### Attachment 1

Dickerson Generating Station Presentation1 

# Mirant: Who We Are

INDEPENDENT POWER COMPANY

**•** Make and sell electricity competitively, reliably, ethically, and safely

 

# 10 power plants in the US

 

# Approximately 10,000 MW of generating capacity ~ 10 million

homes

 

# Coal, natural gas, and oil fuel electric generation fleet



# • Mid

- Atlantic’s generation output sold to PJM wholesale electricity

market

**•** Mirant employs nearly 1,600 employees in the U.S.

# Summary of Mid

- Atlantic Air Pollution Control Projects

**•** Investing for the Future: Air Quality Control Systems (>$1.6B)

 

# Flue Gas Desulphurization (aka FGD or Scrubbers)

– Up to 95% removal of SO 2 

# for MD fleet

– Morgantown, Chalk Point and Dickerson Scrubbers placed in service December, 2009

 

# Selective Catalytic Reduction (SCR)

– Up to 90% removal of NOx for MD fleet

– Morgantown

• 

# Unit 1 placed in service June 2007

• 

# Unit 2 placed in service May 2008

– Chalk Point

• 

# Unit 1 placed in service May 2008

– Dickerson

• 

# Selective Non

- Catalytic Reduction (SNCR); Units 1, 2, 3 placed in service July 2009

 

# Together, FGDs and SCRs reduce ionic Hg by >80%

# • Flue Gas Desulphurization System

 

# One system for Units 1, 2 and 3

 

# ‘Wet’ scrubber technology



# • Removes ~ 95% of SO 2 

# from Flue Gas

 

# MDE regulations set annual tonnage limits

 

# Nearly 30,000 tons/year removed from the units



# • Creates a Commercially Saleable By

- Product

**•** SO 2 

# reductions help the State of Maryland achieve compliance with the National Ambient Air Quality Standard (NAAQS) for particulate matter smaller than 2.5 microns (PM 2.5) 

# SO 2 

# Control System at Dickerson

# Dickerson Generating Station

 Three coal

- fired boilers,

182 MW each

 Two Combustion Turbines (CTs),

167 MW each

 One 13 MW Blackstart CT

 Water source: Potomac River

 Emissions control units:

- Selective non

- catalytic reduction (SNCR)

- Electrostatic Precipitators

- Baghouse

- Flue Gas Desulfurization (FGD) System

# To reduce the SO2, NOx, and Hg emissions of coal combustion via

chemical reactions between water, flue gas, and limestone. 

# Purpose of FGD:

Limestone arrives in

trains Mixed with water to create slurry Stack gases routed

to absorber vessel

Wastewater (from IWWTP) and river water • Clean flue gas

• Wastewater

• Gypsum

# • 

# SO **2** 

# in flue gas reacts with water to create sulfurous acid ( H 2 

# SO 3 

# )

 

# H 2 

# SO 3 

# reacts with the calcium carbonate ( CaCO 3 

# ) in limestone slurry to create calcium sulfite (

CaSO 3 

# ), and liberates CO 2 

# as a gas & H 2 

# O as a liquid

• 

# O 2 

# is added by natural and forced oxidation

 

# CaSO 3 

# + 1⁄2 O 2 

# combine to produce gypsum (

CaSO 4 

# ) 

# FGD Chemistry7 

# FGD Waste Water Treatment

 Physical Chemical Treatment

 Metals Reduction



#  Biological Treatment

 Nitrogen Reduction

## Alkali (pH control) Organo

sulfide (metals precip.) Ferric

Chloride (coagulant) Polymer

Sludge

Tank Dewatering Sludge

Filtrate Treated

Wastewater



# ( to biological

treatment

or

backwash 

# ) Recycle Sludge

Cake FGD Purge

from
Hydroclones



## Clarification Hydrochloric

Acid

Gravity

Filtration

Backwash Stream Equalization 

# Physical Chemical System

Landfill

# Biological Treatment Stage

Performed downstream of physical

- chemical
treatment, after removal of TSS and

metals

 

# Nitrogen removal



# – Activated Sludge reactors to

remove N

– Nitrogen levels of discharge less than 4 ppm

# FGD Wastewater Treatment

Constituent Typical Influent (mg/L) Typical Effluent (mg/L)

TSS 10,000

- 40,000 <30.0

pH 4.5

- 6.0 6.5

- 8.5

As 0.05

- 3.0 <0.05

Cd 0.04

- 0.5 <0.10

Cr 0.3

- 5.0 <0.10

Cu 0.1

- 0.85 <0.10
Hg 0.05

- 0.8 <0.002

Ni 0.2

- 6.0 <0.3

Pb 0.1

- 3.0 <0.05

Zn 0.4

- 8.0 <0.10

Total N 20

- 290 <4.00 

# Physical Chemical System

Treatment Effectiveness11 

# Nitrogen Sources

 Makeup Water

 River Water

 Sewage Treatment Plant Effluent

 Industrial WWTP effluent

 Flue Gas

 Ammonia Slip from SCR/SNCR Equipment

 Nitrous Oxide (NOx)

 95% NO and 5% NO 2 

#  Nitrogen (N 2 

# )



#  FGD System Nitrogen Containing Additives

 Polymers, DBA, etc

### Attachment 2

Dickerson Generating Station FGD System Process Flow Diagram

### Attachment 3

Dickerson Generating Station FGD Wastewater Treatment System Process Flow Diagram

### Attachment 4

Dickerson Generating Station FGD Wastewater Treatment System DescriptionShaw Stone & Webster, Inc.

- Stoughton, MA 1 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] SYSTEM DESCRIPTION

The treatment system(s) for all three (3) stations utilize the same treatment processes.

**♦** General The FGD purge stream is unsuitable for reuse by other power plant facilities and therefore must be treated separately and discharged. The characteristics of this wastewater stream require extensive treatment. A dedicated FGD wastewater treatment system offered for this application consists of three (3) major sub

- systems:

**•** Physical/Chemical Treatment

**•** Biological Treatment System

**•** Sludge De watering System

The FGD purge stream is initially directed to the Purchaser

- supplied equalization tank to partially attenuate any chemical or hydraulic fluctuations resulting from the FGD operations. In addition, the equalization tank shall receive flow from the filtrate sump pumps, which consists of filtrate from the filter presses, backwash reject from the continuous backwash gravity filters, building trench drains and tank overflow.

