EHTiRGY ARKANSAS, INC. WHITE BLUFF STATION UNITS

1 AND 2 EVALUATION
OF WET VS. DRY FGO TECHNOLOGIES SL-009510 Rev.
3 October 28, 2008 Project 12303-004 Prepared
by • LundyLLC 55 Eas

t Monroe Street

• Ch

i cago

, IL 60603 USA

• 312-269-2000LEGAL NOTICE This report was prepared by Sargent
& Lundy, L.L.C., hereinafter. referred
to as S&L, expressly for Entergy Arkansas, Inc., hereinafter referred
to as Entergy. Neither S&L nor any person acting on its behalf (a) makes any warranty, express or implied, with respect
to the use of any information

or methods disclosed

in this report or (b) assumes any liability with respect
to the use of any information

or methods disclosed

in this report.**~V~S,lt\IC.** WHITE 

### BLUFF STATION UNITS



## 1 AND 

## 2 Section

I SL-009510 

# 1. INTRODUCTION ............................................................................................................................

-

..... 

# 1-1 l.l PURPOSE ........................................................................................................................................................



## l-1 1.2 STIJDY APPROACH .........................................................................................................................................



### l-1 1.3 STUDY BASIS .................................................................................................................................................

1-2 1.3.1 

## UnitDesign ...........................................................................................................................................

l-2 1.3.2 

## Economic Infonnation ...........................................................................................................................

l-3 

## 1.3.3 Fuel Information .....................................................................................................................

: .............. l-4 

# 2. SULFUR REDUCTION TECHNOLOGY EVALUATIONS ..........................................................................



# 2-1 2.1 PURPOSE ........................................................................................................................................................



### 2-1 2.2 TECHNOLOGY DESCRJPTIONS ........................................................................................................................

2-1 

### 2.2.1 

## Lime Spray Dry FGD (LSD FGD) ........................................................................................................

2-2 

## 2.2.2 Wet Limestone FGD 

## with Forced Oxidation (LSFO FGD) ................................................................



## 2-ll 

# 3 •. COMPARISON
OF LSD AND LSFO 

# FGD PROCESSES .........................................................................



# 3-1 3.1 DESIGNBAS!S ................................................................................................................................................



## 3-l 3.2 GENERAL ARRANGEMENT .............................................................................................................................



### 3-3 

## 3.2.1 

## Lime Spray Dryer (LSD) FGD ..............................................................................................................

3-3 

## 3.2.2 Wet FGD ...............................................................................................................................................

3-3 

## 3.3 COMPARISON

OF 

## SYSTEJI.I FEATURES ............................................................................................................



## 3-4 3.3.1 AbsorberVessel ....................................................................................................................................



## J-4 3.3.2 Chimney ...............................................................................................................

; ................................

3-5 3.3.3

3-5**~y~me,**

il SIAl09510 WHITE BLUFF STATION UNITS

1 AND 2 Section 3.3.9 Mercury Collection ...............................................................................................................................

3-8 3.3.1
0 Preliminary C0 2 Considerations

for Dry and Wet FGD .......................................................................

3-9 3.4 COMPARISON

OF CONSUMABLES AND WASTES ..........................................................................................

3-10 3.4.1 3.4.2 3.4.3 3.5 3.5.1 3.5.2 3.5J 3.5.4 Power Consumption ............................................................................................................................

3- I 0 Reagent Consumption .........................................................................................................................

3-11 Waste Byproducts ...............................................................................................................................

3-11 SULFUR REDUCTION TECHNOLOGY COST EVALUA TlON ............................................................................

3-12 Capital Cost .......................................

- ..................................................................................................

3-12 Fixed and Variable Operating Costs ...................................................................................................

3-15 Preliminary Cost Summary .................................................................................................................

3-17 Sensitivity Analyses ............................................................................................................................

3-18 3.6 SULFUR REDUCTION TECHNOLOGY CONCLUSIONS ....................................................................................

3-24**ettU<if~lt0C.** WHITE BLUFF STATION UN!TS

1 AND
2

iii SL-009510 Table 1-l. l\1ajor Economic Parameters ......................................................................................................................................

l-3 Table 2-l. FGD System Deployment

in U.S ...............................................................................................................................

2-1 Table 3-l. Design Basis Used for Dry FGD vs. Wet FGD. Comparison .....................................................................

; .............. 3-l Table 3-2. Typical PRB Coal S0 2 Emissions Expe9ted from FGD Teclmology ........................................................................

3-7 Table 3-3. FGD System Labor Requirements ...........................................................................................................................

J-15 Table 3-4. O&M Cost Basis (both units combined) ..................................................................................................................

3- I 6 Table 3.-5. Summary Comparison
of Wet and Dry FGD Levelized Costs (yr. 2013) for White Bluff Units

l & 2 .................. 3-17 Figure 2-1. Relationship Between S02 to Dry FGD and S0 2 Reduction Efficiency ..................................................................

2-3 Figure 2-2. Typical Dry FGD System .........................................................................................................................................

2-4 Figure 2-3. Typical SDA (B&\V) .............................................................................................

, ..................................................

Z-8 Figure 2-4. Typical Pulse Jet Fabric Filter ................................................................................................................................

2-10 Figure2-5. Typical Wet Limestone FGD System .....................................................................................................................

2-15 Figure 2-6. Typical Ball Mill for Large FGD System ...............................................................................................................

2-16 Figure 2-7. Typical FGD Scrubber with Absorption Tray ........................................................................................................

Z-18 Figure 2-8. FGD Scrubber with Open-Spray Tower .................................................................................................................

Z-19 Figure 2-9

.. Typical Vacuum Belt Filter ....................................................................................................................................

2-22 Figure 2- I 0. Typical Rotary Drum Vacuum Filter. ........................

: ..........................................................................................

2-23 Figure 3-l. ImpactofS0

2 in Fuel on Levelized Cost ...............................................................................................................

3-19 Figure 3-2. Impact of Rail Delivery on Levelized Cost ............................................................................................................

3-20 Figure 3-3. Impact of Two Dry FGD Absorber Modules on Levelized Cost ...........................................................................

3-21**t~~wc.** WHITE BLUFF STATION UNITS

1 AND
2 A. Dry FGD General Arrangement B. Wet FGD General Arrangement C. Dry FGD Capital Cost Estimate D. Wet FGD Capital Cost Estimate E. Financial Analysis Summary

lv SL-009510WHITE BLUFF STATION UNITS

1 AND 2 

## 1. 1.1 PURPOSE 

### INTRODUCTION

1·1 SL·D09510 The purpose of the study was to select the flue gas desulfurization (FGD) process best suited for application

at Entergy's White Bluff Station Units

1 and 2. The most commonly used wet and dry FGD processes were evaluated relative
to one another using

a structured methodology

to achieve that goal. The study developed conceptual designs, order of magnitude cost estimates, and economic analyses of adding wet or dry FGD systems. 1.2 STUDY APPROACH The initial task for the study was to evaluate emission control technologies that might be applied to reduce SOx emissions from Entergy's White Bluff Station. The most commonly used wet and dry technologies were identified as potential solutions for SOx control for these units based on current configurations. The following

is a list of the major activities that were performed

in the conceptual design of the technologies described

in this report.WHITE BLUFF STATION UNITS

1 AND 2

1-2 Sl-009510 Material balances and process flow diagrams were developed

to identify how the White Bluff units currently operate and how the addition of SOx control technologies would change their operation. • Based on the material balances that were developed, preliminary sizing of various emission control technology equipment was done for SOx control technologies

as well as balance-of-plant (BOP) equipment and structures. a General arrangement (GA) drawings were prepared for wet FGD and dry FGD to estimate approximate quantity of duct material • Inputs for specific capital costs for wet FOD and dry FGD were developed by comparison with historical vendor budgetarY quotations for each technology implementation. o Inputs for O&M costs were developed

in parallel with Entergy.

A detailed· model projecting annualized costs for each unit over
a 40-year study period was prepared for wet FGD and dry FGD. 1.3 STUDY BASIS The basic data listed below were used as inputs to the study: • Unit Design Information. Unit size, boiler type, capacity factor, heat input, flue gas temperature, pressure profiles, and water quality. • Economic Information. Real interest rate, escalation rate, replacement energy and capacity charges, and process consumables. • Fuel Information. Basic fuel properties for Jacob's Ranch Powder River Basin (PRB) coal. 1.3.1 Unit Design S&L initiated its evaluation using the heat input to the boiler of each unit provided by Entergy
to generate material balances. Heat input to the boiler is a primary parameter used to calculate the quantity of flue gas that would need treatment

at each White Bluff unit. A team of S&L and Entergy analyzed the various heat input data and concluded that 8,950 rnmBtu/hr would be anappropriate heat input for the design of the FGD system. This resulted
in eccmoimzer modification

on Unit
2 Table 1-1 lists theWHITE BLUFF STATION UNITS

1 AND
2 

### Table 

### 1-1. Major Economic Parameters Amortization life, years Interest rate for discounting.



### % Commercial service date Capacity factor, 

## % Debt percentage

in capital structure,


## % Preferred stock percentage

in capital structure,


## % Equity percentage

in capital structure,


## % O&M escalation rate, 

## % Debt interest rate, % Preferred stock rate,% Capital escalation rate, % Federal and state tax rate, 

## % Equity retum, % Annual property taxes and insurance,



## % AFUDC,% Tax depreciation schedule Auxiliary electric power energy charge, $/MWh Ash disposal cost, $/ton Operating labor rate, $/hr Raw makeup water, $/1000 gal Cooling tower blowdown water, $/1000 gal 

### $/ton

40 

## 8.24 Sept2013 72.0 41.97 

## 4.44 53.59 

## 2.0 6.34 5.99% 

## 3.0 39.225 9.90 0.944 8.24 Amortized over 84 months 

## 47.00 8.58 

## 40.00. 0.92 0.48 

## 107.00



## 1-3 Sl...009510E:NTtftGYtm:.WHITEBLUFFSTATIONUNITS1AND21-4Sl-009510econoniicevaluationforS02controlwasassessedat2lbS02/mmBtusulfurand0.8lbS02/mmBtuoperatingsulfurasabaseline.Asensitivityanalysiswasperformedfordesignsulfurlevelsat3lbS02/mmBtu(operatingat0.8lbS02/mmBtu)and5lbSOlmmBtu(operatingat5lbS02/mmBtu)forwetFGD,andat3IbS02/mmBtufordryFGD.DryFGDwouldnotbecompetitiveat5lbsSOlmmBtu.**iMltfUiY~#IIC.-** WHITE BLUFF STATION UNITS

1 AND 2 2. SULFUR REDUCTION 2.1 PURPOSE EVALUATIONS

2-1 SL-009510 The purpose of the sulfur reduction technology evaluations

is to develop

a conceptual design for retrofitting

a wet or dry FGD technology for White Bluff Station, then to compare the economics
of each technology, and finally to recommend the technology best suited for application. The economics identifY the cost of SOz removal based on a net present value (NPV) assessment and normalized cost for $/ton of S0 2 removed. 2.2 TECHNOLOGY DESCRIPTIONS FGD technology has been applied
in the U.S. since the 1960s and, with the nearly 40 years of development,

it is considered

a mature technology.

