Cy Tec Solutions 8

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I S S U E 8 A P R I L 2 0 0 3

acorganotesacorga notes

Metal Extract ion Products

(pages 4-6)

Compañía

MineraDisputada DeLas Condespages 2-3

Manufacturing

Qualitypages 7-8

Organizational

Newspage 8

Solvent Extraction of Copperfrom High Concentration

Pressure Acid Leach Liquors

Fifth Annual

TechnicalACORGASeminar inChilepage 9

Aqueous Con-

tinuous: Flexibilityto MaintainProduction withFalling PLS CuGradepages 10-11

Upcoming

Industry Eventspage 12



Compañía Minera Disputada DeLas Condes: A New SX/EW Plant

At The San Francisco DepositGonzal o Al varez Brantes, Techni cal Manager, Avecia Chi le Ltda., Sant iago

Compañía Minera Disputada de

Las Condes harvested its first cathode

on February 27, 2002. This new

Solvent Extraction and Electrowinning

(SX/EW) plant is located only 65 km

Northeast of Santiago, at an altitude of

2,750 meters, and is fed by leaching

the low grade ore from the San

Francisco deposit. With this new plant

Minera Disputada adds 20,000 metrictons/year of cathode production to

the 5,200 tons/year produced by

the El Soldado property and the

11,900 tons/year produced by the

Los Bronces property.

The project feasibility studies

were completed in late 1999 and

engineering and construction began

in early 2000. Engineering design

work was completed by Ingeniería

SX, a group formed by the companies

Bechtel and ARA. Vial and Vives

Construction completed the project

construction work.

The Los Bronces Mine is expected

to generate a total of 1,200 million

metric tons of material from the San

Francisco deposit. Approximately 60%

of the total ore will be leached (720

million tons of low-grade ore at 0.2-

0.7% Cu). Mining is planned for a 25-

year period. Leaching design will pro-

vide 200,000 m3 of area for leaching.

Both the solvent extraction and

the electrowinning plants are unique

from the construction point of view

because they are located in the old Mill

and Concentrator buildings. These

structures have not been in operation

since 1992. The use of the existing

buildings provided a savings of $2.5

million dollars on the construction

project. The location of the SX/EW

processes in the enclosed facilities

also provides protection from the

2



snow during the winter, when operations take place at tem-

peratures well below zero degrees Celsius. A traditional tank

farm is not seen at the Los Bronces plant.

The solvent extraction plant was designed withtwo stages of extraction and one stage of stripping using

traditional mixer settlers. The mixers consist of a primary

pump mixer, with two auxiliary mixers for extraction

stages and one auxiliary mixer for the stripping stage (all

stainless steel). Coalescers are used to reduce any aqueous

entrainment in the loaded organic. Flexibility was included

in the design to allow PLS flows to be fed as either: one

stream, processed through the two extract stages in series;

or, two separate PLS streams to each extract stage, processed

in parallel. Seven 1,000 HP impulsion pumps take the

raffinate up to the leaching area.

The Electrowinning plant, located in the same building,

operates with stainless steel starter sheets and has 66 cells.

Current density is 330 A/m2. To minimize the acid mist in

the tankhouse, Minera Disputada helped develop a system

to capture the acid mist from the EW operation. The SAME

system consists of a hood located over each electrolyte cell.

The hood collects the mist and processes it in a countercur-

rent scrubber with a water shower. The captured acid fromthe mist is then returned to the process.

The start up of the new plant was very smooth.

Several factors contributed to this success. Site staff was

hired early during the engineering and construction stages,

and personnel were selected who had significant experience

in plant operation. This approach allowed members of the

team to be incorporated in the project at the appropriate

time and, at the same time, allowed their participation

in appropriate training courses. One such example was

the SX/EW course given by the members of the Avecia

Santiago office. Minera Disputada’s approach and the

training received by the workers were significantcontributions to the successful start-up of the plant.

waste dump

1150 m3/ hr flow in series operation

(2645 m3/ hr flow in parallel operation)

2.27 gpl Cu; 1.8 – 3.0 pH; 3.6 gpl Fe+++; 42.7 gpl SO4—;

200 mg/ l Cl-; 438 mg/ l Mn; 4.37 gpl Al.