At a fairly constant rate, flow from the equalization tank shall be pumped to reaction tank No. 1. The wastewater will cascade by gravity to reaction tank No. 2, then on to the solids contact clarifier and on to the heat exchanger feed tank. Reaction tank No. 1 and No. 2 are elevated chemical conditioning tanks where hea vy metal precipitation, reaction and coagulation are carried out prior to clarification.

In reaction tank No. 1, pH adjustment/gypsum “desaturation” is conducted. In the pH adjustment/gypsum “desaturation” phase, hydrated lime is added to elevate the pH to between 8.5 and 9.2 to aid in the precipitation of soluble metals as insoluble hydroxides and oxyhydroxides. This operating pH range has been selected to achieve optimal metals reduction while minimizing the formation of magnesium hydroxide which can o ccur at higher pH. The other function of the reaction tank is to provide “desaturation” of gypsum from the wastewater which has a tendency to be supersaturated when received from the FGD process. If not brought to equilibrium, this supersaturation can re sult in gypsum scale formation in the downstream wastewater treatment plant equipment. In order to achieve the “desupersaturation” operation in a controlled fashion via a crystal growth mechanism, sludge is recycled from the downstream solids contact clar ifier to provide seed crystals for gypsum nucleation. In addition, an organosulfide reagent is added to this tank to form organosulfide heavy metal complexes which have very low solubility products thus resulting in maximum heavy metal removal. Of partic ular importance for this project is the removal of mercury.

In reaction tank No. 3, ferric chloride is added to form a dense flocculant and enhance the settling characteristics of the precipitate. Additionally, the hydrolyzed form of this coagulant provi des precipitation sites for co

- precipitation of other metals.Shaw Stone & Webster, Inc.

- Stoughton, MA 2 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] One (1) 100 percent capacity solids contact clarifier will be provided for clarifying the chemically conditioned waste stream. Polymer shall be injected into each clarifier influent

line in or der to form a denser floc which in turn will enhance the settling characteristics.

Overflow from the solids contact clarifier will flow by gravity to the heat exchanger feed tank for subsequent transfer to the heat exchangers and on to the SBR influent eq ualization tank for subsequent batch transfer to the biological treatment system. Upstream of the heat exchanger feed tank, HCl is dosed into the wastewater to reduce the pH to approximately 7.5 to 8.0. A static type mixer is provided to enhance the pH a djustment process.

In order to discharge the treated effluent into the receiving body of water, the physical/chemical treated effluent must undergo further treatment in order to reduce the total nitrogen concentration.

The reduction of total nitrogen (am monia nitrogen and nitrates) is achieved by the use of a biological treatment process. In order to be in compliance with the discharge limitations for total nitrogen, the biological treatment system must first convert ammonia nitrogen to nitrates. This p rocess is termed nitrification and is achieved in the presence of oxygen thus the nitrification process is aerobic. After nitrification, nitrates are converted to elemental nitrogen (a gas) and this process is termed denitrification and is achieved in the absence of oxygen thus the denitrification process is anoxic.

The nitrification, denitrification and subsequent clarification processes could be carried out in a continuous flow system with separate tankage for each process step. However, if a

continuou s flow process is utilized, there is very little operational flexibility as the various process steps (nitrification, denitrification and clarification) are fixed based on the tank

volumes.

Recognizing on FGD applications that design values versus that wh ich may actually occur can vary, Siemens highly recommends the use of sequencing batch reactor (SBR) technology which greatly enhances the operational flexibility of the system.

The proposed biological treatment system shall consist of a SBR influent equa lization tank which is used to store the pH adjusted physical/chemical treatment effluent for subsequent batch transfer to the two (2) sequencing batch reactors which carry out the biological treatment process in adjustable batch cycles and a SBR effluent equalization tank which is used to store the batch biologically treated SBR effluent for subsequent polishing and transfer to the continuous backwash gravity filters for further suspended solids reduction.

The filtered effluent will flow by gravity to the treated water storage tank and shall be subsequently conveyed to the point of discharge by the treated wastewater discharge pumps. During low flow conditions and/or if the pH/TSS of the treated wastewater is out of compliance, the discharge pumps shall b e used to recycle flow back to the equalization tank for reprocessing.

Sludge from the solids contact clarifier is pumped via the sludge recycle/transfer pumps to the sludge holding tank. Dewatering is achieved by recessed plate and frame filter presse s. Filtrate from the dewatering operation, as well as any drain water, is directed to the filtrate sump and pumped to the equalization tank for subsequent treatment.Shaw Stone & Webster, Inc.

- Stoughton, MA 3 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] **♦** Equalization Tank

The equalization tank (100 percent capacity) will receive flow from the FGD purge pumps and the various waste streams from the filtrate sump.

The purpose of the equalization tank is to store the fluctuating flow/solids loads generated by the FGD system so that a fairly constant flow rate/solids load can be conveyed to th e downstream treatment system. By obtaining

- maintaining a fairly constant flow rate/solids load to the downstream treatment system, a fairly constant treatment performance can be achieved/maintained with less operator attention.

As a means of blending th e waste streams and in order to prevent the settling out of solids, the equalization tank will be equipped with a bridge

- mounted propeller type mixer.

Morgantown

Station Dickerson

Station Chalk Point

Station Horsepower 20 15 15 Mixing Intensity (HP/m illion gallons) 279 363.7 363.7 Pumping Rate (gpm) 106,904 67,545 67,545 Turnover Rate (once every) 40 seconds 36.6 seconds 36.6 seconds

The equalization tank will also be equipped with anti

- vortexing baffles, equally spaced around the perimeter of the tank.

Wastewater forwarding pumps will be used to supply a fairly constant flow rate to reaction tank No. 1. The pumps will be controlled by an ultrasonic level control provided by Siemens.

