,G B

Mechanical 160 m /cell 136 m3 /cell _ 4 _ 2 ave flow@ave density@effective cell volume % (100-% Air Holdup) % 15 minutes 2.30 minutes 2.33 m/cell 60.0 t/m/h 1.05 1.43 t/m/h 0.78 1.01 _ 1.5 forced/induced Induced Not Applicable m3/h kPa Not Applicable degrees C Not Applicable 3

% Cu % % % Cu % Cu % Cu % Cu % % t/h % µm _

0.64 55.57 78.81 0.290 0.140 17.18 11.33 2.07 1.31 100.2 39.8 110 3.65

D D D D B F

0.50-1.00 51.96-58.23 75.71-80.93 0.213-0.457 0.221 15.48-19.59 13.68 2.84 1.70 84-138 30.0 - 42.0 125 3.53-3.83

B D B,D B,D

F D D I D D G I I I

A B C/D C B/D C/D C/D C/D C/D C/D D,G C C/D

A A 1 1 1 A A C C A C C C 0 0 0 0

| |

Ball mill cyclone operating range Lime added to one line

|

| | | Industry standard

Vendor specification

A C C 1 C 1 1 1 1 1 1 1 B

| | | | | | | |

Concentrate Product Destination

A. Normal B. Alternate C. Alternate

Polishing mill Regrind mills Column Cells


F F

Normally - 1st cell feeding polishing mill

25 of 64

Sociedad Minera Cerro Verde S.A.A. Primary Sulfide Project Project No PSP108



4:02

Scavenger Flotatio n

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev

Feed rate Pulp flow rate % Solids by mass Lime addition Slurry pH

t/h m3/h % Yes/No

4,675 13,882 27.8 No 10-11

5,200 15,400 27.6-27.8

B/D B/D B/D A,G C

0 1 C 1 1

Cell type Cell Volume Effective Cell volume No of rows of cells No. of cells/row Residence time basis Effective Volume Air Holdup Pulp residence time Concentrate collection lip length Lip loading factor Froth factor for concentrate design

Mechanical 160 m3 /cell 136 m3 /cell _ 4 _ 8 ave flow@ave density@effective cell volume % (100-% AIR HOLDUP) % 15 minutes 19.30 m/cell 60 t/m/h 0.51 _ 1.5

B I B/D B/D D I D I D C

A A 1 1 1 A A C A 1 A

I I I

0 0 0


Flotation air Air volume/cell Air pressure

forced/induced m3/h kPa

Induced Not Applicable Not Applicable

Feed grade Stage recovery Tailing grade Conc grade

% Cu % % Cu % Cu

0.140 76.4 0.035 4.76

0.098-0.221 73.7-79.3 0.027-0.055 3.68-6.31

B/D B/D B/D B/D

C C C C

Weight floated % of plant feed Weight floated % of plant feed Concentrate rate - solids only Slurry flow rate Concentrate % solids Concentrate P80 microns Concentrate solids S.G.

% % t/h m3/h % µm _

3.98 5.29 256.3 992.3 21.96 125 3.17

4.53 5.00-6.24 223.8-303.6 868-1164 21.93-22.52 115-150 3.07-3.35

C/D C/D C/D C/D C/F C C

C 1 C 1 1 A C

| As per Float model, lime added @Regr.

Vendor recommendation

| | |

Vendor recommendation Vendor recommendation

Vendor specification Vendor specification

|

4 stages average

Vendor recommendation Vendor recommendation

Includes Rougher # 2 cons Excludes #2 Rougher cons Includes #2 Rougher cons Includes #2 Rougher cons Includes #2 Rougher cons Includes #2 Rougher cons

| | | |


A. Normal B. Alternate

Regrind mills None


| |

26 of 64





4:03

Rougher Concentrate Polishing


Date:

15-Mar-04

Rev

A

Date:

27-Jan-06

Rev

1

Units

Nominal

no.of % type kW -

2 93 SMD 355 355 Top

% of plant feed % of plant feed t/h t/h % µm µm % Load t/h mm kg/t ore conc _ pH

2.07 3.38 100 164 39.5 110 40 26 4.5 3 0.335 3.65 10.5

kWh/t _ type mm/kt ore

Design*

Source

Rev

I G K

0 C 0 C 0


No. of Mills Availability Mill type Mill motor Mill Feed Location New feed rate total New feed rate total New feed rate total New feed rate total Pulp percent solid Feed size - P80 Product size - P80 - (Minimum) Media Ball load average Normal operating charge Maximum media ball size Estimated media ball consumption Solids S.G. Pulp pH Specific power consumption Sizing basis Liner material Liner wear rate

Based on Rougher cons from 1 st cell

K

1 1 0 0 1 C A 1 1 1 1 C A

5 Power Requirement

C G

1 A

METSO

magnetic rubber 0.14

I H

1 1


2.84 4.54 140 224 39.8 50

B/D C B/D C B/D C C I I C C

3.83

Based on Rougher cons from 1 st 2 cells

| |

Based Rougher cons from 1 st cell Based Rougher cons from 1 st 2 cells

| DML LC test report Sep04

| | | |

METSO METSO METSO METSO

METSO recommendation

| |

METSO

| |

27 of 64




4:04

Scavenger Concentrate Regrind

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

_ % type kW -

3

Design*

Source

Rev


No. of Mills Availability Mill type Mill motor Mill Feed Location

I G K

C C C C A

35

B/D B/D F/D C C I I I I H B I

1 1 1 C 1 1 1 1 1 1 C A

pH

10.5-11.0

C

A

Specific power consumption Sizing basis

kWh/t _

12.2

I C

1 C

Liner material Liner wear rate (screw only)

type kg/t ore

I I

A 1

New feed rate to cyclone total % of plant feed New feed rate total t/h Mill feed percent solids by mass % Feed size - P80 µm Product size - P80 µm Ball load average % Load Normal operating charge t Recommended ball size mm Maximum ball size mm Estimated ball consumption kg/t feed Solids S.G. _ % Vertical mill grinding efficiency improvement Pulp pH

93 VTM 1500

1119 Bottom 5.29

5.00-6.24

256

224-304

64.5

64-65

125

168

30

30-35

26 128 12.5 31 0.25 3.17

3.07-3.35

Power requirement magnetic 0.0014


Does not include any portion of Clean. Scav. Conc.

| | |

NB New circuit feed not cyclone underflow NB Circuit product from regrind cyclones

| | | | | |

Basis: Metso/DML test report #63383, Sept04

|

|

28 of 64





4:05

Regrind Circuit Classification


Units

Date:

15-Mar-04

Rev

A

Date:

27-Jan-06

Rev

1

Nominal

Design*

Source

Rev


No. cyclone clusters per pump No. installed cyclones per cluster No. cyclones operating Cyclone size, type Vortex finder diameter Apex diameter Cyclone feed rate Cyclone feed rate - Minimum Cyclone feed rate (solids)

m3/h m3/h t/h

Cyclone feed pulp density Cyclone feed % Solids by mass Cyclone feed D80 Cyclone feed D50

t/m3 % µm µm

1.34 36.8 85 35

Cyclone underflow pulp density Cyclone underflow % Solids by mass Cyclone u/f D50 Cyclone overflow pulp density Cyclone overflow % solids by mass Cyclone O/F rate, dry Cyclone o/f P80 Cyclone o/f P50

t/m3 % t/m3 % t/h µm µm

1.80 65 70 1.17 21.7 258 30 14

_

3.17

kPa

125

%

160

Solids S.G. Cyclone inlet pressure Circulating load

_ _ _ mm mm mm

µm

1 14 12 380, high efficiency 113 75 1,367 1,610 1,190 671 810


34 - 38

60 - 70

18 - 22 310 25 - 35

3.07 - 3.35

140 - 180

I I I I I I B/D C C

A 1 0 A 0 0 1 C 1

B/D B/D C C

1 1 A A

| |

B/D B/D C B/D B/D

| |

C C

1 1 A 1 1 1 A A

C

C

I

A

I

1

|

Includes lime addition

|

Includes lime addition

|

| | |

|

Initial Estimate -

29 of 64




4:06

Cleaner Flotatio n - 1st Cleaner Cells

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev

Conditioning time Feed rate Pulp flow rate % Solids by mass Lime addition Slurry pH

minutes t/h m3/h % Yes/No

0 461 1,849 21.4 No 10.0 - 11.0

F C,D C,D C C C

1 1 1 C A A


mechanical 160 C/B m /cell 136 C/B m3 /cell _ 1 C _ 6 C ave flow@ave density@effective residence time % (100-% Air holdup) % 15 I minutes 26.48 C/B/D m/cell 60 I t/m/h 1.74 I _ 3 F