A wide range ofFGD technologies

is available. Table 2-llists the various types of utiljty power plant FGD installations

in the U.S. As shown in this table, wet FGD, with either limestone
or lime as the reagent,

is the most prevalent, with almost 75% of the total flue gas scrubbing capacity. Dry lime FGD, typically used when sulfur levels are less than 2 lb S0
2 /mmBtu,

is the next most selected technology with over 15% of all installations. This section discusses wet limestone FGD and dry lime FGD technology

in detaiL FGDType Wet limestone Wet lime Dry lime/SDA Sodium carbonate aqueous carbonate Table 2·1. FGD System Deployment

In U.S. Boiler Units (No.) 105 58 35 Installed FGD Units (%) 48 26 16 4.1 0.5WHITE BLUFF STATION UNITS

1 AND 2 2.2.1 lime Spray Dry FGD (LSD .FGD)

2·2 SL-009510 The LSD FGD technology was developed beginning

in 1977, to serve users of low-sulfur coal who had to meet

a requirement
of only 70% S0 2 removal. As the technology's experience grew and matured,

it demonstrated much higher performance capabilities and now can provide
as much as 95% S0 2 removal
in many applications. Gradually,

it has been adopted by users of medium-sulfur coals, and now is frequently considered
formediumsulfur coals of 3 lb/mmBtu S0 2 content. Maximum spray dryer absorber (SDA) vessel size had an equivalent capability
of 150 MW of flue gas in the initial installations, but absorber vessels have grown to an equivalent
of 350 MW of flue gas. 2.2.1.1 Description
of Process In an LSD FGD system, flue gas is brought into contact with lime slurry in the SDA vessel. This process can use (pulverized) hydrated lime (Ca(OH)2)

or (pebble) quicklime (CaO); however, large quantities
of lime are consumed,

so the more economical quicklime generally

is used at large utility installations. CaO must be hydrated before use. This hydration occurs in a slaker, where lime is mixed with water and slurry of fine lime particles results. The chemical reaction
is as follows: SOz absorption takes place in an SDA. Calcium reacts with the S0 2 to form waste solids sulfate (CaS0

4 ) and sulfite (CaS0

3 ), as shown in the following chemical reaction scheme. About **one~third** of the waste is sulfate andtwothirds
is sulfite.

GaO + HzO <-+ Ca(OH)z Ca(OH)z

+ S02 +H 2 0--> CaS0

3 • 1 /2H
2 0 +

3 /zHzOWHITEBLUFFSTATIONUNITS1AND22-3Sl-009510TheS02removalefficienciesoftheexistingLSDsystemsrangefrom85-95%,dependingontheSDAinletS02concentration.Theeffectivenessofspraydryertechnologydecreaseswithfuelsulfurlevelsabove3lbSOiMMBtu(asshowninFigure2-1).Athighersulfurlevels,theamountofsorbentrequiredforremovalofS02fromthegasstreamincreasessubstantially,andtheeconomicsgenerallyfavorwetscrubbing.ThecurveinFigure2-1representstheamountofS02reductionexpectedforanLSDsystemwithabaghouse.ThisisageneralguidelineforapplicationofLSDtechnology,andisderivedfromS&L'sin-housedatabaseonthetechnology'sperformance,whichisbased onguaranteedataprovidedfromvarioussuppliersofFGDsystems.FigureRelationshipBetweenS02toDryFGDandS02ReductionEfficiency100r-----r----'-----...,----,..-...,-------,23456TheprimaryoperatingparametersthataffectS02removalusingLSDFGDare:"Thelimestoichiometricratio(SR)varieswiththeamountofS02intheSDAinthefluegas.TheSRcanrangefrom1.2lb-molelime/Ib-moleofS02attheinletto1.6lb-moleHme/lb-moleofS02attheinlet.AnSRvalueof1.2isapplicableforinletS02valuesoflessthan1IbSOimmBtu,whilethelargervalueisforinletSOzvaluesgreaterthan2lbSOz/mmBtu.ThefluegastemperatureintotheSDAisimportant.Temperaturesabove300°Fallowmorewaterandlimetobeinjectedwiththefluegas.Thisincreasesso2removalandtheutilizationofthelime.Iftheinlettemperatureisbelow300°F,theefficiencywillbereduced.LSDseveralWHITEBLUFFSTATIONUNITS1AND2•ReagenthandlingandpreparationAbsorptioninaspraydryerabsorber0Particulatecollection•FluegassystemandstackWastehandlingsystemanddisposalFigure2-2.TypicalDryFGDSystemOptionalFfyashPre-CollectionHeadTank.---1IIIIIIIIIIBaghouse-il-·-----,lIRecycleISolidsIIiIIIII2--4SL-009510**EM'I:RGY~WC.** WHITE BLUFF STATION UNITS

1 AND 2 2.2.1.2.1 Reagent Handling and Preparation

2·5 Sl-009510 Lime is conveyed by truck, barge, or rail to an enclosed storage silo. A detailed study will be performed

if dry technology

is selected for White Bluff. Utilities usually require

a storage capacity of at least seven days, depending on the delivery method and lime source proximity. For delivery by truck, the maximum recommended
silo height should be 120 feet if the truck's onboard blowers are used for unloading. However, the lime supplier should verify the capability
of the truck blowers to transport the lime. If the silo needs to be taller than 120 feet,
a permanent pressurized blower system needs to be installed. For lime delivered
by truck, silos are usually sized for a 7- to 14-day capacity,

7 days if the lim.e source
is close to the power plant and 14 days if a distant source
is used. A 14-day capacity silo with truck delivery

is used for this study. The bulk storage silo feeds directly into the lime-slaking train and no transfer system
is **need~** d. Delivery by truck may not allow for competitive bidding
to supply lime if one source
is significantly closer to the plant. Rail delivecy allows for more sources
to be considered. For delivery by rail, larger quantities of lime are stored on site. Durations
of 14 days or more have been the norm for most utilities. The strategy for selecting the storage capacity depends on the railroad used and the number of rail cars that the site can handle. Some utilities receive an entire unit train of!ime, while others receive one-third
or onehalf of a unit train. The lime silo has either

a bin activator or a fluidizer
to promote lime flow ability.
A rotacy feeder in series with
a volumetric feeder supplies the lime to a slaker, where the pebble lime, CaO, is hydrated

to Ca(OH)

2 • The slaking process

is exothermic and the heat release helps to shatter the lime into fme particles. The slaked lime slurry then flows to a storage tank where
it is held until it is needed by the atomization process. Truck-delivered lime will remain in large pieces when
it enters the slaker, but lime pneumatically transferred several times

to be in a fonn. The detention

reaction.

# """""'_...,. WHITE BLUFF STATION UNlTS



### 1 AND 

### 2

2-6 

### Sl-009510 The. vessel
is also fitted with
a classifier section that separates the sufficiently slaked particles from the coarse lime particles. The larger particles are recycled back to the slaker vessel while grit material, consisting
of inert material as well as uncalcined limestone and magnesium oxide particles,

is removed. An 

### attrition slaker is comprised
of a vessel and
a set 

### of agitators with
a common axle, which produce

a counter current flow that induces lime particle interaction

in order to speed up the slaking process. The main difference

· between detention slakers and attrition slakers
is the degree of solids interaction. Attrition slakers may also be mated to grinding or grit 

### removal equipment for impurity removal. In a ball 

### mill slaker, pebble lime and water


### is added continuously

to a horizontal vessel that contains grinding media, which allows grinding and slaking
to occur simultaneously. The product flows through

a classifier that separates the final slaked product from the coarse material, which 

### is then fed back to the ball mill to be processed further. Due to the grinding function of the ball mill slaker,

a grit removal system
is not necessary. A vertimill slaker operates



## in a similar fashion
to the ball 

### mill slaker, with the exception that the vessel is vertically oriented and includes

a double pitch helix that agitates the grinding media.


### A classifier system

is also used to ' 

### recycle the coarse product back to the grinding vessel. Similarly

to the ball 

### mill slaker, the vertimill does not require

a grft removal system. The advantage
of the ball mill type slakers
is the less stringent requirements
for quicklime size and slaking water quality,
as well as eliminating the need for the grit removal system. Although

a slaker type has not been specified, the horizontal ball 

### mill was used in the cost evaluation for the slaking process. Reagent preparation with two 100% slurry trains is used for this study. Each train is made up of a solo, feeder, and slaker. The slurry is stored in a dedicated storage 

### tank. 2.2.1.2.2 Recycle Ash 

### the SDA several times 

### lime corlsumptlOll. The**£~Y~t8C.** WHITE BLUFF STATION UNITS

1 AND
2

2-7 Sl..009510 high SOz removal efficiencies. There
is residual activity left in the lime after it has been passed through the system once; therefore,

it is re-introduced

to gain additional lime utilization. 2.2.1.2.3 Spray Dryer Absorber The SDA is a vertical, open chamber with concurrent contact between the flue gas and lime slurry (Figure 2-3). The slurry
is injected

at the top of the tower using either

a rotary atomizer
or a dual-fluid nozzle, which produces fine droplets
to absorb the S0 2 • In the process of evaporating the droplets, the flue gas is cooled from the absorber inlet temperatureof approximate;y 3l8°F to an outlet temperature

of l60-180°F depending
on the adiabatic saturation temperature. The actual outlet temperature

is chosen based on the optimum reagent utilization, the flue gas saturation temperature, and the required S0 2 removal efficiency. The absorber typically will be operated

at 30°F above the gas saturation temperature (also known as the approach temperature)

to prevent solids deposition
on the walls of the absorber and to avoid moisture condensing

in the particulate collector. The residence time of the cooled flue gas in the SDA should be at least 10 seconds
to ensure high removal efficiencies. Most current designs utilize

a residence time of over 12 seconds...,...,.._IIIG WHITE BLUFF STATION UNITS

1 AND 2 EVALUATION
OF WET VS. DRY FGO TECHNOLOGIES Figure 2-3. Typical SDA (B&W)

: Fiu darry ; **drop~ts**

2-8 SL-009510 The slurry comes into contact with the flue gas inside the SDA vessel, and the slurry should be dry before

it contacts the SDA walL Corrosion of the SDA walls can occur if a high-chloride coal is fired; however, this is rarely a concern with Powder River Basin (PRB) coals. Because the flue gas exiting the SDA typically

is held at 30°F above saturation, carbon steel ductwork

is adequate and alloys are not needed. Therefore, the downstream ducts, baghouse, and chimney liner can all be made of carbon steel. Precautions should be taken around access doors and other penetrations where cool ambient air can leak into the duct and form cool spots in the SDA where acids in the flue gases can condense.
In these locations,

it is common
to spray

a coating over the carbon steel for a minimal amount of corrosion protection. The dry absorber does have some capability

to remove mercury from the flue gas, but the mercury must be in the ionic form to be absorbed. PRB coal is low in chlorides and the mercury from firing PRB is not in the ionic form, EntergyArlmnsas WBI-2_Dry

vs Wet FGD Study ReY 3 Issued 10·28-08 Project

I 2303

- 004

**Luncfy**

**'~ ~'t~ftK.**  WHITE BLUFF STATION UNITS

1 AND 2

2-9 SL-009510 but rather,

is mostly in the elemental form. However, dry FGD has potential

to remove significant amounts of mercury
if the elemental form can be converted

to the ionic form in the flue gas. Coal additives have completed this conversion
of elemental

to ionic mercury. Coal additives could be a halogen, such as bromine or iodine. Tests to date have shown that another halogen, chloride,

is the least effective of these compounds, but bromine
or iodine have been effective

in utility tests. Dry FGD has the potential
to capture 70-80% of the mercury
in the PRB coal if additives are used. Additives are believed
to be less expensive than powdered-activated carbon. The SDA vessel will have

a discharge hopper on the bottom
to allow any small material buildup on the walls to slide down and to be removed. 2.2.1.2.4 Particulate Collector The SDA typically

is located after the air heater outlet, and needs to be followed by a particulate collector, which
is almost always

a baghouse. Dry FGD systems usually are coupled with
a fabric filter baghouse because S0 2 removal efficiencies

up to 95% are then possible.

