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High Density Sludge Process

Britannia Mine Acid Mine Drainage Treatment

BritamiaBeach, BC

August 1997

DISCLAIMER

Environment Canada, British Columbia Ministry of Environment, Lands and Parks, and Cominco Ltd, sponsored the research in this report. Environment Canada acknowledges, with thanks, the cooperation and assistance provided to this project by Coopers Lybrand Ltd and Mr Morris Neale of Britannia Beach.

The views and opinions expressed by the author do not necessarily state or reflect the opinions of the sponsors of the project.

1+1 Canada Canada

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Environment Environnement

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Readers wishing to comment on this report are invited to do so before December 30, 1997.

Head Pollution Prevention and Assessment Division Environment Canada 224 West Esplanade North Vancouver, BC Vi" 3H7 CANADA

August 29,1997

PILOT SCALE TESTING OF THE HIGH DENSITY SLUDGE PROCESS

BRITANNIA MINE ACID MINE DRAINAGE TREATMENT

BRITANNIA BEACH, B.C.

August 1997

Prepared By

COMINCO ENGINEERING SERVICES LIMITED WATER TREATMENT TECHNOLOGY

1636 WEST 75TH AVENUE VANCOUVER, B.C. V6P 662

CANADA

DISTRIBUTION: Cominco Limited CESL Environment Canada

(2) copies (2) copies (2) copies

Summary

A pilot plant study examining the application of the High Density Sludge (HDS) process at

the Britannia Mine, Britannia Beach, British Columbia, has been completed. The purpose of

the test work was to assess the treatment of acid mine drainage (AMD) and develop basic

operating design parameters for two reagent systems. Specifically the objectives to produce

a sludge under standard HDS conditions and to test combustion ash from a nearby pulp and

paper operation as neutralizing agent. This work was done under a cooperative agreement

between Environment Canada and Cominco Limited.

The technical objectives laid.out ahead of time were used to evaluate the success of the

project. Included in these objectives were:

to obtain greater than 12% solids in the clarifier underflow with lime neutralization

an effluent low in suspended solids and dissolved metals

determination of the optimum pH range for oxidation of dissolved iron and metals

removal

to determine the effects of precipitator catch and top ash on clarifier underflow density as

well as the rate of combustion ash consumption

establish process design and operating parameters

A standard HDS design was developed and applied in the testing of both lime and ash

reagents. The acid mine drainage from the 4100 portal (lower flume) was the feed source

for all but the last test, where AMD from the 2200 adit was used.

Using lime neutralization and an average retention time of about 37 minutes in reaction

tanks, the process was able to increase the clarifier underflow sludge density from 2 to 15.9

percent solids and control the metals of concern to below discharge limits. Using precipitator

catch and a retention time of about 42 minutes, sludge density reached 38 percent solids

and the effluent met discharge requirements. When top ash was used in place of lime with a

37 minute retention time, sludge density exceeded 41 percent solids and the effluent again

met discharge requirements.

During the pilot scale test work, the HDS pilot plant consistently produced high density

sludge, ranging between 11 and 41 percent solids, depending on the neutralizing reagent

used. Recycle ratios ranged from 2:l to 751. Optimum recycle ratios were not determined

however, good results were obtained with a ratio of 20:l using lime, 4:l with precipitator

catch and 1O:l using top ash (as determined by the ratio of recycled to freshly precipitated

solids).

Although lime HDS treatment has been extensively confirmed in reported test work and

numerous full scale operations, this test program is believed to be the first successful

application of a waste material as a HDS Process reagent.

Based on the results of the pilot plant tests, a full scale HDS system using lime neutralization

should successfully remove the metals of issue from the 4100 portal AMD and also produce

a chemically stable sludge of at least 15% solids. Much higher sludge densities can be

achieved by using pulp mill combustion ash however the volume of sludge generated also

increases. The effluent might also contain toxic combustion ash contaminants which were

not assayed for in this test program.

The sludge filterability tests showed good filtering characteristics for all three sludge types.

The underflow slurries were easy to filter and the filter cakes had relatively low moisture

contents for hydroxide sludges. This was highest for lime neutralization (-68 %) and lowest

for neutralization with top ash (-34 %). The filter cakes had excellent release characteristics.

Sludge stability tests were not conducted due to budget limitations.

It is noteworthy that the sludge solids from the use of lime contain about 4.64% copper and

4.99% zinc. These favourable metal concentrations and the form of the sludge may make it

very suitable for disposal with metal recovery in a smelter. In a full scale treatment plant,

lime HDS and ash HDS treatment would generate about 6.3 tonnes per day and 42.2

tonnes per day solids based upon a flow of 522 m3/hr, respectively.

TABLE OF CONTENTS

1.0 INTRODUCTION .............................................................................................................. 1

1.1 THE PROJECT .................................................................................................................... 1

1.2 THE HDS PROCESS ........................................................................................................... 2

2.0 PROJECT BACKGROUND AND OBJECTIVES ............................................................. 7

2.1 BACKGROUND .................................................................................................................... 7

2.2 PROJECT OBJECTIVES ....................................................................................................... 8

3.0 EXPERIMENTAL OUTLINE ............................................................................................. 9

3.1 TEST PROGRAM ................................................................................................................. 9

3.2 SAMPLE PREPARATION ....................................................................................................... 9

3.3 GENERAL APPROACH ....................................................................................................... 10

4.0 TEST DESCRIPTIONS AND RESULTS ........................................................................ 17

4.1 COMMISSIONING AND NEUTRALIZATION WITH HYDRATED LIME ............................................ 17

4.2 NEUTRALIZATION WITH PRECIPITATOR CATCH ................................................................... 18

4.3 NEUTRALIZATION WITH TOP ASH ....................................................................................... 20

4.4 OVERALL TEST RESULTS .................................................................................................. 21

4.4.1 Analytical Results .................................................................................................... 22

4.4.2 Acute Lethality Tests ............................................................................................... 24

4.4.3 Dioxins and Furans in Woodwaste Ash Ovefflow .................................................... 24

4.4.4 Potential Solids Generation ..................................................................................... 26

4.4.5 Clarifier Feed Settling Tests .................................................................................... 27

4.4.6 Sludge Filterability Tests ......................................................................................... 27

4.4.7 Sludge Drainage Tests ............................................................................................ 28

4.5 REAGENT REQUIREMENTS ................................................................................................ 29

4.5.1 Air ............................................................................................................................ 29

4.5.2 Flocculant ................................................................................................................ 30

4.5.3 Lime ........................................................................................................................ 30

4.5.4 Precipitator Catch and Top Ash ............................................................................... 30 5.0 CONCLUSIONS AND RECOMMENDATIONS .............................................................. 31

5.1 CONCLUSIONS ................................................................................................................. 31

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1.0 INTRODUCTION

1.1 The Project

To facilitate development of a solution to the Britannia mine drainage issue, Mr. Robert

M'Candless of Environment Canada, North Vancouver, in response to a need to treat acid

mine drainage from the Britannia Mine, solicited a proposal for pilot scale testing of the high

density sludge process from Cominco Engineering Services Ltd. (CESL) of Vancouver

through Cominco Limited. The pilot plant study was jointly funded by Cominco Limited and

Environment Canada. The test work was carried out under the direction of Mr. Waiter Kuit of

Cominco Limited. Its purpose was to determine the applicability of the HDS process with

alternative reagent systems. The first phase focused on lime to produce a metal rich sludge

while the second examined the use of precipitator catch and top ash from the pulp and paper

industry as a neutralizing agent instead of lime. A parallel study of pulp mill ash properties

and supplies was funded by Environment Canada and Howe Sound Pulp and Paper Ltd.

Acid mine drainage has been occurring at the Britannia Mine for many years and at present

it is being discharged untreated directly into Howe Sound. The pH of the AMD coming from

the 4100 portal is approximately 3.2 and the major metal contaminants are zinc at 25 mglL,

copper at 20 mglL, aluminum at 32 mglL, iron at 10 mglL and manganese at 6 mglL. With

appropriate reagent additions, these metals are routinely treatable using the HDS process.

However, due to the low dissolved iron concentration and appreciable aluminum, the sludge

density is expected to remain relatively low, in the range of 10 to 15 percent solids. Since

sludge disposal is one of the key factors for selecting any treatment process, it is important

to consider both the amount and the nature of the sludge that would be produced.

Preliminary bench scale testing and sampling had been conducted at various times and by

various parties. The purpose of the pilot plant study was to determine a suitable and viable

treatment of the AMD from the mine and present some options for sludge disposal. Based

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Pilot Scale Testing of the High Density Sludge Process

Britannia Beach, B.C. Britannia Mine AMD Treatment

Page 2

on CESL's past experience with similar feed types, it was decided to proceed directly to HDS

pilot plant testing rather than conduct bench scale HDS simulations.

This report reviews the project objectives, the experimental approach used, experimental

results, interpretation, conclusions and recommendations. The pilot plant was

commissioned between April 09 and April 12, 1997. Testing began on April 14, 1997 and

was completed on May 2, 1997. The individual tests were carried out for a duration of 17 to

49 hours for each major parameter change. An additional test using AMD from the 2200 adit

was conducted on June 4 and 5,1997.

The test data, graphs and analytical results from the experiments are provided in the

appendices.

1.2 The HDS Process

The effective removal of base metals in a chemically stable form in the HDS process is

primarily the result of the formation of co-precipitates with iron on the surfaces of the

recycled sludge particles. The stability of the precipitates is favourably influenced by a high

iron to total iron to total metals ratio in the plant feed. A simple recycle is not sufficient to

change metal ratios and, in extreme examples, iron may have to be added. Otherwise, the

storage site for the sludge produced must allow for the possibility of longer term instability.

In all cases the oxidation of ferrous to ferric iron is the principal oxygen-consuming reaction.

However, if air is sparged into the reactor for oxidation, the oxygen transfer may well be

controlling the reaction and hence the reactor tank sizing. Oxygen transfer will be the

dominant factor in agitator design.

Design plant throughput is influenced by the volume of water to be treated. For example,

seasonal changes will determine run-off, much of which may have to be treated. Increased

flow may be accompanied by a dilution of contaminants, both acid and metal, and the

resulting plant influent may require reduced oxidation and/or residence time, which may

compensate for the increased flow.

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The near-complete precipitation of the metals as hydroxides in the neutralization process

proceeds according to the following reactions:

M+* + SO; + Cat++ 2(OH)- + H20 + M(OH)2 +CaSO,.H,O

2M+++ + 3(SO,)’+ 3Ca”+ 6(OH)-+ 6H20 + 2M(OH)$ + 3CaS0,.H20

As implied by the equations above, the products of these reactions are metal hydroxide

precipitates and calcium sulfate (gypsum). If the sulfate concentration of the wastewater is

high enough, there will be sufficient gypsum produced to exceed its solubility and it will

precipitate with the sludge. The presence of the gypsum increases the buffering capacity of

the sludge and is partially responsible for the sludge’s improved chemical stability. In fact,

treated solutions are often supersaturated in gypsum. This High Density Sludge technology

is especially beneficial to operations which produce high sulfate from pressure oxidation and

biooxidation processes.

The main features of the HDS process can be summarized as follows: Lime and recycled

sludge are added to the lime-sludge mix tank at the head of the process and this becomes

the main neutralization agent. This mixture is discharged to the rapid mix tank where it is

mixed with influent, thereby achieving neutralization. This mixture is fed to the main lime

reactor where a combination of aggressive aeration and high shear agitation ensures

optimum process chemistry and clarifier performance. The discharge from the lime reactor

is treated with flocculant in the flocculation tank. The clarifier separates the treated effluent

from the sludge, a portion of which is recycled to the head of the process.

The HDS process is normally run at a pH between 9.0 and 9.5, as most metals encountered

precipitate at or below this concentration of hydroxide ions. Oxidation of ferrous to ferric iron

takes place quite rapidly at this pH and oxygen from air is the most common oxidizing agent.

There is no reason why other agents cannot be used for oxidation, although all the plants

built by the authors so far have used air for oxidation.

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The process itself depends upon sludge recycle from the treated effluent and in most plants

this has been achieved in a thickener style clarifier which offers a pumpable sludge as the

separated solids product. Clearly. recycle from a settling pond presents some material

handling problems, as do filter-style clarifiers, but either procedure could be used.

Some general comments on the construction materials and design parameters are as

follows:

Untreated water supply -All pumps in contact with this water should be 316 SS because of

the acid pH of the water. Any surge tanks should also be 316 SS. Pipelines are best in high

density polyethylene. The process water flow rates and contaminant levels must be fully

known in order to develop a proper design.

Lime-sludge mix tank - This vessel is normally made of carbon steel since the vessel

contents are at a high pH. The agitator must be able to supply adequate mixing power to the

vessel as the sludge can be quite thick.

Rapid mix tank - This vessel must be made of 316 SS because of the corrosive nature of

the untreated water being put into the tank although normally the pH is around 9.5. The

agitator and shaft should be 316 SS or rubber covered.

Lime reactor - This tank can be either concrete or mild steel. In very large tanks concrete

may be preferred because of the high power input requirements of the agitator. The final

selection is dependent on an economic analysis and whether or not the possibility of freezing

exists in the plant. The agitator gear reducer must be of a very heavy duty design to handle

the difficult process requirements of keeping solids in suspension, dispersing the air into

small bubbles, and contacting the air, water and solids. Designing for a low maintenance

requirement is also an important factor.

Pilot Scale Testing of the High Density Sludge Process Britannla Mine AMD Treatment Britannia Beach, B.C. Page 5

Flocculation l ank - This vessel can be concrete or mild steel. The agitation is gentle to

avoid breaking any of the flocs produced.

Clarifier - This vessel can be either steel or concrete. Site objectives and location will form

part of the economic evaluation to determine which material is selected. The rake arms

should be fitted with thixo-posts to minimize disturbance of the sludge bed. The introduction

of the flocculated feed into the clarifier must be gentle to avoid breaking up the flocs and the

clarifier overflow must be properly collected to reduce the problems of freezing where low

temperature is a concern.

Sludge disposal - This may require pumping over a long distance. The line loss

characteristics of the sludge must be known to properly size the pumps required. Proper

start-up and shut-down of this batch pumping operation are important to avoid plugging. The

sludge lines can be HDPE or steel.

Process control - The pH in the rapid mix tank is the primary parameter used to control

lime addition to the sludge-lime mix tank. Optimum operation is achieved through time-

proportional control of a pinch valve, which taps a small proportion of the slurry circulating in

a loop from the lime slurry storage tank. The pH in the lime reactor is monitored and may be

used to adjust the set-point of the primary pH control loop based on operating parameters

such as feed rate, metals loading, and sludge recycle rate.

Flocculant - Flocculant may be added at various locations prior to the flocculation tank and

in the feed to the clarifier. Flocculant flow is measured prior to dilution and controlled to an

operator determined set-point. An on-line settling rate analyzer is commercially available

and can be used to determine the settling characteristics of the clarifier feed and thus speed

up the establishment of optimum flocculant requirements in addition to monitoring the effects

on clarifier overflow turbidity. Monitoring of clarifier underflow density is essential. This

parameter combined with sludge recycle flow rate determines recycle mass flow, the control

of which is paramount in achieving optimum process performance. Duplication of the sludge

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recycle circuit with the use of variable-speed pump controllers and automatic line-flush

sequencing has been found to provide good operating flexibility.

Clarifier ovemow turbidity and pH are monitored and can be used to shut down plant feed or

redirect clarifier ovemow in the event that they exceed operational limits. F.inal discharge

flow is monitored and grab samples are taken automatically for analysis and reporting.

Fresh water consumption can be reduced through the use of treated water (from clarifier

overflow) for lime slaking, flocculant dilution and line flushing.

In order to minimize labour costs, various automatic sequences for equipment operation can

be included with the use of programmable logic controllers. For example, operation of lime

slakers can be automated based on the draw down of slurry from the lime slurry storage tank

and flocculant preparation can be similarfy controlled. At remote sites where the plant is

mainly unattended, an automatic power on-restart sequence (which can restart the plant in

the event of a brief power interruption) has been found to be beneficial.

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2.0 PROJECT BACKGROUND AND OBJECTIVES

2.1 Background

Acid mine drainage has been occurring at the Britannia Mine for decades. At the present time

there is no treatment facility and the AMD, containing elevated levels of copper, iron, zinc and

other metals, is simply discharged into Howe Sound. Approximately 600 kilograms of copper

and zinc alone are released into the sound each day. Due to the toxicity of these metals in

high concentrations, a suitable and economical process is required to neutralize the acid and

remove the metals. The sludge that results from the neutralization process must be easy to

handle. If permanent storage is conducted, it should also be chemically stable.

Sludge disposal is an important factor in the selection of an appropriate process. If it is to be

shipped off site for disposal or processing for metals recovery it must be in a form conducive to

that. At many sites, High Density Sludge plants, both pilot scale and full size operations, have

been successfully tested and built by CESL. These plants produce chemically stable sludge

for long term storage as well as a clean effluent. CESL embarked on a pilot scale test program

at the Britannia site to confirm that the AMD occurring there could be successfully treated using

the HDS process.

Traditionally, neutralization is carried out using some form of lime. However, due to the

proximity of several pulp mills which produce a highly alkaline boiler combustion ash waste,

this by-product would be tested as an alternative to lime neutralization. The combustion ash is

produced from the burning of wood waste (eg. Bark, sawdust) and is disposed of in landfills

located at each site, often at substantial cost. Using combustion ash in the High Density

Sludge process could potentially reduce both HDS operating costs and pulp mill waste disposal

costs.

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2.2 Project Objectives

A study was undertaken to demonstrate the viability of the High Density Sludge process for

the treatment of acid mine drainage at Britannia Beach, specifically AMD from the 4100

portal of the abandoned mine. A secondary objective was to investigate the possibility of

using pulp mill waste in the HDS process as a competitive alternative to lime neutralization.

AMD from the 2200 portal was tested briefly. Success of the project was based upon a

predetermined set of performance guidelines regarding effluent quality and sludge density,

volume and stability. The performance evaluation of the pilot scale testing was based upon

the following project goals:

obtain greater than 12 percent solids in the clarifier underflow with lime

neutralization

an effluent low suspended solids and dissolved metals

determine the optimum pH for oxidation of dissolved iron and metals removal

determine the recycle ratio which results in sufficient sludge density and minimal

reagent consumption

to determine the effects of precipitator catch and top ash on clarifier underflow as

well as the rate of combustion ash consumption

establish process design and operating parameters

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3.0 EXPERIMENTAL OUTLINE

3.1 Test Program

Based on CESL's previous experience, the HDS process was expected to achieve a sludge

density of 10 to 15 percent solids with lime neutralization and at least 30 percent solids using

combustion ash. Other objectives were to obtain the necessary design parameters such as

flow rates, recycle ratios, reagent consumption and aeration requirements to allow the

project to continue to the preliminary design phase. Preliminary operating parameters were

selected based upon previous experience with similar effluent treatment projects. The test

work was designed to confirm the HDS process under standard and modified conditions.

The main indicators used during the tests to evaluate treatment efficiency were the solids

density (or specific gravity) of the sludge generated and the quality of the effluent.

3.2 Sample Preparation

AMD feed was obtained from the 4100 portal by means of a sump pump which was used to

fill a 500 litre feed tank as needed. The temperature of the AMD ranged from 12 to 16

degrees Celsius. The feed was brownish-orange in colour and the pH was between 2.7 and

3.6. The lime used was industrial grade calcium hydroxide and it was prepared at 15% w/v

initially and at 10 percent for Tests BMHDS-2 and 3. The precipitator catch and top ash

came from Howe Sound Pulp and Paper of Port Mellon, B.C. The precipitator catch was dry

and used as received. Its particle size is typically 25-75% minus 200 mesh (75 pm). The

top ash sample was screened with a 20 mesh (850 pm) sieve at Chemex Labs Ltd. of North

Vancouver. The oversize material was rotary plate pulverized to pass through the same

sieve and the two portions were then combined.

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3.3 General Approach

The pilot plant was set up to run in the standard HDS configuration shown in Figure 3.1

below. The initial commissioning stage lasted 71 hours and the purpose was to generate

sludge inventory and to condition and densify the metal hydroxide sludge. The retention

time in each tank is dependent upon the flow rate and sludge recycle rate and was vaned

between tests as different conditions were tested.

LIME' - 4

LIME *I SLUDGE MIX TANK

AIR I'

*Lm wed h Cornmi- IM Tells BMHDS.1 lo 3

Top Ash wad h TeNs BMHDS-3 M 10 P ~ C d C n w a d h T H U B M H D S 4 1 0 7

SLUDGE RECYCLE v - SLUDGE PURGE - I

Figure 3.1 -Standard HDS

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All tests were run continuously for a duration of 17 to 48 hours. The process was shut down

for 48 hours every 5 days as well as after each phase of testing (lime, precipitator catch and

top ash) to allow for sludge and slurry removal and cleaning. Due to time constraints and

practical limitations, during each phase of testing the conditions were changed without

purging the sludge from the clarifier. This allowed for continuous operation without major

upsets in the plant operation.

Commissioning and Tests BMHDS-1 to BMHDSS were run using lime addition. Tests

BMHDS-4 to BMHDSJ operated with precipitator catch and Tests BMHDS-8 to BMHDS-10

used top ash. The principal reactors were vigorously agitated and aerated at approximately

6 litreslminute. The feed for commissioning and the above tests was acid mine drainage

from the 4100 portal of the Britannia Mine. Test BMHDS-11 used AMD from the 2200 adit.

The flocculant used for the pilot study was Allied Colloids Percol E-IO. It was added as a

0.025% solution during commissioning and Test BMHDS-1 and as a 0.0125% solution for all

other tests, except BMHDS-11, where the concentration was 0.05%.

Commissioning

The first four days of testing consisted of assembling and commissioning the pilot plant and

verifying the basic process. Three full days of operation were necessary to produce an

adequate sludge volume at a density sufficient for recycle. There was no underflow recycle

for the first 38 hours of operation due to the limited sludge volume and the low sludge

density. The commissioning stage was fairly slow due to the relatively low metals

concentration in the feed. The recycle ratio used during the latter stage of commissioning

ranged from 251 to 351. The sludge density increased to 10 percent solids after 71 hours

of continuous operation.