The equalization tank will be of field erected carbon steel co nstruction provided by Shaw Stone & Webster, with an operating capacity based on a 1 ft

- 6 in. freeboard and as follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Diameter (ft) 29 22 22 Height (ft) 16 16 16 Operating Capacity (gallons) 7 1,645 41,232 41,232 Hydraulic Retention Time (hours) 5.97 6.25 6.25 Transfer Rate (gpm) 263 145 145

**♦** Wastewater Forwarding Pumps A/B [P&ID D

- 603

- Sheet 02]

Two (2) 100 percent capacity, skid

- mounted wastewater forwarding pumps will be provided.

The w astewater forwarding pumps will be horizontal, centrifugal, rubber lined, belt

- driven
type.Shaw Stone & Webster, Inc.

- Stoughton, MA 4 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] Each wastewater forwarding pump shall be rated as follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Capacity (gpm at ft TDH) 263 at 70 145 at 7 0 145 at 70 Horsepower 15 7.5 7.5

The wastewater forwarding pump set shall be provided with pneumatically actuated suction and discharge valves which will allow for automatic forward/back flushing of either the suction or discharge lines.

The common di scharge line of the wastewater forwarding pumps to reaction tank No. 1 will be equipped with a Siemens

- supplied flow meter for monitoring/ controlling the forward flow

rate to the reaction tank via the VFD.

Each pump discharge will be provided with a pr essure indicator.

**♦** Reaction Tank No. 1 The wastewater forwarding pumps will discharge into the 100 percent capacity reaction tank
No. 1. From reaction tank No. 1, the tank contents will be blended with the solids contact clarifier recycled solids along w ith lime, where pH adjustment/gypsum “desaturation” is

conducted.

The pH adjustment/gypsum “desaturation” process is achieved by the addition of hydrated lime, which elevates the pH to a range of 8.5 to 9.2. The addition of the hydrated lime is

controlle d by the influent flow meter and trimmed pH monitor/controller. In addition, an organosulfide reagent is added/blended with the influent stream to form organosulfide heavy metal complexes which have very low solubility products, thus resulting in maximum heavy

metal reduction.

Reaction tank No. 1 will be equipped with anti

- vortex baffles and a bridge

- mounted agitator to maintain solids suspension and to blend the liquid stream with the ferric chloride. The

effluent from reaction tank No. 1 will flow to th e reaction tank No. 2. The agitator will provide a mixing energy intensity as follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Horsepower 7.5 7.5 7.5 Mixing Intensity (HP/million gallons) 537.3 773.5 773.5 Pump Rate (gpm) 19,761 19,7 61 19,761 Turnover Rate (once every) 42.3 seconds 29.4 seconds 29.4 secondsShaw Stone & Webster, Inc.

- Stoughton, MA 5 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] Reaction tank No. 1 will be of steel construction and will provide the operating conditions as

follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Diameter (ft ) 12 10 10 Height (ft) 18 18 18 Operating Capacity (gallons) 13,958 9,693 9,693 Hydraulic Retention Time (minutes) 48 60 60

**♦** Reaction Tank No. 2

The wastewater forwarding pumps will discharge into the 100 percent capacity reaction tank

No. 2. From r eaction tank No. 2, the tank contents will be blended with the solids contact clarifier recycled solids along with lime, where pH adjustment/gypsum “desaturation” is

conducted.

The pH adjustment/gypsum “desaturation” process is achieved by the addition of hydrated lime, which elevates the pH to a range of 8.5 to 9.2. The addition of the hydrated lime is controlled by the influent flow meter and trimmed pH monitor/controller. In addition, an organosulfide reagent is added/blended with the influent stream to form organosulfide heavy metal complexes which have very low solubility products, thus resulting in maximum heavy

metal reduction.

A ferric chloride reagent is added/blended with the stream to form a dense flocculant which

in turn enhances the downstre am settling characteristics. In addition, the hydrolyzed form of this coagulant provides precipitation sites for co

- precipitation of other metals.

Reaction tank No. 2 will be equipped with anti

- vortex baffles and a bridge

- mounted agitator

to maintain sol ids suspension and to blend the liquid stream with the ferric chloride. The effluent from reaction tank No. 2 will flow to the solids contact clarifier. The agitator will provide a mixing energy intensity as follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Horsepower 7.5 7.5 7.5 Mixing Intensity (HP/million gallons) 537.3 773.5 773.5 Pump Rate (gpm) 19,761 19,761 19,761 Turnover Rate (once every) 42.3 seconds 29.4 seconds 29.4 seconds

Reaction tank No. 1 will be of steel constructi on and will provide the operating conditions as

follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Diameter (ft) 12 10 10 Height (ft) 18 18 18 Operating Capacity (gallons) 13,958 9,693 9,693 Hydraulic Retention Time (minutes) 48 60 60Shaw Stone & Webster, Inc.

- Stoughton, MA 6 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] **♦** Solids Contact Clarifier

The solids contact clarifier will be of the torque cage type with a sloped bottom influent/ recirculation column, a reaction cone and sludge scraper arms installed by the Purchaser

within a coated circular carbon steel tank fu rnished by Shaw Stone & Webster.

Polymer is added/blended with the influent stream to further enhance the settling

characteristics.

The solids contact clarifier will have an effective surface area, resulting surface settling rate, effective capacity, and hydraulic retention time as follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Diameter (ft) 30 23 23 Height (ft) 24 24 24 Effective Surface Area (sq ft) 678.56 387.19 387.19 Surface Settling Rate (gpm/sq ft) 0.30 0.29 0.29 Capacity (gallons) 104,865 62,541 62,541 Hydraulic Retention Time (hours) 6 6.47 6.47

The reaction cone will effectively divide the solids contact clarifier into an inner flocculating

reaction zone and an outer settling zone. The flocculating

- reaction zone will be equipped

with a variable

- speed up

- draft style turbine mixer to mix the chemically conditioned influent stream and recirculated precipitate. The turbine will be installed within a draft tube extended

to the bottom of the clarifier to ensure the recircu lation of the precipitated solids. The design recirculation rate of the clarifier is approximately 11 times the forward flow rate. The draft tube will be equipped with recirculation inlet ports near the bottom and outlet ports near the liquid surface.

T he chemically conditioned influent will enter the draft tube and be blended with recirculated precipitate, which enters the draft tube near the bottom. The blended stream will exit near the liquid surface, discharge into the reaction cone (which provides solids contact), and flow

downward.

