APPENDIX J TECHNOLOGY EVALUATION REPORT

APPENDIX J

law

Text Box

TECHNOLOGY EVALUATION REPORT

MILLBROOK WASTEWATER TREATMENT PLANT

WASTEWATER TREATMENT CAPACITY CLASS EA

TECHNOLOGY EVALUATION

Prepared for:

TOWNSHIP OF CAVAN MONAGHAN

This report is protected by copyright and was prepared by R.V. Anderson Associates Limited for the account of the Township of Cavan Monaghan. It shall not be copied without permission. The material in it reflects our best judgment in light of the information available to R.V. Anderson Associates Limited at the time of preparation. Any use which a third party makes of this report, or any reliance on or decisions to be made based on it, are the responsibility of such third parties. R.V. Anderson Associates Limited accepts no responsibility for damages, if any, suffered by any third party as a result of decisions made or actions based on this report.

2001 Sheppard Avenue East, Suite 400

Toronto, Ontario M2J 4Z8 Canada Tel: (416) 497-8600 Fax: (416) 497-0342

Email: [email protected]

RVA 122670

March 2013

Township of Cavan Monaghan TOC - 1

Millbrook WWTP – Wastewater Treatment Capacity Class EA – Technology Evaluation RVA # 122670 March 2013

TABLE OF CONTENTS 1.0 INTRODUCTION ............................................................................................................. 1

2.0 DESIGN FLOWS, LOADINGS, AND EFFLUENT REQUIREMENTS .............................. 2

3.0 LONG LIST OF SECONDARY AND TERTIARY TREATMENT OPTIONS ..................... 4

3.1. LONG LIST OF SECONDARY TREATMENT OPTIONS ........................................................... 4 3.1.1. Suspended Growth Processes .............................................................................. 4

3.1.1.1. Conventional Activated Sludge .......................................................................... 4 3.1.1.2. Extended Aeration ............................................................................................. 5 3.1.1.3. High-Rate Activated Sludge .............................................................................. 5 3.1.1.4. Sequence Batch Reactor ................................................................................... 5 3.1.1.5. Membrane Bioreactor ........................................................................................ 6

3.1.2. Fixed Film Processes ............................................................................................ 6 3.1.2.1. Moving Bed Bioreactor ...................................................................................... 6 3.1.2.2. Rotating Biological Contactor ............................................................................ 7 3.1.2.3. Trickling Filter .................................................................................................... 7

3.1.3. Hybrid Processes .................................................................................................. 7 3.1.3.1. Integrated Fixed-film Activated Sludge .............................................................. 8 3.1.3.2. Biological Aerated Filters ................................................................................... 8

3.2. LONG LIST OF TERTIARY TREATMENT OPTIONS ............................................................... 8 3.2.1. Tertiary Clarifications ............................................................................................ 9

3.2.1.1. Conventional Tertiary Clarifiers ......................................................................... 9 3.2.1.2. Microsand Ballasted Clarification ....................................................................... 9 3.2.1.3. Magnetite Ballasted Clarification ....................................................................... 9 3.2.1.4. High-Rate Solids Contact Clarification ..............................................................10

3.2.2. Tertiary Filtration ..................................................................................................10 3.2.2.1. Conventional Automatic Backwash Filters ........................................................10 3.2.2.2. Continuous Backwash Filters ...........................................................................10 3.2.2.3. Adsorptive Media Continuous Backwash Filters ...............................................11 3.2.2.4. Cloth Media Disc Filters....................................................................................11

3.2.3. Membrane Filtration .............................................................................................11 3.2.3.1. Membrane Ultrafiltration ...................................................................................11 3.2.3.2. Membrane Bioreactor .......................................................................................12

4.0 EVALUATION OF LONG LIST OF SECONDARY AND TERTIARY TREATMENT OPTIONS ..................................................................................................................................13

5.0 DETAILED REVIEW OF SHORTLISTED OF SECONDARY TREATMENT OPTIONS ..16

5.1. EXTENDED AERATION – ADVANTAGES AND DISADVANTAGES ...........................................17 5.2. SEQUENCE BATCH REACTOR – ADVANTAGES AND DISADVANTAGES ................................17 5.3. MEMBRANE BIOREACTOR – ADVANTAGES AND DISADVANTAGES .....................................19 5.4. MOVING BED BIOREACTOR – ADVANTAGES AND DISADVANTAGES ...................................20 5.5. BIOLOGICAL AERATED FILTER – ADVANTAGES AND DISADVANTAGES ...............................21 5.6. SUMMARY OF SECONDARY TREATMENT ADVANTAGES AND DISADVANTAGES ...................23

6.0 DETAILED REVIEW OF SHORTLISTED OF TERTIARY TREATMENT OPTIONS .......25

6.1. MICROSAND BALLASTED CLARIFICATION – ADVANTAGES AND DISADVANTAGES ................25 6.2. CONTINUOUS BACKWASH FILTERS – ADVANTAGES AND DISADVANTAGES ........................27



6.3. MEMBRANE ULTRAFILTRATION – ADVANTAGES AND DISADVANTAGES ..............................29 6.4. MEMBRANE BIOREACTOR – ADVANTAGES AND DISADVANTAGES .....................................30 6.5. SUMMARY OF TERTIARY TREATMENT ADVANTAGES AND DISADVANTAGES .......................30

7.0 EVALUATION OF SHORTLIST OF SECONDARY AND TERTIARY TREATMENT OPTIONS ..................................................................................................................................32

7.1. TERTIARY TREATMENT CONCEPTUAL DESIGN AND EVALUATION ......................................32 7.2. COMPLETE SYSTEM CONCEPTUAL DESIGN .....................................................................34

8.0 SUMMARY AND CONCLUSIONS .................................................................................39



LIST OF TABLES Table 2.1 – Design Flows ........................................................................................................... 2Table 2.2 – Raw Wastewater Characteristics ............................................................................. 2Table 2.3 – Effluent Limits .......................................................................................................... 3Table 4.1 – Evaluation of Long List of Secondary Treatment Options .......................................13Table 4.2 – Evaluation of Long List of Tertiary Treatment Options ............................................14Table 5.1 – Summary of Secondary Treatment Advantages and Disadvantages ......................23Table 6.1 – Summary of Tertiary Treatment Advantages and Disadvantages ...........................31Table 7.1 – Comparison of Tertiary Treatment Options .............................................................33Table 7.2 – Tertiary Treatment Options Evaluation ...................................................................34Table 7.3 – Conceptual Design Processes ................................................................................35Table 7.4 – Sludge Storage Capacities by Secondary Treatment Option ..................................36Table 7.5 – Comparison of Complete Systems by Secondary Treatment Option ......................37Table 7.6 – Complete Systems Evaluation by Secondary Treatment Option .............................38 LIST OF FIGURES Figure 1-1 – Aerial View of Millbrook WWTP (Bing) ................................................................... 1Figure 5-1 – Typical Extended Aeration Process Configuration .................................................17Figure 5-2 – ISAM™ SBR System (www.fluidynecorp.com) ......................................................18Figure 5-3 – Typical ISAM™ SBR Process Configuration .........................................................18Figure 5-4 – Typical MBR Process Configuration ......................................................................19Figure 5-5 – Typical MBBR Process Configuration ...................................................................20Figure 5-6 – Degremont BIOFOR®-N System (www.degremont-technologies.com) .................21Figure 5.7 – Typical BAF Process Configuration .......................................................................22Figure 6-1 – Veolia Water Actiflo™ System (www.veoliawaterst.com) ......................................26Figure 6-2 – Typical Microsand Ballasted Clarification Process Configuration ..........................26Figure 6-3 – Parkson DynaSand® System (www.parkson.com) ................................................27Figure 6-4 – Typical Continuous Backwash Filter Process Configuration ..................................28Figure 6-5 – GE Z-PAK™ Ultrafiltration System ........................................................................29Figure 6-6 – Typical Membrane Ultrafiltration System Configuration .........................................30



APPENDICES Appendix A – MOE Memorandum Dated February 1, 2013 Appendix B – Budgetary Quotations from Manufacturers

Township of Cavan Monaghan 1


1.0 INTRODUCTION

The Millbrook Wastewater Treatment Plant (WWTP) is owned by the Township of Cavan

Monaghan and operated by OCWA. It currently operates under an Amended Certificate of

Approval (C of A) No. 1685-5VSLQ7 dated February 18th, 2004. The plant has a rated capacity

of 1,326 m3/day.

The Millbrook WWTP was constructed in 1975 as an extended aeration plant consisting of an

aeration tank and clarifier. The plant was expanded in 2003 to add sludge treatment and

storage capacity and to replace the former chlorine disinfection system with UV disinfection.

Figure 1-1 – Aerial View of Millbrook WWTP (Bing) Under this project the rated capacity of the plant will be expanded to 2,520 m3/day with a peak

flow capacity of 8,242 m3/day. In addition to this, it is expected that effluent criteria will be given

to the plant for the removal of total ammonia nitrogen (TAN) and total phosphorous (TP). To

achieve these objectives a new treatment train will be constructed. This train will be complete

with biological treatment system for TAN removal, tertiary treatment for TP removal, and

disinfection prior to discharge.



2.0 DESIGN FLOWS, LOADINGS, AND EFFLUENT REQUIREMENTS

The selection and evaluation of process options are based on the flows, loadings, and effluent

criteria as identified below. Table 2.1 provides a summary of design flows and Table 2.2

presents the raw wastewater characteristics.

Table 2.1 – Design Flows

Design Flows Value Unit Average Day Flow (ADF) 2,520 m3/d

Peak Hour (PHF) 8,242 m3/d

Table 2.2 – Raw Wastewater Characteristics

Parameter Value Unit

BOD5 190 mg/L

TSS 210 mg/L

TKN 25 mg/L

Phosphorus 5 mg/L

Average Temperature 15 °C

Minimum Temperature 8 °C

Maximum Temperature 20 °C

The effluent requirements, as agreed with the MOE in their memorandum dated February 1,

2013 (Appendix A) are summarized in Table 2.3 below.



Table 2.3 – Effluent Limits

Parameter

Effluent Limit

(mg/L)

Loading (kg/d)

Effluent Objective

(mg/L)

cBOD5 7.0 17.7 5.0

TSS 6.0 15.1 5.0

Total Phosphorus 0.15 0.38 0.1

Total Ammonia Nitrogen (Summer) 2.0 5.0 1.0

Total Ammonia Nitrogen (Winter) 3.0 7.6 2.0

E.Coli (org/100mL) 100 N/A 100

pH 6 to 9.5 N/A N/A



3.0 LONG LIST OF SECONDARY AND TERTIARY TREATMENT OPTIONS

There exist a large number of treatment options to meet the effluent requirements. A long list of

options was generated and is discussed further in this section.

3.1. Long List of Secondary Treatment Options

Secondary treatment will be used at the Millbrook WWTP to remove total ammonia nitrogen

(TAN) and biological oxygen demand (BOD5) for a non-toxic effluent. The technologies to be

considered fall under one of three categories:

• Suspended Growth Processes

• Fixed Film Processes

• Hybrid Processes

3.1.1.

Suspended Growth Processes

Suspended growth processes make use of microorganisms which are maintained in suspension

in the wastewater to consume nutrients.

3.1.1.1. Conventional Activated Sludge

The conventional activated sludge (CAS) process utilizes primary clarifiers, aeration tanks, and

secondary clarifiers. This type of activated sludge process has a shorter hydraulic retention

time in the aeration tank as compared to the extended aeration process. Following the primary

clarifier, the wastewater passes through an aeration tank, with a hydraulic retention time of at

least 6 hours, where oxygen is introduced to allow bacteria to grow and consume the

components of the wastewater, thus removing TAN and other toxic components. Following this

the wastewater enters a secondary clarifier where biologically active sludge settles out and the

effluent is discharged to tertiary treatment. This biologically activated sludge is continually

recycled back to the aeration tank as Return Activated Sludge (RAS).



This process has seen significant use in the past and is very common. Due to the large area

required for at least three process tanks, this option requires the most area relative to other

secondary treatment options.

3.1.1.2. Extended Aeration

The current process being employed by the Millbrook WWTP is an extended aeration system

with a mechanical aeration tank and a secondary clarifier.

Extended aeration is similar to CAS as it requires an aeration tank and secondary clarifier. The

aeration tank for this system must be sized with a minimum hydraulic retention time of 15 hours,

making it 2.5 times larger than the CAS aeration tank. However, due to this increased retention

time, no primary clarification is required.

The secondary clarifier and RAS system are similar to those described for the CAS system. As

a result of this, this system will be smaller than the CAS system.

3.1.1.3. High-Rate Activated Sludge

The high rate activated sludge system is similar to CAS system but requires less hydraulic

retention time. However, as a result of this decrease in retention time it is not capable of

providing the necessary nitrification.

3.1.1.4. Sequence Batch Reactor

The sequence batch reactor is operated as a fill-and-draw activated sludge system. This

system acts as multiple treatment stages in a batch system. The tank is first filled with

wastewater and then aerators in the tank are started to provide oxygen for biological growth and

nitrification. The air is then stopped to allow the system to settle. After a pre-set amount of

time, decanters allow the clarified effluent to be removed from the top of the tank while some

waste activated sludge is removed from the bottom.



This system does not require any additional tankage for primary or secondary clarification. The

drawbacks for this system are its relatively complex controls and requirement for multiple tanks

so that one may be filling at all times.

To limit the influence of peak flows on the system a true batch system includes additional

tankage before the sequence batch reactor tanks. These tanks allow for flow equalization, more

thorough mixing of batches, and sludge storage and thickening. This form of sequence batch

reactor system will be considered as the base sequence batch reactor.

3.1.1.5. Membrane Bioreactor

The membrane bioreactor (MBR) requires a similar aeration tank as the conventional activated

sludge system where suspended growth can occur. Inside a separate tank are a series of

membrane ultrafiltration units which filter the water that passes through them to a very fine level.

As a result of this, the MBR is capable of providing secondary and tertiary treatment in one

process. No primary or secondary clarification is required for this technology. Permeate pumps

are required in order to create a vacuum to pull effluent through the membrane ultrafilters in

addition to special cleaning chemicals to clean the ultrafilters when required. Due to the

sensitivity of the membrane ultrafilters, fine screening is required upstream of the aeration tanks

to remove particles which could damage them.

3.1.2.

Fixed Film Processes

Fixed film processes make use of packing in the aeration tank on which a biological film may

grow, providing biological treatment.

3.1.2.1. Moving Bed Bioreactor

Moving bed bioreactors consist of an aeration tank which contains engineered packing and a

secondary clarifier. The packing in the aeration tank are specialized geometric shaped carriers

which create a large surface area to volume on which a biofilm can grow. This additional biofilm

area increases the breakdown of nutrients in the aeration tank and as such a smaller aeration



tank is required. The aeration system, in addition to providing the oxygen required for the

bacteria to live, mixes the packing throughout the tank. Tanks are equipped with screens to

keep the media within the tank.

This system requires secondary clarifiers, but activated sludge recirculation is not required as

the media provides sufficient area for the biofilm to continue to live. This technology requires a

relatively small area.

3.1.2.2. Rotating Biological Contactor

A rotating biological contactor utilizes rotating discs, on which biofilm can grow to allow for

biological treatment. These discs are partially submerged, allowing the biofilm to be rotated out

of the wastewater in order to supply oxygen for biological growth. The biofilm build-up on these

discs grows until it reaches a point where it sloughs off into the wastewater and is carried to the

secondary clarifiers. Due to this, secondary clarifiers are required for this technology. These

contactors also require effective primary clarification before them, to remove any scum or

grease to prevent fouling of the discs. Because these systems are exposed to open air, they

are greatly impacted by temperature and as such are not recommended for colder climates

unless they are housed in a temperature controlled area, as per MOE Design Guidelines.

3.1.2.3. Trickling Filter

Trickling filters are large beds of media in which wastewater is sprayed on top of and is then

allowed to trickle down through the media. The biofilm grows on the media to allow for

biological treatment. Because this system is not submerged, oxygen is readily available to the

biofilm. These filters require both primary and secondary clarification as they are very

susceptible to solids fouling. This type of filter is heavily impacted by temperature and is not

recommended for colder climates.

3.1.3.

Hybrid Processes

Hybrid processes use a combination of suspended growth and fixed film for the biological

treatment of wastewater.



3.1.3.1. Integrated Fixed-film Activated Sludge

The integrated fixed-film activated sludge (IFAS) process is similar to the MBBR process

described above. However, less packing is used for IFAS, as suspended growth is also used.

In order to ensure that a sufficient amount of suspended growth is maintained a RAS system is

required. As a result, this system requires secondary clarification.

3.1.3.2. Biological Aerated Filters

Biological aerated filters (BAF) contain a fixed bed of media on which biomass is grown.

Wastewater is either introduced to the top or bottom of the tank and must flow through the

media to leave the tank. Air is introduced into these tanks underneath the media to provide for

biological growth and to allow for scouring of the media during backwashing. Eventually the

biofilm in the media grows too large and must be removed, at this point the tank must be shut

down and backwashed. This adds an additional level of complexity to this process as compared

to other tertiary treatment options. Since the media in the filters can be fouled, primary

clarification is required. Due to the filtration action by the media, no secondary clarification is

required for this process. However, due to the need to backwash these systems, additional

tanks are recommended, including all associate backwash and air piping systems.

3.2. Long List of Tertiary Treatment Options

Tertiary treatment will be used at the Millbrook WWTP to remove phosphorous from the plant

effluent prior to discharge to Baxter Creek. The technologies considered will be categorized as

follows:

• Tertiary Clarification

• Tertiary Filtration

• Membrane Filtration



3.2.1.

Tertiary Clarifications

Tertiary clarifiers use gravity in tanks to settle out flocculated phosphorous and other

contaminants.

3.2.1.1. Conventional Tertiary Clarifiers

Conventional tertiary clarifiers utilize the same mechanism as typical primary and secondary

clarifiers. These clarifiers take up a substantial area as compared to other treatment

technologies. This technology is also not known to be reliable in terms of TP removal and there

are no known installations in Ontario.

3.2.1.2. Microsand Ballasted Clarification

This type of ballasted clarification seeds the effluent with microsand particles which promote the

removal of flocculated phosphorous. These systems require flash mixing tanks to introduce

microsand to the effluent and a gravity clarifier where the flocculated contaminants can settle.

From here the microsand is separated from the flocculated contaminants and is recycled back

to the system while the contaminants are removed. These systems require significant amounts

of material handling to ensure that the microsand is continuously topped off. This system

requires a relatively small area.

3.2.1.3. Magnetite Ballasted Clarification

This type of ballasted clarification is similar to the microsand system described above except

that it uses magnetite instead of microsand particles. The magnetic properties allow this system

to more effectively remove total phosphorous from the wastewater. This system, however,

requires additional steps to recycle the magnetite and requires a significant amount of labour.

This treatment technology has not been used in Ontario.



3.2.1.4. High-Rate Solids Contact Clarification

High-rate solids contact clarifiers use the same clarifier configuration as the ballasted

clarifications systems. With this system, however, no ballast is added, so it relies on chemical

addition and a larger area for settling. This results in a larger treatment area than the ballasted

systems but a smaller area than the conventional tertiary clarifiers. This system has no

installations in Ontario.

3.2.2.

Tertiary Filtration

Tertiary filtration utilizes media that plant effluent must pass through which physically removes

phosphorous and other contaminants.

3.2.2.1. Conventional Automatic Backwash Filters

Conventional automatic backwash filters pass effluent through a shallow bed of sand by gravity.

This is the most common form of tertiary treatment. The system allows for continuous treatment

of plant effluent with separate filters cells being taken offline for backwashing at pre-determined

times. The sand bed typically consists of either a single layer (sand) or dual layer (sand and

anthracite). This type of tertiary filtration requires a significant footprint relative to other

treatment processes.

3.2.2.2. Continuous Backwash Filters

Continuous backwash filters are an up flow type of filter whereby the effluent is directed to the

bottom of a deep bed of sand media and then flow upwards through the media where total

phosphorous is removed. The media in this filter is continuously cleaned by cycling it through

the use of compressed air and a central air lift pipe, and as such, does not require filters to be

taken offline for backwashing of the media. These filters take up a relatively small footprint as

compared to other options but do require either deep excavation to install them or lift pumps to

pump up to a high level.



3.2.2.3. Adsorptive Media Continuous Backwash Filters

Adsorptive media continuous backwash filters operate in the same way as the continuous

backwash filters described above. The only difference is that the media used has a chemical

coating on it which is able to adsorb total phosphorous on to it, increasing its effectiveness.

Additional equipment is required to continually clean and regenerate the media in this system.

Pilot tests have been completed for this technology, but there have been no installations in

Ontario.

3.2.2.4. Cloth Media Disc Filters

Cloth media filters utilize a cloth media in which effluent is passed through. This media comes

in various materials and geometries. Effluent is directed to either the inside or outside of a

series of media discs and must flow through the media to the inside or outside of the disc to flow

out. This type of tertiary filtration has the highest operating cost as operator attention is required

for the removal, cleaning, or replacement of the media discs. This system has a relatively small

footprint as compared to the other tertiary filtration options. Currently, cloth media filters are not

proven to be able to achieve the required effluent quality.

3.2.3.

Membrane Filtration

Membrane filtration use specialized membrane filters to remove phosphorous and other

contaminants.

3.2.3.1. Membrane Ultrafiltration

Membrane ultrafiltration uses very fine membranes to physically separate phosphorous and

other contaminants from the plant effluent as it passes through them. The ultrafilters are fine

enough to remove bacteria in the water and thus does not require disinfection to be run

continuously afterwards. Due to the fine nature of these ultrafilters, pumping is required to pull

water through them. These systems are capable of providing an effluent with less than 0.05

mg/L total phosphorous. Operating costs for these units will be relatively high as membranes

need to be replaced and cleaned on an ongoing basis in addition to the high energy costs



associated with the additional pumps and blowers required to run this system. This technology

requires a relatively small area.

3.2.3.2. Membrane Bioreactor

A membrane bioreactor (MBR) is membrane ultrafiltration system immediately following

biological secondary treatment. As a result of this it provides all the same benefits and

drawbacks as the membrane ultrafilters. Additional equipment, such as permeate pumps, air

scour blowers, and cleaning chemicals are required for this system.



4.0 EVALUATION OF LONG LIST OF SECONDARY AND TERTIARY TREATMENT OPTIONS

The long list of secondary and tertiary treatment options were evaluated on a Pass/Fail basis.

The Pass/Fail criteria to be used are:

• Experience and approval in Ontario with similarly sized plants

• Ability to meet effluent limits

• Minimizes process footprint

The evaluation for the secondary treatment technologies is shown in Table 4.1.

Table 4.1 – Evaluation of Long List of Secondary Treatment Options

Process

Experience and

Approval in Ontario

Able to Meet

Effluent TAN Limits

Minimizes Process Footprint Notes

Suspended Growth Processes

Conventional Activated Sludge

YES YES NO

Largest secondary treatment process. Primary treatment required.

Extended Aeration YES YES YES High-Rate Activated Sludge

YES NO YES Does not provide nitrification.

Sequence Batch Reactor YES YES YES Membrane Bioreactor YES YES YES Fixed Film Processes Moving Bed Bioreactor YES YES YES Rotating Biological Contactor

LIMITED YES YES

Requires temperature controlled area. Primary treatment required.

Trickling Filter

LIMITED YES YES

Not recommended for cold climates. Primary treatment required.

Hybrid Processes Integrated Fixed-film Activated Sludge

LIMITED YES YES

Usually an upgrade option. Approval may require a 12-month process audit.

Biological Aerated Filters YES YES YES



Based on this evaluation the following secondary treatment technologies are shortlisted to be

compared in more detail:

• Extended aeration

• Sequence batch reactor

• Membrane bioreactor

• Moving bed bioreactor

• Biological aerated filter

The evaluation for the tertiary treatment technologies is shown in Table 4.2.

Table 4.2 – Evaluation of Long List of Tertiary Treatment Options

Process

Experience and

Approval in Ontario

Able to Meet 0.1 mg/L TP Objective

Minimizes Process Footprint Notes

Tertiary Clarification Conventional Tertiary Clarifier

NO NO NO

Largest area. Cannot consistently meet 0.1 mg/L TP

Microsand Ballasted Clarification YES YES YES Magnetite Ballasted Clarification NO YES YES No installations in Ontario. High-Rate Solids Contact Clarification

NO YES NO

Larger area than ballasted clarification. No installations in Ontario.

Tertiary Filtration Conventional Automatic Backwash Filters YES YES NO

Largest tertiary filtration area required.

Continuous Backwash Filters YES YES YES Adsorptive Media Continuous Backwash Filters NO YES YES No installations in Ontario. Cloth Media Disc Filters

NO YES YES

Limited experience in Ontario. Not proven in full scale to meet 0.1 mg/L TP limit.

Membrane Filtration Membrane Ultrafiltration

YES YES YES Membrane Bioreactor YES YES YES



Based on this evaluation the following tertiary treatment technologies are shortlisted to be

compared in more detail:

• Microsand Ballasted Clarification

• Continuous Backwash Filters

• Membrane Ultrafiltration

• Membrane Bioreactor



5.0 DETAILED REVIEW OF SHORTLISTED OF SECONDARY TREATMENT OPTIONS

The shortlisted secondary treatment technologies were evaluated based on several criteria to

make a final selection. In order to compare these technologies more thoroughly,

suppliers/manufacturers were contacted to obtain further information. The manufacturers

selected for each technology were:

• Extended aeration – No supplier required as this is not a proprietary process

• Sequence batch reactor – ISAM™ SBR manufactured by Fluidyne Corporation

• Membrane bioreactor – Z-MOD™ MBR manufactured by GE Water & Process

Technologies, Enviroquip® MBR manufactured by Ovivo, and MicroClear™ MBR

manufactured by Newterra Ltd.

• Moving bed bioreactor – CFIC® manufactured by Biowater, Meteor® manufactured by

Degremont, and Anoxkaldnes™ manufactured by Veolia Water

• Biological aerated filter – BIOFOR®-N manufactured by Degremont

These manufacturers were contacted to provide budgetary quotations in order to evaluate the

shortlisted technologies. The budgetary quotations and background information are provided in

Appendix B. It should be noted that there exist other manufacturers of similar technologies and

that this list should not be perceived as a pre-selection of one manufacturer. The final selection

of technology manufacturer should be done through a formal pre-selection during the

preliminary design phase.

A summary of each of these technologies can be found in Section 3.1. This section will detail

the advantages and disadvantage of each technology including their costs, treatment

requirements, and other processes required in addition to meet the required effluent criteria.



5.1. Extended Aeration – Advantages and Disadvantages

The extended aeration system is a very common treatment system and as such requires no

proprietary technology. It consists simply of aeration tanks and secondary clarifiers. This

process is what is currently being used by plant staff so it will require little additional training. A

typical schematic for the extended aeration process can be seen in Figure 5-1.

Figure 5-1 – Typical Extended Aeration Process Configuration

The extended aeration system, due to the minimum 15 hours of retention time, requires the

largest aeration system of all the selected options. This tank increases the amount of land

required for the plant. In addition to this, large aeration blowers will be required which will give

this system a relatively high operational cost.

This process will required additional tertiary filters to meet the TP effluent criteria. This will add

to the total required area, capital and operating costs.

5.2. Sequence Batch Reactor – Advantages and Disadvantages

Traditional sequence batch reactors (SBR) require separate tanks which handle all flow in batch

processes. Due to the variations in flow these systems would require flow equalization to

operate properly. For this technology review, the ISAM™ SBR system was investigated which

utilizes a series of tanks to eliminate the need for flow equalization while providing all process

requirements in one set of tanks. A section of this system can be seen in Figure 5-2.

Extended Aeration Tank

Secondary Clarifier Secondary

EffluentScreened Influent

RAS

WAS

Process Air



Figure 5-2 – ISAM™ SBR System (www.fluidynecorp.com)

This SBR system incorporates additional tankage before the SBR tanks. The first tank is the

ISAM™ tank which allows for solids to be removed and stored. In doing so, the sludge removed

from this tank is relatively thick and can be sent to the plant’s digester system. The second tank

is the SAM™ tank where flow can be equalized. This tank contains submersible pumps for

conveying the influent to the SBR tank. When enough flow has entered the SAM™ tank the

pumps convey the fluid to the SBR tank and an aeration system is started as required for the

process. By having two full trains no additional flow equalization will be required. A typical

schematic of this system can be seen in Figure 5-3.

Figure 5-3 – Typical ISAM™ SBR Process Configuration

In the SBR tank, the process follows a series of steps: mixing without aeration, mixing with

aeration, settling, and decanting. During the decant period the clean water in the SBR tank

Screened Influent

Secondary Effluent

Sludge

ISAM™ Tank

SAM™ Tank

SBR Tank

Process Air



flows out while the remaining sludge is used to seed the next batch in the SBR. An overflow

line in the SBR tank allows fluid to return to the SAM™ tank to keep this portion of the train

seeded and to allow the mixing process to take place while the system is being loaded.

This system requires very little equipment to operate. As such it has the lowest operating and

maintenance cost of all the options investigated.

This process, however, requires the largest area for the proposed tanks. Due to the staged

process, automated controls are needed to ensure all valves and equipment are operated when

required. The effluent produced from this system will have to be treated by a tertiary system.

5.3. Membrane Bioreactor – Advantages and Disadvantages

Membrane bioreactors (MBR) consist of biological treatment followed by an ultrafiltration

membrane system. The membrane system utilizes vacuum pumps to pull the mixed liquor

through the membranes, producing an effluent which meets tertiary effluent requirements in

terms of TAN and TP. Additionally due to the fine nature of the ultrafilters continuous

disinfection is not required following the MBR. A typical layout for this system can be seen in

Figure 5-4.

Figure 5-4 – Typical MBR Process Configuration

Various configurations for the aeration tanks are recommend by different manufacturers. Some

manufacturers recommend separate anaerobic, anoxic, and aerated tanks to optimize the

Screened Influent

Secondary/ Tertiary Effluent

RAS

Fine Screens

Aeration Tanks

MBR Tanks

WAS

Process Air



biological process while others require different aeration tank volumes to optimize the mixed

liquor concentrations. All of these options are considerably smaller than the extended aeration

system.

Additional equipment is required for this system. Air scour blowers are required to keep the

membranes clean as sludge builds up on the outside of the units. The aforementioned vacuum

or permeate pumps must run continuously to convey treated effluent through the membranes.

Similar RAS/WAS pumps and aeration blowers as the extended aeration system will be required

for the biological treatment portion of this process.

The membranes themselves pose a significant maintenance item as they require chemical

cleaning and will eventually breakdown and need replacement. Cleaning is to be conducted at

regular intervals with chemicals not normally stocked at the treatment plant. The membrane

units are relatively expensive and their eventual replacement must be budgeted by the plant.

5.4. Moving Bed Bioreactor – Advantages and Disadvantages

The moving bed bioreactor (MBBR) system is similar to the extended aeration system as it

contains an aerated basin and secondary clarifier. The key differences are the addition of

packing in the aeration tank to promote biofilm growth and the elimination of the return activated

sludge system. A typical schematic of this system can be seen in Figure 5-5.

Figure 5-5 – Typical MBBR Process Configuration

MBBR Tanks

Secondary Clarifier Secondary

EffluentScreened Influent

WAS

Process Air



Depending on the manufacturer of the MBBR system, different configurations of MBBR tanks

are recommended. The configurations vary from one large tank to four smaller tanks in series.

At the core of each of these processes, however, is the use of specially design media. Each

manufacturer utilizes a different packing configuration in order to maximize the surface area

available for biofilm growth. Air is added to this system through diffusers which promotes the

growth of biofilm on the media while keeping it suspended. Screens are installed in the tank to

keep the media from leaving the tank with the effluent.

Due to the increased biomass in the aeration tank, a smaller tank can be used as compared to

extended aeration. Secondary clarification is still needed because the biofilm on the packing

will eventually be sloughed off and carried through the screens.

Tertiary treatment is required for this system to remove phosphorous.

5.5. Biological Aerated Filter – Advantages and Disadvantages

Biological aerated filters (BAF) utilize a layer of media to promote biofilm growth. For this

review the BIOFOR®-N system by Degremont was investigated. A section of their system can

be seen in Figure 5-6.

Figure 5-6 – Degremont BIOFOR®-N System (www.degremont-technologies.com)



Influent is introduced to the BAF tanks below the media layer where it must flow up through the

media. In addition to this, process air is introduced along with the influent to provide air for

biofilm growth on the media. The fine nature of the media allows for a significant amount of

biomass to accumulate in the tank which must eventually be cleaned. To accommodate this a

backwash system incorporated a separate backwash water tank, pumps, and air scour system

must be provided. This additional equipment increases the overall complexity and maintenance

requirements of the system. A control system would be required to facilitate the backwashing of

tanks as required.

A benefit of the fine media is that it removes solids from the water, thus eliminating the need for

secondary clarification. This benefit is negated, however, by the need for primary clarification

prior to the BAF system. Primary clarification is required to remove some solids as well as fats,

oils, and greases to ensure that the filters do not become prematurely fouled. A typical

schematic of the system can be seen in Error! Reference source not found..

Figure 5.7 – Typical BAF Process Configuration A disadvantage of this system is the requirement for both clean water and waste water tanks to

be used by the backwash system. These extra tanks add to the overall size of the system. The

extra equipment required to backwash the filters will also increase the overall operating cost of

this system.

Tertiary treatment would be required following the BAF process.

BAF Tank

Primary ClarifierScreened

Influent

Process Air

Secondary Effluent

Wash Water

Sludge

Clean WaterTank

Waste WaterTank



5.6. Summary of Secondary Treatment Advantages and Disadvantages

A summary of advantages and disadvantages of the secondary treatment technologies

investigated is present in Table 5.1.

Table 5.1 – Summary of Secondary Treatment Advantages and Disadvantages Process Advantages Disadvantages

Extended Aeration • No proprietary processes

• Plant familiarity

• Does not require primary

clarification

• Large footprint

• High energy costs

• Requires tertiary treatment

Sequence Batch

Reactor • Fewest pieces of equipment

• Low operating cost

• Does not require primary or

secondary clarification

• Provides long sludge storage

time

• Automated controls

• Large footprint


Membrane Bioreactor • Small footprint


secondary clarification or

tertiary treatment

• Does not require continuous

disinfection

• Requires periodic chemical

cleaning

• High operating cost

• Complex process

• High maintenance cost

Moving Bed

Bioreactor • Low complexity

• Smaller aeration tank as

compared to extended

aeration

• Does not require primary

clarification

• Require proprietary packing in

aeration basin




Process Advantages Disadvantages

Biological Aerated

Filter • Does not require secondary

clarification

• Susceptible to fouling

• Complex controls required


• Requires primary clarification

• Requires additional backwash

clean water tank




6.0 DETAILED REVIEW OF SHORTLISTED OF TERTIARY TREATMENT OPTIONS

The shortlisted tertiary treatment technologies were evaluated based on several criteria to make

a final selection. In order to compare these technologies suppliers/manufacturers were

contacted to obtain further information. The manufacturers selected for each technology were:

• Microsand ballasted clarification – Actiflo™ manufactured by Veolia Water

• Continuous backwash filters – DynaSand® manufactured by Parkson Corporation

• Membrane ultrafiltration – Z-PAK™ manufactured by GE Water & Process Technologies

• Membrane bioreactor – Z-MOD™ manufactured by GE Water and Process

Technologies, Enviroquip® manufactured by Ovivo, and MicroClear™ manufactured by

Newterra Ltd.

These manufacturers were contacted to provide budgetary quotations in order to develop the

evaluation of the shortlisted technologies. The budgetary quotations and background

information can be seen in Appendix B. It should be noted that there exist other manufacturers

of similar technologies and that this list should not be perceived as a pre-selection of one

manufacturer. The final selection of technology manufacturer should be done through a formal

pre-selection during the preliminary design phase.

6.1. Microsand Ballasted Clarification – Advantages and Disadvantages

The microsand ballasted clarification technology was evaluated based on the Actiflo™ system

by Veolia Water. A section of the Actiflo™ system can be seen in Figure 6-1.



Figure 6-1 – Veolia Water Actiflo™ System (www.veoliawaterst.com)

The Actiflo™ system is a series of tanks which perform specific tasks. In the first tank the

secondary effluent is treated with a polymer to promote coagulation of phosphorous. Following

this, the effluent is injected with the microsand ballast which when mixed with the effluent

increases flocculation. The next tank provides less intense mixing to allow the flocs to grow

larger until the effluent enters a sedimentation tank. Using plate settlers the area required for

this settling tank is minimized while removing the ballasted flocs. A typical schematic for this

system can be seen in Figure 6-2.

Figure 6-2 – Typical Microsand Ballasted Clarification Process Configuration

The floc that settles out of the sedimentation tank is sent to a hydrocyclone unit which separates

the microsand ballast and sludge. The microsand ballast is recycled back into the process while

the sludge is sent to the plant’s digester system.