A substantial amount of the S0 2 is removed
in _the baghouse because the lime rich product and fly ash remain on the surface of the bags and the flue gas is pulled through tbis layer of lime. This close contact betlveen the flue gas and lime accounts for another

I 0-15% of the overall S0 2 removaL A pulse jet baghouse (Figure 2-4) with an air-to-cloth ratio of 3.5 ft!min (J.l rn/min) typically

is used doWnstream of a dry-FGD system on coal-fired units. The baghouse

is provided with

a spare compartment
for routine maintenance. The waste is pneumatically conveyed

to a waste storage silo with typically

a 3-day storage capacity. The baghouse
or ESP casing must be well insulated

to contain the heat witbin the casing and to keep the interior skin temperature about 30°F above saturation.**~Enief8Y. '"""""~--**  WHITE BLUFF STATION UNITS

1 AND
2 EVALUATION
OF Wt:r VS. DRY FGD TECHNOLOGIES Figure 2-4. Typical Pulse Jet Fabric Filter Source

: Wheelabrator 2.2.1.2.5 Waste Handling

2-10 SL-009510 The waste collected

in the baghouse

is pneumatically transported

to a storage silo. A portion of the waste is recycled
to increase the reagent utilization. The dry FGD waste is mixed in a pug mill with water to prevent dusting if being transported

in open top

( tarp covering) style trucks for disposal. Sale of the waste products from dry scrubbing

is rare and the material

is typically sent to a landfill. Dry FGD waste contains reacted calcium compounds En t ergyArkansas WB1·2_Dlyvs Wet FGDStudy Rev 3 I ssued 10..28..()8 Project

I 2303-004**£~~we.** WHlTE BLUFF STATION UNITS

1 AND 2

2-11 Sl-009510 and unreacted lime, Ca(OH)

2 • The waste has pozzolanic properties and when water
is mixed with the waste,
it cures into a low-grade concrete. Because this solid product

is impermeable, disposal
in a landfill

is a safe practice. One plant in the U.S. fonns pellets with the waste and sells them as gravel for fill or sub-base. 2.2.1.2.6 Flue Gas System and Stack Ducts downstream
of the SDA can be fabricated out of carbon steel, but the ducts and expansion joints must be insulated with insulation pillows
to contain the heat in the flue gas and maintain the gas at about 30°F above saturation. The chimney liner typically

is insulated but its exit can have cool ambient air pulled down into the top of the liner under certain atmospheric conditions. The inside of a carbon steel liner is typically coated in the top 50 feet to negate any impact of sulfurous acid condensation. 2.2.1.2.7 **StaJ71n~** The conceptllal design economic analysis includes
16 additional people for the O&M of the new dry FGD system, as summarized below.
A detailed listing of the staffing cost can be found in Section 3.5.2. • Lime unloading will require

a crew to move the rail cars or trucks through the unloader and to connect the equipment

to each hopper. This crew will work one shift between five and seven days per week to unload the cars. e FGD process operations will require an **opera~or**
to walk down the process equipment and check for malfunctions. The rotary atomizers will need to be switched on a 60- to 90-day cycle to clean

· their atomization wheels and perform other maintenance. Dual-fluid atomizers will be cleaned weekly. • Waste loading
to truck or rail cars will continue
as currently practiced for fly ash. Disposal of larger amounts of solids will require additional time for these activities. Wet Limestone FGD with Forced Oxidation (LSFO FGD)**"""""""'~""'** WHITE BLUFF STATION UNITS

1 AND
2

2-12 SL-009510 Wet limestone FGD systems have been operating

in utility applications since the 1960s. Early generations
of wet FGD technology had internal scaling problems that caused the absorbers

to be brought off line for cleaning every few months. To achieve acceptable availability
for multi-unit use, many smaller absorbers were installed on one . unit so that one absorber could be taken off line for cleaning and repair while the others handled 100% of the flue gas. Over the years, utilities learned
to combat scaling problems using two technological advances. The first advance was to use forced oxidation of the precipitate

in the absorber reaction tank, which effectively addressed the problem of scaling in the absorber. The second advance was to introduce most of the water needed by the process into the mist eliminators
of theLSFO FGD. The water required for mist eliminator wash typically has less than 1000 mg/L total dissolved solids and less than 50% saturated calcium sulfates. Service water from

a well or lake usually

is acceptable for this application. Cooling tower blowdown and ash pond water are not acceptable. Good water quality significantly reduces the plugging of the mist eliminators. These advances solved many of the chemistry problems and made the process much less complex. State-of-the-art wet FGD systems do not experience scaling issues. Spare absorber modules are rarely installed and single absorbers are routinely installed on large units. Early-generation
wet FGD technology experienced significant problems with corrosion of the absorber metals. Absorbers were coated with rubber or flake glass lined to avoid corrosion, but these systems required very high maintenance.
To avoid high maintenance and to minimize the corrosion
in the absorbers, alloys later were used inside the absorbers. The alloys ranged from 317 L to C-276, depending on the level of chlorides
in the absorber recycle slurry. Utilities have identified the reasons for the corrosion and have learned
to make better selections of alloys within the absorber. Developers
of alloys have also responded with newer; more corrosion-resistant
and lower-cost alloys. Utilities have also learned that the chloride level is the most important parameter

to monitor. Modem wet FGD systems use blowdown water from the absorber

to control the chloride concentration

in the scrubber

to within the capabilities
of the materials of construction. These advances have allowed utilities
to some value 

### inWHITEBLUFFSTATIONUNITS1AND22-13SL-009510transported.Gypsumcanbewashedtoremoveflyashand!orchloridessoitcan be.usedforwallboardmanufacturing,orasasoiladditiveinagriculturalareas.Wastesolidsthatareland-filledaredenseandinert.Issuessuchasleachingandgroundwatercontaminationarenotaconcernforland-fillinggypsum.Ithasbeenshownthatmostgypsumisland-filled,butifeitheroftheothertwousesisapplicable,thegypsumcanbesoldorgiven·away,therebyavoidingtheland-fillingcosts.WetLSFOFGDsystemsarethepredominantwetFGDtechnologyusedbyutilities.Itismostapplicableformedium-tohigh-sulfurcoalswhereremovalof95-99%oftheinletS02canbeachieved.LSFOFGDisalsoeffectiveonlow-sulfurcoalswhereitcanremove93-95%oftheinletS02•WetFGDsystemsarelimitedtoaminimumoutletconcentrationofbetween0.03-0.041b/mmBtuofS02•Drivingtheconcentrationlowerisnotcosteffective.Insummary,thebasicwetlimestonescrubbingprocessisnowreasonablysimpleandwell-established.RecentadvancesinthewetlimestoneFGDprocessincludedesignchangestopromoteS02absorptionathighremovalrates.Afterexperiencingpoorreliabilityinthefirstgenerationofthistechnologyduringthe1970sandearly1980s,wetlimestone·scrubbertechnologyhasmaturedandisnowcapableofmeetingavailabilitylevelsof99%.Additionally,gypsumcannowberecoveredasasalablebyproductwherefeasible.Extensiveoperatingexperiencehasincreasedindustryconfidenceindesigninglarger,morereliablelimestonescrubbermodules.Singleabsorberstreating1,000MWofthefluegasareinoperation.In1994,wetlimestonescrubberswereusedon70units,(35,100MWeofthetotalscrubbingcapacity).Today,therearemorethan100operatinglimestonescrubbers,withmoreunderconstructiontomeetnewemissioncriteria.LSFOFGDisaviabletechnologyforanycoal-firedboiler.2.2.2.1DescriptionofProcessInanLSFOFGDsystem,fluegascontainingS02isbroughtintocontactwithlimestone-slurrydropletsandtheso2isabsorbedintothewaterWithinthedroplet,theandcalciumfromthelimestone(CaC03)reacttoWHITE BLUFF STATION UNITS

1 AND 2 CaC0

3 + 80 2 -+ CaS0

3 + C02 CaS0

3 +

1 / 2 0 2 (flue gas) + 2H 2 0 -> CaS04

• 2H 2 0

2-14 SL-009510 Before the use of forced oxidation, the bisulfite ions would be recirculated through the absorber and wouldscaleout on the internals of the vessel. Force oxidizing the bisulfite ions turns them into
a precipitate

in the reaction tank so it cannot scale out onto the internals of the absorber. Most of the solids are recycled through the absorber several times, and a small bleed stream
is sent to a dewatering step. Vacuum drnm or belt filters are used to concentrate
the bleed slurry stream to 85-92% solids. The water from· this process

is returned
to the FGD process.
lf salable-grade gypsum

is to be produced, the solids are washed with dean water to remove the chlorides. This water is also returned
to the process. The absorber

is very effective
at removing hydrochloric acid (HCl) from the flue gas. The HCI reacts with the limestone and stays in solution
as chloride ions. Chloride ions are very corrosive
to ferrous-based metals, thus carbon steel is not an acceptable metal for construction
of the absorbers. For chloride concentrations

of 15,000 ppm or less,
a new stainless steel alloy is being used, alloy 2205. This alloy is used for the lowest-capital cost absorber. All the internals can be made from this alloy, including supports, recycle grids, trays, and reaction tanks. In most cases, recycle piping
is not made of alloy, but of fiber-reinforced plastic (FRP) with
a wear-resistant coating. PRB coal has minimal chlorides

to be collected, but if a moderate-sulfur coal with higher chlorides

is to be considered,

a higher quality alloy could be used at a greater cost. 2.2.2.2 Discussion
of Features A typical wet FGD system comprises several subsystems, including: <» Limestone handling " Limestone slurry preparation in the fuel. These

# • . . =Entergy. **l'.-ratGY~IMC.** WHITE BLUFF STATION UNITS

1 AND 2 EVALUATION

OF WET VS. DRY FGD TECHNOLOGIES. Figure 2·5. Typical Wet Limestone FGD System 2.2.2.2.1 Limestone Handling System

2·15 SL-009510 Crushed limestone (typically, 3/4 x 0-inch or 1.91 x 0-cm) received
at a plant typically

is delivered
bybottomdump railcars or trucks and is unloaded into
a receiving hopper:

It is assumed that limestone will be delivered by truck at White Bluff. The trucks will unload the limestone

to an outdoor, uncovered limestone storage pile. There are two storage piles

- one active pile (30 days' storage) that feeds the reclaim hopper and one inactive pile that is used only if limestone deliveries are interrupted.