Based upon past experience and visual observations during the commissioning of the pilot

plant, it was decided that the initial residence time of approximately 30 minutes provided

adequate time for oxidation once the reaction vessels had approximately 5% solids loading.

Pilot Scale Testing of the High Density Sludge ProCeSS Blltannla Mine AMD Treatment Britannia Beach, B.C. Page 12

Test BMHDS-1 Standard HDS - DH 9.5. Moderate Recvcle

Once the solids generation rate and underflow sludge density were determined, an

appropriate recycle ratio was chosen. For this test, which lasted 48 hours, the underflow

recycle ratio averaged 34:l and ranged from 28:l to 46:l. Hydrated lime at 15% solids was

used for neutralization to pH 9.5.

Once base-line plant operation was established and sufficient sludge inventory was

obtained, the clarifier underflow sludge was monitored to determine the increase in sludge

density as the thixotrophic sludge converted to high density sludge. The percent solids of

the underflow was determined approximately every 8 hours.

Feed and clarifier overflow samples were collected for analyses after 21 hours, 31 hours and

48 hours of operation. The rate of solids settling in the clarifier feed was measured several

times during the test to produce settling curves.

Test BMHDS-2 Standard HDS - DH 9.5. Hiah Recvcle

For this test, which lasted 48 hours, the recycle ratio was increased by reducing the feed

rate and increasing the underflow recycle rate. The average recycle ratio was 59:l and it

ranged between 53:l and 74:l. Hydrated lime at 10% solids was used for neutralization to

pH 9.5.

The percent solids of the underflow was determined approximately every 8 hours and

samples of the feed and clarifier overflow were collected for analyses every 12 hours. The

underflow percent solids was determined and several solids generation and settling tests

were also done to assess overall test performance under the selected conditions.

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Test BMHDS-3 Standard HDS - DH 9.5, Low Recvcle

For this final test using lime neutralization, the recycle ratio was decreased by reducing the

recycle to about one-third of the previous rate. The recycle ratio ranged from 21:l to 23:l.

The duration of the test was 23 hours.

Once again, the percent solids of the underflow was determined on a regular basis.

Samples of the feed and clarifier overflow were collected for analyses after 13 and 23 hours

of operation. As well, the underflow percent solids was determined and several solids

generation and settling tests were also done to assess performance.

Test BMHDS4 Modified HDS (Precidtator Catch) - DH 8.5

The sludge and slurry were emptied from the reactors and the lime slurry was replaced with

precipitator catch at 42% w/v solids. The operating pH was reduced to 8.5 and the feed rate

was decreased by approximately 20 percent. The longer retention time was necessary to

oxidize the increased metals introduced in the precipitator catch. The recycle ratio was

much lower since the solids generation rate was about eight times higher than with lime

neutralization.

Solution samples were collected for analysis at 35 and 48 hours. Clarifier feed and

underflow samples were also taken throughout the run for various tests.

Test BMHDS-5 Modified HDS (Precidtator Catch) - DH 9.0

The conditions and procedures for this test were similar to those for the previous one, with

the pH in the second reactor increased to 9.0. The test was run for 30 hours.

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Test BMHDS-6 Modified HDS (Precipitator Catch) - pH 9.5

The conditions and procedures for this test were similar to those for the previous two tests,

with the pH in the second reactor increased to 9.5. The test was run for 18 hours.

Test BMHDS-7 Modified HDS (Precipitator Catch) - pH 8.0

in this test, the feed rate was increased and the recycle rate was decreased to determine the

effects of a shorter residence time and a lower sludge recycle ratio on effluent quality. The

pH in the second reactor was decreased to 8 and the test ran for 17 hours.

Test BMHDS-8 Modified HDS (Top Ash) - pH 9.0

Prior to starting this test, the sludge and slurry were emptied from the reactors and the

precipitator catch slurry was replaced with top ash at 39% w/v solids. The operating pH was

set at 9.0 and the feed and recycle rates were adjusted for a retention time of about 38

minutes. The test was run for 25 hours.

Test BMHDS-9 Modified HDS (Top Ash) - pH 8.5

The conditions and procedures for this test were similar to those for the previous one, with

the pH in the second reactor decreased to 8.5. The test duration was 24 hours.

Test BMHDS-10 Modified HDS (TOD Ash) - DH 8.0

In this test, the feed rate was increased and the recycle rate was decreased to keep the

recycle ratio similar to that in the previous two tests. The pH in the second reactor was

decreased to 8 and the test ran for 24 hours.

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Test BMHDS-11 Standard HDS - DH 9.5

The conditions for this test were similar to those for Test BMHDS-3, where lime

neutralization was used. The feed source was AMD from the 2200 adit, which has higher

metal concentrations than the AMD collected from the 4100 adit. The test was run for a total

of 13 hours over 2 days.

3.4 Analytical Work

Samples were collected from both the clarifier overflow and the feed tank several times

during each test and bottled for analyses. One set of samples was filtered through a 0.45

micron membrane filter, preserved with nitric acid and submitted for a dissolved metals ICP

scan at Environment Canada’s Pacific Environmental Science Centre (PESC) in North

Vancouver, B.C. A duplicate set of samples, unfiltered, was treated with nitric acid and

submitted for total metals ICP analysis at the same laboratory. Additional samples of the

clarifier overflow (unfiltered, untreated) were also sent to PESC for suspended solids

determination, anions, and acute lethality tests.

In addition to the solution samples mentioned above, a dried sludge sample from each test

was submitted to an assay laboratory for an ICP scan, whole rock analysis and, in some

cases, individual metal assays. The majority of the work was done by Environment Canada,

with some analyses performed by Cominco’s ERL laboratory in Vancouver and Chemex

Labs of North Vancouver.

Process Monitoring

The process work sheets provided in Appendix A were normally completed every two hours.

All process irregularities were also noted in the project data book. The clarifier feed was

sampled periodically for specific gravity measurement, percent solids determination and rate

of settling. The clarifier underflow was also sampled regularly for specific gravity

1

~1 ~1 I

Pllot Scale Testing of the High Density Sludge Process Britannia Mine AMD Treatment Britannia Beach, B.C. Page 16

~

I 1

determinations to evaluate the progress of the HDS process. A sample of sludge from each

phase of testing was collected for filterability and long-term settling tests. Solids generation

tests were done on the pilot plant feed using the appropriate neutralizing reagent for each

test. An 80 litre sample of effluent was collected near the end of each phase of testing for

an Acute Lethality Test using rainbow trout.

I Pilot Scale Testing of the High Density Sludge Process

I Britannia Mine AMD Treatment Britannia Beach, B.C. Page 17

4.0 TEST DESCRIPTIONS AND RESULTS

This section provides detailed descriptions of the test work performed and the results of that

work. The data for individual tests are provided in Appendix A and the results can be found

in the additional appendices.

4.1 Commissioning and Neutralization with Hydrated Lime

The commissioning of the pilot plant occurred over a three day period using feed from the

4100 portal of the Britannia Mine. This was collected in a 500 litre tank by turning on a sump

pump in the drainage line as needed. The primary reason for the extended commissioning

period was to allow for sufficient solids to build up in the clarifier and to condition the sludge.

This required a relatively long period due to the low metals content of the AMD. During

commissioning it was decided that a 30 to 40 minute retention time would be sufficient time

for oxidation and metals precipitation. The aeration rate used in the two reactors was determined from previous test work, approximately 5.7 litreslminute air for all tests.

The hydrated lime slurry was prepared at 150 g/L for commissioning and Test BMHDS-I and

reduced to 100 glL for the remaining tests. The lime strength was decreased to allow for

better pH control. Flocculant scoping tests indicated that Allied Colloids Percol 156, 727 and

El0 performed equally. For all tests in the HDS treatment program Percol E-IO was used,

the concentration ranging between 0.125 and 0.250 glL. The test conditions for

commissioning and the first three tests are summarized below.

Table 4.1.1 -Test Conditions, Standard HDS (Lime Neutralization)

I Pilot Scale Testing of the High Density Sludge Process

,I Britannia Mine AMD Treatment Britannia Beach, B.C. Page 10

Initially the sludge generated was greenish-white in colour but over time it became more

brown in colour. This darker brown colour was due to the oxidation of ferrous iron. The first

half of commissioning was without underflow recycle due to an insufficient sludge volume.

The pH was increased to 9.5 for the first 3 tests because early ICP results showed that

manganese and zinc were not being precipitated sufficiently enough to meet discharge

limits. The underflow density increased steadily during the tests. The results of these

individual tests are summarized in graph form in Appendix 6. Lime consumption vaned with

the recycle rate and flocculant consumption increased as the amount of solids in the system

built up. The effluent was clear however some very fine suspended solids were present in all

tests. Reducing the clarifier rake speed helped alleviate this problem however at times it

negatively effected the underflow density. The important parameters and results are

summarized in the table below. Detailed data for each test are provided in Appendix A..

Table 4.1.2 -Test Summary, Standard HDS (Lime Neutralization)

4.2 Neutralization with Precipitator Catch

The next phase of testing used precipitator catch in place of lime as the neutralizing reagent.

The theory was that the pulp mill waste could be used to reduce reagent costs for HDS plant

operation as well as diminish the waste disposal problem. Wlth the high concentration of

some metals, specifically copper and zinc, in the combustion ash, the possibility of

,I Pilot Scale Testing of the High Denslty Sludge Process Britannia Mine AMD Treatment Britannia Beach, B.C. Page I S

recovering these metals from the high density sludge was also considered. Four tests were

run using precipitator catch collected from Howe Sound Pulp and Paper. The conditions for

the four tests are summarized in the following table.

Table 4.2.1 -Test Conditions, Modified HDS (Precipitator Catch Neutralization)

The sludge and slurry from the previous tests were removed before beginning this phase of

testing. The solids generation rate using precipitator catch compared to lime was

approximately eight times higher, therefore the recycle ratios in these tests were much lower

when similar recycle flow rates are compared. The solids density increased much more

quickly than during commissioning due to the higher solids generation rate. It can be seen

from the summary table below that precipitator catch consumption was at least ten times

higher than lime consumption under similar conditions. Flocculant consumption was

generally lower because it was apparent that increasing the amount of flocculant added did

not improve overflow clarity. Fine, light-coloured suspended solids were present in all tests

along with larger, black solids.

Table 4.2.2 -Test Summary, Modified HDS (Precipitator Catch Neutralization)

I I

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I I I I I I I I I I I I I I I I I

The underflow density increased from Test BMHDS-4 to BMHDS-6 and decreased slightly

during the last test because the recycle rate was greatly reduced to lower the recycle ratio.

The resulting sludge from these tests was black in colour and filtered easily. A low operating

pH and a high sludge recycle will minimize precipitator catch consumption and the rate of

sludge production.

4.3 Neutralization with Top Ash

The next three tests used top ash instead of precipitator catch as the neutralizing reagent.

The reactors were emptied prior to starting Test BMHDS-8 so the initial underflow density

was low, although it increased rapidly due to the high metals content of the top ash. The

recycle ratio was maintained around 1O:l once sufficient solids were present in the clarifier.

The conditions for each test were similar. as noted below.

Table 4.3.1 -Test Conditions, Modified HDS (Top Ash Neutralization)

The top ash sample had a higher neutralizing potential than the precipitator catch and this

was reflected in the lower top ash consumption when similar tests (4 and 9, 5 and 8) were

compared. Since the top ash had a lower total metals to iron ratio than the precipitator

catch, metals removal was poorer in these last tests. Suspended solids in the clarifier

overflow appeared higher and this observation was confirmed by higher total metals levels in

the effluent. Underflow density exceeded 40% yet the slurry was easy to filter.

Pilot Scale Testing of the High Density Sludge Process Britannia Mine AMD Treatment Britannia Beach, B.C. Page 21

Table 4.3.2 -Test Summary, Modified HDS ( lop Ash Neutralization)

4.4 Overall Test Results

The data for all the tests have been evaluated on a more global basis to examine any trends

that may be present. The metals of concern were precipitated to acceptable levels at pH 9.0

and 9.5 using lime, precipitator catch and top ash as neutralizing agents. In all of the tests a

densified sludge was obtained. Figure 4.4.1 below shows the relationship between clarifier

undertlow specific gravity and percent solids for the three phases of testing. Although this is

a known relationship, the graph provides a useful conversion chart as specific gravity is

much simpler and quicker to measure than percent solids. Graphs of specific gravity over

time for each test are provided in Appendix B.

I I I

I Pilot Scale Testing of the Hlgh Denslty Sludge Process

I Britannia Mine AMD Treatment Britannia Beach, B.C. Page 22

~

Clatifhr Unkrflow Pomnt Solids VI. Swcific Gnvily

1 45 1

35 - -

EMHDS4 to 7 BMHDS-8 to 10

1.07 1.09 1.12 1.17 1.26 1.29 1.19 1.29 1.32

S W a Gravity

Figure 4.4.1

The underflow solids density increased slowly during the first three tests and it is possible

that it would have exceeded 16 percent solids had Test BMHDS-3 been extended. This

would occur as the low density sludge is purged from the system with time, the overall

percent solids thereby increasing. The clarifier underflow percent solids versus specific

gravity curves for Tests BMHDS-4 to 7 (Precipitator Catch) and BMHDS-8 to 10 (Top Ash)

appeared to be leveling off at 39% and 41% respectively, and were probably close to

maximum under the specific conditions. Increasing the underflow recycle rate would not be expected to improve the solids densities significantly. Additional tests on the clarifier

underflow sludge (Section 4.4.6 below) indicated that it will dewater and further densify

under conditions that permit free draining.

4.4.1 Analytical Results

Table 4.4.1 below provides a partial summary of the analytical results for the major metals

present in the Britannia 4100 adit AMD. Samples of feed, clarifier overflow and clarifier

underflow were collected several times during most tests and at the end of each test. All

solution samples were submitted for analysis at Environment Canada's Pacific

Environmental Science Centre (PESC) in North Vancouver, B.C. The sludge samples were

analyzed at three laboratories in the Vancouver area. The detailed results are provided in

Appendix C.

Pilot Scale Testing of the High Density Sludge Process Britannia Mine AMD Treatment Britannia Beach, B.C. Page 23

I I I I I I I I I I I I I I I I I

Table 4.4.1.1 - Partial summary of Analytical Data (as reported by PESC)

NIA = Not Analyzed T.S.S. = Total Suspended Solids

Table 4.4.2 below summarizes the permissible levels of several metals as outlined in the

Metal Mining Liquid Effluent Regulations of the Fisheries Act (Canada Gazette Part 11, Vol.lll,

No. 5).

Table 4.4.1.2 - Schedule 1, Part 1 -Authorized Levels of Substances

The above tables show that the metals of primary concern, (copper and zinc) have been

removed to below discharge requirements. The method detection limit for lead (0.5 mglL)

I

I I I I I I I I

Pilot Scale Testing of the High Densky Sludge Process Britannia Mine AMD Treatment Britannia Beach, B.C. Page 24

was higher than the discharge requirement (0.2 mglL). The manganese concentration

started to increase as the operating pH was decreased in the last reactor (i.e. below pH 9.0).

The test results indicate the importance of the final HDS effluent pH in removing the metals

of concern to acceptable levels. This information is useful should regulations for effluent

discharge limits be changed in the future. Generally, the tests using the three different

neutralizing agents and the two feed types produced high quality effluents low in both

dissolved metals and suspended solids.

4.4.2 Acute Lethality Tests

Approximately 80 litres of effluent was collected near the end of each phase of testing for an

Acute Lethality Test using rainbow trout. The tests were conducted at Environment

Canada's Aquatic Toxicology Section in North Vancouver. Effluent collected from both Test

BMHDS-3 (lime neutralization) and Test BMHDS-10 (top ash neutralization) was non-lethal

to rainbow trout at 100 percent concentration. Effluent collected from Test BMHDS-7

(precipitator catch neutralization) showed toxicity with 5/10 fish mortalities after 96 hours at

100 percent concentration however there were no fish deaths at a concentration of 56%. The

test results are provided in Appendix D.

4.4.3 Dioxins and Furans in Woodwaste Ash Overtlow

I I I I

Environment Canada performed analyses on the clarifier overtlow and provided the following

results and interpretation. The woodwaste ash used as a neutralizing agent came from a

pulp mill where some of the woodwaste had been saturated with salt (marine) waters.

Combustion of such waste ("salty hog") may create the toxic compounds known as dioxins

and furans. Consequently the clarifier ovemow was sampled twice for trace concentrations

of these compounds. Significant levels were found as shown below. Note that the same

samples were non-toxic to rainbow trout. Complete test results are in Appendix D.

I I

I Pllot Scale Testing of the High Density Sludge Pmcess

I Britannia Mine AMD Treatment Britannia Beach, B.C. Page 25

Dioxins (2,3,7,8-TCDD, or 2,3,7,8-tetrachlorodibenzo-para-dioxin)

I Date Sampled I Effluent I Detection I Spiked Matrix I Conc. (pglL)

17/18 1.5 I 1 April 25,1997

(PglL) Limit(pg/L) DetermJExpected

I April 30, 1997 I 10 same same

Furans (2,3,7,8-TCDF, or 2,3,7,8-tetrachlorodibenzofuran)

Date Sampled Spiked Matrix Detection Effluent Conc. (pglL) (PglL) Limit (pglL)

Determ./Expected April 25, 1997

same same I00 April 30, 1997 19/18 I .5 130

Toxic Eauivalents (combining all dioxin-like compounds in the sample)

I Date Sampled I TEQ I

I April 30, 1997 I 67.4 I The 1992 Pulp and Paper Mill €fluent Chlorinated Dioxins and Furans Regulations under

the federal Fisheries Act prohibit effluent from pulp mills using chlorine bleaching from

having, “ ... any measurable concentration of 2,3,7,8-TCDD, or measurable concentration of

2,3,7,8-TCDF.” Present regulatory requirements set measurable concentrations as greater

than 15 pg/L for 2,3,7,8-TCDD and 50 pg/L for 2.3.7.8-TCDF. These limits apply to the very

large flows discharged from pulp mills, and not necessarily to treated leachate from landfills

presently receiving woodwaste ash. A comparison of treated drainage flows from the

Britannia mine, and the much larger effluent flows from a pulp mill, may show that the

potential mass loading to the environment of dioxins and furans, if present, may not be

significant, but the environmental impact of treating Britannia mine drainage with salt-

contaminated woodwaste ash requires careful consideration and assessment.

Pilot Scale Testing of the High Density Sludge Process Britannia Mine AMD Tmatment Britannia Beach, B.C. Page 26

4.4.4 Potential Solids Generation

An important parameter in the design of a full size HDS plant will be the potential solids

generation value. This value dictates the rate of solids generated by the plant feed which will

impact on aeration and disposal requirements as well as the clarifier underflow recycle rate.

The average solids generation for lime neutralization was 0.47 kglm'. The relatively.low

metals concentration of the 4100 portal AMD would require a high recycle ratio for solids

densification however aeration requirements would be minimal. As the table below

indicates, using precipitator catch or top ash instead of lime increased the average solids

generation significantly. An HDS system using either of these pulp mill byproducts is

expected to require a longer residence time to fully utilize their neutralization potential.

Table 4.4.4.1 - Potential Solids Generation

Consumption (kg/m3) Sludge Characleristics Solids Generation Neutralizing (kg/m3) at pH: at pH:

Reagent 8.0 9.5 9.0 8.5 9.5 9.0 8.5 Generation Rate

15.9 1.115 14,377 2,286 0.47 0.50 n/a 0.35 0.33 n/a n/a Lime

Solids (kgR) (wet tonneslyr.) (dry tonnes/yr.) % S.G. Generation Rate

Prec. Catch

38.7 1.323 44,191 17,102 nla 3.74 3.65 n/a 5.37 3.65 2.75 Top Ash

37.9 1.291 42,710 16,187 3.37 3.54 3.68 9.06 7.40 5.34 2.29'

Notes: n/a = not available Calculations are based on an average AMD flow rate of 522 m3/hr. Consumption is low due to the recycle of high pH sludge from the previous test (BMHDS-6. pH 9.5).

Tests with precipitator catch at pH 8.0 resulted in 0.07 mg/L Cu and 0.66 mgR Zn in the final effluent. Tests with lime at pH 9.0 8 9.5 resulted in a very clean final effluent.

Tests with precipitator catch at pH 9.0 8 9.5 resulted in a belter quality effluent.

It should be noted that at pH 9.0 the consumption of precipitator catch was 22 times higher

than lime and top ash consumption was 16 times higher than lime consumption. The yearly

sludge generation using combustion ash will be approximately 43,450 tonnes at an average

of 38.2% solids compared to 14,400 tonnes at 15.9% solids using lime. The sludge

generated using combustion ash is approximately 3 times greater than with lime. Therefore,

I Pilot Scale Testing of the High Density Sludge Process

I Britannia Mine AMD Treatment Britannia Beach, B.C. Page 27

for the purpose of sludge disposal, neutralization with combustion ash would require a larger

area than that needed for standard HDS neutralization with lime.

4.4.5 Clarifier Feed Settling Tests

Samples of the feed to the clarifier were collected regularly for settling tests. Settling curves

can be found in Appendix E. For all tests, initial solids settling was rapid, however overflow

clarity was variable and appeared to worsen as the pH was lowered. The pulp density of the

settled sludge ranged from 9 to 12 percent after 2 hours when lime was used. The

supernatant from these tests was normally clear of suspended solids within 10 minutes.

Using precipitator catch, the settled sludge pulp density ranged from 18 to 26 percent with

suspended solids visible in the supernatant for up to one hour. Pulp density was higher

when neutralization was done with top ash, ranging from 24 to 39 percent. This last value

appears unusually high and may indicate that the residue was not completely dry before

being weighed. Omitting this number, the range would be 24 to 31 percent solids. A clear

overflow free of suspended solids required a settling time between 30 and 120 minutes for

these tests. The clarifier volume was small relative to the flows used in testing and it is

expected that a residence time more typical of operating plants would result in an overflow

with little or no suspended solids. The clarifier feed ranged from 1.1 to 4.7 percent solids

during the test program.