Secondary Effluent

Waste

Coagulation Tank

Injection Tank

Maturation Tank

Tertiary Effluent

Sedimentation Tank

Hydrocyclone

Sand



The Actiflo™ system is relatively small, using a compact series of tanks to allow for TP removal.

The primary disadvantage of this system is its relative complexity and the requirement to be

closely monitored. The loss of microsand ballast through continuous operation requires manual

replenishment, resulting in an increase to the overall operating and maintenance cost.

6.2. Continuous Backwash Filters – Advantages and Disadvantages

The continuous backwash filer technology was evaluated based on the DynaSand® system by

Parkson. A section of the DynaSand® system can be seen in Figure 6-1.

Figure 6-3 – Parkson DynaSand® System (www.parkson.com)



Secondary effluent is treated with a coagulant and then directed to the bottom of a series of

deep bed sand filters. As the water passes up through the sand media, phosphorous and other

impurities are removed and the cleaned effluent flows over weirs and leaves the system. As the

system runs the media becomes fouled with the contaminants it removed from the water. In

order to clean the sand it is continuously cycled through an air lift pipe and gravity cleaning

system. The air lift pipe operates by having a compressor system continuously inject air at its

base which induces a suction which carries sand from the bottom of the filter to a cleaning

chamber at the top where the sand is separated from the contaminants and is allowed to settle

down on top of the media bed. The contaminated water is removed from the system and sent

back to the head of the plant to be re-treated. A typical schematic for this system can be seen

in Figure 6-4.

Figure 6-4 – Typical Continuous Backwash Filter Process Configuration

This system contains no moving parts which makes its operation very simple. The only

additional equipment required are air compressors for the air lift system. This system requires a

small footprint.

One disadvantage of the continuous backwash filter system is the stream of waste water that

needs to be recycled through the plant. This negatively impacts the plants overall capacity as it

is being consumed to re-treat tertiary filter wastes. It should be noted that by introducing

controls to the system, the filters may be intermittently washed which reduces the load on the

plant’s capacity.

Secondary Effluent

Tertiary Effluent

Continuous Backwash Filters

Process Air

Waste



Another disadvantage of this system is the overall depth of the tanks. The filters can be 6m

deep which would require either very deep excavation or additional pumping.

6.3. Membrane Ultrafiltration – Advantages and Disadvantages

The membrane ultrafiltration technology was evaluated based on the Z-PAK™ ultrafiltration

system by GE. A section of the Z-PAK™ system can be seen in Figure 6-5.

Figure 6-5 – GE Z-PAK™ Ultrafiltration System

The system consists of a series of ultrafilter modules that permeate pumps pull the secondary

effluent through. This system operates in a similar manner to the MBR system but with less



robust membranes as they are not exposed to the mixed liquor of the aeration tanks. A typical

schematic for this system can be seen in Figure 6-6.

Figure 6-6 – Typical Membrane Ultrafiltration System Configuration

The advantage of this system is that it can produce a tertiary effluent with TP levels of less than

0.05 mg/L. For the Millbrook WWTP, the effluent limit for TP has been set to 0.1 mg/L so this

advantage is not crucial for the selection of tertiary treatment.

Disadvantages are similar to those discussed for the membrane bioreactor technology. As

such, membrane ultrafiltration systems are both operations and maintenance intensive, require

relatively complex controls, and require periodic cleaning with chemicals not normally stocked at

the treatment plant. Due to the extra equipment required to run this system, additional building

space will be required.

6.4. Membrane Bioreactor – Advantages and Disadvantages

Please see Section 5.3 for discussion on membrane bioreactors.

6.5. Summary of Tertiary Treatment Advantages and Disadvantages A summary of advantages and disadvantages of the tertiary treatment technologies investigated

is present in Table 6.1.

Secondary Effluent

Membrane Ultrafilters

Process Air

WasteTertiary Effluent

Backwash



Table 6.1 – Summary of Tertiary Treatment Advantages and Disadvantages

Process Advantages Disadvantages

Microsand Ballasted

Clarification • Relatively small footprint • Labour intensive process

• Requires many pieces of

equipment

Continuous

Backwash Filter • Only one piece of equipment

• Relatively simple operation

• Possible continuous waste

stream

• Deep excavation or pumping

required

Membrane

Ultrafiltration • Produces very clean tertiary

effluent


disinfection


cleaning


• Complex process


Membrane Bioreactor • Produces very clean tertiary

effluent

• Small footprint


secondary clarification or

tertiary treatment


disinfection


cleaning


• Complex process




7.0 EVALUATION OF SHORTLIST OF SECONDARY AND TERTIARY TREATMENT OPTIONS

To evaluate all the secondary and tertiary treatment options a conceptual level design was

prepared for each. Capital costs were determined by the quotations received from the

suppliers/manufacturers in addition to estimates for excavation, concrete tanks, buildings, and

other necessary equipment and processes. Operating costs were similarly determined based

on budgetary quotations of motor sizes and chemical requirements coupled with the extra

equipment deemed necessary. Based on these designs a rough estimate of the foot print

requirement for the entire process were determined for comparison.

In order to properly compare the secondary treatment options with the membrane bioreactor

option, the tertiary treatment options were evaluated first. In this way, the highest scoring

tertiary treatment system could be coupled with the secondary treatment options to provide a

complete system comparable to membrane bioreactor. The ultrafiltration option was modified to

include provision for fine screens.

For the secondary treatment options these conceptual level estimates include inlet works,

primary or secondary clarification, tertiary treatment, UV disinfection, sludge thickening, and

aerobic digester upgrades to existing tanks as required.

7.1. Tertiary Treatment Conceptual Design and Evaluation

The tertiary treatment options to be evaluated are:

• Microsand Ballasted Clarification

• Continuous Backwash Filters

• Membrane Ultrafiltration

The membrane bioreactor system was evaluated as a complete system along with the other

secondary treatment options as it fills the rolls of both secondary and tertiary treatment.



The submittal from Veolia Water consisted of an entire system. It was split up to obtain the cost

of their proposed Actiflo™ system.

Based on the submittals received the following costs and footprint requirements in Table 7.1

were determined.

Table 7.1 – Comparison of Tertiary Treatment Options

Technology Manufacturer Name Total Capital Cost

Present Value of 20 Year O&M

Footprint (m²)

Microsand Ballasted Clarification Veolia Actiflo™ $1,181,005 $1,198,119 25 Continuous Backwash Filters Parkson DynaSand® $773,707 $401,498 51 Membrane Ultrafiltration GE Z-PAK™ $2,119,076 $1,060,725 225

The equipment costs for either continuous backwash filter systems were considerably less than

that of the other options and as such have the lowest expected operating and maintenance

costs. The microsand ballasted clarification system has the lowest cost with respect to site

works and as such it has the smallest footprint. The membrane ultrafiltration system has the

highest costs and area required. The reason for the membrane ultrafiltration system’s relatively

high costs are the large amount of equipment required for the proper operation of this system

and the building needed to store all of this required equipment.

To evaluate these options the following criteria were used:

• Process Complexity

• Footprint

• Total Capital Cost

• Present Value of 20 Year Operation and Maintenance



Each criterion was assigned a maximum score of 25 points, making 100 points the best score.

More points were awarded based on the least complex process, lowest capital or O&M cost, or

footprint requirement. The process complexity criterion is based on the discussion of the

technology in Section 6.0. The following formula was used to determine a score for the cost

and footprint criteria:

×=

ActualMinimumScore 25

The scores of each option are shown in the following Table 7.2.

Table 7.2 – Tertiary Treatment Options Evaluation

This evaluation shows that, the highest ranked option is the continuous backwash filter system,

following by the microsand ballasted clarification system.

7.2. Complete System Conceptual Design

To evaluate the secondary treatment options, conceptual designs for complete systems were

developed. Each secondary treatment process has different requirements, both upstream and

downstream of it to provide the required effluent quality. A summary of the evaluated options

and their other process requirements can be seen in Table 7.3 below.

Technology

Criteria Criteria Weight

Microsand Ballasted

Clarification

Continuous Backwash

Filters

Membrane Ultrafiltration

(Z-PAK™)Process Complexity 25 15.0 20.0 10.0Footprint 25 25.0 12.1 2.8Total Capital Cost 25 16.4 25.0 9.1Present Value 20 Year O&M 25 8.4 25.0 9.5Total Score 100 64.8 82.1 31.4Rank 2 1 3



Table 7.3 – Conceptual Design Processes

Option Extended Aeration

Sequence Batch Reactor

Membrane Bioreactor

Moving Bed Bioreactor

Biological Aerated Filter

Pump Station Upgrades √ √ √ √ √ Equalization Tank √ Inlet Works √ √ √ √ √ Fine Screens √ Primary Clarification √ Biological Process √ √ √ √ √ Secondary Clarification √ √ Secondary Effluent Pumps √ Tertiary Treatment √ √ √ √ UV Disinfection √ √ √ √ √ Existing Tankage Refurbishment √ √ √ √ √ Sludge Thickening √ √ √ √ Admin Building √ √ √ √ √ Site Works √ √ √ √ √

The sludge thickening and aerobic digester upgrade items had to be carefully considered for the

conceptual designs. It is planned that once the new plant is operating, the old tanks on-site will

be re-purposed for either aerobic digestion or flow equalization. For all options, except the

sequence batch reactor, the sludge production resulted in the need to convert the existing

aeration tank and secondary clarifier into an aerobic digester. Following the digester, the sludge

would have to be run through a thickener to obtain sludge of at least 4.5% solids. This would

allow the existing sludge storage tank to provide the required 240 days of sludge storage.

For the sequence batch reactor system investigated, no digestion or thickening will be required

due to that fact that it contains a sludge storage tank with approximately 180 days of sludge

storage capacity. In this tank the sludge is digested anaerobically and thickened. In addition to

this tank, the existing sludge storage tank will be used to provide enough storage to get the

systems total storage time to above 240 days. As such, for this system, the existing tanks will

be re-used as a post biological treatment equalization tank. This will reduce the load on the

tertiary treatment and UV system so they do not need to be designed to handle the large flows

expected during decant periods.



A summary of the sludge storage capacities of each conceptual design is shown in Table 7.4

below.

Table 7.4 – Sludge Storage Capacities by Secondary Treatment Option

Technology Manufacturer Name

Sludge Storage in Existing

Storage Tank (days)

Sludge Storage in

Process Tank (days)

Total Sludge Storage (days)

Extended Aeration N/A

Extended Aeration 236 15 251

Sequence Batch Reactor Fluidyne ISAM™ 120 180 300 Membrane Bioreactor GE Z-MOD™ 236 21 257 Membrane Bioreactor Newterra MicroClear™ 236 20 256 Membrane Bioreactor Ovivo Enviroquip® 236 18 254 Moving Bed Bioreactor Biowater CFIC® 236 4 240 Moving Bed Bioreactor Degremont Meteor® 236 4 240 Moving Bed Bioreactor Entex BioPortz™ 236 4 240 Moving Bed Bioreactor Veolia Anoxkaldnes™ 236 4 240 Biological Aerated Filter Degremont BIOFOR®-N 236 15 251

Based on the identified requirements for each process a conceptual level costing was prepared

for each complete system. As a result of the analysis in Section 7.1, continuous backwash

filters will be used for the tertiary treatment portion of all of the options which require it. The

summary of the analysis can be seen below in Table 7.5.



Table 7.5 – Comparison of Complete Systems by Secondary Treatment Option

Technology Manufacturer Name

Secondary & Tertiary Equipment

Cost

Total Capital Cost

(Includes Mark-up)

Present Value of 20 Year O&M

Footprint (m²)

Extended Aeration N/A

Extended Aeration $2,636,000 $12,140,148 $4,943,130 630

Sequence Batch Reactor Fluidyne ISAM™ $891,000 $9,526,290 $3,054,402 913 Membrane Bioreactor GE Z-MOD™ $1,564,219 $10,503,752 $4,190,852 540 Membrane Bioreactor Newterra MicroClear™ $2,627,619 $11,565,981 $6,217,332 639 Membrane Bioreactor Ovivo Enviroquip® $2,242,619 $11,214,268 $4,994,481 582 Moving Bed Bioreactor Biowater CFIC® $3,440,000 $12,435,545 $5,495,399 556 Moving Bed Bioreactor Degremont Meteor® $3,034,000 $11,956,213 $5,163,465 627 Moving Bed Bioreactor Entex BioPortz™ $3,101,500 $13,123,624 $6,014,149 521 Moving Bed Bioreactor Veolia Anoxkaldnes™ $4,276,000 $12,573,973 $6,077,429 556 Biological Aerated Filter Degremont BIOFOR®-N $2,311,000 $11,085,476 $5,093,056 473

The total equipment cost included in the table shows the differences in the amount of equipment

required to run each system.

The sequence batch reactor resulted in the lowest capital and O&M costs but produced the

system requiring the largest area. This increased footprint is a result of this system’s added

tankage to allow for influent equalization, sludge storage and stabilization. As a result of this, it

will not require additional sludge handling processes, which will provide capital and operating

cost savings. The membrane bioreactor systems were all relatively similar in all categories.



The Z-MOD™ system by GE was the lowest in all the categories so it will be used in the

evaluation as the representative for membrane bioreactors. The moving bed bioreactor options

were all relatively similar in all categories but for the evaluation of technologies the Meteor®

system by Degremont will be used as it resulted in the lowest capital and O&M costs with only a

slightly larger footprint. The biological aerated filter system had a relatively high O&M cost as a

result of the additional equipment required to run the system.

The same evaluation criteria and weightings were used as in Section 7.1. This results in the

following scores in Table 7.6 for each treatment technology:

Table 7.6 – Complete Systems Evaluation by Secondary Treatment Option

The highest ranked technology is the sequence batch reactor followed by extended aeration.

Although the sequence batch reactor scored the lowest for footprint it was the least expensive in

terms of both capital and O&M costs.

Technology

Criteria Criteria WeightExtended Aeration

Sequence Batch Reactor

(ISAM™)

Membrane Bioreactor(Z-MOD™)

Moving Bed Bioreactor(Meteor®)

Biological Aerated Filter(BIOFOR®-N)

Process Complexity 25 25.0 20.0 10.0 25.0 15.0Footprint 25 18.8 13.0 21.9 18.9 25.0Total Capital Cost 25 19.6 25.0 22.7 19.9 21.5Present Value 20 Year O&M 25 15.4 25.0 18.2 14.8 15.0Total Score 100 78.8 83.0 72.8 78.6 76.5Rank 2 1 5 3 4



8.0 SUMMARY AND CONCLUSIONS

A long list of secondary and tertiary treatment technologies was prepared in order to provide the

required effluent quality for the Millbrook WWTP. This list was evaluated on a pass-fail basis to

produce a short list of options to be investigated in more detail.

The evaluation for tertiary treatment indicated that continuous backwash filters technology

scored significantly higher than all other tertiary treatment technologies investigated.

Based on the results of the conceptual level design evaluations, the sequence batch reactor and

extended aeration systems were the top ranked. Both of these systems will provide the

required plant effluent quality. Each system has its own advantages and disadvantages. The

sequence batch reactor has the lowest capital and O&M costs and a low process complexity.

This system, however, requires the largest tankage of all the options resulting in a considerable

footprint requirement, but is still within the footprint available for the treatment plant. The

extended aeration system requires a slightly smaller area but has significantly higher capital and

O&M costs associated with it. The extended aeration system benefits from the fact that it is the

system currently being employed by the Millbrook WWTP.

It is recommended that these two options be carefully considered by the Township to determine

which factors are the most important. Following the treatment technology selection it is

recommended that a formal pre-selection be conducted for secondary and tertiary treatment to

allow for the most cost effective system to be implemented.

Township of Cavan Monaghan

Millbrook WWTP – Wastewater Treatment Capacity Class EA – Technology Evaluation RVA # 122670 February 2013

Appendix A

MOE Memorandum

Dated February 1, 2013

Ministry of the Environment Ministère de l'Environnement P.O. Box 22032 C.P. 22032 Kingston, Ontario Kingston (Ontario) K7M 8S5 K7M 8S5 613/549-4000 or 1-800/267-0974 613/549-4000 ou 1-800/267-0974 Fax: 613/548-6908 Fax: 613/548-6908 M E M O R A N D U M February 1, 2013

TO: Keith Jamieson Senior Environmental Officer Peterborough District Office Eastern Region FROM: Victor Castro Surface Water Scientist Technical Support Section Eastern Region RE: Township of Cavan Monaghan Millbrook Water Pollution Control Plant Baxter Creek Assimilative Capacity Study I have reviewed the report titled “Baxter Creek Assimilative Capacity Study Final Draft Report” dated December 19, 2012 prepared by Greenland International Consulting Ltd. and offer the following comments for your consideration. The Millbrook WPCP is located at 25 Centennial Lane, in the Village of Millbrook, Township of Cavan Monaghan. The WPCP operates under Certificate of Approval No. 1685-5VSLQ7issued February 18, 2004. It consists of an extended aeration activated sludge sewage treatment plant with a design rated capacity of 1,326 m3/day, including phosphorus removal and ultraviolet disinfection, discharging to Baxter Creek. The plant is operated by the Ontario Clean Water Agency (OCWA) on behalf of the municipality. Growth pressures and the age of the existing plant have warranted that the Township look at upgrading and increasing the WPCP’s design rated capacity. The Township is proceeding under the Municipal Class Environmental Assessment process, and has commissioned the preparation of an assimilative capacity study to support possible alternatives that involve the continued discharge of treated effluent to Baxter Creek. Baxter Creek is a cold water system that supports salmonid species such as brook trout and brown trout. The creek originates in the Oak Ridges Moraine and drains a relatively small watershed area (92 km2). The Village of Millbrook is located adjacent to Baxter Creek, approximately 10 kilometres upstream of its confluence with the Otonabee River.

- 2 - Analysis of Baxter Creek Water Quality Historic data from the Provincial Water Quality Monitoring Network (PWQMN) was used to define ambient water quality conditions for Baxter Creek for the purposes of characterizing the receiving stream as a Policy 1 or Policy 2 system. In addition, grab samples were taken from Baxter Creek in September 2012 during low to medium flow conditions. The purpose of the water quality sampling was to collect recent data for comparison against historic results. The analysis focused on the conventional pollutants associated with municipal sewage treatment discharges (i.e. total phosphorus, ammonia-N, CBOD5, total suspended solids, and E. coli), as well as some other relevant parameters such as pH and nitrates. The Provincial Water Quality Objective (PWQO) for TP in streams and rivers is 30 ug/L. Tables5.1 and 5.2 in the report summarize the historic water quality for Baxter Creek at Zion Road (Station A) and Hutchinson Drive (Station B). The reported TP concentrations show that both mean and median levels exceed the PWQO for the period of record (i.e. Policy 2). On the other hand, the consultants indicate that the median concentration of TP at Station A for the period of record 2004 to 2008 was 0.02 mg/L (i.e. Policy 1). I agree that when the purpose of the analysis is to assess water quality that is representative of current watershed conditions, it is appropriate to truncate long-term data to reflect more recent observations. However, my preference would have been that a record longer than 5 years be used (e.g. 2000 to 2010). Ultimately, it does not make a significant difference in this case, since the consultants have proposed a very low effluent TP design objective (0.1 mg/L) that is consistent with what the Region would request for Policy 2 receivers. With respect to the other pollutants of concern (i.e. ammonia-N, dissolved oxygen, BOD, and fecal coliforms) the consultants conclude, using the PWQMN summary data, that Baxter Creek is Policy 1 with respect to these parameters. I agree with this finding, with the exception of fecal coliforms. The historic data for Baxter Creek taken from Hutchinson Drive (Station B) shows that fecal coliforms are significantly higher downstream of Millbrook compared to the upstream station at Zion Road (Station A). The annual performance assessment reports produced by OCWA show that E. coli concentrations from the Millbrook WPCP consistently meets the effluent limit of 200 counts/100 ml. This suggests that there are other diffuse sources of bacteria entering Baxter Creek, such as storm water runoff and agricultural inputs. Assimilative Capacity Analysis of Baxter Creek To determine the assimilative capacity of Baxter Creek, the consultants calculated a 7Q5 flow from available data sources, and estimated 7Q20 flows using two statistical approaches. A value of 343 L/s was selected for use in dispersion modeling and to

- 3 - predict theoretical maximum effluent concentrations that would not exceed the PWQO downstream of the WPCP. In regard to the theoretical maximum effluent concentrations, these do not represent recommended discharge concentrations, but are simple mass balance calculations to show that under complete instantaneous mixing of the effluent, the PWQO’s would be met downstream of the discharge. Effluent dispersion modeling using Cormix was used to assess the size of the mixing zone for an un-ionized ammonia discharge of 0.2 mg/L under 7Q20 flow conditions. The results showed that PWQO concentrations will be achieved at approximately 285 m downstream of the outfall. The assumptions used in the modeling scenario are quite conservative given that the proposed ammonia-N design objectives of 1 mg/L (summer) and 2 mg/L (winter) will produce un-ionized ammonia levels well below the 0.2 mg/L threshold used in the model. I agree with the consultants that the proposed ammonia-N objectives should not pose a risk of acute toxicity within the mixing zone. The following effluent limits have been proposed for the expansion of the Millbrook WPCP: Expansion of Millbrook WPCP to 2,521 m3/day Parameter Effluent Limit (mg/L) Loading (kg/d) Effluent Objective (mg/L) CBOD5 7 17.7 5 TSS 6 15.1 5 TP 0.15 0.38 0.10 TAN

‐ May-Oct 2 5 1 ‐ Nov-Apr 3 7.6 2

E. coli (org/100ml) 100 n/a 100 pH 6 to 9.5 n/a n/a The proposed effluent criteria should be based on a monthly average, with the exception of E. coli which should be based on a monthly geometric mean. The pH limit should be based on a never to exceed for all measured values. To confirm that the final effluent is non-acutely lethal, toxicity testing should be undertaken on a quarterly basis to be reduced to annual following 24 months of consistent passes. The testing should be performed on Daphnia Magna and rainbow trout in accordance with the most current procedures published by Environment

- 4 - Canada. In the event of a toxicity failure on any test, the owner would be required to investigate the possible causes of the toxicity based on sampling data and monitoring, and upon determination of the cause or source of lethality determine appropriate control measures. It is my understanding through discussions with the consultants that effluent disinfection will be undertaken through a new ultraviolet system. In summary, I am satisfied with the proposed effluent limits and objectives for the expansion of the Millbrook WPCP. If you have any questions regarding these comments please contact me at (613) 540-6862. Victor Castro B.Sc. M.Pl. VC/gl c: File SW PB CM 03 07 (Millbrook WPCP) ec: G. Dagg-Foster

V. Mitchell



Appendix B

Budgetary Quotations from Manufacturers



ISAM™ Sequence Batch Reactor

Fluidyne Corporation

FLUIDYNE CORPORATION 5436 Nordic Drive, Suite D Cedar Falls, IA 50613 Ph.: 319-266-9967 Fax: 319-277-6034 TO: R.V. Anderson Associates, LTD From: Erick Mandt ATTN: Valera Saknenko, Ph.D, PE, PMP Date: January 14, 2013 RE: Millbrook, Ontario – 2520 m3/day Fluidyne ISAM™ system Dr. Saknenko: We have reviewed the design information for the above project. We have designed a Fluidyne ISAM™ System based on the following data: MONTHLY AVERAGE INFLUENT DESIGN EFFLUENT Desing Flow: 2,520 m3/day Peak Hour Flow: 8,242 m3/day Design BOD5: 190 mg/l < 10 mg/l Design TSS: 210 mg/l < 10 mg/l Design TKN: 25 mg/l < 1 mg/l NH3 Design P: 5 mg/l < 0.10 mg/l with chem

Precipitation and filtration We have assumed the wastewater is non toxic and readily biodegradable and the pH is close to 7 and sufficient alkalinity in the waste stream. Please see the attached process design calculations showing tank and equipment sizing and power requirements based on the above data. OPTION #1: Brand New Facility Internal Tank Dimensions are as follows: Two (2) ISAM tank each 8.00m long X 14.00m w X 5.50m TWL X 6.00m wall height (tank to be covered and vented with bottom of tank cover starting at 6m) Two (2) SAM tank each 6.50m long X 14.00m w X 5.50m TWL X 6.00m wall height Two (2) SBR tanks each 13.00m long X 14.00m w X 5.50m TWL X 6.00m wall height

Alternate tank geometries to optimize tank layout and construction costs could be utilized. Please see the drawings of the proposed equipment and layout. The system will be divided into three compartments. The first compartment is the ISAM™ tank. This tank is used to remove solids and to store waste sludge from the aerobic process. The next tank is the SAM™ tank. This tank is used for flow equalization as well as anoxic mixing prior to the SBR. With the SAM™ tank an integral part of the process; we can operate in a true batch mode without affecting the process or the clarification stage. Each SBR is equipped with an overflow weir. The overflow weir returns mixed liquor back to the SAM™ tank. This allows nitrate return for effective and rapid denitrification. The overflow weir also returns any scum that may be in the SBR back to the SAM™ tank. Therefore, before decanting, no scum or floatable solids are present in the SBR tank. With the sludge reduction features of the ISAM™, our process calculations indicate that our design has approximately 180 days of sludge storage in the process. We anticipate the sludge in the anaerobic tank to be in the 3 to 5% solids concentration. We are proposing the Fluidyne jet aeration/mixing headers to provide oxygen to the system. Jets are highly efficient in dirty water applications with a designed alpha value of 0.9. Our decanter is a fixed style mounted to the wall with no submerged or moving parts. An air lock prevents solids from entering the decant during fill or react. Fluidyne proposes the following: ISAM™ Two (2) ISAM™ Influent Diffusers Four (4) ISAM™ Overflow Assembly Two (2) 3 HP Sludge Haul-Out Pumps and accessories SAM™ Four (4) SAM™ Tank Influent Diffusers Two (2) Sets of Level Sensors Two (2) Fluidyne model# FAS-10 SAM tank mixer/aspirators. Four (4) 12 HP Submersible SBR Feed Pump/Jet Motive Pumps with discharge elbow, guide rail brackets, power cord and lifting. Four (4) Waste Sludge Control Valves in weatherproof valve box

SBR Four (4) Fluidyne model # DM2JA7 Jet Aeration Headers including all in-basin air and liquid piping, stainless steel supports and pneumatic backflush. Three (3) 30 HP Positive Displacement Blower Packages (one blower to be an in-line spare. Two (2) Fluidyne model # FOW-14 SBR Overflow weir/anoxic mix assembly Two (2) Fluidyne model # DSED-14 Solids Excluding Decanters including vent valve, siphon break and discharge control valve Two (2) Sets of Level Sensors Two (2) Dissolved Oxygen Sensors Two (2) TSS Sensors One (1) Multi-Channel analyzer for DO and TSS monitoring. CONTROLS One (1) ISAM Control Panel with PLC, operator interface, switches, indicating lights and relays to automatically control the ISAM functions The budgeted price for the above equipment is $495,000 CDN FOB-factory with freight allowed to the jobsite. Pricing is based on exchange rate as of January 14, 2013. Our proposal does not included is any tanks or tank covers, electrical or mechanical installation, out of basin or interconnecting piping, valving or supports, motor starters, remote panels, pre-treatment equipment, sludge handling equipment, guide rails, interconnecting piping between blowers and in-basin equipment, blower sound enclosures, disinfection equipment; sludge wasting discharge piping, chemical feed equipment or chemicals, filtration equipment, disinfection equipment, tank spool pieces, interconnecting hardware or gaskets, anchor bolts, taxes duty or anything not specifically mentioned above. OPTION #1: Utilization of existing facility: Fluidyne has reviewed the existing tankage at the Millbrook facility. We have the following option: The existing sludge storage tank is nominally 20.1m long X 13.6m wide X 4.2m water depth. We believe this tank can be converted into the ISAM portion of our process. It has very similar storage volume as the new ISAM tanks detailed in option #1 above. Ideally this existing tank would be divided into two separate tanks for flexibility in operation. Our layout drawing shows this tank divided into two separate structural tanks. The existing aeration tank is nominally 80’ long X 28’ wide X 14.5’ water depth. We believe this tank can be converted into the SAM portion of our process. It

has very similar storage volume as the new SAM tanks detailed in the option #1 above. Ideally this existing tank would be divided into two separate tanks for flexibility in operation. Our layout drawing shows this tank divided into two separate structural tanks. We would recommend building two (2) new SBR basins on the East side of the SAM tanks. These two SBR tanks would have the same nominal geometry of the SBR tanks in option # 1 above. To provide a square footprint for the SBRs, we have sized each at 13.50m long X 13.50m w X 5.50m TWL X 6.00m wall height. Alternate tank geometry could be used. We believe the existing clarifier can be converted into an effluent equalization tank to take the decanted batch from the SBR and allow pumping to the filtration/UV system. This tank is nominally 61’ X 19’ X 10’ water depth. This tank stores a minimum of one batch volume based on these dimensions. Alternately to provide additional flow equalization, this tank could be cross connected with the SAM tanks to provide additional flow equalization. This tank also could be converted to a sludge storage tank. The above changes would result in some additional equipment, piping and engineering to accommodate the use of the existing tanks. We would budget this option for $30,000 more than the brand new facility. We estimate a delivery time of 12 to 16 weeks after release to production. The Fluidyne proposal offers numerous advantages including:

1. Control strategies based on varying aeration/mixing requirements depending on the strength of the incoming wastewater. This design minimizes operating costs and controls over/under aeration.

2. No need for automated influent control valves.

3. Built in scum skimming mechanism removes all scum from SBR prior to

decanting.

4. Energy efficient jet aeration equipment with high alpha values and oxygen transfer. Test data demonstrates alpha values of 0.9.

5. Jet aeration equipment will last 3 to 4 times as long as course or fine

bubble diffusers. This results in less maintenance and operation costs.

6. Jets have large solids handling capability with minimum 1 1/2” solids handling. A built in backflush allows cleaning of the jet header without entering or draining the tank. Therefore plugging is not a concern compared to fine or coarse bubble diffusers.

7. The decanter has no moving parts in the basin that can freeze or

malfunction.

8. Submerged aeration/mixing header provides multipoint mixing locations for energy efficient off-bottom solids suspension. The jet manifold provides anoxic mixing by not running the blower. This minimizes in-basin equipment, as a separate mixer is not required.

Please let me know if you have any questions or need additional information. Best regards,

Erick Mandt CC: Albert Wakim – H2Flow Equipment

FLUIDYNE SEQUENCING BATCH REACTOR CALCULATIONSPROJECT: Millbrook, ONTENGINEER: egmPROJECT #: 2520m3/day 2400 m3/dayDATE & TIME: Two Train Two Train1/14/2013 14:54 Design Design

INFLUENT CONDITIONS Flow (mgd) 0.6658 2520 m3/dayFlow(gpm) 462 29 lpsBOD5 (mg/l) 190 (lb/d) 1055 478 kg/dayTSS (mg/l) 210 (lb/d) 1166 529 kg/dayTKN (mg/l) 25 (lb/d) 139 63 kg/dayP (mg/l) 5 (lb/d) 30 13.6 kg/day

EFFLUENT REQUIREMENTS (Monthly Average) Design ObjectiveBOD5 (mg/l) 10TSS (mg/l) 10NH3-N (mg/l) Winter 1NH3-N (mg/l) Summer 2P (mg/l) 0.10* Chemical addition and filtration required by others as back-up to biological P removal

OXYGEN REQUIREMENTSPounds TKN required for synthesis 52.75Pounds of NO3-N produced 86Pounds O2 recovered/pound NO3-N reduced 2.6Pound of Oxygen/ pound of BOD 1.4Pound of Oxygen/pound of TKN 4.6Actual Oxygen Demand (lb 02/d) Total 2116 959 kg/dayAlpha 0.85Beta 0.95Theta 1.024Operating Dissolved oxygen (mg/l) 2Clean Water oxygen sat. at op. temp (mg/l) 9.09Clean Water oxygen sat. at std. temp (mg/l) 9.09Clean water 02 sat, std temp,mid depth(mg/l) 11.50Std. condition ambiant pressure (psia) 14.7Oper. condition ambiant pressure (psia) 14.2Wastewater temperature (c) 20SOR/AOR ratio 1.58Standard Oxygen Demand (lb 02/d) total 3347 1518 kg/dayStandard Oxygen Demand (lb 02/hr) 279 126 kg/hrStandard Oxygen Demand (lb O2/hr/SBR tank) 139 63 kg/hr/tankSpecific oxygenation rate (mg/l-hr) 42Pounds of oxygen/pound of air 0.23Clean water efficency (%) 24Pounds of air/cubic foot of air 0.075Aeration hours per day 12.00Air flow rate (scfm/tank) 561NITRIFICATION/DENITRIFICATIONRequired alkalinity for nitrification (mg/l) 111Alkalinity recovered, denitrification (mg/l) 47Net alkalinity required (mg/l) 64Mixed liquor temperature, C 20ML dissolved oxygen (mg/l) 1Max. nitrifier growth rate, day-1 0.334Minimum SRT required for nitrification, days 3.00Actual or design SRT, days 19.15

Page 2PROJECT: Millbrook, ONTKn, half velocity constant (mg/l) 0.73Design growth rate for heterotrophs/nitrifiers 0.0522Projected effluent soluable NH3-N, mg/l 0.14Specific utilization rate, lbs BOD5/lb mlvss 0.19lbs. mlvss required for BOD & NH3 removal 5676mlvss (mg/l) 1500Tank volume req. for BOD & NH3 removal (MG) 0.454Denitrification rate (g/g/day) 0.066lbs mlvss required for denitrification 1304Tank volume required for NO3 removal (MG) 0.104Total tank volume required (MG) 0.5580SBR TANK CONFIGURATIONNo. of tanks 2Overall length (ft) 90.2 27.50 mLength SAM + SBR (ft) 64.0 19.50 mLength ISAM (ft) 26.2 8.00 mLength SAM tank (ft) 21.3 6.50 mLength SBR tank (ft) 42.7 13.00 mWidth (ft) 45.9 14.00 mBottom water level (ft) 13.0 3.96 mTop water level (ft) 18 5.49 mTop of Wall (ft) 20 6.10 mNo. Decanters/tank 1Total SAM™+SBR Volume @ TWL(MG) 0.7913 2995 m3Total Tankage Volume @ TWL(MG) 1.1159 4224 m3SAM™+SBR HRT (hrs) 28.52Total HRT with I-Tank 40.23CYCLE TIMES/CAPACITY CALCULATIONSTotal decant volume (cubic feet) 19,590Total decant volume (gallons) 146,532 555 m3Decant volume per tank (gallons) 73,266 277 m3Number of cycles per day/tank 4.54Total time per cycle (minutes) 317 Fill rate (gpm) 2794 176 lps Fill time (minutes) 26 Interact period (min) 213 Settle period (minutes) 45Average decant rate (gpm/ft decanter) 80Decanter length (feet) 28 Decanting time (minutes) 33Decanting rate (gpm) 2240Peak decanting rate (gpm at start of decant) 2464Maximum aeration period available (hours/day) 18.12

EQUIPMENT SELECTIONAir flow per nozzle (scfm) 45Number of nozzles required (per tank) 12.47Number of nozzles provided (per tank) 14Actual airflow per nozzle required (scfm) 40.10SCFM per tank 561

Page 3 PROJECT: Millbrook, ONTPOWER CONSUMPTION CALCULATIONSPump efficiency 0.76Pump horsepower, BHP/tank 21Mixing BHP/MG 54Blower horsepower, BHP/tank 25Total horsepower, BHP/tank 46Aeration BHP/MG 117Total design equivalent horsepower, BHP 46SLUDGE PRODUCTIONSludge Yield Factor 0.7Net Sludge Yield (lbs/d) 739Sludge Concentration (%) 0.700Sludge Wasting Rate (gpd) 12650Waste Sludge /cycle (gal) 1392WAS Pumping Rate (gpm) 50Waste Sludge Cycle Time (min) 27.8Thickened Sludge Concentration (%) 3.5Thickened Sludge (gpd) 2530

MLSS (mg/l) @ TWL 2143MLSS (mg/l) @ BWL 2967Sludge inventory (lbs) 14141SRT ( 1/days ) 19.15F/M 0.07SVI (ml/g) 150Sludge blanket level (ft) 5.79Organic loading (lbs BOD/1000 ft3) 7.07

ISAMSurface Area Required 1332Number of tanks 2Length required (ft) total 28.99 8.84 mLength (ft) provided each tank 26.25 8.00 mWidth (ft) 45.93 14.00 mTWL (ft) 18 5.49 mTotal volume (gal) available 324,625 1,229 m3Days sludge storage available undigested 128.31Total sludge age including SBR (days) 147.46Pounds sludge destroyed 522% sludge reduction 71Thickened, digested sludge (gpd) 743Inerts accumulation (gal/d) 399Days sludge storage available after digestion 180



Z-MOD™ Membrane Bioreactor

GE Water & Process Technologies


Budget Proposal for

Millbrook WWTP Expansion – MBR Option Z-MODTM-L MBR System Submitted to:

R.V. Anderson 2001 Sheppard Avenue East Suite 400 Toronto ON M2J 4Z8 Attention: Valera Saknenko, Ph.D., P.Eng., PMP Senior Associate

January 14th, 2013 Proposal Number : 759344

GE Water & Process Technologies Geoff Totten, Regional Sales Manager Tel: (905) 465-3030 Email: [email protected] Local Representation By:

Pro Aqua Inc. Scott Lenhardt, P.Eng. 416-861-0237 x 228 905-330-9244 Cell Email: [email protected]


GE Water & Process Technologies Confidential and Proprietary Information

GE Water and Process Technologies (“Seller”) submits the information contained in this document for evaluation by R.V. Anderson (“Buyer”) only. Buyer agrees not to reveal its contents except to those in Buyer’s organization necessary for evaluation. Copies of this document may not be made without the prior written consent of Seller’s Management. If the preceding is not acceptable to Buyer, this document shall be returned to Seller. This proposal is for budgetary purposes only and does not constitute an offer of sale.