3 - 5.5 °C

90%

1156 m3

/ hr flow~9.0 v/o ACORGA® PT- 5050MD

Escaid 110; 0.5 % of aromatic diluent

2E + 1S (with flexibility to operate as 1E + 1E + 1S)

38 gpl Cu; 156.4 gpl H+; 0.6 gpl Fe+++; 18 mg/ l Cl-;

20 mg/l Mn; 140 mg/ l Co++ at 41 - 49 °C.

1112.5 m3/ hr flow

66

60

61

140 l/ hr per m2

276 - 370 A/ m2

92 %

OPERATIONAL PARAMETERS

Leaching:

PLS:

PLS Temperature:

Recovery Target:

Organic:

Configuration:

Lean Electrolyte:

Lean Electrolyte to Cells:

Number of cells:

Cathodes per cell:

Anodes per cell:

Specific flow to cells:

Current density:

Current efficiency:



4

THE KONKOLA DEEPS EXPANSION PROJECT

Solvent Extraction of Copperfrom High Concentration

Pressure Acid Leach Liquors

Kathryn C. Sole, Anglo American Research Laboratori es (Pty) Ltd, Johannesburg, South Af ri ca

The Konkola Deeps sulphide

deposit in Zambia occurs in the

immediate vicinity of a large surface

oxide deposit known as the Chingola

refractory ore (CRO), as well as sometwo decades’ worth of accumulated

oxide tailings material from the

adjacent Nchanga Tail ings Leach Plant.

Both oxides contain economically

attractive quantities of copper (~1%).

As part of an assessment of various

scenarios associated with the expansion

of the underground mine, a hydromet-

allurgical process route for the

treatment of both the sulphide and

oxide materials was evaluated.

Process Conc ept

In the proposed hydrometallurgical

flow sheet (Figure 1), the sulphide

material was concentrated by flotation

to 40-45% Cu and then subjected to a

high pressure acid leach (HPAL) under

conditions that maximized recovery of

copper and cobalt while rejecting iron

as hematite. The autoclave discharge

contained 60 g/l Cu and 5 g/l H2SO4.

This enabled the pregnant leach

solution (PLS1) to be purified directly

by SX without neutralization. The high

tenor SX1 circuit removed the bulk

of the copper, the extraction of

50 g/l Cu generating a raffinate stream

that contained about 80 g/l H2SO4.

This acid was then used to leach

copper from the CRO. The aggressive

leaching conditions were necessitated

by the substantial amounts of

aluminum, magnesium, and calcium

oxides and carbonates in this material

that consume acid in leaching and

effectively act as an ‘acid sink’. Copper

was recovered from the atmospheric

leach liquor in the low tenor SX2

circuit. Both SX circuits were integrat-

ed with electrowinning to produce a

high-grade copper cathode product.

This flow sheet capitalized on the

synergy that exists between the leach-

ing of the sulphide copper concentrate

(acid producing) and the oxide copper

ore (acid consuming). Copper leachedin the autoclave provided a convenient

way of ‘transferring acid’ from the sul-

phide circuit to the oxide circuit. Key

to the concept was the specification of

a copper SX circuit operating at a high

extraction efficiency of copper (∆Cu =

50 g/l), thereby providing a raffinate

solution of sufficient acid strength to

successfully leach the refractory CRO

minerals. The high tenor SX circuit

(SX1) focused on maximizing the

copper extraction using a high

extractant concentration and a high

flow rate of the organic phase relative

to the aqueous phase (O:A). The low

tenor circuit (SX2) was responsible for

generating a raffinate as low in copper

as possible (<0.5 g/l).

Pilot-Plant Evaluation

The integrated flow sheet waspiloted at AARL during 2000, produc-

ing 24 kg/h cathode copper. The eight-

week campaign treated 27 tons of CRO

and 2.5 tons of Konkola concentrate,

and produced 940 kg of LME A Grade

copper cathode [1, 2].

The HPAL achieved high extrac-

tions of both copper (98.1%) and

cobalt (96.5%) from the concentrate.

The acid tenor of the autoclave dis-

charge liquor averaged 6.5 g/l.

O/ F

O/ FU/ F

Raffinate

Konkola concentrate

U/ F

CRO ore

ResidueCopper cathode

High tenor SX

Thickener

High pressureacid leach

Second-stageatmospheric leach

Thickener

Filtration

CCDLow tenor SX

Copper EW

First-stageatmospheric leach

Figure 1: The hydrom etallurgical flow sheet for the Konko la project.