After the initial downward flow pattern, the influent will begin to flow horizontally and upward. The quiescent condition outside of the reaction cone is ideally suited for liquid/solids separation.

Heavier suspended solids settle toward the bottom of the clarifier and clarified liquids flow upward toward the effluent collection troughs.

The solids that settle out to the bottom of the clarifier are gently conveyed to the centrally located sludge hopper by the rotating sludge collector mechanism. The sludge collector mechanism will consist of a drive unit and two rake arms with scraper blades which will sweep the clarifier bottom twice each complete revolution. The output speed of the drive

unit will be such that one revolution will occur approximately every 15 minutes.Shaw Stone & Webster, Inc.

- Stoughton, MA 7 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] The clarifier will be equipped with an automatic rake lift mechanism which will be controlled by the torque monitor which will raise the rake mechanism up to 2 feet if a high torque load

is encountered

.

The clarifier rake arm drive unit will be equipped with a torque overload device, drive and lift

motors.

Clarified liquid will be collected in effluent collection troughs located radially around the tank and will flow by gravity to the heat exchanger f eed tank. The effluent collection troughs will be “L” shaped and will be equipped with V

- notch weirs on both sides.

The clarifier effluent to the heat exchanger feed tank will be injected with hydrochloric acid to reduce the pH to approximately 7.0. The discharge line downstream of the injection point will be equipped with a pH monitor/controller.

**♦** Heat Exchanger Feed Tank and Feed Pumps

Clarified/pH adjusted effluent from the physical/chemical treatment portion of the wastewater treatment system shall be conveyed by gravity to the shop fabricated, FRP constructed heat exchanger feed tank for subsequent transfer by the heat exchanger feed pumps to/through the heat exchangers and on to the SBR influent equalization tank.

The heat exchanger feed tank sha ll be based on the following:

Morgantown

Station Dickerson

Station Chalk Point

Station Diameter (ft) 8 8 8 Height (ft) 15 15 15 Capacity (gallons) 6,016 6,016 6,016 Hydraulic Retention Time (minutes) 28 50 50

Two (2) 100 percent capacity, skid

- moun ted heat exchanger feed pumps will be provided. The heat exchanger feed pumps will be horizontal, centrifugal, vinyl ester type.

Each heat exchanger feed pump shall be rated as follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Capacity (gpm at ft TDH) 210 at 50 120 at 50 120 at 50 Horsepower 7.5 5 5

The common discharge line of the heat exchanger feed pumps to the heat exchangers will be equipped with a Siemens

- supplied flow meter for monitoring/ controlling the forward flow

rate to the reaction tank via the VFD.

Each pump discharge will be provided with a pressure indicator.Shaw Stone & Webster, Inc.

- Stoughton, MA 8 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] **♦** Temperature Reduction; Heat Exchangers

The downstream biological treatment system utilizes mesophilic bacteria. Therefore, the temperature of the waste s tream needs to be reduced to approximately 95 degrees F in order to optimize the biological treatment process.

Cooling of the waste stream will be achieved by the use of two (2) 100 percent capacity plate and frame heat exchangers.

The waste stream (hot side) will be pumped to the heat exchangers by the heat exchanger feed pumps and following cooling will discharge to the SBR influent equalization tank.

Plant service water will be used for cooling. The cooling water supply pressure shall be 75 psig or g reater and shall be used for flushing/plant utility water after passing through the heat exchangers.

Each heat exchanger will be equipped with pressure and temperature indicators on hot/cool sides of the waste and cooling water lines.

**♦** SBR Influent Equal ization Tank

The downstream biological treatment system for the reduction of ammonia nitrogen and nitrates is a batch process. Therefore, the SBR influent equalization tank is used to store clarifier effluent for subsequent transfer to the sequencing ba tch reactors during a fill cycle.

In addition, the SBR influent equalization tank shall receive backwash reject from the tertiary continuous backwash filters for reprocessing.

The SBR influent equalization tank shall be equipped with a jet mixing system which will be utilized to blend the tank contents and to help keep the solids in suspension. The jet motive source shall be the contents of the SBR influent equalization tank and pumping source shall be the SBR feed pump (A or B) after the completion of a fill cycle. The jet mixing header shall be equipped with entrainment ports which result in entraining approximately 4 times the jet motive pump capacity resulting in a high turnover rate of the tank contents.

The SBR influent equalization tank shall be field erect carbon steel construction by Shaw Stone & Webster and be based on the following:

Morgantown

Station Dickerson

Station Chalk Point

Station Diameter (ft) 34 26 26 Height (ft) 16.5 16.5 16.5 Capacity (gallons) 101,865 55,597 55,597

Volumetri c Capacity (Equal to number of SBR batch cycle volumes) 2.75 2.7 2.7Shaw Stone & Webster, Inc.

- Stoughton, MA 9 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] **♦** SBR Feed Pumps A/B [P&ID D

- 603

- Sheet 08]

Two (2) 100 percent capacity skid

- mounted SBR feed pumps will be provided. The SBR feed pumps will be horizontal, centrifugal type of vi nyl ester construction.

Each SBR feed pump shall be rated as follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Capacity (gpm) 310 170 170 Head (ft TDH) 18 18 18 Horsepower 5 3 3

Each pump discharge will be provided with a pressure i ndicator.

Each pump shall be equipped with a suction isolation valve, drain valve, discharge isolation valve and discharge check valve.

**♦** Sludge Recycle/Sludge Transfer Pumps A/B

A portion of the clarifier settled solids will be periodically removed from the solids contact clarifier by the sludge recycle/sludge transfer pumps. They will recycle the settled solids back to the equalization tank to maintain the proper solids concentration within the reaction

tank.

Solids contact clarifier settled solids wi ll be periodically removed from the solids contact clarifier by the sludge recycle/sludge transfer pumps. They will pump the solids during normal operation to the sludge holding tank.

The pumps will be horizontal, belt

- driven, rubber lined, centrifugal t ype.