GE Confidential and Proprietary Information Page 3

Table of Contents

1 ZMOD Introduction ................................................................................................... 4

2 ZMOD - Low LifeCycle Cost MBR ............................................................................ 5

2.1 LEAPmbr…Simple, Reliable, Efficient ................................................................................ 5

2.2 Membrane life, cleanability & replacement ................................................................. 5

3 ZMOD - Simple MBR Operations ............................................................................. 6

3.1 Membrane Aeration System Design ................................................................................ 6

3.2 Membrane Cleaning Systems ............................................................................................. 6

4 ZMOD - Robust Design Basis .................................................................................. 7

4.1 Positive Displacement Permeate Pumps ....................................................................... 7

4.2 Permeate for Cleaning Solution ......................................................................................... 7

4.3 Mixed Liquor Operating Range .......................................................................................... 7

4.4 Electrical Design ....................................................................................................................... 7

5 Basis of Design .......................................................................................................... 8

5.1 Influent Flow Data .................................................................................................................... 8

5.2 Influent Quality .......................................................................................................................... 9

5.3 Effluent Quality .......................................................................................................................... 9

5.4 Influent Variability & Equalization ..................................................................................... 9

5.5 Biological System Design ................................................................................................... 10

5.6 Ultrafiltration System Design ........................................................................................... 10

5.7 Z-MOD™-L Equipment Description ............................................................................... 10

5.8 Scope of Supply by GE ........................................................................................................ 13

6 Buyer Scope of Supply ............................................................................................ 15

7 Commercial .............................................................................................................. 17

7.1 Pricing Table ............................................................................................................................ 17

7.2 Power & Chemical Consumption Estimates .............................................................. 17

7.3 Freight ........................................................................................................................................ 18

7.4 Bonds .......................................................................................................................................... 18

7.5 Equipment Shipment and Delivery ................................................................................ 18

7.6 Pricing Notes ........................................................................................................................... 18

7.7 Conditional Offering ............................................................................................................. 19



1 ZMOD Introduction

Z-MOD™ MBR Systems are GE Water’s pre-engineered, modular MBR systems that bring proven ZeeWeed® membrane bioreactor (MBR) technology to municipal, industrial, or land development applications.

Engineered to enable a high level of flexibility with a multitude of design options, features and benefits to enable engineers, clients and operators to design and configure the MBR system that best fits each individual application.

The ZMOD range of systems is designed with 3 key attributes in mind:

� Lowest Lifecycle Cost MBR – lowest cost of ownership for the Owner

� Simple Operations – simple & automated operations coupled with GE Water support for the operating team

� Robust Design – prove design parameters with scope and configuration flexibility and options for a wide variety of conditions

ZMOD™ Systems are focused on the Ultrafiltration system as the heart of the MBR process, with the ability to add biological or other additional components into the system as required.



2 ZMOD - Low LifeCycle Cost MBR

At the heart of ZMOD are the two most important parameters in a Low Lifecycle Cost MBR which are efficiency in MBR design & operation and the best chance of long membrane life in operation.

2.1 LEAPmbr…Simple, Reliable, Efficient ZMOD is designed to incorporate the latest innovations of LEAPmbr technology making ZMOD the most energy efficient and productive MBR that GE Water is able to provide to owners.

LEAPmbr’s combined initiatives will directly impact your plant design by:

� Improving your Productivity by 15%,

� Decreasing your membrane system footprint by 20%,

� Removing equipment needed to provide aeration to your membranes by 50%,

� Saving you over 30% in MBR power costs

2.2 Membrane life, cleanability & replacement ZMOD incorporates GE Water’s ZW500 membrane technology with the following key benefits to ensure an owner’s peace of mind for the life of their MBR facility:

� ZeeWeed MBR membrane with a proven membrane life and high resistance to upset conditions

� System designed with multiple cleaning options to ensure the highest chance of achieving maximum membrane life

� GE Water as a single point of responsibility provides an integrated supply chain between the system & membrane warranty provider and the membrane manufacturer

� A straight forward membrane warranty with clear performance triggers



3 ZMOD - Simple MBR Operations

ZMOD is designed to ensure the MBR system is simple to operate without compromising any operational robustness.

The operators have a range of flexible options to ensure the MBR system is able to meet varying operating conditions should they arise.

3.1 Membrane Aeration System Design Aeration is one of the most important operations for successful long term MBR operation and is a significant proponent of operating cost.

ZMOD utilizes a very simple aeration strategy which minimizes the amount of instrumentation and controls required to achieve a energy efficient method for membrane aeration.

No complex control loops or complicated airflow measurement devices are required for LEAP MBR Aeration Technology to achieve energy efficiency.

3.2 Membrane Cleaning Systems GE has developed MBR design principles based on best engineering practices that ensure the permeability of the membrane is maintained over the life of the membranes.

A fully automated suite of membrane maintenance procedures will ensure long-term, successful operation, including:

� In situ chemical membrane cleaning performed directly in the membrane process tanks so your operators don’t waste time moving cassettes,

� The ability to increase or decrease the frequency of maintenance cleans to fit the operating conditions.

� The ability to backpulse when needed to greatly improve your operator’s ability to recover from non-design conditions.

The above cleaning systems are automated resulting in operators having available a full suite of comprehensive cleaning systems which are simple to use and initiate.



4 ZMOD - Robust Design Basis

ZMOD systems are designed to ensure operators have a system with sufficient design robustness to accommodate a wide range of potential conditions.

4.1 Positive Displacement Permeate Pumps ZMOD uses positive displacement permeate pumps to draw effluent through the membranes.

� The positive displacement design of these pumps allows for variations within the hydraulic profile that will not adversely affect the pump performance.

� The pumps come complete with an ability to backpulse the membranes should sludge conditions deteriorate

� A wide range of pump turndown provides the operator to wide window of flow adjustment for a variety of situations.

This pump selection provides a high level of security and flexibility for engineers and operators.

4.2 Permeate for Cleaning Solution ZMOD systems ensure a volume of clean permeate is always stored ready for use for cleaning solutions.

� ZMOD takes permeate from its production cycle and stores this treated water in the backpulse tank ready for use. This ensures no reliance or costs from a potable water system to supply cleaning solution to the site for the membrane cleaning process.

� ZMOD systems include a backpulse tank which provides the operations staff with a readily available source of water for cleaning whenever it is required.

This allows cleaning processes to occur automatically while allowing the operator flexibility to select different cleaning methods

4.3 Mixed Liquor Operating Range GE Water MBR systems rely solely on the pore size of the membrane to effect filtration of the mixed liquor. This allows the MBR at a wide range of mixed liquor concentrations.

This reduces the need for mixed liquor concentrations to be within the intended operating range during start-up processes or low flow scenarios.

4.4 Electrical Design ZMOD systems are designed based on the following electrical architecture:

� Central PLC and common equipment I/O panel

� Remote I/O panel, VFD and Disconnect mounted on the permeate pump skid

This design basis allows the system to readily accommodate additional trains and allows operators to isolate or troubleshoot individual trains without the loss of the central PLC.



5 Basis of Design

This proposal is offered based on GE supplying a Z-MOD™-L Membrane Bioreactor System (MBR), for the Millbrook WWTP Expansion project, designed to treat an average daily flow (ADF) of 2,520 m3/day.

For this site, a Peak Hourly Flow (PHF) of 8,242 m3/day was provided for an assumed duration of 6 hours. It is understood that a portion of the existing tankage will be used for sludge stabilization and storage once the expansion is complete. However, based on MBR sludge volumes being less than conventional, it is assumed that a portion of existing tankage will be available to provide some flow equalization during peak flows. Therefore, to minimize the size/capacity of the membrane system, the membranes are sized to treat a peak hour flow (PHF) of 5,800 MGD for 6 hours, which requires an equalization volume of 611 m3. Please refer to Table 5.5 below for average sludge production from this MBR system.

In addition, the system can support the average daily flow with one ZeeWeed membrane train offline for cleaning and maintenance purposes for periods up to 24 continuous hours.

The following tables summarize the main design parameters on which the Z-MOD™-L MBR system has been designed.

5.1 Influent Flow Data

The influent design flows are summarized in the table below.

Average Day Flow 2,520 m3/day

Maximum Month Flow 1 3,150 m3/day

Maximum Day Flow 1 3,780 m3/day

Peak Hour Flow 2 5,800 m3/day

Maximum Flow with one train offline for maintenance or cleaning (less than 24 hrs)

2,520 m3/day

Note 1: Parameter value assumed

Note 2: As described in the above paragraphs, this value assumes that a portion of existing tankage will be available to provide some flow equalization during peak flows. Although this site has an estimated Peak Hourly Flow (PHF) of 8,242 m3/day for an assumed duration of 6 hours, the membranes are sized to treat a peak hour flow (PHF) of 5,800 MGD for 6 hours, which requires an equalization volume of 611 m3.

• Average Day Flow (ADF) – The average flow rate occurring over a 24-hour period based on annual flow rate data.

• Maximum Month Flow (MMF) – The average flow rate occurring over a 24-hour period during the 30-day period with the highest flow based on annual flow rate data.

• Maximum Day Flow (MDF) – The maximum flow rate averaged over a 24-hour period occurring within annual flow rate data.

• Peak Hour Flow (PHF) – The maximum flow rate sustained over a 1-hour period based on annual flow rate data.



5.2 Influent Quality

The design solution proposed is based on the wastewater characteristics detailed below.

Minimum Influent Temperature 8 ºC

BOD5 190 mg/L

TSS 210 mg/L

TKN 25 mg/L

NH3-N 1 18 mg/L

TP 5 mg/L

Alkalinity 2 n/a -

Note 1: Parameter value assumed

Note 2: GE is assuming that sufficient influent alkalinity is available to ensure proper performance of the biological system. GE has included a NaOH dosing system for pH control in its scope of supply; however this will not be adequate in the case of severe long term deficiency in influent alkalinity.

5.3 Effluent Quality

The following performance parameters are expected upon equipment startup and once the biological system has stabilized based on the data listed in sections 5.1 and 5.2.

BOD5 <5 mg/L

TSS <5 mg/L

NH3-N <1 mg/L

Unionized Ammonia <0.2 mg/L

TP 2 <0.1 mg/L

Turbidity < 1 NTU

Note 1: TN less than 10mg/L corresponds to minimum design temperatures of 10ºC and <1.5 mg/L recalcitrant dissolved organic nitrogen in the influent

Note 2: With coagulant addition

5.4 Influent Variability & Equalization

The system may be optimized by incorporating equalization into the design. The potential for equalization should be reviewed to optimize membrane surface area and to reduce capital costs associated with equipment sizing and membrane tank volume.

Flows or loads in excess of the design criteria defined above must be equalized prior to the MBR system. In the event that the influent exceeds the specifications used in engineering this proposal, or the source of influent changes, the ability of the treatment system to produce the designed treated water quality and/or quantity may be impaired. Buyer may continue to operate the system, but assumes the risk of damage to the system and/or additional costs due to increased membrane cleanings, potential for biological upset and/or increased consumable usage.

The process may be easily enhanced for significant phosphorus reduction by adding a metal salt, such as ferric chloride or alum. As the Z-MOD™ MBR process does not rely on settling for solids-liquid separation, a minimal volume of metal salts is needed to create “pin-flocs”. The



membrane then effectively blocks the microscopic floc from entering the effluent stream resulting in effluent phosphorus levels down to below 1 mg/L.

5.5 Biological System Design

The biological system for this project consists of aerobic zones, but anoxic volume can easily be added in the future for denitrification and alkalinity recovery. The corresponding volumes for each zone are listed in the table below.

Flow Basis of Biological Design 2,520 m3/day

Temperature Range 8 to 25 ºC

Total Aerobic Volume (excluding membranes) 869 m3

Membrane Tank Volume 97 m3

Design HRT 9.2 hours

Design SRT 20.8 days

Average Sludge Production 40 m3/day

Bioreactor MLSS 8,000 – 10,000 mg/L

Minimum water depth 5.5 m

Note 1: Tank sizes are preliminary only and may change once final detail design commences.

Note 2: The biological system is designed for installation within concrete tanks supplied by Buyer

5.6 Ultrafiltration System Design

The ultrafiltration design of this system is described in the table below where membrane modules are assembled into cassettes and cassettes are installed in concrete tanks supplied by Buyer.

Type of Membrane ZeeWeed® 500d

Number of Trains 2

Number of ZMOD L Permeate Pump Skids 2

Type of Cassette (16 or 48Module) 48

Number of Cassettes Installed per Train 3

Number of Modules Installed per Train 124

Total Number of Cassettes 6

Total Number of Modules 248

5.7 Z-MOD™-L Equipment Description The following is a description of the equipment included in GE’s Scope of Supply. Pre-assembled components include the permeate pump skids, membrane cassette assemblies, and chemical addition system skids. Critical items that will be shipped loose for installation by Buyer include the master control panel, motor control center, backpulse tank, blowers, RAS pumps and other equipment. Please refer to section 5.8 below for a complete list of GE supplied equipment.



Master PLC Panel

An Allen-Bradley Compact Logix Programmable Logic Controller (PLC) and Panel View 1250 HMI with a Human Machine Interface (HMI), installed in the main control panel, monitors and manages all critical process operations.

The master PLC panel will also include I/O for common equipment items such as membrane blowers, air compressors, RAS pumps and other items (if included in GE Scope)

Level controls monitor the level of mixed liquor in the process tanks and transmit this information to the Z-MOD™ PLC. The PLC will automatically adjust the flow of the Z-MOD™ trains based on proportional control to the process or membrane tank levels.

Permeate and Backpulse Pump Equipment

One permeate pump per train is employed to draw water through the membranes. The permeate pump, associated valves and piping for the train are mounted on a factory assembled, epoxy-coated carbon steel skid.

Each permeate skid is designed to include a remote I/O panel which distributes control wiring to the pump, skid mounted VFD and instruments located on the permeate pump skid.

Also mounted on the skid are the permeate pump VFD, motor disconnect and instrumentation including pressure transmitter and magnetic flowmeter required to operate the pump system.

Optional turbidity meter is available for inclusion onto the permeate pump skid for turbidity monitoring of each individual membrane train.

Membrane Scour Aeration System

One duty membrane blower per train will be supplied with one common standby blower to be shared by all trains.

Blowers will typically come complete with required isolation valves, check valves, pressure relief valve, pressure indicators and flow indicators.

Sludge Wasting System

Sludge wasting is accomplished by periodically diverting mixed liquor from the recirculation return line, via manual control or by pulling directly from the bioreactor. The frequency of wasting is a function of influent characteristics, reactor design and operator preference. In certain operating circumstances, bioreactors can be designed to accommodate client preferences with regards to wasting frequencies.

Process Aeration System

The process aeration blowers provide air for the biological tank and ensure that sufficient oxygen is available to maintain the biological processes in the tank. The process aeration blowers are shipped loose for installation on site.

Fine Bubble Diffusers

A fine bubble diffused aeration system delivers air from the aeration blowers to the aerobic zone of the process tank.



Mixed Liquor Recirculation Equipment

Recirculation pumps are used to transfer mixed liquor from the bioreactor to the membrane tank at a rate of 5 × ADF. The sludge returns to the bioreactor using gravity at a rate of 4 × ADF.

1 x Recirculation per membrane train will be supplied as well as check valves, isolation valves and pressure indicator.

Sodium Hypochlorite Dosing System

The Sodium Hypochlorite Dosing system is used during membrane cleaning applications to remove organic fouling from the membrane surface.

Citric Acid Dosing System

The Citric Acid Dosing system is used during membrane cleaning applications to remove inorganic scaling from the membrane surface.

pH Adjustment System

The pH Control System doses Sodium Hydroxide into the process tank in order to maintain a desired pH for optimal biological performance. This system is meant for infrequent pH adjustment and is not meant as a substitute for insufficient alkalinity in the plant influent. If alkalinity deficiency has been identified as a potential concern in your application, alkalinity supplementation will also be required.

Coagulant Addition System

The Coagulant Dosing system is used to feed a metal salt to assist in precipitating phosphorus in the mixed liquor. This precipitate is then filtered by the ZeeWeed® 500 ultrafiltration membranes, preventing phosphorus from entering the effluent.

Effluent Flow Measurement

Each train will include a flow meter, however a common effluent flow meter can be included to provide daily discharge flow measurements.

Effluent Turbidity Analyzer

Effluent turbidity analyzers monitor effluent water quality and alert operators if effluent turbidity rises beyond acceptable parameters. Each train has a turbidity meter to be mounted on the permeate pump skid.

Remote Monitoring & Diagnostics

Remote Monitoring & Diagnostics has been supplied with your MBR system for the first year of operation. Long term data monitoring is available for a yearly fee. Remote Monitoring & Diagnostics is a powerful plant process support tool that provides fully automated process data monitoring and trend analysis.

The system stores field-acquired and calculated values in a central database and the Remote Monitoring & Diagnostics service provides your plant with a monthly email summary of key trends with recommendations to improve plant operation and membrane cleaning. Annually, GE Water provides a comprehensive report with analysis of key trends and recommendations. The Remote Monitoring & Diagnostics tool and service support helps plant operators to quickly view trends, improve productivity and optimize processes with full web access to the plant's Remote Monitoring & Diagnostics data.



5.8 Scope of Supply by GE

Quantity Description

The MBR System will consist of one (1) ZMOD-L System including the following equipment:

ZeeWeed® Membranes & Tankage

For 6 cassettes

Membrane tank cassette mounting assemblies

6 ZeeWeed® 500 membrane cassettes

248 Membrane modules

2 sets Permeate collection & air distribution header piping

2 Membrane tank level transmitters, one per train

2 Membrane tank Drain/WAS pumps, valves, instrumentation, loose shipped

Master Control Panel

1 Master Control Panel w/ Allen Bradley Compact Logix PLC and Panelview 1250 HMI and Flexlogic I/O

Permeate Pump Skid

1 Permeate pump equipment skid - epoxy coated carbon steel

1 Positive Displacement, Reversible Lobe Permeate pump

1 Required Pump Isolation Valves and Check Valves

1 Remote I/O Panel - includes Allen Bradley Flex I/O.

1 Motor Disconnect

Lot Pressure transmitter, pressure gauge, flow meter

Lot Chemical Injection Ports and Valves

1 Optional Turbidimeter per train - includes isolation valves, throttle valve and backplate.

Backpulse System

Incl Permeate pumps will also provide backpulse duty

1 Flow Through Backpulse water storage tank, with tank level control and associated valves

Membrane Air Scour Blowers

2 + 1 Membrane air scour blowers – 2 duty + 1 online standby, includes isolation valves, flow switches, pressure gauges

Mixed Liquor Recirculation Equipment

2 Mixed liquor recirculation pumps, used to transfer mixed liquor from the bioreactor to the membrane tanks - includes isolation valves

Biological Equipment (for two biological trains)

2 Fine bubble diffuser system for process aeration -loose shipped (without tank downcomer piping)

1 + 1 Process blowers – 1 duty + 1 online standby, includes flow switches, isolation valves

2 Aerobic dissolved oxygen sensor

Chemical Dosing Systems




1 Coagulant dosing system - includes dosing pump, and associated valving.

1 pH adjustment system – includes dosing pump and integrated pH sensor

Membrane Cleaning Systems

1 Sodium hypochlorite chemical feed system - includes dosing pump and associated valving.

1 Citric acid chemical feed system - includes dosing pump and associated valving

Miscellaneous

2 Air compressors for pneumatic valve operation and refrigerated air drier

1 VFDs for Permeate Pumps and Motor Starters for Membrane Blowers, Biological Blowers, Subersible RAS Pumps, and Membrane Tank Drain/WAS pumps

1 Autodialer - auto dialing remote monitor system

General

Included P&IDs and Equipment general arrangement and layout drawings

Included Operating training

Included Operating & maintenance manuals

Included Field service and start-up assistance * - 35 days support over 3 site visits from GE Water field-service personnel for commissioning, plant start-up and operator training

Included Remote Monitoring & Diagnostics process monitoring service – 1 year

Included 24/7 emergency phone support – 1 year

Included Equipment mechanical warranty - 1 year or 18 months from shipment

Included Membrane warranty– 8 year (2 year cliff and 6 year prorated)

Note1: Additional man-hours will be billed separately from the proposed system capital cost at a rate of $1,300 per day plus living and traveling expenses. Detailed GE Water service rates are available upon request.

Note2: All GE supplied equipment is designed for installation in an unclassified area.



6 Buyer Scope of Supply

The following items are for supply by Buyer and will include, but are not limited to:

� Overall plant design responsibility

� Installation on site of all GE Water-supplied skids and loose-shipped equipment

� Review and approval of design parameters related to the membrane separation system

� Review and approval of GE Water-supplied equipment drawings and specifications

� Detail drawings of all termination points where GE Water equipment or materials tie into equipment or materials supplied by others

� Equipment foundations, civil work, full floor coverage equipment contact pads, buildings, etc.

� Receiving, unloading and safe storage of GE Water-supplied equipment at site until ready for installation

� HVAC equipment design, specifications and installation (where applicable)

� UPS, Power Conditioner, Emergency power supply and specification (where applicable)

� Lifting devices including Crane able to lift 5 ton for membrane removal, lifting davit crane and guide rails for submersible mixers and pumps, hoists, etc…

� 1 to 2 mm Pretreatment fine screen

� Equalization tank – as required

� Bioreactor tanks

� Membrane tanks c/w Tank Coating to be suitable for appropriate chemical contact

� Treated water storage tank – as required

� Acoustical enclosures for membrane and process blowers

� Process and utilities piping, pipe supports, hangers, valves, etc. including but not limited to:

• Piping, pipe supports and valves between GE-supplied equipment and other plant process equipment

• Piping between any loose-supplied GE equipment

• Process tank aeration system air piping, equalization tank system piping, etc.

• Interconnecting pipe between GE-supplied Skids and Tanks (as applicable)

� Electrical wiring, conduit and other appurtenances required to provide power connections as required from the electrical power source to the GE control panel and



from the control panel to any electrical equipment, pump motors and instruments external to the GE-supplied enclosure

� All bolts, brackets and fasteners to install GE-supplied equipment. Seismic structural analysis and anchor bolt sizing.

� Alignment of rotating equipment

� Raw materials, chemicals, and utilities during equipment start-up and operation

� Supply of seed sludge for process start-up purposes

� Disposal of initial start-up wastewater and associated chemicals

� Weather protection as required for all GE supplied equipment. Skids and electrical panels are designed for indoor operation and will need shelter from the elements.



7 Commercial

7.1 Pricing Table

Pricing for the proposed equipment and services, as outlined in Section 5.8, is summarized in the table below. All pricing is based on the operating conditions and influent analysis that are detailed in Section 5 of the proposal. The pricing herein is for budgetary purposes only and does not constitute an offer of sale. No sales, consumer use or other similar taxes or duties are included in the pricing below.

Price: All Equipment & Service

One (1) Z-MOD™–L system, as per Section 2.7. $ 1,291,600 CAD

7.2 Power & Chemical Consumption Estimates

The data presented below is for information purposes only and is based on the design information provided by the Buyer and presuming that the equipment is operated according to the design basis and in accordance with Seller’s Operations and Maintenance manuals.

Daily power consumption estimate 1

Equipment kWh/day

Permeate Pumps 28

Membrane Blowers 2 250

Bioreactor Aerobic Blowers 482

Recirculation Pumps 240

Air Compressors 12

Total 1,012 kWh/day

Note1: Power consumption estimate is calculated at ADF conditions

Note2: Assumes membrane relaxation for sludge prevention method

Annual chemical consumption estimate

Chemical L/year

Sodium Hypochlorite (10.3% w/w, SG: 1.168) 4,410

Citric Acid (50.0% w/w, SG: 1.24) 3,465 Note: Cleaning chemical consumption estimates based on the following frequencies and concentrations

summarized in the table below. Frequencies are assumed, actual frequency of maintenance and recovery cleans may change with final design, or may change once system is in operation.

Basis of chemical consumption estimate

Chemical Maintenance Clean Recovery Clean

Sodium Hypochlorite solution (10.3% w/w, SG: 1.168)

Frequency 2 times per week 2 times per year

Concentration 200 mg/L 1,000 mg/L

Citric Acid Solution (50.0% w/w, SG: 1.24)

Frequency weekly 2 times per year Concentration 2,000 mg/L 2,000 mg/L



7.3 Freight

The following freight terms used are as defined by INCOTERMS 2000.

All pricing is FCA from Oakville, ON.

7.4 Bonds

Performance or Payment Bonds are not included in the system price. These bonds can be purchased on request but will be at additional cost.

7.5 Equipment Shipment and Delivery

Equipment Shipment is estimated at 24 to 36 weeks after order acceptance. The Buyer and Seller will arrange a kick off meeting after contract acceptance to develop a firm shipment schedule.

Typical Drawing Submission and Equipment Shipment Schedule

6-8 weeks 2 weeks 16-26 weeks 2 weeks

Acceptance of PO

Submission of Drawings

Drawings Approval

Equipment Manufacturing

Equipment Shipment

Plant Operations Manuals

The delivery schedule is presented based on current workload backlogs and production capacity. This estimated delivery schedule assumes no more than 2 weeks for Buyer review of submittal drawings. Any delays in Buyer approvals or requested changes may result in additional charges and/or a delay to the schedule.

7.6 Pricing Notes

� All prices quoted are in Canadian Dollars.

� Any applicable sales or value added tax is not included.

� The Buyer will pay all applicable Local, Provincial, or Federal taxes and Duties

� The equipment delivery date, start date, and date of commencement of operations are to be negotiated.

� Commercial Terms and Conditions shall be in accordance with Seller’s Standard Terms and Conditions of Sale.



7.7 Conditional Offering

Buyer understands that this proposal has been issued based upon the information provided by Buyer, and currently available to Seller, at the time of proposal issuance. Any changes or discrepancies in site conditions (including but not limited to system influent characteristics, changes in Environmental Health and Safety (“EH&S”) conditions, and/or newly discovered EH&S concerns, Buyer’s financial standing, Buyer’s requirements, or any other relevant change, or discrepancy in, the factual basis upon which this proposal was created, may lead to changes in the offering, including but not limited to changes in pricing, warranties, quoted specifications, or terms and conditions. Seller’s offering in this proposal is conditioned upon a full Seller EH&S, and Buyer financial review.

Millbrook WWTPJan-13

MBR

Item Equipment No. Units

Installed

No. Units

Operating

at ADF

Design

Capacity

(per unit)

Operating

Capacity

(per unit)

Design TDH

or Discharge

Pressure

Operating

TDH or

Discharge

Pressure

Motor HP (per

unit)

Connected

Motor HP

(all units)

Hours of

Operation

per Day

Power Consumed

per Day

1 Permeate Pumps 2 2 638 USgpm 292 USgpm 20.0 ft 5.0 ft 15.00 HP 30.00 HP 23.00 hr 28 kW.hr

3 Membrane Aeration Blowers 3 1 624 scfm 540 scfm 6.0 psig 4.7 psig 25.00 HP 75.00 HP 24.00 hr 250 kW.hr

4 Bioreactor Aeration Blowers 2 1 600 scfm 583 scfm 8.9 psig 7.6 psig 40.00 HP 80.00 HP 24.00 hr 482 kW.hr

6 RAS pumps 2 2 1,271 USgpm 1,271 USgpm 10.0 ft 10.0 ft 7.50 HP 15.00 HP 24.00 hr 240 kW.hr

8 Air Compressors 2 1 20 scfm 20 scfm 100 psi 75 psi 7.50 HP 15.00 HP 4.00 hr 12 kW.hr

Connected Power 215.0 HP

Daily Power Consumption 1,012 kW.hr

Tertiary UF


Installed

No. Units

Operating

at ADF

Design

Capacity

(per unit)

Operating

Capacity

(per unit)

Design TDH

or Discharge

Pressure

Operating

TDH or

Discharge

Pressure

Motor HP (per

unit)

Connected

Motor HP

(all units)

Hours of

Operation

per Day

Power Consumed

per Day


2 Backwash Pumps 2 1 840 USgpm 840 USgpm 115.3 ft 71.5 ft 50.00 HP 100.00 HP 1.00 hr 20 kW.hr


8 Compressors 2 1 20 scfm 20 scfm 100 psi 100 psi 7.50 HP 15.00 HP 2.00 hr 6 kW.hr


Daily Power Consumption 241 kW.hr



MicoClear™ Membrane Bioreactor

newterra ltd.

© 2012 by newterra, ltd. All rights reserved. No part of this document may be reproduced or transmitted in any form or by any means, electronic, mechanical, photocopying, recording, or otherwise, without prior written permission of newterra ltd.

BUDGET PROPOSAL 300249R2 2,600 Cubic Meters/Day

Peterborough, ON

newterra MicroClearTM MEMBRANE BIOREACTOR WASTEWATER TREATMENT

SYSTEM

1/14/2013

At newterra we understand that our performance will have a direct impact on your success of your project We are extremely committed to ensuring that you are successful. This means that if we do not live up to

your expectations, we will do whatever it may take to resolve an issue immediately.

Submitted To:

R.V. Anderson Associates Limited 2001 Sheppard Avenue East, Suite 400, Toronto, ON M2J 4Z8

Attn:

Valera Saknenko [email protected]

416-497-8601 ext. 250 Submitted By: newterra 1325 California Avenue Brockville ON K6V 5Y6 Alexander Crowell Regional Manager Cell: 902-818-8335 Office: 1-800-420-4056 [email protected]

Local Representative: SPD Sales Ltd. 6415 Northam Drive Mississauga, ON L4V 1J2 Frank Farkas Cell: 905-678-2882 Office: 1-800-811-2811 [email protected]

mailto:[email protected]


300249R2 Page 2 © 2012 by newterra, ltd. All rights reserved. No part of this document may be reproduced or transmitted in any form or by any means, electronic, mechanical, photocopying, recording, or otherwise, without prior written permission of newterra ltd.

newterra ltd. 1325 California Avenue, Brockville, ON K6V 5Y6 744 Gordon Baker Road, Toronto, ON M2H 3B4

(800) 420-4056 / www.newterra.com

TABLE OF CONTENTS Design Parameters: ...................................................................................................................................... 3

Influent Wastewater Characteristics and Effluent Quality: ............................................................................ 3

Scope of Supply: ........................................................................................................................................... 4

Price Breakdown: .......................................................................................................................................... 7

Estimated Power Consumption and Cost ..................................................................................................... 8

Estimated Parts Replacement Cost .............................................................................................................. 9

Estimated Chemical Consumption and Cost ................................................................................................ 9

Design Brief ................................................................................................................................................. 10

1.0 INTRODUCTION ......................................................................................................................... 10

2.0 DESIGN BASIS ........................................................................................................................... 11

3.0 UNIQUE FEATURES OF newterra MEMBRANES ..................................................................... 11

4.0 PROCESS DESCRIPTION ......................................................................................................... 12

PRE-TREATMENT .............................................................................................................................. 12

BIOLOGICAL TREATMENT ................................................................................................................ 12

5.0 TELEMETRY CONTROL AND REMOTE ACCESS ................................................................... 14

6.0 CALCULATION TABLES FOR SIZING AND LOADING............................................................. 15

Table 1: Feed water specification ........................................................................................................ 15

Table 2: Effluent Water Specification ................................................................................................... 16

Table 3: Membrane Calculation ........................................................................................................... 16

Table 4: Kinetic Constants at 20°C ...................................................................................................... 17

Table 5: Kinetic Constants at Design Temperature ............................................................................. 17

Table 6: Sludge Yield ........................................................................................................................... 18

Table 7: Biological parameters ............................................................................................................ 18

Table 8: Design of aerobic tank ........................................................................................................... 18

Table 9: Chemical sludge + final sludge for aerobic zone ................................................................... 19

Table 10: Size of Equalization tank ..................................................................................................... 19

7.0 MEMBRANE SPECIFICATIONS ................................................................................................ 20

8.0 PRELIMINARY SYSTEM DRAWINGS ....................................................................................... 21




DESIGN PARAMETERS: Average design flow 2,520 m3/d

Maximum daily flow (max. 7 consecutive days) 3,780 m3/d

Peak Hourly Flow (max. 4 hours per day) 8,242 m3/d

Minimum inlet temperature 8º C

Site power Three-phase, 575V, 60Hz

System Area Classification According to NFPA 820

Ambient outdoor temperatures: max: 37 °C, min: -40 °C

Elevation < 500 m

INFLUENT WASTEWATER CHARACTERISTICS AND EFFLUENT QUALITY: Parameters Unit Influent Wastewater

Characteristics Effluent Quality

pH s.u 6.5 – 8.5 6.5 – 8.5

FOG mg/L < 30

BOD5 mg/L 190 < 5

TSS mg/L 210 < 5

TKN mg/L 25

TAN (winter / summer) mg/L < 2 / 1

TP mg/L 5 0.1

Alkalinity (assumed) mg/L as CaCO3 > 200




SCOPE OF SUPPLY: Equalization Tank Components:

In-ground equalization tank by others with the following items supplied loose for installation by others: High level alarm switch Submersible level transmitter Coarse bubble air diffusers Four (4) sump pumps with rails (2 duty, 2 standby)

o One pair feeds each inlet screen All components installed by others

Equalization Blowers (Supplied loose for installation inside customer building):

Two (2) rotary lobe blowers: 1 blower duty, 1 blower standby

NOTE: This system has been quoted including new pumps, blowers and air diffusers. If existing equipment is available and can be reused for this purpose, a deduct price can be provided.

Inlet Screen (to be installed outside):

Two (2) screw screens Each heat traced and insulated Each gravity feeds into one aeration tank

Aeration Tank Components:

Two (2) in-ground aeration tanks by others with the following items supplied loose for installation in each tank by others:

High level alarm switch Level transmitter Dissolved oxygen transmitter pH transmitter Fine bubble air diffusers Three (3) sump pumps with rails, one feeding each membrane tank One (1) sump pump with rails for sludge wasting All components installed by others

NOTE: This system has been quoted with a sludge wasting pump in each aeration tank. No additional sludge conditioning or treatment equipment has been included as it was indicated that existing equipment and tanks at the site will be used for this purpose. If sludge treatment equipment is required, a proposal can be provided.




Aeration Blowers (Mounted on newterra skid):

Four (4) rotary lobe blowers for each aeration tank VFD controlled 1 blower duty, 1 blower standby for each tank

Membrane Tank Components:

Six (6) membrane treatment trains in in-ground tanks by others. The following items will be supplied loose for installation by others in each train:

High level alarm switch Pump control switch Two (2) Weise Water MB4-5 flat sheet membrane modules with:

o 304SS Construction o Full surface distribution o Fine bubble scouring o Laser sheet welding

Membrane Aeration Blower (Supplied loose for installation inside customer building):

Six (6) Sutorbilt rotary lobe blowers: One blower for each membrane tank

Permeate Extraction System (Mounted on newterra skids):

Each membrane tank to include one permeate extraction system (total of 6 systems) with Water flow transmitter Backflush tank with solenoid valve to each membrane tank Permeate pump

Chemical Injection (Supplied Loose):

Two (2) chemical metering pumps One pump to inject alum into each aeration tank

Two (2) chemical cleaning systems One for citric, one for sodium hypochlorite

System Skids:

Six (6) 8’ x 6’ epoxy-coated steel skids, each with the following equipment mounted and plumbed: Permeate extraction equipment for one membrane tank

Control System (Panel Supplied Loose):

DirectLogic PLC control panel with user interface touchscreen VFD’s for the following motors:




o Aeration tank blowers o Permeate pumps

Panels to be installed by others inside customer supplied building All wiring from panel to all components by others

NOTE: This system has been quoted including a main power disconnect, motor contactors and starters. An MCC can be quoted if it is required.