A bulldozer

is then used to move limestone between the two piles

. Reclaim of the limestone from the bottom of 

### the active storage pile is by underground reclaim hoppers equipped with vibrating belt feeders

. The feeders supply the reclaim conveyor, whlch carries the limestone

to the day. silos located immediatCiy above the wet grinding ball mills. Rain water around the active and inactive limestone piles is handled by installing

a drain ditch around the piles where the water can be collected. EntergyArl<ansas WBI

· 2 _ Dry \'S Wet FGD Study Rev 3 Issued 10·28..{)8. Project 12303..Q04!JII1'flt(i'f Aa.\NS.U. llfC.. WHITE BLUFF STATION UNITS

1 AND 2 EVALUATION

OF WET VS. DRY FGD TECHNOLOGIES 2.2.2.2.2 Limestone Slurry Preparation System

2-16 SL-009510 Preparation
of the limestone slurry involves wet grinding the limestone

in a horizontal ball mill. The limestone received on site is similar to gravel. The limestone day bins and gravimetric feeders deliver the limestone

to a 2 x 100%-capacity ball mill system for both units. Figure 2-6 shows typical ball mills. One ball mill runs continuously, while the second ball 

## mill provides 100% spare capability. The ball 

### mill grinds the limestone and discharges



### it into
a small receiving 

### tank 

### that is then pumped through hydroclone classifiers. The limestone that is 95% less than 325-mesh

is ready for use and sent to a storage tank, but the larger particles are retwned
to the ball mills for further grinding and size reduction. Two

I 00"/o-capaeity classification pumps are used to ensure high reliability
of the classification system. Process makeup water or recycle water
is added to the ball 

### mills to produce 70% by weight solids slurry. The slurry classification process produces 30% by weight solids slurry, which
is stored up to 24 hours until it is fed as reagent makeup into an absorber. The slurry conceiltrations

are measured using nuclear density meters. The. ball mills are rubber-lined

to reduce erosion of the 

### mill internals. Steel balls are added as needed
to replenish the balls in the mill. Since White Bluff
is located in a warmer climate, the reagent preparation system will not need to be in a building
to protect the equipment and staff from the weather. Figure 2-6. Typical Ball Mill for Large FGD System 2.2.2,2.3 Absorber System Figure 2-7 depicts

a typical absorber (B&W) utilizing

a vertical spray/tray tower concept, with counter-current contact between the flue gas and scrubber slurry. This counter-current type is the most commonly used absorber
in the utility industry. Other absorber types available include jet bubbling reactor and **co current/count~r-current** 
flow. EntergyArkansas WBI-2_Dry

vs Wet FGD Study Rev 3 Issued 10-28-08 Project 12303-004

Lundy'''



# IWHITE BLUFF STATION UNITS

1 AND 2

2-17 SL.-009510 First-generation absorbers relied on packing
to provide the mass transfer, but in conventional absorbers the mass transfer occurs in the tray and in the open-spray zone

.. Some vendors rely on the sprays to provide the mass transfer, while other vendors use the tray for mass transfer. The tray is a horizontal perforated plate with
a two-foot-tall egg crate on top that causes the slurry to form

a several-inch froth layer on top of the tray. Flue gas that is forced up through the tray, comes in contact with this froth, and then gives up itS 80 2 to the slurry. When

a tray is present, most of the sulfur collection occurs
at the tray and the spray levelsdo less of the sulfur collection. One advantage
of the tray is that it smoothes the upward flow of flue gas, evenly distributing the flow so the entire absorber area is used for sulfur collection. Including

a tray in the design allows reduction of the liquid-to-gas (LIG) ratio. B&W and Siemens both use trays. An open-spray tower
is a **se~ond** popular absorber design. This type of absorber relies on several spray levels to create enough droplets.
to carry out the necessary mass transfer. The LIG ratio for an open-spray tower
is greater than for a tray, and the uniform downward flow of slurry is responsible for spreading the upward flow of flue gas for uniform flow. Open-spray towers use a baffle around the inside circumference

of the absorber
to prevent gas flow from bypassing the spray zone. Designers of this type of absorber point out that there are no internals
in the absorber

to corrode or scale. Alstom and Babcock Power Inc. both use open-spray towers. Figure 2-8 depicts Alstom's open-spray tower........... -.......s....c. WHITE BLUFF STATION UNITS

1 AND 2 EVALUATION
OF WET VS. DRY FGD TECHNOLOGIES Figure 2·7. Typical FGD Scrubber with Absorption Tray EntergyArkansas WBJ-2

_ Dry vs Wet FGD Study Rev 3 Issued 10 - 28-08 Project **1230~004**

Source

: Babcock

& Wflcox

2-18 SL-009510 Luncfy!\tWHITE BLUFF STATION UNITS

1 AND 2 EVALUATION

OF WET VS. DRY FGD TECHNOLOGIES Figure 2-8. FGD Scrubber with Open.Spray Tower

2-19 SL..()()9510 After falling through the spray zone, the slurry accumulates

in the reaction tank. Modem absorbers integrate the reaction tank. into the bottom of the absorber, whereas earlier-generation FGD systems used

a separate external tank. The tanks hold the slurry for at least 15 hours (solids residence time) to allow the reaction between the limestone and **S~** to complete and let gypsum crystal grow above 20 microns. The reaction tank is agitated
to keep the solids in suspension and air is forced into the reaction tank to force-oxidize
the CaS0

3 in the slurry. Fresh limestone

is added to the tank so there is an excess of calcium and all sulfur is reacted. The retention time in the reaction tank allows all the sulfite to react with oxygen so the solution

is not supersaturated with sulfite andbisulfite ions. Without the forced oxidation step, the absorber would be susceptible

to scaling and would need frequent cleanings. With forced oxidation, there is no need to clean the absorbers of scale that could disrupt absorber performance. Ent e: rgyAik:msas WBI·2_Dry

vs Wet FGD Study Rev 3 Issued 10-28-QS Project 12303

- 004

J,..unc:ty••<



# I I 

## t 

## I IWHlTE BLUFF STATION UNITS

1 AND
2

2-20 Sl-009510 The forced oxidation air is supplied by a set of compressors

in the absorber building. Compressed
air is injected below the reaction tank agitators through

a sparger network
to achieve greater than 99% oxidation
of calcium sulfite (CaS0

3 ) to calcium sulfate (CaS04).

A 3:1 stoichiometric ratio (SR) of oxygen to S0 2 is used to size these air compressors. From the reaction tank the slurry
is pumped back into the absorber's spray zone. High-horsepower pumps are used for the recycle. Conventional absorbers have at least one spare recycle pump to provide high availability
of the absorber. Slurry
is sprayed through several headers that span the diameter of the absorber. Slurry is abrasive and the spray nozzles are erosion-resistant. Occasionally,

a piece of scale can become lodged in the spray nozzle, causing pluggage
or sending the flow in an unpredicted direction,
so many smaller nozzles are used. The spray header material

is either alloy or FRP, with the latter gaining more use in recent absorber installations

. .

;

**~** Above the spray zone is the mist eliminator, which removes the entrained slurry droplets so they do not exit the absorber and create particulate emissions leaving the chimney. The mist eliminator must be washed with clean water to remove limestone deposits. Early-generation
wet FGD systems attempted

to use cooling tower blowdown or other wastewater, but this caused plugging of the mist eliminators

.. When high-quality water is used, plugging

is virtually eliminated. The absorber must be constructed
of materials that resist corrosion, erosion, and scaling. To reduce corrosion when firing PRB coal, an A-2205 SS alloy can be used so long as the chlorides
in the recycle slurry are maintained between 8,000-15,000 ppm with typical chloride less than 12,000 ppm. PRB coals usually have

a minimal amount of chloride
so this is usually the highest alloy that needs to be considered. The absorber inlet duct is an especially corrosive environment because of the wet/dry interface that occurs when some of the slurry deposits on the inlet floor of the duct. To combat this highly corrosive environment,
the inlet duct is made of C-276 from the absorber back about 10 feet. The outlet duct to the chimney

is also
a location subject to corrosion and either C-276 or FRP is used for this duct. FRP would be used if the unit is
an FRP liner in the chimney.
If FRP is riot used in the a

interfere with the process.WHITE BLUFF STATION UNITS

1 AND 2

2-21 SL..009510 Because wet FGD systems absorb HCI from the flue gas at 99% efficiency,

a minimal amount

is released to the environment. Wet FGD systems do not collect S0 3 very effectively, and they can cause S0 3 to condense
as very fine droplets that can result in a blue plume immediately after the flue gas exits the stack if the concentration

of S0 3 exceeds 7-10 ppm. Fortunately, when PRB coal is fired, the amount ofS0

3 in the flue gas is minimal and a colored plume will not result. Installation
of an SCR will increase S0 3 concentrations. The wet absorber does have some capability

to remove mercury from the flue gas, but the mercury must be in the ionic form to be absorbed. PRB coal is low in chlorides and the mercury from firing PRB is not in the ionic form, but rather,
is mostly in the elemental form. However,

a wet FGD has potential
to remove significant amounts of mercury
if the elemental form can be converted

to the ionic form in the flue gas. Coal additives added to the coal have completed this conversion
of elemental

to ionic mercury. Coal additives could be a halogen, such as bromine or iodine. Tests to date have shown that another halogen; chloride,

is the least effective "Of these-compounds,
but bromine or iodine have been effective
in utility tests. A wet FGD has the potential

to capture 70-80% of the mercury
in the PRB coal if additives are used. Additives are believed
to be less expensive than powdered-activated carbon. 2.2.2.2.4 Primary and Secondary Dewatering and Byproduct Handling Systems The bleed stream from the reaction tank is pumped
to a set ofbydroclones

for primary dewatering. The hydrodone overflow

is recycled back into the scrubber. The hydroclone underflow, contairung 50% solids,
is fed to a belt filter for secondary dewatering,

as shown in Figure 2-9. Belt filters are designed
to achieve 90% solids in the gypsum byproduct

to meet the requirements

of gypsum buyers, if the gypsum
is being sold to the wallboard industry. The gypsum cake is washed with fresh water on the belt filters to remove any residual chlorides

to a level typically less than 100 ppm by weight chloride in the dry solids. The wash water used for gypsum cake washing should not contain chlorides more than 50 ppm if the product
is intended for sale to a wallboard manufacturer. The filtrate from the horizontal belt filter returned
to the process.
If gypsum
is

in a landfill,

a **lower~capital-cost** shown in 2-10.I J I f I· I 911UGY AIIIIAHSAS. !NC. WHITE BLUFF STATION UNITS

1 AND 2 EVALUA'noN
oF Wcr vs. DRY FGD TECtiNOLoates Figure 2-9. Typical Vacuum Belt Filter Slurry

feed EntergyArkansas WBI- 2_D ry v s Wet F G D Srudy Rev 3l ss ued l0-28-08 Project

I 2303..()()4

I , t'

2-22 SL-009510 'Lundy'
'\'

# ! : 

# I I 

# l 

# I



# • =Entergy. llmiiGl--..s.OO:. WHITE BLUFF STATION UNITS

1 AND
2 EVALUATION
OF 

### WET VS. DRY 

### FGO TECHNOLOGIES Figure **2-10~** Typical Rotary Drum Vacuum Filter

2-23 SL-009510 As mentioned earlier, chlorides are absorbed from the flue gas and they concentrate

in the recycle slurry solution

. A small blowdown stream may be required
to remove chlorides and other contaminants from the process. If the gypsum

is not being sold, washing the filter cake is not required and chloride-control

of the dewatering process

is significantly less complicated. Less costly rotary drum vacuum filters can be u5ed if the gypswn

is to 

### be sent to a landfill, although

a water treatment faCility will still be necessary

to treat the blowdown from the absorber

. Landfill disposal requirements
are very site-specific, and depend on parameters such as the actual chemical makeup of the gypswn waste product, local climate, and soil conditions. Dewatered gypsum from the belt filter is deposited on a collecting conveyor, then conveyed out of the dewatering building and stacked on the

· ground. The gypsum

is then loaded into trucks with
a front-end loader and then hauled away

. Gypsum also bas potential for reuse,

e . g., feeds

t ock for wallboard manufacturing.
For this 

### to be an attractive form of reuse,

a large quantity of gypsum

is needed. Utilities with 500 MW gross or more of capacity and firing **high.~** sulfur coal are likely candidates

to pursue wallboard manufacturing options

. These type plants would also need 

### to be relatively ncar markets that would be in demand of large quantities of wallboard, such as urban areas. Gypsum can also be used for agricultural purposes

, as a soil additive

, or as an additive
to concrete

. Gypsum's inert nature renders

it viable for land-filling. E ntergyArkan
sas WBI

· 2 _ Dry vs We r FGD Srudy Rev )I ssu ed J 0- 28..08 P ro ject

1 23 03 .{)() 4

' Lundy'"twl'HG'f' **~JJK.** WHITE BLUFF STATION UNITS

1 AND
2 2.2.2.2.5 Staffing

2-24 Sl..009510 The conceptual design economic analysis includes
21 additional people for the O&M of the new wet FGD system, as summarized below. A discussion of the staffing costs can be found in Section 3.5.2

. ., Limestone unloading will require

a couple of personnel

to move the limestone into the reclaim hopper underneath the active pile and to move the rail cars through the unloader. o FGD process operations 

### will require an operator
to walk down the process equipment and check for malfunctions. Typical maintenance activities for the FGD system would involve the. conveyors, ball mills, including changing of ball load, recycle slurry pumps, mist eliminator, spray headers and nozzles, booster fans, hydroclones, rotary **dru~** filters, and waste conveyors

. ., Lab Technician/System Engineer for chemistry monitoring

. ., Waste loading
to trucks 

### will require additional operators. The larger amounts of solids requiring disposal will also require more time for this activity.