4.4.6 Sludge Filterability Tests

Table 4.4.6.1 below compares the filtering rate and moisture content of sludge produced

from tests using the three neutralizing agents. Filtering tests indicated that moisture

retention in the filter cake from lime neutralization Test BMHDS-3 was about 50 percent

higher than in Test BMHDS-7 (precipitator catch) and double that of a composite sludge

sample from Tests 8 to 10 using top ash. The filtering rate (dry tonnes/m3/hr) for precipitator

catch was approximately 50 percent higher than top ash and 6.6 times higher when lime was

used. In all tests there was good release of the filter cake from the filter cloth and no cake

Pilot Scale Testing of the High Dsnslty Sludge Pmcsss Britannia Mine AMD Treatment Britannia Beach, B.C. Page 28 ~1 cracking occurred during the drying cycle. The detailed filtering results are presented in

Appendix F.

Table 4.4.6.1 - Clarifier Underflow Sludge Filtering Tests

Test Neutralizing Agent Rate

Cake Moisture (%) tonnes/m3/hr)

BMHDS-3 69.0 0.58 Hydrated Lime

I BMHDS-7 I Precipitator Catch I 3.82 I I 46.7

I BMHDS-8,9810 I Top Ash I 2.47 I 34.6 I 4.4.7 Sludge Drainage Tests

The sludge generated using each type of neutralizing agent was further tested to determine

whether or not it would dewater if disposed of in a freedraining containment area. The table

below shows that dewatering occurred with each sludge type, with increase in percent solids

most significant with the lime-generated sludge. More detailed test results and a graph

(Figure 4.3.5) comparing leachate volume collection over time for the three samples is

provided in Appendix F.

Table 4.4.7.1 - Clarifier Underflow Sludge Drainage Tests .

Neutralizing Agent Final % Solids Initial % Solids Sludge S.G.

Hydrated Lime 26.0 18.1 1.135

Precipitator Catch

Top Ash

46.8 36.1 1.289

48.6 41.3 1.332

Pilot Scale Testlng of the High Density Sludge Process Britannia Mine AMD Treatment Britannia Beach, B.C. Page 29

I 4.5 Reagent Requirements

4.5.1 Air

The basic mechanism for oxidation of ferrous iron to its ferric state is as follows:

Fe '* + 1/402 + H+ + Fe3' + 1nH,0, and

Fe3' + 3H20 + Fe(OH), + 3H'

The efficiency (or rate) with which the oxidation reactions take place are very much

dependent upon the pH of the AMD being treated. It should be noted that the above

reactions combined are acid generating, hence the importance of the presence of ferric iron

for overall long-term sludge stability. When the pH is greater than 8, the oxidation rate is fast

enough that it is not necessary to maintain oxygen saturation for the reactions to take place.

At a pH lower than 8, a much higher dissolved oxygen level is required.

For a pH above 8, the efficiency of oxygen transfer is about 20 percent. For each I gram of

ferrous iron present, approximately 3.5 grams of air or about 0.003 m3 at standard conditions

is required for complete oxidation. Using these numbers, the estimated aeration

requirement for the Britannia AMD (based on mean data from 1996) would be as follows:

AMD Source Air Requirement Fez+ Mean Discharge

(m3/hr) (mg/L) I (kg/hr) I (Std.m3/hr) I (SCFM)

I 2200 adit I 108 I 29 I 3.132 I 11.0 I 6.4 I I 4100 adit I 414 I 5.8 I 2.40 I 8.4 I 4.9 I I 2200+4100 I 522 I 10.6 I 5.53 I 19.4 I 11.3 I

' I Pilot Scale Testing of the High Density Sludge Process Britannia Mine AMD Treatment Britannia Beach, B.C. Page 30

4.5.2 Flocculant

The flocculant used during the pilot-scale testing was Allied Colloids Percol E-IO. Flocculant

consumption for a full-scale plant is very difficult to calculate from the pilot plant data.

Average flocculant consumption ranged between 0.7 mg/L and 5.0 mg/L during testing and

was between 1 and 2 mg/L for most tests. Past experience has shown that flocculant

consumption at the pilot-scale level is usually significantly higher than for a full-scale plant.

4.5.3 Lime

Lime consumption in the HDS process using the 4100 portal AMD and a 41 minute retention

time at pH 9.5 with an underflow recycle ratio of approximately 23:l is expected to be

approximately 0.4 kg/m3 based on the tests conducted here. Lime consumption can be

decreased by increasing the clarifier underflow recycle rate and perhaps by providing a

longer retention time in the HDS circuit, thus giving the lime more time to react. Lowering

the operating pH would also reduce lime consumption although effluent metals

concentrations would be expected to rise. Typically, the HDS process produces a reduction

in lime consumption over straight lime neutralization due to the slow reactivity of lime,

therefore some unreacted lime reports back to the lime/sludge mix tank with the recycled

sludge.

4.5.4 Precipitator Catch and Top Ash

Precipitator catch consumption ranged from 2.3 kg/m3 to 9.1 kg/m3 depending upon the

operating pH and the recycle ratio. Top ash consumption was between 2.8 kg/m3 and 5.4

kg/m3. Because feed and recycle rates as well as operating pH were different for many

tests, it is difficult to compare the consumption rates for a particular set of conditions. An

operating pH of at least 9 and a recycle ratio of at least 8:l would probably be required for

sufficient metals removal.

I Pilot Scale Testing of the High Density Sludge Process Britannia Mine AMD Treatment Britannia Beach, B.C. Page 31

5.0 CONCLUSIONS AND RECOMMENDATIONS

5 1 Conclusions

All project objectives defined in the test proposal were met for the treatment of the Britannia

AMD collected from the 4100 portal and neutralized with lime and combustion ash in the

HDS process. Specifically, these were as follows:

Clarifier underflow solids were consistently greater than 12 percent using lime

neutralization and greater than 30 percent using combustion ash

Analytical results indicated that all metals of concern were precipitated from solution to

below regulation requirements with a pH of at least 9.0

A clean overflow, low in suspended solids was obtained

Free-drained sludge densities of 26, 47 and 49 percent solids were achieved using lime,

precipitator catch and top ash neutralization respectively

Recycle ratios of at least 20:l for lime neutralization and 8:l for combustion ash

neutralization are indicated

It has been demonstrated that the HDS process can be applied successfully to the 4100

portal AMD despite its low iron to total metals ratio. Neutralization can be accomplished

using hydrated lime or pulp mill combustion ash. The effluent from the HDS pilot plant had

reasonable clarity and was low in dissolved metals. Based on extensive CESL experience

with pilot and full scale plants, it is expected that an operating plant will achieve significantly

better clarity. Higher than normal suspended solids resulted in elevated total metals in some

tests where the operating pH was low. The test work undertaken for the pilot plant study

showed that all of the dissolved metals of interest were precipitated to below requirement

limits at the higher end of the operating pH range.

The HDS process also produced an effluent low in metals using feed from the 2100 portal

and lime neutralization.

Pilot Scale Testing of the High Denslty Sludge Plocens Britannia Mine AMD Treatment Britannia Beach, B.C. Page 32

5.2 Recommendations

Based upon the results of this test program, the following recommendations can be made to

Environment Canada regarding the abandoned Britannia mine.

Further testing of combustion ash as a lime replacement should be undertaken to

investigate:

the potential of toxins in the ash (dioxins, for example) being introduced into the

HDS effluent

the long-term stability of the sludge (SWEP or TCLP Testing)

optimum operating conditions

Additional testing should be done on the 2200 adit AMD and an AMD mi) dure that w rould

be representative of the water to be treated by an on-site neutralization plant

A feasibility study should be conducted to determine the costs and benefits of an HDS

treatment plant using lime, combustion ash or a combination of lime and combustion ash

Sludge disposal options should be evaluated. For the lime HDS sludge, these should

include smelter processing with metals recovery and, for the ash HDS sludge, disposal

underground in the mine should be considered.

Sincerely,

Cominco Engineering Services Ltd.

Sohan S. Basra

APPENDIX A

HDS PROCESS WORKSHEETS

Date & Time Cumu Hour!

9/04/97 8:00

15 23:OO 13 21:OO 11 19:oo 9 17:OO 7 15:OO 5 13:OO 3 1l:OO 1 9:oo 0

0/04/97 1:00 17 3:OO 19 5:OO 21 7:OO 23 9:00 25

1l:OO 27 13:OO 29 1500 31 17:OO 33 19:oo

39 23:OO 37 21:oo 35

1/04/97 1:OO 41 3:OO 43 300 45 7:OO 47 9:oo 49

11:OO 51 13:OO 53 1500 55 17:OO 57 19:oo 59 21:OO 61 23:OO 63

2/04/97 1:00 65 3:OO 67 500 69 7:OO 71

PILOT SCALE TESTING OF THE HIGH DENSITY SLUDGE PROCESS BRITANNIA MINE AMD TREATMENT

Table I : Test BYHDS-Commissioning

- - Flow F Feed

1360 1340 1440 1440 1420 1440 1450 1440 1430 1425 1460 1450 1440 1460 1420 1400 1420 1440 1400 1510 1490 1470 1470 1465 1460 1470 1460 1460 1470 1470 1450 1490 1460 1470 1460 1460 1560

-

-

qiii - Floc

2.0 2.0 2.0 2.0 4.0 3.0 3.5 3.2 3.2 3.2 3.2 3.3 5.0 5.0 5.0 5.0 5.5 5.5 5.2 5.2 5.0 4.8 5.0 5.4 5.0 5.1 5.1 5.1 5.1 5.1 5.0 6.0 5.0 4.8 6.5 6.8 6.8

1.25 Pn -

-

linute) - Xar. Uff RGCyCk

0 0 0 0

140 140 140 138 138 137 137 137 137 158 158 194 196 196 194 194 195 196 195 195 196 196 192 196 197 197 226 225 225 227 224 246 244

-

-

- :lar.UF S.G.

-

1.036 1.044 1.047 1.049 1.048 1.043 1.044 1.041 1.047 1.045 1.055 1.058 1.063 1.063 1.067 1.047 1.064 -

- ilar. UIF b solidi

-

10.1

- Ratio

-

30.5 : I

- Lime

onsump

0.0 0.2 0.7 1.5 1.8 2.0 2.2 2.4 3.0 3.5 4.0 4.3 4.5 5.0 5.2 5.6 5.8 6.0 6.3 6.7 7.2 7.8 8.0 8.3 8.8 9.2 9.8 10.0 10.5 11.0 11.0 11.5 12.0 12.3 12.8 13.1 13.5

(L)

-

-I- - teactol

# I 9.0 8.4 9.0 9.5 9.4 9.2 8.8 8.8 9.1 8.9 8.8 8.8 8.9 9.0 8.6 8.4 8.7 8.1 8.8 8.7 8.9 8.5 8.7 9.1 8.9 8.5 9.2 8.7 8.4 9.3 8.9 8.6 9.4 8.7 9.2 8.8 8.9

-

-

#2 9.0 9.4 9.0 9.5 9.0 9.0 9.0 9.1 9.0 8.9 9.1 9.0 8.8 9.0 8.9 8.8 8.7 8.5 9.0 8.8 9.2 8.9 8.8 8.9 9.1 8.9 9.0 9.1 8.8 9.0 9.2 8.9 9.1 9.0 8.9 9.1 9.2

-

-

- lar. Off

9.5

9.0

8.5 9.0 9.0 9.0 9.0 9.0 9.1 9.0 9.0 9.0 9.0 9.0 9.0 9.1 9.0 9.1 9.0 9.0 9.1 9.0 -

Feed Rate: 1449 mUMin Feed pH: 3.3 Clarifier UIF Recycle Rate: 185 mUMin pH in Reactor 1: 8.9 Average Recycle Ratio: 25.8 : 1 pH in Reactor 2: 9.0 Retention Time: 31.8 Minutes pH in Clarifier O/F: 9.0 Solids Generation Rate: 0.50 kgIm3 Reactor Aeration Rate: 5.7 UMin Lime Consumption Rate: 0.328 kglm3 Reactor Temperature: 13 "C Flocculant Consumption Rate: 0.78 mg/L

Date &Time Cumu Hour:

14/04/97 8:OO

15 23:OO 13 21:OO 11 19:oo 9 17:OO 7 1500 5 13:OO 3 11:oo 1 9:oo 0

15/04/97 1:OO 17 3:OO 19 5:OO 21 7:OO 23 9:00 25

11:OO 27 13:OO 29 1500 31 17:OO 33 19:oo

37 21:oo 35

39 23:OO 16/04/97 1:00 41

3:OO 43 5:OO 45 7:OO 47 8:OO 48

PILOT SCALE TESTING OF THE HIGH DENSITY SLUDGE PROCESS BRITANNIA MINE AMD TREATMENT

Table 2 : Test BMHDS-I

- Flow R Feed - - 1380 1360 1320 1390 1360 1380 1380 1400 1390 1380 1380 1360 1360 1360 1380 1380 1360 1370 1370 1360 1380 1370 1360 1360 1360 -

qiii - Floc 1.25 plL - 6.8 5.0 5.0 5.2 5.6 4.8 5.0 5.0 5.0 8.4 8.5 9.4 8.3 9.4 9.5 9.5 9.5 9.0 9.0 9.0 9.0 7.8 7.8 8.0 9.2 -

[inute) - :lar. UIF Recycle

246 I85 185 185 185 186 185 184 I85 I85 184 185 186 185 184 186 186 I85 I85 184 I84 184 184 I84 184

-

-

- :Isr.U/F S.G.

- 1.055 1.067 1.066 1.069 1.072 1.072 1.073 1.074 1.080 1.069 1.078 1.079 1.080 1.086 1.085 1.085 1.086 1.084 1.088 1.087 1.091 1.091 1.098 1.093 1.096 -

- lar. UR b Solid:

-

10.1

10.8

10.3

10.7

11.6

- 12.5

- Recycle

Ratio

-

27.5 :I

30.2 :I

37.9 :I

39.0 :I

42.4 :I

45.7 :I -

- Lime

ionsump

0.0 0.1 0.4 0.6 1.1 1.4 2.1 2.4 2.8 3.1 3.5 3.7 4.6 4.7 5.0 5.5 6.1 6.3 6.5 7.0 7.5 7.8 8.3 8.7 9.2 9.3

(L)

-

I - 7eactor #I 8.2 9.5 9.4 9.5 9.5 9.7 9.5 9.3 9.3 9.8 9.4 9.3 9.7 9.6 9.6 9.5 9.5 9.5 9.3 9.8 9.6 9.4 9.8 9.5 9.5 9.6

-

-

#2 8.5 9.5 9.7 9.6 9.8 10.0 9.8 9.5 9.4 9.9 9.6 9.5 9.7 9.5 9.7 9.6 9.6 9.5 9.5 9.6 9.7 9.5 9.7 9.4 9.5 9.5

-

- L

- ,Jar. OIF

- 9.1 9.2 9.6 9.4 9.6 9.7 9.6 9.5 9.5 9.8 9.6 9.4 9.6 9.6 9.6 9.6 9.5 9.5 9.5 9.7 9.6 9.5 9.6 9.5 9.5 9.5 -

Test Summary

Feed Rate: 1370 mUMin Feed pH: 3.5 Clarifier UIF Recycle Rate: 187 mUMin pH in Reactor 1: 9.5 Average Recycle Ratio: 33.7 : 1 pH in Reactor 2: 9.6 Retention Time: 33.4 Minutes pH in Clarifier OIF: 9.5 Solids Generation Rate: 0.45 kglrn3 Reactor Aeration Rate: 5.7 UMin Lime Consumption Rate: 0.354 kglrn3 Reactor Temperature: 14 "C Flocculant Consumption Rate: 1.38 mg/L

im L Engineering

PILOT SCALE TESTING OF THE HIGH DENSITY SLUDGE PROCESS BRITANNIA MINE AMD TREATMENT

Table 3 : Test BMHDS-2

16/04/97 8:00 0 1200 9:oo 1 1200

11:oo 3 1200 13:OO 5 1200 15:OO 7 1190 17:OO 9 1200 19:OO 11 1230 20:oo 12 1220 21:OO 13 1215 23:OO 15 1200

17/04/97 1:00 17 1200 3:OO 19 1215 5:OO 21 1200 7:OO 23 1200 9:00 25 1200

11:OO 27 1200 13:OO 29 1200 15:OO 31 1200 17:OO 33 1200 19:oo 35 1200 21:oo 37 1200 23:OO 39 1200

16/04/97 1:00 41 1190 3:OO 43 1200 500 45 1180 7:OO 47 1190 8:OO 48 1190

m Floc' 8.125 $1 - 18.0 18.0 18.4 38.0 38.0 60.0 50.0 50.0 42.0 41.3 39.0 46.0 47.0 48.0 51.0 55.0 58.0 58.0 46.0 63.0 58.0 59.0 59.0 62.0 62.0 60.0 60.0 -

linute) - X r . U/F Recycle 250 248 248 248 248 248 247 246 246 247 247 246 246 246 246 246 246 246 246 247 246 246 245 245 245 246 246

-

-

- :lar.U/F S.G.

- 1.096 1.086 1.095 1.100 1.089 1.093 1.084 1 .084 1.085 1.085 1.087 1.087 1.086 1.082 1.090 1.093 1.090 1.091 1.092 1.094 1.091 I .093 1.092 1.092 1.087 1.092 1.092 -

:lar. UIF Recycle 6 Solar Ratio

12.4 73.8 :I

11.8 50.8 :I

12.1 52.8 :I

12.9 66.1 : I

13.4 68.7 :I

12.6 55.0 :I

- Lime

:onsump

0.0 0.1 0.2 0.7 1.1 1.8 2.0 2.2 2.5 3.0 3.5 4.0 4.5 5.0 5.5 6.0 6.5 7.0 6.9 8.2 8.8 9.5 9.8 10.2 10.7 11.5 12.0

(L)

-

- ?eactor

# I 9.5 9.6 9.6 9.6 9.6 9.6 9.5 9.6 9.7 9.7 9.8 9.3 9.4 9.5 9.6 9.5 9.7 9.6 9.5 9.6 9.4 9.4 9.4 9.5 9.5 9.5 9.5

-

-

leacto1 #2 9.5 9.5 9.5 9.7 9.4 9.7 9.6 9.7 9.8 9.8 9.5 9.3 9.3 9.5 9.8 9.5 9.7 9.6 9.5 9.4 9.4 9.4 9.5 9.5 9.5 9.4 9.5

-

-

- :lar. OF

9.5 9.5 9.5 9.7 9.4 9.5 9.4 9.5 9.8 9.6 9.6 9.4 9.4 9.4 9.5 9.5 9.6 9.6 9.5 9.6 9.4 9.4 9.5 9.5 9.5 9.5 9.5

-

-

Feed Rate: 1201 mUMin Feed pH: 3.5 Clarifier U/F Recycle Rate: 247 mUMin pH in Reactor 1: 9.5 Average Recycle Ratio: 59.3 : 1 pH in Reactor 2: 9.5 Retention Time: 35.9 Minutes pH in Clarifier OIF: 9.5 Solids Generation Rate: 0.43 kg/m3 Reactor Aeration Rate: 5.7 UMin Lime Consumption Rate: 0.347 kg/m3 Reactor Temperature: 14 "C Flocculant Consumption Rate: 5.03 mg/L

L m Engineering

late & Time Curnu How

3/04/97 8:OO

13 23:OO 12 21:oo 11 19:oo 10 18:OO 9 17:OO 8 16:OO 7 15:OO 5 13:OO 3 11:oo 1 9:oo 0

3/04/97 1:oo 15 3:OO 17 5:OO 19 500 21 7:OO 23

Test Summaw

PILOT SCALE TESTING OF THE HIGH DENSITY SLUDGE PROCESS BRITANNIA MINE AMD TREATMENT

Table 4 : Test BMHDS-3

- - Flow F Feed

1190 1190 1200 1200 1200 1200 1200

1200

1200 1180 1200 1210 1200 1200

-

-

es(ml - Floc.