Figure 2: SX1 solvent-extraction circuit used in the Konkola pilot cam paign.

Although slightly higher than the target value of 5 g/l, this

was still low enough to allow the liquor to be fed directly to

the SX1 circuit. Copper extraction from the CRO material

averaged 77.5%. The acid concentration of the atmospheric

leach liquor was 2.7 g/l. Two extractants were tested during

the campaign. The Avecia extractant tested was ACORGA®

M-5640. The diluent was Shellsol 2325. The operating con-

ditions for the two SX circuits are shown in Table I.

Parameter

Extractant concentration (vol. % )Temperature (ºC)Mixer volume (l)

Settling area (m2

)

32407. 5

0.15

Clarified autoclave d ischarge60 g/ l Cu, 4.2 g/l H2SO 4

4. 950

0. 937 g/ l Cu, 170 g/ l H2SO 4

46 g/ l Cu, 156 g/ l H2SO 4

164012

0.22

Clarified CRO leach liquor5.3 g/ l Cu, 1.6 g/ l H2SO 4

1. 04. 8

1. 837 g/ l Cu, 170 g/ l H2SO 4

45 g/ l Cu, 157 g/ l H2SO 4

Extraction circuitPLSPLS compositionAdvance O: ATarget ∆Cu (g/l)

Strip circuitAdvance O:AStrip liquor (SE)Loaded strip liquor ( AE)

SX1 SX2

Table I: Konkola pilot-plant operating cond itions for the SX circuits.

The SX1 circuit consistentlyobtained the required copper extrac-

tion of 50 g/l. The performance of

the SX2 circuit also exceeded the

specifications; with average raffinate

tenors of 0.25 g/l Cu - well below the

target value of 0.5 g/l. Typical solution

analyses obtained during the campaign

are given in Table II. Although normal

crud formation occurred, no adverse

physical effects on the organic phase

were observed.

Electrowinning of copperfrom the loaded strip liquor

consistently produced LME A Grade

throughout the campaign, with all

cathodes meeting the BSI standard BS

6017:1981 with respect to individual

element impurities.

SX1

CuCoFeAl

MgCaMnZn

59.291.231.221.127.950.651.310.10

15.6< 0.001< 0.001< 0.001< 0.001< 0.001< 0.001

0.001

6.2< 0.001< 0.001< 0.001< 0.001

0.001< 0.001< 0.001

PLS

5.810.611.771.316.830.691.220.05

8.85< 0.001< 0.001< 0.001< 0.001< 0.001< 0.001< 0.001

3.8< 0.001< 0.001< 0.001< 0.001< 0.001< 0.001

0.001

LO SO

Element(g/ l)

SX2

PLS LO SO

Table II: Typical perform ance of SX1 and SX2 circuits during the Konkola piloting cam paign.

“Th e su ccessfu l compl et ion of t he Konkola pi lot plant d em onstr at ed tha t exi st in g ext racta nt s can be used in t hi s

non-trad i t ional appl icat ion wit hout problem s.”



6

CONCLUSIONS

Pressure leaching technologies currently under

development for the treatment of copper sulphide concen-

trates yield leach liquors that can contain in excess of 50 g/l

Cu. The purification of such liquors by SX requires an

integrated flow sheet in which the large quantities of acidproduced by the extraction reaction can be accommodated.

This work demonstrated that extractant concentrations up

to 32 vol.% can achieve copper transfers of >50 g/l in three

stages. Adequate stripping is achieved in two stages with

a conventional composition of the spent electrolytes, and

producing an advance electrolyte from which LME A Grade

copper cathode can be electrowon.

The performance of conventional SX extractants and

circuit configurations for transferring such high amounts of

copper without neutralization had not been documented

previously for continuous trials. The successful completion of

the Konkola pilot plant demonstrated that existing

extractants can be used in this non-traditional application

without problems.

ACKNOWLEDGMENTS

This article is published courtesy of Anglo American

Research Laboratories (Pty) Ltd.