## ElfltltGY-""' WHITE BLUFF STATION UNITS

1 AND
2 

## 3. COMPARISON 3.1 DESIGN BASIS


## AND FGD

3-1 Sl.009510 S&L developed and issued to Entergy separate design basis documents for dry and wet FGD, as summarized



### in Table 3-1. Table 3-1. Design Basis Used for Dry FGD vs. Wet FGD. Comparison Parameter NetMW Heat input to boiler; mmBtu/hr Coal type Coal composition Carbon Hydrogen Nitrogen Sulfur Oxygen Moisture Chlorine Ash HHV, Btu/lb Flue gas flow, acfm Day bin

Value 844 each 8,950 100% PRB 49.92% 3.58% 0.67% 0.87% (2.0 lb S0
2 /mmBtu) 12.01% 27.72% 0.02% 5.2% 8,725 3,685,000
at 318"F 95% hoursWHITE BLUFF STATION UNITS

1 AND 2 Parameter Absorber Booster fans Waste recycling Waste storage Stack Reagent, ton/hr Trucks per day Waste, ton/hr Ttucks per day Makeup water, gpm Wet FGD..Specific Liquid-to-gas ratio Limestone stoichiometric. ratio Limestone quality Limestone storage pile Day bin storage Ball mills Absorber Booster fans Primary dewatering Secondary dewatering Stack Reagent, ton/hr

Value 3 x 33%, carbon steel (each unit) 2 x 50% (each unit) 1 x 100% (each unit) 3 days,

1 x 100% (each unit) No modifications 8.4 (both units) 10 17.8 (both units) 22 2,100 (both units) 80 1.03 90% CaCOa 30 days (both units) 24 hours {both units) 2 x 100% (both units) 1 x 100%, alloy 2205 (each unit) 2 x 50% (each unit) Hydrocyclones,

2 x 100% (both units) Drum filters,
2 x 100% (both units) 35-foot diameter, 1003-foot height FRP liner (each unit) 11.7 (both units)

3·2 Sl..009510

## WHITE BLUFF 

## STATION UNITS



# 1 AND 

# 2 

# 3.2 GENERAL ARRANGEMENT 3.2.1 Lime Spray Dryer (LSD) FGD S&L developed general arrangement (GA) drawing of major equipment and structures for the White Bluff Station dry FGD system. The GA drawing for the LSD FGD is presented

as Appendix
A. This GA was the preferred arrangement primarily because



# it minimized the ductwork length between the SDA outlet and the baghouse inlet, and eliminated turns or elevation changes in the duct. This offers long-term maintenance benefits because the shorter duct length results in minimizing the amount of solids that can drop out and accumulate
on the duct floor. Implementing
the GA will require demolishing White Bluff Station's Ash Handling Maintenance Building due to the location of the new spray dryers, and building

a new building directly north of the FGD system. Two lime silos are arranged near the lime preparation area **am~** 

# are sufficiently sized to store the reagent for 14 days of operation. The lime in the bulk storage silo will be pneumatically blown to a day silo located in the reagent preparation area. Because the reagent preparation area is located near the SDAs, lime slurr:Y will need to be pumped only
a short distance
to the top of each SDA. The recycle portion· of the dry FGD process will be local to the prospective unit and not included
in the combined reagent preparation area. A set of silos will be located near the baghouse inlet to receive baghouse recycle fly ash that will be slurried and re-injected into the SDAs. Two new booster lD fans will be placed in series with the existing lD fans. The booster fans will be sized to handle the additional pressure drop associated with the dry 

# FGD. 

# 3.2.2 Wet FGD S&L developed GA drawings of major equipment and structures for the White Bluff Station wet FGD system. Appendix

B is a GA
the

and structures for a wet LSFO FGD system.**mt"':dtG:Y~W(.** 

## WHITE BLUFF STATlON 

## UNITS

1 AND


## 2



# 3-4



# SL-009510 The absorber vessel for each unit is located
to the cast of the unit. The duet located after the existing ID fans is the location of the tie-ins for the wet FGD for each unit. A rather short duct is added to divert the flow to each absorber area. Two new booster ID fans are then shown to feed
a single absorber, which then feeds

a single new chimney per unit. The old ehimney could be demolished

or capped and left in place. If this is the case, routine maintenance will need to be performed
on the chimney for structural integrity and potential deterioration. The arrangement
for the wet FGD flue gas path is relatively straightforward. The dewatering system
is common for both units and located north of the units. This location allows easy access for the trucks that 

# will haul away ihe gypsum byproduct The existing ESP and fly ash system will remain as is and are unaffected by the retrofit of the wet FGD, because the wet FGD is downstream
of the ESP. 

# 3.3 COMPARISON
OF SYSTEM FEATURES 3.3.1 Absorber Vessel The wet FGD system has an advantage

in that
a single absorber can be used at each linit 

# at White Bluff. Single absorbers have been built for up to 1,000 MW of flue gas. A single absorber per unit greatly reduces the capital cost of a wet scrubber. A dry FGD system uses
a spray dryer. For White Bluff Station three SDAs were considered per unit. Some utilities are starting with SDAs that could be sized for one-half of a White Bluff Station unit's flow. The feasibility
of a SDA vessel of this large

a size has not yet been proven. A single vessel allows the system to be designed without dampers. This is a significant cost saving and reduces O&M of dampers and auxiliary power for heated seal air. With two or more dampers will be included
to Without

the

of a two- or three-absorber**El'lfi"EnGY~tfiC** WHITE BLUFF STATION UNITS

1 AND
2

3·5 SL-009510 15,000 ppm are expected inside of the vessel. This alloy is a fairly new material that only recently

is being used on FGD systems. Additionally,
the wet/dry interface
at the wet absorber's inlet will need alloy C-276 to protect this very corrosive location.
In general, wet FGD materials are more expensive than dry FGD materials. The single-absorber vessel represents cost savings in wet FGD but the carbon steel materials of construction are an advantage for dry FGD. Both of these features have been- considered

in the capital cost estimates completed for these two technologies. 3.3.2 Chimney Wet FGD technology typically

is installed benveen the outlet of the existing particulate collector and chimney. However, most retrofit wet lin_Iestone FGD units are unable to use the existing chimney,

as the chimneytypicallywould have been designed rofhotflue·gas

at bet\veen 70-100 fi/sec exit velocities: To accommodate saturated flue· gas from

a wet limestone FGD system, wet stacks typically are designed using

a corrosion-resistant

flue with

a design gas velocity of 55 fi/sec or less. Adding

a new chimney for each unit is deemed more cost-efficient

as opposed to a common chimney with dual flues for both units, due to complications with duct work aroun.d the existing coal conveyor. Using one chimney for each unit will minimize expensive ductwork downstream
of the absorber that typically requires either FRP- or C-276-clad liners to avoid corrosion. The capital cost estimate includes two new FRP-lined chinmeys. Reuse of the existing chimney

is often

a significant cost advantage for a dry FGD system. 3.3.3 Chemistry The wet FGD system has a more complex system operating chemistry

to monitor than the dry FGD. The wet FGD scrubber vessel liquor chloride content must be monitored

to prevent absorber corrosion. The pH level must also be monitored

to maintain high S0 2 removal efficiency and minimum corrosion. Scale oxidation rate is monitored

to avoid scrubber
and

the constant,

it

to have an that**~y~wc,_** WHITE BLUFF STATION UNITS



### 1 AND 

### 2



### 3-6 SL-009510 

### two. Generally,

a dry 

### FGD system needs to be monitored more carefully from hour to hour, whereas,

a wet FGD system opetates
at a fairly steady pace. 

### 3.3.4 Chloride Slowdown The wet FGD system absorbs HCl 

### from the flue gas and 

## it is concentrated

in the recyele water. The absorber can be designed for up to 15,000 ppm of chloride without corrosion problems. To limit chloride buildup, some water
is blown down to 

### remove chlorides. This water
is often mixed with other plant water and allowed
to discharge with other effluents.
If commercial-grade gypsum

is to be produced, there will be a wastewater stream off the belt filters 

## that will 

### have to be treated. If the product

is to be land-filled, the wastewater will be discharged with the blowdown stream and 

### will have to be treated as well. Based on the chloride level of200 ppm in the fuel and the chloride level np to 390 ppm 

## in the blowdown water, there will be always be a blowdown from the wet FGD. The cost estimate therefore includes the wastewater treatment facility. Dry FGD does not have
a wastewater blowdown stream or a wastewater treatment facility. 

### 3.3.5 Water Consumption System design calculations
for wet and dry FGD systems
at White Bluff Station predict that a wet FGD system would consume 1,260 gallons per minute (gpm) per uuit and the dry 

### FGD system 1,050 gpm per unit, while burning 2lb SO:JmmBtu coal. The wet FGD system

is estimated

to 

### have
a waste discharge of 43 

### gpm per unit 

### that would need to 

### be ehemical1y treated to 

### precipit;te out the metals for the base case. This 43-gpm level can be reduced,
if 

### necessary and is 

### based on land-filling the gypsum. The dry 

### FGD system does not have
a wastewater discharge. 

### 3.3.6 S0
2 

### Control The FGD systems considered have unique capabilities

to remove 

### S0 2 . 

### As previously



### a wet FGD is known
to 

## FGD Q"dPYYI<!



### can achieve lower**~~11$(:.** 

### WHITE BLUFF STATICN.UNITS



### 1 AND


### 2



## 3-7

SL-009510 Table 3-2. Typical PRB Coal S0 2 

### Emissions Expected from FGD Technology Parameter

Lime SDAFGD WetLSFOFGD Lowest achievable 

## S0 2 

### emission (lb/mmBtu) 0.06-0.08 0.03-0.06 Achievable 24-hour average (lb/mmBtu) 0.12-0.15 0.09-0.10 Achievable 30-day average {lb/mmBtu) 0.10-0.12 0.07-0.10 Achievable annual average (lb/mmBtu) 0.08-0.10 0.06-0.08 

# 3.3.7 Particulate Control Particulate control
is a pivotal issue in selecting dry 

## or wet FGD systems because, although

it is not a necessary part of the wet FGD process,

it is integral
to a dry 

## FGD system. Recently, wet FGD suppliers have provided particulate control guarantees

as low as 0.015 lb/mmBtu with inlet particulate
up to 0.12 lb/mmBtu. Since White Bluff Station is equipped with an existing ESP, the particulate enlissions would be maintained with wet FGD or lowered
to O.OISlb/mmBtu.
The baghouse for the dry 

## FGD would be designed
to lower the emission
to O.Ol2lb/mmBtu giving an advantage
to the dry 

## FGD system over the wet FGD. As for condensable particulate matter, the wet FGD system promotes the condensation

of sulfuric acid mist more than the dry 

## system due to the lower outlet temperature. For either system the condensable particulate

is found assuming 0.8% 

## of the S0 2 

## in the boiler is converted
to S0
3 , 

## the outlet of the stack would contain

2 ppm of S03, or 63 

## lblhr; converting this emission
to a sulfuric acid mist basis gives 77 lblhr of condensable particulate. Even with the addition of SCR on the unit, the additional conversion
of 

## S0 2 

## to S0 3 

## would result in 7 ppm of S0
3 , 

## or 289lblhr of sulfuric acid mist. This level

is greater than the current operating pennit limit of 261 lblhr of condensable particulate matter,

a permit revision would then be necessary once an SCR is 

## in place. Fugitive emissions and additional emission points from ancillary equipment must be taken into account when choosing
an FGD technology. The wet FGD process limestone and gypsum piles, which adds

aWHITE BlUFF STATION UN!TS



### 1 AND 

### 2

3-8 

### SL-009510 Similarly

to the fugitive emission sources, several transfer and emission point sources are added to each FGD system. Storage silos, common
to both types ofFGD systems, contribute

to particulate emissions, but are controlled by vent filters by up to 95%. The reactant preparation building, common

to both types of FGD, also contributes

to particulate matter emissions, but ventilation fans reduce these emissions by up to 75%. Lastly, the wet FGD system conveys limestone and gypsum byproduct via belt conveyors, which add potential emission points, but dust suppression system are available that can reduce these emissions by up to 75%. 