Operation and Maintenance Manual:

Two hard copies and one electronic copy provided




PRICE BREAKDOWN: Budget Equipment Purchase Cost: $ 2,355,000.00

Equipment Freight to Site: Not Included

Sales Tax on Equipment: Not Included

START-UP/COMMISSIONING: CAD $1,200.00/day plus expenses for travel, meals and accommodation

CURRENCY: All prices are quoted in CAN dollars.




ESTIMATED POWER CONSUMPTION AND COST

Equipment Qty per Unit

# Duty #

Standby Unit hp

Total Installed

hp

Total Operating

hp

Total Operating kW

Daily Run Time (h/d)

System Daily Operating (kWh/d)

Annual Energy Cost

($)

Equalizaiton Tank

Pumps 4 2 2 7.5 30 15 11.250 24 270 $9,855

Air Blowers 2 1 1 14 28 14 10.500 24 252 $9,198

Inlet Screen

Rotary screen 2 2 0 1 2 2 1.500 24 36 $1,314

Aeration Tank

Air Blowers* 4 2 2 6.9 27.6 13.8 10.35 20.4 211.14 $7,707

Membrane Feed Pumps 6 6 0 7.5 45 45 33.75 24 810 $29,565

Sludge Wasting Pump 2 2 0 7.5 15 15 11.25 3 33.75 $1,232

MBR Tanks

Air Scour Blowers 6 6 0 13.1 78.6 78.6 58.95 22 1296.9 $47,337

Permeate Pumps 6 6 0 7.5 45 45 33.75 18 607.5 $22,174

Chemical Injection

Metering Pumps 2 2 0 17Watts 0.034 24 0.816 $30

Sum 171.33 $128,411

Annual operation days 365

Cost per kWh $0.10 * Blowers have been sized including extra capacity for peaking/safety factors. 85% usage is assumed.

300249R2 Page 9 © 2012 by newterra All rights reserved. No part of this document may be reproduced or transmitted in any form or by any means, electronic, mechanical, photocopying, recording, or otherwise, without prior written permission of newterra



ESTIMATED PARTS REPLACEMENT COST

Qty in System Expected Life

(yrs) annual cost

EQ Tank

Submersible pump 4 5 $ 5,704.00

Diffusers (set) 1 5 $ 4,019.50

Blower 2 10 $ 1,504.00

Inlet Screen

Brushes 2 1 $ 2,520.00

Aeration Tank

DO transmitter 2 1 $ 2,730.00

pH transmitter 2 1 $ 2,730.00

Diffusers (set) 2 5 $ 3,639.00

Submersible pump 8 5 $ 4,048.00

Blower 2 10 $ 1,504.00

Membrane Tank

Membranes 1200 8 $ 166,560.00

Blower 6 10 $ 4,872.00

Permeate

Pump 6 5 $ 29,112.00

Modulating valve 6 4 $ 6,195.00

Solenoid valve 12 5 $ 1,992.00

Chemical Injection

Feed Pump 2 10 $ 257.00

Total

$ 237,386.50

ESTIMATED CHEMICAL CONSUMPTION AND COST

Chemical Annual Usage

(liters) Cost per

liter Total Annual

Cost

Sodium Hypochlorite (12%) 1,785 $ 0.30 $ 536.00

Citric Acid (50%) 2,141 $ 0.20 $ 428.00

Alum (48%) 143,372 $ 0.07 $ 10,036.00

Total $ 11,000.00




DESIGN BRIEF 1.0 INTRODUCTION The newterra MBR system is designed specifically for decentralized applications and can easily meet required effluent discharge criteria of BOD < 5 mg/L, TSS < 5 mg/L, TP < 0.1 mg/L and E. Coli < 100 CFU/100mL (after UV). The newterra MBR system, employing submerged MicroClearTM membranes, is designed to be the simplest, easiest-to-operate, and most operator-friendly flat plate ultrafiltration (UF) membrane technology available. The newterra MBR system produces ultra-clean water which effectively meets any water standards for discharge and reuse. As a result, there are over 1,000 installations worldwide using the submerged MicroClear membrane technology. The advantages that the newterra MBR Package WWTP offers include:

No chemical cleaning required for daily membrane operation/performance; Factory assembled and tested; Designed and built to work in extreme and harsh cold weather conditions; Reliable and low maintenance system; Superior effluent quality that is suitable for reuse; Compact footprint; Minimal noise and odourless operation; Backflushable flat plate membrane system; Low transmembrane pressure system – only 0.1 to 0.2 bar vacuum required; Excellent membrane structure life.

In addition, the ultrafiltration (UF) membranes, with a pore size of 0.04 µm provide an absolute physical barrier for a total removal of fecal coliforms and 4-log removal of viruses.

newterra UF MEMBRANE FILTRATION LEFT: RAW SEWAGE RIGHT: MBR EFFLUENT




2.0 DESIGN BASIS

The newterra MBR system is designed based on the following:

Average Design Flow : 2,520 m3/d Influent wastewater temperature (min) : 8 0C Altitude : < 500m Max FOG (fat, oil and grease) : < 30 mg/L Power available at site (assumed) : three-phase 575V 60Hz Area classification as per NFPA 820 Site noise constraints: none Ambient temperatures: max: 37 0C, min: -40 0C

Prohibited items (MBR)

Hydrocarbons – lubricants, gasoline, diesel, etc. High amounts of fat, oil and grease (FOG), silicone, iron and manganese. Silicone based defoamer. Paints and solvents.

Wastewater Characteristics and Treated Effluent Quality

Parameters Unit Influent Wastewater

Characteristics Effluent Discharge

Objective

pH (assumed) s.u. 6.5 – 8.5 6.5 – 8.5

FOG mg/L < 30 n/a

BOD5 mg/L 190 < 5

TSS mg/L 210 < 5

TKN mg/L 25

TAN (winter / summer) mg/L < 2 / 1

TP mg/L 5 0.1

Alkalinity (assumed) mg/L as CaCO3 200 -

3.0 UNIQUE FEATURES OF newterra MEMBRANES newterra membranes provide the following unique features:

Low electric power consumption - filtrate is drawn through and out of the filter by a slightly negative pressure (vacuum) of only 0.1 – 0.2 bar;




Membrane sheet-to-backing sheet welding by laser – perfect welding, ensures no ingress of dirty wastewater into the clean permeate;

Laser-welded flat plate membrane during Pressure Test

UF membranes with a molecular weight cut-off of 150k Dalton, equivalent to a pore size of 0.04 µm, leaving out any bacteria (1 – 2 µm), parasites (5 – 50 µm), with a bacteria removal of 99.9999% and virus removal of 99.99%;

No weekly/monthly maintenance cleaning required; Cleaning during operation by cyclic backflushing – probably the only backflushable flatsheet

membrane modules in the marketplace; Patented special design of backing sheet surface – thus no need for a gauze between the membrane

and backing sheets to prevent adhesion; FSD™ (full surface distribution) – full membrane surface utilization for permeate collection by multiple

outflow points, thus no short-circuiting and even flux distribution; Easily expandable with modular design.

4.0 PROCESS DESCRIPTION MBR treatment technology is a simple, yet an effective combination of activated sludge biological treatment process with membrane filtration. The UF membranes act as a physical barrier against the passage of all particulate solids, contrary to gravity settlement of mixed liquor in the conventional activated sludge process. As a result, the MBR can operate at a much higher MLSS concentrations (typically 8 to 15 g/L vs. 2 to 4 g/L in conventional activated sludge system). This results in a robust, versatile, and ultra compact wastewater treatment system (only 30% footprint of comparable conventional treatment system). In addition, the high concentration of biomass inventory in MBR system provides resilience to changes in influent quality.

PRE-TREATMENT The source of the wastewater will be municipal sewage.

The equalization tank is provided to minimize loading fluctuation and balance flow to the newterra MBR WWTP. Submersible pumps will deliver wastewater to the aeration tank (see attached calculations).

BIOLOGICAL TREATMENT Inlet Screen

Two fine screens with 2 mm openings are required after the equalization tank to remove hair and fibrous materials for membrane protection. The screenings drop into a solids bin for offsite disposal by others. Wastewater flows into the aeration tanks after the screens.

FSDTM (full surface distribution)




Aeration Tank

Objective: (i) Oxidation of carbonaceous BOD, (ii) Nitrification (conversion of NH4-N to NO3-N)

A fine-bubble diffused aeration system is installed inside each aeration tank to meet biological oxygen demand and mixing requirements. MLSS in the aeration tank is maintained between 8 to 12 g/L, with a design value of 10 g/L in the aeration tank.

Chemical metering pumps will inject Alum for phosphorus removal.

The waste activated sludge is periodically wasted from the aeration tank to customer supplied on-site tanks.

Membrane Tanks

Objective: (i) Mixed liquor filtration, (ii) Supplemental biological oxidation

Each membrane tank contains one MB4-5 Membrane cassette (membrane cassette complete with stainless steel housing, medium-bubble diffused aerators, and permeate piping). Vacuum pumps draw clear water through the membranes under a slight vacuum of 0.1 to 0.2 bar. The permeate obtained is almost as clear as the city water. A small portion of the permeate is stored in a backflush tank to provide water for backflushing the units via gravity.

Vacuum pumps operate on a cyclic basis – for example, permeation for 9 minutes, and then stop permeation for about 45 seconds to allow for backflushing (injection of clean water in the reverse direction), which more thoroughly removes the particles precipitating inside the membrane pores. After this, permeation is restarted, and the cycle is repeated continuously. Length of the cycle is adjustable to meet the particular plant operating needs. During plant operation, a combination of backflushing and relaxation is used.

In addition to this, air diffusers placed below the membrane cassette provide optimized air distribution for continuous scouring of the membrane surface removing the accumulated dirt layer. This way, membranes are kept clean to the maximum extent during operation. The medium-bubble air diffusers installed below the newterra flat plate membrane cassette also allow for the efficient dissolution of oxygen into the mixed liquor, providing oxygen credit to the overall air demand, which complements the biological oxidation process taking place in the aeration tank.

Mixed liquor from the membrane tanks is constantly recycled back to the aeration tank by gravity to maintain even biomass inventory inside the aeration and membrane tanks.




5.0 TELEMETRY CONTROL AND REMOTE ACCESS

newterra SITE-LINK is a customized software program and hardware configuration which provides a real-time link to a treatment system via cellular modem or customer supplied internet connection using our secure Site-Link Server. An annual Telemetry Service Agreement with newterra is required which includes all costs associated with the service.

newterra Site-Link comes with the following customizable features:

Customized P&ID layout with system status Start/Stop/Reset of system Manual control of all system components† Data logging exports in .csv format Daily system status reports (E-Monitor) Alarm history including current alarm status Hour meters for equipment†† Customization of all system set points† Live and historical trending††† Immediate text & email on alarm (E-Alarm)

†certain restrictions apply †† only applies when hour meters are quoted with system ††† must be requested at quote stage

The basic system requires that the customer provide a standard computer network cable to the control panel. If the customer’s computer network is accessible to the internet, this system can also be monitored from any internet enabled computer.

This system is not available if customer supplied internet connection or cellular service is not available at the site. During internet outages, reports cannot be sent and system status cannot be monitored remotely.




6.0 CALCULATION TABLES FOR SIZING AND LOADING Table 1: Feed water specification Parameter Value ADF (m3/d) 2520 Qa (m3/h) 105.02 Peak flow (m3/d) 8242.00 Qp (m3/h) 343.42 Max. Daily flow (m3/d) 3780.00 Qm (m3/h) 158.00 COD (mg/L) 380 BOD (mg/L) 190 TSS (mg/L) 210 VSS/TSS (%) 80 VSS (mg/L) 168 iTSS (mg/L) 42 non-biodegradable VSS, nbVSS (mg/L) 56.0 TKN 25 NH4-N (mg/L) 20 TN (mg/L) 27.78 TP (mg/L) 5 FOG (mg/L) - assumed 30 Min Tw (˚C) 8 Site elevation (m) 200 Alkalinity (mg/L) - assumed 250 COD load (kg/d) 957.78 BOD load (kg/d) 478.89 TN load(kg/d) 63.01 TN in WAS (kg/d) 25.61 TP loading (kg/d) 12.60




Table 2: Effluent Water Specification

Parameter Set Value Design Objective TN (mg/L) COD BOD (mg/L) 5 NO3-N (mg/L) NH4-N (mg/L) 1 TSS (mg/L) 5 TP (mg/L) 0.1 E.coli/TC (cfu/100ml) Table 3: Membrane Calculation Parameter Value Assumptions & notes 1. Capacity Selected Average Design Flux (LMH) 20 at 20°C Membrane area required 5251 Surface Area / Membrane casssette (m2) 7 MicroClear MCXL No. of membrane tank 6 Operating Number of Module in a Membrane Tank 2 Selection of Module MB4-5 Membrane cassette per selected module 100 Total membrane area/module (m2) 700 Total membrane area (m2) 8,400 Actual design flux (LMH) 13 15.77 Total Installed Number of cassette 1200 Modules 2. Scouring Aeration Air flow per membrane unit (Nm3/h) 250 Air flow per membrane tank (Nm3/h) 500 Total MBR air flow (Nm3/h) 3,000 Alpha value at design MLSS, α 0.40

Actual oxygen transfer efficiency, AOTE (%/m) 0.02 Air density (changes based on temp & altitude) (kg/m3) 1.20 % oxygen in air (%) 21 Oxygen saturation mass in water (kg O2/m3) 0.251 Oxygen credit by membrane aeration (kg O2/h) 24.0768 Oxygen credit by membrane aeration (kg O2/d) 577.8432 3.Membrane Tank Design Square Tank L (m) 4.1 Tank W (m) 3.4




Tank H (m) 4 Volume/tank (m3) 55.8 Volume displaced by each MBR cassette (%) 20% Effective MBR tank volume (m3) 44.6 Total effective MBR volume (m3) 267.6 HRT (h) 2.55 Blower headloss, psi 6.6 Table 4: Kinetic Constants at 20°C BOD, T=20˚C (bCOD = 1.6x BOD for domestic only) Ammonia, T=20˚C Parameter Value Parameter Value Ks (g BOD/m3) 32 µm,n (g VSS/g VSS.day) 0.75 ke or kd (per day) 0.12 Kn (g NH4-N/m3) 0.74 Y (g VSS/g BOD) 0.30 ken or kdn (g VSS/g VSS.day) 0.08 µm (g VSS/g VSS.day) 6 Yn (g VSS/(g NH4-N) 0.12 Y=0.28 -0.67 (domestic)

Table 5: Kinetic Constants at Design Temperature BOD removal at design temperature NH4-N removal at design temperature Parameter Value Parameter Value Design temp, oC 8 Design temp, oC 8 Ks (g BOD/m3 ) 32 µm,n (g VSS/(g VSS.day) 0.33 ke or kd (per day) 0.07 Kn (g NH4-N/m3) 0.40 Y (g VSS/g BOD) 0.30 ken or kdn (g VSS/g VSS.day) 0.05 µm (g VSS/g VSS/day) 2.66 Yn (g VSS/(g NH4-N) 0.12 k (g BOD/g VSS/day) 8.88 k0 (g/m3) 0.5 fd (g VSS/g BOD) 0.88 µn . theoretical(g/(g/day)) 0.11 Yobs (g VSS/g BOD) 0.28 Safety factor 1.5 YH (g TSS/g BOD) 0.38 SRTaerobic, theoretical (day) 13.79 Yobs ( gTSS/g BOD)-overall 0.90 SRTtotal, design (day) 20




Table 6: Sludge Yield Parameter Value Effluent BOD, Se (g/m3) 1.57 NOx (g/m3) 15.00 Px,bio (kg VSS/day) 134.85 X0 (kg/day) 141.15 Px,vss= Px,bio+ X0 (kg/day) 276.00 Px,tss (kg/day) 426.81 Qw, biomass (m3/day) 53.35 Nitrogen uptake through sludge production (6% solids content) (mg/L) 10.16 Phosphorus uptake through sludge production (1.5% solids) (mg/L) 2.5 Table 7: Biological parameters Parameter Value V(m3), aerobic tank + membrane tank 1067.01 HRT (h), aerobic tank + membrane tank 10.16 F:M ratio (range of 0.04 to 0.12 ) (kg BOD/kg MLSS.d)-aerobic 0.056 F:M ratio (range of 0.06 to 0.2 ) (kg BOD/kg MLVSS.d)-aerobic 0.094 Overall SRT (d) = SRTaerobic +SRT anoxic + SRT post anoxic 20 Organic Loading rate (kg COD/m3.d) 0.90 Organic Loading rate (kg BOD/m3.d) 0.45 Table 8: Design of aerobic tank Parameter Value V (m3) 799.37 Number of aeration tank 2.00 Individual AT volume (m3) 399.68 L (m) 11.10 W (m) 8 D (m) 4.5 HRT (h) 7.61




Table 9: Chemical sludge + final sludge for aerobic zone Parameter Value Effluent TP limit (mg/L ) 0.10 Al:P molar ratio (changes based on effluent TP limit) 3.00 Dosage of alum to phosphorus ratio (25% safety factor) 42 Phosphorus required to be removed (mg/L) 2.4 Alum dosage concentration (mg/L) 98 Alum solution by weight 48% Alum solution density (kg/m3) 1310 Daily alum solution dosage (48%) (L/d) 394.2 Daily alum solution dosage (48%) (L/h) 16.4 Alum storage (d) 30.0 Required alum storage volume (L) 11,825 Chemical sludge produced (as AlPO4 and Al(OH)3) (kg/d) 53.5 Total sludge produced (kg TSS/d) 480.3 Sludge wasting rate (at 1%, 10g /L) (m3/d) 48.0 Table 10: Size of Equalization tank Parameter Value Qp (m3/h) 343.42 Qa (m3/h) 105.02 peak factor 3.27 duration of peak (h) 3.49 Volume (m3) 832.01 HRT (h) 7.92 Aeration (m3/m3.min) 0.01 Blower Capacity (m3/h) 499.2032744 Blower Capacity (scfm) 293.7 Effective water depth (m) 4 Tank L (m) 24.38 Tank W (m) 8.53 Minor piping and fitting loss (kpa) 8.0 Total head loss (kPa) 47 Total headloss (psi) 6.81




7.0 MEMBRANE SPECIFICATIONS




8.0 PRELIMINARY SYSTEM DRAWINGS



Enviroquip® Membrane Bioreactor

Ovivo USA, LLC

© Copyright 2010 GLV. All rights reserved.

This document is confidential and shall remain the sole property of Ovivo. This document may not be reproduced or distributed without prior written approval of Ovivo. The data and information provided is furnished on a restricted basis and is not to be used in any way detrimental to the interests of Ovivo.

Ovivo USA, LLC 2404 Rutland Drive Austin TX 78758 USA Telephone: 512.834.6000 Facsimile: 512.834.6039 www.ovivowater.com

MBR Proposal/Submittal Township of Cavan-Millbrook-North Monaghan

January 14, 2013 Ovivo Proposal #010713-1-AK-R0

Prepared For Valera Saknenko

RV Anderson Associates 2001 Sheppard Avenue

East, Suite 400 Toronto, ON M2J 4Z8

Phone: 416.753.2490 Fax: 416.497.0342

Design SummaryMillbrook WWTP (AAF 2,520 M3D)

Parameter Flow Temperature Typical Event Duration Design Durations

Average Annual Flow (AAF) 2,520 m3/day 15 °C * 9 consecutive months 9.0 months *Max Month Flow (MMF) 3,274 m3/day 10 °C 3 consecutive months 3.0 months *Peak Week Flow (PWF) ** 3,929 m3/day 10 °C * 3 non‐consecutive weeks 3.0 weeks *Peak Day Flow (PDF) ** 6,549 m3/day 10 °C * 8 non‐consecutive days 8.0 days *

Peak Hourly Flow (PHF) ** 6,549 m3/day 10 °C * 4 hrs with 24 hrs between PHF 1.0 hours

Influent

190 mg/L

210 mg/L

25 mg/L

18 mg/L *5 mg/L

25 mg/L *300 mg/L *

20 °C274 m *

Value

2

1

6

RW 400

Parameter

No. of Membrane BasinsNo. of Membrane Rows per BasinNo. of Membrane Units per Basin

Membrane Unit Type

TSS

< 75 mg/L *< 10 mg/L *< 0.1 mg/L

< 1 mg/L

< 3 mg/L *< 5 mg/L

BOD

Parameter

< 5 mg/L

Elevation

Maximum Wastewater Temperature

Alkalinity

Effluent Limits

TN

TP

cartridge: 515HP

Basis of Design

** Peak values assumed to occur during MMF, to be verified by consulting engineer.

12 units total

* Value assumed by Ovivo, to be verified by consulting engineer.

MBR Zone (Membrane) Design

NH3

TKN

Notes

RW‐400400

1.45 m2/cartridge

0.36 m3/(m2 x day)0.47 m3/(m2 x day)0.56 m3/(m2 x day)0.94 m3/(m2 x day)0.94 m3/(m2 x day)

140 m3/basin

148.9 m3/hr/unit

348 kg O2/day11,487 mg/L

Value

159 m3/basin

5.2m x 6.8m x 4.6m SWD

9,190 mg/L

4 Q

Flux @ 2,520 m3/day

Flux @ 3,274 m3/day

Flux @ 3,929 m3/day

Flux @ 6,549 m3/day

Surface Area per Cartridge

Flux @ 8,242 m3/day

Membrane Basin Volume

Membrane Unit TypeNo. of Cartridges per Unit

cartridge: 515HP4,800 membrane cartridges total

4.3m x 6.8m x 4.9m SWD

TMP Ranges from 3.4 ‐ 21 kPa

Parameter

Membrane Air Scour Rate for SizingAOR Supplied by Air Scour

MBR Basin MLSS

6,957 m2 total

From MBR to Anoxic Basin

@ 52.7 kPa discharge

Basin Volume

Anoxic Zone DesignNotes

Basin Dimensions

Anoxic MLSS

318 m3 Total

Recycle Rate

© Copyright 2010 GLV. All rights reserved. 010713-1-AK-R0 Design Summary, Page 1


Value

175 m3/basin

5.1m x 6.8m x 5.2m SWD

9,190 mg/L

515 kg O2/day

Value

80 m3/basin

2.5m x 6.8m x 4.9m SWD

Value

454 kg sludge / day1.15%

39,547 liters sludge / day0.75

Value

7.8 hrs18 days0.06

V l

WAS Volatile Fraction

Parameter

Plant HRTDesign Plant SRT

System Design Parameters

F:M ratio

Feed Forward Pump Design

Anaerobic Zone Design

Notes

solids

349 m3 Total

N t

Sludge Flow

159 m3 Total

Total Sludge ProductionSludge Concentration

Parameter

Notes

P t

Notes

Basin Volume

Assumed

Notes

Pre‐Aeration Zone Design

MBR Waste Activated Sludge Production Parameters

Parameter

Basin Volume

Basin Dimensions

Parameter

Basin Dimensions

Pre‐Aeration MLSS

Fine Bubble Diffuser AOR

Value

4

SUBMERSIBLE

409 m3/hr

6.1 m

Feed Forward Pumps

Unit CapacityTDH

Notes

2 Duty, 2 StdbyType

Parameter



Value

4

SUBMERSIBLE

68 m3/hr

3.0 m

Value

2

8'' valve152 m3/hr

Value

2

CENTRIFUGAL

152 m3/hr

7.6 m

Value

3

POSITIVE DISPLACEMENT

579 SCFM52 75 kP di h

TDH

MBR BlowersType

Unit MBR Blower CapacityMBR Bl Di h P

Parameter

Notes

Permeate Pumps

Type

Unit Permeate Pump Capacity

Permeate Pump Design

2 Duty, 0 StdbyParameter

Blower DesignNotes

2 duty, 1 Common Stdby

2 Duty, 2 StdbyParameter

Bio‐P Recycle Pump Design

Unit CapacityType

Notes

TDH

Pump‐Assisted Gravity Design

Bio‐P Recycle Pumps

Flow Control Valve (MODULATING BUTTERFLY)Max Design Flow Capacity per FCV

Permeate Pump‐Assisted Gravity Flow Control Valve DesignParameter Notes

Permeate Flow Control Valves

52.75 kPa discharge2

POSITIVE DISPLACEMENT

197 SCFM60.65 kPa discharge

Value

Sodium Hypochlorite1‐2

5.11 L/cartridge12.26 m3/basin

0.0025

245 L/basin/cleaningOxalic Acid

1‐25.11 L/cartridge12.26 m3/basin

0.01

123 L/basin/cleaning

Parameter

Cleaning chemical (organic fouling)

Typical Cleaning ScheduleVolume per Membrane

Volume of Cleaning SolutionCleaning Solution ConcentrationVolume of 100.0% Stock solution

Cleaning Solution ConcentrationVolume of 12.5% Stock solution

Cleaning chemical (inorganic fouling)

Pre‐Aeration (PA) BlowersType

Unit PA Blower CapacityPA Blower Discharge Pressure

MBR Blower Discharge Pressure

Typical Cleaning ScheduleVolume per Membrane

Volume of Cleaning Solution

2 times/yr

cleanings/basin/yr

Notes

Chemical Cleaning Design

2 times/yr

cleanings/basin/yr

2 duty


Scope of SupplyMillbrook WWTP (AAF 0.67 MGD)

Headworks General Equipment Information

Function Name TypeSize or Unit

CapacityValue Material Manufacturer Model or Specification

Motor

HPQTY

SCREENING FINE SCREEN BAR SCREEN 700 gpm SS bars and rakes ENVIROQUIP FM‐1400 0.25 3

INFLUENT FLOW MEASUREMENT

FLOW METER ELECTROMAGNETIC 10 Inch POLYURETHANEENDRESS & HAUSER

PROMAG 10W2F‐ULGA1RA0B4AA

N/A 1

PLANT WATER ISOLATION

VALVE BALL 2 Inch PVC ASAHI 1601‐020 N/A 1

LEVEL MEASUREMENT

LEVEL SWITCH FLOAT N/A N/A POLYURETHANE CONERY 2900B1S1 N/A 4

Anaerobic Zone General Equipment Information



Motor

HPQTY

BASIN MIXING MIXER SUBMERSIBLE 21,065 gallons STAINLESS STEEL WILO TR36‐.89‐8/8 1.65 2

MIXER SUPPORTMIXER SUPPORT

HARDWARE & GUIDE RAIL MOUNT SS N/A N/A N/A N/A N/A 2

LEVEL MEASUREMENT

LEVEL TRANSMITTER HYDROSTATIC 23 feet SS BLUE RIBBON BC001‐10‐40 N/A 1

LEVEL MEASUREMENT

LEVEL SWITCH FLOAT N/A N/A POLYURETHANE CONERY N/A N/A 2

Anoxic Zone General Equipment Information



Motor

HPQTY




LEVEL MEASUREMENT

LEVEL TRANSMITTER HYDROSTATIC 23 feet SS BLUE RIBBON BC001‐10‐40 N/A 2

LEVEL MEASUREMENT


l l l i f iInternal Recycle General Equipment Information



Motor

HPQTY

Feed Forward PUMP SUBMERSIBLE 1,802 gpm CAST IRON WILO FA25.74‐36HP 36 4

PUMP ISOLATION VALVE PLUG 12 Inch CAST IRON PRATT PBPV‐120 N/A 8

FLOW DIRECTION VALVE SWING CHECK 12 Inch CAST IRON KEYSTONE 810‐120 N/A 4

PUMP INLET PRESSURE

GAUGE COMPOUND ‐30‐+15Inch Hg/PSI

SS MCDANIEL MPB/SCA‐GF N/A 4

PUMP OUTLET PRESSURE

GAUGE PRESSURE 0‐15 PSI SS MCDANIEL MPB/SCU‐GF N/A 4

Feed Forward FLOW METER


PROMAG 10W3H‐ULGA1RA0B4AA

N/A 2

MBR BASIN ISOLATION

VALVE PLUG 12 Inch CAST IRON PRATT PBPV‐120 N/A 2

Bio‐P Recycle General Equipment Information



Motor

HPQTY

BIO‐P RECYCLE PUMP SUBMERSIBLE 300 gpm CAST IRON WILO FA10.51‐2.8HP 2.8 4

PUMP ISOLATION VALVE BALL 4 Inch PVC ASAHI 1602‐040 N/A 4

FLOW DIRECTION VALVE SWING CHECK 4 Inch PVC ASAHI 1201‐040 N/A 4

PUMP INLET PRESSURE





© Copyright 2010 GLV. All rights reserved. 010713-1-AK-R0 Scope of Supply, Page 1


Pre‐Aeration Zone General Equipment Information



Motor

HPQTY




AERATION DIFFUSER FINE BUBBLE 197SCFM / basin

N/A AEROSTRIP N/A N/A 2

DISSOLVED OXYGEN MEASURMENT

DO PROBE LDO 0‐10 mg/L DO SS HACH 57900‐00 N/A 2

DO TRANSMITTERANALOG

TRANSMITTERSC200 N/A N/A N/A HACH LXV404.99.70112 N/A 2

MBR Zone General Equipment Information



Motor

HPQTY

MEMBRANE FILTRATION

SUBMERGED MEMBRANE UNIT

FLAT PLATE N/A N/A SS304 KUBOTA RW‐400 N/A 12

VIBRATION ISOLATION

DIFFUSER EXPANSION JOINT

BULB 3 InchSYNTHETIC RUBBER / SS

API AMS203 N/A 12

DIFFUSER INLET ISOLATION

VALVE BUTTERFLY 3 Inch CAST IRON KEYSTONE 221‐030 N/A 12

DIFFUSER OUTLET ISOLATION

VALVE PLUG 3 Inch CAST IRON PRATT PBPV‐030 N/A 12

PERMEATE BRANCH ISOLATION


LEVEL MEASUREMENT


DIFFUSER CLEANING AUTOMATED VALVE 2 POSITION PLUG 8 Inch CAST IRON PRATT / BETTISPBPV‐080 / EM840F‐48‐

C4‐02‐001N/A 2

CHEMICAL CLEANING ISOLATION


CIP VENT VALVE BALL 2 I h PVC ASAHI 1601 020 N/A 4CIP VENT VALVE BALL 2 Inch PVC ASAHI 1601‐020 N/A 4

PERMEATE HEADER ISOLATION

VALVE BUTTERFLY 8 Inch PVC ASAHI 3730‐080 N/A 4

FABRICATION FASTENERS N/A N/A N/A SS304 ENVIROQUIP N/A N/A 12

FABRICATIONSTRUCTURAL GUIDES & STABILIZER PIPES

N/A N/A N/A SS304 ENVIROQUIP N/A N/A 12

FABRICATIONIN‐BASIN PIPING &

SUPPORTSN/A N/A N/A SS304 ENVIROQUIP N/A N/A 12

FABRICATIONIN‐BASIN PIPING &

SUPPORTSN/A N/A N/A PVC ENVIROQUIP N/A N/A 12



Permeate Control General Equipment Information



Motor

HPQTY

TMP MEASUREMENTPRESSURE

TRANSMITTERDIAPHRAGM ‐15‐+15 PSI N/A

ENDRESS & HAUSER

CERABAR T PMC 131‐A22F1V6N/Q4H

N/A 2

PERMEATE PUMP PUMP CENTRIFUGAL 667 gpm GRAY IRON GORMAN RUPP T6A3S‐B 7.5 2

VIBRATION ISOLATION

EXPANSION JOINT BULB 8 InchSYNTHETIC RUBBER / SS

API AMS208 N/A 4

PUMP ISOLATION VALVE BUTTERFLY 8 Inch PVC ASAHI 3730‐080 N/A 4

VENT VALVE Solenoid 1 Inch TBD TBD TBD N/A 2

PUMP INLET PRESSURE





FLOW DIRECTION (PUMPED)

VALVE SWING CHECK 8 Inch CAST IRON KEYSTONE 810‐080 N/A 2

FLOW DIRECTION (GRAVITY)

VALVE SWING CHECK 8 Inch CAST IRON KEYSTONE 810‐080 N/A 2

ON/OFF VALVE NEEDLE 0.25 Inch POLYPROPYLENE ASAHI 5313.002 N/A 1

FLOW MEASUREMENT


PROMAG 10W2H‐ULGA1RA0B4AA

N/A 2

FLOW CONTROL AUTOMATED VALVEMODULATING BUTTERFLY

8 Inch PVC ASAHI / BETTISXV3‐080 / EM810F‐15‐C4‐

02‐103N/A 2

TURBIDITY MEASUREMENT

TURBIDITY METER OPTICAL 0‐100 NTU N/A HACH 60101‐01 N/A 1

TURBIDITY / PH TRANSMITTER

ANALOG TRANSMITTER

SC200 N/A N/A N/A HACH LXV404.99.70112 N/A 1

MBR Aeration General Equipment Information



Motor

HPQTY

Capacity HP

MBR BLOWER BLOWERPOSITIVE

DISPLACEMENT579 SCFM CAST IRON AERZEN GM25S‐50 50 3

MBR NOISE SUPPRESSION

SOUND ENCLOSURE WITH BLOWER N/A N/A N/A AERZEN N/A N/A 3

MBR BLOWER TEMPTEMPERATURE

GAUGEWITH BLOWER N/A N/A N/A AERZEN N/A N/A 3

MBR BLOWER PRESSURE

PRESSURE GAUGE WITH BLOWER N/A N/A N/A AERZEN N/A N/A 3

MBR BLOWER TEMP SWITCH

TEMPERATURE SWITCH

WITH BLOWER N/A N/A N/A AERZEN N/A N/A 3

MBR BLOWER FLOW CONTROL

VALVECHECK (WITH BLOWER)

N/A N/A N/A AERZEN N/A N/A 3

MBR BLOWER PRESSURE RELIEF

VALVEPRESSURE RELIEF (WITH BLOWER)


MBR BLOWER PRESSURE

PRESSURE TRANSMITTER

DIAPHRAGM ‐15‐+15 PSI N/AENDRESS & HAUSER


N/A 3

MBR AIR ISOLATION VALVE BUTTERFLY 8 Inch CAST IRON KEYSTONE 221‐080 N/A 5

MBR AIR FLOW MEASUREMENT

FLOW METER MASS AIR FLOW 8 Inch SSENDRESS & HAUSER

65I‐80AA0AD1ACBBBA N/A 2



PA Air Supply General Equipment Information



Motor

HPQTY

PA BLOWER BLOWERPOSITIVE

DISPLACEMENT197 SCFM CAST IRON AERZEN GM10S‐20 20 2

PA NOISE SUPPRESSION

SOUND ENCLOSURE WITH BLOWER N/A N/A N/A AERZEN N/A N/A 2

PA BLOWER TEMPTEMPERATURE

GAUGEWITH BLOWER N/A N/A N/A AERZEN N/A N/A 2

PA BLOWER PRESSURE

PRESSURE GAUGE WITH BLOWER N/A N/A N/A AERZEN N/A N/A 2

PA BLOWER TEMP SWITCH

TEMPERATURE SWITCH

WITH BLOWER N/A N/A N/A AERZEN N/A N/A 2

PA BLOWER FLOW CONTROL

VALVECHECK (WITH BLOWER)


PA BLOWER PRESSURE RELIEF

VALVEPRESSURE RELIEF (WITH BLOWER)