Each solids recycle/sludge transfer pump shall be rated as follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Capacity (gpm) 160 70 70 Head (ft) 70 70 70 Horsepower 7.5 5 5

The solids recycle/sludge transfer pump operation shall be periodically adjusted (cycled) by the operator based on the process needs (solids concentration in reaction tank and actual sludge yield). Based on the design conditions, the estimated solids recycle and sludge

transfer rates are as follows:

**•** Solids R ecycle Rate 54%

**•** Sludge Transfer Rate 46%

The solids recycle/sludge transfer pump set shall be provided with pneumatically actuated suction and discharge valves which will allow for automatic forward/back flushing of either the suction or discharge l ines.Shaw Stone & Webster, Inc.

- Stoughton, MA 10 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] Each recycle and transfer discharge lines will be equipped with a flow meter for monitoring the recycle and/or sludge transfer rate. The recycle line on each pump set shall be provided with a flow control valve for controlling the recycle rate.

Ea ch pump discharge will be provided with a pressure indicator.

**♦** Sequencing Batch Reactor

Siemens’ Omniflo ® Sequencing Batch Reactor process offers clear advantages not available in any other “periodic process”. Patented mechanical features including the Omniflo ®
process piping, ID/SC Manifold and decanter, combine with the Omniflo ® batch proportional operating strategy to offer process flexibility and reliability unmatched by any other process.

**•** Periodic Processes

The Omniflo ® Sequencing Batch Reactor p rocess is a unique combination of equipment and controls for operating a complete secondary wastewater treatment facility. Because there are currently less than six manufacturers offering “periodic” processes, one must

understand how each manufacturer add resses the treatment goals, in order to appreciate the unique advantages of the Omniflo ® process. Periodic processes are simply batch activated sludge processes that accomplish, in discrete time periods within one tank, what conventional continuous flow p lants accomplish in multiple tanks.

There is a widespread belief that periodic processes are a recent development, and still in the developmental stage. In truth, most early activated sludge plants were designed to operate in a batch treatment mode. Re cent improvements in microprocessor control systems, automatic valves, and aeration equipment have made batch, or periodic, processes not only practical, but for most applications, very desirable.

**•** The Sequencing Batch Reactor Process

The sequencing batc h reactor process is an activated sludge process, as are all periodic processes, but bears no similarity to the extended aeration process. A sequencing batch reactor operates in a true batch mode under non

- steady state conditions. It provides for

inheren t flow equalization and flow blending, and greatly reduces operator skill and attention requirements. Controls range from a simplified float and timer based system to a PC based SCADA system with color graphics.

Siemens’ Omniflo ® D.O. controlled aerat ion to reduce energy consumption and enhance selective pressures for BOD, nutrient removal and control of filaments. The Omniflo ®

sequencing batch reactor has improved the technology in four major areas:

**∗** Control strategy

**∗** Mechanical equipment requirements

**∗** Decanter design

**∗** Sludge wastingShaw Stone & Webster, Inc.

- Stoughton, MA 11 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] In a true batch sequencing batch reactor, there are five basic cycles in each batch. All cycles and variations of cycles are described as follows:

**∗** Fill

**∗** React

**∗** Settle

**∗** Decant

**∗** Idle

Anoxic Fill

During Anoxic Fill, the basin is loaded with food in the influent through Siemens’ patented Influent Distribution/Sludge Collection Manifold (ID/SC) creating a high F:M ratio with zero D.O. conditions. The Fill period is primarily anoxic, or without aeration.

Aeration is usual ly initiated late in the Fill period, and continues in the React period, after

the influent flow has been diverted to another basin. The Influent Distribution Manifold (ID/SC) allows intimate contact of the influent (food) with the settled biomass in the sludge blanket throughout the length of the basin (please refer to the “Equipment” section of the manual for a complete description of the ID/SC Manifold). During this time, the soluble BOD is absorbed and stored by the facultative biomass until air is re ceived to metabolize the food. The selective pressures exhibited on the biomass of zero D.O. in Anoxic Fill allows good settling, facultative organisms to predominate.

Aerated Fill

Subject to the ammonia nitrogen concentration prior to the end on the fill cycle, the blowers and pumps are automatically turned on to provide air and complete mixing which initiates the “feast” environment for the biomass. The biomass begins to metabolize the food they have absorbed. They utilize the oxygen provided very rapidly with high D.O. uptake rates and low residual D.O. values. It is during the initial stages of

Aerated Fill that both Nitrification and Denitrification occur. The ammonia is converted to nitrates within the highly aerated plume of the jet. The nit rates are converted to nitrogen gas in the low D.O. areas of the basin. The denitrifying organisms use the BOD as a food source and the oxygen off the nitrates converting the nitrates to nitrogen gas.

Denitrification

Siemens offers an exclusive seco ndary denitrification phase in which the blowers are turned off and the jet mixing pump continues to mix. This provides anoxic mixing to drive denitrification. Denitrification can be inserted at any point during the aerated cycle (Aerated Fill, React) th rough the control system. Typically, the denitrification step falls somewhere in the middle of the aerated cycle. The control system allows movement of the denitrification cycle by the operator for maximum flexibility. This can also be easily

controlled via a Siemens D.O. Control System.Shaw Stone & Webster, Inc.

- Stoughton, MA 12 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] React

React begins after the basin has completed filling, and the influent flow has been diverted to another sequencing batch reactor tank. No more food (influent) enters the reactor basin during React. This for ces the organisms to scour for any remaining BOD. Aeration continues in the full reactor until complete biodegradation is achieved; mixed liquor is drawn through the ID/SC and used as motive liquid for the jet aerator. React

continues until the food is c onsumed and the biomass enters its “famine” state. True React (no influent, no effluent) is critical to achieve intense famine conditions for optimum organism selection. Tests have shown that the food is consumed when the

residual D.O. in the basin excee ds 2 mg/L, at which time the residual D.O. begins to rise quickly. Siemens uses self

- cleaning D.O. probes to monitor the D.O. level and signal the blower and pump to cease operation, allowing energy conservation.

Decant

Following the Settle cycle the effluent withdrawal, or Decant cycle, begins. Decant is initiated by opening an automatic valve. Treated effluent is discharged through the decanter from approximately 18 inches below the surface, avoiding discharge of any

surface contaminates. Decant c ontinues until approximately the upper one

- third of the basin is discharged.