55.0 46.0 7.3 9.4 14.0 14.6 14.6

1.125gil -

15.0

15.0 15.0 15.0 15.5 15.0 15.0 -

KiiiGi - :lor. U F Recycle

90 90 90 90 90 90 78

85

84 84 85 85 85 85

-

-

:lar.UF % Solids S.G. Clar. U F

1.085 1.084 1.114 1.125 15.3 1.125 1.115 1.115 1.118 15.8 1.110

1.111 1.115 15.9 1.101 1.115 1.106 15.2 1.111

- Recycle

Ralio T; 23.0 :I

20.5 :I

22.6 :I

21.5 :1 -

0.1 9.6 9.5 0.8 9.6 9.5 1.5 9.6 9.7 2.6 9.6 9.4 3.0 3.5 9.6 9.7 3.7 4.0 9.6 9.7 4.1 4.2 9.4 9.5 4.8 9.4 9.5 5.7 9.3 9.4 6.1 9.4 9.5 6.5 9.4 9.4 7.2 9.5 9.5

- lar. OIF

9.5 9.5 9.5 9.7 9.4

9.5

9.7

9.5 9.5 9.5 9.5 9.5 9.5

-

-

Feed Rate: 1198 mUMin Feed pH: 3.2 Clarifier U/F Recycle Rate: 87 mUMin pH in Reactor 1: 9.5 Average Recycle Ratio: 22.5 : 1 pH in Reactor 2: 9.5 Retention Time: 40.5 Minutes pH in Clarifier OIF: 9.5 Solids Generation Rate: 0.50 kgIm3 Reactor Aeration Rate: 5.7 UMin Lime Consumption Rate: 0.436 kglm3 Reactor Temperature: 15 "C

@YL Engineering .-k;

Date & Time Cumul Hours

21/04/9712:00 I 13:OO 0

11 23:OO 9 21:oo 7 19:oo 5 17:OO 3 1500

22/04/97 1:00 13 3:OO 15 5:OO 17 7:OO 19 9:oo 21

1l:OO 23 13:OO 25 1500 27 17:OO 29 19:OO 31 21:oo 33 23:OO 35

23/04/97 1:OO 37 3:OO 39 500 41 7:OO 43 9:oo 45

11:oo 47 12:OO 48 13:OO 49

PILOT SCALE TESTING OF THE HIGH DENSITY SLUDGE PROCESS BRITANNIA MINE AMD TREATMENT

Table 5 : Test BMHDS4

- Flow R Feed - - I010 I000 1020 1030 1015 I000 I010 1000 980 1060 1070 1040 1042 1040 1040 1040 1040 1040 1040 1032 1050 1038 1040 1039 1040 1040 -

es(ml - Floc. 1.125 fl - 8.2 6.0 6.0 6.5 9.0 9.3 9.5 9.6 17.0 18.0 25.5 23.5 22.5 29.1 30.4 23.7 28.2 30.0 26.0 25.5 24.3 24.1 24.0 24.2 24.0 24.0 -

linute) - :lar. U/F Recycle -

134 137 146 147 150 150 150 150 147 148 148 148 147 147 148 148 149 148 146 146 146 146 146 146 146 -

:lar.U/F %Solid! S.G. Clar. U/i

1.088 1.047 1.078

7.2

1.084

31.0 1.245 1.245 1.231 1.232

29.6 1.236 1.227 1.216 1.205

25.3 1.200 1.203 1.183 1.184

25.2 1.192 22.7 1.174

1.176 1.176

22.4 1.170 19.4 1.130

1.132 1.101

14.5 1.091

- Recycle

Ratio

-

2.1 :I

4.7 :I

6.5 :I 6.8 :I

7.0 : I 7.7 :I

12.2 :I

12.0 :I

- 12.5 :I

- '. Catch :onsump (L)

0.0 1.5 3.0 5.0 6.5 8.0 9.7 11.0 13.0 15.0 16.5 18.5 19.5 20.5 23.0 24.5 26.0 27.5 28.5 30.5 32.0 34.0 35.8 37.8 38.3 36.8 -

- ?eactor

# I 9.6 9.4 8.4 8.5 8.7 8.4 8.4 8.4 8.3 8.3 8.3 8.3 6.2 8.1 8.2 8.2 8.3 8.3 8.2 8.2 8.4 8.3 8.3 8.2 8.2 8.3 8.3

-

-

#2 9.6 9.4 8.5 8.9 9.0 8.8 8.6 8.8 8.6 8.7 8.6 8.6 8.6 8.7 8.5 8.6 8.5 8.5 8.7 8.6 8.6 8.6 8.6 8.7 8.5 8.5 8.5 6.5 8.5 8.5 8.5 8.6 8.6 8.7 8.5 8.6 8.5 8.5 8.6 8.7 8.5 8.6 8.5 8.5 6.5 8.5 6.5 8.5 8.5 8.5 8.5 8.5

Test Summaty

Feed Rate: 1031 mUMin Feed pH: 3.0 Clarifier U/F Recycle Rate: 147 mUMin pH in Reactor 1: 8.4 Average Recycle Ratio: 8.5 : I pH in Reactor 2: 8.6 Retention Time: 44.2 Minutes pH in Clarifier O/F: 8.6 Solids Generation Rate: 3.68 kglm3 Reactor Aeration Rate: 5.7 UMin Precipitator Catch Consurnpt: 5.34 kglm3 Reactor Temperature: 14 "C Flocculant Consumption Rate: 2.37 rng/L

I= Engineering

Date 8 Time Cumu Hours

3/04/9713:00

10 23:OO 8 21:OO 6 19:OO 4 17:OO 2 1300 0

4/04/97 1:00 12 3:OO 14 300 16 6:OO 17 7:OO 18 9:oo 20

11:oo 13:OO

22

30 19:OO 28 17:OO 26 1500 24

PILOT SCALE TESTING OF THE HIGH DENSITY SLUDGE PROCESS BRITANNIA MINE AMD TREATMENT

Table 6 : Test BMHDSS

Test Surnrnaty

Flow Rates (mUMinute) Feed I Floc. I Clar. UIF

Ctar.U/F S.G.

Recycle 84 04 82 84 83 02 03 04 86 85 82 82 02 82 02 82 84

-

-

- 1.245 1.190 1.274 1.262 1.263 1.276 1.278 1.258 1.237 1.261 1.300 1.300 1.302 1.300 1.290 1.275 1.279 -

- tiar. UIF b Solar

31.0

33.7

34.4

35.7

31 .O

36.0

-

35.0 -

Recycle Consump. Ratio P. Catch

7.2 :I 0.0 3.2

7.8 :I 5.4 7.7

8.1 :I 11.7 9.7

13.7 0.4 : I

33.2 7.5 :I 31.4 29.0 26.4 24.2 22.2 20.7 8.2 :I 19.2 17.7 7.4 : I 15.7

(L) teactor

# I 8.6 0.7 8.6 8.6

8.5 0.4 0.6 8.6 8.6 8.7 8.7

-

8.4

8.7

8.7 0.8

8.7 8.7 -

Ifi !eaclol #2 9.0 9.2 9.1 9.1 8.9 8.9 8.0 8.9 0.9 8.8 9.0 9.0 9.0 9.1 9.0 9.1 9.0