NOTE

This work was carried out in 2000, during whichtime Konkola Copper Mines was jointly owned by Zambian

Consolidated Copper Mines (ZCCM) and Zambian Copper

Investments (ZCI), of which Anglo American plc was the

major shareholder. Anglo American currently holds no

financial interest in KCM.

REFERENCES

1.Whyte, R. M., Schoeman, N., and Bowes, K. G. (2001),

Processing of Konkola copper concentrates and Chingola

refractory ore in a fully integrated hydrometallurgical

pilot plant circuit. Copper, Cobalt, Nickel and Zinc

Recover, South African Institute of Mining and

Metallurgy, Johannesburg, 15 pp.

2.Sole, K. C. (2002), Solvent extraction of copper from

high concentration pressure acid leach liquors,

Proceedings International Solvent Extraction

Conference ISEC 2002, Sole, K. C., Preston, J. S., Cole,

P. M. and Robinson, D. R. (eds.), South African Institute

of Mining and Metallurgy, Johannesburg, pp. 1033-1038.

FOR FURTHER INFORMATION on the work reported or

on the piloting capabilities available at AARL, please contact

Kathy Sole at [email protected] o.za or visit our Web site at

www.aarl.co.za.

Experiment

Model

00

4

8

12

16

20

20 40

[

C u ] o r g

( g / l )

[Cu]aq (g/ l)

60 80

SIMULATIONMODELING

Potential extractant systems that

could achieve the high copper transfers

required for the processing of autoclave

discharge solutions were identified

by simulation modeling, using the

software packages supplied by the

extractant manufacturers (MEUM™from Avecia). A comparison of experi-

mental isotherm data for ACORGA®

M-5774 with the model prediction

shows extremely good agreement

(Figure 1), thereby confirming the

validity of using modeling results for

predictive purposes and the prelimi-

nary selection of extractant composi-

tions and operating conditions.Figure 1. Comparison of experimental data with MEUM model predictions.

Extraction of copper from a synthetic solution (70 g/l Cu, pH 1.6) by 32

vol.% ACORGA M-5774.



A key component to MEP's success is the ability of the

members of our manufacturing facility in Mt. Pleasant, TN toapply Avecia's values to guide their manufacture of the high-

est quality SX reagent available on the market; to work with

customers to meet tight demand schedules, especially in

times of critical need; and to keep a continual focus on SHE

(Safety, Health, and the Environment).

While much of this appears transparent to our

customers, all of these priorities are extremely important

because all these activities around Mt. Pleasant translate

into assurance of supply both in the short term as well

as the long term.

Manufacturing InnovationAvecia's innovative abilities go beyond new product

development. Avecia engineers applied this innovation to

redesign the reagent manufacturing process in 1993. The

improved process not only delivers a high quality reagent, it

also reduces the generation of hazardous waste from the

reagent manufacturing process. The Avecia patented process

reduced organic effluent by up to 85% compared to all other

practiced manufacturing routes. In the Avecia process, it is

also significant to note that the effluent from the process

contains essentially only benign inorganic salts. This

achievement was recognized through the presentation of a

Queen's Award for Environmental Achievement in 1999.

ManufacturingQuality

Mt. Pleasant Acorga Manufacturing Team, Avecia

•Safety, wh ich i s our number 1 objecti ve

•Givi ng signi fi cant val ue to our customers

th rough our products and servi ce

• Being flexible in meeti ng their needs

Avecia is commit ted to: In October 2002 the Mt. Pleasant site received another envi-

ronmental award for demonstrating outstanding achieve-

ment in environmental protection. The award was present-

ed by the Tennessee Association of Business (TAB) in recog-

nition of the site’s hazardous waste management program.

The Mt. Pleasant facility is ISO 9002 certified. But better

than having the procedures in place as directed by these

standards, Avecia has been able to deliver the highest level of

product quality that the ISO certifications hope to enable a

plant to achieve. Avecia is the only Cu SX reagent supplier

to never have a quality rejection of a delivery. The plant has

also never missed a scheduled reagent production delivery

date. This is due to the special efforts Avecia has made to

design the most robust process possible.

Improvements to the manufacture process and proce-

dures continue today with a focus on improving the safety

of the plant; exceeding environmental/regulatory targets;

and maintaining our high product quality while improv-

ing/maintaining plant reliability.

Quality of the People

The plant was commissioned in 1994 with a strong crewof people who brought the original plant on-line at Mt.