### 3.3.8 

## S03 Removal Sulfur trioxide (S0

3 ), 

### which condenses

to sulfuric acid aerosols
in an FGD system,

is removed efficiently (greater than 90%) with
a dry FGD/baghouse equipment combination. Wet scrubbers have less affinity for acid mist and they typically capture between 25-50% of sulfuric acid aerosols, according

to FGD suppliers. 

### Alkali injection (i.e., Trona) upstream of a particulate collection system or even the addition of a wet ESP would be required for a wet limestone FGD system to achieve the same level of acid mist removal
as the inherent removal
in a dry 

### FGD system. S&L would expect alkali injection

to be considered BACT for acid mist. The emission of sulfuric acid mist, if above

a threshold value of 7-10 ppm at the stack, may result 

## in a pale blue plume Visible after the water vapor plume dissipates. White Bluff Station fires PRB coal, which has low S0 3 

### concentrations,

so a colored plume
is not expected. The current 80 3 

### emission from the White Bluff units is estimated

to be 3 ppmvd (@3%0

2 ) 

### or less with 2lb SOimmBtu PRB fuel (assuming 0.6% oxidation

in boiler, 25% removal across air heater, and 2 ppm across ESP). With wet FGD, the outlet concentration will be approximately

2 ppmvd (@3%

0 2 ) 

### with 25% removal efficiency and with dry FGD, the concentration will be less than

1 ppmvd (@3%02). The advantage
of a dry FGD could be realized only in the case of a future SCR system. If the future SCR system

is designed with 3% SOrto-S0

3 

### oxidation (only with PRB coal), the emissions from the wet FGD could 

### be as high as 9-12 ppmvd S0
3 , 

### compared
to dry FGD, which could be limited


### to 2WHITE BLUFF STATION UNITS

1 AND
2

3-9 SL-009510 the fuel additive injection
to convert elemental mercmy into ionic mercury will be required. ACI inject halogenated activated carbon before the SDA and up to 90% removal
is with
a 2 lb/mmacffeed rate. Similar
to dry FGD, wet FGD can remove oxidized mercury. Unfortunately, mercury
in PRB coal usually

is in the elemental state, which is not as easily removed. To use the wet FGD capability

to remove mercury,

a halogenated (chloride
or bromide based) fuel additive can be used that converts the elemental mercmy
to the oxidized form. The mercmy can then be captured by the wet FGD. An overall removal of 70..80%

is possible with wet FGD. To achieve higher removal efficiency,
an additional activated carbon injection system ahead of the ESP or ahead of a polishing baghouse may be required. The technology
of converting elemental mercmy
to oxidized mercury still· needs to mature. However,

if this technology develops
as **anticipa~ed,**

an ACI system may not be required
if wet FGD systems arc installed on the White Bluffunits. On February

8, 2008, the U.S. Circuit Court of Appeals for the District of Columbia rejected the strategy of regulating mercury emissions through

a cap-and-trade program and therefore vacated the Clean Air Mercury Ru1e (CAMR). The rejection of the cap-and-trade regulation will compel the U.S. EPA to develop

a new set of standards for electric generating units to reduce mercury.

It is uncertain when this will occur, however

it is believed

it will take several years. 3.3.10 Preliminary COa Considerations
for Dry and Wet FGD The area needed for the C0
2 removal system (physical footprint) for a wet FGD is somewhat smaller than for a dry FGD. This is primarily due to the fact that C0 2 removal on a unit equipped with

a dry FGD requires adding

a wet chimney since the gas has to be further cooled before entering the CO:z equipment. The C0 2 equipment requires

a pre-scrubber/cooler

to obtain S0 2 emissions below 10 ppm, which
is the maximum inlet S0 2 concentration into
a absorber

to reduce sulfur contamination. Therefore treatment

to remove additional would be needed onWHITEBLUFFSTATIONUNITS1AND23-10Sl-009510AwetFGDsystemproducesmoreC02thanadryFGDduetothechemicalreactionswithcalciumcarbonate(CaC03),thereleaseofonemoleofC02isaccomplishedforeverymoleofS02absorbed.TheC02isformedthroughthedecompositionoflimestone{CaC03)toformcalciumsulfite(CaS03).C02makesupapproximately44%byweightofthelimestone,dependingonpurity.Thereforeforeachtonoflimestoneconsumed,therewillbeapproximately0.44tonsofC02formed.Withtheoperatingcaseofaninletconcentrationof0.8lbSOz/nunBtuatotalof11.7tphoflimestonewouldbeconsumedforbothunitscombined,whichtranslatesto5.1tphofCOz,frombothunits.Thistotals45,100additionaltonsofC02peryearfromWhiteBluff.Toputthisinperspective,thecombustion-basedC02emissionsfortheWhiteBluffunitstotalslightlyover16milliontonsperyearcombined.Therefore,theC02producedfromthepresenceofCaC03isveryminimalwhencomparedwiththeC02emissionsfromthecombustionofcoaLThecombustionofthecoalproducesroughly940tphperunitatWhiteBluffStation,whiletheaddedC02producedinthewetFGDsystemislessthan1%ofthistotal.ThedryFGDuseslime,whichhasnoaddedproductionofC02initsuse.NoteworthyisthatlimeisaproductoflimestoneandeventhoughdryFGDisnotemittingC02,thekilnthatisproducingthelime(CaO)generatesC02fromthegasdrivenoffthelimestonewhenheatingitto2000-2400°F.OnemoleofC02isdrivenoffforeachmoleoflimestoneconsumed;thisresultsinmoreC02beingproducedinforminglimethanitdoesinusinglimestoneasareagent.Additionally,thereisfuelconsumedtoproducetheheat,whichemitsC02,andthemotorsthatdrivethemechanicalportionoftheprocessrequireenergy;thisdrivestheC02emittedfromthelifecycleoflimetoalevelexceedinglimestone,butthereleasepointismovedtothelimesupplierandEntergywouldnotbeconcernedwiththisemission.3.4COMPARISONOFCONSUMABLESANDWASTES3.4.1PowerConsumptionTheO&Mcostspresentedhereinaccountforpowerconsumption.ThewetFGDconsumes8.9MWandtheboosterWHITE BLUFF STATION UNITS



### 1 AND 

### 2 

### 3.4.2 Reagent Consumption

3-11 SL-009510 

### Dry FGD systems use a more expensive reagent (quicklime
or hydrated lime) than limestone-based FGD systems (more dollars per mole of calcium), and the reagent must be stored in a steel or concrete silo. Limestone can be stored outdoors
in a pile and moisture

is not a problem
in its reactivity. The wet FGD system consumes 5.9 tph of reagent per unit, while the dry 

### FGD system consumes 4.2 tph of reagent per unit. Reagent utilization for a dry FGD system
is poorer compared

to a wet limestone system meaning the reagent SR for a dry 

### FGDsystem

is higher than the SR for a wet limestone FGD system (on the same basis) to achieve comparable S01 

### removal (more moles of calcium per mole of sulfur dioxide). The cost of reagent

is provided for in the O&M costs presented herein. **3~4.3** 

### Waste Byproducts For dry 

### FGD systems, the resulting byproducts are in dry 

### form and can be handled with conventional pneumatic fly ash handling equipment. The dry 

### FGD waste containing CaS0

3 • 

### 0.5H

2 

### 0, CaS0

4 • 

### 2H20, Ca(OH)2, and fly ash is 

### land-filled similarly
to waste containing just fly ash. This material

is stable in the landfill and could be fixated with fly ash to make
it less permeable. Wet FGD waste
is 99% CaS0

4 • 

### 2H 2 

### 0, which would be land-filled. Again, the wet FGD waste can be fixated with fly 

### ash and addition oflime to make
it 

### less permeable. Currently, most utilities can dispose both of these wastes in a lined landfill. Additionally, there is no liquid waste from

a dry 

### FGD system, whereas wet FGD systems typically produce

a liquid waste stream, depending on the disposition
of the byproduct.

In the caSe of the White Bluff Station,

a wastewater treatment plant may be required
to treat the liquid waste prior to discharge due to the high chloride level of the makeup water from cooling tower blowdown. The wastewater treatment plant produces

a small volume of solid waste, rich in heavy metals (including oxidized mercury) that can be disposed of in a typical landfill.
A dry FGD can provide an outlet for process wastewater from other parts of the power plant. Since the dry FGD system OYilroauct. The**I!H'n:t:Gl'~WC** WHITE BLUFF STATION UNITS



### 1 AND 

### 2 

### 3.5 SULFUR REDUCTION TECHNOLOGY COST EVALUATION 3.5.1 Capital Cost

3-12 SL-009510 S&L's capital cost estimates for a retrofit dry FGD and
a retrofit wet FGD system for White Bluff Units

I and 2 encompass the equipment, material, labor, and all other required direct costs. The underlying assumption

is that the project will be implemented

on a multiple contracting basis. The capital costs are based on burning 100% PRB coaL The capital cost estimates provided herein are "total plant cost," and include the following: • Equipment and material " Installation labor " lndirect field costs and BOP engineering • Contingency (20%) • Erection contractor profit (at 10% of material and labor) • General and administration

(at 5% of material and labor) ., Freight o Allowance for funds used during construction (AFUDC [8.24%]) " Sales/use tax (not included) " Startup and commissioning " Spare parts

( 1% of equipment) License fees and royalties are not expected for the proposed control strategies. The capital costs are summarized



### in Appendixes

C and D for dry and wet FGD, respectively. The capital cost estimates for installing dry FGD or wet FGD at White Bluff Units

l and 2 include the following:WHITE BLUFF STATION UNITS

1 AND 2 " Slurry storage tank with 24 hours of capacity " Slurry feed pumps for each absorber " Slurry pipe loops for the Units

l and 2 absorbers 3.5;1.1.2 Dry FGD " Lime delivered by truck o Silos for long term storage, 14 days " Ball mill slakers " Slurry storage tank with 24 hours of capacity " Feed slurry pumps 3.5.1.2 Absorber Systf!ms 3.5.1.2.1 **~etFGlJ** "