-

-

- lar. OF

0.5 9.0 9.1 9.2 9.0 9.0 9.0 9.0 9.0 8.9 8.9 9.0 9.0 9.1 9.0 9.0 9.1

-

-

Feed Rate: 1039 mLlMin Feed pH: 3.0 Clarifier UIF Recycle Rate: 83 mUMin pH in Reactor 1 : 8.6 Average Recycle Ratio: 7.6 : 1 pH in Reactor 2: 9.0 Retention Time: 46.4 Minutes pH in Clarifier O/F: 9.0 Solids Generation Rate: 3.54 kglm3 Reactor Aeration Rate: 5.7 UMin Precipitator Catch Consumpt: 7.40 kglm3 Reactor Temperature: 15 "C Flocculant Consumption Rate: 1.43 mglL

~~~~~ ~~ ~ ~

(m E L ngineering

Date &Time Cumul Hours

24/04/9719:00

4 23:OO 2 21:oo 0

25/04/97 1 :00 6 2:oo 7 3:OO 8 4:OO

14 9:00 12 7:OO 10 500 9 4:05 9

11:OO 16 13:OO 18

PILOT SCALE TESTING OF THE HIGH DENSlTY SLUDGE PROCESS BRITANNIA MINE AMD TREATMENT

Table 7 : Test BMHDS-6

- Flow F Feed - - 1140 1160 1170 1170 1205 1180 1220 1240 1215 1225 1230 1230 1230 -

q - 3 - Floc.

l . m g n

10.9 11.0 10.5 15.6

15.0 15.0 13.0 12.5 12.5 13.0 14.5 14.5

-

-

linute) - 3ar. U/F Recycle

84 62 64 65 56 49 46 242 89 91 92 91 90

-

-

:lar.UIF Clar. UII S.G. %Solidi

1.279 35.6 1.303 1.297 36.5 1.297

1.280 1.329 37.5 1.312 1.299

1.291 37.9 I .289 1.306

- qecyde Ratio

- 7.8 :I

5.9 : I

4.2 :I

8.4 :I

a. Catch Reactor I ReactorlClar. Off :onsump.

PH

4.0 8.0 11.5 13.0 15.2 16.8 16.8 17.8 20.5 23.8 26.2 28.2 -

9.3 9.4 9.2

9.4 9.3 9.3 9.3 9.2 9.2 9.2 9.1 -

9.6 9.5 9.5

9.5 9.5 9.5 9.5 9.5 9.5 9.5 9.4 -

9.4 9.6 9.6

9.6 9.6 9.6 9.6 9.6 9.6 9.5 9.5 -

Test Summary

Feed Rate: 1201 mUMin Feed pH: 3.4 Clarifier UIF Recycle Rate: 86 mUMin pH in Reactor 1: 9.2 Average Recycle Ratio: 7.9 : 1 pH in Reactor 2: 9.5 Retention Time: 40.4 Minutes pH in Clarifier O/F: 9.5 Solids Generation Rate: 3.37 kglm3 Reactor Aeration Rate: 5.7 UMin Precipitator Catch Consumpt: 9.06 kglm3 Reactor Temperature: 15 "C Flocculant Consumption Rate: 1.37 mglL

i@h Engineering

PILOT SCALE TESTING OF THE HIGH DENSITY SLUDGE PROCESS BRITANNIA MINE AMD TREATMENT

Table 8 : Test BMHDS-7

Date &Time pH P. Catch Recyck Clar. Uff Clar.U/F Flow Rates (mUMinute) h m u l Hours Clar. OF Reactor Reactor Consump. Ratio %Solids S.G. Clar. UIF Floc. Feed

(0.125 glL) #2 # I (L) Recyck 25/04/9713:00

1320 6 19:OO 8.8 8.5 8.1 0.6 1.308 51 14.4 1195 4 17:OO 9.1 9.0 8.6 0.6 1.300 89 14.5 1200 2 15:OO 9.5 9.4 9.1 0.0 1.306 90 14.5 1230 0

8.1 7.9 7.8 1.8 4.3 :I 38.5 1.301 32 9.2 1460 10 23:OO 8.3 8.2 7.9 0.6 1.296 47 9.3 1328 9 2200 8.5 8.4 8.0 0.6 1.301 53 10.0 1310 8 21:OO 8.5 8.4 8.0 0.6 7.7 : I 37.6 1.314 52 12.0

26/04/9700:00 11 1480 9.3 32 1.298 2.8 7.7

8.2 8.1 7.8 7.6 17 6:OO 8.2 8.2 7.7 6.8 4.0 :I 36.6 1.268 31 7.5 1440 16 500 8.1 8.0 7.8 5.3 1.304 31 7.5 1470 14 3:OO 8.1 8.1 7.7 3.8 1.298 32 7.2 1450 12 1:00 8.1 8.0

Test Summary

Feed Rate: 1353 mUMin Feed pH: 3.5 Clarifier UIF Recycle Rate: 49 mL/Min pH in Reactor 1: 8.0 Average Recycle Ratio: 7.0 : 1 pH in Reactor 2: 8.4 Retention Time: 37.1 Minutes pH in Clarifier OIF: 8.5 Solids Generation Rate: 1.94 kglm3 Reactor Aeration Rate: 5.7 UMin Precipitator Catch Consumpt: 2.29 kglm3 Reactor Temperature: 15 "C Flocculant Consumption Rate: 0.97 mglL

- i ! Engineering

late 8 Time Cumul Hours

3/04/9712:00

11 23:OO 9 21:oo 7 19:oo 5 17:OO 3 1300 1 13:OO

0.5 12:30 0

3/04/97 1:00 13 3:OO 15 500 17 7:OO 19 7:30 19.5 9:oo 21

11:OO 23 13:OO 25

PILOT SCALE TESTING OF THE HIGH DENSITY SLUDGE PROCESS BRITANNIA MINE AMD TREATMENT

Table 9 : Test BMHDS-8

rn - Feed - 1400 1340 1335 1320 1298 1210 1200 1185 1200 1185 1215

1200 1210 1185 -

es(ml - Floc. l.125gil - 4.0 4.0 3.5 3.5 5.0 5.8 5.8 5.8 9.0 8.9 8.8

8.9 11.0 11.0 -

linute) - :lar. U/F Recycle -

116 117 117 133 134 133 133 135 135 135 134 134 133 -

- :iar.U/F S.G.

1.098 1.088 1.122 1.119 1.145 1.161 1.192 1.191 1.170 1.185 I .206 1.230 1.232 -

- Iar. Un 1 Solid

-

13.6

17.4

20.3

23.7

28.0 30.2 30.7 -

?ecycle Ratio

-

3.3 :I

4.4 :I

6.2 :I

7.1 : I

8.5 :I 9.1 :I 9.4 :I -

- Top Ash :onsump (L)

0.0 1 .o 4.2 7.0 9.5 10.5 12.8 15.5 17.0 19.0

42.0 20.5

22.8 24.2 26.0 -

- leactol # I

8.7 8.6 8.5 8.5 8.5 8.5 8.6 8.5 8.5 8.5 8.8

-

8.5 8.4 8.5 -

eacto #2

9.0 9.2 9.1 9.0 9.0 9.0 9.0 8.9 9.0 8.9 8.9

-

8.9 8.9 9.0 -

lar. OIF

-

9.3 9.0 9.0 9.1 9.0 9.0 9.0 9.0 8.9

8.9 8.9 9.0 -

Test Summary

Feed Rate: 1249 mUMin Feed pH: 3.3 Clarifier U/F Recycle Rate: 130 mUMin pH in Reactor 1: 8.5 Average Recycle Ratio: 6.5 : 1 pH in Reactor 2: 9.0 Retention Time: 37.7 Minutes pH in Clarifier O/F: 9.0 Solids Generation Rate: 3.74 kglm3 Reactor Aeration Rate: 5.7 UMin Top Ash Consumption Rate: 5.37 kglm3 Reactor Temperature: 13 "C Flocculant Consumption Rate: 0.68 mglL

i m Engineering

Date 8 Time Cumu Hourz

29/04/9713:00

10 23:OO 8 21:oo 6 19:OO 4 17:OO 2 15:OO 0

30/04/97 1:00 12 3:OO 14 500 16 7:OO 18 9:oo 20

1l:OO 22 13:OO 24

PILOT SCALE TESTING OF THE HIGH DENSITY SLUDGE PROCESS BRITANNIA MINE AMD TREATMENT

Table I O : Test BMHDSI

Flow Rates (mUMinute) Feed I Floc. I Clar. uff

1205 1200

- :lar.U/F

S.G.

- 1.232 1.250 1.228 1.270 1.274 1.290 1.288 1.289 1.300 1.320 1.308 1.323 1.313 -

- ilar. U/F b soras

30.7 32.5

33.7

36.5

36.3

38.1

38.7 38.4

-

-

9.9 : I

10.6 : I 4.7

7.7

13.0

I - teactor

# I 8.5 8.2 8.6 8.2 8.2 8.2 8.2 8.2 8.2 8.1 8.1 8.2 8.1

-

-

P Reactof #2 9.0 8.6 8.6 8.5 0.5 8.5 8.5 8.5 8.5 8.5 8.5 0.5 8.5

-

-

- lar. OIF

- 9.0 8.7 8.7 8.6 8.5 8.6 8.5 8.5 8.5 8.5 8.5 8.5 8.5 -

Test Summary

Feed Rate: 1200 mUMin Feed pH: 3.6 Clarifier UIF Recycle Rate: 128 mUMin pH in Reactor I : 8.2 Average Recycle Ratio: 10.0 : 1 pH in Reactor 2: 8.5 Retention Time: 39.1 Minutes pH in Clarifier OlF: 8.6 Solids Generation Rate: 3.80 kglm3 Reactor Aeration Rate: 5.7 UMin Top Ash Consumption Rate: 3.65 kglm3 Reactor Temperature: 13 "C Flocculant Consumption Rate: 1.39 mglL

'',=L Engineering ,,-

PILOT SCALE TESTING OF THE HIGH DENSITY SLUDGE PROCESS BRITANNIA MINE AMD TREATMENT

Table 11 :Test BMHDS-10

1350

- Cbr.UII

S.G.

- 1.313 1.312 1.324 1.341 1.324 1.339 1.327 1.322 1.332 1.341 1.336 1.322

- Clrr. UIF %Solids

- 38.4 39.2

40.4

40.1

39.1

41.3

39.9

-

Recycle Ratio

- 12.0 :I 10.4 :I

10.4 :I

10.8 :I

9.9 :I

Top Ash Clar. OIF Reactor Reactor Consump.

pH

(L) 8.1 0.0

#2 #I

7.7 4.5 8.2 8.0 7.7 3.0 0.2 8.0 7.5 2.3 8.3 8.0 7.5 0.7 8.5 8.5

8.2 8.0 7.7 8.7 8.1 8.0 7.6 7.5 8.1 8.0 7.7 6.2 8.1 8.0 7.6 5.0 8.1 8.0

10.6 :I 1 10.5 I 7.7 I 1:; I 1:: 1 10.2 :I 12.5 7.7

11.5 7.6 8.0 8.2

13.5 7.6 8.0 8.2

Test Summary

Feed Rate: 1319 mUMin Feed pH: 3.6 Clarifier UIF Recycle Rate: 108 mUMin pH in Reactor I: 7.7 Average Recycle Ratio: 9.7 : 1 pH in Reactor 2: 8.0 Retention Time: 36.5 Minutes pH in Clarifier OIF: 8.2 Solids Generation Rate: 3.35 kglm3 Reactor Aeration Rate: 5.7 UMin Top Ash Consumption Rate: 2.75 kglm3 Reactor Temperature: 14 "C Flocculant Consumption Rate: 2.06 mgIL

a I I I I I 1 1 I I 1 I I I

1 1 SJ

PILOT SCALE TESTING OF THE HIGH DENSITY SLUDGE PROCESS BRITANNIA MINE AMD TREATMENT

Table 12 : Test BMHDS-I1

Date &Time umul Flow Rates (m b o u r s l m

110 1.102 100 1.094 116 1.093 117 1.096 117 1.091 117 I nap,

Clsr. UiF % Solas

Recycle Ratio

- Lime PH

Consump.

10.3 9.8 9.7 0.0 #2 # I (L)

Clar. OF Reactor Reactor

9.7 9.9 10.2 2.0 9.3

9.5 9.5 9.4 9.3 9.4 9.4 3.0 9.4 9.5 9.5 9.4 9.3 9.3 9.6 9.5

Test Summary

Feed Rate: 943 mUMin Feed pH: 3.1 Clarifier UIF Recycle Rate: 113 mUMin pH in Reactor 1: 9.5 Average Recycle Ratio: NIA pH in Reactor 2: 9.6 Retention Time: 49.2 Minutes pH in Clarifier O/F: 9.7 Solids Generation Rate: NIA kglm3 Reactor Aeration Rate: 5.7 LlMin Lime Consumption Rate: 0.44 kglm3 Reactor Temperature: 15 "C Flocculant Consumption Rate: 9.98 mg/L

~~

APPENDIX B

GRAPHS OF SPECIFIC GRAVITY VS. RUN TIME

FOR INDIVIDUAL TESTS &

PERCENT SOLIDS VS. SPECIFIC GRAVITY

I I I

1

Smcific Gmvltv vs Run Time Test BMHDSCommissloning

1.iw -.

i I

1.080 A- - ~-

"" ___ "" ~ "" ~ - .

"""-----~" "

0 10 20 30 40 54 60 70 Run TIM (hn)

Figure4.1.1

Figure 4.1.2

Specific Gnvltv vs Run Time Test BMHDS-2

1.120

1.060 ' ""

S~eclfic Gnvltv vs Run Time Test BMHDS-3

1.200 ,

Figure 4.1.4 ,- -L-, -. sFS,'L Engineering

I I

I I

0 8 16 24 32 40 Run T i m (hn)

48

Figure 4.1.5

SDecific Gnvitv vs Run Time Test BMHDS-6

1.400 , " ".

~~ ~

!

1.100 J 0 4 8 12 16 20

Run Tlrm (hn)

Figure 4.1.7

Smcific Gravlhr vs Run Time Test BMHDS-7

1.400

1.100 0

-

4 8 12 16 2C

Run Time (hn)

Figure 4.1.8 7-

Engineering -LC-?

S ~ c i f i c Gravltv vs Run T h e Test BMHDS-8

Figure 4.1.9

8 16 24 32 "

40 48

1.400 _-.-

Figure4.1.10 - -~ " , - 7 3 ' ) - Engineering " _-

Clarifier Underflow Percent Solids vs. Smcific Gravitv Tests BMHDSC. 1.2 & 3

I 1

y = 129.05~ - 128.3

~

1.05

6 2~"- . ~ ~ .

1.07 1 .os 1.11 1.13 CIariflw U&mow Sp.clfic Gmvily (k&)

Figure 4.3.1

Clarifier Underflow Percent Solids vs. Swcific Gravity Tests BMHDS4.5.6 & 7

y = 112.46x - 108.86 Rz = 0.9758

i

,- -J 7 "_

is l a j I In ~ I

~

.c 10 10 / +

1 0 4 ! 1.00

, "4 1.05 1.10 1.15 1.20 1.25 1.30 1.35 1.40

ClariMr Undemow Sp~lf ic Gmvily (k&)

Figure 4.3.2

;-

'&%E.% Engineering

I

I

Clarifier Underflow Percent Solids vs. Swcific Gravity Tests BMHDS-O. 9 & 10

45 -~ !

~ ""

35 "

y = 108.45~ - 104.03 Rz = 0.9888

15 L-~-

I

Clarifier Feed Percent Solid8 vs. Swclfic Gravity Tests BMHDS-1 to 10

J

1.00 1.01 1.02 1.03 1 .M 1.05 Clarlflor Feed SpeclRc Gravily (kgh) i

" . ~ - .- ~" -

Figure 4.3.4

I I I I I I I I I I I I I I I I

APPENDIX C

ANALYTICAL RESULTS

I I I I I I I I I I I I I I I I I I I

Pilot Plant Testina of the Hiah Densitv Sludae Process Britannia Mine AMD Treatment

Britannia Beach, British Columbia

Solution Analvoio bv ICP

Element Clarifier Overflow Feed Clarifier Overflow Feed

Test BMHDS-Commissioning-39 Hours Test BMHDS-Commissioning-29 Hours

Dissoived I Total Total Dissolved Total Dissolved Total Dissolved

Ag mglL

Ba mgIL B mgIL As mglL

2.9 1.4 35.2 31.5 1.8 1.1 32.8 31.7 AI mglL c0.1 <0.1 <0.1 co. I co.1 <o. 1 co.1 co.1

Be mglL Ca mg/L Cd mglL Co mglL Cr mgIL

Cu mglL Fe mglL K mg/L Mg mgIL Mn mg/L

Mo mglL Na mglL Ni mg/L P mg/L Pb mglL

S mglL Sb mg/L Se mgIL Si mglL Sn mgIL

Sr mgIL Ti mg/L V mg/L Zn mg/L

'HC mglL "HT mgIL 16401 N/AJ 1660 I N/A] NIA~ N/AI 17401 N/AI 'HC = Hardness, Ca + Mg N/A=Not Analyzed

c0.5

0.03 co.01 0.5 0.5 ~0.6

0.01 0.01 437 451 0.11 0.10 0.14

~0.06 0.07 0.10

19 20 7.49 10.2 1 .o 2.0 82 83

5.78 5.49

co.1 14

<o. 1 12

c0.2 c0.2 -=I <I

~ 0 . 5 ~0.6

529

~ 0 . 6 c0.5 17.9 19.1 ~0.6 ~ 0 . 5 ~0.6 c0.5 538

2.32 2.35 co.02 c0.02 co.1 22.8

co.1 21.7

1430 NIA

<0.5 0.6

<0.01

<0.01 555

~ 0 . 0 5 ~0 .05 0.06

<0.05 ~ 0 . 0 5

< I 66

1.47

co.1 12

c0.2 4

<0.5

489 c0.5 ~ 0 . 5

1.4 <0.5

2.40 c0.02 co. I 0.2

1650

~0.6 0.5

0.03

0.01 562

c0.06 c0.06 co.06

0.47 0.29 2.0 71

1.59

co.1 10

c0.2 < I

c0.6

529 ~0.6 ~0.6

1.3 c0.6

2.59 c0.02 co.1 0.67

NIA

C O S

<0.01 co.01 0.3 0.8 <0.6

0.01 <0.01 441 453 0.09 0.08 0.10 0.13

co.06 ~0.06

19 21 7.55 10.9 1 .o -=I 82 87

5.80 5.86

co.1 <0.1 14 12

c0.2 <0.2 4 < I

c0.5 <0.6

530 574 ~ 0 . 5

c0.6 4 5 19.0 19.1 ~0.6 ~ 0 . 5 c0.6

2.32 2.49 c0.02 c0.02 co.1 co.1 23.0 23.3

NIA N/A

~ 0 . 5

0.03 co.01 0.7 0.6

c0.6

0.01 co.01 581 566

~0 .05 ~0 .06 ~ 0 . 0 5 0.07

~0.06 0.06

0.09 1 .o <0.05 0.5

2 68

C l

57 1 .o 1.1

<0.1 13

c0.1 13

c0.2 c0.2 < I < I

~ 0 . 5 <0.6

510 503 c0.5 ~0.6 ~ 0 . 5 ~0.6

1.4 1.9 C0.5 c0.6

2.53 2.50 0.03 ~0.02 co.1 c0.1 0.12 1.0

1730 N/A

"HT = Hardness. Total

I I I I I I I I I I I I I I I I I I a

Pilot Plant Testina of the Hiah Densitv Sludae Process Britannia Mine AMD Treatment

Britannia Beach. British Columbia

Solution Anahrds bv ICP

BMHDS-1 (21 Hours) BMHDS-1 (48 Hours) BMHDS-1 (31 Hours) Element Clarifw Overflow Feed Clarifar Overflow Feed Clarifer Overflow Feed

Ag mg/L <0.1 C0.i <o.i . < O . l e0.i CO.l <0.1 4 . 1 4 . 1 4 . 1 4 . 1 <0.1 AI mglL

<0.01 cO.01 0.02 cO.01 0.02 <0.01 0.04 0.02 0.02 0.03 0.04 <0.01 Ba mg/L 0.4 0.5 0.4 0.5 0.5 0.7 0.6 0.5 0.4 0.5 0.5 0.5 B mg/L

<0.6 <0.5 ~0.6 <0.5 c0.6 ~0.5 <0.6 ~0.5 c0.6 c0.5 <0.6 <0.5 As mglL 2.3 0.9 34.8 23.5 1.6 0.7 42.6 28.9 2.8 0.9 37.5 33.3

Be mglL <0.01 0.01 ~0.01 ~0 .01 0.01

<0.06 <0.05 0.17 <0.05 0.14 <0.05 0.10 0.11 <0.06 c0.05 0.16 ~0.05 Cr mglL 0.08 ~0.05 0.06 0.06 <0.06 ~0.05 0.10 0.08 c0.06 <0.05 0.13 0.07 Co mglL <0.06 ~0.05 0.09 0.08 <0.06 <0.05 0.16 0.10 ~0.06 c0.05 0.13 0.10 Cd mglL

498 475 369 291 536 520 472 342 552 478 443 399 Ca mglL 4 .01 <0.01 0.01 <0.01 4 . 0 1 CO.01 0.01

Cu mglL 19.9 22.3 ~0.05 1.59 17.2 25.3 ~0.05 0.41 15.0 21.7

0.38 0.15 5.31 4.06 0.45 0.30 6.74 4.90 0.58 0.29 6.13 5.66 Mn mglL 58 54 86 60 69 66 110 72 73 62 97 84 Mg mg/L <I < I 1 I C l < I 1 1 <I <I 2 <I K mg/L

0.44 ~0.05 13.8 2.85 0.18 ~ 0 . 0 5 14.4 1.62 0.78 ~0.05 12.0 7.74 Fe mglL 0.78 ~0.05

MO mglL <0.1 <0.1 ~ 0 . 1 ~ 0 . 1 <0.1 ~ 0 . 1 <0.1 <0.1 <0.1 ~ 0 . 1 ~ 0 . 1 ~ 0 . 1 Na mglL 11 14 11

~0.6 ~0.5 <0.6 <0.5 ~0.6 ~0.5 <0.6 <0.5 ~0.6 <0.5 ~0.6 ~0.5 Pb mg/L <I -=I <I <I <I <I <I <I <I 4 <I 4 P mglL

~ 0 . 2 ~ 0 . 2 <0.2 ~ 0 . 2 ~ 0 . 2 ~ 0 . 2 <0.2 <0.2 c0.2 ~ 0 . 2 <0.2 <0.2 Ni mglL 10 11 10 9 13 12 13 10 12

S mglL 527 583 480 537 446 649 518 518 379 511 455 468 Sb mglL ~0.5 <0.6 < O S c0.6 <0.5 ~ 0 . 6 < O S ~ 0 . 6

~ 0 . 6 ~0.5 ~0.6 <0.5 ~ 0 . 6 ~0.5 <0.6 <0.5 c0.6 <0.5 <0.6 ~0.5 Sn mglL 2.2 1.6 19.8 14.8 1.8 1.4 22.8 16.9 2.5 1.2 20.7 18.7 Si mglL

<0.6 <0.5 <0.6 ~0.5 ~ 0 . 6 c0.5 c0.6 <0.5 c0.6 c0.5 ~0.6 <0.5 Se mglL <0.6 ~0.5 ~ 0 . 6 <0.5

Sr mglL 2.31 2.58 2.41 2.69 1.94 2.89 2.57 2.59 1.64 2.28 2.26 2.33 Ti mglL ~0 .02 0.0500 <0.02 c0.02 <0.02 <0.02 c0.02 <0.02 <0.02 0,0600 ~0.02 <0.02 V mg/L <O.l

0.89 0.05 21.3 16.6 0.44 0.04 26.4 20.0 1.20 0.06 24.8 22.3 Zn mg/L <0.1 <0.1 <0.1 <O.l <0.1 cO.1 cO.1 ~ 0 . 1 ~ 0 . 1 ~ 0 . 1 cO.1

'HC mglL 1340 N/A 1450 N/A 1150 N/A 1570 N/A 976 N/A 1410 N/A "HT mglL 1560 N/A 1460 N/A 1330 N/A 1580 NIA 1130 N/A 1410 NIA 'HC = Hardness, Ca + Mg N/A=Not Analyzed "HT = Hardness, Total

Dissolved Total Dissolved Total Dissolved Total Dbaolved Total Dissolved Total Dissolved Total

Pilot Plant Testing of the Hiah Densitv Sludge Process Britannia Mine AMD Treatment

Britannia Beach, British Columbia

Solution Analysis by ICP

Element Test BMHDS-2 (24 Hours) Test BMHDS-2 (12 Hours) Feed Clarifier Overflow Feed Clarifier OverRow

Dissolved I Total Dissolved I Total Dissolved 1 Total Dissolved I Total Ag mg/L co.1 I c0.1 co.1 I co.1 co.1 I co.1 co.1 I co.1 AI mglL As mg/L B mglL Ba mglL

Be mglL Ca mg/L Cd mg/L Co mglL Cr mglL

cu mglL Fe mg/L K mglL Mg mglL Mn mg/L

Mo mg/L Na mg/L Ni mg/L P mglL Pb mg/L

S mg/L Sb mg/L Se mg/L Si mglL Sn mglL

Sr mg/L Ti mg/L V mg/L Zn mg/L

'HC mg/L

21.3 c0.5 0.4

co.01

<0.01 247

~ 0 . 0 5 ~0 .05 ~ 0 . 0 5

13.0 5.05

< I 54

3.54

co.1 9

c0.2 < I

~ 0 . 5

330 ~ 0 . 5 < O S 12.2 c0.5

1.47 <0.02 co.1 14.0

840

29.2 ~ 0 . 6 0.6

0.01

0.01 328 0.06 0.06

CO.06

18.7 9.53

< I 73

4.76

co.1 10

co.2 < I

~ 0 . 6

463 c0.6 ~ 0 . 6 16.4 ~ 0 . 6

2.02 co.02 co.1 19.4

N/A

1.4 ~ 0 . 5 0.4

co.01

co.01 355

~ 0 . 0 5 ~ 0 . 0 5 ~ 0 . 0 5

~ 0 . 0 5 ~0 .05

41 <I

0.1 5

co.1 9

c0.2 < I

~ 0 . 5

347 < O S ~ 0 . 5

1.1 c0.5

1.73 c0.02 co.1 c0.02

1050

2.5 ~ 0 . 6 0.4

co.01

0.01 414

~0.06 c0.06 c0.06

0.72 0.34

46 < I

0.33

co.1 9

c0.2 < I

~ 0 . 6

410 ~ 0 . 6 ~ 0 . 6

~ 0 . 6 1.6

1.97 co.02 co.1 0.74

NIA

26.9 c0.5 0.4

co.01

co.01 306 0.06

~ 0 . 0 5 ~ 0 . 0 5

15.6 I .83

67 < I

4.48

co.1 I1

c0.2 < I

~ 0 . 5

404 ~ 0 . 5 ~ 0 . 5 14.7 ~ 0 . 5

1.82 <0.02 co.1 17.8

1040

31.5 ~ 0 . 6

0.01 0.5

0.01 353 0.10

c0.06 co.06

19.6 7.62

< I 79

5.13

co.1 10

co.2 -=I

~ 0 . 6

497 ~ 0 . 6 ~ 0 . 6 17.4 ~ 0 . 6

2.17 <0.02 co. 1 20.9

N/A

0.9 c0.5 0.3

<0.01

co.01 395

<0.05 ~ 0 . 0 5 ~ 0 . 0 5

~ 0 . 0 5 0.1 < I 45

0.15

co.1 10

c0.2 < I

~ 0 . 5

382 ~ 0 . 5 C O S

1.3 ~ 0 . 5

1.95 co.02 <o. 1 0.02

1170

2.1 <0.6 0.6

<0.01

0.01 410

c0.06 c0.06 c0.06

0.45 0.16

46 < I

0.30

c0.1 10

c0.2 < I

~ 0 . 6

409 ~ 0 . 6 ~ 0 . 6

1.5 ~ 0 . 6

2.02 c0.02 c0.1 0.48

N/A I-HT mglLl 9781 N/AI IMOl N/A~ 12101 N/AI 11801 N/AI 'HC = Hardness, Ca + Mg N/A=Not Analyzed *'HT = Hardness. Total

'&&% Engineering ^i "C

Pilot Plant Testina of the Hiah Densitv Sludae Process Britannia Mine AMD Treatment

Britannia Beach. British Columbia

Solution Analvsis bv ICP

A i mglL As mglL B mglL Ba mg/L

Be mglL Ca mg/L Cd mglL co mglL Cr mg/L

Cu mglL Fe mg/L K mg/L Mg mg/L Mn mglL

Mo mg/L Na mg/L Ni mg/L P mg/L Pb mg/L

S mg/L Sb mg/L Se mglL Si mg/L Sn mg/L

Sr mg/L Ti mglL V mg/L Zn mg/L

'HC mg/L

23.5 C O S 0.4

co.01

<0.01 271

<0.05 <0.05 <0.05

13.8 5.26

< I 59

3.87

<0.1 10

<0.2 < I

<0.5

359 C O S ~ 0 . 5 12.9 < O S

1.61 <0.02 co.1 15.5

920

33.8 ~ 0 . 6 0.7