586 2,253 21.1 - 22.1

3



Induced air Not Applicable Not Applicable

Feed grade Stage recovery Tails grade Conc grade

% Cu % % Cu % Cu

4.82 94.66 0.45 10.53

Weight floated % of plant feed Concentrate rate - solids only Concentrate % solids Concentrate P80 microns Concentrate solids S.G. Concentrate slurry flow rate

% t/h % µm _ m3/h

4.12 200 23.9 30 3.64 692

A A A A A A A A 1 A C A

| | |

Industry standard

| Vendorspecification

A I I

0 0 0

3.72 - 6.74 91.1 - 94.9 0.32 - 0.76 8.71 - 13.16

C,D C,D C C,D

1 1 C 1

| |

3.55 - 5.79 158 - 280 18 - 26

C,D C,D C,D C C,D C,D

1 1 1 A 1 1

| | |

3.49 - 3.87 959

|

| |

Including water addition



Column cells Regrind circuit


30 of 64




4:07

Cleaner Flotatio n - Cleaner Scavengers Cells

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev



minutes t/h m3/h % Yes/No

0 261 1,163 19.6 No 10.0 - 11.0

F C C,D C,D C C

1 C 1 1 A A


mechanical 160 C/B m3 /cell 3 136 C m /cell _ 1 C _ 4 C ave flow@ave density@effective residence time % (100-% AIR HOLDUP) % 15 I minutes 28.1 C,D m/cell 60 I t/m/h 0.02 I _ 1.5 F

A A A A A A A A 1 A C A



Induced Not Applicable Not Applicable

Feed grade Stage recovery Tails grade Conc grade

% Cu % % Cu % Cu

0.45 6.3 0.43 5.02

% t/h % % µm µm

0.03 1.5 22 18-24 30 25-35 3.34 10.7

Weight floated % of plant feed Concentrate rate - solids only Concentrate % solids Concentrate % solids - range Concentrate P80 microns Concentrate P80 microns - range Concentrate solids S.G. Concentrate slurry flow rate

3

m /h

302 1,293 19.3 - 20.5

A I I

0 0 0

0.32 - 0.76 2.7 - 14.6 0.31 - 0.66 3.37 - 7.81

C C,D C C,D

C 1 C 1

0.01 - 0.09 0.5 - 4.3

C C,D C C C C C C,D

C 1 C A A A C 1

3.18 - 3.63 16.4

| | |

Industry standard

| Vendor specification

| | | |

3

Including wash water (5.0 m /h)



Regrind circuit columns


31 of 64

|




4:08

Cleaner Flotation - Final Column Cells

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev



minutes t/h

Column diameter Column height No. of Columns

m m _

5.0 12.0 4

type

drip pans 180 +ve

m3/h % Yes/No

0 300 882 27.3 No 10.0 - 11.0

420 1220 27.0 - 27.6

F C C,D C,D C C

1 0 1 1 A A

|

C/I C/I C/I

1 1 1

| | |

C J

A A

|

C G F

0 A A

I I C

0 0 A

| |

Wash water addition method Wash water volume Wash water bias

m3/h

Carrying Capacity - Nominal Limiting Carrying Capacity Froth factor for concentrate design

t/h/m2 t/h/m2 _

1.2 1.50 3

Air supply pressure Air volume per column Air Superficial Velocity

kPag Nm /h cm/sec/m2

580 703 1.0

% Cu % % Cu % Cu

12.75 74.1 4.89 29.09

11.06 - 15.28 69.0 - 76.4 3.77 - 7.18 27.43 - 30.92

B/D B/D B/D B/D

1 1 1 1

| | | |

% t/h % µm _

2.01 97 31.9 30 4.01 235

1.67 - 2.94 74 - 143 28-34 25-35 3.93 - 4.10 339

B/D B/D B/D C B/D B/D

1 1 1 A 1 1

| | |

Feed grade Stage recovery Tails grade Conc grade Weight floated % of plant feed Concentrate rate - solids only Concentrate % solids Concentrate P80 microns Concentrate solids S.G. Final Concentrate slurry flow rate

3

m3/h

325

1.8


Industry standard

Vendor is 4

| |

Including all water additions

32 of 64




4:09

Copper Moly Concentrate Thickening

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


Feed Thickenin g

No. of thickeners Thickener diameter Thickener type Thickener feed rate

Fresh feed Overall Thickener feed rate - Minimum Fresh feed Overall Flocculant addition Diluted feed % Solids Diluted feed % Solids - Range Underflow % Solids Underflow % Solids - Range Specific Area (design)

m type t/h t/h t/h t/h g/t Conc % % % % 2 m /t solids/day

1 30.0 conventional 97 129 74 98 0 22.2 40 0.15


143 191

21.0 - 26.0 50 35 - 50

B B D D D D D A D D F F D

A C C 0 1 0 1 1 1 1 1 1 1

Fresh feed only Overall Fresh feed only Overall

| | | | | | | |

33 of 64




5:01

Moly Ro-Scav Flotation

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


Flotation

Conditioning Tank volume Conditioning time Fresh Feed rate Feed rate (Combined) Pulp flow rate (Combined) % Solids by mass % Solids by mass - range Lime addition Slurry pH P80 feed

3

D C,D D D/F D/I D F,D D/F C C

1 1 1 1 1 1 1 1 1 1

Cell type Tank Mechanical 3 Cell Volume 30 m /cell 3 Effective Cell volume 25.5 m /cell No of rows of cells _ 1 No. of cells/row _ 6 No. of Rougher cells _ 4 No. of Rougher/Scavenger cells _ 2 Pulp residence time minutes 28.2 Froth factor for concentrate design _ 3.0 Air supply (O 2 depleted) Induced air, recirculated within closed cells and tanks

C,D I I F,D F,D F,D F,D F,D F I

1 1 1 1 1 1 1 1 1 1

Feed grade

C/D C/D C/D C/D C/D C/D C/D C/D C/D

1 1 1 1 1 1 1 1 1

D D F,D C F,D

1 1 1 1 1

| | | | |

D D F,D C

1 1 1 A

| | |

Tails grade Rougher Concentrate grade Final concentrate grade Mo Recovery (final)

m minutes t/h t/h 3 m /h % % Yes/No µm

56.5 15 97 127 224 39.7

74 - 143 98 - 191 326 37.0 - 42.0

No 11 30

% Mo % Cu % Mo % Cu % Mo % Cu % Mo % Cu %

0.677 29.1 0.068 29.4 3.60 12.00 55.0 0.5 90.0

% t/h % µm _

23.8 23.2 25.0 30 4.06

% t/h % µm

7.4 7.2 25.0 30

0.5-0.9 23 - 30

Nominal Fresh feed only Cu-Mo Conc/1st Cleaner Tail/Ro-Scav Con Combined Combined

| | | | | | | | | | | | | | | | | | | |

B,D B,D

Fresh feed (Cu-Mo Concentrate) Fresh feed (Cu-Mo Concentrate)

Mo. Rougher Flot. Only (4 cells) Mo. Rougher Flot. Only (4 cells)

| | | | | | | | |

Rougher

Weight floated % of moly plant feed Concentrate rate - solids only Concentrate % solids Concentrate P80 microns Concentrate solids S.G.