1 x 100% absorber for each unit • Spray headers along with one slurry recycle pump for each header " Oxidation
air compressors
for each unit • 2205 alloy absorber, wet/dry interface- solid C-276, and outlet duct C-276 clad 3.5.1.2.2 Dry FGD o
3 x 33.3% absorbers for Unit

I and 3 x 33.3% absorbers for Unit
2 " Pulse-jet baghouse, 3.5:
I air-to-cloth ratio, one for each absorber 3.5.1.3 Flue Gas Systems 3.5.1.3.1 Wet FGlJ • Inlet (carbon steel) and outlet

3-13 SL-009510

# --""" WHITE BLUFF STATim4 UNITS

1 AND
2 3.5.1.3.2 Dry FGD • Inlet and outlet ducts (carbon steel) e 2 x 50% booster induced draft (ID) fans for each tmit 3.5.1.4 Byproduct/Waste Handling 3.5.1.4.1 WetFGD e Hydroclone separator for each unit 

## • Sluny pipeline from each absorber 

### • Rotary drum vacuum filters 

### • Stackout conveyors e W astcwater treatment

- minimal 3.5.1.4.2 Dry FGD • Waste recycle system • Waste conveying system • Silos with
3 days of waste storage capacity • Dustless unloaders 3.5.1.5 Electrical/Instrumentation 3.5.1.5.1 Wet/Dry FGD • Transformers • Switchgear • Instrumentation 3.5.1.6 Makeup Water Supply/Wastewater TreatmentWHITE BLUFF STATION UNITS

1 AND
2 3.5.1.7 **Balance~of-Plant** 3.5.1.7.1 Wet/Dry FGD "' Compressor
for instrument air, service air "' Foundations, steel, demolition, relocations, new storage warehouse, etc. "' Roads, storm drainage, etc. 3.5.2 Fixed and Variable Operating Costs

3-15 Sl-009510 The fixed O&M costs determined for this study consist of operating labor, maintenance labor, maintenance material, and administrative labor. The wet .FGD will require an estimated
21 additional full-time operators and ,. maintenance personnel and the dry FGD will require an estimated

16 additional full-time operators and maintenance personnel for eac"[ shift fqr both units. The operators would be looking afteF the absorber system, reagent preparation, and byproduct/waste system. The limestone receiving/handling
will also require an operator. The existing shift supervisor's will handle added responsibility
for the FGD system. Due to existing work load on the plant chemist, an additional lab technician will be added for the .FGD system. S&L's estimated staffing levels for White Bluff are as shown in Table 3-3. Table 3-3. FGD System Labor Requirements Staff Reagent unloading Absorber Dewatering/reagent preparation Gypsum handling 1-l<>•r'\!rloltlu ash hnncrillru' OryFGD 2 10 0 0 WetFGD 2 10 5 2

# --""- WHITE BlUFF STATION UNITS

1 AND 2



### 3-16 SL-009510 Annual maintenance material and labor costs shown herein have. been estimated based on teclmology operating experience

in the U.S. The annual maintenance cost includes maintenance material for various subsystems and the labor required
to perform the maintenance. The annual maintenance material and labor is 0.07% and 0.065% of the initiai equipment cost in the capital cost estimate for wet and 

### dry FGD respectively. Variable O&M costs determined for each application include the cost 

### of consumables, including reagent (lime or limestone), byproduct management, water, and power requirements. These costs have been calculated based on the capacity factors provided by Entergy. The O&M 

### cost basis with 0.8lb SOimrnBtu

as operating 

### sulfur is shown in Table 3-4: Table 3-4. O&M Cost Basis (both units combined) Parameter WetFGO DryFGO Cost($) Limestone,
tlh

11.7

0 38.00 $/ton Lime, tlh

0

8.4 107.00 $/ton Waste disposal, tlh

22.6
17.8
8.58 $/ton Auxiliary power, MWH

28.0
22.8 47.00 $/MWH Water, gpm

2,522 2,100 0.92 $/1000 gal Bag replacement

0 Every

3 years 110 per bag The following basis was used to calculate net present value (NPV): • Evaluation period

- 40 years • Discount rate

- 8.24% • Capital cost escalation rate- 3.0% • O&M cost escalation rate

- 2.0%**~Y'~IHC.** 

### WHITE BLUFF STATION UNITS



# 1 AND 

# 2

3-17

SL-009510 

## Also note that for the wet LSFO FGD and dry 

## FGD, reagent cost and byproduct management cost a!e at 

# 95% SOz removal. 

# Wet FGD 

# is capable of98% S0 2 

## removal, but the system comparison

is based on 95% as the compliance with SlP requires the emission limit of 0.15 lb S0 2 

## /mmBtu. Auxiliary power costs developed reflect the additional power requirements associated with operation
of the new booster ID fans as well as the estimated power consumption
for the absorber, reagent preparation, and byproduct handling areas. 

# 3.5.3 Preliminary Cost Summary Based on the economic parameters-
the total capital cost, fixed O&M cost, and variable O&M cost-

a fmancial model was developed

to calculate the NPV and 

# leveliz~d annualized cost to determine

a low-cost solution. The model.inputand resultS for the base case are presented


# i!l Appendix
E, which **s~arizes**



## a comparison
of wet and dry 

## FGD installation costs for two units. Table 3·5. Summary Comparison

of Wet and Dry FGD Levellzed Costs (yr. 2013} for White Bluff Units

1 

## & 2 

## WetFGD- DryFGDWith Cost Parameter Limestone

Bag house Capital cost, M$ ($/kW)


# 744.8 (441) 706.9 (419) Fixed O&M cost, M$/yr ($/kW-yr)



# 8.4 (4.95)

7.1 (4.22) Variable O&M cost, M$/yr {$/MWh)


# 17.4 (1.58)
19.9 (1.81) Total O&M cost, M$/yr



# 25.8

27.0 NPV,M$



# 1,484
1,449 Differential, M$



# 35

0 Annualized cost, M$/yr



# 113.8
111.1 Differential, M$/yr



# 2.7



# 0

### WHITE BLUFF STATION UNITS



### 1 AND 

### 2 

# 3.5.4 Sensitivity Analyses Sensitivity analyses were perfonned with the following key parameters: • Evaluate impact of burning higher-sulfur fuels-

3 !b SO:/mmBtu and 5 

## lbs SOimmBtu. • Eva1uate impact of! ow-cost reagent delivery by train. **<~~** 

## Evaluate impact of two-absorber module design for dry 

## FGD. • Evaluate impact of mercury control with ACI for future Hg-MACT. .. Impact of SCR- related to sulfuric acid control.



# 3-18 SL-009510 

# 3.5.4.1 Evaluate Impact of Burning Higher-Sulfur Fuels-

3 lb S0 2 

# /mmBtu and Sib S0
2 

# /mmBtu The economic analysis was performed with
a variation
in the fuel levels of S0 2 

## subjected

to scrubbing. Figure 

# 3-1 suffimarizes the impact due'to 'the changes in 

# so2 operating levels.- AlllUU!SA5. ""'- WHITE BLUFF STATION UNITS

1 AND 2 Figure 3·1. Impact of S0 2 In Fuel on levelized Cost

3-19 Sl-009510 **170~~~~~~~~~~~~======~.------------------------------------------------------,** Des. S02 lbfmmBtu
2.0 3.0 5.0 Oper. S021b/mmBtu

0.8 0.8 5.0 **100~--------------------------------------~----------------------------------------~--------------------------------~** 0

2

3

4

5

6 S02, lb/mmBtu The base case comparison
for 2lb SOz/mmBtu (operation

at 0.8lb SOz/mmBtu) indicates that the dry FGD would cost approximately LO% lower cost than wet FGD. The main difference

is due to the cost differential between lime and limestone. The annual differential

in O&M cost due to reagent cost of more than $3.4 million negates the higher capital cost for wet FGD. The differential

is trigher at 3 lb/mmBtu coal predominantly due to somewhat higher cost associated with capital for wet FGD system. Again, the O&M cost was based on 0.8 lb SOz/mmBtu.WHITE BLUFF STATION UNITS

1 AND 2

3-20 SL-009510 cost of rail delivery
is lower than $10 million, the reagent cost saving due to lower-per-unit cost could be justified with rail delivery. The results are shown in Figure 3-2. Figure 3-2. Impact of Rail Delivery on Levelized Cost 1M **~~~~==~==~~~~~========;---~-------------------------------------------------,** [)<)s.. S02 lblmmBtu
2Jl 3.0 5.0 Oper. 502 lb/mmBtu
0.8 0.8 5.0 150 140 **~** :e 

### !130

·- . --

- . -- . .--
.. ! ] 110

. ---·-··

155.60 WetFGO **100~----------------------~----------------------------------------------~-J** 0

2

3

4

5

6 S02, lb/mmBtu 3.5.4.3 Evaluate Impact of Two-Absorber Module

for FGD The dry FGD system
is based on the use of three absorber modules. Alstom htid proposed two modules on units with

a similar gas flow in the past. However, B&W and Siemens had utilized three modules. The use of twoWHITE BlUFF STATION UNITS

1 AND 2 Figure 3-3. Impact of Two Dry FGD Absorber Modules on levelized Cost **~** ::e 140 **~** 0 **~** 130 j

.. ..

**3~21** SL-009510 110 ---- --- ------ ------- _______
..._ __ ----------- ---------------------------------------------- --------------------------- •10'7.08 **~108.22** ,..,......

. OryFGO II. 1'0.:>.21 **100~----------------------~------------------------------------------------~** 0

2

3

4

5 S02, lb/mmE!tu By lowering the capital cost for dry FGD by 7%, the annualized cost differential reduces
to 2% from 6.5% still favoring wet FGD. However,

if the sulfur level drops to approximately

1.5 lb SO:JmmBtu,
the dry FGD becomes cost-competitive. 3.5.4.4 Evaluate Impact of Mercury Control with ACI for Future Hg-MACT and FGD

PRBWHITEBLUFFSTATIONUNITS1AND2achieved(similartoregulationsinIllinois),byACIaheadoftheESPforwetFGD,thesensitivityisaspresentedinFigure3-4.Figure3-4.ImpactofMercuryControlwithACIforFutureHg-MACTonlevefizedCost170Des.S021bfmmBtu2.03.05.0150::;;140u..,130jOper.S02lbfmmBtu0.80.85.0.....---..•126.59100023456S02,lbfmmBtuACIaheadoftheESPraisestheevaluatedcostsignificantlyforthewetFGDsystem,renderingdryFGDalow-costsolutionbelow2and3!bS02/rnmBtufuel(operatingat0.8lb/mmBtuPRBcoal).However,ifACIhasamajorpertbnma11ce,aCORPAVmayberequired.ThesensitivityofaddingCORPACtowetFGDisshmvnin**~Y~I#C.** WHITE BLUFF STATION UNITS

1 AND 2 Figure 3-5. Impact of Mercury Control with ACI Ahead of COHPAC Baghouse for Wet FGD to Meet Future Hg·MACT

3-23 SL-009510 **170~~~~~~~~~~~======~~---------------------------------------------------------------------,** Des. 502 lb/mmBtu
2.0 3.0 5.0 

# ,160 Oper. S021b/mmBtu

0.8 0.8 5.0 Rr.££GO **~)%CI EtA!lsori?.~IJf!l!niMJ!!fmroACEL** 

··--

. Wet FGO

• ACI at COHPAC Inlet (1.51blmmACF) 5lb/mmBtu
do not require ACI 

### B11a.az

WetFGO 110 -·-··-"··-·-· --

.. ----·-·--··--·--------------·--·-------------·----- **100~. ------------------------~----------~----------~----------~----------~**  0

2

3

4

5 502, lb/mmBtu The differential between dry and wet FGD increases significantly



### if wet FGD requires the additional baghouse, rendering dry FGD even more economical. 3.5.4.5 Evaluate Impact of SCR

- Related to Sulfuric Acid Control The base dry and wet FGD system designs are based on the use of high-sulfur PRB coal. The dry system will have wet
the

level ofWHITE BLUFF STATION UNITS



## 1 AND 

## 2

3-24 SL..009510 

## dry 

## FGD system installed on 3 lb/mmBtu fuel will not require any additional alkali injection.

It 

## is assumed that if S0 3 

## control
is required, the 

## emissions will have to be lowered
to similar levels as dry 

## FGD, which could be lower than 

## 5 ppmvd (@3%0

1 ). 