0.01

0.01 380 0.09 0.09

CO.06

20.9 10.3 I .o 85

5.54

co.1 12

c0.2 C l

~ 0 . 6

534 ~ 0 . 6 ~ 0 . 6 19.2 ~ 0 . 6

2.33 c0.02 co.1 22.5

NIA

1.1 < O S 0.5 0.0

eo.01 392

<0.05 <0.05 ~ 0 . 0 5

~ 0 . 0 5 <0.05

< I 44

0.13

<o. 1 10

<0.2 c l

< O S

372 <0.5 < O S

1.5 < O S

1.91 c0.02 <0.1 0.02

1160

2.0 ~ 0 . 6 0.5

0.02

co.01 488

c0.06 co.06 co.06

0.40 0.10

< I 54

0.29

co.1 10

c0.2 < I

<0.6

482 ~ 0 . 6 ~0.6

1.3 e0.6

2.39 c0.02 co.1 0.35

N/A

28.4 < O S 0.3

<0.01

0.01 326 0.07

~ 0 . 0 5 <0.05

15.9 2.35

< I 71

4.71

co.1 13

<0.2 < I

<0.5

428 0.6

<0.5 15.3 <0.5

1.93 <0.02 co.1 18.8

1110

34.5 <0.6

0.5 co.01

0.01 391 0.07 0.07

co.06

20.8 10.4

< I 87

5.67

e0.1 12

co.2 C l

c0.6

551 c0.6 <0.6 18.6 <0.6

2.39 co.02 co.1 23.1

NIA

0.9 <0.5 0.5

<0.01

<0.01 466

<0.05 ~ 0 . 0 5 ~ 0 . 0 5

~ 0 . 0 5 <0.05

4 52

0.22

<o. 1 11

c0.2 < I

< O S

44 1 <0.5 ~ 0 . 5 0.8

< O S

2.21 <0.02 <0.1 0.02

1380

1.9 ~ 0 . 6 0.5

c0.01

<0.01 489

~0 .06 c0.06 < O M

0.48 0.27

< I 55

0.38

<0.1 10

c0.2 < I

~ 0 . 6

487 <0.6 0.7 1.4 <0.6

2.35 <0.02 <0.1 0.46

N/A I"HT mg/Ll 10701 N/A~ 11701 N/A~ 12801 N/A~ 13801 N/AI 'HC = Hardness, Ca + Mg MA-Not Analyzed "HT = Hardness, Total

"?&k Engineering ,,-

Pilot Plant Testina of the Hiah Densihr Sludge Process Britannia Mine AMD Treatment

Britannia Beach, British Columbia

Solution Analvsic bv ICP

Element Test BMHDSJ (23 Hours) Test BMHDS-3 (13 Hours) Feed Clarifier Overflow Feed Clarifier Overffow

Dissolved I Total Dissolved I Total Dissolved I Total Dissolved I Total Ag mglL co.1 I co. 1 co.1 I GO.1 co.1 I co.1 co.1 I <0.1 A i mg/L As mg/L B mglL Ba mg/L

Be mglL Ca mglL Cd mglL Co mglL Cr mglL

Cu mglL Fe mg/L K mglL Mg mg/L Mn mglL

Mo mglL Na mglL Ni mglL P mglL Pb mglL

S mglL Sb mg/L Se mg/L Si mglL Sn mglL

Sr mglL Ti mglL V mglL Zn mglL

'HC mglL

30.3 C O S 0.4

<0.01

<0.01 342 0.08 0.05

~ 0 . 0 5

18.0 6.49 1 .o 76

4.99

co.1 10

c0.2 <I

~ 0 . 5

479 ~ 0 . 5 ~ 0 . 5 16.6 C O S

2.13 c0.02 co.1 19.8

1170

36.5 c0.6 0.4

0.02

<0.01 410 0.15 0.12 0.12

21.6 10.90

2.0 90

5.84

co.1 13

c0.2 <I

c0.6

560 ~0.6 ~0.6 20.0 ~ 0 . 6

2.48 c0.02 GO.1 24.1

NIA

0.7 ~ 0 . 5 0.5

co.01

-=0.01 444

~ 0 . 0 5 <0.05 ~ 0 . 0 5

~0.05 ~0.05

2.0 58

0.20

co.1 10

<0.2 -=I

~ 0 . 5

448 <0.5 < O S

1.3 ~ 0 . 5

2.27 c0.02 co.1 0.04

1350

2.3 ~0.6 0.5

<0.01

co.01 510

~0.06 <0.06 0.17

0.68 0.28

1.0 66

0.34

CO. 1 12

c0.2 < I

<0.6

503 ~0.6 ~0.6

1.8 ~ 0 . 6

2.54 c0.02 co.1 0.68

NlA

28.3 ~ 0 . 5 0.4

co.01

co.01 319 0.08 0109

~ 0 . 0 5

16.9 6.09

1 .o 71

4.65

co.1 10

G0.2 <I

<0.5

448 ~ 0 . 5 ~ 0 . 5 15.5 ~ 0 . 5

1.99 e0.02 co.1 18.7

1090

34.9 ~ 0 . 6 0.5

0.02

co.01 394 0.10 0.13 0.07

20.7 10.10

1.0 86

5.62

co.1 12

c0.2 4

<0.6

536 ~0.6 ~ 0 . 6

~0.6 18.8

2.39 c0.02 co.1 23.4

NIA

1.1 ~ 0 . 5 0.5

co.01

<0.01 498

~ 0 . 0 5 ~0.05 <0.05

~ 0 . 0 5 C0.05

2.0 67

0.34

CO.1 13

c0.2 <I

c0.5

503 <0.5 ~ 0 . 5 1.1 C0.5

2.50 G0.02 co.1 0.05

1520

2.6 ~0.6 0.5

0.01

c0.01 562

~0.06 C0.06 C0.06

0.73 0.25

< I 75

0.54

c0.1 13

c0.2 < I

~0.6

555 ~ 0 . 6 ~ 0 . 6

1.9 <0.6

2.74 c0.02 g0.1

0.76

NIA I-HT mg/Ll 13601 NlA 13501 NIA~ 12701 N ~ A I 1530) NIA~ 'HC = Hardness, Ca + Mg N/A=NoI Analyzed "HT = Hardness. Total

@$$ - Engineering

Element

Ag mglL AI mglL As mglL B mglL Ba mglL

Be mg/L Ca mglL Cd mglL Co mglL Cr mglL

Cu mg/L Fe mglL K mgll Mg mglL Mn mglL

Mo mgll Na mgll Ni mgll

Pb mgll

S mgll Sb mgll Se mgll Si mgll Sn mgll

Sr mgll Ti mgll V mgll Zn mgll

P mgll

‘HC mgll

Pilot Plant Testina of the Hiah Densitv Sludae Process Britannia Mine AMD Treatment

Britannia Beach. British Columbia

Solution Analvsis bv ICP

Test BMHDS-4 (35 Hours) Clarifier Overflow Feed Clarifier Overflow Feed

Test BMHDS-I (48 Hours)

Dissolved I Total Disfoived I Total Dissolved I Total Dissolved I Total <O.l I <O.l co.1 I <O.l <O.l I so.1 <0.1 I co.1

- - - -

- ‘HC = Hardness, Ca + Mg **HT Hardness. Total

33.4 < O S 0.5

<0.01

<0.01 329 0.09 0.06 0.06

19.8 9.49 2.0 78

5.04

<0.1 12

<0.2 < I

<0.5

480 <0.5 <0.5 17.2 <0.5

2.06 <0.02 <0.1 18.2

1140

35.9 ~ 0 . 6

0.01 0.5

co.01 354 0.10 0.09

~ 0 . 0 6

21.1 13.8 2.0 82

5.29

<0.1 11

c0.2 <I

e0.6

503 c0.6 ~ 0 . 6

<0.6 18.4

2.16 <0.02

eo.1 19.9

NlA

~0.5 ~0.5

1.5 0.1 1

<0.01 489

<0.05 ~0.05 ~0.05

<0.05 <0.05

140 75

2.17

<0.1 341 <0.2 <I

~0.5

659 <0.5 ~0.5 2.3 <0.5

2.68 <0.02 GO.1 0.31

1530

0.7

1.6 0.16

co.01 561

c0.06 c0.06 <0.06

~ 0 . 6

0.17 0.22 158 85

2.47

382 0.1

c0.2 <I

~ 0 . 6

731 e0.6 <0.6 3.0

~ 0 . 6

3.01 <0.02

eo.1 0.58

NIA

33.7 < O S 0.4

<0.01

<0.01 328 0.10 0.10 0.06

20.1 9.43 I .o 78

5.05

<0.1 11

c0.2 C l

< O S

479 <0.5 e0.5 17.5 < O S

2.06 <0.02

co.1 18.2

1140

40.0 <0.6 0.5

0.02

<0.01 390 0.15 0.10

<0.06

23.6 14.9 1.0 91

5.86

<0.1 13

<0.2 < I

~ 0 . 6

551 <0.6 ~ 0 . 6 20.9 <0.6

2.38 0.03 GO.1 21.9

NIA

~0.5 <0.5

1.3 0.13

<0.01 431

~0.05 <0.05 ~0.05

~0.05 C0.05

118 67

1.95

eo.1 288 c0.2

< I ~0.5

569 ~0.5 <0.5

< O S 1.8

2.34 <0.02 <0.1 0.35

1350

~ 0 . 6 0.91 1.6

0.16

<0.01 577

<0.06 <0.06 <0.06

0.17 0.35 158 87

2.56

<O.l 381 <0.2 <I

<0.6

744 ~ 0 . 6 <0.6 3.3

~ 0 . 6

3.04 <0.02 <0.1 0.82

NlA 13501 NIA( 15401 N/AI 13501 N/AI 13601 NIA

NIA-Not Analyzed

&&L Engineering “e ~

-

Pilot Plant Testina of the Hiah Densitv Sludae Process Britannia Mine AMD Treatment

Britannia Beach, British Columbia

Solution Analvsis bv ICP

Element Test BMHDS-5 (24 Hours) Test BMHDS-5 (12 Houn) Feed Clarifier OverRow Feed Clarifier Overflow

Dissolved I Total Dissolved I Total Dissolved I Total Di550ived 1 Total Ag mglL co.1 I co.1 co.1 I co.1 co.1 I co. 1 co.1 I GO. 1 AI mglL As mglL B mglL Ba mglL

Be mg/L Ca mglL Cd mglL Co mglL Cr mglL

Cu mglL Fe mglL K mglL Mg mglL Mn mglL

Mo mglL Na mglL Ni mglL P mglL Pb mglL

S mglL Sb mglL Se mglL Si mglL Sn mglL

Sr mglL Ti mglL V mglL Zn mglL

'HC mglL

31.3 < O S 0.5

0.01

<0.01

0.09 0.14 0.15

19.1 8.20 3.0 74

4.93

co.1 16

c0.2 < I

~ 0 . 5

463 c0.5 < O S 17.2 c0.5

348

2.03 0.04 co.1 18.2

1170

35.9 ~ 0 . 6 0.5

0.04

0.01 400 0.12 0.20 0.15

22.4 12.3 3.0 a8

5.81

co.1 19

<0.2 < I

~ 0 . 6

541 c0.6 c0.6 19.8 c0.6

2.34 0.07 co.1 22.3

NIA

0.5

1.3 0.15

<0.01 540

~ 0 . 0 5 0.06

c0.05

c0.5

0.23 c0.05

160 70

1.31

0.1 390 c0.2

< I 0.5

728 < O S c0.5 2.8

< O S

2.80 0.03 co.1 0.22

1630

1.6 ~ 0 . 6

1.8 0.17

co.01 615

co.06 co.06 ~0.06

0.27 0.36 190

1.63

co.1 454 c0.2

< I c0.6

a5

a16 <0.6 c0.6 3.2

~ 0 . 6

3.34 c0.02

co.1 0.86

NlA

27.4 c0.5 0.5

co.01

<0.01 320 0.06

~ 0 . 0 5 c0.05

16.8 6.37

65 4

4.48

co.1 12

c0.2 < I

c0.5

471 ~ 0 . 5 c0.5 16.3 c0.5

1 .85 c0.02

co.1 17.1

1070

36.0 c0.6

0.5 0.02

0.02 431 0.10 0.07

co.06

22.8 11.5 1 .o 89

6.08

co.1 13

c0.2 -=I

c0.6

570 c0.6 c0.6 20.0 ~ 0 . 6

2.51 c0.02 co.1 23.7

NIA

0.9 c0.5

1.6 0.16

co.01 550

~ 0 . 0 5 c0.05 ~ 0 . 0 5

0.25 ~0.05

187 64

0.77

0.1 445 c0.2

< I < O S

678 ~ 0 . 5 c0.5

1.7 c0.5

2.83 c0.02 co.1 0.12

1640

1.7 ~ 0 . 6

1.6 0.18

0.02 565

c0.06 c0.06 c0.06

0.24 0.25 192 70

0.93

453 0.1

c0.2 < I

~ 0 . 6

733 ~ 0 . 6 c0.6 2.7

c0.6

2.99 c0.02 c0.1 0.70

NlA 1-HT mg/Ll 13701 NIA 16401 N/AI 12401 NIA~ 1640 I N/AI 'HC = Hardness, Ca + Mg N/A=Not Analyzed "HT = Hardness. Total

tm Engineering

Pilot Plant Testina of the High Densitv Sludge Process Britannia Mine AMD Treatment

Britannia Beach. British Columbia

Solution Analvsk bv ICP

A i mglL As mg/L B mglL Ba mglL

Be mglL Ca mglL Cd mglL Co mglL Cr mglL

Cu mg/L Fe mg/L K mg/L Mg mglL Mn mglL

Mo mglL Na mglL Ni mglL P mglL Pb mglL

S mglL Sb mglL Se mglL Si mglL Sn mglL

Ti mg/L Sr mglL

V mglL Zn mglL

23.1 ~0.5

0.5 <0.01

<0.01 314 0.08 0.09 0.06

14.9 4.54

3.0 60

4.15

<0.1 16

e0.2 <I

<0.5

390 < O S ~ 0 . 5 14.3 <0.5

I .80 0.03 <O.l 16.6

1030

30.5

0.7 0.03

0.01 415 0.14 0.09 0.07

20.2 9.58 2.0 81

5.64

<o. 1 19

c0.2 <I

<0.6

<0.6

526 <0.6 ~ 0 . 6 18.8 ~ 0 . 6

2.39 0.03 co.1 23.0

NIA

0.7 ~ 0 . 5

1.4 0.18

<0.01 544

<0.05 <0.05 e0.05

~ 0 . 0 5 q0.05

258 56

0.21

608 0.2

c0.2 <I

<0.5

764 <0.5 <0.5

1.8 ~ 0 . 5

2.86 <0.02 <0.1 0.06

1590

1.7 <0.6

0.21 1.6

0.02 538

~0.06 ~0.06 C0.06

0.25 0.21 264

58 0.34

0.2 614 c0.2 <I

<0.6

736 0.7

e0.6 2.6

~ 0 . 6

2.88 <0.02 <0.1 0.60

NIA

24.7 <0.5 0.4

<0.01

<0.01 337 0.09 0.08 0.05

16.3 4.56 1 .o 64

4.51

<0.1 13

c0.2 <l

~ 0 . 5

494 <0.5 <0.5 16.7 ~0.5

1.95 <0.02 <0.1 18.1

1110

26.4 <0.6 0.6

0.02

<0.01 370 0.07 0.07

< O M

17.6 8.29 4 71

4.98

co.1 13

c0.2 <I

<0.6

465 <0.6 <0.6 17.2 <0.6

2.1 I <0.02 co.1 20.8

N/A

0.8 <0.5 I .4

0.17

<0.01 553

<0.05 <0.05 <0.05

0.10 <0.05

216 53

0.29

0.1 499 <0.2 <I

< O S

659 <0.5 ~ 0 . 5

1.4 < O S

2.83 <0.02 <0.1 0.08

1600

1.3 <0.6

1.4 0.21

0.01 595

<0.06 <0.06 <0.06

0.29 0.53 228 60

0.44

52 1 0.2

e0.2 <I

<0.6

733 <0.6 <0.6

3.1 ~ 0 . 6

3.09 0.03 <0.1 0.84

'HC mg/L "HT mglL 11801 N/A~ 15901 NIA~ 12701 N/A] 16001 'HC = Hardness, Ca + Mg N/A=Not Analyzed "HT = Hardness, Total

Pilot Plant Testing of the Hiah Densihr Sludae Process Britannia Mine AMD Treatment

Britannia Beach, British Columbia

Solution Analvsis bv ICP

Element Test BMHDS-7 (17 Hours) Test BMHDS-7 (8 Hours) Feed Clarifier Overtlow Feed Clarifier OverRow

Dissolved I Total Dissolved I Total Dissolved I Total Dissolved I Total Ag mglL co.1 I <0.1 <0.1 I co.1 <0.1 I c0.1 eo.1 I eo.1 AI mglL As mglL B mg/L Ba mglL

Be mglL Ca mglL Cd mglL Co mglL Cr mglL

Cu mglL Fe mglL K mglL Mg mglL Mn mglL

Mo mglL Na mglL Ni mglL P mglL Pb mglL

S mglL Sb mg/L Se mglL Si mglL Sn mglL

Sr mglL Ti mglL V mglL Zn mglL

'HC mglL "Hi mglL 12901 NIA~ 16401 N/A~ 13801 N ~ A I 15801 N/A~ 'HC = Hardness, Ca + Mg NIA-Not Analyzed *'HT = Hardness, Total

24.5 ~0.5

30.4

<0.01 <0.01 0.4 0.4

<0.6

<0.01 qo.01 342 437 0.07 0.10 ~0.05 <0.06 d0.05 <0.06

16.3 20.7 4.18 8.79

< I 66

1 .o 83

4.47 5.71

<O.l co.1 10 16

s0.2 c0.2 < I < I

<OS <0.6

412

~ 0 . 6 < O S 19.9 15.4 <0.6 <0.5 0.6 <0.5 552

2.03 2.51 <0.02 G0.02 <0.1 co.1 18.0 23.1

1130 NlA

~0.5 ~0.5

1.3 0.08

<0.01 543

~0.05 e0.05 <0.05

<0.05 <0.05

16 66

2.63

co.1 42

c0.2 < I

<0.5

505 <0.5 <O S 2.4 <0.5

2.58 co.02

CO. 1 0.64

1630

0.8 <0.6

1.4 0.12

0.01 633

<0.06 ~0.06 <0.06

0.26 0.32

18 76

3.05

<0.1 52

<0.2 4

~ 0 . 6

607 <0.6 ~ 0 . 6 3.8

<0.6

2.87 c0.02 <0.1 1.24

NIA

25.6

1.1 0.3 0.3 <0.5 e0.6 ~0.5 <0.5 28.6

<O.Ol <0.01 0.14

<0.01 <0.01 37 I 426

<0.01 525

0.08 0.10 ~0.05 0.07 0.09 e0.05 <0.05 <0.06 ~0.05

17.0 19.3 0.07 I .25 1.48 ~0.05

< I < I 96 70 80 64

4.82 5.45 2.68

co.1 15

<0.1 17

<0.1 233

<0.2 e0.2 c0.2 < I < I < I

< O S ~ 0 . 6 < O S

441

~ 0 . 5 <0.6 ~0.5 3.6 10.8 16.7 e0.5 ~ 0 . 6 ~0.5 <O S <0.6 c0.5 577 531

2.16

0.66 22.4 19.9 <0.1 <0.1 <0.1

c0.02 <0.02 <0.02 2.57 2.44

1210 NlA 1570

0.9 ~ 0 . 6

1.1 0.19

0.01 576

c0.06 0.08 0.09

0.45 0.37 106 71

2.99

2500 0.1

<0.2 < I

~ 0 . 6

619 ~ 0 . 6 e0.6 3.8

<0.6

2.75 0.12 <0.1 1.08

NIA

'\;z9 , , Engineering

Pilot Plant Testina of the Hiah Densitv Sludae Process Britannia Mine AMD Treatment

Britannia Beach. British Columbia

Solution Analysis bv ICP

Element Test BMHDS-8 (24 Hours) Feed I Clarifier Overflow

Ag mglLl Dissolved I Total

co.1 I 0.1 I co.1 I c0.1 A/ mglL As mglL B mglL Ba mglL

Be mglL Ca mg/L Cd mglL Co mglL Cr mglL

Cu mglL Fe mglL K mglL Mg mglL Mn mglL

Mo mglL Na mglL Ni mglL P mglL Pb mglL

S mglL Sb mglL Se mglL Si mglL Sn mglL

Sr mglL Ti mglL V mglL Zn mglL

'HC mg/L "HT mglL 12801 N/AI 13801 NIA~ 'HC = Hardness, Ca + Mg N/A=Not Analyzed

21.3 ~0.5 0.3

<0.01

co.01 350

~0.05 ~ 0 . 0 5 ~0.05

15.1 2.1 1

< I 63

4.29

co.1 6

c0.2 < I

~0.5

407 ~ 0 . 5 ~0.5 14.8 ~0.5

2.10 c0.02 co.1 19.4

1130

24.9 ~0.5 0.3

co.01

0.01 414 0.10 c0.06 c0.m

17.9 8.70 <I 74

5.03

co.1 9

c0.2 -4

c0.6

505 ~ 0 . 6 c0.6 17.5 c0.6

2.43 c0.02

0. I 22.7

NIA

0.9

0.05 0.8 0.8

~ 0 . 6 ~0.5 0.9

0.08

<0.01 0.01 466 558

~ 0 . 0 5 ~0.06 ~0.05 ~0.06 ~ 0 . 0 5 ~ 0 . 0 6

~ 0 . 0 5 0.27 ~ 0 . 0 5 0.36

60 75 51 61

0.99 1.26

co.1 164

c0.1 193

c0.2 c0.2 4 < I

~0.5 ~ 0 . 6

486

~ 0 . 6 < O S ~ 0 . 6 ~0.5 579

2.1 2.8 ~0.5 <0.6

2.30 2.69 c0.02 c0.02 co.1 c0.1 0.09 0.42

1370 NIA

"HT = Hardness. Total

Pilot Plant Testina of the Hiah Densitv Sludge Process Britannia Mine AMD Treatment

Britannia Beach. British Columbia

Solution Anrlvsis bv ICP

A i mglL As mglL B mglL Ba mglL

Be mglL Ca mglL Cd mglL Co mglL Cr mglL

Cu mglL Fe mglL K mglL Mg mglL Mn mglL

Mo mglL Na mglL Ni mglL P mg/L Pb mglL

S mglL Sb mglL Se mg/L Si mglL Sn mglL

Sr mglL Ti mglL V mglL Zn mglL

17.1 < O S 0.3

<0.01

co.01 346

~ 0 . 0 5 <0.05 ~ 0 . 0 5

12.6 1.68 4 53

4.01

<O.l 15

c0.2 4

~ 0 . 5

390 ~ 0 . 5 ~ 0 . 5 12.7 ~ 0 . 5

I .84 c0.02 co.1 18.9

I080

20.3 ~ 0 . 6 0.3

<0.01

<0.01 354

~0 .06 0.06 0.08

14.4 4.96

61 <I

4.25

co.1 15

<0.2 4

~ 0 . 6

430 ~ 0 . 6 ~ 0 . 6 13.9 ~ 0 . 6

2.03 <0.02 co.1 20.4

NIA

~ 0 . 5 < O S 0.7

0.05

co.01 477

~0.05 ~ 0 . 0 5 ~ 0 . 0 5

0.28 0.1 1

49 56 I .94

co.1 120 0.3 <I 0.7

467 ~ 0 . 5 ~ 0 . 6 3.0

~ 0 . 5

2.21 c0.02 <o. I 0.32

1420

0.7 ~ 0 . 6 0.9

0.06

<0.01 504

co.06 0.1

co.06

0.31 0.27

53 64

2.18

CO.1 140

c0.2 -=I

<0.6

529 ~ 0 . 6 ~0.6 2.9

~ 0 . 6

2.52 <0.02 co.1 0.65

NIA

22.0 ~ 0 . 5 0.3

co.01

co.01 368

~ 0 . 0 5 <0.05 ~ 0 . 0 5

15.3 I .89

65 -4

4.42

co.1 11

<0.2 <I

~ 0 . 5

456 <0.5 ~ 0 . 5

~ 0 . 5 14.8

2.19 c0.02

0.1 21.7

1190

22.6 <0.6 0.3

<0.01

<0.01 409 0.1

0.09 co.06

16.3 5.86 <I 69

4.83

<O.l 13

<0.2 <I

e0.6

492 ~ 0 . 6 ~ 0 . 6 15.7 <0.6

2.34 c0.02 co.1 23.7

NlA I

0.5 ~ 0 . 5 0.7

0.04

CO.01 473

~ 0 . 0 5 ~ 0 . 0 5 ~0.05

~ 0 . 0 5 ~ 0 . 0 5

49 52

1.73

co.1 130

c0.2 <I

~ 0 . 5

481 c0.5 ~ 0 . 5 2.3

c0.5

2.21 <0.02

0.1 0.24

1390

1.01 ~ 0 . 6

'HC mglL "HT mglL 1 N/AI NlAI 1400 I 13401 N/A I 14301 N/A 12101 'HC = Hardness. Ca + Mg N/A=Nat Analyzed

1 .o 0.07

c0.01 580

c0.06 c0.06 c0.06

0.26 0.21

64 70

2.26

c0.1 170

<0.2 <I

~ 0 . 6

605 ~ 0 . 6 ~ 0 . 6

3.6 ~ 0 . 6

2.86 c0.02 c0.1 0.68

NIA

'WT = Hardness, Total

Pilot Plant Testina of the Hiah Densitv Sludge Process Britannia Mine AMD Treatment

Britannia Beach. British Columbia

Solution Analvsis bv ICP

Element Test BMHDS-I1 (12 Hours) Feed

Dissolved I Clarifier Overflow

Dissolved I Total Total

Ag mglL AI mglL As mglL B mglL Ba mglL

co.01 I co.01 co.01 I co.01

Be mglL Ca mglL Cd mglL Co mglL Cr mglL

Cu mglL Fe mglL K mg/L Mg mglL Mn mglL

Mo mglL Na mglL Ni mglL P mglL Pb mglL

S mglL Sb mglL Se mglL Si mglL Sn mglL

Sr mglL Ti mglL V mglL Zn mglL

'HC mglL "HT mglL 8401 NIA~ 14701 N/AJ *HC = Hardness, Ca + Mg WA-Not Analyzed "HT = Hardness, Total

42.4 ~ 0 . 0 5 0.02

0.010

0.003 105

0.169 0.056 0.021

67.8 39.9 0.4

47.5 2.92

co.01 2.9

0.05 0.1

c0.05

302 0.14

~ 0 . 0 5 18.8

c0.05

0.291 0.013 co.01 27.0

457

45.1 co.06

0.0 0.01 1

0.003 111

0.17 0.06

co.006

73.1 41.1

0.4 49.2 3.12

co.01 2.7

0.05 0.1

0.12

337 0.17 ~0.06

19.8 co.06

0.312 0.013 co.01 26.8

NlA

0.84 ~ 0 . 0 5 0.06

0.002

0.007 542

~0.005 ~0.005 <0.005

~0.005 0.02 0.5

26.7 0.015

CO.01 2.6

C0.02 0.1

~ 0 . 0 5

371 <0.05 ~ 0 . 0 5 0.1 1

10.05

1.01 <0.002 co.01 0.169

1460

0.86 c0.06 0.06

0.002

0.007 541

co.006 ~0.006 CO.006

0.302 0.843

0.4 26.5

0.027

<0.01 2.6

c0.02 c0.1

c0.06

396 c0.06 ~0.06 0.18

c0.06

1.03 <0.002 c0.01 0.584

NIA

(&L Engineering -35

I I- u €Iement

1 ;: :;;

1 E; :;;

Pilot Plant Testing of the High Density Sludge Process Britannia Mine AMD Treatment

RESIDUE AND COMBUSTION ASH ANALYSIS BY ICP Clarifier Underflow Solids Combustion Ash

Ag uglg ~ 2 0

0.5 <2 -=2 <2 c2 2 2 1 2 6 NIA 10 Be uglg 540 387 515 513 560 467 485 430 462 4 <5 8 NIA 40 c80 <80 <80 <80 c80 NIA 4 0 c80 94 90 3.82 1.96 3.86 3.71 3.96 3.48 3.27 4.14 3.54 7.66 6.32 7.30 AI % 2.5 <20 c20 <20 <20 <20 <20 2.5 <20 c20 <0.4

Ca % 8.03 8.16 10.8 13.5 13.5 14.2 207 Cd uglg

8.75 9.97 13.4 8.65 13.0 11.4 172 21 3 44 34 37 45 40

2.19 2.93 0.75 0.76 0.79 0.60 0.63 0.79 0.60 ~0.02 ~0.01 ~0.02 % 2.90 2.11 3.55 3.47 3.66 3.00 3.00 2.88 3.04 2.58 1.87 2.39 Fe %

40.03 eO.02, 0.56 ,0.45 0.50 0.67 0.48 0.54 0.69 4.64 3.95 '4:23 Cu 96 152 38 110 95 94 70 64 91 54 4 5 16 50 10 53 55 53 36 32 34 42 206 148 170 9 4 39 34

Mn % 0.84 1.17 1.15 0.70 0.65 0.69 0.71 0.70 0.62 0.63 0.43 0.44

BMHDS-1 TopASh P. Catch BMHDS-10 BMHDS-9 BMHDS-8 BMHDS-7 BMHDS-6 BMHDS-5 BMHDS-4 BMHDS-3 BMHDS-2

I 6.73 6.82 3.22 3.26 3.36 1.71 1.76 2.14 1.60 c0.02 cO.01 0.05 c20 Mo Na uglg % I

;g % 4.01 2.28 2.39 2.69 2.71 3.04 3.57 3.48 3.63 3.41 5.00 4.13

8