The treated effluent shall discharge into the sequencing batch reactor effluent equalization tank.

Perfect Quiescent Settle

The biomass is allowed to settle in perfect quies cent conditions; no influent is introduced during settle and no effluent is decanted. Since the reactor is under true quiescent conditions during settle, 100 percent of the reactor capacity is available for liquid/solids separation. The relative loading rate during clarification is zero for the batch reactor.

A conventional plant has loading rates ranging from 300 to 1,200 gpd per sq ft.

The control system allows Perfect Quiescent Settling in the cycle at flows up to 3.5 times average design flow, main taining consistent treatment during heavy rain infiltration.

Idle/Waste Sludge

While the reactor waits to receive flow, the automatic waste sludge valve shall open drawing settled sludge through the Influent Distribution Sludge/Collection Manifold (ID/ SC) and static pressure shall convey the sludge to the sludge chest transfer wetwell. The jet motive liquid pump is utilized as a waste sludge pump. The settled sludge is withdrawn through the sludge collection manifold which runs the length of the basin

. The multi

- point sludge withdrawal yields the thickest sludge possible, reducing side stream sludge treatment operation and maintenance.Shaw Stone & Webster, Inc.

- Stoughton, MA 13 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] **♦** Sequencing Batch Reactor Tanks

The biological treatment system shall consist of two (2) field erect coated carbon steel tanks provided by Shaw Stone & Webster and as follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Diameter (ft) 38 26 26 Height (ft) 24.5 24.5 24.5 Capacity, Total (gallons) 381,732 182,676 182,676 Number of Batch Cycles/Day 8 8 8 Cycle Duration (hours) 6 6 6 MLSS concentration (mg/L) 3,000 3,000 3,000

**♦** SBR Jet Motive Pumps A/B/C

Three (3) 50 percent capacity SBR jet motive pumps shall be provided to supply liquid motive to the SBR jet aeration/mixing headers.

SBR jet motive pump A shall draw suction from SBR A and shall discharge to SBR jet aeration/mixing header A. SBR jet motive pump B shall serve SBR jet aeration/mixing header B. SBR jet motive pump C shall be a common standby.

Each pump shall be rated as follows:

Mor gantown

Station Dickerson

Station Chalk Point

Station Capacity (gpm) 1,465 732 732 Head (ft TDH) 21 21 21 Horsepower 20 10 10

**♦** SBR Effluent Equalization Tank

At the end of each SBR batch cycle, roughly one

- eighth of the total daily flow rate will

dis charge from the SBR during the decant cycle which has a duration of approximately 30 minutes. In order to level off the flow to the downstream polishing steps, the system design incorporates a SBR effluent equalization tank.

The SBR effluent equalization tank shall be as follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Diameter (ft) 34 26 26 Height (ft) 16.5 16.5 16.5 Capacity (gallons) 101,865 55,597 55,597 Volumetric Capacity (Equal to number of SBR batch cycle volumes) 2.7 2.7 2.7Shaw Stone & Webster, Inc.

- Stoughton, MA 14 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] The SBR effluent equalization tank shall be equipped with a jet aeration/mixing header to add dissolved oxygen to the biologically treated effluent.

**♦** Tertiary Filter Feed Pumps A/B Two (2) 100 percent capacity tertiary filter feed pumps shall be p rovided to transfer biologically treated effluent from the SBR effluent equalization tank to the tertiary continuous backwash gravity filters for polishing.

The tertiary filter feed pumps shall be of the horizontal, centrifugal type, of vinyl ester

constr uction, and shall be provided with variable frequency drives for flow control.

The tertiary filter feed pumps shall be rated as follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Capacity (gpm) 210 113 113 Head (ft TDH) 25 25 25

Motor Horsepower 3 2 2

**♦** Tertiary Continuous Backwash Gravity Filters A/B

The FGD wastewater treatment system will include a filtration step to reduce the TSS and enhance the reduction of TSS metals in the biologically treated effluent.

Siemens’ design makes use of continuous backwash gravity filters because of their compactness, simple operation and low operating cost.

The wastewater to be processed is transported into the filter by means of the feed line. The wastewater enters the filter bed through the su pply pipe and the distributors. The wastewater is filtered as it flows through the media filter in an upward direction. The filtrate is discharged in the upper part of the filter.

The filter media bed is continuously moving downward as the water flows u p. The dirty sand is removed from the sand bed and washed, after which it is released back on the top of the sand bed. This sand cleaning operation is automatic and continuous.

The sand circulation is based on the airlift principle, forcing a mixture of dirty sand and water upward through a central pipeline. The intensive scouring movements separate the impurities from the sand particles. At the top of the pipeline the air is released, the dirty water is discharged and drained to the filtrate sump for reprocessing. The sand settles in the

washer.

The washer with its well

- designed hydraulic features is positioned around the airlift pipeline. The sand particles fall through the washer, where they are finally washed by a small amount of clean filtrate, flowing through the washer counter

- currently. The filtrate flow is generated by a difference in discharge level between the filtrate and the wash water.Shaw Stone & Webster, Inc.

- Stoughton, MA 15 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] The filter performance can be optimized in function of the feed water quality and the filtrate
targe ts. The air flow through the airlift is adjustable, in order to vary the sand circulation speed.

The filtered effluent shall be conveyed by gravity to the treated water storage tank.

Backwash reject shall be conveyed to the SBR influent equalization tan k for reprocessing.

The design data for the gravity filter is as follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Number of Units (100 Percent Capacity) Two (2) Two (2) Two (2) Total Surface Area (sq ft/filter) 53.8 32.28 32.28

Filtr ation Rate:

gpm/sq ft with two (2) filters in service gpm/sq ft with one (1) filter in service 1.95

3.9 1.75

3.5 1.75

3.5

**♦** Treated Water Storage Tank

The filtered effluent will gravity flow to the treated wastewater storage tank.

The 100 perce nt capacity tank will have a closed top and be of FRP construction.

The design data for the tank is as follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Nominal Diameter (ft) 10 8 8 Nominal Height (ft) 20 18 18 Operating Capacity (ga llons) 11,162 6,203 6,203 Hydraulic Retention Time at Design Discharge Pumping Rate (minutes) 53 54 54

The tank will be equipped with a level control for controlling the operation of the pumps.