Pleasant within a very short time and met many large order

requirements right from the first months of operation.

Many are still working with the process today. This has

brought a lot of continuity to the plant and helped the focus

of the team remain on efforts to continually improve the

process. There is a procedure for every step of the process

ensuring good communication of what is occurring. Every

change is agreed upon and understood by all members of

the team. The supervisors are on call 24 hours per day to

assist if there is ever a problem.

Cont inued on page 8



8

Organizational News

Brian Townson Tony Moore

Safety Program

At Avecia, safety is the number one priority. Avecia

employees are proud of their safety performance – but are

always looking for ways to improve. The Safety Through At

Risk Reduction (STARR) program is used to constantly

improve the safety of the plant. The STARR committee iscomposed of volunteer representatives from functions across

the manufacturing site. They work with members of the site

to observe and evaluate how job tasks are completed. Their

outside observations are used to improve the safety of proce-

dures across the plant.

The Acorga plant has never had a lost time accident

since it began operation at Mt. Pleasant. The last OSHA

recordable injury was in M ay of 1995. Not only does this

provide the safest possible work environment for our

employees, it helps guarantee that the facility will be in the

best condition to produce a quality reagent.

Manufacturing Quality continued

Brian Townson, Regional Manager for Australia and Europe,

retired at the end of 2002. Brian was a long service employee

with ICI, Zeneca, and Avecia and played a major role in

MEP's growth, particularly in Australia and China. Brian

chose to kick back in the UK after many years of successfulinternational business activities.

Tony Moore has been promoted to Manager-Australasia,

effective 12/1/02. In this expanded role, Tony will assume

commercial and technical responsibility for this region.

With the expanded geographic remit, additional technical

support will be provided to supplement Tony's activities.



Avecia Chile Limitada held its fifth

annual Solvent Extraction Technical

Seminar in Iquique, Chile on October 3

and 4, 2002. The two-day seminar

was a remarkable success with much

sharing of invaluable knowledge and

experiences among the SX plant

operators as well as those who work to

support the plants. More than ninetyprofessionals attended the seminar and

their active participation helped make

the seminar a resounding success.

Attendees included professionals

from many different mining compa-

nies, including: C.M . Doña Inés de

Collahuasi; Codelco Norte (Radomiro

Tomic and Chuquicamata); Alliance

Copper; Andina, Salvador; C.M.

Mantos Blancos’ Manto Verde and

Mantos Blancos divisions; Lipesed;

Southern Perú; C.M . Cerro Dominador;

Grupo Milpo Minera RayRock S.A.;

BHP Billiton Escondida and Tintaya

divisions; Grupo Mexico’s Mexicana

de Cobre and Mexicana de Cananea

divisions; and Olympic Dam

from Australia.

In addition to representatives from

mining operations, many organizations

were also represented that support

the mining industry, including:

Kvaerner; Outokumpu; 3M; Oxiquim;

Universidad Técnica Federico Santa

María; Universidad Católica del Norte;

and Universidad Arturo Prat.

Participation in the event further

included authorities such as Mr. Olaff

Olmos, Seremi de Minería Región de

Tarapacá; Mr. Patricio Cartagena,

Executive Vice President of the

Comisión Chilena del Cobre; GIEC

President (International Group for

Copper studies) and Jorge Cristi,

Copper Sales Manager for North

America, Trading and Futures

Markets-Codelco Chile.

In addition to the strong technical

program of presentations from the

various operations, social and cultural

activities were also included. Attendees

enjoyed a dinner and performance of

the Artistic Folk Group from the City

Hall Theater. Attendees toured the

Iquique Port during which Mr. Osvaldo

Castro – Avecia Chile Ltda. and Mr.

Manuel Neira – BHP Billiton Tintaya,

made a presentation of flowers at the

Naval memorial.

Fifth Annual TechnicalACORGA Seminar in Chile



0

Keith Cramer, Techni cal Special ist, M etal Extraction Products, Phoeni x

Troy Bednarski, Techni cal Special ist, M etal Extraction Products, Phoeni x

Aqueous Continuous: Flexibilityto Maintain Production with

Falling PLS Cu Grade

Without question, phase continuity is an important

consideration in the operation of a copper solvent

extraction circuit. Traditionally, conventional circuit

configurations with flows at or close to design are operated

with the E1 stage aqueous continuous and all other stages

organic continuous. Under design conditions, there are

benefits to operating with these continuities. But imposing

strict rules on stage mixer continuities can constrain howa plant reacts to changing solution conditions, possibly

limiting a plants production capacity and increasing its

operating costs. Running additional extract stages aqueous

continuous can have significant metallurgical benefits that

can reduce an SX plant’s overall operating costs.