200 Pb uglg 1 e200 P ug/g 56 40 80 90 90 80 60 59 70 160 89 100 Ni uglg

21 20 <20 <20 c20 <20 c20 15 <20 <20

N/A ~ 2 0 0 9500 9880 <200

NIA 4 0 <80 <80 C80 <80 4 0 NIA 4 0 ~ 8 0 NIA 230 Se uglg I NIA 4 0 4 0 4 0 100 100. 100 NIA 100 280 14 360 Sb uglg NIA 5.84 0.19 0.19 0.31 4.11 4.35 N/A 4.63 3.88 N/A 3.47 S % 325 90 450 380 470 200 100 125 180 180 99 6810 7300 ~ 2 0 0 <200 <200 <200

Si uglg 3580 NIA 2010 1700 NIA 1810 2150 1700 1600 1500

561 586 485 483 537 630 656 726 631 340 230 NIA c80 4 0 4 0 4 0 4 0 e80 NIA <80 4 0 <2 NIA 1810

Ti ug/g 20 400 33 1280 1700 1330 1240 2318 2248 2319 1050. 3100 -20 <2

B.36 1.36 1.15 0.98 1.13 2.73 2.49 >1.0 2.58 4.99 4.20 4.01 69 50 70 70 70 60 70 71 60 c20

WHOLE ROCK ANAmSSi~~Cu 8 Zn bv AA I

1 ;:: 2 :::

% Si02

% Fe20: % MnO

% CaO % Na20

% P205

% Total cu %

NlA=Not I

- Clarifier Underflow Solids Combustion Ash

8.14 9.10

NIA NIA 0.06 0.06 0.06 0.04 0.04 N/A 0.04 0.01 0.02 0.01 1.48 1.95 2.11 2.11 2.20 2.92 2.99 2.36 2.84 0.14 0.05 0.10 2.24 3.43 1.23 1.25 1.23 0.81 0.87 0.91 0.05 0.01 0.00 0.01 7.18 9.49 4.88 5.21 4.92 2.00 2.09 3.48 2.05 0.03 0.27 0.12 15.42 21.36 13.52 13.76 14.32 19.11 20.44 21.02 19.75 14.46 1.3.19 12.97 3.68 4.57 4.78 4.84 5.17 6.28 6.17 6.06 6.11 8.27 7.36 6.75 0.50 0.56 0.80 0.79 0.01 0.87 0.83 0.82 0.87 1.3i 1.34 1.35 4.00 3.49 5.48 5.36 5.30 4.40 4.46 4.72 4.59 3.52 3.78 3.81 6.74 4.89 9.72 9.55 9.39 7.23 6.88 7.61 7.48 13.75 14.01 14.09 0.50 0.23 0.64 0.62 0.63 0.25 0.27 0.29 0.27 0.01 0.00 0.01 33.63 19.09 40.13 40.93 39.59 22.63 22.97 23.34 23.05 8.57

34.29 32.99 31.87 20.61 18.79 23.15 23.15 14.36 13.23 13.23 13.92 19.06 81.65 82.11

NIA 1.41 1.11 1.01 0.96 2.62 2.42 2.38 2.57 E 4.48 E 5.01 E4.81 NIA NIA 0.55 0.47 0.43 0.63 0.45 N/A 0.67 E 3.90 E 4.51 €4.08

94.43 82.98 96.58 97.71 98.06 89.68 89.19 89.40 88.51 82.01

BMHDS-1 TopASh P.Catch BMHDS-10 BMHDS-9 EMHDS-8 BMHDS-7 BMHDS-6 BMHDS-5 BMHDS-4 6 ° K - 3 BMHDS-2

ialyzed E=exceeds calibration 'Fe203 is Total Fe as Fe203

I

APPENDIX D

ACUTE LETHALITY TEST RESULTS

I I I 1 I 1 1 I I I 1 I 1 r I

, a ACUTE LETHALITY TEST USING RAINBOW TROUT (LC50 AND LT50)

REPORT FORM/ ANALYST LOG

EnvironmsntCansda Collator 25/53 -90 I Pacific Environmental Sdenm Centre (PESC) Aquatic Tox*dogy Ssdh 2645 D o H a ~ i o n m.. Nom Vancouver British Columbir. V7H 1VZ

csw

DILUTION WATER B'FRESH WAER a SALT WAER /oo SALlNlN

SOURCE J P E S C W L L 0 DECHLORINAED MUNICIPAL a BURRARD INLET

DILUT NS MEASURED BY

Source Cl VOLUME 0 ACTIVE INGREDIENT

U OmrsamOni used: L G H T ' I/&-/OLESAMPLE

FISH S F Rainbow Tmut (Ommhynchus Mykiss)

Description of Test Conditions All testing is done in environmental moms separate horn the fish holding facilii. The mom' photoperid and temperalum. as well as the waler delNefy temperatures. am computer controlled. 10 g a b allglass aquaria covered with smoked plexglas l i s am used as lest vessels.

Aention: Oil free compressed air is delivered lo the test concentrations at a rate of 6.5 f 1 mUUmin by means of disposable borosilicate glass pasteur pipets.

Protocol Used

Tests are Performed following, where appropriate, the biological test methods, Report EPS 1/RM/9 (July 1990) and Report EPS I /RM/ l I (July 1990). amended May 1996.

ANALYSIS RESULTS

96 Hr (Slatic) LC50 is ~ O / , concentration 95% confidence limits - The median lethal concentration (Le.. the concentration of material in water that is eslimated lo be lelhal to 50% of the test organisms) over an exposure period of 96 houfs

96 Hr (Slatic) LT50 Is - Period of exposure estimated to cause 50% morlalily in a group of fish held in a particular test solution.

- a1 - concentration 95% confidence limits c

The statistical method used was - COmpUter program used to generate,(he result Stephan (Melhods for Calculating an LC50 in: Aquatic Toxicology and Hazard

Evaluation. ASTM. 1977).

Reference toxicant 96 Hr L C ~ O 8.6 my1 L concentration 95% conmence limits %L

Chemical used ' Phenol

Geometric mean LC50 and warnmg llmlts (+/-2SD) 9. t Date of test A P T . , (13.2 -5 .0 ) I m3 l L

-

Protocol Variances 8 -

Notes

status of control fish 0e-n A.

Analyst Date- e, Results verified b Date ? /in4 /q=i

r

mncentrations

~ . revised March 1997 ~

penon minutes A Q L L

. . 0 c, -I ACUTE LETHALlh' E S T USING RAINBOW TROUT (LC50 AND LT50)

l REPORT FORMI ANALYST LOG

Pacific Envimnnmntrl Scicnm Can- (PESC) EnvironmentCanada cottator ZGT? - lo I

% E & ~ ~ ~ ~ ~ ~ a - r CSRX

SOURCE 0 DECHLORINATED MUNICIPAL ' 0 BURRARD INLET

DILUTIONS MEASURED BY

&A A L E SAMPLE '=bow Tmut (Oncomynchur Mykiss) U Othersalmonid used:

U VOLUME 0 ACTIVE INGREDIENT Source Sf&,il u, JJed

SAY LOADING I FORK I RANGE DENSITY LENGTH

0

Description of Test Conditions All testing is done in environmental rooms separate from the fish holding facilily. The rooms' photoperiod and temperature. as well as the Water delivery temperatures, are computer conlmlkd. 10 gallon r&glass aquaria covered with smoked Plexiglas lids are used as test vessels.

Aeration: Oil fne compressed air is delivered to the test concentrations at a rate of 6.5 f 1 mlRlmin by means of disposable borosilicate glass pasteur pipets.

I Tests are pelformed fOllowi~g. where appropriate, the biological test methods, Report EPS l/RM/S (July 1990) and Report EPS l lRW13 (July 1990). amended May 1996.

1 I 1

ANALYSIS RESULTS

96 Hr (Static) LC50 is ,no "A concentratJon 95% confidence limits The median lethal concentration (i.e.. the concentration of material in water that is estimated lo be lethal to 50% of the test organisms) over an exposure period of 96 hours

96 Hr (Static) LT50 is 7& h t'+ at k c o n c e n t r a t i o n 95% confidence limits Period of exposure estimated to cause 50% mortality in a group of fish held in a particular test solution.

The statistical method used was

4 Reference 9.16 +,# omcentralion 95% confdence limits dd8 - 13- +L \

Chemical used Date of test

. r- 13. a y / . J.

Protocol Variances

Date b%+q " 7 /997 ~u ~ Results verified b Date mbi / 1497

hncentrations' 6 revised March 1997 penon minutes

0 0 ACUTE L E T H A U h E S T USING RAINBOW TROUT (LC50 AND LT50)

I REPORT FORM/ ANALYST LOG ~ EnviroMnntcm-

Pacific Environmsnhl S&nm Cemo (PESG) , Aquatic Toxicology Scdion 2645 Dollarton Hwy.. NOM Vancouwr British Columbii. v7n 1vZ

BIOASSAY TEMPERATIJRg

OAGIUAL

SAMPLE PREPARATION DILUTION ' TEMP

14 DENSrPl

4TER

HARDNESS

400

See data sheet (Attached)

or See data sheet (Attached)

or

4 1 I I 1 I I I I

Test Log OBSERVAllON CODES

EPSlRUR

.. ,. 1.:

1.33 hr

R Skittering 5.33 hr

Q Gyrating 2.67 hr

P Erratic

Description of Test Conditions

AM testing is done in environmental manr separate fmm the fih holding facility. The moms' pholopemd and temperature. as well as the water delivery temp.sntures. am computer controllad. 10 gallon a&glass aquaria covered with smoked Plexiglas lids are used as test vessels.

Aeration: disposable borosilicate glass Pasteur pipets. Oil free compressed air is delivered to the test conantrations at a rate of 6.5 i 1 mll l lmin by means of

Protocol Used Tests are performed following. where appropriate. the biological test methods. Repolt EPS llRM19 (July 1990) and Report EPS 1IRW13 (July 1990). amended May 1996.

ANALYSIS RESULTS

96 Hr (StaUc) LC50 is ,'?6+ ' h S l > , 0.f /OD % concsntraUon 95% wnfdence limits The median lethal conceritration (i.e.. the concentralion of material in water that is estimated to be lethal to 50% of the test organisms) over an exposure period of 96 houn

96 Hr (Static) LT60 is &f 0 9 I 6 at a c o n c e n t n t i o n 95% confidence limits Period of exposure estimated to uuse 50% morlali4y in a group of fish held in a parfwlartest solulion.

\ $4

The stalislical melhod used was

Computer program used to generate-the result: Slephan (Methods for Calculating an LC50 in: Aquatic Toxicology and Hazard Evaluation, ASTM. 1977).

Reference toxicant 96 Hr LCSO 9. i 6 7 / / . concentration 95% confdence limits

Chemical used Date of test Geometric mean 7. I .nn i -

3 -13.2 y// . Protocol Variances

Notes

Analyst Date /)kw 7. /997

Results verified b Date MAA fi%/c& u- t #wneentrations 6

revised March 1997 penon minutes 920

I !

ANAL1519 REPORT POLYCHLORINATED DIBENZODIOX~NS AND DlllEHZOFURANS

CLIENT SAM?LE I.D.: ~7104)~ Apr25/37 1630 Mtannta AXYS FILE S702-01 LI

CLIENT: Envlronrnanr Canad. DATE: 11/Jun/07

SAMPLE TYPE Eflluonr METHOD NO.: DX-EQ1IVer.z

GAMPLE 61ZE 0.09 L INSTRUMCHT: GC-HRMS

CONCU(TRATl0N I N pglL

WCDD - Told

13C-TICDF 1SC.T4CDD OC-WCDF 11C-PSCDD laGH6CDF 13C.H6CDD I~C-WCDP

73C.wCDD 15C.H7CDD

DSO 11

41

1400

940 30 s3 59

270 140

07

I .5 1.5

1.5 1.5

3.0

3.0 3.0

3.0

s.0 5.0

8.0

2,3.76. TCDD mas (umlng NATO I - T E ~ )

2.3.7.S - TCDD TEas (ND-II2 DL) = 80.4 p@L

2,3,7,8. TCDb-TEQS (ND-0) = 80.3 ps/L

.. . -

I.

I I 1

I

* .

ANALYSIS REPORT POLYCHLORINATED DlENZODlOXlNS AND DIBENTOFURANS

CLIENT SAMPLE I.D.: S7-2 97.04.10 Brlunnla h e h PllDt PIMt AXYS FILE: e702.02 LI

CLIENT: Envlrrnmmt Canada Dl- 11IJunle7

SAMPLC m P E Eflluenl METHOD NO.: DX-E02N.r.2

SAMPLE SIZE 0.- L INSIRUYEHT: GC-HRMS

CDNCENTRATlON IH: ps/L

Dloxlna ConsmnbaUon (SDL) FUr.n. Concantradon

OICDD- Tolml 140

13C-T4CDF lDGT4CDD ISC-PSCDF 13C-PSCDD 11C4i6CDF 1aC-HICDD ' - lfGH7CDD 1¶C.H7CDF

l a C - ~ C D D

3.5 3.5

3.6 1.5

3.5 3.5 3.5 3.5

7 3 7.5

8.0

.x Resorry

53 58

49 54

70 82

44 58

30

720 1 0 0

300 26 31

130 17 13

NOR 18

NO

26 26 NO

NO

P L )

1.5 I .5

2.0 2.0 2.0

3.0 3.0 3.0 3.0

3.0

5.0 5.0 5.0

0.0

2.3.7.6 - TCDD EO# (Ualnp NATO I-TEF-)

2,3,7,8 .TCDDlEOs (NO-112 DL) = 67.4 pglL

2,3,7.0 -TCDD TEO. (NOLO) c 67.2 Pg/L

pOLYCHLORINAM DIBENZODIOXlNS AND DlBENZONRANb ANALYSIS R6PORT

CLIENT SAMPLE I.D.: Prossdural Blank AXYS FIE DX-E-BLK lE71 Ut

CLIENT: Envlronm-1 Canada DArr: 1 rlJunl97

SAMPLE TfPE: Blank METHOD NO.: DX.E.02/Vu.Z

SAMPLE SI= 1 M L INSTRUMENT: GGHRMS

CONCENTRATION I N ppR

DlO.ln* ConcmlrmUon (SDL) Rvmm ' C a c n b a U m @DL)

TLCDD - T d d ND 1.5

z m a ND 1.5

PSCDD - 1d.I ND 3.0 1,z3,7b ND 3.0

H7CDD - lohl ND 1.2.3I.P.rC ND

5.0 5.0

WCDD . Told NDR 27 17

lJGT4CW 13GT4CDD r5C-PSCDF 13C-PSCDD 1OC-HCCDF IJGHSCDD lSCeH7CDF

1JG01CDD 1SC.MCDD

80 63 51 sa 72

54 56 28

m .. . . -

ND 2.0 ND 2.0

ND 2.0 NO 2.0 ND 2.0

5.3 3.0 ND ND

3.0

NO 3.0 3.0

ND 3.0

ND 7.0 NO 7.0 ND 7.0

ND 17

ANALIS18 REPORT POLYCHLORINATED DIBCNZOMOXlNS AND DIBENZORIRANS

CUENT SAMPLE I.D.: Splk-d Mdrlx AXYS F I E DX-E-SPM 798 LI

CLIEM: Env l ramwl Canada D A e l l l JunP7

SAMPLE TYPE Ef f l um METHOD NO.: DX.E.OZAIar.2

SAMPLE SIP: 1.00 L INSTRUMENT: GGHRMS

CONCENTRATION IN: pp/L

Dlculn* Dnumln.d E x p u l d W R r o l u y Furuo D.tamlnd E1prI.d YR.eorwy

OICDD - Told 101

18 04

50 102

54 65 50 $2 84

71

74 136

48 44

45

47 36

46 57 30 18

1s

41 41

44 43 32 s3

43 27

90

10

46 46

46 40

46 46

A6 46

74

05

8S OS

06 93 70 72

93 59

122

I I I I

APPENDIX E

CLARIFIER FEED SETTLING DATA & CURVES

SElTLlNG TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA BRITANNIA MINE AMD TREATMENT

Test Date: April 14, 1997 Tested By: K. Timewell Test I.D.: BMHDS-IS1

1. INITIAL CONDITIONS I

SAMPLE Clarifier feed from Test BMHDS-1 at 15 hours pH 9.5, Temperature 14"C, Specific Gravity=l.005. Percent Solids=1.3

2. TEST CONDITIONS I I

FLOCCULANT Settling vessel size (mUcm): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500.0 Concentration = 0.025% Slurry weight (9) 502.4 Addition (mglL) = 0.79 Dry Solids weight (9) 6.7

Final interface Height (mL) 60

3. COMMENTS

Thickened Pulp Description: . Creamy-white Supernatant Description: Overflow clear with very low suspended solids

Phase separation was immediate

4. SETTLING DATA AND CALCULATIONS Time (min) Volume imL) Heiaht (mm) Pulp Density

0 500 248 1.3 0.5 1

1.5 2

2.5 3

3.5 4 5 10 20 30 60 120

180 140 120 115 100 105 100 95 92 77 73 70 65 60

89 69 59 57 50 52 50 47 46 38 36 35 32 30

3.7 4.7 5.5 5.7 6.5 6.2 6.5 6.9 7.1 8.4 8.9 9.3 9.9 10.7

!FEJ, Engineering

SElTLlNG TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA BRITANNIA MINE AMD TREATMENT

Test Date: April 15, 1997 Tested By: Sohan S. Basra Test I.D.: BMHDS-IS2

1. INITIAL CONDITIONS I

SAMPLE Clarifier feed from Test BMHDS-1 at 25 hours pH 9.6, Temperature 14"C, Specific Gravity=l.OlO, Percent Solids=1.6

2. TEST CONDITIONS I

FLOCCULANT Settling vessel sue (rnucrn): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.025% Slurry weight (g) 505.1 Addition (mg/L) = 1.35 Dry Solids weight (9) 8.0

Final interface Height (mL) 65

3. COMMENTS I

Thickened Pulp Description: Light brown Supernatant Description: Overflow clear with very low suspended solids

Phase separation was immediate

4. SElTLING DATA AND CALCULATIONS I

I Time (rnin) Volume fmL) Heiaht (mm) Pub Density

0 500 248 0.5 225 Ill 1 160 79 2 150 74 5 130 64 10 90 45 20 85 42 30 75 37 60 70 35 90 68 34 120 65 32 180 65 32

1.6 3.5 4.8 5.2 5.9 8.4 8.9 10.0 10.7 10.9 11.4 11.4

I ( Engineering

SElTLlNG TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA BRITANNIA MINE AMD TREATMENT

Test Date: April 15. 1997 Tested By: K. Timewell Test I.D.: BMHDS-2S1

1. INITIAL CONDITIONS 1

I SAMPLE Clarifier feed from Test BMHDS-2 at 13 hours

I pH 9.8, Temperature 14"C, Specific Gravity=I.O17. Percent Solids=2.1

2. TEST CONDITIONS I

FLOCCULANT Settling vessel size (mUcm): 20.2 Type : Allied Colloids - Percol €40 Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (9) 508.6

Final interface Height (mL) 100 Addition (mglL) = 3.50 Dry Solids weight (9) 10.5

3. COMMENTS

Thickened Pulp Description: Golden brown Supernatant Description: Ovetflow had fine suspended solids for first hour

Phase separation was quick but not immediately complete

4. SElTLING DATA AND CALCULATIONS

Time (minl Volume fmL) Heiaht (mm) PUID Denbily

0 500 248 2.1 0.5 455 225 1 375 186

2.3 2.7

1.5 315 156 3.2 2 280 139 3.6

2.5 255 126 3 240 119

4.0 4.2

3.5 230 114 4 220

4.4 109

5 205 101 4.9 4.6

10 155 77 6.4 20 145 72 30

6.8 135 67

60 7.3

120 59 120 100 50 9.7

8.2

Engineering ,'

I I I I B

SEHLING TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA BRITANNIA MINE AMD TREATMENT

Test Date: April 17, 1997 Tested By: Sohan S. Basra Test ID.: BMHDS-2S2

1. INITIAL CONDITIONS I

SAMPLE Clarifier feed from Test BMHDS-2 at 27 hours pH 9.5, Temperature 14"C, Specific Gravity=l.O14, Percent Solids=2.1

2. TEST CONDITIONS I

FLOCCULANT Settling vessel size (mUcm): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (9) 507.2 Addition (mglL Slurry 4.58 Dry Solids weight (9) 10.5

Final interface Height (mL) 83

3. COMMENTS I I

Thickened Pulp Description: Golden brown Supernatant Description: Overflow very clear after 5 minutes

I I

4. SETTLING DATA AND CALCULATIONS I

0 0.5 I 2 3 5 10 20 30 60 120 150 180

500 400 325 255 225 200 160 148 135 120 90 85 83

248 2. I 198 2.6 161 3.2 126 4.0 111 4.5 99 5.1 79 6.3 73 6.8 67 7.4 59 8.3 45 10.8 42 11.4 41 11.6

, ,rKZ-,c "

',':4=?JL Engineering

I I I I I I I I I I I I I I I I I I b

SElTLING TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA BRITANNIA MINE AMD TREATMENT

Test Date: April 17, 1997 Tested By: K. Timewell Test I.D.: BMHDS-2S3

1. INITIAL CONDITIONS I

SAMPLE Clarifier feed from Test BMHDS-2 at 39 hours pH 9.4, Temperature 15"C, Specific Gravity=1.016, Percent Solidsr2.2

2. TEST CONDITIONS r

FLOCCULANT Settling vessel size (mUcm): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Sluny weight (9) 508.1 Addition (mglL Slurry 4.92 Dry Solids weight (9) 11.1

Final interface Heiaht ImL) 87

3. COMMENTS

Thickened Pulp Description: Golden brown Supernatant Description: Overflow clear after 10 minutes

L

1. SETTLING DATA AND CALCULATIONS

Time (min) Volume (mL) Heiaht (mm) Pulp Density

0 500 248 2.2 0.5 455 225 2.4 1 380 18% 2.9

1.5 325 161 2 290 144

3.3

3 250 124 4.3 3.7

5 212 105 5.0 10 167 83 6.3 20 135 67 7.8 30 115 57 9.0 60 100 50 10.3 120 90 45 11.3 180 87 43 11.7

i - -. . -. L-~ Engineering

SElTLlNG TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA BRITANNIA MINE AMD TREATMENT

Test Date: April 18, 1997 Tested By: Sohan S. Basra Test I.D.: BMHDS-2S4

SAMPLE Clarifier feed from Test BMHDS-2 at 48 hours pH 9.4, Temperature 13T, Specific Gravity=l.015, Percent Solids=2.4

2. TEST CONDITIONS I

FLOCCULANT Settling vessel size (mUcm): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (9) 507.5 Addition (mglL Sluny 5.00 Dry Solids weight (9) 12.0

Final interface Height (mL) 80

3. COMMENTS I 1

Thickened Pulp Description: Black Supernatant Description: OverRow clear after 8 minutes

I 1

4. SETTLING DATA AND CALCULATIONS