17 - 35 23 - 30 30 - 50

Rougher/Scavenger

Weight floated % of moly plant feed Concentrate rate - solids only Concentrate % solids Concentrate P80 microns


5.6 - 10.6 23 - 30 30 - 50

34 of 64




5:02

Moly Cleaner Flotation

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


st

1 Cleaner

Conditioning Tank volume Conditioning time Feed rate Feed rate - Minimum Pulp flow rate Pulp flow rate - Minimum % Solids by mass Lime addition Slurry pH D80 feed Cell type Air supply (O 2 depleted)

3

56.5 21 32 23 3 160 m /h 3 115 m /h % 17.2 Yes/No No 11 30 µm Mechanical Induced air, recirculated within closed cells and tanks Cell Volume 8.5 m3 /cell 3 Effective Cell volume 7.2 m /cell No of rows of cells 1 No. of cells/row 7 Pulp residence time min 19 Froth factor for concentrate design 3.0 Conc grade Weight floated % of moly plant feed Weight floated % of moly plant feed - range Concentrate rate - solids only Concentrate % solids Concentrate P80 microns Concentrate solids S.G.

m min t/h t/h

% Mo % Cu % % t/h % µm -

7.00 3.50 9.7 7-13 9.5 25.0 30 4.10


48 242 16 - 21

7.0 - 14.4 22.0 - 27.0 30 - 50

D C,D D D D D D/F D/F F C C,D I I I D/F D/F D/F F

1 1 1 1 1 1 1 1 1 1 1 1 C 1 1 1 0 1

C/D C/D D D D F,D C F/D

1 1 1 0 1 1 A C

| | | | | | | | | | | |

Nominal

| | | | |

Nominal

| | | | | | | |

35 of 64




5:02


Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


nd

2 Cleaner

Conditioning time Feed rate Feed rate - Minimum Pulp flow rate Pulp flow rate - Minimum % Solids by mass Lime addition Slurry pH D80 feed Column Diameter Column Height Column Effective Volume No. of Columns Wash water addition method Wash water volume Pulp residence time Carrying Capacity Air Volume - Normal Pressure - Normal Temperature - Normal Conc grade

Weight floated % of moly plant feed Concentrate rate - solids only Concentrate % solids Concentrate D80 microns Concentrate solids S.G.

min t/h t/h

µm

0 17.0 12.5 86 58 17.2 No 11 30

m m

2.6 10.0

3

m /h 3 m /h % Yes/No

m -

3

26.0 128 16 - 20

39.8 1

F D D D D D/F D/F F C

C 1 1 1 1 1 1 1 1

| | | | | | | |

I I D/I D/I

1 1 1 1

| | | |

drip pans 18.9

20.0

I D

1 1

| |

28 1.3

19 2.1

D D/I

1 1

| |

C

190 580 20

I I F

0 0 A

% Mo % Cu

12.96 2.20

C/D C/D

1 1

| |

% t/h % µm -

7.3 7.1 25.0 30 4.43

D D D/F C F/D

1 1 1 A C

| | |

type 3

m /h min 2

t/h/m /cell

3

Nm /h kPag o


4.8 - 9.6 5.3 - 10.9 23 - 27 30 - 50

36 of 64




5:02


Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


rd

3 Cleaner



min t/h t/h

µm

0 10.3 7.6 57 38 15.8 No 11 30


C 1 1 1 1 1 1 1 1

| | | | | | | |

m m

2.0 10.0 23.6 1

I I D/I D/I

1 1 1 1

| | | |

drip pans 17.6

20.0

I D

1 1

| |

25 1.3

16 2.0

D D/I

1 1

| |

C

113 580 20

I I F

0 0 A

% Mo % Cu

22.24 1.62

C/D C/D

1 1

| |

% t/h % µm -

4.3 4.2 25.0 30 4.46

D D D/F C F/D

1 1 1 A C

| | | | |

3


m -

3

type 3

m /h min 2

t/h/m /cell

3

Nm /h kPag o


15.7 87 15.0 - 18.5

3.5 - 5.5 3.1 - 6.4 23 - 27 30 - 50

37 of 64




5:02


Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


th

4 Cleaner



min t/h t/h

µm

0 5.8 4.3 32 21 15.9 No 11 30


C 1 1 1 1 1 1 1 1

| | | | | | | |

m m

1.6 10.0 15.1 1

I I D/I D/I

1 1 1 1

| | | |

drip pans 9.3

12.0

I D

1 1

| |

28 1.3

19 2.0

D D/I

1 1

| |

C

72 580 20

I I F

0 0 A

% Mo % Cu

32.90 1.16

C/D C/D

1 1

| |

% t/h % µm -

2.7 2.7 25.0 30 4.58

D D D/F C F/D

1 1 1 A C

| | |

3


m -

3

type 3

m /h min 2

t/h/m /cell

3

Nm /h kPag o


8.9 47 15.0 - 17.3

1.8 - 3.3 2.0 - 4.1 23 - 27 30 - 50

38 of 64




5:02


Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


th

5 Cleaner



min t/h t/h

µm

0 3.9 2.9 23 16 15.2 No 11 30


C 1 1 1 1 1 1 1 1

| | | | | | | |

m m

1.6 10.0 15.1 1

I I D/I D/I

1 1 1 1

| | | |

drip pans 2.0

12.0

I D

1 1

| |

40 1.2

25 1.8

D D/I

1 1

| |

C

72 580 20

I I F

0 0 A

% Mo % Cu

36.10 0.88

C/D C/D

1 1

| |

% t/h % µm -

2.4 2.3 25.0 30 4.58

D D D/F C F/D

1 1 1 A C

| | |

3


m -

3

type 3

m /h min 2

t/h/m /cell

3

Nm /h kPag o


6.0 36 14.0 - 18.0

1.4 - 3.0 1.7 - 3.6 23 - 27 30 - 50

39 of 64




5:02


Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


th

6 Cleaner



min t/h t/h

µm

0 2.3 1.7 9 6 22.0 No 11 30


C 1 1 1 1 1 1 1 1

| | | | | | | |

m m

1.0 10.0 5.9 1

I I D/I D/I

1 1 1 1

| | | |

drip pans 7.6

12.0

I D

1 1

| |

40 1.4

31 2.0

D D/I

1 1

| |

C

28 580 20

I I F

0 0 A

% Mo % Cu

55.00 0.50

C/D C/D

1 1

| |

% t/h % µm -

1.1 1.1 25.0 30 4.60

D D D/F C F/D

1 1 1 C C

| | | | |

3


m -

3

type 3

m /h min 2

t/h/m /cell

3

Nm /h kPag o


3.6 12 21 - 25

0.8 - 1.3 0.8 - 1.6 23 - 27 30 - 50

40 of 64




5:02


Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


Cleaner-Scavenger

Conditioning time Feed rate Feed rate - Minimum Pulp flow rate Pulp flow rate - Minimum % Solids by mass Lime addition Slurry pH D80 feed Cell type Cell Volume Effective Cell volume No of rows of cells No. of cells/row Pulp residence time Froth factor for concentrate design Conc grade

Weight floated % of moly plant feed Concentrate rate - solids only Concentrate % solids Concentrate P80 microns Concentrate solids S.G.