**♦** Treated Wastewater Discharge Pumps A/B

Two (2) 100 pe rcent capacity, horizontal, centrifugal type treated wastewater discharge pumps will be provided, which will draw suction from the treated wastewater storage tank and convey the treated effluent to the point of discharge which it has been assumed to not

re quire more than 65 ft TDH

.

The common discharge line of the treated wastewater discharge pumps will be equipped with a flow meter for monitoring/controlling the discharge flow rate via the variable frequency

drive.Shaw Stone & Webster, Inc.

- Stoughton, MA 16 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] Each treated wastewater discharge pump shall be rated as follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Capacity (gpm) 210 115 115 Head (ft TDH) 65 65 65 Horsepower 10 5 5

**♦** SBR Waste Sludge Pumps A/B

A portion of the settled solids will be periodically removed from t he SBRs by the SBR waste sludge pumps. They will convey the waste sludge to the sludge holding tank for subsequent dewatering.

The pumps will be horizontal, vinyl ester, centrifugal type.

Each SBR waste sludge pump shall be rated for 70 gpm at 50 ft TDH and shall be equipped with a 5 HP, 1800 rpm, 460

- Volt, 3

- Phase, 60

- Hertz, TEFC motor.

The discharge line will be equipped with a flow meter for monitoring the waste sludge

transfer area.

Each pump discharge will be provided with a pressure indicator.

**♦** Process Blowers

A total of five (5) 25 percent capacity process blowers shall be provided to supply air (oxygen) to the various process users within the treatment system.

The capacity of each process blower shall be as follows:

Morgantown

Station Dic kerson

Station Chalk Point

Station Capacity (scfm) 240 112 112 Discharge Pressure (psig) 11 11 11 Horsepower 25 15 15

Each blower shall be complete with a motor/blower base, V

- belt drive, inlet filter, inlet silencer, discharge silencer, pressure indi cator, check valve and pressure relief valve.

**♦** Sludge Holding Tank

Solids removed by the sludge recycle/transfer pumps and SBR waste sludge pumps will be pumped to the sludge holding tank for subsequent dewatering.

The 100 percent capacity sludge holdin g tank will be FRP construction, open top and equipped with anti

- vortex baffles and shall be provided by Siemens.Shaw Stone & Webster, Inc.

- Stoughton, MA 17 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] As a means of blending the solids and in order to prevent the settling out of solids, the sludge holding tank will be equipped with a bridge

- mounted propeller type mixer.

Morgantown

Station Dickerson

Station Chalk Point

Station Horsepower 7.5 7.5 7.5 Mixing Intensity (HP/million gallons) 334 454.6 454.6 Pump Rate (gpm) 29,707 29,707 29,707 Turnover Rate (once every) at H.W.L 45 seconds 33.3 seconds 33.3 seconds

The estimated average sludge volume is as follows:

Sludge Morgantown

Station Dickerson

Station Chalk Point

Station lbs/day (dry) 53,950 29,666 29,666 Solids Concentration (%) 9.8 9.8 9.8 gallons/day 66,028 36,204 36,204

The design data for the sludge holding tank is as follows:

Morgantown

Station Dickerson

Station Chalk Point

Station Diameter (ft) 14 12 12 Height (ft) 21 21 21 Operating Capacity (gallons) (Based on 1 ft

- 6 in. Freeboard at H.W.L.) 22,452 16,495 16, 495

Hydraulic Retention Time (hours) 8.16 10.9 10.9

**♦** Filter Press Feed Pumps

On a batch basis, solids removed from the solids contact clarifier and SBRs shall be dewatered by recessed plate and frame filter presses. Based on the estimated sludge produ ction, the proposed dewatering system will process the solids in the following number of batch cycles per day:

Morgantown Station 7

Dickerson Station 5

Chalk Point Station 5

The filter press feed pumps shall be used to transfer approximately two

- third s of the batch volume within approximately one

- third of the batch cycle time and then pressurization shall occur transferring the balance of the batch volume and to pressurize the cake to enhance the

solids concentration.

The proposed dewatering system ha s been designed to allow simultaneous operation of both filter presses except for core air blow which shall be sequencing at approximately 10

- minute intervals. The core air blow requires a substantial amount of service air. By sequencing the
core blows, the size of the air compressor system is minimized.Shaw Stone & Webster, Inc.

- Stoughton, MA 18 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] Two (2) 100 percent capacity, horizontal, centrifugal Discflo pumps shall be provided. Each pump shall be equipped with a 50 HP, 460

- Volt, 3

- Phase, 60

- Hertz, TEFC, VFD controlled

motor.

Each pump disch arge shall be equipped with a 0 to 120 psig pressure indicator.

**♦** Filter Presses A/B

Two (2) 100 percent capacity recessed plate and frame filter presses shall be provided for dewatering the solids removed from the waste stream. The filter presses shall be located on an elevated mezzanine to simplify solids handling.

Based on a solids density of 100 lbs/cu ft and a predicted dewatered cake dry solids concentration of 50 percent, the design solids volume will be as follows:

Morgantown Station 1,079 cu ft

Dickerson Station 594 cu ft

Chalk Point Station 594 cu ft

The filter presses proposed shall be semi

- automatic and equipped with 1500 mm plates

based on a 1.25

- inch cake thickness will have rated capacity as follows:

Morgantown Station 175 cu ft

Dick erson Station 125 cu ft

Chalk Point Station 125 cu ft

A typical press cycle shall consist of the following steps and/or cycles:

**•** PLC shall confirm press closure.

**•** VFD controlled fast fill pump shall draw suction from the sludge holding tank and convey

t he solids to the filter press.

**•** Filter press pump speed shall ramp up as pressure differential increases.

**•** At the end of the pressurization cycle, compressed air shall be used to blowdown the press core (fill lines).

**•** Following the core blow cycle, the pre ss shall open and the plates shall be shifted to dislodge the cake from the plates which shall fall into roll

- off boxes located on the ground

level.

**•** During the fill cycle, filtrate and core blow shall be conveyed to the filtrate sump to subsequent reproce ssing.Shaw Stone & Webster, Inc.