Time (rnin) Volume ( rnU Heqht (rnrn) Pub DensQ

0 500 248 2.4 0.5 400 198 2.9 1 315 156 3.7

1.5 290 144 3 235 116 4.9

4.0

5 205 101 10 165 82 7.0

5.6

20 135 67 30

8.4 120 59 9.4

45 105 52 10.7 60 100 50 11.2 120 05 42 180 83 41 13.3

13.0

210 80 40 13.7

SETTLING TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA Test Date: April 18. 1997 BRITANNIA MINE AMD TREATMENT Tested By: K. Timewell

Test I.D.: BMHDS9Sl

SAMPLE Clarifier feed from Test BMHDS-3 at I 1 hours pH 9.5, Temperature 15"C, Specific Gravity=l.008, Percent Solids=1.2

2. TEST CONDITIONS

FLOCCULANT Seffling vessel size (mUcm): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (9) 504.2 Addition (mglL Slurry 1.59 Dry Solids weight (g) 5.9

Final interface Height (mL) 52

3. COMMENTS I I

Thickened Pulp Description: Golden brown Supernatant Description: Overflow clear after 3 minutes

4 . SETTLING DATA AND CALCULATIONS

Time (mini Volume (mL) Heiaht (mm) Pub Density

0 500 248 1.2 0.5 330 163 1.8 1 180 89 3.2

1.5 145 72 2 130 64

4.0 4.4

2.5 120 59 3 112

4.8 55

5 95 47 5.1

10 77 38 5.9 7.3

30 63 31 8.8 60 57 28 90 55 27

9.6 10.0

120 53 26 10.3 150 52 26 10.5

SElTLlNG TEST DATA AND CALCULATIONS

ENVIRONMENT CANADA BRITANNIA MINE AMD TREATMENT

Test Date: April 21, 1997 Tested By: K. Timewell Test I.D.: BMHDS4SI

I. INITIAL CONDITIONS

SAMPLE Clarifier feed from Test BMHDS4 at 11 hours pH 8.6, Temperature 14"C, Specific Gravity=l.007, Percent Solids=2.0

2. TEST CONDITIONS I

FLOCCULANT Settling vessel sue (mUcrn): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (9) 503.6 Addition (mglL Slurry 1.01 Dry Solids weight (9) 10.0

Final interface Height (mL) 52

3. COMMENTS

Thickened Pulp Description: Black Supernatant Description: Overflow mainly clear after 8 minutes, however some very fine,

lighter coloured suspended solids were visible for about I hour

1. SETTLING DATA AND CALCULATIONS

Time (min) Volume (mL) Heiaht (mml Pulp Oensity

0 500 248 2.0 0.5 250 124 3.9 1 135 67 7.2

1.5 115 57 8.4 2 105 52 9.2 3 93 46 10.4 5 80 40 12.0 12 65 32 14.6 20 62 31 15.2 30 60 30 15.7 60 57 28 120

16.5 52 26 18.0

180 52 26 18.0

SETTLING TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA BRITANNIA MINE AMD TREATMENT

Test Date: April 22, 1997 Tested By: Sohan s. Basra Test I.D.: BMHDS4S2

1. INITIAL CONDITIONS I

SAMPLE Clarifier feed from Test BMHDS-I at 21 hours pH 8.6, Temperature 14"C, Specific Gravity=l.O25. Percent Solids=3.8

2. TEST CONDITIONS I

FLOCCULANT Seffling vessel sue (mUcm): 20.2 Type : Allied Colloids - Percol E-10 Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (9) 512.7 Addition (rnglL Slurry 1.83 Dry Solids weight (9) 19.3

Final interface Height (mL) 70

3. COMMENTS

Thickened Pulp Description: Black Supernatant Description: Overflow mainly clear after 10 minutes, however some very fine

lighter coloured suspended solids remained.

Time (rnin)

0 0.5 I 2 3 5 10 20 30 60 120 180

Volume (mL) Heiaht (mm) Pub Densily

500 248 3.8 160 79 11.2 135 67 13.1 120 59 14.5 110 54 100 50

15.7 17.1

85 42 19.8 80 40 20.8 75 37 22.0- 70 35 23.3 70 35 23.3 70 35 23.3

SElTLING TEST DATA AND CALCULATIONS

g&Q ENVIRONMENT CANADA BRITANNIA MINE AMD TREATMENT

Test Date: April 22, 1997 Tested By: K. Timewell Test I.D.: BMHDS-IS3

1. INITIAL CONDITIONS I 1

SAMPLE Clarifier feed from Test BMHDS-I at 33 hours pH 8.7. Temperature 13"C, Specific Gravity=1.028, Percent Solids=3.9

2. TEST CONDITIONS I

FLOCCULANT Settling vessel size (mUcm): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (9) 514.1 Addition (mglL Slurry 2.87 Dry Solids weight (9) 20.3

Final interface Height (mL) 80

3. COMMENTS

Thickened Pulp Description: Black Supernatant Description: Overflow mainly clear after 10 minutes, however some very fine

suspended solids were visible for -45 minutes.

1. SETTLING DATA AND CALCULATIONS

Time Win) Volume (mL) Hsiaht tmml Pub Dsntity

0 500 248 3.9 0.5 240 I19 8.0 I 180 89 10.5. I .5 155 77 12.0 2 143 71 3 125 62 14.6

12.9

5 107 53 16.8 10 93 46 19.0 20 87 43 20.1 30 84 42 20.7 60 83 41 20.9 120 80 40 21.6 180 80 40 21.6

.- L"- " ~.

SEllLlNG TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA Test Date: April 23, 1997 BRITANNIA MINE AMD TREATMENT Tested By: Sohan S. Basra

Test I.D.: BMHDMS4

1. INITIAL CONDITIONS I I

SAMPLE Clarifier feed from Test BMHDS-I at 44 hours pH 8.5, Temperature 14"C, Specific Gravity=1.034, Percent Solids=4.8

2. TEST CONDITIONS

FLOCCULANT Settling vessel sue (mUcm): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (g) 517.2 Addition (mglL Slurry 2.44 Dry Solids weight (9) 24.7

Final interface Height (mL) 78

3. COMMENTS I

Thickened Pulp Description: Black Supernatant Description: Overflow mainly clear after 4 minutes, however some very fine

suspended solids were visible for about I hour.

4. SETTLING DATA AND CALCULATIONS

Time (minl Volume (mL) Height (mm) Pub Dsnsity

0 500 248 4.8 0.5 180 89 12.5 1 160 79 13.9

1.5 145 72 2 135

15.2 67

3 16.2

125 62 4

17.4 115 57

5 18.7

110 54 10

19.4 95 47 22.0

20 85 42 24.2 30 85 42 24.2 60 80 40 25.4 120 78 39 25.9

SElTLING TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA BRITANNIA MINE AMD TREATMENT

Test Date: April 23, 1997 Tested By: K. Timewell Test I.D.: BMHDS-5SI

1. INITIAL CONDITIONS 1

SAMPLE Clarifier feed from Test BMHDS-5 at 12 hours pH 9.0, Temperature 14"C, Specific Gravily=1.030, Percent Solids=3.5

2. TEST CONDITIONS I 1

FLOCCULANT Settling vessel sue (mUcm): 20.2 Type : Allied Colloids - Percol E-10 Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (9) 515.1 Addition (mglL Slurry 0.94 Dry Solids weight (9) 17.9

Final interface Height (mL) 67

3. COMMENTS

Thickened Pulp Description: ' Black Supernatant Description: Overflow mainly clear after 2 minutes, however some very fine

suspended solids were visible for -1 hour.

4. SETTLING DATA AND CALCULATIONS

Time (min) Volume (mLI Height ImmI Pulp Denrity

0 500 248 3.5 0.5 180 89 9.2 1 135 67 11.9

1.5 113 56 14.0 2 103 51 15.2 3 93 46 16.6 4 85 42 5 82 41

17.9 18.4,

10 75 37 19.9 20 70 35 21.0 30 70 35 21.0 60 68 34 21.5 120 67 33 21.8 180 67 33 21.8

I

SEllLlNG TEST DATA AND CALCULATIONS

gJ!Q ENVIRONMENT CANADA Test Date: April 24, 1997 BRITANNIA MINE AMD TREATMENT Tested By: Sohan S. Basra

Test I.D.: BMHDS-5S2

1. INITIAL CONDITIONS I I

SAMPLE Clarifier feed from Test BMHDSQ at 20 hours pH 9.0, Temperature 15°C. Specific Gravity=l.O24, Percent Solids=3.4

2. TEST CONDITIONS I

FLOCCULANT Settling vessel size (mUcm): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (9) 512.2 Addition (mglL Slurry 1.05 Dry Solids weight (9) 17.4

Final intarfar* Haioht (mL\ 60

3. COMMENTS ~

Thickened Pulp Description: Black Supernatant Description: OverRow mainly clear after 10 minutes, however some very fine

suspended solids were visible after 1 hour.

4. SETTLING DATA AND CALCULATIONS

Time (min) Volume tmLI Heiaht (mm) Pulp Density

0 500 248 3.4 0.5 105 52 14.8 1 100 50 15.5

1.5 90 45 17.0 2 85 42 3 80 40 18.9

17.9

5 75 37 20.0 10 70 35 21.2 20 65 32 22.5 30 65 32 22.5 60 63 31 23.1 120 60 30 24.1

SETTLING TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA Test Date: April 25, 1997 BRITANNIA MINE AMD TREATMENT Tested By: K. Timewell

Test I.D.: BMHDS-GSI

1. INITIAL CONDITIONS

SAMPLE Clarifier feed from Test BMHDS-6 at 6 hours pH 9.6, Temperature 14°C. Specific Gravity=l.021, Percent Solidsr2.9

2. TEST CONDITIONS

FLOCCULANT Settling vessel size (mUcm): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (9): 510.5 Addition (mglL) = 1.76 Dry Solids weight (9): 14.6

Final interface Height (rnL): 57

3. COMMENTS

Thickened Pulp Description: Black Supernatant Description: Overflow mainly clear after 10 minutes, however some very fine

suspended solids were visible for 20 minutes.

SETLING DATA AND CALCULATIONS

Time (min) Volume (mU HeiQht (mm) Pub Density

0 500 248 2.9 0.5 140 69 9.7 1 105 52 12.6

1.5 90 45 14.5 2 83 41 15.6 3 75 37 17.1 4 70 35 18.1 5 67 33 18.8 10 63 31 19.9 20 60 30 20.7 30 60 30 20.7 60 58 29 21.3 120 57 28 21.6

, .

Engineering " ?__

SElTLlNG TEST DATA AND CALCULATiONS

CLlENT ENVIRONMENT CANADA BRITANNIA MINE AMD TREATMENT

Test Date: April 25, 1997 Tested By: Sohan S. Basra Test I.D.: BMHDS-7SI

I. INITIAL CONDITIONS I I

SAMPLE Clarifier feed from Test BMHDS-7 at 3 hours pH 8.9, Temperature 15°C. Specific Gravity=1.017, Percent Solids=2.9

2. TEST CONDITIONS I

FLOCCULANT Seffling vessel size (mUcrn): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (9) 508.4 Addition (mg/L Slurry 1.63 Dry Solids weight (9) 14.5

Final interface Heiaht (mL) 56

3. COMMENTS I 1

Thickened Pulp Description: Black Supernatant Description: Overflow clear after 20 minutes.

4. SETLING DATA AND CALCULATIONS

Time (mini Volume ImL) Heiaht (mm) Pub Dsnritg

0 500 248 2.9 0.5 175 87 7.9 1 95 47 14.0 2 78 39 3 70

16.8 35

6 65 18.5

32 10 60 30 21.2

19.8

20 60 30 21.2 30 59 29 21.5 60 57 28 22.2 120 56 28 22.5

I

.”. -==Y dE53& Engineering

SETTLING TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA BRITANNIA MINE AMD TREATMENT

Test Date: April 25, 1997 Tested By: K. Timewell Test I.D.: BMHDSJS2

I. INITIAL CONDITIONS I 1

SAMPLE Clarifier feed from Test BMHDS-7 at 12 hours pH 8.9, Temperature 15"C, Specific Gravity=1.017, Percent Solids=1.4

2. TEST CONDITIONS I

FLOCCULANT Settling vessel size (mUcm): 20.2 Type : Al l id Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (9) 508.4 Addition (mg/L Slurry 0.78 Dry Solids weight (9) 6.9

Final interface Height (mL) 30

3. COMMENTS I I

I Thickened Pulp Description: Black Supernatant Description: Overflow clear after 20 minutes.

4. SElTLING DATA AND CALCULATIONS

Time (mini Volume (mLI Heiaht (mmI Pub Dansily

0 500 248 I .4 0.5 65 32 1 50 25

9.4 11.8

1.5 43 21 13.4 2 40 20 14.3

2.5 38 19 14.9 3 38 19 5

14.9 35 17 15.9

10 33 16 16.7 20 30 15 18.0 60 30 15 18.0 120 30 15 18.0

SElTLlNG TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA BRITANNIA MINE AMD TREATMENT

Test Date: April 29, 1997 Tested By: K. Tirnewell Test I.D.: BMHDS-8SI

1. INITIAL CONDITIONS I I

SAMPLE Clarifier feed from Test BMHDS-8 at 12 hours pH 9.0, Temperature 14"C, Specific Gravity=1.015, Percent Solids=2.4

2. TEST CONDITIONS I I

FLOCCULANT Settling vessel size (mUcm): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (9) 508.4 Addition (mglL Slurry 0.48 Dry Solids weight (9) 12.1

Final interface Height (mL) 43

3. COMMENTS

Thickened Pulp Description: Black Supernatant Description: Overflow clear after 30 minutes.

. SETTLING DATA AND CALCULATIONS

Tim Irnin) Volume (mL) Hekaht (mm) Pulp DensiIy

0 500 248 2.4 0.5 150 74 1

7.6 80 40 13.7

I .5 70 35 15.4 2 63 31 16.9 3 55 27 5 50 25 20.7

19.1

10 47 23 21.0 20 45 22 22.7 30 45 22 22.7 60 45 22 22.7. 120 43 21 23.5

-e':-. Engineering

SElTLlNG TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA BRITANNIA MINE AMD TREATMENT

Test Date: April 29, 1997 Tested By: Sohan S. Basra Test I.D.: BMHDS-8S2

1. INITIAL CONDITIONS I 1

SAMPLE Clarifier feed from Test BMHDS-8 at 23 hours pH 8.9, Temperature 14°C. Specific Gravity=l.021, Percent Solids~3.55

2. TEST CONDITIONS

FLOCCULANT Settling vessel size (mUcm): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (g) 510.5 Addition (mglL Slurry 0.92 Dry Solids weight (9) 18.1

Final interface Height (mL) 50

3. COMMENTS I I

Thickened Pulp Descriptiin: Black Supernatant Description: OverRow clear after 2 hours

4 . SEITLING DATA AND CALCULATIONS

rime (rnin) Volume (mL) Wmht tmrn) Pub Dens*

0 500 248 3.5 0.5 80 40 20.0 1 70 35 22.5

1.5 67 33 23.4 2 65 32 3 60 30 25.7

24.0

5 55 27 27.6 10 52 26 29.0 20 51 25 29.4 30 50 25 29.9 60 50 25 29.9 120 50 25 29.9

SETTLING TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA Test Date: April 29, 1997 BRITANNIA MINE AMD TREATMENT Tested By: K. Timewell

Test I.D.: BMHDS-9S1

1 . INITIAL CONDITIONS

SAMPLE Clarifier feed from Test BMHDS-9 at 10 hours pH 8.5. Temperature 14T, Specific Gravity-1.030, Percent Solids=4.2

2. TEST CONDITIONS

FLOCCULANT Settling vessel size (mUcm): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (9) 515.2 Addition (mglL Slurry 1.12 Dry Solids weight (9) 21.7

Final interface Height (mL) 56

3. COMMENTS

Thickened Pulp Description: Black Supernatant Description: Overflow clear after 30 minutes.

-

4. SETTLING DATA AND CALCULATIONS

Time (min) Volume (mL) Hebhl (mm) Pub Density

0 500 248 4.2 0.5 150 74

1 95 47 19.7 13.1

1.5 83 41 22.1 2 76 38 3

23.8 68 34

5 26.1

62 31 10 58 29

28.1

20 29.6

57 28 30.1 30 57 28 30.1 60 56 28 30.5 120 56 28 30.5

I

~

i C ? G 2 Engineering -=s

SElTLlNG TEST DATA AND CALCULATIONS

CLlENT ENVIRONMENT CANADA BRITANNIA MINE AMD TREATMENT

Test Date: April 30, 1997 Tested By: K. Timewell Test I.D.: BMHDS-9S2

1. INITIAL CONDITIONS I I

SAMPLE Clarifier feed from Test BMHDS-9 at 18 hours pH 8.5, Temperature 14°C. Specific Gravity=l.027. Percent Solids=3.9

1. TEST CONDITIONS

FLOCCULANT Settling vessel size (mUcm): 20.2 Type : Allied Colloids - Percol E-IO Undecanted slurry vol. (mL): 500 Concentration = 0.0125% Slurry weight (9) 513.5 Addition (mg/L Slurry 2.18 Dry Sol is weight (9) 19.9

Final interface Height (mL) 52

3. COMMENTS I

Thickened Pulp Description: ' Black Supernatant Description: Overflow clear after 2 hours.

I

Time (min) Volume (mLI H s i h t (mm) Pulp Density

0 500 248 3.9 0.5 105 52 16.8 1 80 40 21.3 I .5 70 35 23.8 2 65 32 25.4 3 60 30 27.1 5 56 28 28.6 10 54 27 29.5 20 53 26 29.9 30 53 26 29.9 60 53 26 29.9 120 52 26 30.4

."L Engineering

Clarifier Feed Settling Curve Test BMHDS-1Sl

0 20 40 100 120 ~ Time (%ut..) I

Figure 4.4.2

Clarifier Fwd Sefflina Curve Test BMHDS-lS2

I

i ' I

0 60 Time

120

Figure 4.4.3

'a I \ Engineering

Clarifier Feed Seltlina Curve Test BMHDS-251

0 20 40 Time (mlnutn)

60 80 100 120

" ~- . Figure 4.4.4

Clarifier Fwd Settling Curve Test BMHDS-2S2

0 30 60 120 150 180 Time (%"ut..,

-~ Figure 4.4.5

__ ~, ,:a, ' ,- c - Engineering

Clarifier Feed Settllna Curve Test BMHDS-2S3

0 30 60 w 120 150 180 T i m (minutes)

." _ _ ~ Figure 4.4.6

Clarifier Feed Settllna Curve Test BMHDS-ZS4

0 i

30 90 120 150 180 210 ~

T h o (minutm) I

Figure 4.4.7

-e.& Engineering

"

Clarifier Feed Settlina Curve Test BMHDSJSI

- e - f 8200.

- - A A - - - ( 1

0 7 0 30 60 90 120 150

Tlme (mlnutu)

Figure 4.4.8

Clarifier Feed Settlina Curve Test BMHDS4SI

0 30.

400

100

Clarifier Feed Settling Curve Test BMHDS4S2

0 30 60 Tim. (anutes) 120

Figure 4.4.10

150 180

Clarifier Feed Settllna Curve Test BMHDS4S3

Clarifier Feed Settllna Curve Test B M H D S a

500 4

400 -.

z3L-a.

m z - - s 9200

A - A -

0 20 40 60 80 loo T i m (minut..)

. "" . ~

Figure 4.4.12

, 400

100

120

~.

I Clarifier Feed Settlina Curve Test BMHDS-5Sl

500 4

I -

1

I -

0 . 0 30 60

Time (minutes) 90 120 150 180 I

Figure 4.4.13

1 I I I I I

Clarifier Feed Settllna Curve l e s t BMHDSSSZ

0 0 20 40 €4 80 100

TIM (minut..) 120 ~

Figure 4.4.14

100

Clarifier F w d Settllna Curve lest BMHDS6Sl

r 0 20 40

Tlme (minutes) 60 80 100

, ~

i j

I 120 ~

Figure 4.4.15

4.

ClaMer F e d Settllna C u m Test BHHDS-'IS1

- !

* b

0 20 80 100 120 !

- i 40

TIM @nut..)

Figure 4.4.16 -

Clarifier F e d Settlina C u m Test BMHDS"IS2

0 20 40 €4 Time (minut..)

e4 100 120

Figure 4.4.17

".

,.-:- Engineering -. ,"_ 6".

500

400

100

Clarifier Feed Settllna Cuwe Test BMHDS-SSl

0 0 20 40 60 BO 100 120

Time (minutm) .~

Figure 4.4.18

500

400

500

400

100

0

100

0 0

Clarifier Feed Settling Curve Test BMHDSBS2

20 40 60 Time (minutes)

80 100 120 ~

J

Figure 4.4.19

I I I I 1 I I I I

500

400

100

ClaMer Feed Settllna Curve TWt BMHDS-9Sl

0 20 40 60 80 1W 120 ' T i m (mlnutos)

Figure 4.4.20 .~

- . ."

Clarifier Feed Settllna Curve Test BMHDS-9SZ

500

400 -

100

0 20 40 60 80 100 120 ~

T i m (mlnutos)

Figure 4.4.21

500

I

400

Clarifier Feed Seltllna Curve Test BMHDS-IOSl

~ 0 20 40 60 80 100 120 ~

i Time (minutes) , Figure 4.4.22

400

3 300 z - m s

~ g 200 1 -

! 100

Clarifier Feed Seltlina Curve Test BMHDS-1OSZ

~

500 +

A - - - A - i

0 20 40 60 80 Time (minutn)

. . "" ~ ~ .

Figure 4.4.23

100 120

. - ~

APPENDIX F

FILTERING AND DRAINAGE TEST RESULTS

I 3 I I I

I

I

I I

Clarifier Underflow Sludae Dralnaae Tests ,

300 "

Lime

- Precipiiator Catch '

I

100

n " 0 10 20 40 50 60

Figure 4.3.5

Sludae Dninaae Test Data

Neutralizing (Final) Collected (mL) (9) (9) (Initial) Agent

%Solids Leachate Solids Water %Solids S.G.

Hydrated Lime

48.6 146 389 552 41.3 1.332 Top Ash 46.8 220 349 617 36.1 1.289 Precipitator Catch 26.0 241 143 649 18.1 1.135