min t/h t/h


A 1 1 1 1 1 1 1 1

| | | | | | | |

m /cell 3 m /cell min -

Mechanical 4.25 3.61 1 7 18 2.8

C,D D/I D/I D/F D/F D/F F

1 1 1 1 1 1 1

| | | | | | |

% Mo % Cu

2.00 4.00

C/D C/D

1 1

| |

% t/h % µm _

1.5 1.5 20 30 4.08

D D F,D C F/D

1 1 1 A C

| | |

3

m /h 3 m /h % Yes/No µm

3

0 9.9 7.3 83 55 10.9 No 11 30


15.1 124 9.5 - 13.5

0.8 - 2.3 1.1 - 2.3 18 - 22 30 - 50

Nominal

41 of 64




5:02


Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


st

Thickening - 1 Cleaner Concentrate

No. of thickeners Thickener diameter Thickener feed rate Thickener feed rate - Minimum Diluted feed % Solids Underflow % Solids Specific Area (design) Regrind

No. of Mills Availability Mill type Mill motor Mill Feed Location

m t/h t/h % %

1 15.0 10.9 8.1 14.5 35.0

m2/t solids/day

0.44

A F 16.7

D D D F D

For Future

_ % type kW -

New feed rate total % of plant feed New feed rate total t/h Pulp percent solids by mass % Feed size - P80 µm Product size - P80 µm Ball load average % Load Maximum ball size mm Estimated ball consumption kg/t ore Solids S.G. _ % Vertical mill grinding efficiency improvement

1

I G K

93 vertical stirred media mill TBD

Bottom

C A C 1 1 1 1 1

TBD

1 1 1 1 1 A A A 1 A

pH

10.5-11.0

C

A

Specific power consumption Sizing basis

kWh/t _

TBD Power requirement

C K

C A

Liner material Liner wear rate

type kg/t ore

I H

C C

Pulp pH

TBD

TBD

TBD

TBD

TBD

TBD

TBD

TBD

TBD

TBD TBD TBD TBD

magnetic TBD


TBD

Depending on vendor information

| | | | |

0 A C C C A

B/D B/D F C C I I H B I

TBD

Position in circuit changed from Feas Study

NB New circuit feed not cyclone underflow NB Circuit product from regrind cyclones

| | | | |

Depending on vendor information Depending on vendor information Depending on vendor information

|

Depending on vendor information

42 of 64




5:02


Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


Regrinding Mo Circuit Classificati on

For Future

No. cyclone clusters per pump No. installed cyclones per cluster No. cyclones operating Cyclone size, type Cyclone feed rate Cyclone feed rate - Minimum Cyclone feed rate (solids)

m /h 3 m /h t/h

1 TBD TBD TBD TBD TBD TBD

Cyclone feed pulp density Cyclone feed % Solids by mass Cyclone feed D80

t/m3 % µm

TBD TBD TBD

Cyclone underflow pulp density Cyclone underflow % Solids by mass Cyclone overflow pulp density Cyclone overflow % solids by mass Cyclone O/F rate Cyclone o/f P80

t/m %

3

t/m % t/h µm

TBD TBD TBD TBD TBD TBD

_

TBD

kPa

TBD

%

TBD

Solids S.G. Cyclone inlet pressure - Nominal Circulating load Nominal

_ _ _ mm 3

3


TBD TBD TBD

TBD

TBD TBD TBD TBD TBD

TBD

I I I I C C C C C C

0 A 1 1 C 1 1 1 1 1 1 1

| | | | | | | | |

C

1 1 1 1 1 1

| | | | | |

C

1

|

I

1

|

I

1

|

C C C C

43 of 64




5:03

Moly Thickening, Dewatering & Drying

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


Thickening

No. of thickeners

-

0

A

A

m

Pressure Filter 8 12.6

F/I D/I I

1 1 1 1

| | | |

Filter

Type Number of chamber Nominal Size Sizing basis Filtration rate Solids feed rate Solids SG Filter feed flow rate % Solids % Solids - range Moisture in filter cake

2

kg/h/m

2

t/h 3 m /h % % %

130

200

D/I

1

|

1.1 4.60 3.8 23.4

1.6

D D D D F/D F/D

1 1 1 1 1 1

| | | | | |

7

5.3 22 - 28 7-8

Dryer

Type Number Area Scrubber Required Type Solids feed rate Moisture in dried product

m Yes/No _

Holo-Flite 1 19 Yes Wet

kg/h %

1077 max

2

F/I D D/I D D 1640 3.0

D A

|

1 A 1 Area to be determined A A

|

|

1 0

1 Denver-Sala Handbook 1 1 1

| | | | |

1

| |

Concentrate Storage

Moly concentrate bulk density Storage volume Storage capacity Discharge control

3

t/m 3 m h

1.92 15.0 26.0 rotary valve

2.0 18

E D D I

Concentrate Packaging

Container type

drums or bulk bags


G

44 of 64





5:04

|

Reagents - NaHS

C-DC-25-901 HPGR Rev. D K. Wood

Units

Date:

15-Mar-04

Rev

A

Date:

27-Jan-06

Rev

1

Nominal

Design*

Source

Rev


Sodium Hydros ulfid e NaHS

Total Addition Consumption Mo Conditioning Tank st Mo 1 Cleaner Conditioning Tank Final Cleaner Flotation Annual (Dry Basis) Distribution Strength Density @ 40% Flow rate to process Mo Conditioning Tank st Mo 1 Cleaner Conditionin Final Cleaner Flotation Total Type 1 Shipping container Shipping Size Storage type Tank Storage Volume Number of Trucks - Storage Volume Equivalent Storage capacity Storage requirements Concentrated NaHS storage Operating temperature Min/Max temperature

g/t Conc g/t Conc g/t Conc g/t Conc t % 3

t/m L/min L/min L/min L/min

C/A D D D D I D D D D D

C 1 1 1 1 1 1 1 1 1 1

D/A D/A I D D D D G

1 1 1 1 1 1 1 1

| | | | | | | |

I I

1 1

| | |

1 1 1 1 1 1 1 1

1.3 1556 490

D/A I I D D D D D D D D D

1 1 1 1

| | | | | | | | | | | |

15

D D

1 1

| |

7,900 4,700 2,400 800 6,262 20 1.28 34 17 6 57

9,203

50 25 8 83

Solution @ 40% Strength type Tanker Truck 3 23 m type Tank 3 120 260 m # 11 d 8 5 Secondary containment o

25-35 C 20-49 C o Note: Minimum temperature increases to 30 C for solution concentration of 45%

Type 2 NaHS Concentration Flake Bag Size Solution produced per bag Mix tank (2.0 x 2.5 m) Bags to fill tank Bags per batch NaHS solution produced per batch Water addition per batch Retention Time Consumption for 14 days NaHS Flakes storage for 14 days Distribution Tank Capacity (4.7 x 4.7 m) Distribution Tank Retention Time

o

% t m3 m3 bags bags m3 m3 h m3 t m3 h

Flakes 72 1 3.3 7 2.0 2 6.60 5.2 1.9 1069

73 21


| | | | | | | | | |

Dry basis

45 of 64





5:05

Reagents - Moly Plant


Units Defoamer

Density Flow rate to Mo Conditioning Tank st Flow rate to Mo 1 Cleaner Conditioning Tank Total flow rate Shipping container Tank storage volume Number of isotainers - storage vol. equivalent Diluted storage capacity Storage requirements

15-Mar-04

Rev

A

Date:

27-Jan-06

Rev

1

Nominal

Design*

Source

g/t g/t g/t t % t/m3 L/min L/min L/min type 3

m # d

TBA 95 61 156 124 Liquid 100 0.85 0.18 0.12 0.30

Rev

1

FUTURE

Type Addition to Mo Conditioning Tank st Addition to Mo 1 Cleaner Conditioning Tank Total Addition Annual Appearance Distribution Strength

Date:

K C/K C/K 180

0.26 0.17 0.43

Isotainer 3.5 3 9

D G G I/K D/K D/K


|

C C C

C C C C

H/K

6

D/K

Secondary containment

G

cst cc/min type

MOLYFLO 2.5 2.0 Liquid 100 0.92 4.58 4.10 Drums

A C/D D G G I I D I

d m3 #

34 0.2 1

C 0

Moly Collector

Type st Addition to Mo 1 Cleaner Conditioning Tank Total annual addition Appearance Distribution Strength Density Viscosity @ 21 oC st Flow rate to Mo 1 Cleaner Conditioning Tank Shipping container Storage capacity Tank Storage Volume Number of drums - storage vol. equivalent Storage requirements

g/t t %

Flow rate to Mo Conditioning Tank st Flow rate to Mo 1 Cleaner Conditioning Tank Total flow rate Tank storage volume Number of trucks - storage vol. equivalent Storage capacity Storage requirements

6.0 23

Secondary containment

Sodium Sili cate (Na2SiO 3)

Type st Addition to Mo 1 Cleaner Conditioning Tank nd th Addition to Mo 2 to 6 Cleaner Columns Total Addition Annual Appearance Density Distribution Strength

2.9

D D D G

FUTURE

g/t g/t g/t t t/m3 % L/min L/min L/min m3 # d

TBD 900 700 1600 1269 Liquid 1.40 20 6.88 5.35 12.24 34 1.5

K C/K C/K 1851

10 8 18

13 9 Secondary containment


D G I/K G D/K D/K D/K H/K D/K G

1 1 1 A A 1 1 1 1 1 1 1 0

| | |

1

|

| | | | | | |

C C C C C C C C C C C C 0

46 of 64




6:01

Copper Concentrate Thickening

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


Concentrate production rate Concentrate production rate - Minimum Concentrate % Solids Thickener feed % Solids Pulp flow rate Slurry pH Solids less than 100µm Solids size P80% passing Solids size P50% passing Solids SG No. of thickeners Thickener type Thickener diameter Rake Drive type Rake lift type Final U/F conc. % solids Specific area Hydraulic loading Concentrate flocculant addition

t/h t/h % % m3/h

96 74 43.7 32.5 224 10.0 - 11.0

% µm µm

99 30 15 4.0

_ _ type m type type % m2/t solids/day m3/m2/h g/t

142

31 - 35 150 - 300

3.9 - 4.1

1 high capacity 20 center Automatic/Hydraulic 64 60 - 70 0.099 0.67 9.6


|

C/D C C/D C/D C/D C

1 C 1 1 1 A

C C C B/D

A A A 1

|

B G C

A C C A A A 1 1 1

| | |

B C D C

| | |

Includes filtrate return

47 of 64

Sociedad Min era Cerr o Verde S.A.A. Primary Sulfide Project Project No PSP108



6:02

Concentrate Slurry Stor age and Dewatering

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


Concentrate slurry storage

Concentrate percent solids by mass Concentrate pulp density Solids SG Storage tank diameter Storage tank height No. of tanks Volume (total live capacity) Capacity (total) Capacity (total) - minimum Storage tank agitation intensity

% t/m3 m m 3

m h h 3 kW/m

63.2 1.90 4.00 11.0 11.0 2 1,900 24 16 Full solids suspension

D D D D D B D D G

1 1 1 A A A A 1 C A

F D B I I C I B F

A C C 1 1 A 1 A A

F F F F

TBC TBC TBC TBC TBC TBC TBC TBC TBC

| | | | | | | | | | |

TBC

|

| | |

| Maximum slurry flow, 115 m3/h

Filter

Type Total filtration capacity required Solids feed rate (average) Solids feed rate--(instantaneous) Slurry feed pressure Solids size P80% passing Membrane press required pressure Moisture in filter cake Number of filters Sizing basis @ 600 690 kPa feed pressure Cake thickness Filtration area per filter Number of filter plates per filter Cake volume per filter Filter cloth type Cake form time Pressing time Air blow time Total cycle time Cloth Washwater requirements Filter feed flow rate maximum

Pressure, Horizontal plate t/d solids t/h t/h kPag µm

kPag %

mm m2 # 3 m type min min min min m3/cycle/filter 3

m /h

2,150 96 600 30 1400 9 2

3,200 141 238

48 144 24 6.5 polypropylene 2 1 2.5 10.5 0.61

D/F I D/F D/F I

1 1 1 1 1 1 1 1 1 1

522

I

1


To be confirmed whether vertical or horizontal

|

| | |

48 of 64




6:03

Concentrate Dry Storage and Loading

Initial Revision


Dat e:

15-Mar-04

Rev

A

Last Revision

P Rosario

Dat e:

27-Jan-06

Rev

1

Un i t s

Concentrate production rate Concentrate production rate Concentrate production rate Concentrate pr production ra rate - Annual

No m i n al

Ref er en c e * If different than the nominal Design based on peak production

| | | |

1 .8 2 .2

C C

A A

% % %

8 9 10 4.00

G K K

A A A C

Angle of repose

degrees

37

G

A

Chute reclaim angle

degrees

60

G

A

t t

3,600 20,000

D D

1 1

| |

G

1

|

Each load, before leaving site Each load, before leaving site

G G

A A

t /h

500

K

A

%

TBD

%

10.00

Covered Concentrate stockpile capacity Working capacity, covered Secondary handling, uncovered Concentrate handling method

t/m3 t/m3

Front end loader, conveyor to pots on tru

Shipment sampling required Shipment weighing required Reclaim rate - instantaneous Flow Moisture (FM) Average Transportable Moisture (FM x 90%) Maximum

142 2,812 3,100

Rev

1 1 1 1

Moisture content Minimum Average Maximum Solids S.G.

96 2,148 2,360 784,000

So u r c e

D D D D

Bulk density (wet) volume calcs Bulk density (wet) wt calcs

t/h dry t/d wet t/d dry t/t/a

Des i g n *


Years 1-10 average Years 1-10 average Years 1-10 average J&J tests

Depends on FM

7 min/truck loading rate

A K

1

Assumed

49 of 64

Sociedad Minera Cerro Verde S.A.A. S.A.A. Primary Sulfide Project Project No PSP108



7:01

Tailing Thickening

Initial Revision

C-DC-25-901 C-DC-25-901 HPGR Rev. D

Dat e:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Dat e:

27-Jan-06

Rev

1

Un i t s

No m i n al

Des i g n *

So u r c e

Rev

Ref er en c e * If different than the nominal

Tailing production rate Tailing production rate - Minimum % Solids Pulp flow rate Slurry pH

t /h t /h % 3

m /h

Solids less than 100 µm Solids size P80% passing Solids size P50% passing Solids SG

% µm µm _

No. of thickeners Thickener diameter

_ m

Rake Drive type Rake lift type Thickener feed rate Final U/F % solids Thickener type Specific area (design) Hydraulic loading (design) Tailing flocculant addition

type type t/h % 2

m /t solids/day m3/m2/h g/t

4,746 3,300 27.1 14,532 10.0 73 119 53 2.73

5,250 26-30 16,040

2.74

2 75 center Automatic/Hydraulic Automatic/Hydraulic Cable 2,373 2,630 55 50 - 60 High Capacity 0.072 1.1 15.6


D C D D C

1 C 1 1 A

C C C B/D

C C C 1

B D/I

A 1 A 1 1 A C C C

D B G C D C/D

| Minimum rate, 1 mill line down.

| |

DML LC testing, Sep04 DML LC testing, Sep04 DML LC testing, Sep04

|

Basis max feed rate, specific area

|

Per unit

| |

Vendor settling test results

|

1

50 of 64





8:01

Tailing Collection & Disposal

C-DC-25-901 HPGR Rev. D A Gun so n

Un i t s

Dat e:

15-Mar-04

Rev

A

Dat e:

27-Jan-06

Rev

1

No m i n al

Des i g n *

So u r c e

Rev

Ref er en c e * If different than the nominal

Tailing Transport specification

Tailing production rate Tailing production rate - Minimum Solids SG % Solids Pulp Density Pulp density - Minimum Pulp flow rate Pulp flow rate - Minimum Slurry pH Solids less than 100 µm* Solids size P80% passing* Solids % passing 150 µm (100 #)* Solids % passing 75 µm (200 #)* Solids % passing 38 µm (400 #)*

t/h

% 3

t/m t/m3 3 m /h 3 m /h

4,746 4,400 2.73 55 1.53 1.46 5,630 5,210 9.0-10.5

5,250

50 - 60 1.61 6,220

% µm % % %

74 134 82.5 67.5 52.9

3

3,518

3,910

1.33 39.0 875

37 - 41 1,100

D D D D D D D D C

1 1 1 1 1 1 1 1 1

C C C C C

1 1 1 1 1

D D D

1 1 1

C C

1 1

D D

1 1 1

Design based on Max tons & Ave % solids Minimum based on Min tons & Ave % solid

| | | | | | | | | | | | | |

Dawson/URS Dawson/URS Dawson/URS Dawson/URS Dawson/URS

1st Stage Tailing Cycloning Specification

Cyclone feed dilution volume Cyclone feed pulp density - average Cyclone feed % Solids by mass Cyclowash volume Cyclone feed D80 Cyclone feed D50 Cyclone feed rate Cyclone feed rate - minimum Cyclone Feed Pressure

m /h t/m3 % 3 m /h µm µm 3

m /h 3 m /h kPa

119 53 9,148 8,480 200

10,160

| | | | | | Nott inc No inclu lude ded d cy cycl clow owas ash h vo volu lume me

|

*Size distribution data is from the URS tailing dam feasibility report.


| | |

51 of 64

Sociedad Minera Cerro Verde S.A.A. Primary Sulfide Project Feasibility Study Project No PSP108




8:01

Tailing Collection & Disposal

C-DC-25-901 HPGR Rev. D A Gun so n

Units

Date:

15-Mar-04

Rev

A

Date:

27-Jan-06

Rev

1

Nominal

Design*

Source

Rev * If different than the nominal

2nd Stage Tailing Cyclo ning Specifi cation

Cyclone feed dilution volume Cyclone feed pulp density - average Cyclone feed % Solids by mass Cyclone feed rate Cyclone feed rate - minimum Cyclone Feed Pressure

3

m /h 3 t/m % m3/h 3 m /h kPa

3,474

% % % t/m3 % % µm % %

33.8 90 33.8 1.80 70.0 65-72 275 48.3 12

1.24 30 5,033 4,660 124

3,860 28-32 5,590

D D D D D D

1 1 1 1 1 1

I/D J J B/D I C J J J

1 1 1 1 1 A 0 0 1

| | | | | |

2nd Stage Cyclone underflow (desired product)

Mass recovery to underflow, % of 1st Stage Feed Assumed cyclone station utilization Required recovery to underflow, net Cyclone underflow pulp density Cyclone underflow % Solids by mass - Design Cyclone underflow % Solids by mass - range Solids size P80 % passing Solids % passing 150 microns (100 #) Solids % passing 75 microns (200 #)


90 34

<=15

Krebs 137&138-Nom MWH Design Criteria MWH Design Criteria 18Nov04 Telecon

Krebs Krebs MWH Design Criteria URS Final feasibility

52 of 64

| | | |

| | |



Process Design Criteria Section: Initial Revision Last Revision

8:02

|

Tailing Embankment Dam & Seepage Collection

C-DC-25-901 HPGR Rev. D A.Gun so n

Units

Date:

15-Mar-04

Date:

27-Jan-06

Nominal

Design*

Rev

A

Rev

1

Source

Rev

Reference

* If different than the nominal

Tailing starter embankment dam

Base elevation Crest elevation Crest width Water storage volume for start-up

| m m m m3

2,400 2,480 15 1,000,000

J J J J

A 0 0 1

2,400 2,660 50 2,500 1.30 1.58

J J J J J J

A A 0 0 1 1

J/D J J J/D

1 A A 1

J/D J/D

1 1

Subject to Review Board Approval

Basis MWH water bal.

|

MWH Vol. 5 Fig 2-1

| |

Tailing dam embankment

Base elevation Final crest elevation Final crest width Final crest length Consolidated tails tailing bulk density - dry basis Compacted dry density of underflow

m m m m t/m3 t/m3

MWH Design Criteria

Tailing seepage collection and pu mping

Seepage volume design Seepage pond volume Seepage pond residence time Seepage pond return pump capacity

m3/h m3 day 3

m /h

810 100,000 5.1 810

870 4.8 1,305

| | | |

Tailing water collection and pumpin g

Tailing pond reclaim water Tailing pond water pump capacity Number of pumps Reclaim distribution water to concentrator Number of pumps Central pond barge pump capacity

3

m /h m3/h m3/h m3/h

8,280 10,935 5 1222 3 4140


10,935

3000 7290

A

3op/2sb/1fut

| | |

D D D

1 1 1

| | |

Includes cyclone dilution

53 of 64




9:01

Reagents - Collector

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


Primary Collector

Type Points of addition Grinding/Ball Mill Feed Scavenger flotation 1st Cleaner flotation Final Cleaner flotation Total Annual Appearance Density Make-up concentration Flow rate to process Grinding/Ball Mill Feed Scavenger flotation 1st Cleaner flotation Final Cleaner flotation Total Shipping and handling shipping container shipping volume Storage capacity Tank Storage Volume Storage requirements Number of Trucks - Storage Vol.Equivalent

C

1

C C C C

1 1 1 1

D I I D

C 1 1 1

0.78 0.29 TBD TBD 1.072

D D D D D

1 1 1 1 1

32

G G/D D

1 1 1 C 0 C

thionocarbamate g/t g/t g/t g/t g/t t t/m3 %

8.8 3.3 TBD TBD 12.1 477 Liquid 1.01 100

L/min L/min L/min L/min L/min

0.704 0.264 TBD TBD 0.97

type

Tanker Truck 23 36

3

m d

3

m

#

530

48 Secondary containment 2

D G

Primary collector is Cytec 5415

|

FUTURE FUTURE

| | | |

| | | | | | | | | | | |

FUTURE FUTURE

Secondary Collector

Type Points of addition Grinding/Ball Mill Feed Scavenger flotation 1st Cleaner flotation Final Cleaner flotation Total Annual Appearance Density Make-up concentration Flow rate to process Grinding/Ball Mill Feed Scavenger flotation 1st Cleaner flotation Final Cleaner flotation Total Shipping and handling Shipping container Shipping Mass Storage capacity, solution Storage type Storage requirements

Sodium isopropyl xanthate g/t g/t g/t g/t g/t

t/m3 %

2.80 1.30 0.30 TBD 4.40 173 Dry 1.35 10.0

L/min L/min L/min L/min L/min

2.20 1.02 0.24 TBD 3.456

type kg d

Bulk Bags 750 15

type

Tank Secondary containment

t -


TBD 193

2.44 1.14 0.26 TBD 3.84

13

C

1

D D D D

1 1 1 1

D I I D

C 1 1 1

| | |

D D D D D

1 1 1 1 1

| | | | |

G G/D D D

1 1 1 A 0

G

|

Aero343

| | | |

FUTURE

FUTURE

| | |

54 of 64





9:02

Reagents - Froth er / Moly Collector


Units

Date:

15-Mar-04

Rev

A

Date:

27-Jan-06

Rev

1

Nominal

Design*

Source

Rev


Frother

Type Points of addition Rougher Flotation Feed Scavenger Flotation Feed 1st Cleaner Flotation Final cleaner Flotation Total Annual Appearance Make-up concentration Density Flow rate to process Rougher Flotation Feed 1st Cleaner Flotation Final cleaner Flotation Total Shipping and handling shipping container shipping volume Storage capacity Tank Storage Volume Storage requirements Number of Trucks - Storage Vol.Equivalent