Plant Operation Options

In a mature market such as North America, copper ore

grades have fallen steadily over the years at many sites. In

most cases the result of this is a reduction in the copper

concentration in the PLS. In order to maintain production,

increased flow through the leach circuit and solvent

extraction plant is required.

There are many ways that the increased PLS flow can

be processed in the plant depending on both plant capacity

and operational philosophy. One way to categorize these

options is to look at how the resulting mixer continuities

will be affected. Some options are presented below for a

series-parallel circuit that either 1) utilize aqueous continu-ous operation in additional extract stages, or 2) maintain tra-

ditional continuities.

Additional options with flexible mixer

continuity requirements.

• Increase PLS flow to series portion of circuit, with E1S

and E2S extract O:A ratios less than 1:1 (aqueous

continuous). (option 1)

• Increase PLS flow to both series and parallel portions of

the circuit equally, both flows above the organic flow

rate. All extracts operate at an O:A ratio less than 1:1

(aqueous continuous). (option 2)

5000

Option 1: Series-parallel, higher flow to series

9000 9000 6000 6000

organic (6000)

E1S E2S

11.0%

Parallel E1S E2S Parallel

E1S E2S Parallel

E1S E2S Parallel

Option 2: Series-parallel, balanced PLS flow

7500 7500 7500 7500

organic (6000)

E1S E2S Parallel

E1S E2S Parallel

Option 3: Extra PLS flow added directly to E2S m ixer

6000 9000 60003000 6000

organic (6000)

PLS

Raffinate

Organic

Option 4: Series-parallel, higher PLS flow to parallel

6000 6000 9000 9000

organic (6000)

Option 5: Extra PLS flow to E1S, then bypassed d irectly to raffinate

9000 60003000 6000 6000

organic (6000)

Option 6: 3 -parallel PLS streams

5000 5000 50005000 5000

organic (6000)

11.3%

11.5%

11.7%

12.5%

14.3%

Metallurgical Comparison of Flow Distribution Optionsv/ o Required for 90% Recovery

* PLS grade 1 .5 gp l Cu; 6,00 0 gp m m aximum organic flow rate;

series-parallel circuit; 15,000 gpm PLS flow



• Add extra PLS flow directly to the E2S mixer (if E1S-E2S

advance line is at capacity). (option 3)

• Add extra PLS flow to the parallel stage, operating

at an extract O:A ratio less than 1:1 (aqueous

continuous). (option 4)

Options that maintain traditional continuities.

• Increase organic flow and/or organic recycle to maintain

mixer O:A ratios above 1:1. (Maximum PLS flow limited

by organic flow capacity.)

• Increase PLS flow to E1S stage but bypass the “extra”

flow directly to the raffinate pond rather than

advancing it to E2S. (see table, option 5)

• Operate with 3 parallel PLS feed streams. (option 6)

There are options available to maintain traditional

mixer continuities at increased PLS flow rates, but they

have lower limits to the maximum PLS flow and generally

have higher operational costs. The increased operational

costs come from higher reagent concentrations and higher

chemical transfer of Fe (lower Cu loading). The best

metallurgical and economic options typically involverunning additional extract stages aqueous continuous.

The actual “best” configuration and PLS flow limits

will be a little different for each plant based on its specific

PLS grade and physical flow capacities. In many situations,

the best metallurgical performance is obtained when more

PLS flow is processed through the series portion of the

circuit, generally requiring that the E2S stage run aqueous

continuous (rather than using a higher organic recycle

flow). The unbalanced PLS flow distribution is preferential

metallurgically even under “normal” flow conditions.

(see below).

Of course all plants cannot just push flows higher

without any consequences. Due to physical performanceconstraints, some plants need to run under all-parallel

flow conditions with traditional continuities. But this

is the exception rather than the rule. Cu production

does not necessarily need to be sacrificed due to concerns

about the physical capabilities of the reagent in the plant.