PA BLOWER PRESSURE

PRESSURE TRANSMITTER

DIAPHRAGM ‐15‐+15 PSI N/AENDRESS & HAUSER


N/A 2

PA BLOWER FLOW CONTROL

AUTOMATED VALVEMODULATING BUTTERFLY

4 N/A CAST IRONKEYSTONE /

BETTIS

221‐040 / EM500F‐15‐C4‐02‐102

N/A 2

PA AIR ISOLATION VALVE BUTTERFLY 4 Inch CAST IRON KEYSTONE 221‐040 N/A 2

Coagulant Dosing General Equipment Information



Motor

HPQTY

ALUM METERING PUMP

PUMP DIAPHRAGM 30 gpd PVDF LMI AA N/A 2

SMU CIP General Equipment Information



Motor

HPQTY

MAZZIE INJECTOR INJECTOR VENTURI 2 Inch POLYPROPYLENEMAZZEI

INJECTOR CORP2081 N/A 1

WATER SUPPLY 1601 020 / EM310F 10WATER SUPPLY VALVE

AUTOMATED VALVE 2 POSITION BALL 2 Inch PVC ASAHI / BETTIS1601‐020 / EM310F‐10‐

C4‐02‐102N/A 1

CIP THROTTLING VALVE BALL 2 Inch PVC N/A N/A N/A 2

INJECTOR PRESSURE GAUGE PRESSURE 0‐15 PSI SS MCDANIEL MPB/SCU‐GF N/A 2

DRAIN VALVE BALL CHECK 1 Inch PVC ASAHI 1210‐010 N/A 1

CHEMICAL ISOLATION


PRESSURE CONTROL VALVEPRESSURE REGULATOR

VALVE2 Inch N/A WILKINS 600/DUC N/A 1

CHEMICAL FLOW FLOW METER ROTOMETER 3 gpm POLYSULPHONE KOBOLD KSM‐4020 N/A 1

FLOW MEASUREMENT


PROMAG 10W50‐ULGA1RA0B4AA

N/A 1

INJECTOR ASSEMBLY PIPE SPOOL SUCTION N/A N/A N/A ENVIROQUIP N/A N/A 1

CHEMICAL TRANSFER TO MBR

HOSE SUCTION 1 Inch PVC TIGERFLEX W100 N/A 1

Controls General Equipment Information



Motor

HPQTY

PLANT CONTROL SCADA SOFTWARE N/A N/A N/A WONDERWARE N/A N/A 1

PLANT CONTROL HMIPANEL

MOUNT/DESKTOP PCN/A N/A N/A N/A N/A N/A 1

PLANT CONTROL PLC PANEL N/A N/A N/A N/A N/A N/A N/A 1



Miscellaneous General Equipment Information



Motor

HPQTY

PROJECT KICKOFF MEETING

N/A N/A N/A N/A N/A N/A N/A N/A 5

MECHANICAL INSPECTION


START‐UP / COMMISSIONING


TRAINING N/A N/A N/A N/A N/A N/A N/A N/A 5

QC & INSPECTION N/A N/A N/A N/A N/A N/A N/A N/A 1

SHIPPING & RECEIVING


INBOUND FREIGHT N/A N/A N/A N/A N/A N/A N/A N/A 1

OUTBOUND FREIGHT N/A N/A N/A N/A N/A N/A N/A N/A 1


Estimated Power Consumption

Millbrook WWTP

Evaluation @ 0.670 MGD

Flow ModeHours per

Mode

Permeate Setpoints Based

on AAF (gpm)

Intermittent 5.2 0

Low Flow 10.3 465

Medium Flow 5.5 698

High Flow 3.0 931

Equipment DutyMotor Nameplate (Hp)

per unitControl Max Flow (GPM) Plant Mode

Status

(hours

online)

Pump

Efficiency

Belt

Losses

Motor

Efficiency

VFD

EfficiencyPower Consumption (Hp) Hp Hours per day

kWhrs per day per

unit

kWhrs per day (all

units)kW hrs / m3

Intermittent

Low Flow

Medium Flow

High Flow


per unitControl

Mixing Volume per Unit

(gallons)Plant Mode Status

Pump

Efficiency

Belt

Losses

Motor

Efficiency

VFD


kWhrs per day per

unit

kWhrs per day (all

units)kW hrs / m3

Intermittent

Low Flow

Medium Flow

High Flow


per unitControl



Pump

Efficiency

Belt

Losses

Motor

Efficiency

VFD


kWhrs per day per

unit

kWhrs per day (all

units)kW hrs / m3

Intermittent

Low Flow

Medium Flow

High Flow


per unitControl



Pump

Efficiency

Belt

Losses

Motor

Efficiency

VFD


kWhrs per day per

unit

kWhrs per day (all

units)kW hrs / m3

Intermittent

Low Flow

Medium Flow

High Flow


per unitControl Total Flow (GPM) Plant Mode Status

Pump

Efficiency

Belt

Losses

Motor

Efficiency

VFD


kWhrs per day per

unit

kWhrs per day (all

units)kW hrs / m3

2,792 Intermittent ON 0.55 0.00 1.00 1.00 25.50 132.58 49.43

2,792 Low Flow ON 0.55 0.00 1.00 1.00 25.50 262.61 97.91

2,792 Medium Flow ON 0.55 0.00 1.00 1.00 25.50 140.23 52.28

2,792 High Flow ON 0.55 0.00 1.00 1.00 25.50 76.49 28.52

l ( ) l k h d k h d ( ll

ON 8.42 43.78 16.32

OFF

ON 6.40N/A N/AN/A

0.00 0.00 0.00

N/A N/A

2

2

2

4.21

2Feed Forward Pump

Fine Screen 12.00

Anaerobic Basin Mixer

Pre Anoxic Mixer

0.25Constant Speed

41,965

46,162Pre‐Aeration Mixer

36 VFD

Constant Speed

2

1.65Constant Speed

4.21Constant Speed

1,201

21,065 59.06

4.4724

0.02

150.69 0.06

N/A 3.30 17.16

0.50 8.95 0.00N/A N/A N/AN/A

456.30 0.18

0.00 0.00N/A N/A N/A N/A

N/A N/A



Pump

Efficiency

Belt

Losses

Motor

Efficiency

VFD


kWhrs per day per

unit

kWhrs per day (all

units)kW hrs / m3

605 Intermittent ON 0.55 0.00 1.00 1.00 2.76 14.36 5.36

605 Low Flow ON 0.55 0.00 1.00 1.00 2.76 28.45 10.61

605 Medium Flow ON 0.55 0.00 1.00 1.00 2.76 15.19 5.66

605 High Flow ON 0.55 0.00 1.00 1.00 2.76 8.29 3.09



Pump

Efficiency

Belt

Losses

Motor

Efficiency

VFD


kWhrs per day per

unit

kWhrs per day (all

units)kW hrs / m3

0 Intermittent OFF 0.55 0.03 0.88 0.97 0.00 0.00 0.00

517 Low Flow OFF 0.55 0.03 0.88 0.97 0.00 0.00 0.00

775 Medium Flow OFF 0.52 0.03 0.88 0.97 0.00 0.00 0.00

1,034 High Flow OFF 0.50 0.03 0.88 0.97 0.00 0.00 0.00


per unitControl Total Flow (SCFM) Plant Mode Status

Aero

Efficiency

Belt

Losses

Motor

Efficiency

VFD


kWhrs per day per

unit

kWhrs per day (all

units)kW hrs / m3

283 Intermittent 100% 0.65 0.03 0.94 0.97 16.22 84.35 31.45

283 Low Flow 100% 0.65 0.03 0.94 0.97 16.22 167.08 62.30

283 Medium Flow 100% 0.65 0.03 0.94 0.97 16.22 89.22 33.26

283 High Flow 100% 0.65 0.03 0.94 0.97 16.22 48.66 18.14


per unitControl Total Flow (SCFM) Plant Mode Status

Aero

Efficiency

Belt

Losses

Motor

Efficiency

VFD


kWhrs per day per

unit

kWhrs per day (all

units)kW hrs / m3

523 Intermittent 0.16 0.64 0.03 0.89 0.97 28.53 23.74 8.85

636 Low Flow ON 0.65 0.03 0.92 0.97 33.04 340.27 126.87

748 Medium Flow ON 0.66 0.03 0.94 0.97 37.49 206.19 76.88

859 High Flow ON 0.66 0.03 0.94 0.97 43.01 129.03 48.11

Totals: 1536.2 0.606

2

50 VFD2MBR Blower

Pre‐Aeration Blower

2.8CAST IRON

20 VFD

2

Permeate Pump (PAG) 7.5Constant Speed

2

Bio‐P Recycle Pump

290.31 0.11

521.42 0.21

0.02

0.00 0.00

49.43

© Copyright 2010 GLV. All rights reserved. 010713-1-AK-R0 Power Estimate, Page 1

Operation and Maintenance CostMillbrook WWTP (AAF 0.67 MGD)

Parameter Value Notes

Number of Cartridges 4,800 cartridgesVolume of Chemical Needed per Cart. 1.35 gal/cartridge

Volume of Dilute Sodium Hypochlorite 6,480 gal Concentration of Dilute Solution 0.25% Concentration of Stock Solution 12.5%

Volume of Stock Solution of Sodium Hypochlorite 130 gal vol. per single plant cleanSodium Hypochlorite Buyout Cost $0.10/lb Assumed

Cleanings per Year 2 times/yr Total Annual Sodium Hypochlorite Chemical Cost $259 Specific Gravity: 1.2

Volume of Dilute Oxalic Acid 6,480 galConcentration of Dilute Solution 1%

Concentration of Stock Solution 100%

Volume of Stock Solution of Oxalic Acid 65 gal vol. per single plant cleanOxalic Acid Buyout Cost $0.71/lb Assumed

• Category 1: Annual Chemical Use Summary

O & M costs based on Average Annual Flow (AAF) are listed below, and have been broken down into four categories.

Table 1: Chemical Usage

Sodium Hypochlorite (Membrane CIP)

Oxalic Acid (Membrane CIP)

Cleanings per Year 2 times/yr

Total Annual Oxalic Acid Chemical Cost $1,266 Specific Gravity: 1.65

ALUM Design Mass Loading 30 gal/dayALUM storage capacity 1,800 galALUM Buyout Cost $0.06/lb Assumed

Total Annual ALUM Chemical Cost $6,575 (per Biowin)Specific Gravity: 1.2

Total Annual Chemical Cleaning Costs $8,100

Parameter Value Notes

Operator Hourly Wage 25 per hour Total Cleaning Man‐hours 24 hr/yr

Total Annual Labor Cost for Cleaning $600 /yr Estimated

Table 2: Membrane CIP Labor

• Category 2: Annual Labor Costs for Membrane Cleaning

ALUM (Phosphorus Removal)

© Copyright 2010 GLV. All rights reserved. 010713-1-AK-R0 O & M Cost, Page 1

Operation and Maintenance CostMillbrook WWTP (AAF 0.67 MGD)

Parameter Value (hr/yr) Notes

Blowers 25 (Oil & filter change) Influent Screens 6

Permeate Pumps 4 (Inspection/lube)

RAS Pumps 16 (Inspection/lube)

Instrumentation 20 (calibrate and/or clean) Sampling 25

Mixers 1.2 (replace seals)

Total Annual Labor Manhours 97.2 hr/yr hr/yr (membrane clean not included) Operator Hourly Wage 25 per hr

Total Annual Labor Cost for O&M $2,430 /yr Estimated

• Category 4: Membrane Replacement Cost

• Category 3: Annual Plant Operation and Maintenance Costs

Table 3: Plant Maintenance & Sampling Costs

No Replacement

20%/yr

No Replacement

0 10 15 20 25

• Years: 1 through 10No replacement.

• Years: 11 through 1520% replacement per year

* Replacement cost. Must add CPI.** Without redundant basin

• Years: 16 through 20 No replacement.

Estimated annual replacement cost = 0.2 X 4,800 cartridges X $65*/cartridge = $62,400/yr **

0 10 15 20 25

Membrane Life (Years)

© Copyright 2010 GLV. All rights reserved. 010713-1-AK-R0 O & M Cost, Page 2

DO NOT SCALE PRINTS

THIRD ANGLE PROJECTIONÉ

SHEETNO. OF

01/09/13

D

010713-1-AK

DLA

AK A11

SECTION A-A

AA

AX-01 PA-01

MB-02

MB-01

SB FC

SB

AX-01 PA-01 MB-01

FC

PA-02AX-02

AN-01

AN-02

AN-01

THIS DRAWING CONTAINS CONFIDENTIAL PROPRIETARY INFORMATION OF OVIVO, AND ITS AFFILIATES, AND IS NOT TO BE DISCLOSED NOR TO BE USED EXCEPT FOR EVALUATING PROPOSALS OF OVIVO OR INSTALLING, OPERATING OR MAINTAINING OVIVO EQUIPMENT. UNLESS OTHERWISE AUTHORIZED IN WRITING BY OVIVO. UNCONTROLLED COPY IF PRINTED

REV

©COPYRIGHT 2010 GLVALL RIGHTS RESERVED - REV E

WORKMANSHIP STANDARD WI-7501-01APPLIES

CHECK'D

DRAWN

DATE

AK

DLA

1/9/2013

010713-1-AK

ORIGINAL S.O.

DO NOT SCALE PRINTS

SHEET1 OF 1

DWG.NO.

MILLBROOK 0.67 MGD WWTPMILLBROOK, CANADA

RW-400 BASIN LAYOUT

D

AS-010713-1-AK

REF. FROM

THIRD ANGLE PROJECTION

Bringing water to life

(mm/dd/yy)

INITIAL RELEASE AREVISION DESCRIPTION EN/ECO BY CHECK'D DATE REV

21'-8

"21

'-8"

14'-0"16'-6"8'-0"

10'-0

"

4'-0"

16'-0

"

16'-0

"

(20'

-6")

(SE

E N

OTE

)

(68'-6") (SEE NOTE)

3'-0"

(1'-6") TYP.(SEE NOTE)

17'-6

" 19'-0

"

NOTE: 1. DIMENSION IS BASED ON WALL AND FLOOR THICKNESSES OF 1'-6" AND IS FOR REFERENCE, ONLY. ACTUAL DIMENSION OF WALLS AND FLOORS ARE THE RESPONSIBILITY OF THE ENGINEER AND NO ACCURACY OR RESPONSIBILITY FOR THE REFERENCE DIMENSIONS ARE TO BE INFERRED OR IMPLIED FROM THIS DRAWING.

(47'

-10"

) (S

EE N

OTE

)

17'-0"

18'-1

1"18

'-11"

17'-0

"

18'-0

"

How we create value

• Single-sourcesupplyforallequipment

• Experiencedtechnicalstafftohelpdeliverprojectsontime,onbudget

• Provenlowesttotalinstalled(project)cost

• Loweroperatingexpenses

• Innovativetechnologiesforsmallestfootprint,leastconcrete

• Onenumbertocall24/7forassistanceandtechnicalsupport

Keyfeatures&benefits

• Fullyintegrated,completesystemsfromheadworksthroughdisinfection

• KUBOTA®membranetechnology

• Membranethickening/digestionforbiosolidsmanagement

• EQLogix™integrationandcontrols

• EQuipTech™aftermarkettechnicalsupport

The Enviroquip® MBR SystemSubmergedMembraneBioreactor(MBR)technologyforwastewatertreatmentandreuse.

One System, Many Solutions…

www.ovivowater.com©Copyright2011GLV.Allrightsreserved

2 www.ovivowater.com©Copyright2011GLV.Allrightsreserved

Why MBR? Putsimply,MBRsystemsarethebestavailabletechnologyforwastewatertreatmentandreuseapplications.Properlydesignedandoperated,anMBRfacilitycanmeetthemoststringentnutrientlimitsandproducethehighestqualityeffluentrequiredforanyreclamationproject.Themostreliable,themostspaceefficientandthemostcosteffectivesolutionsuseMBRtechnology.

Module Cassette MBR

Water feature using recycled water in Tulalip, WA (Commissioned 2002)

What is an MBR?AnMBRcanbestbedescribedasonepartofabiologicalprocesswheresmallmicrobesdegradepollutantsbeforebeingfilteredbyacollectionofsubmergedmembranes.Membranesarehousedinmodulesthatare,inturn,assembledintocassettesandinstalledinatank(calledanMBR).Airintroducedthroughintegraldiffusersscoursmembranesurfacesduringfiltration,mixesthetankandprovidesoxygentothebiologicalprocess.

Permeate Quality

Parameters Typical Achievable Values Values

BOD5 <2.0 mg/l Non-Detect

TSS <2.0 mg/l Non-Detect

Ammonia (NH3) <1.0 mg/l Non-Detect

Total Nitrogen (TN) <10.0 mg/l <3.0 mg/l

Phosphorus (TP) <1.0 mg/l <0.03 mg/l

Turbidity <0.10 NTU <0.05 NTU

Fecal Coliform <2.2 CFU/100ml Non-Detect

SDI <3 <2

“ReliableSpaceEfficientCostEffective

”

3

What is an MBR System? An MBR system is a complete, integrated set of components that allows a process to function. Assumingthe same reuse quality effluent and similar solids management goals, an Enviroquip® MBR system canbe 50% less complicated than a comparable conventional wastewater treatment plant and require lessthan25%ofthefootprint(landarea).

“1/2thecomplexity1/4thefootprint

”

Equivalent Enviroquip® MBR System

Conventional Treatment Producing ReuseEffluent and Stabilized Biosolids

MBR

MBT PAD®-K


MBR technology has been succesfully used for thetreatment of municipal, commercial and industrialwastewatersfordischargeandreusesincethe1980s.With thousands of installations operating worldwide,MBR technology has reshaped the way we viewwastewatertreatmentandwaterconservationacrossthe globe. Since our first US installation in BandonDunes,Oregonmorethan10yearsago,OvivoUSA,LLChasbecometheindustryleaderforcompleteMBRsystems.

An ISO 9001 certified company, our diverse,experiencedtechnicalteamcandesignandsupplyarangeofofferingsfromsimplemembraneequipmentpackages to complete, ready-to-operate, systems.StartingwithheadworksdesignedspecificallyforMBRapplicationsandendingwithprovenmembrane-basedsolids management, each Ovivo plant is a unique,tailoredsolution.

Inadditiontosingle-sourceresponsibility(SSR),Ovivooffersourclientsthefollowing:

Better Project Delivery

More Experience

KUBOTA® Membrane Technology

The Best Technical Support

Proven Cost-Control Strategies

Industry Leading Innovation

Enviroquip® MBR Systems by Ovivo

4

4

4

4

4

4

4

4

4

M Headworks

M Pumps

M Mixers

M Membranes

M Blowers

M Fine bubble

M Controls

M Technical support

M Waste solids

treatment

Commissioned in 2001, the first Enviroquip® MBR System (Bandon Dunes, OR)

5

Project Delivery Capabilities

In terms of project delivery and support, our experienced technicians, award-winning (ACAD) designers,programmers,engineersandprojectmanagerscansupportclientsfromconceptthroughthelifeoftheplant.Inaddition,Ovivocanfabricate,assembleandfactorytestequipmentatour42,000ft2shopnearAustin,Texasprior toshipment,savingtimeandmoney. Successfullyexecutedprojectsrangeinsizefrom5,000gallonsperday (GPD)upto6.0milliongallonsperday (MGD). Amongthe275projects insomestageofdesign,constructionoroperation,aresystemsranginginsizeuptonearly50MGD.

Illahee State Park, WA (5,000 GPD)The 3D (Inventor) model below was used to support engineering documentation and forfabrication.ThisprojectwasoneoffiveawardedtoOvivoaspartofasinglecontract.Fourofthefivefacilitiesarenowinservice..

3D Model by Ovivo Factory Assembled Skid by Ovivo

Union Rome, OH (3.0 MGD)Ourstaffsupportedtheengineerandcontractorbydevelopingdetailed3Dmodels,providinghydraulicandprocessmodeling(PipeFloandBioWin)anddevelopingtheSCADAsystem.

3D Model by Ovivo Contractor Installed Parts by Ovivo


ExperienceAsacompany,Ovivohasover330MBRsinoperationworldwideand180MBR/MBTinstallationsintheUS.Manyprojectswere upgradesorexpansionsofoldplants.More commonthaninyearspast,agingfacilitiesare beingrehabilitatedtomeetneworimpendingnutrientlimits.Someofthecasestudiesbelowillustratehowcosteffectiveplantsroutinelymeettightnitrogenlimitsacrossarangeofclimates.

Coppermine, GA

Installation Type NewConstruction

Commissioned 2009

Rated Capacity 1.0MGD(Builtfor6.0MGD)

Total Phosphorus (TP) Limit 0.13mg/l

Actual Effluent TP 0.08mg/l

Number of Violations 0

Climate Warm/ColdWeather

Solids Management Centrifuge+Landfill

Total Project Cost $13.1M

Rio Del Oro, NM

Installation Type CASUpgrade+Expansion

Commissioned 2006

Rated Capacity (GPD) 0.2MGD(Phase2:0.4MGD)

TN Limit 10.0mg/l

Actual Effluent TN <6.0mg/l


Climate Warm/ColdWeather

Solids Management Reducedhaulingby50%

Total Project Cost $1.3M(Phase2:$0.7M)

Upper Wallkill, NJ

Installation Type NewConstruction

Commissioned 2009

Rated Capacity 0.27MGD

TN Limit <7.0mg/l

Actual Effluent TN <3.0mg/l


Climate ColdWeather

Solids Management ScalpingPlant


Dover, OH

Installation Type DitchUpgrade+Expansion

Commissioned 2008

Rated Capacity 3.0MGD

Ammonia Limit <1.0mg/l(Summer)

Actual Effluent Ammonia <1.0mg/l


Climate ColdWeather

Solids Management PAD-K™(UsingMembranes)


< 0.13 TP

< 3 TN

7

The Most Reliable Membrane TechnologyTheOvivoandKUBOTApartnershipgoesbackmorethanadecadeintheUnitedStatesandlongerthroughourUKoffices.Inresponsetomarketdemandsformoreenergyandspaceefficienttechnology,severalinnovationshavehelpedtoreducedenergydemandby70%andimprovespaceefficiencyby50% sinceearly2001.Despitetheseimprovements,themembranematerialhasnotchangedinover20yearsandisusedinmoreinstallationsaroundtheworld(>3,500)thanallofthecompetitioncombined.Moreimportantthana reference list,KUBOTAhasdemonstratedanunwaveringcommitment toOvivo,ourclientsandtoMBRtechnology.

The Best Technical SupportOvivoofferstailoredaftermarkettechnicalsupportandservicethroughourEQuipTech™program.Planscaninclude,butarenotlimitedto:

• 24/7phoneorweb-basedSupport

• Anetworkofcertifiedtechnicalsupportandservicecenters

• Plantaudits(EQIDEASSM)includingenergy,chemicalsandlabor

• Classroomrefreshertraining

• Arangeofguarantiesfrombasicworkmanshiptolong-termmembrane andprocessperformance

“Installed in more MBR systems than any other membrane technology.”

“The most durable, proven membrane technology available for MBR.”

®

Plant Audits (EQIDEAS™)

Classroom Training Sessions


Proven Cost-Control StrategiesAtOvivo,weprovideourclientsrealstrategiestocontrol totalprojectcoststhatgobeyondmembranetanksandequipment.Ourexperienceresideswithourstaffandincomprehensive,readilyaccessibleDesignGuidelines developed through real, MBR experience. With each newproject, our clients get the benefit of hundreds of installations andthousandsofman-hoursinthefieldworkingwithMBRplantoperators.SomeofthemethodsbywhichOvivocanhelpcontrolinstallationcostsascomparedtoothersuppliersinclude:

“Ovivo is innovating

at the System level to

make the best available

technology more accessible, easier to

operate and truly

sustainable.”

• Speciallydesignedheadworks

Smallerprocessvolumes(concentratedoxygenoptions)

• Simplifiedmechanicalpipingandelectricaldesign

Patentedstrategiesforrepurposingofflineequipment

• No(orminimal)chemicalstorage

Proven,repeatableEQLogix™automation

• OptimizedClean-In-Place(CIP)designs

Mostefficientmixingandaerationtechnologies

• Integratedsolidstreatmentoptions(MBTorPAD®-K)

Stormflowmanagementoptions

OvivoPiping CompetitorPiping

OvivoCIPSystem CompetitorCIP System

Process Solids Solids Required Concrete/ Concentration Wasting Process Space Rate Volume Savings

Unthickened 1.0% 76,882 gpd 2,149,000 gal 0%

PAD®-K 3.0% 25,361 gpd 520,040 gal 76%

PAD®-K

9

Innovation Over the lastdecade,Ovivohasspentmillionsofdollarsonresearchandde-velopment to advance every facet ofMBR system technology. Some exam-plesincludeEQProSimSM(dynamicsim-ulator), ourRapidRecoveryUnit (RRU) and most recently, BLOXTM (advancedMBRsolutions).Thelistgoesonandsodoesourcommitment.

BetterEnergyEfficiencyOvivo has developed numer-ousenergysaving technologies,toolsandstrategies.Oneexam-ple is the EQProSimSM dynamicsimulator that gives operatorskeyfeedbackonspecificwaystoimproveenergyefficiency.

ReducedRiskEvery submerged membranetechnologyissusceptibletowhatiscalledlocalizeddewateringasaresultofimproperoperationorextremesystemupsets.Ovivoistheonlycompanytohavedevel-oped a deployable technology(theRRU)toefficientlyandsafelyrecoverfromthistypeofevent.

SustainabilityIn addition to our core technol-ogy,OvivooffersvariousBLOX™ systems that intensify biologicalprocesses and efficiently man-ageshort-termstormfloweventsmaking plants smaller, less ex-pensive, easier to operate andmoresustainable.Dependingonthe project, BLOX systems canrequire 80% less concrete and50% fewer electrical compo-nentsthanalternativesystems. “80% less concrete

than conventionalprocesses.”

“50% less rotatingequipment and

electrical components.”


Why Ovivo? While there are many membrane suppliers in theglobal market today, Ovivo is the industry leaderfor MBR systems. Our ability to support projectsfrom concept through end of life separates ourcompanyfromagrowinglistofcommoditysuppliers.Moreover, our technology portfolio enables us toprovidethebestsolutionforeachuniqueapplication.Our network of certified contractors and technicalsales representativescomplementourstaffofover100professionalsdedicated toservicing theMBRmarket.

Best Value & Lowest Total Installed CostOvivo understands how to effectively work withdelivery teams to control costs and bring projectsinontimewithoutsacrificingvalue.Acrossarangeof flows and operating conditions, MBR systemscost significantly less to build, despite the highperformanceandpremiumcomponents.

Best Value

Lowest Total Cost

Lower Operating Cost

Reliable Performance

25% – 54%Lower Total

Installed Cost

Tota

l Pro

ject

Co

st

Ovivo is

25%Less Expensive

Ovivo is

54%Less Expensive

0.5 - 1.0 1.0 - 2.0 2.0 - 3.0 3.0 - 6.0

Ovivo is

25%Less Expensive

Ovivo is

47%Less Expensive

Rated Plant Capacity (MGD)

Other

11

Animportant,oftenoverlooked,componentofowner-shipcostislabor.Dependingonmanyfactorsinclud-ing the sizeof a facility, labor canaccount formorethanhalf of anoperatingbudget. Industry data sug-geststhatEnviroquipMBRsystemsrequire50%lesslabor to run thanalternativeoptions. The reason forthe stark contrast is not a simple function of mem-braneequipment,butreflectstheOvivophilosophyofrobust,efficientMBRsystemdesign.

Aslessthan5%ofoperationalissuesarecausedbymembrane equipment, the key to reliable operationis generally a healthy biological process, goodhydraulics,reliableancillarycomponents/subsystemsandsoundautomation.

Ovivo has a large portfolio of heritage brands todraw from in addition to strategic agreements witharangeofequipmentvendorstobringtheverybesttoeachproject.EverycomponentissizedtoexactlymeettheneedsofaprojectandiscontrolledbyanEQLogix™ supervisory control and data acquisition(SCADA)system.

50%Less Labor

Lower Operating Costs & Reliable Performance

“With Ovivo, operators have just 1 number to call for

technical support 24/7”

AncillaryEquipment

95%

Membrane5%

Full Time Employee (FTE) PER MGD

“OurEnviroquip®MBRSystemhasbeen inservice foroversixyearsand recently handled flows up to12MGDwithoutaproblem.”

ToddTeman,SuperintendentDelphos,OH(2011)

15

10

5

0

Other

FTE

/MG

D

Max.FTE/MGD

Avg.FTE/MGD

Min.FTE/MGDOvivo

Comparison data taken from a survey of 29 MBR facilities ranging in capacity from 0.5 MGD to 6.0 MGD.

www.ovivowater.com

©Copyright2011GLV.Allrightsreserved

For the right MBR System,just follow the numbers…

330

275180100 54 50 10 3

1

OvivoMBRplantsoperatingworldwide

EnviroquipMBRsystemsindesign,underconstructionorinoperation

MBRsandMBTsoperatinginNorthAmerica

Dedicated,trainedMBRstaff

Percentlessexpensivetobuild

Percentlesslabortooperate

Yearsofdemonstrated, reliablesystemperformance

Proventotalnitrogenlimitin differentclimates

Systemguaranteeandnumberto callforsupport24/7.

microBLOX™ready-to-operate,

deployabletechnology

STORMBLOX™peakflowsandstorm

flowmanagement

ECOBLOX™spaceefficient,cost

effectivedesign

FormoreinformationonourBLOX™technologies,pleaseseethesebrochures:

KubotaisaregisteredtrademarkoftheKubotaCorporation



CFIC® Moving Bed Bioreactor

Biowater Technology US LLC

Biowater Technology US LLC 2155 Diamond Hill RoadSuite 2, Mailbox 4Cumberland, RI 02864

Ph: +1 401-305-3622Fax: +1 [email protected]

January 13, 2013

Re: Biowater Conceptual Design and Budget Estimates (CFIC® Process)

Dear Albert,

Biowater Technology (Biowater) is a supplier with process engineers holding over 40 years of experience in biofilm processes. Our engineers were involved in the development of the moving bed biofilm (MBBR) process and have since patented advancements to the MBBR. Our CVs and partial installations list are attached hereto.

Biowater provides this design summary and budgetary estimate for retrofitting the Millbrook WWTP in Millbrook Ontario, Canada with a new CFIC® biofilm process while repurposing existing tankage.

I. Proposed Biofilm Process

The Continuous Flow Intermittent Cleaning (CFIC®) process has continuous inflow to the reactor and intermittent (forward flow) cleaning or wasting of captured biological solids. The CFIC® biofilm process contains highly packed biofilm carriers to a degree that little movement of the carriers occurs (typically 90-99% bulk volumetric fill). The packed nature of the bed allows for continuous biological treatment by the biofilm with solids capture from the packing factor. There are two modes of operation: normal and wasting, which are depicted in Figure 1. During normal mode, CFIC® effluent flows to the downstream clarification or tertiary filtration step. During wasting mode, the water level in the reactor is elevated allowing free movement of the carriers facilitating collisions and sloughing of excess biomass and accumulated solids, and the sloughed biomass may be directed to primary clarifiers, gravity settling, or waste sludge storage basins.

Microorganisms colonize the carrier surface creating a biofilm that oxidizes organics, ammonia and degradable organic nitrogen. The packed bed creates high carbon and nutrient gradients as well as increased oxygen transfer efficiency , as the vertical pathway of the air is significantly increased creating long retention.

Figure 1. CFIC®general depiction of operational modes

II. Biological Design Considerations

The existing basins will remain online during construction of the new CFIC® process basins. The CFIC® process will be constructed as two (2) process trains of three (3) reactors operated in series. Raw wastewater must be screened to 6mm or less, preferably to 3mm. CFIC® effluent will flow to the existing secondary gravity clarifier in which the stream will be chemically treated (flocculated) for phosphorus precipitation and setting of solids before flowing to a DynaSand filter (DSF). The DSF will polish phosphorous removal to meet the effluent requirement of 0.1 mg/L and will provide effluent filtration of solids, meeting 5mg/L BOD and TSS. The design criteria for the CFIC® process follows:

Parameter CFIC® Influent CFIC® Effluent DSF Effluent

Design Flow 2,520 m3/d(peak 343 m3/hr.)

BOD5 190 mg/L (479 kg/d) < 5 mg/L sBOD < 5 mg/L

TSS 210 mg/L (529 kg/d) 40 mg/L (Normal Operation) < 5 mg/L

TKN 25 mg/L (63 kg/d)

TP 5 mg/L (13 kg/d) < 0.1 mg/L

NH3 <2 mg/L Winter (8°C)< 1 mg/L Summer (15°C)

Design Temperature 8°C (Winter) & 15°C (Summer)20°C (Maximum Aeration

Design)

III. Summary of Biological Design Criteria

After completion of CFIC® construction and startup, we recommend that the existing aeration basin be used for flow equalization during wet weather conditions, as the peaking factor is approximately 3.25:1. The aeration basin will provide approximately 2.5 hours of HRT during peak events.

The existing sludge storage basin (1,148m3) will receive CFIC® waste solids. We recommend the sludge storage basin be equipped with aeration and liquid/solids decanting capabilities. Decanted liquid from the sludge storage basin may be pumped to the EQ tank and fed directly back to the CFIC® process or to the downstream secondary clarifier. The existing aerobic digester (163m3) will continue to operate as such.

The CFIC® wasting cycle is expected to have a frequency of 1-2 cycles per day with 1-2 hour duration for each cycle. The volume and solids content of each wasting cycle is expected to be:

Volume: 105 – 210 m3 per cycle with 1 – 2 cycles per day (105-420 m3/d) Waste Solids (directed to sludge storage): 287 kg/d [TSS] in waste solids: (700 – 2,750 mg/L)

The CFIC® process basin dimensions and operational requirements are provided in the summary table below.

Design Parameter Operational Considerations

Number of Process Trains 2

Number of Aerobic Basins in Series 3

Biological Process Configuration Continuous Flow Intermittent Cleaning (CFIC®)

Biofilm Carrier Type BWT-S

Biofilm Specific Surface Area, m2/m3 628

Design Side Water Depth CFIC® or Normal Mode 4m / Wasting Mode 5m

Recommended Freeboard CFIC® or Normal Mode 2m / Wasting Mode 1m

CFIC® Basin Dimensions, each 4.75m W by 4.75m L

Required fixed film surface area, m2 312,394

Blower Airflow Requirements 553 scfm @ 6.75 psig 20.5 BHP in Normal Mode 565 scfm@ 8.17 psig 25 BHP in Wasting Mode

Estimated CFIC® Reactor Effluent TSS, mg/L 40 mg/L to secondary clarifier during Normal Mode700-2,750 mg/L to sludge storage during Wasting Mode

IV. Scope of Supply

Biowater’s scope of supply includes process design, controls and instrumentation, and CFIC® process basin internals as listed below and depicted in Figure 2.

Figure 2. 3D Cutaway CFIC® Internals [Normal Mode (l) and Wasting Mode (r)]Pipes and Valves Typ. Industrial Installations

Channels and Gates Typ. Municipal installations BWT-S biofilm carriers will be provided with specific surface area and total fixed film area given above, specific to design

criteria as stated above. The BWT-S specification document is attached hereto.

A complete site specific, engineered diffused aeration system will be provided in 304L stainless steel including header and lateral piping for each aerobic reactor. All supports for the aeration grid systems, manifolds and drop pipes internal to the basins will be supplied. The termination point for the aeration system drop pipe will be a flanged connection at the tank wall height. Materials of construction are schedule 5 and Schedule 10 304L Stainless Steel piping. All flanges will be 150 lb. ANSI style.

Biofilm carrier retention sieve assemblies will be provided for each reactor containing biofilm carriers. Sieve assemblies will be designed at a peak instantaneous flow plus recycle streams, when applicable. Sieve assemblies will be of 304L stainless steel construction. Normal, wasting, and drain assemblies will be supplied.

Controls and Instrumentation are included herein. Operating level will be controlled in the two modes of operation either by automated valve or by actuated gate, either included herein.

On-site startup support, submittals and operations and maintenance manuals are included.

Also included are:

o Process Engineering consisting of aeration system sizing and configuration, sieve and outlet design. o P&I Diagram for the biological treatment process. o Preliminary General Arrangement Drawings and review and approval of final General Arrangement Drawings for

the biological treatment process. o Review of biological process drawings with respect to nozzles, penetrations and dimensions, excluding structural

design. o Functional specification for pumps, blowers, and ancillary equipment related to the biological treatment process.

V. Notes and clarifications

Unloading, storage and installation of equipment is by others.

All civil/site, rigging, electrical work, interconnecting piping, and startup to be provided by others.

Tanks for housing the multi-stage process internals will be required and are NOT included herein. Our design is based upon concrete, shared wall construction.

Blowers will be required to supply the reactors with airflows given above and are NOT included herein.

Tertiary filtration will be required and is NOT included herein. We recommend the DynaSand filter (DSF) for polishing solids and phosphorous.

Duties and taxes are not included herein.

Subject to Biowater Technology’s standard terms and conditions.

The budgetary estimate for this proposed scope of supply is $804,000 USD FOB Factory with Freight Allowed to Millbrook, ON. This estimate is budgetary and subject to change. Firm pricing can be provided upon request. We look forward to working with you on this project. Please feel free to contact us at 401-305-3622 or via email at [email protected] if you have any questions or concerns.

Best regards,

Joshua HanlonSales Director

Attachments: BWT-S Biofilm Carrier SpecificationBiowater Installations ListBiowater CVs


BioWater reserves the right to change the specification without any further notice.

Page 1 of 1

BioWater™ Biofilm carrier HS Code 8421.99.00

Product Name: BWT S™ Prepared by: TA Approved by: TA Trade mark/design registration

Rev.no: 001 Date: 27.06.2011

Application:

The BWT S™ biofilm carrier element is used in biological treatment processes for both water- and wastewater treatment plants.

Design:

The BWT S™ elements consists of 9 cells is angled and have the following dimensions;.

Material:

Polyethylene, high density (HDPE). Colour: Natural The raw material has a specific weight of 0,96 (± 0,02) kg/ltr, while the material after extruding has a specific weight of about 0,95 (± 0,02) kg/ltr. Add-Max® 104 is added to the material to improve stabilization for the extruding process. The biofilm carrier elements are produced from a material and with a procedure that ensures that the material will have a long aging time giving a proper operation for its service life, provided: - stored and packed as from the producer - applied in the reactors according to normal procedures The shape of the biomedia might be in some cases uneven, this has no negative effect on the total surface area guaranteed.