Methyl isobutyl carbinol 85%/glycol 15% g/t g/t g/t g/t g/t t % t/m3

6.9 TBD 1.5 1.5 9.9 390 Liquid 100 0.81

L/min L/min L/min L/min

0.69 0.15 0.15 0.99

type

Tanker Truck 23 53

C

1

C/D D C/D C/D C/D D I I/D I

1 1 1 1 1 1 1 1 1

0.76 0.17 0.17 1.10

D D D D

1 1 1 1

| | | |

48

G G/D D

| | |

434

|

Aero70

| | | | | | | | |

FUTURE

70 Secondary containment 3

D G

1 1 1 C 0

MOLYFLO

C

1

|

g/t g/t g/t g/t g/t t % t/m3 cst

18.80 7.20 1.50 TBD 27.50 1084 Liquid 100 0.92

D D D D

1 1 1 1

| | | |

D G G/D I I

1 A 1 1 1

|

L/min L/min L/min L/min

1.65 0.63 0.13 2.41

1.83 0.70 0.15 2.68

D D D D

1 1 1 1

| | | |

type

Tanker Truck 23 21.4

19.2

G G/D D

1 1 1 C 0 C

| | |

3

m d

3

m

#

Moly Collector

Type Points of addition Grinding/Ball Mill Feed Scavenger Flotation 1st Cleaner Flotation Final Cleaner Flotation Total Annual Appearance Make-up concentration Density Viscosity @ 21 oC Flow rate to process Grinding/Ball Mill Feed Scavenger Flotation 1st Cleaner Flotation Total Shipping and handling shipping container shipping volume Storage capacity Tank Storage Volume Storage requirements Number of Trucks - Storage Vol.Equivalent

3

m d

3

1205

4.58

m

70 Secondary containment

#

3


D G

FUTURE

| | |

55 of 64




9:03

Reagents - Floccu lants

Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

P.Rosario

Date:

27-Jan-06

Rev

1

Units

Nominal

Design*

Source

Rev


Flocculant - Concentrate

Type Point of addition Cu Concentrate thickener Annual Appearance Make-up concentration Bulk density Solution S.G. Flow rate to process Cu Concentrate thickener Shipping and handling Shipping container Container Size Storage capacity, live Storage requirements

Anionic

K

0

g/t Conc t

9.6 8

C D

1 1

%

Dry Powder 0.5 0.85 1.0

F D I D

A 1 1 1

| | |

D

1

|

3

t/m

11

Design based on peak production

| |

m3/h

0.18

kg h

Bags 25 4 Secondary containment

H/K H/K D/K G

A A A 0

Anionic

K

A

15.6 603

C D

1 1

| |

F D I D

A 1 1 1

| | |

D

1

H/K H/K G D/K

A A 0

0.27

Flocculant - Tailing

Type Point of addition Nominal total addition rate Nominal Annual Appearance Make-up concentration Bulk density Solution S.G. Flow rate to process, design Shipping and handling shipping container Container Size Storage requirements Storage capacity, live

g/t Tailing t

% 3

t/m

m3/h

kg h

670

Dry Powder 0.5 0.85 1.0 7.4

8.2

Bulk Bags 750 Secondary containment 8


|

per thickener

A

56 of 64




9:04


Initial Revision

K. Wood

Last Revision

|

Reagents - Lime

Units

Date:

15-Mar-04

Rev

A

Date:

27-Jan-06

Rev

1

Nominal

Design*

Source

Rev


Quicklime

Quality (min. CaO) Bulk density Solids S.G. Top Size Delivery method Total dry storage capacity Total dry storage capacity Consumption Total Ball Mill Grinding Flotation Daily Daily Daily Daily Annual Make-up pulp density Slurry S.G. Flow rate to process Ball Mill Grinding Flotation Slaking system Preparation schedule Total slaked lime storage capacity Total slaked lime storage capacity Storage requirements

% 3

t/m

mm

80 0.85 3.15 15 Pneumatic tanker

d

5.5

t

500

g/t g/t g/t t

1,000 910 90 108

t t t t % solids

120

128.4 142.7 82 91 102.2 113.5 37,294 41,438 15 1.1 3 31.9 35.4 m /h 3 3.1 3.5 m /h h/d 18 24 h 10 416 m3 Secondary containment


|

L/I K K K D D D C/A C/D C/D

1 A A A 1 1 1 C 1 1

CaO Ca(OH)2 Ca(OH)2 Ca(OH)2

D

1

Ca(OH)2

D D D D F D D D G D D G

1

Ca(OH)2 + CaO(NR)

1 1 1

CaO CaO at 80% CaO at 80%

| | |

A A 1 1 1 1 1 0

| | | | | | |

| | | | |

57 of 64




9:05

|

Process/Fresh Water Systems

Initial Revision


Date:

15-Mar-04

Last Revision

A.Gunson

Date:

27-Jan-06

Units

Nominal

Design*

A

Rev Rev

1

Source

Rev * If different than the nominal

A - Ri o Chi li Pumping Sys tem

A.1 Existing Rio Chili Intake system (Pump station No.1 A) Flow rate Number of pumps

360 3

792

1 A

m³/h m

2,880 5 40.5

3,600

1 1 1

m³/h -

3,017 2

3,600

1 A

m³/h m

3,050 3 32

3,600

1 1

m³/h -

3,048 13

3,600

m³/h -

Tested max capacity of 220 l/s

| |

A.2 New Rio Chili Intake system (Pump station No.1) Flow rate Number of pumps Discharge head, design

5 operating, 1 future

| | |

Existing settling basins feed filter banks

|

2 operating / 1 standby

| | |

A.3 Existing Rio Chili settling basins Flow rate Number of basins

A.4 Rio Chili filter system pumps Flow rate Number of pumps Discharge head, design

A.5 Rio Chili filter system Flow rate Number of filters

A.6 Existing Rio Chili 1st stage booster system (Pump station No.2) Flow rate Number of pumps Revised discharge point

m³/h -

1 1

| | |

13 operating

Change discharge point to new stage 3 feed tank

360 360 3 New pump station 3 A feed tank

|

1 A A

|

A.7 New Rio Chili 1st stage booster system (Pump station No.2 A) Flow rate Number of pumps Discharge head, design

m³/h m

2,688 5 395.5

3,240

1 1 1

| | | |

5 operating

A.8 Existing Rio Chili 2nd stage booster system (Pump station No.3) - to be dismantled Flow rate Number of pumps Future status

0 360 m³/h 3 Decommission after new system operational

|

1 A A

A.9 New Rio Chili 2nd stage booster system (Pump station No.3 A) Flow rate Number of pumps Discharge head, design

m³/h m

3,048 5 396.5


3,600

1 1 1

| | | |

5 operating

58 of 64




9.05

|


Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

A.Gunson

Date:

27-Jan-06

Rev

1

Source

Rev

Units

Nominal

Design*

Reference


B - Site Water Storage & Treatment

B.1 Process Water Storage Tank Number of tanks Tank capacity, live Tank dimensions Retention time

m³ m dia. x m h h

2 7,500 25 x 17 1.3

0.9

A A A 1

|

(both tanks)

B.2 Fresh and Fire Water Storage Tank Number of tanks Tank capacity, live Tank dimensions Fire water reserve volume, minimum Fire water reserve time, minimum Fresh water volume, live Fresh water demand, nominal Retention time, nominal

m³ m dia. x m m³ min m³ m³/h h

1 8,500 25 x 19 680 120 7,820 3,048 2.6

m³/h m³/h m³/h

2 0/1 340 340 0

m³/d

23.1 1 8 3.12

A 1 1 0 0 1 1 1

| |

Including existing water

| | |

B.3 Fire Water Pumping System Number of pumps Number of pumps operating Capacity per pump Maximum supply Average demand