- Stoughton, MA 19 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] **♦** Filtrate Sump/Return Pumps

A below grade concrete sump shall be provided to collect filtrate from the filter presses, press area drains, secondary containment drain, and backwash from the continuous gravity

filter.

The filtrate sump shall be d esigned with inside dimensions as follows:

Morgantown Station 16 ft wide by 16 ft long by 13.25 ft deep

Dickerson Station 12 ft wide by 12 ft long by 13.25 ft deep

Chalk Point Station 12 ft wide by 12 ft long by 13.25 ft deep

Based on a 1

- 1/2 ft freeb oard, a 3 ft pump submergence, and an 8 ft

- 3 in. high water level, the filtrate sump shall have an effective capacity as listed below which provides a volumetric capacity equal to approximately 2 filtrate volumes at design.

Morgantown Station 15,798 gallo ns Dickerson Station 8,886 gallons

Chalk Point Station 8,886 gallons

Two (2) 100 percent capacity submersible type filtrate return pumps shall be provided. Each pump shall be rated at 50 ft TDH with a 20 HP, 460

- Volt, 3

- Phase, 60

- Hertz motor and the

f ollowing capacity:

Morgantown Station 600 gpm

Dickerson Station 400 gpm

Chalk Point Station 400 gpm

Each pump shall be equipped with a 0 to 50 psig pressure indicator and automatic flow

valve.

The liquid level within the filtrate sump shall be monito red by an ultrasonic level indicator/

transmitter.

One (1) 100 percent capacity bridge

- mounted propeller type agitator shall be provided to prevent the settling out of solids. The filtrate sump shall be equipped with four (4) anti

vortexing baffles.

Mo rgantown

Station Dickerson

Station Chalk Point

Station Horsepower 3 3 3 Mixing Intensity (HP/million gallons) 189.9 337.6 337.6 Pump Rate (gpm) 21,143 21,143 21,143 Turnover Rate (once every) at H.W.L. 44.8 seconds 25.2 seconds 25.2 secondsShaw Stone & Webster, Inc.

- Stoughton, MA 20 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] **♦** Chemical Feeds

**•** Lime [

The purpose of the lime is for pH adjustment.

Lime slurry shall be delivered to the site in 10 percent lime slurry form and off loaded into the lime slurry storage tank.

The lime feed system shall consist of a lime slurry storage tank (tw o for Morgantown) with agitator and duplex lime slurry feed pumps. Each lime storage tank shall be of FRP construction with a domed top, 14 ft diameter by 21 ft high with an effective capacity of 22,452 gallons.

The chemical is added to the process bas ed on a predetermined dose and the flow rate to the system.

**•** Sulfide

The purpose of the sulfide is to form organosulfide heavy metal complexes to maximize heavy metal reduction.

The sulfide is from Purchaser

- supplied totes. The prepared chemical is a dded to the process based on a predetermined dose and the flow rate to the system. Two (2) 100 percent chemical feed pumps will be provided on the sulfide feed skid.

**•** Ferric Chloride

The purpose of the ferric chloride is to promote the formation of dens e flocculent which in turn enhances the settling characteristics and co

- precipitation of metals.

Ferric chloride is from Purchaser

- supplied totes. The prepared chemical is added to the process based on a predetermined dose and the flow rate to the system . Two (2) 100 percent chemical feed pumps will be provided on the ferric chloride feed skid.

**•** Polymer (Clarification Process)

The purpose of the polymer is to agglomerate the finer particles of flocculent and to enhance the coagulation process in the so lids contact clarifier.

The polyblend unit is used to mix the polymer from Purchaser

- supplied totes with plant water. The prepared chemical is added to the process based on a predetermined dose and the flow rate to the system. Two (2) 100 percent chemic al feed skids will be provided.Shaw Stone & Webster, Inc.

- Stoughton, MA 21 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] **•** Hydrochloric Acid

The purpose of the acid is to reduce the pH of the treated water.

Hydrochloric acid is from Purchaser

- supplied totes. The chemical is added to the process based on the pH of the water. One (1) chemic al feed pump and one (1) spare are provided on the hydrochloric acid feed skid.

The hydrochloric acid feed system shall include a HCl fume (caustic) scrubber.

**•** Carbon Source Feed

The purpose of the carbon feed is to promote cell growth within the biolog ical treatment

process.

Carbon is from Purchaser

- supplied totes. The chemical is added to the process based on the pH of the water. One (1) chemical feed pump and one (1) spare are provided on

the carbon source feed skid.

**•** Hypochlorite Acid

The purpos e of the hypochlorite is to breakpoint chlorinate the treated effluent to ensure low concentration of ammonia nitrogen; thus low total nitrogen in the final effluent.

Hypochlorite acid is from Purchaser

- supplied totes. The chemical is added to the

proces s based on the pH of the water. One (1) chemical feed pump and one (1) spare are provided on the hypochlorite acid feed skid.

**•** Bisulfite Feed

The purpose of the bisulfite is to reduce the chlorine residual prior to discharge.

Bisulfite is from Purchase r

- supplied totes. The chemical is added to the process based on the pH of the water. One (1) chemical feed pump and one (1) spare are provided on

the bisulfite feed skid.

**♦** Plant and Instrument Air System

The treatment system will be provided with an ai r compressor package which will produce instrument quality compressed air to use within the system.

Two (2) 100 percent capacity rotary screw type air compressors will be provided. Each air compressor shall be rated for 333 scfm at 100 psig and shall be equipped with a 75 HP,

460

- Volt, 3

- Phase, 60

- Hertz motor.

Instrument quality air will be achieved by conveying wet air through a 100 percent capacity desiccant type dryer.Shaw Stone & Webster, Inc.

- Stoughton, MA 22 [Mirant Mid

- Atlantic FGD Retrofit

- Morgantown, Dickerson, and Chalk Point Generating Station s] Instrument quality air will be conveyed to the air receiver. The vertical air re ceiver will have a capacity of 1,500 gallons and will be equipped with a pressure relief valve, pressure indicator, pressure switch and automatic condensate drain.

Condensate from the air compressor system will be collected in the building drain trench an d conveyed to the filtrate sump for subsequent processing within the treatment system.