Main data:

The weight of the BWT S™ is : 131kg/m³ (in bulk, at production) Efficient surface : 4,80 m2/kg Content of a big bag : Dependent on the preferred bag size Protected surface area pr. bag : 628 m2 pr. m3 in bag (randomly packed)

Quality

assurance

The producer is instructed to take visual inspections/regular tests to control form, dimensions and density (kg/m³ in bulk), in order to ensure conformity to the specification.

Width/hight : 15 mm (±0,5mm) Length : 9 mm (+0,2/-0,5mm) Perimeter outside : 56 mm Perimeter inside : 197 mm Tolerances according to : DIN 16941/3 Wall thicknesses : 0,35 mm (±0,1mm)

Page 1 of 2 Revised: 01/09/2013

cmf

Reference List Project Company Installation

Type Year Country Technology Hydraulic

Capacity, m3/h (MGD)

BOD, mg/L Media Type/ Quantity m3

Vike RA Hof Kommune Municipal/ Upgrade 2009 Norway CMFF® 70 (0.44) 182 --/--

Kimberly Clark Haztec Pulp, Paper/ Upgrade 2009 Brazil CMFF®(MBBR) 200 (1.26) 600 BWT35/10

Standard Process

Environmental Health

Foods/ Upgrade 2009 USA CFAS® 32 (0.20) 1,500 BWT-X/35

Trysil RA Municipality of Trysil

Municipal/ New 2010 Norway CFAS®/

Flotation 1065 (6.75) 2,250 BWT-X/252

Vigor, Sao Paulo Acqua Engenharia Dairy/ Upgrade 2010 Brazil CMFF®(MBBR) 50 (0.32) 1,800 BWT35/246

Harestua RA Municipality of Lunnar

Municipal/ Upgrade 2011 Norway

CFAS®/ Flotation (turnkey)

80 (0.51) 190 BWT-X/58

Elverom RA Norde Land Municipality

Municipal/ Upgrade 2011 Norway CMFF®(MBBR) 95 (0.60) 150 BWT-X/8

Medite Evergreen Engineering

Pulp, Paper/ Upgrade 2011 Ireland CMFF®(MBBR) 50 (0.32) 2,000 BWT-X/143

Pachuca STP Iberaltec Municipal/ Upgrade 2011 Mexico CFAS® 360 (2.28) 350 BWT15/390

Sintek Eco Digital Electronics/ Upgrade 2011 Taiwan CMFF®(MBBR) 62 400 BWT35/380

Nordfjord Kjott Nordfjord Kjott Foods/ Upgrade 2011 Norway

CMFF®(MBBR)/Chemical

Precipitation 24 (0.15) 1,850 BWT-X/57

Arengau WWTP JS Umwelttechnik Municipal/ Upgrade 2012 Switzerland CFAS® 84 194 BWT15/84

Page 2 of 2 Revised: 01/09/2013

cmf

Project Company Installation Type

Year Country Technology Hydraulic Capacity, m3/h

(MGD)

BOD, mg/L Media Type/ Quantity m3

Roros RA Roros Kommune Municipal/ Upgrade 2012 Norway CMFF® 200 186 BWTX/115

Flums JS Umwelttechnik Municipal/ Upgrade 2012 Switzerland CFAS® -- -- BWT15/150

Wetico Weitco Industrial/ New 2012 Saudi

Arabia CMFF® 84 250 BWTX/232

Kan PaK Kan Pak Foods/ New 2012 USA CMFF® 41

(0.029) 2880 BWTX/300

Schofteland JS Umwelttechnik Municipal/ Upgrade 2012 Switzerland CFAS® 167 168 BWT15/205

Bloomingdale Fleis & Vanderbrink Eng.

Municipal/ Upgrade

Under Construction

2013 USA CMFF® 19

(.121) 575 BWTX/129

Barlidalen Municipal/ Upgrade 2012 Norway CMFF® 850 120 BWTX

Saignelegier JS Umwelttechnik Municipal/ Upgrade 2012 Switzerland CMFF® 60 233 BWT15/193

Langmatt JS Umwelttechnik Municipal/ Upgrade 2012 Switzerland CFAS® 1196 91 BWT15/496

Tek Coal H2Flow Mining/ New

Under Construction

2013 Canada CMFF® 329

(2.09) 40 BWTX/141

Johanna Foods Johanna Foods Foods/ Upgrade

Under Construction

2013 USA CFIC® 63

(.40) 4500 BWTX/561

Hyflux Hyflux Industrial/ Upgrade 2012 Singapore CFIC® 47 600 BWTS/168

RPM H2Flow Plastics Recycling

Under Construction

2012 Canada CMFF® 8.33

(0.05) 737 BWTX/9

Wickford Village Ricci Drain- Laying Co., Inc.

Municipal/ New

Under Construction

2013 USA CFAS® .016

(2.54) 12 BWTX/9

www.biowatertechnology.com www.biowatertechnology.com

product sheet

CFIC® BIoFIlm ProCessContInuous Flow IntermIttent CleanIng

Bioreactor being filled with media.

the Next GeNeratioN iN Biofilm techNoloGy

the cfic®, complete mix fixed film system, is the next generation of biofilm technology. it has all of the benefits of a traditional biofilm process with moving carriers but has many additional benefits.

aBout fixed film techNoloGy

the basis of our cfic® biofilm technology is the biological growth on polyethylene pieces called media or carriers. these surfaces provide a protective surface area for the biology to grow. the biofilms can handle extremely high loading conditions without any problems with clogging or shock.

the cfic reactor contains highly packed biofilm carriers (typically 90-99% bulk volumetric fill) that hinders movement of the carriers that normally occurs in an mBBr reactor.

the cfic® process is designed to increase treatment capacity while reducing footprint and overall energy costs.

Benefits CFIC®:

Energy Savings20-40% Less Than MBBR

FlexibleUpgrade an Existing BAF, MBBR, MBR

Performance & Footprint 20-40% Less Than MBBR

Makes Solids Handling Less Complicated

www.biowatertechnology.com www.biowatertechnology.com

product sheet

headquartersBiowater technology asrambergvn. 5, 3115 tonsberg, Norway

phone: +47 911 10 600email: [email protected]

Biowater Technology is an innovative company with over forty years of experience in the Biological treatment field. Our focus is on saving energy and resource recovery, with wastewater as our major resource.

Biowater usaBiowater technology us llc2155 diamond hill rd, suite 2, cumberland, ri 02864

phone: +1 401-305-3622email: [email protected]

BeNefits

• energy savings - substantial reduction in energy consumption - up to 20-30%!

• reuse - recycling of water and wastewater for reuse. • effluent quality - superb effluent quality. • low capital costs - reduction in capital costs by reducing the size of the membrane or tertiary treatment.

• flexible - upgrade an existing sBr, mBr or mBBr to provide additional capacity.

• performance - improves biological treatment which makes membranes perform more efficiently.

Influent

Was

h w

ater

Con

cent

rate

Wash water treatment

Sludge liquor

Effluent

MF or UF membranes

CFIC® biofilm reactors

Primary treatment

Primary sludge

Biological sludge

complete system supply

we offer systems complete with biofilm carriers, aeration, retention sieves, mixing tanks as well as any tertiary treatment or additional equipment to suit the design.

services

Biowater technology will guide you through the process from start to finish:

• upgrade existing plants • Greenfield plants • training/education

CFIC® reactor contains highly packed biofilm carriers to a degree (typically 90-99% bulk volumetric fill) that little movement of the carriers occurs in the reactor during normal operation.

Products from Biowater:

CMFF - Complete Mix Fixed FilmCFAS - Combined Fixed Film Activated SludgeCFIC - Continuous Flow Intermittent CleaningPackage Plants

• consulting • pilot testing • Budgetary planning • energy analysis



Meteor® Moving Bed Bioreactor

Infilco Degremont Inc.

METEOR® IFAS BOD & Ammonia Reduction Preliminary Design Proposal PROJECT: 50136737.01

Project: Millbrook WWTP – Ontario, CanadaPrepared For: R.V. Anderson Associates Limited

Date: 1-15-13

INFILCO DEGREMONT INC. 8007 DISCOVERY DRIVE, RICHMOND, VA 23229 USA P.O. BOX 71390, RICHMOND, VA 23255-1390 USA TEL 804 756-7600 | FAX 804 756-7643

January 15, 2013 Re: Millbrook, Cavan Monaghan Township – Ontario, Canada METEOR® IFAS System Inquiry No: 50136737.01 Dear Valera, With regard to your recent request, Infilco Degremont (IDI) is pleased to submit an alternative proposal for a METEOR® Integrated Fixed Film System (IFAS) system. Specifically, the proposed design is composed of a Single Stage IFAS BOD & Ammonia Reduction System.

The scope of supply includes: biofilm carriers, carrier retention screens, instrumentation, and an aeration grid for the METEOR® IFAS system. Our design is based on the information provided by R.V. Anderson Associates Limited.

We have endeavored to provide complete information in this proposal. However, if you have any questions or need additional information, please feel free to contact our Biological Systems Manager, Amit Kaldate or me directly. Sincerely,

Lee Stewart Applications Engineer - Biological Systems Group

TABLE OF CONTENTS 1 APPLICATION ................................................................................................... 4 1.1 Project Background......................................................................................... 4 1.2 Process Design Basis ..................................................................................... 4 2 TREATMENT APPROACH ................................................................................ 5 2.1 METEOR® DESIGN ....................................................................................... 6 2.2 Design Analysis .............................................................................................. 7 2.3 Aeration System ............................................................................................. 8 2.4 NUTRICELLTMDTi Biofilm carriers ..................................................................... 9 2.5 Carrier Retaining Screens ............................................................................. 10 3 SCOPE ............................................................................................................. 11 3.1 Scope of Supply ............................................................................................ 11 3.2 Items by Others ............................................................................................ 12 3.3 Additional Items by Installing Contractor ....................................................... 13 4 BUDGET PRICE .............................................................................................. 15

IDI METEOR System

Millbrook WWTP 4 January 15, 2013 Proposal No. – 50136737.01

1 Application

1.1 Project Background

The Millbrook WWTP in Ontario Canada is in the process of evaluating technologies for BOD & Ammonia Removal. An Integrated Fixed Film System (IFAS) process is attractive to the client as it allows for the removal of pollutants in a compact footprint. The objective of our proposed design is to treat the influent flow listed below in Table 1 and achieve the required effluent BOD & Ammonia level required. 1.2 Process Design Basis

The following design is specifically for a Single Stage BOD & Ammonia Reduction IFAS system. Table 1 summarizes the flow and water quality parameters used for the proposed design.

Table 1. Design Parameters for Millbrook WWTP

Treatment Parameter Influent Desired Effluent

Design Flow, MGD 0.67 -

Design Temperature, oC 10 -

BOD, mg/l (Assumed) 190 5

TKN, Total Kjeldahl Nitrogen 25 -

NH4, Ammonia - 1

IDI METEOR System


2 Treatment Approach

The proposed biological process is a METEOR® IFAS Single Stage BOD & Ammonia Reduction system, which is an Integrated Fixed Film System (IFAS). This design consists of NUTRICELL™DTI biofilm carriers, carrier retaining screens and an aeration system. This process employs proprietary mobile biomass carriers (NUTRICELL™DTI) to support a very high concentration of attached biomass. The neutrally buoyant HDPE NUTRICELL™DTI biofilm carriers within the bioreactor tank provide a stable base for the growth of a diverse community of micro-organisms. The attached growth biofilm carriers have a very high surface-to-volume ratio, allowing for a high concentration of biological organisms to thrive within the internally protected areas. The detached biomass from the biofilm carriers will remain suspended within the Fluidized Fixed Film reactor, and is continuously removed from the process by the existing flow stream, resulting in an operator free biological system.

METEOR® Process Advantages:

Increased Nitrification - via biofilm retention in basin. Micro-organisms on the biofilm carriers have extended retention time and proliferate resulting in consistently low effluent Total Nitrogen

Improved Process Stability - during peak flow conditions resulting from retention of biomass in treatment basin

NUTRICELL™DTI - biofilm carriers were specifically designed for hybrid applications allowing large screen openings and biofilm carrier apertures. Local production in the US minimizes shipping, duties and installation time.

Field Proven at Full Scale – These systems have recently been selected for similar plants such as Moorhead, MN, the Region of Peel (Canada), City of Raisio (Finland), Groton, CT, Falling Creek, VA and Proctor’s Creek, VA, East Providence WWTP, RI and has been evaluated using full-scale testing at the Waterdown WWTP.

Upgrade Within Existing Basin - Enables the upgrade of conventional activated sludge plants without additional real estate.

IDI METEOR System


Conventional activated sludge processes may experience inconsistent Nitrification and denitrification at low Solids Retention Times (SRT) due to fluctuations in flow and operation. The biomass retention offered by biofilm carriers maintains a stable population of autotrophic bacteria, despite flow variation that would otherwise cause washout. The fixed film nature of NUTRICELL™DTI prevents washout, and provides a larger biomass population, resulting in a consistent effluent at lower suspended solids SRTs. Biomass retention on the carriers enables a much lower solids load downstream, as the biofilm is retained in the aeration basin. The biofilm thickness and mass is self-regulating, responding to both high and low influent mass loadings.

2.1 METEOR® DESIGN

The system for the Millbrook WWTP has been designed using proprietary models to perform process selection and determine the optimal biofilm carrier fill fraction and other operating parameters. An extensive analysis of design revealed that a Single Stage METEOR® (IFAS Biofilm Carrier process) would be suitable for the upgrade, as it is capable of achieving the desired effluent BOD & Ammonia levels. The proposed process consists of the following design: Design

1. The overall basin design will consist of an 881.1 m3 tank with a 4.267 m SWD. It will be constructed and configured into a METEOR® process with a Single Stage configuration. System setup is based on a single aeration basin. This process is ideal for BOD & Ammonia Reduction.

2. NUTRICELLTMDTI biofilm carriers will be added to the aeration zone, resulting in increased biomass concentrations due to the active biomass growth on the biofilm carriers. The attached biomass on the biofilm carriers will enhance nitrification. Air will be supplied to the aeration tank by means of existing or new blowers if necessary.

3. Our proposal includes the cost of providing a completely new fine bubble diffused aeration system.

IDI METEOR System


2.2 Design Analysis

A summary of the IFAS design is provided in Table 2. This table demonstrates the biofilm carrier fill fraction required to achieve the required effluent BOD & Ammonia level

Table 2. Design Summary for Tomato Processing Plant

Parameter Value

Design

Flow MGD 0.67

Effluent BOD mg/l 5

Effluent Ammonia mg/l 1

Aerobic (Aeration) Zone Volume m3 888.1

Biofilm carrier fill (Aerobic Zone) % 30

Biofilm carrier Type - NUTRICELLTMDTI Biofilm carrier Surface Area m2/m3 450

Biofilm carrier Volume (Total) m3 266

12” Carrier Retaining Screens (Cylindrical) # 3

Process Air Flow Required (20 deg) scfm 706

IDI METEOR System


2.3 Aeration System

The air requirement is based on the estimated amount of oxygen required and the amount of air needed to thoroughly mix the bioreactor. The total air requirement for the proposed design is indicated in Table 2. Note that this air requirement is based on a fine bubble air diffusion system at 20 oC. The aeration system will consist of a 304L stainless steel vertical drop leg including elbow and vertical flange for connection to the air main. Upstream piping of the flanged elbow will be provided by others. The drop leg will be connected to a 304L stainless steel manifold which will have further connections to each air distributor header. The manifold pipes will be provided with stainless steel supports, hold down straps, cradle, and adjusting/locking mechanism. The 304L stainless distribution headers will consist of factory installed diffuser holders, positive locking anti-rotational joint connections, support stands with hold down clamps, locating plates, and anchor bolts. The aeration system for each grid will be complete with a purge system with eductor piping and isolation valve

The fine bubble aeration system is provided due to its primary advantage of higher oxygen transfer efficiency and consequent lower air requirements and energy costs as compared to coarse air bubble aeration system.

IDI METEOR System


2.4 NUTRICELLTMDTi Biofilm carriers

The fluidized fixed film reactor utilizes NUTRICELLTMDTI biofilm carriers. NUTRICELLTMDTI has the following advantages for this application: Automatically Responds to Load Fluctuations - As the contaminant load

increases, the microbial population in the biofilm increases, enabling additional treatment capacity. Likewise, during low loading conditions, the population self adjusts and decreases through aggressive sloughing action.

Resilient to Toxic Shocking – in a toxic situation, the outer layer of dead bacteria is removed by normal detachment mechanisms present in the bioreactor while the inner layer provides a seed for microbial growth and enables the system to continue treatment of the contaminant load

High Surface Area Fixed Film Biomedia - Suspended carrier elements designed for high rate fixed-film biological digestion within a small footprint.

Biomass Retention – Nitrifiers are protected from washout by retention in the basin on the biomass carrier. Recovery period following suspended biomass washout is significantly reduced due to the retention of fixed film biomass in the system and constant re-seeding of the basin with nitrifiers.

Figure 1. NUTRICELLTMDTI Biomass carrier with biofilm growth, as an example

IDI METEOR System


2.5 Carrier Retaining Screens

The Millbrook WTTP system will consist of three 12” cylindrical media carrier retaining screens depending on the alternative (Figure 2). The cylindrical screens can be flange or slide-in mounted. The screens are manufactured from 304L stainless steel wedge wire. Each screen has abundant open area, with slot widths of 3/8” (10 mm) to provide excellent flow capacity. The biomass carriers constantly scour the screen surfaces and keep it free from debris. The large size of biomass carriers enables large screen openings, resulting in significantly reduced head loss across the screens, and less of a tendency to foul. The head loss through the screens is expected to be less than 0.5 inch. The total number of screens is based on hydraulically handling the various peak flows of 2.2 MGD.

Figure 2. Typical cylindrical slide-in and flange mounted screen

IDI METEOR System


3 Scope

3.1 Scope of Supply

The following table outlines IDI’s METEOR® system scope of supply for the proposed project. Item Description

QTY

1 266 m3 NUTRICELLTM 50 Biofilm carriers delivered in super sacks

2 3

304 L SS Cylindrical Biofilm Carriers Retaining Screens; 12” dia x 72” long Horizontal Cylindrical Screen Assemblies including

Mounting hardware Overflow screens Drain screens Termination point shall be flange(s)

3 1 Fine Bubble aeration system with diffusers, basin piping for c/w drop legs, flanged diffuser pipes, mounting brackets and connection fasteners. Capacities: 706

4 2 DO Analyzers

5 1 PLC Control System

6 2 Sets of O&M Manuals

7 2 Sets of Detailed Shop Drawings

8 10 Service Days, to inspect equipment installation, test all supplied components, assist in start-up and train plant personnel.

IDI METEOR System


3.2 Items by Others

The following items are specifically not by Infilco. They may or may not be required.

General Air Main Piping and all accessories

including valves, bolts gaskets and connectors for attaching to drop pipes

Overflow structures including baffles and weir plates

Chemical Feed Systems for alkalinity correction, external carbon and defoamer

Online instrumentation such as pH, DO, Temperature, etc.

Chemicals for operation: Including external carbon, alkaline solution, defoamer Power

Cleanouts Process Air Blowers

Concrete Reactor Tank

Drains Sludge handling and disposal

Engines/Generators Support Platforms

Foam control Transformers

Hoses /Bibs Variable Frequency Drives

Laboratory Ventilation

Ladders Walkways/Roofing/Stairs/Gratings/Handrails

Lighting Wireways/Wiring

Liquid sampling and analytical work Yard Hydrants

Motor Control Center (MCC) Yard Piping

Non-potable water supply

IDI METEOR System


3.3 Additional Items by Installing Contractor

1. Obtain necessary construction permits and licenses, construction drawings (including interconnecting piping drawings) field office space, telephone service, and temporary electrical service.

2. All site preparation, grading, locating foundation placement, excavation for foundation, underground piping, conduits and drains.

3. Demolition and/or removal of any existing structures, equipment or facilities required for construction and installation of the METEOR® system.

4. Installation of all foundation - supply and installation of all embedded or underground piping, conduits and drains.

5. All backfill, compaction, finish grading, earthwork and final paving. 6. Receiving (preparation of receiving reports), unloading, storage, maintenance

preservation and protection of all equipment and materials supplied by Infilco. 7. Installation of all equipment and materials supplied by Infilco. 8. Supply, fabrication, installation, cleaning, pickling and/or passivation of all

interconnecting steel piping components. 9. Provide and install all embedded pipe sections and valves for tank drains and

reactor inlets and elbows. 10. All cutting, welding, fitting and finishing for all field fabricated piping. 11. Supply and installation of all flange gaskets and bolts for all piping

components. 12. Supply and installation of all pipe supports and wall penetrations. 13. Install and provide all motor control centers, motor starters, panels, field

wiring, wireways, supports and transformers. 14. Install all control panels and instrumentation as supplied by Infilco, as

applicable. 15. Supply and install all electrical power and control wiring and conduit to the

equipment served plus interconnection between the Infilco equipment as required, including wire, cable, junction boxes, fittings, conduit, cable trays, safety disconnect switches, circuit breakers, etc.

16. Supply and install all insulation, supports, drains, gauges, hold down clamps, condensate drain systems, flanges, flex pipe joints, expansion joints, boots, gaskets, adhesives, fasteners, safety signs, and any specialty items such as traps.

17. All labor, materials, supplies and utilities as required for start-up including laboratory facilities and analytical work.

18. Provide all chemicals required for plant operation and all chemicals, lubricants, glycol, oils or grease and other supplies thereafter.

IDI METEOR System


19. Install all anchor bolts and mounting hardware supplied by Infilco; and supply and install all anchor bolts and mounting hardware not specifically supplied by Infilco.

20. Provide all nameplates, safety signs and labels. 21. Provide all additional support beams and/or slabs. 22. Provide and install all manual valves. 23. Provide and install all piping required to interconnect to the Infilco’s

equipment. 24. The Contractor shall coordinate the installation and timing of interface points

such as piping and electrical with the Infilco Supplier. All other necessary equipment and services not otherwise listed as specifically supplied by Infilco.

IDI METEOR System


4 BUDGET PRICE

Our current budget estimate price for METEOR® System, as described in this proposal is:

Description Price

METEOR® IFAS Single Stage BOD & Ammonia Reduction System As Advised By Rep

NOTES – 1. Our Price and Payment Terms are based on IDI's standard terms and

conditions, which can be provided upon request. 2. This price will be valid for thirty (30) days. 3. All prices are excluding Wisconsin state sales and use taxes and any

federal taxes which shall be the sole responsibility of the Owner. No additional duties will have to be paid for the equipment supplied by IDI.

4. Pricing is subject to the all applicable indices for the items in scope of supply calculated from the original proposal date and is in accordance with the Scope of Supply and terms of this proposal and any changes that may require the price to be adjusted. Any other escalation indices can be discussed further and mutually agreed upon.

Shipping TermsFOB Shipping Point, Full Freight Allowed

METEOR® SPECIFIC TECHNOLOGY

METEOR® IFAS/MBBR technology is based on proprietary polyethylene biofilm carriers, which, when added to a treatment basin, provide a large internal surface area for the growth of micro-organisms.

METEOR®

IFAS/MBBR Process

The Meteor® IFAS/MBBR technology offers flexible solutions to a multitude of biological process upgrade applications such as nitrogen removal, treatment capacity increase and wastewater reuse.

Carrier size, geometry and specific internal surface area are critical features. Our unique carriers have been designed with optimal performance in mind.

The upgrade to IFAS or MBBR often consists of simply adding carriers and screens to existing basins and can therefore be completed in a cost-effective and timely manner without major civil engineering requirements and no requirement for additional land. PLC based control system optimize IFAS/MBBR process performance by minimizing energy and chemical costs.

» The METEOR® process can be used for a wide range of biological treatment applications: • Increased Flow Capacity • BOD Removal Enhancement • Nitrification for Ammonia Removal • Total Nitrogen Removal • Total Nitrogen and Phosphorus

Removal

APPLICATIONS

INFILCO

» IFAS/MBBR systems were designed to optimize mass transfer, biomass density and contaminant removal rates through intensive research.

» The combination of large aperture area, high specific biomass and UV resistance makes Meteor® well suited for IFAS/MBBR applications.

» A 22mm diameter carrier offers the ability to utilize a larger screen mesh size, thereby minimizing headloss across the screen and the tendency to foul.

» Highly resilient process for flow and contaminant loading variations.

WASTEWATER

MAIN FEATURES

IFAS, the integrated fixed film activated sludge (Meteor®) process incorporates the positive traits of two fundamental biological treatment processes, namely fixed-film technology and suspended growth technology (conventional activated sludge), together into one hybrid system.

By combining high biomass quantities typical of IFAS fixed-film technologies with fluidization typical of a conventional activated sludge (CAS), the Meteor® technology achieves high removal rates in a small volume.

Conventional activated sludge bioreactors are generally retrofitted with the addition of IFAS carrier retaining screens and modifications to the aeration grid to accommodate the addition of IFAS biofilm carriers. The media facilitates the growth of attached biomass and due to its size, is fluidized throughout the bioreactor.

In MBBR systems all the biomass is supported on the biofilm carrier with no recycled activated sludge.

This attached growth significantly increases the microbial population within the tank, thereby increasing the SRT of the system without increasing the suspended growth population.

Such conditions are conducive to the proliferation of nitrifying autotrophic bacteria and can be designed to ensure that a sufficient population exists to maintain nitrification through cold water conditions when process kinetics slow. The biofilm carriers can also be added to anoxic tanks to improve denitrification, if necessary.

These characteristics make Meteor® technology an attractive option for upgrading existing BOD removal facilities for nitrogen removal in response to new regulatory requirements without costly physical expansion. Since addition of biofilm carriers reduces/eliminates dependence on the suspended growth phase, this technology is also advantageous after secondary treatment where virtually no mixed liquor suspended solids (MLSS) are available.

HOW IT WORKS

» Easy installation» Nitrifi cation and denitrifi cation in cold water

conditions» Minimal plant downtime for process implemen-

tation» Non-invasive basin retrofi t» Adaptable to many basin geometries, process designs and confi gurations» Quick system start-up» Requires no additional land» Operating procedures are unchanged

PRODUCT HIGHLIGHTS

INFILCO METEOR®

METEOR® : An easy-to-implement and cost eff ective way to upgrade WWTPs

CARRIERS

SCREEN

» Increased capacity of activated sludge basins by 100% to 200% with an in-basin retrofi t

» Upgrade of existing BOD removal facilities to full nitrifi cation and total nitrogen removal in response to new regulatory requirements:- Ammonia removal to < 1 mg/L NH3-N- Nitrate removal to < 1 mg/L NO3-N- Total Nitrogen removal to < 3 mg/L TN

» Suspended solids with better settling characteristics than that from conventional activated sludge

» Reduced suspended growth MLSS after a retrofi t, resulting in reduced solids loading on the clarifi ers

» Increase in oxygen transfer effi ciency due to the presence of the media

TECHNICAL FEATURESBIOFILM CARRIER ADVANTAGES

Multiple basin configurations are possible depending on existing installations and effluent objectives (i.e. roughing reactor before CAS for enhanced BOD removal, separate stage nitrification and/or denitrification following CAS, MLE process or 4-stage process for total nitrogen removal, or a 5-stage process for TN and TP removal).

• Unique biofilm carriers were developed specifically for IFAS®/MBBR operation with high MLSS values – other media were designed for operation with no return sludge. The geometry of the carrier prevents overgrowth and provides excellent mass transfer.

• The biofilm carriers have larger apertures (internal openings) to prevent and resist clogging tendencies. The large apertures are designed to allow high mass transfer rates to promote active treatment productivity.

• The biofilm carriers are significantly larger than other free-floating media types. The larger media size allows installation of screens that have much larger openings. This mitigates the impact of overall plant headloss that can be a problem for processes employing smaller media.

BIOFILM CARRIER OPTIONS

• Surface area - 450 m2/m3 • Surface area - 515 m2/m3

MECHANICAL ADVANTAGES

• The biofilm carriers are made from high quality High Density Polyethylene (HDPE), and unlike other media, are formulated with UV inhibitors for a long service life (twenty years or more) even in open basins exposed to constant sunlight.

• Meteor® process is compatible with both coarse and fine bubble aeration. Some competing media are not compatible with fine bubble due to reduced scour of small apertures in the media.

TECHNICAL ADVANTAGES

WASTEWATER

RAW WASTEWATER SCREEN / GRIT METEOR®-C PRIMARYCLARIFICATION

METEOR®-C-N-DN

METEOR®-N-DNSECONDARYCLARIFICATION

TERTIARYFILTRATION

UV, OZONE, or CI

2 DISINFECTION

METEOR® IN THE TREATMENT LINE

COMPLETE TREATMENT SOLUTIONS

Infilco Degremont offers an array of water, wasetwater and industrial treatment solutions for any size client. Headworks, clarification, filtration, biological and disinfection systems are several of the product disciplines in our portfolio. With a

variety of product disciplines in our BIOLOGICAL department, our engineers carefully evaluate each application to provide the most cost-effective and efficient treatment solution.

• Biofor®

• Ferazur®/Mangazur®

• METEOR®

• Climber Screen®

• Helico®

• Vortex

• ABW®

• Cannon Mixer®

• 2PAD • Thermylis • DensaDeg®

• AquaDAF®

If interested in this product, check out some of the complementary products:

SERVICES - INFILCARE™

PILOTING SERVICES

Infilco Degremont offers pilot systems and services for this and many other of our product offerings. Pilot studies are a practical means of optimizing physical-chemical and biological process designs and offer the client several benefits, such as:

• Proof of system reliability• Optimal design conditions for the full-scale system• Free raw water lab analysis• Regulatory approval

If interested in a pilot study for this system, please contact us for a proposal and more information.

PART SALES

Infilco Degremont sells parts and components for most INFILCO brand equipment as well as parts for demineralizers, thickeners, nozzles, pressure filters, and valves. We offer reliable spare parts at competitive prices. We maintain records of previous installations to quickly identify your requirements. Many items are shipped directly from stock for quick delivery.

REBUILDS, RETROFITS AND UPGRADES

Infilco Degremont offers cost-effective rebuilds and upgrades for INFILCO provided systems, no matter what year they were built. If you are interested in an economical alternative to installing a whole new system, contact us for a proposal.

INFILCO DEGREMONT INC.

8007 Discovery DriveRichmond, VA 23229-8605, USATel: +1 804 756 7600Fax: +1 804 756 7643info-infi [email protected]

DEGRÉMONT LIMITÉE

1375, route Transcanadienne, Bureau 400Dorval (Qc) H9P 2W8, CanadaTel: +1 514 683 1200Fax: +1 514 683 [email protected]

CONTACTS WWW.DEGREMONT-TECHNOLOGIES.COM

Copyright © 2010 Infilco Degremont Inc., Degremont Technologies - BOS03202EN-V3-08/2010 - Subject to change without prior notice, contact Degremont Technologies for more information.

INFILCO METEOR®WASTEWATER

Pilot Study Investigations of Nitrogen Removal Using Emerging Fixed Film and Hybrid Technologies

Authors: Amit Kaldate, PhD & Mervyn W. Bowen

These pilots were required by the plants, to check the effectiveness of emerging hybrid technologies and to develop the design parameters for a full scale plant. They were also used for checking and adjusting the accuracy of current modeling programs. Our versions of these programs have been adjusted as data from these and other studies has been gathered. Several of our studies have been driven by specific projects, but others have been driven by the need to understand the effect of the biomass carriers on the oxygen transfer efficiency. The first study was carried out during the period of November 2005 through June 2006 at the Harrisburg, PA WWTP. Harrisburg, along with many other Pennsylvania plants, discharges into the Susquehanna River, which eventually drains into the Chesapeake Bay where local and federal regulations require that nutrient levels be significantly reduced. In this case the plant utilized a pure oxygen activated sludge system for carbonaceous BOD5 removal. The proposed upgrade was to add a nitrification stage rather than try to modify the covered pure oxygen system. The average ammonia level was 17 mg/l, and the objective was for a Phase 1 reduction to less than 3 mg/l and Phase 2 to less than 1 mg/l. Brinjac Engineering Associates, based in Harrisburg, operated the pilot with support from us. Malcolm Pirnie Engineers provided the protocol and the process feedback. Systems that employ floating biomass carriers are typically referred to as “IFAS” (Integrated Fixed Film Activated Sludge) or “MBBR” (Moving Bed Biofilm Reactors) systems. In this case the MBBR system was used. The biomass in an MBBR is supported entirely by the floating carriers and is oxygenated using fine or coarse bubble aeration systems. In this specific case, the MBBR was based on two tanks operated in series.

Degremont Technologies – Infilco supplied a trailer specifically equipped for MBBR operations. Two other trailers are available for full IFAS studies.

The MBBR trailer is equipped with two trains, which allows for two arrangements to be tested side by side. For Harrisburg two fill fractions were tested; one with 35% fill by volume, the other 50% by volume. For your information, the water displacement is approximately 4% and 6%, respectively. In this case the nitrifiers were developed naturally; in other studies the carriers can be seeded with the plant’s activated sludge.

Test Period #

Biofilm Carrier Fill

Fraction

Pilot Unit Flow

Corresponding full-scale plant

flow

Hydraulic Retention

Time

Test Period Duration

% GPM MGD Hours From To

1 50 3 26.9 4.78 12/22/2005 02/14/2006

2 50 5 45.0 2.87 02/15/2006 02/27/2006 3 50 4.2 37.7 3.41 02/28/2006 03/21/2006 4 35 3 26.9 4.78 03/22/2006 04/04/2006 5 35 5 45.0 2.87 04/05/2006 04/11/2006 6 35 4.2 37.7 3.41 04/12/2006 05/03/2006 7 35 6 53.9 2.39 05/04/2006 05/22/2006 8 35 7 62.8 2.05 05/23/2006 06/01/2006 9 35 8 71.8 1.79 06/02/2006 06/09/2006

Chart No. 1

Chart Number 1 shows the testing period and the set-ups. It is interesting to note that the study started in December with water temperatures in the order of 9 - 13.5°C.

Chart No. 2

Chart Number 2 shows the results achieved over the testing period with the following average results:

Temperature: 13.7 oC Influent TKN: 18.4 mg/l

Influent NH3-N : 15.2 mg/l Effluent NH3-N: 0.33 mg/l

0

5

10

15

20

25

30

22-Dec 19-Jan 16-Feb 16-Mar 13-Apr 11-May 8-Jun

Date

NH

3-N

Con

cent

ratio

n (m

g/L)

Influent NH3-N Effluent NH3-N

Chart No. 3

Chart Number 3 shows the surface loading rates, the following recommendations are required to meet the objectives of less than 3 & 1 mg/l of ammonia nitrogen respectively.

For less than 3 mg/l NH3-N: 1 g/m2/d For less than 1 mg/l NH3-N: 0.85 g/m2/d

HRT: 2.4 – 2.9 hours The second study was carried out at a plant in Chesterfield County, Virginia during the period June 2006 to May 2007. The Proctor’s Creek WWTP discharge quickly reaches the Chesapeake Bay and will be required to control its total nitrogen discharge to less than 5 mg/l. The pilot study objective was to develop a process that could achieve the TN requirement while using the existing tanks. R. Stuart Royer (now part of Malcolm Pirnie) was the local engineer overseeing the process. For this study, a true IFAS system was employed with the biomass carriers residing in the aeration basins along with the mixed liquor biology. In addition to determining the media fill fraction, mixed liquor suspended solids levels were also investigated.

Harrisburg, PA - IDI ActiveCellTM Pilot StudySurface Loading Rates - NH3-N

0.00

0.20

0.40

0.60

0.80

1.00

1.20

1.40

1.60

1.80

2.00

2.20

0.0 0.2 0.4 0.6 0.8 1.0 1.2 1.4 1.6 1.8 2.0 2.2 2.4 2.6 2.8 3.0 3.2 3.4 3.6 3.8 4.0 4.2 4.4

Applied (g NH3-N/m2/d)

Rem

oved

SLR

(g N

H 3-N

/m2 /d

)Reactor 1 Reactor 2 Combined Reactors

To achieve the low TN level required, a four-stage system was employed. Stage 1 was anoxic with submerged mixers. Mixed liquor was recycled back to this zone as a pre-denitrification stage. The stage 2 aeration system combines the floating biomass carriers with the activated sludge process to achieve nitrification with a 50% media fill and an MLSS concentration of around 2,800 mg/l. Stage 3 is a second anoxic zone with submerged mixers and an external carbon feed, methanol. Stage 4 is a short re-aeration zone.