Can this be done in a com m ercial plant?

ACORGA® reagents used in plants today give the

needed operational flexibility to cope with demanding

conditions. It has been repeatedly shown that when a

plant seems to be “pushing the limit” of flow there is

actually more room to give. All of the circuits discussed

above have been, or are currently in use at large commercial

SX operations.

Yes, really, shift the PLS flow to the series not parallel stage.

0.00 0 . 0

0

2 . 0

0

4 . 0

0

6 . 0

0

8 . 0

0

0.38 0.75

Copper in Aqueous phase

Higher PLS flowto series extraction stages

C o p p e r i n O r g a n i c p h a s e

1.13 1.50

Extraction section

0.00 0 . 0

0

2 . 0

0

4 . 0

0

6 . 0

0

8 . 0

0

0.38 0.75

Copper in Aqueous phase

Higher PLS flowto parallel stages

C o p p e r i n O r g a n i c p h a s e

1.13 1.50

Extraction section

Typically in a series-parallel circuit, the recovery of the

parallel stream does not drop very much if you increase the

flow to this stage. Consequently the tendency is to put any

additional PLS flow into the parallel stage. The Cu recovery

is actually higher if you do the opposite – increase the

PLS flow to the series portion of the circuit. (see diagram

options 1 and 4)

When more PLS flow is directed to the series portion of

the circuit, less is directed to the parallel. The Cu recovery

for the parallel stream increases at the new higher O:A

ratio, but this is not where the biggest benefit comes from.

Because of the higher O:A ratio in the parallel stage, the Cu

concentration of the organic that advances to the E2S stage

is lower. The lower Cu loading entering the E2S stage allows

the series portion of the circuit to also achieve a higher

Cu recovery. The overall performance for the train is better.

The McCabe-Thiele diagrams below illustrate the effect of

changing the extract O:A ratios.



COPYRIGHT© 4/ 03 Avecia Inc.

All rights reserved.

Printed in U.S.A.

Acorga is a trademark, the property of Avecia, Ltd.,

an Avecia Group Company.

MINCHEM and MEUM are trademarks of Avecia, Ltd.

Acorga Notes will be published approximately twice per year for

the international mining industry. Editorial content will include:

industry news; information on progress particularly in hydromet

technology; relevant scientific articles; and news on the Metal

Extraction Products Business (MEP) of Avecia Inc.

Editor: Keith Cramer

Coordinator: Valerie Calvarese

Design/Layout: Creative Marketing Group, Inc.

Please direct any questions, comments, or requests for corrections

or changes to the distribution list to Valerie Calvarese:

Phone (U.S.) 1-800-435-8679 - Ext. 8113

Phone (Direct): 1-302-477-8113email: [email protected]

Business Headqua rters

Avecia Inc.

Metal Extraction Products

1405 Foulk Road

P.O. Box 15457

Wilmington, DE 19850-5457 USA

Tel: (302) 477-8243

Fax: (302) 477-8250

North American Regional Office;

Regional Office for Europe,

Africa and the Middle East

Avecia Inc.

Metal Extraction Products3259 E. Harbour Dr., Suite 100

Phoenix, AZ 85034 USA

Tel: (602) 470-1446

Fax: (602) 470-5030

UpcomingIndustry Events

October 2003

Avecia South American

Users Conference,

(by invitation only)

May 4-7

CIM

Montreal, Canada

May 18-23,

ALTA 2003

Perth, Australia

August 24-27

Hydro 2003

Vancouver, Canada

August, 31 - Septem ber, 3

Gordon Ritcey

Digby, Nova Scotia

Canada

October 22-25

Expo Minera 2003

Acapulco, Mexico

South American Reg ional OfficeAvecia Limitada

Metal Extraction Products

Andres de Fuenzalida 147

Providencia, Santiago

CHILE

Tel: 56-2-3365300

Fax: 56-2-3365310

Australian Regional Office

Avecia Trading Limited

15 Edgars Road

P.O. Box 247

Thomastown, Victoria 3074Australia

Tel: 61-(0)-3-9460-7704

Fax: 61-(0)-3-9460-7758

Metal Extract ion Products

Cy Tec Solutions 8

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Transcript of Cy Tec Solutions 8