+ 1 jockey pump

A A A 0 A

B.4 Domestic Water Treatment Plant Plant capacity, per unit No of plants installed Average run time Peak supply, total

h/d m³/h


1 1 1 1

Supply sulfide project only

Vendor

59 of 64

| | | | |




9.05

|


Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

A.Gunson

Date:

27-Jan-06

Rev

1

Source

Rev

Units

Nominal

Design*

C - Fresh Water Users

Reference


C.1 - General Distribution C.1.1 - Hose stations Number operating Demand per station Average total hose demand

m³/h m³/h

1 20 20

C.1.2. - Maintenance shop Demand

m³/h

15

C.1.3. - Miscellaneous Demand

m³/h

Total Nominal fresh water demand (General)

H H

A A A

15

K

A

46

46

D

0

|

m³/h

81

81

D

0

|

m³/h m³/h

4 45.3 181

50.4 201

I I

A 1 1

| |

m³/h

56

91

1

| |

C.2.4 Gland Seal Water and High Pressure Pumping Demand m³/h Number of pumps Number of pumps operating High pressure flow rate m³/h

120 2 1 82

252

169

D/I D D D

1 A A 1

| | | Assumed gravity flow to lower bench |

C.2.5 Reagents and Lime Preparation Demand

m³/h

49

178

I

1

Does not include moly plant

C.2.6 Process Make-up Water Nominal demand

m³/h

1,139

1,800

D

1

Primary Crushing

m³/h

29

42

D/I

1

C.O. Reclaim

m³/h

3

3

D/I

1

@ 89% availability

Secondary and Tertiary Crushing

m³/h

317

354

D/I

1

@ 89% availability

Total Demand

m³/h

349

399

D/I

1

@ mixed availability

m³/h

586

654

I

1

|

m³/h

2.9

3.0

I

1

|

m³/h

360

360

A

1

|

m³/h

123

137

I

1

|

m³/h

3,047

3,600

C.2. Process Consumption C.2.1 - Final Column Wash Water Number of columns Demand per column Total wash water demand

C.2.3. - Molybdenum plant, NaHS, and sodium silicate fresh water Total Demand

| |

C.2.7 Crushing Area Water

| | | |

@ 70% availability

C.2.8 Grinding Water Nominal demand C.2.9 Regrind/Polishing Water Nominal demand C.2.10 Existing SX/EW Operation Nominal demand C.2.11 Plant Air Compressors Nominal demand Total fresh water demand (Process)

1

| |

Adjusted for availability. Design flows not additive


60 of 64




9:05

|


Initial Revision


Date:

15-Mar-04

Rev

A

Last Revision

A.Gunson

Date:

27-Jan-06

Rev

1

Source

Rev

Units

Nominal

Design*

Reference


D - Process Water Users

D.1 - Crushing and Grinding Circuit D.1.1 Tertiary Scrubbers Total Demand

m³/h

295

340

D

1

|

D.1.2 Ball Mill screen feed dilution Total Demand

m³/h

8,605

9,600

D

1

|

D.1.3 Ball Mill Grinding Total Demand

m³/h

2,385

13,600

D

1

|

D.2 - Flotation and Tailings Circuit D.2.1 Rougher cells feed Demand dilution/startup Demand concentrate wash water Total demand (All 4 lines)

m³/h m³/h m³/h

0 1.5 6

500 14.5 1,000

A 1 1

| |

D.2.2 Cleaner/Regrind/Column areas Total Demand

m³/h

10

500

1

|

D.2.3 Tailings Area Flushing/Startup Tailing Flocculant Dilution Tailing Thickener Area Total Demand

m³/h m³/h m³/h

0 0 0

65 1,000 1,000

A A A

D.2.4 Concentrate Area flushing/startup Total Demand

m³/h

0

250

A

D.2.5 Moly Plant Circuit process water Total Demand

m³/h

28

150

1

Including NaHS

|

Total process water demand

m³/h

11,322

17,000

1

Adjusted for availability Design flows not additive

|


61 of 64




9.05

|


Initial Revision


Last Revision

A.Gunson

Date: Date:

Units

Nominal

15-Mar-04 27-Jan-06

Design*

Rev

A

Rev

1

Source

Rev

Reference


E - Net Water con sumers

E.1 Concentrator E.1.1 Final Concentrate Total consumption

m³/h

9.6

14

0

E.1.2 Domestic water consumption Total consumption

m³/h

1.00

2.3

1

|

Total consumption

m³/h

10.6

16

1

|

E.2 Tailing Embankment / Impoundment Dam E.2.1 Evaporative losses Total consumption (net)

E.2.2. Seepage Losses Total recovery flow consumption

m³/h

m³/h

E.2.3. Embankment Dam building entrained water recovery Total flow consumption m³/h

413

413

|

Includes Moly Conc.

| MWH TO CONFIRM ALL | 1 60,00 per month X 1.08 + increase | URS+MWH due to 2 pond impoundment Volume 6, scenario 1, Avg. year 3 evaporation

| |

290

290

MWH

1

Recycled to tailing pond - not lost

|

520

580

MWH

1

Design = Nominal + 11% 15% & 95% Avail

| | |

Recycled with seepage E.2.4. Stored Tailing tailings contained water + foundation losses Total consumption

See note 1

| | | |

Ref. Section D.1

|

m³/h

2,261

2,817

D

1

Design = Nominal + 15% & 95% Avail

m³/h

2,674

3,230

MWH

1

NB. Excludes initial foundation losses

By difference overall - evaporation Total overall tailing consumption

E.3 Other Users Total fresh water demand (General)

m³/h

81

81

D

1

Existing leach - SX/EW

m³/h

360

360

L

Overall consumption

m³/h

3,131

3,693

D

1

Less ore feed moisture Make up water required

m³/h m³/h

84 3,048

93 3,600

D D

1 1

|

1

E.4 Overall

| | Adjusted for availability | Not accounted in MWH water balanc | | Design flows not additive

Note 1: Basis MWH final water balance scenario 1, adjusted from 108,00 t/d to tailing tonnage 105,957 t/d and adjusted for 93% pumping availability on make-up water


| |

62 of 64





9:06

Reagents - Water Treatment

AJ Gu ns on K. Wood

Units

Date:

25-Oct-05

Rev

A

Date:

27-Jan-06

Rev

1

Nominal

Design*

Source

Rev

G

1

J D J D

1 1 1 1

D

1

J J D


An ti -Scal ant

Type Points of addition Recycle water to process water tank Storage capacity

ppm L/h m3 d

Delivery form Annual Consumption

m3

Millsperse 815-5 100% Concentration 1 5 8.9 50 3

2 x 10 m 100 18 Liquid in Isotainers 73 407

| | | | | | | | | | | | | | | | | | | | | | | | | | | | | | | | | | | | | |

Corrosion Inhibitor

Drewgard 120

Type Addition points Secondary/Tertiary crushing cooling water Addition rate Total Consumption Tank Storage Volume Plant air compressor cooling water Addition rate Total Consumption Tank Storage Volume

ppm L/h L/d m3 d ppm L/h L/d 3

100% Concentration 1 5 0.30 1.80 7.1 40 5 700 1 0.1 22

m d

2.5 113

ppm kg/d

Solid 50 1.3

125 5 0.7 19

D D D

130

D D

1 1 1 1 1 1 1 1 1 1

100 11.6

J J J

1 1 1

J J J J

1 1 1 1

J J J

1 1 1

D

Domestic Water Treatment

Aluminum Sulfate type A Form Dosage Consumption Flocculant polymer Form Dosage Consumption Sodium Hypochlorite Form Dosage Consumption

Nalco8173 HMW Cationic polymer dry solid 1 4.5 ppm kg/d 0.03 0.1

13% concentration solution ppm L/d

7


38 31

Page 63 of 64

Criterios de Diseño

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