For this study, the biomass carriers were seeded using the plant’s returned activated sludge. For an IFAS study, the pilot trailer must be equipped with clarification and a returned sludge capability. A wide range of tanks are also needed so that hydraulic retention times can be adjusted to simulate the full scale facility. In this case automatic samplers were added along with data acquisition equipment.

Test

Period Flow simulates HRT (hrs) Duration

gpm (Flows in MGD) Total Pre-

Anoxic Aerobic Post-Anoxic

Re-aeration From To

Period 1 Start-up & Acclimation 23-Jun-

06 13-Jul-

06 Period

2 1.6 New Basins (17 MGD) 11.40 3.99 5.13 1.71 0.57 14-Jul-

06 28-Aug-

06 Period

3 2.6 Old Basins (14 MGD) 7.02 2.46 3.16 1.05 0.35 31-Aug-

06 31-Oct-

06 Period

4 3.025 Old Basins (14 MGD) 6.05 2.12 2.72 0.91 0.3 1-Nov-

06 21-Dec-

06

Period 5 3.5

Peak (16.2, 28.8

MGD) 5.20 1.82 2.35 0.78 0.26 22-Dec-

06 30-Jan-

07

Period 6 2.065 New Basins

(17 MGD) 8.84 3.09 3.98 1.33 0.44 31-Jan-07

13-Feb-07

Period 7 3.025 Old Basins

(14 MGD) 6.05 2.12 2.72 0.91 0.3 14-Feb-07

30-Apr-07

Chart No. 4

Chart No. 4, shows the testing periods and the hydraulic retention times assigned to each stage.

0

4

8

12

16

20

24

28

32

36

40

44

22-Jun 22-Jul 21-Aug 20-Sep 20-Oct 19-Nov 19-Dec 18-Jan 17-Feb 19-Mar 18-AprDate

Nitr

ogen

Com

pone

nts

Con

cent

ratio

n (m

g/L)

Influent TN Effluent TN TIN

16 - 25° C 11 - 16° C 16 - 18° C

Chart No. 5 In chart no. 5 we see the test results and the average performance, which later became the basis of design. Note that, in this case, water temperatures varied from 11°C to 25°C. Below are the average figures for study

Influent TN: 28.1 mg/l Influent TKN: 26.7 mg/l

Effluent TN: 3.5 mg/l Effluent TIN: 1.63 mg/l

Effluent NH3-N: 0.29 mg/l

Chart No. 6

Chart No. 6 shows the surface loading rates and below we show the applied loading rates.

NH3-N applied loading rate: 0.72 g/m2/d NH3-N removal loading rate: 0.71 g/m2/d

Here we can see a summary of all the results that were achieved.

NH3-N removal efficiency: 98.5% TKN removal efficiency: 91.6% TN removal efficiency: 87.3%

Low effluent NH3-N achieved at average loading rate of 0.67 g/m2/d and up to 1.04 g/m2/d Effluent BOD: less than 5 mg/l

Net alkalinity consumption of 65 mg/l.

0.0

0.1

0.2

0.3

0.4

0.5

0.6

0.7

0.8

0.9

1.0

1.1

1.2

0.00 0.10 0.20 0.30 0.40 0.50 0.60 0.70 0.80 0.90 1.00 1.10 1.20

Applied SLR (g NH3-N/m2/d)

Rem

oved

SLR

(g N

H3-

N/m

2 /d)

However, the pilot operated without any supplemental alkalinity. Average MLSS: 2,850 mg/l

Since methanol was the external carbon source to be used initially, control of this chemical was critical. The methanol control used on the pilot was one that had proven successful on operating facilities for several years.

As can be seen from chart No. 7, the required TN level of 8 mg/l was held very closely, optimizing methanol consumption.

PLC

MeOH Dosing Control Interface Effluent NOxN set-point MeOH/NO3-Neq value

Denitrification

MeOH

NOx-N Flow DO NOx-N

Chart No. 7



BioPortz™ Moving Bed Bioreactor

Entex Technologies Inc.

400 Silver Cedar Court, Suite 260, Chapel Hill, NC 27514 919.933.2770 phone 919.287.2258 fax www.entexinc.com

February 4, 2013

Valera Saknenko, Ph.D., P.Eng., PMP

Senior Associate

R.V. Anderson Associates Limited

2001 Sheppard Avenue East Suite 400

Toronto ON M2J 4Z8

Re: Millbrook, ON IFAS Design

Dear Valera:

Thank you for the opportunity to present a proposal for Entex’s BioPortzTM

moving media system for the

IFAS design in Millbrook, ON. Based upon the information received we have modeled the system using our

BioPortz moving media for BOD, TSS, and NH3-N removal.

1) Basis of Design

We based the design on a flow of 2,520 m3/d. The base design parameters modeled are:

Influent Effluent

Flow 2,520 m

3/d

(Avg. daily)

2,520 m3/d

(Avg. daily)

BOD 190 mg/L 5 mg/L

TSS 210 mg/L 5 mg/L

TKN 25 mg/L - mg/L

NH3-N - mg/L 2 mg/L (winter)

1 mg/L (summer)

Temp. 8 oC (min.) --

pH 7 – 8 --

Alkalinity 200 mg/L as CaCO3 --

2) Description of system

Entex proposes constructing a one train IFAS design for biological treatment of BOD, TSS, and NH3-N

using Entex BioPortz moving media. The IFAS process train will consist of three (3) aerobic reactors (in

series). Entex retention screens will be added in the BioPortz basins to retain the media and an Entex

aeration system will be provided for the air required in each of the aeration basins.

Entex Technologies Inc. Page 2

We propose the following dimensions and media fill, per train:

Aerobic 1 43,085 gal 18 ft x 20 ft x 16 ft swd 65% media fill



3) Summary of proposed scope of supply

Equipment as follows:

Entex BioPortz moving

media

Aerobic 1 – 65% fill

3,744 ft3 of BioPortz media with

670,170 ft2 of biologically active surface area.







Media retention screens

Three (3) sets of retention screens (total – eighteen (18)

screens) with 10 mm openings and 2 inch pressure drop

across each set of screens. 304 grade stainless steel.

Aeration System Full floor coverage of Entex coarse bubble diffusers for

aerobic basins.

Operation &

Maintenance (O&M)

Manuals

Two (2) O&M manuals

Process Engineering for all equipment, including sizing and selection.

Review and approval of P&I Diagram for the Entex aeration basin.

Preliminary General Arrangement Drawings and review and approval of final General Arrangement

Drawings for the Entex supplied equipment.

Review of BioPortz biological process reactor drawings with respect to nozzles, penetrations, and

dimensions, excluding structural design.

Manufacturers’ service for installation, inspection, & start up training.

Entex Technologies Inc. Page 3

Items not included (but not limited to):

Unloading and storage of materials on-site

Installation of system

Interconnecting piping and valves, and installation and interconnections

Electrical, including motor controllers

Blowers

Pumps

Freight

4) Pricing

An estimate for the enclosed scope of work is $465,500.00.

We look forward to working with you on this project. Please call me at 919-606-5734 or e-mail me at

[email protected] if you have any additional questions or concerns.

Sincerely,

Erin Gallimore

Manager, Municipal Systems

400 Silver Cedar Court, Suite 260, Chapel Hill, NC 27514 919.933.2770 phone 919.287.2258 fax www.entexinc.com

BioPortzTM Installations Updated: December 2012 Frontier Refining North Plant Cheyenne, WY 2006 320,000 gpd

Chevron Phillips Orange, TX 2006 15,000 gpd sanitary WW Drilling Specialties Conroe, TX 2006 2,800 gpd

MCI Paper Portneuf, QB 2006 1.6 mgd

Frontier Refining South Plant Cheyenne, WY 2007 320,000 gpd Specialty Chemicals Manufacturer NC 2008 120,000 gpd Oak Creek WTP Oak Creek, CO 2009 250,000 gpd post lagoon

Tabernacle SD Tabernacle, NJ 2009 20,000 gpd denite Seneca Landfill Seneca, PA 2010 114,000 gpd leachate Owens Corning Starr, SC 2010 1 mgd

Ciales WTP Ciales, PR 2011 1 mgd Seneca Landfill- Phase 2 Seneca, PA 2011 114,000 gpd leachate

Brattleboro WTP Brattleboro, MA 2011 3 mgd Owens Corning* Tlaxcala, MX 2011 300,000 gpd

*in progress

BioPortz™ by ENTEX Technologies

BioPortz moving media system

Increased capacity.Increased biomass.

BioPortz media

provide high

biologically active

surface area for

increased biomass

growth.

The large size of the

BioPortz media allows

for exceptionally high

open area screens.

Engineering

a Clean Water

Environment

BioPortz is a moving media system for use in Integrated Fixed-�lm Activated Sludge (IFAS) and submerged �xed-�lm (SFF) systems. Independently movingBioPortz carriers continually circulate through the aeration basin in a random motion, ensuring excellent oxygen and substrate transfer to the biomass.

BioPortz is a cost-e�ective solution for existing activated sludge plants that need more advanced treatment. Because little or no additional tankage is required, BioPortz is an ideal solution for plants with limited room for expansion. It is also an excellent choice for space e�cient, high performance new plant designs.

BioPortz moving media provides extensive surface area for biomass growth. �e attached biomass population can more than double thee�ective MLSS concentration.

�e vigorous motion of the media through the aeration basin provides a high shear on the biomass, maintaining a thin biological�lm. �e thin �lm provides for high ratebiological kinetics.

Components:

The basic elements

of the BioPortz system

include:

1. attached growth media,

2. media retention screens, and

3. an aeration system.Entex Technologies Inc.400 Silver Cedar CourtSuite 260Chapel Hill, NC 27514

919.933.2770 phone919.287.2258 fax www.entexinc.com

Nitrification & Denitrification

Optimized Screening

BioPortz Retention Screens

BioPortz is

versatile

BioPortz can be

used in a variety

of configurations,

including many

different biological

nutrient removal

(BNR) processes.

Media can be

added to aerobic

zones for

carbonaceous

or ammonia

removal and to

anoxic zones for

denitrification.

BioPortz by ENTEX Technologies, continued

Cost Effectiveness

Advanced Systems. Proven Solutions.

ENTEX’s unique media design maximizes biologically active surface area at an exceptional176 �2/�3. BioPortz is made of durable HDPE; the media never needs replacement.

Servicing aeration systems is simpli�ed because of the 0.96 speci�c gravity. It �oats when the air is turned o� for easy movement out of the basin.

BioPortz improves wastewater treatment with little or no addition of aeration basins or clari�ers. It’s a signi�cantly less expensive way to upgrade activated sludge plants.

ENTEX engineers have been involved in hundreds of plant installations.We’d like to be involved in yours.

ENTEX’s larger BioPortz media allowsfor media retention screens withexceptionally large open area. Because inlet screening needs to be 2/3 smaller than the media retention screens, BioPortz systems only require normal �ne screens, saving capital cost as wellas operator time and attention.

BioPortz provides stable growth platforms for slow-growing nitri�ers. Nitrifying plants perform better; non-nitrifying plants are able to nitrify. Plants needing to convert to nitri�cation can do so at a far lower cost than adding new basins. BioPortz can also be used in anoxic zones for denitri�cation.

High Performance Media



Anoxkaldnes™ Moving Bed Bioreactor

Actiflo™ Microsand Ballasted Clarification

Veolia Water

MILLBROOK WWTP VALERA V. SAKNENKO SENIOR ASSOCIATE R. V. ANDERSON ASSOCIATES LIMITED

BUDGETARY PROPOSAL ANOXKALDNES™ MOVING BED BIOFILM REACTORS TECHNOLOGY MILLBROOK WWTP JANUARY 15TH , 2013 PREPARED BY: ROBERT LAFOND / CHRISTIAN CABRAL

PROPRIETARY NOTICE This proposal is confidential and contains proprietary information.

It is not to be disclosed to a third party without the written consent of Veolia Water Solutions and Technologies Canada.

Millbrook WWTP

BUDGET PROPOSAL - ANOXKALDNESS™ MBBR

16/01/2013, Rev1 ii

EXECUTIVE SUMMARY Veolia Water Solutions and Technology Canada Inc. (VWS Canada Inc.) provides unique water and wastewater solutions to both industrial and municipal clients. As part of Veolia Water Solutions & Technologies, VWS Canada Inc. draws upon more than 500 technologies and over 3,000 patents to find the best solution for each specific application. These resources, combined with our experience gained over the last 155 years in the water treatment industry, ensure that your water and wastewater treatment needs are met through cost-effective, environmentally sound solutions implemented through projects focused on safety, quality and customer satisfaction.

VWS Canada Inc. is pleased to offer this proposal for our AnoxKaldnes™ Moving Bed Biofilm Reactor (MBBR) technology. This biological treatment solution has been proven effective in more than 500 facilities worldwide over the past 21 years. The first MBBR installed 19 years ago is still using its same biomedia and aeration system. As the original inventor of this technology, AnoxKaldnes has the capabilities and expertise unparalleled by its competitors in the industry.

The basic concept of an MBBR process is to have a non-clogging biofilm reactor with low head loss, high surface area, and no need for backwashing or cleaning of the elements. This robust system is easy to operate and has been the technology of choice for a variety of municipal and industrial applications. Flexibility in the various ways that this technology can be applied makes it uniquely suited to diverse needs for biological treatment. The MBBR is particularly appropriate for retrofit of existing facilities, and can operate as pre-treatment to existing processes or as a stand-alone system.

A major advantage of the technology is the small footprint of the system as compared to its treatment efficiency. The key to the technology is the biofilm carrier elements that provide a very large surface area for biological growth within a very small space. The system typically occupies only one-fourth of the space required by a conventional plant. Aeration in the system provides oxygen for biological activity as well as complete mixing for enhanced treatment.

The MBBR system offered in this budgetary proposal is specifically designed to fit into a small footprint. The train MBBR followed by Actiflo™ has the minimal space requirement in the market especially when average design flows and peak flow are far apart. As Total Phosphorous requirement at the final effluent are very low (less than 0.1 mg/L) we also propose the use of tertiary membranes to attain such water quality.

Millbrook WWTP


16/01/2013, Rev1 iii

TABLE OF CONTENTS

Page No.

SECTION 1. INTRODUCTION ......................................................................................... 5 SECTION 2. DESIGN BASIS ............................................................................................. 6 SECTION 3. PROPOSED TREATMENT CHAIN .......................................................... 7 SECTION 4. SCOPE OF SUPPLY................................................................................... 14 SECTION 5. ESTIMATED COST AND SCHEDULE................................................... 17 List of Appendices

APPENDIX 1: Carbon Footprint Memo APPENDIX 2: ACP 2-40 Cut Sheet APPENDIX 3: Norit X-Flow Skid Cut Sheet

Millbrook WWTP


16/01/2013, Rev1 iv

LIST OF TABLES Page No.

Table 1 Design Parameters.....................................................................................................6 Table 2 Design Parameters.....................................................................................................6 Table 3 Design Parameters...................................................................................................14 Table 2. Scope of Supply ......................................................................................................15 Table 3. Schedule ..................................................................................................................... LIST OF FIGURES

Page No. Figure 1. Simplified PFD ..........................................................................................................7 Figure 1 Biofilm Growth in the Media ......................................................................................8 Figure 2. Aeration Grids ..........................................................................................................9 Figure 3. Sieves ......................................................................................................................9 Figure 4. Actiflo™ Unit ..........................................................................................................10

Millbrook WWTP


16/01/2013 - 5 -

SECTION 1. INTRODUCTION

VWS Canada Inc. is pleased to provide this budgetary proposal for the upgrade of the Millbrook WWTP project with our AnoxKaldness Moving Bed Biofilm Reactor (MBBR) technology. This proposal is for a complete equipment supply with all the required equipment and controls required for operation of the secondary and tertiary portions of the new wastewater treatment.

We understand existing site has limited footprint for conventional biological treatment options (aka, SBR or Activated Sludge). Our proposed solution relies on the most compact solids settler system in the market, the Actiflo. The train MBBR followed by Actiflo and Norit tubular membranes will be extremely compact. Our efficient filtration system (NORIT X-Flow membranes) will allow much higher fluxes than conventional submerged membranes such as on MBR applications. As a result, less membrane replacement costs and energy consumption is expected.

In terms of overall dimensions, the three main blocks to be installed in the existing site are:

The MBBR reactors (outdoors): approximate dimensions of 150 m2

The Actiflos room: approximate dimensions of 100 m2

The Tertiary (membranes and coagulation tank) room: approximate dimensions of 150 m2.

The mechanical building and chemical dosing skids and storage area:

approximate dimensions of 140 m2.

Millbrook WWTP


16/01/2013 - 6 -

SECTION 2. DESIGN BASIS

VWS Canada Inc.’s process solution is designed specifically to meet the needs of your facility based on the wastewater characteristics provided by the email received on December 28th. The parameters of concern and influent values are listed in Table 1 below:

Table 1. Influent Design Parameters (hypothesis)

Parameter Units Value Flow (average) m3/d 2,520 Peak Hydraulic Flow m3/d 8,242

BOD5 (Ave Daily/Peak) mg/L (kg/d)

190 (479)

TSS (Ave Daily/Peak) mg/L (kg/d)

210 (529)

TKN (Ave Daily) mg/L (kg/d)

25 (63)

TP (Ave Daily) mg/L (kg/d)

5 (13)

Max month Load factor 1.25 Temperature C 10 - 20

Table 2. Effluent Objectives

Parameter Units Value cBOD5 mg/L 5 TSS mg/L 5 Total Ammonia (winter) Total Ammonia (summer) mg/L 2

1 Unionized Ammonia mg/L 0.2 Total Phosphorous mg/L <0.1

NOTE:

1. pH level is considered to be neutral 2. Soluble grease levels in the MBBR influent considered to be <50 mg/L 3. Calcium concentrations in the MBBR influent assumed be low (30-50 mg/L) 4. Toxicity is not addressed in this design.

Millbrook WWTP


16/01/2013 - 7 -

SECTION 3. PROPOSED TREATMENT CHAIN

3.1. PROCESS OVERVIEW

Our proposed system consists of two trains of four (4) MBBR reactors (in series) capable of treating up to 2,520/8,242 m3/d (ave/peak) followed by an Actiflo™ units to remove biomass solids and phosphorus and membrane skids to polish and achieve the stringent effluent prior to discharge. Other equipment to be provided consists of: blowers, chemical dosing system, tertiary coagulation mixer etc. All equipment is controlled and powered though local panels.

As overall philosophy, the system proposed has 2 trains, each train designed at 50% of the plant capacity.

The design for the proposed trains is based on different steps and units that are further described in the next section. The overview of the system is presented in Figure 1.

Figure 1. Simplified PFD

MBBRTank 1

BOD removal

MBBRTank 2

BOD removal

MBBRTank 4

Nitrification

Membranes

MBBRTank 3

NitrificationInfluent

EffluentSludge Storage

(existing storage)Supernatant

Actiflo

Millbrook WWTP


16/01/2013 - 8 -

3.2. PROCESS DESCRIPTIONS

3.2.1. Pre-treatment (not included)

Our proposed train requires influent pre-treatment (screen and grit removal) equipment to prevent particles of 6 mm or larger to get into the MBBR reactors. The units must be designed for a peak flow of 8,242 m3/d.

3.2.2. Moving Bed Biofilm Reactor (MBBR)

The biofilm media form AnoxKaldnes™ K5 is installed in the MBBR reactors and is the key component to the biological process. The MBBR process utilizes a cylindrical plastic carrier about 25 mm in diameter, as seen in Figure 2, to provide an environment in which bacterial populations and protozoa can grow very effectively. The carriers are retained in tanks and aerated to provide the oxygen needed for growth in aerobic configurations. This aeration also supplies mixing energy to cause the carriers to be completely mixed and dispersed throughout the liquid.

Figure 2. Biofilm Growth in the Media

A MBBR consists of a tank equipped with an outlet sieve to retain the media, the media itself, and a means of aeration or mixing. Aeration is by a medium bubble system design using 304 stainless steel laterals and diffusers, as seen in Figure 3.

One of the important features of the process is that biofilm thickness is controlled by the movement of the media so that oxygen diffusion through the biofilm is encouraged. Detached/sloughed biofilm is suspended within the reactor and leaves the reactor with the treated wastewater. The sloughed biofilm will be captured in a separation device downstream.

The MBBR is a stand-alone biological treatment system with no need for backwashing of the media. The wastewater treatment plant will operate as a fixed-film process with no return activated sludge being pumped back from the clarification unit to the bioreactor.

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Figure 3. Aeration Grids

Figure 4. Sieves

3.2.3. ACTIFLO™

The ACTIFLO™ system proposed is designed to treat biological effluent as solids separation unit. The selected modular plant (ACP-2-40) is easy to install and operate. One unit per MBBR train (two units total). One unit can achieve the total flow in case of emergency.

Sand-ballasted settling is a high-rate coagulation/flocculation/sedimentation process that utilizes microsand as a seed for floc formation. The microsand provides a surface area that enhances flocculation and acts as a ballast or weight. The resulting floc settles very fast, allowing for compact clarifier designs with high overflow rates and short detention times. The use of microsand also permits the unit to perform well under dramatically changing flow rates without impacting final effluent quality and therefore the downstream process.

Raw water enters into the coagulation tank of the sand-ballasted system where a coagulant, such as alum, ferric chloride, or ferric sulphate, is added to destabilize the suspended solids and

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colloidal matter in the influent stream. The water then flows into the maturation tank where polymeric flocculent and microsand are added to initiate floc formation. These serve as a “seed” for floc formation and development in the next process step. From this tank, the fully formed ballasted floc enters a settling tank equipped with a lamella, which provides the rapid and effective removal of the microsand/sludge floc. The clarified water exits the system via a series of collection trough or weirs.

The sand-sludge mixture settles to the bottom of the clarifier. Scrapers force the sludge collected at the bottom of the clarifier into a center cone from which it is continuously withdraw and pumped to hydrocyclone where sludge and microsand are separated by centrifugal force. After separation, the higher density microsand is discharged from the bottom of the hydrocyclone and re-injected into the process for re-use. The lighter density sludge is discharged from the top of the hydrocyclone and directed to the sludge management facilities.

Actiflo™ is a compact and very robust alternative for MBBR clarification at Millbrook. Hundreds of references in Canada and Worldwide show that a system properly installed and maintained needs little attention from operators and is very resilient to effluent variations. The figure below presents the internals of the Actiflo™ units but detailed cut sheets will be provided upon request.

Figure 5. Actiflo™ Unit

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3.2.4. Biological Tanks

The proposed plant is mainly two (2) trains of four (4) concrete tanks with standard dimensions set at 4 m width and 4 m of side water depth (SWD) with an extra 900 mm of free board (civil works by other). The total length of each train will be 17 m, 304 stainless steel aeration grids and sieves, instrumentation (DO/pH/Temp probes) place inside of the MBBR reactors will complete the process. These tanks can be installed outdoor providing savings in regards to civil works.

3.2.5. Effluent Tertiary Treatment

The proposed tertiary treatment is a membrane filtration process that was developed by NORIT X-Flow (now Pentair X-Flow) and uses proprietary X-Flow Ultrafiltration membrane modules. The modules, identified as SXL-225, are 0,2 meter (8”) in diameter and 1,5 meter (60”) long. The SXL225 module contains 40 m2 of membrane area from the more than 11,000 hollow fibres contained in each module. These modules will come in 2 skids of overall dimensions of 7.5 m in length, 2,5 m in width and 3.4 m tall (each). Given the compact size of the skid units, the system provided is to be installed indoors for easy maintenance.

The membrane fibres are engineered to possess excellent chemical resistance properties. They can be operated over a wide pH range (1 to 13) and are very oxidant tolerant, thus providing the opportunity to treat chlorinated feed water, or to clean the membranes with an oxidizing agent. The fibres also demonstrate a high temperature resistance and excellent mechanical strength.

These membranes ensures removal of colloids, solids, bacteria and Cryptosporidium and Giardia oocysts (greater than 6 Log removal), and of a large fraction of virus as well (greater than 4 Log removal). This membrane has been granted Log Removal Values of 4 - 4 - 1 (for Crypto, Giardia and Virus, respectively) for applications in the province of Quebec.

The membrane fibres are operated inside-out, i.e., the feed suspension is pumped into the lumen of the fibres. The membranes are operated inside-out, which means that the substances that are retained by the membrane are in a clearly defined space, where they are easily removed by either backwashing or chemical cleaning. One of the major advantages of the inside-out operation is the fact that the feed water is never allowed to enter the shell side (outside) of the membrane, where solids may build up between the membrane fibres. Once solids are caught between the individual fibres, they may be difficult if not impossible to remove, especially where the ends of the fibres are potted in resin.

The modules are used in a vertical configuration allowing for a more robust hydraulic backwash due to the introduction of air bubbles inside the lumen of the fibres during a typical backwash cycle. The added robustness provided by the vertical membrane application and very efficient hydraulic backwash will allow for unpredicted conditions (for instance, sudden lake turn-over and very high turbidity conditions) to have limited or no impact on the finished water quality. An example of skid with similar dimensions in provided in the Appendix C.

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As indicated on Figure 1, a coagulation tank and a mixer will be used to provide a minimum coagulation/flocculation time of approximately three minutes. The coagulation dosing system is included with this proposal and has two pumps (one duty, one stand-by).

At regular intervals (say between 30 and 60 minutes) a short hydraulic backwash will be performed. Two backwash pumps are supplied (1 duty, 1 stand-by) to perform this task using permeate (treated) water. At regular intervals (say 24 to 48 hours) a chemical enhanced backwash (CEB) is performed on each train, one at a time. There are generally two CEBs performed back-to-back, the first one consisting of soaking the membranes for 10 minutes in a solution at a pH of 12, and a second one consisting of soaking the membranes for 10 minutes in a solution at a pH of 2 to 3. The chemical dosing systems used (acid, alkali and hypochlorite) are included with this proposal with two pumps per chemical (1 duty, 1 standby).

A control panel with a color touch screen HMI is provided to control all aspects of the membrane filtration and dewatering processes. Integrity tests can also be performed automatically on a regular basis in order to quickly assess membrane integrity. A compressor is provided to perform the air integrity tests as well as provide air used for backwash purposes and for valve actuators.

3.2.6. Sludge Handling Equipment

The sludge produced by the solids removal step of the biological treatment (that is, from the Actiflo™ process) will be continuously collected at the existing tanks which operate as an aerobic digester and sludge holding tank. Modifications of the existing tanks are not addressed within this proposal.

3.2.7. Other Equipment

The standard solution from VWS Canada Inc. comes with standard chemical dosing skids necessary for solids coagulation and concentration but does not include other chemical systems that may be necessary, depending on influent conditions, such as pH control (acid and/or caustic injection system), or foam control chemicals.

The standard scope of supply includes automation for the new equipment but has limited scope outside our typical scope of supply. The following equipment may be incorporated as part of Veolia’s scope: pretreatment units, monitoring instrumentation (such as turbidity meter), auto-samplers, pump stations (influent, effluent or local sump pumps), septic hauler and other commercial discharge processing stations, etc. VWS Canada Inc. has a wide range of products to provide fully automated systems that need minimal physical presence at site. We would be glad to further describe such options if appropriate.

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3.3. DESIGN PARAMETERS

Table 3 shows the characteristics of the MBBR™ process and the basic design parameters.

Table 3. MBBR™ Characteristics and Design Parameters

Items

Value

Unit

Total tank volume 521 m3

Total Hydraulic retention time (average) 5.0 Hrs

Number of trains 2

Number of MBBR reactors per train 2 for BOD

2 for Nitrif.

% fill of K5 media in MBBR reactors

BOD reactors

Nitrification reactors

45

45

%

%

Total air requirement (average summer) 1700 Nm3/hr

Blowers Operation Pressure 6.5 Psig

4000 mm depth

4000 mm width

16300 mm long

Water depth of MBBR reactors

Width of MBBR train

Total Length of MBBR train

900 mm freeboard

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SECTION 4. SCOPE OF SUPPLY

4.1. SUPPLIED AND OPTIONAL ITEMS

The preliminary scope of supply for this project is presented in Table 4 below.

Table 4. Scope of Supply

Pre-treatment (not included in this proposal)

Carrier (media) K5 Media design at 7 Celsius

lot

Each MBBR train will include:

Medium Bubble aeration system in 304L stainless steel including header and lateral piping within the reactors (one per reactor). Vertical down comer are include

10 headers

(two per BOD reactor one per nitrif reactor)

Sieve assembly in 304L stainless steel to retain the

carrier elements and to minimize head loss, 450 mm diam x 1000 mm long (3 per reactors)

24

(3 per reactor) Dissolved Oxygen probe with 4-20 mA signal.

Transmitters included Foaming detector TSS probe with 4-20 mA signal

Transmitters included

8

6 2

Blowers Three (3) blowers of 60 HP (two in operation and one

backup) will be providing (one in operation and one standby). Each blower will be mounted in an acoustic enclosure.

3 (2+1)

Tetiary Coagulation System:

Mixer and coagulant dosing skids for post coagulation upstream membranes,

2

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Norit Skids

NORIT X-Flow model SXL-225: 0,2 meter (8”) in diameter and 1,5 meter (60”) long with 40 m2 of membrane area. Total flow per skid of 4,000 m3/d (38 modules). The system will include all chemicals for CEB.

2

Controls

Control panel (NEMA 12) for the operation of equipment included in this proposal. Interface to allow equipment operation.

MCC of our motors is including in our control panel.

Actiflo Secondary Clarifier

Prefab Actiflo ACP-2/40 with all accessories and panel control, one per MBBR file.

Polymer chemical dosing system (3 pumps, 2 in

operation + 1 standby) and all the accessories. Automatic polymer preparation system Hydrapol-250

Alum chemical dosing system (3 pumps, 2 in

operation + 1 standby) and all the accessories.

Alum reservoir of 10 000 litre including level indicator and instrumentation

Control panel for automation of the two clarifiers,

integrated in the main MBBR control Panel

1

2

1

1

1

1

1

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ITEMS NOT SUPPLIED BY VWS

The following items are beyond this scope of supply and are to be addressed by the client:

Foundations, buildings, concrete tanks, splitter boxes and site work;

Permanent utilities (service water, instrument air etc.… );

Influent pumping, sump and transfer pumps;

First fill of chemicals for start-up;

Installation of all equipment

Sludge handling and retrofits

4.2. CLARIFICATIONS

VWS Canada Inc. has used the following preliminary list of assumptions and constraints in developing the scope and pricing for the proposed project:

Veolia’s specifications for electrical, mechanical, civil and structural construction and coatings apply.

Water will be conveyed by the others to the treatment system. Piping between tanks and other equipment (inside or outside building) and associated manual valves are not part of this proposal.

Veolia will provide supervision of operation and maintenance services for the wastewater system during start-up and commissioning under this proposal.

Space for an adequate and secure construction lay-down area is available near the proposed construction site.

All freight, taxes and bonds are excluded.

Estimates have been prepared assuming that Veolia’s Standard Terms and Conditions apply.

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SECTION 5. ESTIMATED COST AND SCHEDULE

5.1. BUDGETARY COST

The estimated budgetary cost for the Millbrook system and associated equipment supply is $4,200,000 CAD. This budgetary, non-binding estimate of probable cost is presented for project planning and evaluation purposes only and is not a firm offer.

If the selected secondary treatment is outside the scope of this proposal, the equipment cost for the tertiary membranes and associated items (coagulation system, chemical cleaning etc…) is $1,500,000 CAD.

5.2. STANDARD TERMS OF PAYMENT

The terms of payment are as follows:

30 percent on submittal of shop drawings

70 percent on the delivery of equipment to the site

All payment terms are net 30 days from the date of invoice.

5.3. SCHEDULE

The projected schedule is shown in Table 5 below.

Table 5. Schedule

ITEM TIMELINE CONDITIONS

Shop drawings 4-6 weeks Submission within designated timeline following receipt of a contract executed by all parties

Complete Equipment Delivery 24-26 weeks After receipt of written approval of shop drawings

Operation and Maintenance manuals 90 days Submission within timeline designated

after receipt of approved shop drawings We trust the enclosed information meets your requirement, and would be please to review the contents with you.

Regards,

Veolia Water Solutions & Technologies Canada Inc.

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ANNEXE

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Project : Millbrook WWTP, ONOur file : 13TO01

Date : 2013-01-25

List of motors (PRELIMINARY)

Application Number of units Installed HP (unit.)

Average Motor Load Power Supply

575V/3/60 460V/3/60 380V/3/50 Details

Actiflo - Pre-Coagulation Mixer 2 1,5 75,0% xActiflo - Coagulation Mixer 2 1,5 75,0% xActiflo - Flocculation Mixer 2 1,5 75,0% xActiflo - Scraper 2 0,5 75,0% xActiflo - Microsand Recirculation Pump 4 5,0 75,0% xAllocation - Dosing Pump 5 0,5 75,0% x

Electrical consumption (PRELIMINARY)

Application Number of unitsInstalled HP (unit.)

Installed kW (unit.)

Load per unit (kW)

Number of hours per day (in h) (2)

Total kWh/d

Total kWh/yr

Actiflo - Pre-Coagulation Mixer 1 1,5 1,12 0,84 24 20,1 7 352Actiflo - Coagulation Mixer 1 1,5 1,12 0,84 24 20,1 7 352Actiflo - Flocculation Mixer 1 1,5 1,12 0,84 24 20,1 7 352Actiflo - Scraper 1 0,5 0,37 0,28 24 6,7 2 451Actiflo - Microsand Recirculation Pump 1 5,0 3,73 2,80 24 67,1 24 506Allocation - Dosing Pump 2 0,5 0,37 0,28 24 13,4 4 901

(2) To be adjusted based on project requirements(3) Preliminary - For information only TOTAL (3) 53 913

TOTAL FOR ESTIMATION (PRELIMINARY): 54 000

MOTOR LIST AND ENERGY CONSUMPTION

PRELIMINARY:Subject to changes Page 1 of 1

Project: Millbrook WWTP, ONID: 13TO01Version: ADate: 2013-01-25

Total Nominal flow: 2 520 m3/d

AlumCommercial strength @ 48,5% = 0,64 kg alum/L

MIN. AVERAGE MAX.Dosage (mg/L or g/m3) 70Dry weight per day (kg/d) 176,4Volume per day (L /d) 275,5Alum volume per year (m3/y) 101

Dry PolymerSolution concentration: 0,20% @ nominal flow = 0,20 g/L

MIN. AVERAGE MAX.Dosage (mg/L or g/m3) 0,8Dry weight per day (kg/d) 2,0Volume per day (L /d) @ 0,20% 1008,0Dry polymer dosage per year (kg/y) 736

Microsand

MIN. AVERAGE MAX.Losses (g/m3) 3,0Dry weight per day (kg/d) 7,6Microsand per year (kg/yr) 2759

ESTIMATED CHEMICALS CONSUMPTION

PRELIMINARY Page 1 of 1



BIOFOR®-N Biological Aerated Filter

Infilco Degremont Inc.

BIOFOR®-N Biological Filtration System Design Proposal

Project: Millbrook, Ontario Biofor® Prepared For: R.V. Anderson Associates Limited

Proposal No. 50136737.01 Date: January 14, 2013

INFILCO DEGREMONT INC. 8007 DISCOVERY DRIVE, RICHMOND, VA 23229 USA P.O. BOX 71390, RICHMOND, VA 23255-1390 USA TEL 804 756-7600 | FAX 804 756-7643

January 15, 2013 Valera Saknenko

R.V. Anderson Associates Limited Re: Millbrook Biofor® Township of Cavan Monaghan Inquiry No. 50136737.01 Dear Valera: With regard to your request for a BIOFOR® design for Millbrook, IDI is pleased to submit the following preliminary design proposal. This proposal describes a Single Stage BIOFOR® - N design for Ammonia removal of secondary treatment. The goal was to achieve an effluent of Ammonia < 2 mg/l during summer temperatures and Ammonia < 1mg/l during winter temperatures. We have assumed a design temperature of 10 degrees C in the winter and 20 degrees C in the summer. The system is sized for 2520 m3/d. The Biofor® - N consists of two (2) filters. The design is based on treating the design flow and loads with One (1) filter under backwash / out-of-service in. We have assumed concrete filter cells (by others) in this proposal. It is also important to note that this system was designed for BOD and TSS effluent limits of < 10 mg/l

We have endeavored to provide complete information in this proposal. However, if you have any questions or need additional information, please do not hesitate to contact Amit Kaldate, our Biological Systems Manager or me directly. Sincerely,

Lee Stewart Application Engineer - Biological Systems Group

BIOFOR System

TABLE OF CONTENTS

1. BIOFOR - General Description ........................................................................ 1

2. Design Conditions ............................................................................................... 3

3. Description of Operation .................................................................................... 4

4. BIOLOGICAL REACTORS ..................................................................................... 5

BIOFOR®-N ........................................................................................................... 5 BACKWASHING ...................................................................................................... 5 BIOFILTER MODULES ............................................................................................. 6 MEDIA AND SUPPORT GRAVEL ............................................................................... 6 BIOFOR®-N ........................................................................................................... 6 CENTRIFUGAL PUMPS ............................................................................................ 6 BIOFOR®-N ........................................................................................................... 6 BLOWERS AND APPURTENANCES ............................................................................ 7 BIOFOR®-N ........................................................................................................... 7 COMPRESSED AIR FOR AUTOMATIC VALVES ............................................................ 8 AUTOMATIC AND MANUAL VALVES (IN INCHES) ........................................................ 8 BIOFOR®-N ........................................................................................................... 8 COMMON VALVES (IN INCHES) ................................................................................ 8 STRAINERS ........................................................................................................... 9 BIOFOR®-N (IN INCHES) ......................................................................................... 9 CONTROLS AND INSTRUMENTATION ........................................................................ 9 Control System ................................................................................................................ 9 Field Instruments, Biofor-N .............................................................................................. 9 General Instruments ...................................................................................................... 10 BIOFOR®-N (IN INCHES) ....................................................................................... 10 FIELD SERVICE ................................................................................................... 10

Budget Estimate ............................................................................................................11

BIOFOR® SYSTEM

Millbrook, Ontario Biofor® Inquiry No. 50136737.01 1

1. BIOFOR - General Description The BIOFOR is a biological, submerged filter containing a fixed, dense granular bed with influent wastewater flowing in the upward direction. The BIOFOR Process is applied individually or in separate stages for carbonaceous BOD5 reduction (BIOFOR-C), nitrification (BIOFOR-N), and denitrification (BIOFOR-Pre-DN, BIOFOR-Post-DN). In aerated systems (C and N), process air is introduced at the bottom of the media bed and flows co-currently with the influent wastewater. The BIOFOR is based on the following basic principles:

A single layer of granular BIOLITE™ media for biomass attachment and retention of suspended solids.

