wtp pilot scale testing high density sludge process
TRANSCRIPT
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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.
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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.
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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
Pilot Scale Testing of the High Density Sludge Process Britannia Mine AMD Treatment Britannia Beach, B.C. Page 20
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
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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.
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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
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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