A discrete process air distribution system (for aerated systems only) Upflow, co-current distribution of air and water Backwash sequence automated and optimized per application requirements

BIOLITE™ Media BIOLITE media is an expanded clay material with a high specific surface area, low density, and good resistance to attrition. The porosity of the material ensures biomass attachment. Different particle sizes ranging from 1mm to 5mm are available depending on the application. OXAZUR® Air Diffusers OXAZUR® air diffusers, present in all aerated BIOFOR® units, are aerating devices with elastic rubber membranes enclosed in a polypropylene casing. The diffusers are installed on a series of process air distribution pipes located at the bottom of the media bed, directly above the plenum. The combination of diffused air and media retention produces a highly efficient aeration system with fine bubble diffusion characteristics. In order to assure homogeneous distribution over long-term operation, a pressurized cleaning water system is provided and operated approximately once per month to flush the diffusers. Upflow Distribution of Air and Water Distribution of process air and influent wastewater is upward through the BIOLITETM media. This co-current, upward flow ensures an even distribution of water and air. It enables the media to retain solids and biomass throughout the entire bed depth and prevents short-circuiting and gas entrapment. In anoxic, denitrifying systems, nitrogen gas bubbles are continuously and effectively released from the media to atmosphere. The media operates in slight expansion, thereby ensuring full use of the available media volume and allowing high hydraulic loading rates.

BIOFOR® SYSTEM


MONOFLOR® Underdrain

Concrete BIOFOR installations have the distribution nozzles located in the poured-in-place filter floor. To ensure an accurate, grout-free installation, the MONOFLOR underdrain is used. This underdrain is simple to install, leak-proof, and has been widely used on filter systems for many years. Backwash Sequence Backwash sequences for biological filters must comply with several requirements:

The entire filter bed must be cleaned of retained solids and excess biomass Sufficient biomass must remain in the reactor following a backwash Air and water flows must not cause filter media to be lost Water and energy consumption must be minimized The backwash sequence must be initiated and carried out automatically.

The standard BIOFOR backwash sequence has been developed specifically to meet the requirements listed above. The backwash sequence may be optimized during start-up and can be modified based on operating experience. The sequence may be initiated manually, on operating time, or upon reaching a pre-set terminal headloss. The main steps of the sequence are:

Quick drain to backflush the influent distribution nozzles Air scour A series of simultaneous air/water washes Water rinse

The water used for backwashing is typically Biofor effluent that is stored in a separate clean water tank. Backwash wastewater is normally stored in a separate holding tank and pumped over time back to the head of the treatment plant.

BIOFOR® SYSTEM


2. Design Conditions The BIOFOR® - N biological aerated filter system described herein is a single-stage wastewater treatment system designed for the removal of Ammonia. The system will have a design flow capacity of 2,520 m3/d. The design is based on treating process wastewater with the following influent characteristics:

Influent Assumed (After Secondary Clarifier)Biological Oxygen Demand (BOD5) – mg/L 20 Total Suspended Solids (TSS) – mg/L 20 Total Kjeldahl Nitrogen (TKN) – mg/L 25 Design Water Temperature: Minimum - °C 10

The BIOFOR® - N system described herein shall be designed to achieve the following effluent quality for the specified flow:

Effluent Requirements mg/lAmmonia-N (NH3) (Summer)– mg/L < 1 Ammonia-N (NH3) (Winter)– mg/L < 2

Biological Oxygen Demand (NO3) – mg/l < 10Total Suspended Solids (TSS) – mg/L < 10

The BIOFOR® - N system consists of two (2) filter cells total. The N-Stage filters are sized at 20.9 m2 (1.5 m W x 1.3 m L). The entire unit is roughly 7.315 m tall. The system will be capable of treating the peak flow of 8,242 m3/d, with the potential for one (1) off-line filter cell in each stage at any given time.

BIOFOR® SYSTEM


3. Description of Operation The influent wastewater is pumped to a common flow channel for the BIOFOR-N unit and is then evenly distributed to the cells through a series of weirs in the central gallery. Wastewater to be treated is introduced into the plenum and flows upward through the BIOLITE® media. As the wastewater and process air flows co-currently through the media bed, attached heterotrophic biomass oxidizes the carbonaceous compounds. Autotrophic biomass also oxidizes the ammonia, and suspended solids along with biomass are retained. Process air, required for biomass growth and activity, is injected through an air distribution system located within the gravel bed immediately above the plenum. As proposed, each Biofor cell has its own dedicated positive displacement process air blower. Due to solids retention and biomass growth within the filter media, backwashing of the Biofor units is necessary to remove retained solids and maintain a thin, active biofilm. Backwashing is initiated either manually or automatically based upon elapsed time or on reaching a pre-set terminal headloss. The backwash sequence includes a number of distinct steps, the duration and extent of each step being optimized during plant start-up and modified based on operating experience. The basic backwash sequence includes the following steps: Quick drain to backflush the underdrain nozzles Air scour Combination air and water backwash Water rinse Repeat of the above steps three times Water rinse with influent wastewater (filter to waste)

A centrifugal pump from the clearwell supplies clean water used for backwashing the cells. The backwash water flow rate can be controlled with an automatic flow control valve while a positive displacement blower supplies air for the air scour. Spare, installed units are provided for both the air scour blower and backwash water supply pump. Wastewater from the quick drain step is collected in a drain sump and typically flows into the backwash waste tank. Wastewater from the remaining steps collects in a common backwash flume and flows to the backwash waste storage tank. Stored backwash wastewater is normally returned to the head of the plant; if necessary, it may need to be treated in a separate side stream due to backwashing considerations.

BIOFOR® SYSTEM


4. BIOLOGICAL REACTORS

Infilco Degremont, Inc. will provide an upflow biological aerated fixed-film reactor as described with BIOLITE® media for biomass support.

Biofor®-N

Design Unit Filtration Area 20.9 m2

Total Number of Cells 2 Biolite® Media Depth 3.68 m

Each reactor in the N-Stage will consist of a concrete tank with monolithic underdrain (MONOFLOR®), bottom influent and air/water backwash distribution system, process air distribution system, granular expanded clay media, gravel support bed, influent channel, effluent and backwash waste channels with stilling baffle. Common instrumentation furnished by IDI includes: process air blowers, air distribution system cleaning pump, air scour blowers, backwash pumps, controls and instrumentation and all associated automatic valves and skid piping.

Backwashing The media will be periodically washed by a sequence of air scour, combination air scour/backwash water, and water only rinse steps. Water used to backwash the biofilter will be pumped from a separate storage tank supplied by others.

BIOFOR® SYSTEM


SCOPE OF SUPPLY Complete IDI Scope of Supply:

Biofilter Modules BIOFOR® – N Reactor, with all internals and required wall pieces.

Each reactor will include the following: Equipment for MONOFLOR® underdrain including forms, polyethylene nozzles

and accessories. 1 - Tranquilizer (stilling) baffle consisting of staggered vertical aluminum slats

extending across the width of the reactor. Installation of the tranquilizer baffle is by others.

Media and Support Gravel

Support gravel, .3048 m (meters) depth in both the BIOFOR N Stages (includes 5% extra)

BIOLITE-“L” media, 2.7mm, to 3.68 m depth in the BIOFOR-N reactors (includes

10% extra)

Biofor®-N

Design 2 Filters

Total Support Gravel Volume - m3 22.37 Biolite “L” 2.7 Media Volume - ft3 169.6

Centrifugal Pumps 2 - Backwash supply pumps, horizontal centrifugal type rated for 60' TDH (1 x 100% duty)

Biofor®-N

Design Flow

Backwash Pump Capacity 10,448 lpm Cleaning Pump Capacity 2,612 lpm

BIOFOR® SYSTEM


Blowers and Appurtenances

2 - Air scour blowers, rotary lobe type, rated for 10.5 psig (1 x 100% duty)

Biofor®-N

Design Flow

Process Air Blower Capacity 133 scfm Air Scour Blower Capacity 1,188 scfm

Each blower provided with: Motor V-belt drive Inlet filter/silencer and outlet silencer Check valve Manual valve for outlet isolation Relief valve Flexible connections Discharge pressure gauge Acoustic enclosure, to meet 85 dBA free field noise requirements. Blowers shipped to site skidded on separate structural steel bases, assembled with piping, silencers, valves and fittings. An automatic by-pass flow control valve is included with each air scour blower.

BIOFOR® SYSTEM


Compressed Air for Automatic Valves

1 - Compressed Air System, comprising: 1 - dual-head reciprocating type compressor rated for 7.5 scfm at 100 psig 1 - standby head 1 - 100 gallon carbon steel receiver Air dryer Required relief, exit, and blowdown valves Pressure gauges System shipped to site pre-piped and skidded on a structural steel base. Pneumatic tubing, valves, and appurtenances for air feed to automatic valves are by others.

Automatic and Manual Valves (In Inches)

Biofor®-N

Biofor N Valve Type - Open/Close Quantity Diameter

Influent 1 14” Backwash Water Inlet 1 12”

Air Scour Inlet 1 8” Air Cushion Vent 1 2.5”

Process Air, Cleaning Water 1 3” Backwash Waste 1 14”

Quick Drain 1 6”

Common Valves (In Inches)

Design Valve Type – Modulating Quantity Diameter

Air Scour Vent Flow Control 1 8” Backwash Water Flow Control 1 12”

BIOFOR® SYSTEM


All automatic valves are butterfly type equipped with double-acting pneumatic cylinder actuators. Solenoids are mounted directly on actuators. Positioners are pneumatic. Valves include open and close limit switches.

There are no manual valves included in IDI’s Scope of Supply.

Strainers

Biofor®-N (In Inches)

Design Strainer Type Quantity Diameter

Oxazur Cleaning Strainer 1 8” Backwash Inlet Strainer 1 12”

Backwash inlet strainers – In-line Y-Type, (one per system with one spare), 2.4-

mm stainless steel mesh, carbon steel body with flanged ends. Air distributor cleaning header strainers – in-line Y-Type, 2.4-mm stainless steel

mesh, carbon steel body with flanged ends. All required process flow strainers, 2-4 mm stainless steel mesh (inline or static).

Controls and Instrumentation

Control System

1 - PLC/PC control system, mounted in a free-standing NEMA 12 enclosure.

Field Instruments, Biofor-N

Quantity Field Instruments – Lot

Pressure Transmitters (Cell) 2 Pressure Transmitters (Plenum) 2

BIOFOR® SYSTEM


General Instruments

Biofor®-N (In Inches)

Design General Instruments – Lot Quantity Diameter

Backwash Flowmeter/Transmitter 1 12” Air Scour Flowmeter/Transmitter 1 8”

Level Transmitters* 4 N/A Strainer Differential Pressure Gages 1 14”

* Ultrasonic Level Transmitters located at Clearwell, Mudwell and individual cells

Field Service 30 - Days total service time by a qualified, factory-trained service engineer to

inspect the Biofor equipment installation, provide start-up assistance and training of operations personnel.

Also included: Four (4) O & M Manuals.

BIOFOR® SYSTEM


Budget Estimate PURCHASE PRICE: As Advised By Rep (Exclusive of taxes per Condition 6 of IDI Conditions of Sale) Our price is based on IDI's standard terms and conditions, which can be provided upon request. The above price in this proposal is tied to the London Metal Exchange index for stainless steel finished products and stainless steel rolled coil. . FOB shipping point, freight allowed. TERMS OF PAYMENT (as follows, subject to Condition 2 of IDI Conditions of Sale): 10% Net Cash, Payable in thirty (30) days from date of submittal of initial drawings for approval; 85% Net Cash, Payable in progress payments thirty (30) days from dates of respective shipments of the Products; 5% Net Cash, Payable in thirty (30) days from Product installation and acceptance or ninety (90) days after date of final Product delivery, whichever occurs first.



DynaSand® Continuous Backwash Filter

Parkson Corporation

Rev 8e Rev Date: 5/25/12

APPLICATION :

DESIGN DATA Temp TSS TP TNdeg C mg/L mg/L mg/L

Peak: m3/hr = 3 MLD Influent 7 25 25 1Design: m3/hr = 2.5 MLD Effluent 5 0.1

* - All effluent limits may require chemical addition (by others)RECOMMENDATIONS:

4 DynaSand filter modules for installation in concrete tanks

No. modules per cell 1 modules No. of filter cells 4 cellsFiltration area per module 4.65 m2 Filtration area per cell 4.65 m2Loading Rate: Peak: 8.97 m/hr, 1 cell out of service Total filtration area 18.6 m2

Design: 5.61 m/hr, all cells in serviceFiltration depth 2 m Total sand requirement 65 MTSand required per module 16 MT Typical headloss across filter 46 to 61 cmDesign headloss across filter 122 cm WC Recommended Compressor Package: Rotary ScrewTotal air consumption 17.7 Stdm3 Compressor Type DuplexTotal reject flow per unit 0.44 to 0.88 L/Sec intermittently Package #: EW-5-DD

Ingersoll-Rand Model : UP6-5-125Filter plant dimensions 5.2 m - Length 6.5 m - Width Motor horsepower: 5 hp

7.2 m - Depth Dryer Type: DesiccantDryer Dew Point: -40 deg C

Total Estimated concrete volume: Qty: 1Structural: 109 m3 Grouting: 25 m3

MATERIALSFeed Manifold: PEFeed Assembly: FRPHardware: 304SSReject compartment and lower stay-in-place mold: FRPAirlift pump: PVC

SCOPEAll filter internals, filter mediaEcoWash* intemittent backwash system including FRP NEMA 4X Central Control Panel and FRP NEMA 4X Air Control Panel.Local headloss gauge, low level float switchGrating over the filter cell supplied by Parkson, Handrails by others (includes grating over feed channel).Compressor package supplied by Parkson.Start-up visit including travel & living expenses.

BUDGET PRICING USD, FOB factory - Equipment & sand freight allowed, taxes extra.

SHIPMENTSubmittals 5 weeks after receipt of written purchase order.Shipment 13 weeks after receipt of approved drawings or submittal waiver.

ON-SITE INSTALLATIONConcrete installed at $654 x 109 m3 =Grout(fill) installed at $163 x 25 m3 =Internals installed at $35 x 96 hours =

Estimated installation cost =Estimated total installed cost =

* EcoWash - PLC control system with HMI, SCADA Ethernet communication, and optional remote monitoring.

0RM: Jean Grenier

pH

$296,000

$71,601

125104

1401 W. Cypress Creek Road, Fort Lauderdale, FL 33309 tel: (954) 974-6610 fax: (954) 974-6182

DYNASAND® SAND FILTER with ECOWASH™ INTERMITTENT BACKWASH SYSTEM

Preliminary BUDGET SizingMILLBROOK, ON

Municipal Biological

NO-x-Nmg/L

TurbidityNTU

16-Jan-13

$4,065$3,360

$79,026$375,026

Rev 8e Rev Date: 5/25/12

APPLICATION :

DESIGN DATA Temp TSS TP TNdeg C mg/L mg/L mg/L

Peak: m3/hr = 3 MLD Influent 7 25 60 1Design: m3/hr = 2.5 MLD Effluent 5 0.1

* - All effluent limits may require chemical addition (by others)RECOMMENDATIONS:

6 DynaSand filter modules for installation in concrete tanks

No. modules per cell 1 modules No. of filter cells 6 cellsFiltration area per module 4.65 m2 Filtration area per cell 4.65 m2Loading Rate: Peak: 5.38 m/hr, 1 cell out of service Total filtration area 27.9 m2

Design: 3.74 m/hr, all cells in serviceFiltration depth 2 m Total sand requirement 98 MTSand required per module 16 MT Typical headloss across filter 46 to 61 cmDesign headloss across filter 122 cm WC Recommended Compressor Package: Rotary ScrewTotal air consumption 26.5 Stdm3 Compressor Type DuplexTotal reject flow per unit 0.44 to 0.88 L/Sec intermittently Package #: EW-5-DD

Ingersoll-Rand Model : UP6-5-125Filter plant dimensions 7.7 m - Length 6.5 m - Width Motor horsepower: 5 hp

7.2 m - Depth Dryer Type: DesiccantDryer Dew Point: -40 deg C

Total Estimated concrete volume: Qty: 1Structural: 159 m3 Grouting: 37 m3

MATERIALSFeed Manifold: PEFeed Assembly: FRPHardware: 304SSReject compartment and lower stay-in-place mold: FRPAirlift pump: PVC

SCOPEAll filter internals, filter mediaEcoWash* intemittent backwash system including FRP NEMA 4X Central Control Panel and FRP NEMA 4X Air Control Panel.Local headloss gauge, low level float switchGrating over the filter cell supplied by Parkson, Handrails by others (includes grating over feed channel).Compressor package supplied by Parkson.Start-up visit including travel & living expenses.

BUDGET PRICING USD, FOB factory - Equipment & sand freight allowed, taxes extra.

SHIPMENTSubmittals 5 weeks after receipt of written purchase order.Shipment 13 weeks after receipt of approved drawings or submittal waiver.

ON-SITE INSTALLATIONConcrete installed at $654 x 159 m3 =Grout(fill) installed at $163 x 37 m3 =Internals installed at $35 x 144 hours =

Estimated installation cost =Estimated total installed cost =

* EcoWash - PLC control system with HMI, SCADA Ethernet communication, and optional remote monitoring.

0RM: Jean Grenier

16-Jan-13

$6,098$5,040

$115,045$476,045

NO-x-Nmg/L

TurbidityNTU

1401 W. Cypress Creek Road, Fort Lauderdale, FL 33309 tel: (954) 974-6610 fax: (954) 974-6182

DYNASAND® SAND FILTER with ECOWASH™ INTERMITTENT BACKWASH SYSTEM

Preliminary BUDGET SizingMILLBROOK, ON

Municipal Biological

pH

$361,000

$103,907

125104



Z-PAK™ Membrane Ultrafiltration



Budget Proposal for

Millbrook WWTP Expansion – Tertiary UF Option Z-PAKTM Ultrafiltration Water Treatment System Submitted to:

R.V. Anderson 2001 Sheppard Avenue East Suite 400 Toronto ON M2J 4Z8 Attention: Valera Saknenko, Ph.D., P.Eng., PMP Senior Associate

January 14th, 2013 Proposal Number : 759344

GE Water & Process Technologies Geoff Totten, Regional Sales Manager Tel: (905) 465-3030 Email: [email protected] Local Representation By:

Pro Aqua Inc. Scott Lenhardt, P.Eng. 416-861-0237 x 228 905-330-9244 Cell Email: [email protected]


GE Water & Process Technologies Confidential and Proprietary Information

GE Water & Process Technologies (“Seller”) submits the information contained in this document for evaluation by R.V. Anderson (“Buyer”) only. Buyer agrees not to reveal its contents except to those in Buyers organization necessary for evaluation. Copies of this document may not be made without the prior written consent of Sellers Management. If the preceding is not acceptable to Buyer, this document shall be returned to Seller.


GE Confidential and Proprietary Information

Page 3

Table of Contents 1 Technical and Engineering Details ........................................................................ 4

1.1 Basis of Design .......................................................................................................................... 4

1.2 Proposed System Configuration ........................................................................................ 4

2 System Process Description and Scope ................................................................ 6

2.1 ZeeWeed® 1500 Process Description ............................................................................. 6

2.2 Scope of Supply by GE ........................................................................................................... 7

3 Buyer Scope of Supply ............................................................................................ 10

4 Commercial Offer .................................................................................................... 12

4.1 Pricing ......................................................................................................................................... 12

4.2 Power & Chemical Consumption Estimates .............................................................. 12

4.3 Equipment Shipment and Delivery ................................................................................ 12

4.4 Freight ........................................................................................................................................ 13

4.5 Bonds .......................................................................................................................................... 13

4.6 Pricing Notes ........................................................................................................................... 13

4.7 Conditional Offering ............................................................................................................. 13



Page 4

1 Technical and Engineering Details

1.1 Basis of Design This proposal is based on the design values in this section.

The proposal reflects the Seller supplying a Z-PAK™ 550 Ultrafiltration Tertiary Water Treatment System, for the Millbrook WWTP Expansion project, designed to treat a net permeate (UF treated water) flow of 2,520 m3/day and a Peak Hour Flow of 5,800 m3/day.

Design Conditions

Design Temperature Range 8 – 25 °C

Design Capacity (Net) With All Trains In Service At 8°C 4,000 m3/day

Peak Capacity (Net) With All Trains In Service At 8°C 1 5,800 m3/day

Design Capacity (Net) With One Train Out Of Service At 8°C 2 2,520 m3/day

Recovery (at design capacity) 90%

Note 1: The maximum flow rate sustained over a 6-hour period.

Note 2: For up to 24 hours

Physical Parameters

The assumed settled water quality from the clarifiers is described below:

Parameter Source Units Average

Minimum Influent Temperature

Given ºC 8

BOD5 Assumed mg/L 5

Average TSS Assumed mg/L 10

Peak TSS Assumed mg/L 20

TP Assumed mg/L 0.5

Ratio of TSS/Turbidity Assumed n/a 1.5

Permeate Water Quality

Parameter Treated Water

TSS ≤ 5 mg/L

Turbidity < 1 NTU

1.2 Proposed System Configuration The proposed system configuration has been based on the water quality as shown in Section 1.1.



Page 5

Parameter Quantity

Z-PAKTM Model 550 6” skid

Ancillary Skid Model Duplex Type of Membrane ZeeWeed® 1500 Module Surface Area (ft2/m2) 550/51.1 Number of Trains 2 Number of 24-Module Rack(s) Per Train 3 Number of Installed Modules Per Train 56 Spare Space (%) 22 Maintenance Clean (MC) Protocol 1/day/train Recovery Clean (RC) Protocol 12/year/train sodium

hypochlorite followed by citric acid



Page 6

2 System Process Description and Scope

2.1 ZeeWeed® 1500 Process Description

ZeeWeed® water treatment is a process technology that produces high quality treated water by filtering water through GE Water & Process Technologies proprietary and patented pressurized ZeeWeed® ultrafiltration membranes. ZeeWeed® 1500 Series membrane utilize "Outside-In" flow, through a hollow-fiber membrane. The small pore size of the ultrafiltration membrane excludes particulate matter from the treated water.

The membranes operate under pressure from a feed pump. Treated water is pumped through membrane pores and enters the inside of the hollow fibers. Water then flows to the treated water storage tank (or distribution system). During backpulsing, air is introduced at the bottom of the membrane modules to create turbulence along the membrane surface. Rising air bubbles scour and clean the outside of the membrane fibers, maximizing membrane performance.

With a ZeeWeed® membrane water treatment system, removal of turbidity requires no process chemicals. On water sources where dissolved contaminants are not a concern, raw water may be fed directly to the membrane filters for a single stage treatment process. In a single stage treatment system, there is no need for coagulants as ZeeWeed® membranes effectively replace both the clarifier and granular media filters found in conventional water treatment plants. This

results in significantly easier control for plant operators, eliminates the need for coagulants and substantially reduces the plant footprint. Alternatively, the membranes may follow flocculation and settling processes replacing the media filters in a conventional system. The ZeeWeed® membrane process can consistently produce high quality water.

ZeeWeed® 1500 Membranes can produce consistent, exceptional quality treated water.



Page 7

2.2 Scope of Supply by GE

GE’s scope of supply for a Z-PAKTM 550 Ultrafiltration Water Treatment System, for the Millbrook WWTP Expansion project, is as follows:


1

Pre-treatment System

- one (1) in-line static mixer, supplied loose

- one (1) pH probe and transmitter, supplied loose

1

pH Adjustment/Coagulant/Oxidant Chemical Feed System

Includes one (1) panel mounted chemical dosing pump, associated isolation valves, calibration column, pressure relief valve, backpressure valve, pressure gauge and level switch. Piping contained on the panel will be PVC.

2

Process Skid(s)

Each skid includes:

- one (1) centrifugal end suction base mounted feed pump with a VFD operated motor (VFD by GE) complete with isolation and check valves, and inlet and discharge pressure gauges

- one (1) automatic backwash strainer complete with required isolation valves, instrumentation and local control panel

- one (1) feed flow magmeter

- one (1) set of valves, pressure transmitters, pressure gauges, and pressure switches installed on the feed side of the membrane modules

- one (1) set of valves, vents and pressure transmitters installed on the permeate side of the membrane modules. Includes valve to supply backwash water to the membrane racks and valves for chemical solution recirculation.

- one (1) set of valves and vents installed on the backwash waste line

- one (1) turbidimeter complete with isolation valves

- all piping contained on the skid is PVC except air lines: Sch 10 316L SS.

2 ZeeWeed® 1500 24-Module Racks (3 per membrane train), skidded and pre-assembled. Includes feed, permeate, waste and air lines.

2 ZeeWeed® 1500 Membrane Modules (56 per membrane train)

1

Ancillary Skid – Duplex

Backwash Skid:

- one (1) duty and one (1) stand-by end suction centrifugal backwash pumps with VFD operated motors (VFD by GE)

- one (1) set of isolation, check valves, inlet and discharge pressure gauges, and pressure switches

- one (1) backwash flow magmeter

- all piping contained on the skid is PVC

1

Ancillary Skid – Duplex

CIP Skid:

- one (1) duty and one (1) stand-by end suction centrifugal CIP pumps with VFD operated motors (VFD by GE)

- one (1) set of isolation, check valves, inlet and discharge pressure gauges, and pressure switches

- one (1) CIP flow magmeter



Page 8

- dosing ports for all cleaning and neutralization chemicals

- one (1) dual chlorine/pH analyzer and transmitter, installed with required isolation valves

- all piping contained on the skid is PVC

1

Process Air Flowmeter

Located on CIP Pump Skid with isolation valve and drain valve

Air piping on skid is Sch 10 316 L SS

1 Aeration Blowers (one (1) duty and one (1) stand-by) with VFD operated motors (VFD by GE), supplied loose, complete with required flow switches and isolation valves.

1 Backpulse Tank, supplied loose, complete with associated valves, and level transmitter.

1 CIP Tank, supplied loose, complete with associated valves, level and temperature transmitters.

1

Sodium Hypochlorite Chemical Feed System


1

Citric Acid Chemical Feed System


1

Sodium Hydroxide Chemical Feed System


1

Sodium Bisulfite Chemical Feed System


1 Air Compressors (one (1) duty and one (1) stand-by), supplied loose and mounted on horizontal air receiver tanks, complete with associated valves, pressure switch and gauge, auto drain, and local control panel with motor starter.

1

Air Dryer, supplied loose, complete with associated isolation valves.

1

Allen-Bradley PLC system complete with one (1) HMI located on the Master Control Panel and 2 remote I/O train panels Note 2

The Master Control Panel is located on the CIP pump skid

The remote I/O train panels are located on each of the Process Skids

Miscellaneous

Slings for transporting modules during installation and repair

General

Engineering Services including Trips to Site or the Engineer’s Office During the Design Phase of the Project

Equipment P&IDs, Electrical, and General Arrangement Drawings

Operating & Maintenance Manuals

Field Service and Process Start-up Assistance Note 3

Operator Training Note 3

1 Year Mechanical Warranty on Equipment



Page 9

8 Year Membrane Warranty (First two (2) years are Full Replacement Warranty followed by six (6) Years Pro-Rated Warranty)

1 Year 24/7 Emergency Telephone Support

1 Year Remote Monitoring & Diagnostics - Monitor/Warranty/Lite Service Note 4

Note 1: It is assumed that all chemical day tanks or totes will be by others. GE’s chemical feed pump

panels may be wall-mounted over the Customer-supplied tank or tote and draw directly from the tank or tote.

Note 2: MCC and SCADA by others.

Note 3: 28 days over 3 trips have been included for equipment off-loading and installation assistance, commissioning and start-up assistance, membrane installation assistance, operator training, and performance testing.

Note 4: Includes data acquisition computer and software set-up.



Page 10

3 Buyer Scope of Supply

The following items are for supply by Buyer and will include but are not limited to:

� Overall plant design responsibility

� Review and approval of design parameters related to the membrane separation system

� Review and approval of GE supplied equipment drawings and specifications

� Detail drawings of all termination points where GE equipment or materials tie into equipment or materials supplied by Buyer

� Design, supply and installation of an Overhead Traveling Beam Crane and monorail beam, conductor bar system, interlocks, etc.

� Civil works, provision of main plant tank structures, buildings, equipment foundation pads etc. including but not limited to:

� Common channels, Housekeeping pads, Equipment access platforms, walkways, stairs etc.

� Flocculation tank

� Treated water storage tank, as required

� HVAC equipment design, specifications and installation (where applicable)

� UPS, power conditioner, emergency power supply and specification (where applicable)

� Plant SCADA system

� Acoustical enclosures for membrane blowers

� Process and utilities piping, pipe supports, hangers, valves, etc. including but not limited to:

• Piping, pipe supports and valves between GE-supplied equipment and other plant process equipment

• Piping between any loose-supplied GE equipment

� Electrical wiring, conduit and other appurtenances required to provide power connections as required from the electrical power source to the GE control panel and from the control panel to any electrical equipment, pump motors and instruments external to the GE-supplied enclosure

� Design, supply and installation of equipment anchor bolts, brackets, and fasteners for GE supplied equipment. Seismic structural analysis and anchor bolt sizing.

� Receiving, unloading and safe storage of GE supplied equipment at site until ready for installation

� Installation on site of all GE supplied loose-shipped equipment



Page 11

� Alignment of rotating equipment

� Raw materials, chemicals, and utilities during equipment start-up and operation

� Disposal of initial start-up wastewater and associated chemicals

� Laboratory services, operating and maintenance personnel during equipment checkout, start-up and operation

� Touch up primer and finish paint surfaces on equipment as required at the completion of the project

� Weather protection as required for all GE supplied equipment. Skids and electrical panels are designed for indoor operation and will need shelter from the elements.



Page 12

4 Commercial Offer

4.1 Pricing

Pricing for the proposed equipment and services as described in this budget proposal:

Budgetary System Price $ 894,000 CAD

All pricing is based on the operating conditions and influent analysis detailed in Section 1. Any pricing herein is for budgetary purposes only and does not constitute an offer of sale.

4.2 Power & Chemical Consumption Estimates

The data presented below is for information purposes only and is based on the design information provided by the Buyer and presuming that the equipment is operated according to the design basis and in accordance with Seller’s Operations and Maintenance manuals.

Daily power consumption estimate 1

Equipment kWh/day

Permeate Pumps 185

Backwash/CIP Pumps 20

Membrane Blowers 30

Air Compressors 6

Total 241 kWh/day

Note1: Power consumption estimate is calculated at ADF conditions

Annual chemical consumption estimate

Chemical L/year

Sodium Hypochlorite (10.3% w/w, SG: 1.168) 1,760

Citric Acid (50.0% w/w, SG: 1.24) 1,175 Note: Cleaning chemical consumption estimates based on the following frequencies and concentrations

summarized in the table below. Frequencies are assumed, actual frequency of maintenance and recovery cleans may change with final design, or may change once system is in operation.

Basis of chemical consumption estimate

Chemical Maintenance Clean Recovery Clean

Sodium Hypochlorite solution (10.3% w/w, SG: 1.168)

Frequency 6 times per week 12 times per year

Concentration 100 mg/L 500 mg/L

Citric Acid Solution (50.0% w/w, SG: 1.24)

Frequency 2 times per week 12 times per year Concentration 1,000 mg/L 2,000 mg/L

4.3 Equipment Shipment and Delivery

Equipment shipment is estimated at 24 to 28 weeks after order acceptance. The Buyer and Seller will arrange a kick off meeting after contract acceptance to develop a firm shipment schedule.



Page 13

Typical Drawing Submission and Equipment Shipment Schedule

4-6 weeks 2 weeks 18 - 20 weeks 2 weeks

Acceptance of PO

Submission of Drawings

Drawings Approval

Equipment Manufacturing

Equipment Shipment

Plant Operations Manuals

The delivery schedule is presented based on current workload backlogs and production capacity. This estimated delivery schedule assumes no more than two weeks for Buyer review of submittal drawings. Any delays in Buyer approvals or requested changes may result in additional charges and/or delay to the schedule.

4.4 Freight

The following freight terms used are as defined by INCOTERMS 2010.

All pricing is FCA from Oakville, ON.

4.5 Bonds

Performance or Payment Bonds are not included in the system price. These bonds can be purchased on request but will be at additional cost.

4.6 Pricing Notes

� All prices quoted are in Canadian Dollars.

� Any applicable sales or value added tax is not included.

� The Buyer will pay all applicable Local, Provincial, or Federal taxes and Duties.

� The equipment delivery date, start date, and date of commencement of operations are to be negotiated.

� Commercial Terms and Conditions shall be in accordance with Seller’s Standard Terms and Conditions of Sale.

4.7 Conditional Offering

Buyer understands that this proposal has been issued based upon the information provided by Buyer, and currently available to Seller, at the time of proposal issuance. Any changes or discrepancies in site conditions (including but not limited to system influent characteristics, changes in Environmental Health and Safety (“EH&S”) conditions, and/or newly discovered EH&S concerns, Buyer’s financial standing, Buyer’s requirements, or any other relevant change, or discrepancy in, the factual basis upon which this proposal was created, may lead to changes in the offering, including but not limited to changes in pricing, warranties, quoted



Page 14

specifications, or terms and conditions. Seller’s offering in this proposal is conditioned upon a full Seller EH&S, and Buyer financial review.

Millbrook WWTPJan-13

MBR


Installed

No. Units

Operating

at ADF

Design

Capacity

(per unit)

Operating

Capacity

(per unit)

Design TDH

or Discharge

Pressure

Operating

TDH or

Discharge

Pressure

Motor HP (per

unit)

Connected

Motor HP

(all units)

Hours of

Operation

per Day

Power Consumed

per Day



4 Bioreactor Aeration Blowers 2 1 600 scfm 583 scfm 8.9 psig 7.6 psig 40.00 HP 80.00 HP 24.00 hr 482 kW.hr

6 RAS pumps 2 2 1,271 USgpm 1,271 USgpm 10.0 ft 10.0 ft 7.50 HP 15.00 HP 24.00 hr 240 kW.hr

8 Air Compressors 2 1 20 scfm 20 scfm 100 psi 75 psi 7.50 HP 15.00 HP 4.00 hr 12 kW.hr


Daily Power Consumption 1,012 kW.hr

Tertiary UF


Installed

No. Units

Operating

at ADF

Design

Capacity

(per unit)

Operating

Capacity

(per unit)

Design TDH

or Discharge

Pressure

Operating

TDH or

Discharge

Pressure

Motor HP (per

unit)

Connected

Motor HP

(all units)

Hours of

Operation

per Day

Power Consumed

per Day


2 Backwash Pumps 2 1 840 USgpm 840 USgpm 115.3 ft 71.5 ft 50.00 HP 100.00 HP 1.00 hr 20 kW.hr


8 Compressors 2 1 20 scfm 20 scfm 100 psi 100 psi 7.50 HP 15.00 HP 2.00 hr 6 kW.hr


Daily Power Consumption 241 kW.hr

Documents

APPENDIX J TECHNOLOGY EVALUATION REPORT