## The Trona requirement was estimated

to achieve this level without any credit for 

## S03 capture 

## by the wet FGD. The injection of Trona required
to control S0 3 

## eliminates the cost advantage of wet FGD over dry 

## FGD up to 3 lb SOJmmBtu fuel. The results can be seen 

## in Figure 3-6. Figure 3-6. Impact of 50 3 

### Control with Trona Injection for Future SCR Resulting

in Increased Sulfuric Acid Emission **180~~~~==~=;;=~~~========~--------------------------------~** Des. 502 lb/mmBtu
2.0 3.0 5.0 

### Oper. S02 lblmmBtu


### 0.8 0.8 5.0 

### 170 2;·3;-amt5ilnrulfurwatf00wl!trequtnr563-con1rot

.. · with trona injection

if fired with Bitumonous co·al 

### 160+------------------------ 

### !>. 150 

## ~ ..r 

## 8 (.) 140 

# , 1l 

# ~ ...I 130 

### 120 

## below Jlb

DryFGD

175.11S'<IUGY-1!1<:. WHITE BLUFF STATION UNITS

1 AND 2

3·25 Sl-009510 sensitivities associated with reagent cost, PM 2.5, or mercury regulations. Dry FGD is the low-cost technology through most of the sensitivities. Dry FGD becomes even more attractive below 3ib/mmBtu fuel under the following scenarios: I. The capital cost can be reduced by 7% with the use of two modules
in lieu of the three modules anticipated in the base case design. 2. The Hg-MACT regulation requiring 90% reduction while burning PRB coal would give dry FGD

a cost advantage. 3. If the operating sulfur is lower than 1.2 lb/mmBtu, the dry FGD becomes cost-competitive with wet FGD due to reduced operating cost for lime as a reagent SCR system and particulate .emissions systems installations have no significant impact on the selection of technology

as long as current permit limits are maintained. The dry FGD system will have an advantage over the wefFGD system if the condensable emission rate is further· lowered from the existing level of265lb/hr (718lblhr
... total- 453lblhr filterable)
or 0.03 Ib/mmBtu.

If all the emission

is assumed
to be sulfuric acid, it will be equal to approximately

10 ppmvd (@ 3% 0 2 ). With the installation


## of either FGD for 2 lb SOz/mmBtu fuel, the sulfuric aCid emission rate will be lower than the current allowable limit. The wet FGD system designed for bituminous coal with 2, 3 and 5 lb/mmBtu will require an additional alkali injection system, whereas the dry FGD system installed on 2 and 3 Ib/mmBtu fuel will not require any additional alkali injection. The impact of future S0 3 control ahnost eliminates the cost advantage of wet FGD. The wet FGD system will have an advantage over dry FGD in the case of C0 2 emission control as it is capable of lowering the S0 2 concentration slightly better than the dry FGD. However, both systems will require some sort of pre-scrubbing, which will result in somewhat higher operating cost for the C0 2 scrubbing installed on the dry FGD.**~Y~mc.** WHITE BLUFF STATION UNITS

1 AND
2

Sl-009510 APPENDIX Dry FGD General Arrangement............ **~** ... -.
. ... . ....... - .... **--.~**

IEMt"''Y-...mc WHITE BLUFF STATION UNiTS 1AND

2

SL-009510 APPENDIX

B Wet FGD General ArrangementWHITEBLUFFSTATIONUNITS1AND2SL-009510APPENDIXCDryFGDCapitalCostEstimateSargent&Lt.ndyC0STsUMMARYREp0RTPage:1ChicagoEIITERGYEstimateNo:23335AWHITEBLUFFSTATIONProjectNo:12303004CONCEPTUALCOSTESTIMATEPreparedby:RK/PAG/DRYFGOSTUDY-EstimateDate:15MAY08Pricelevel:2008PROJECTSTART:JAN10;FINISH:SEP13COMMERCIALOPERATINGDATE:,SEP13TOTALTOTALTOTALACCT.NO.DESCRIPTIONEQUIPMENTCOSTMATERIAlCOSTLABORCOSTTOTALCOST101UNIT1ABSORBERAREA24,000,0001,362,00014,400,00039,762,000102UNIT2ABSORBERAREA24,000,0001,362,00014,400,00039,762,000103REAGENTPREPSYSTEM11,965,0008,687,00020,652,000104WASTERECYCLINGSYSTEM4,n4,ooo3,543,0008,267,000105ASHHANDLINGSYSTEM15,880,0001,341,0009,396,00026,617,000106COMMONSTRUCTURESAREA3,007,0003,171,0006,178,000107REAGENTKANOLINGSYSTEM1,750,0002,732,0006,512,00010,994,000111UNIT1flUEGASSYSTEM240,0001f,685,00017,620,00029,545,0001122FlUEGASSYSTEM240;00011,685,00017,620,00029,545,000113UNIT1BOOSTERFANS5,700,000168,000564,0006,432,006114UNIT2BOOSTERFANS5,700,000168,000564,0006,432,000115BAGHOIJSE44,000,0003,012,00022,000,00069,012,000121CIVIL\lORI(1,412,0003,115,0004,527;000151MECHANICALMISCELLANEOUS1,355,0002,797,0003,699,0007,851,000181PIPERACK2,652,0003,406,0006,058,000190DEMOLITIONCOSTS500,000500,000201ELECTRICAL8,475,0004,020,00012,710,00025,205,000211lllSTRUMEIITATION2,008,000811,000656,0003,475,000301MOBlliZATION/OEMOB!LIZATlOila1%OFLABOR1,426,0001,426,000302COSTDUETOOVERTIME•20,029,00020,029,0005-101S304PERDIEM-a$10PER19,754,00019,754,000HOUR305SPAREPARTSa1%OF1,500,0001,500,000EQUIPMENTQ5%TOTALCONSTRUCTIONCOSTS207,903,000417,297,000Sergent
& Lundy Chicago 1\CCT.IiO.

C 0 S T OESCRIPTION INDIRECT EXPENSES ESCALATION SAl.ES/USE TAX CONTINGENCY TOTAL PROJECT COST AFUOC (COll'!pOUI"lded Annually) GRANO TOTAl COST SUMMARY REPORT TOTAL TOTAL EQUIPMENT COST MATERIAL COST TOTAL LABOR COST FINANCIAl ASSUMPTIONS: ESCAlATlOU RATES: Equipment 3.000% Material 3.000% labor 3.000% Indirects 3.000% SAlES/USe TAX RATES: Equipment 0.000% Material 0,000% COOTIIIGEIICY RATES: Equipment 20.0% Material 20.0% Labor 20.0% Indirects 20.0% AFUOC Rate 8.240% from 2010

Page:

2 Estimate no: 23335A TOTAL COST 41,574,000 47,059,000 101,186,000 607,116,000 99,781,000 706,897,000Sargent

& Lundy Chicago Prf ce leva

t : 2008 SUMMARY CASH FLOW E!iTERGY WHITE BLUFF STATION CONCEPTUAL COST ESTIMATE DRY FGO STUDY

- PROJECT START: JAN10; FINISH: SEP13 COMMERCIAl OPERATING DATE: SEP13 Note: All costs are in thousands
of dollars 2010 2011 2012 2013 2014 2015 2016 TOTAL DIRECT AND

A 77246 209057 133748 38820 INDIRECT CCST

c 77246 286303 420051 458871 ESCALATION COST

A 4704 19385 16787 6183 c 4704 24089 40876 47059 COUTINGENCY

A 16391) 45689 30106 9001 c 16390 62079 92185 101186 TAXES

A

0

0

a

0 c

0

0

0

0 

## ------ ------ TOTAL CASH FLOW

A 98340 274131 180641 54004 c 98340 372471 553112 607116 AFUDC

A 1931 17650 40768 39432 c 1931 19581 60349 99781 

### ------ GRANO TOTAL COST

A 100271 291.781 221409 9!436 c 100271 392llg_ 613461 706897

2017 2018 Page:

3 Estimate No:·23335A Project No: 12303004 Prepared by: RK /PAG/ Estimate Date: 15MAY08 Cash flow by Year 2019 2020 2021**E~~tm:.** WHITE BLUFF STATION UNITS

1 AND 2

SL-009510 APPENDIX

0 Wet FGD Capital Cost Estimate

### Sargent

& Lundy



### C 0 S T 

# SUMMARY

R E P 0 R T
Page:

1 Chicago

EMTERGY

Estimate No: 2333411 WHITE BLUFF STATION

Project No: 12303004 CONCEPTUAL COST ESTIMATE
Prepared by: 

### RK /PAG/ \lET fGD CONCEPTUAL OESIGH COSTS Estimate Oate: 15MAY08 Price level: 

### 2008
PROJECT START: JAN10; FINISH: SEP13 COMMERCIAl OPERATING OATE: SEP13 TOTAL TOTAL TOTAL ACCT.!IO. DESCRIPTION EQUIPMENT COST MATERIAl COST LABOR COST
TOTAL COST 101 UNIT

1 ABSORBER-AREA 34,926,000 2,454,000 28,120,000 65,500,000 102 UNIT
2 ABSORBER AREA 34,926,000 2,454,000 28,120,000 65,500,000 103 REAGENT PREP SYSTEM 14,282,000 10,369,000 24,651,000 104 DEWATERING SYSTEM 12,687,000 9,211,000 21,898,000 105 COMMON STRUCTURES AREA 1,232,000 16,401,000 17,062,000 34,695,000 106 REAGENT HANDLING SYSTEM 2,500,000 1,891,000 3,715,000 8,106,000 107 GYPSUM HANDLING SYSTEM 4,500,000 156,000 2,422,000 7,078,000 111 UN IT 1 FLUE GAS SYSTEM 30,000,000 3,n4,ooo '5,819,000 39,593,000 112 UN IT 2 FlUE GAS SYSTEM 30,000,000 3,942,000 6,198,000 40,140,000 113 UNIT

1 BOOSTER FANS 5,300,000 168,000 564,000 6,032,000' 114 UNIT
2 BoOsTER FANS 5,300,000 168,000 564,000 6,032,000 121 CIVIL

I 

### SITEWORK

1,537,000 953,000 2,490,000 151 MECHANICAL MISCELLANEOUS 1,087,000 2,605,000 3,020,000 6,712,000 181 PIPE RACK

1,980,000 2,336,000 4,316,000 190 DEMOLITION COSTS

500,000 500,000 201 ELECTRICAL
8,625,000 4,945,000 13,171,000 26,741,000 211 INSTRU!o!ENTAT!ON
4,000,000 455,000 811,000 5,266,000 301 MOBILIZATION/OEMOB!LIZATI

1,330,000 1,330,000 ON 

# a 1X OF LABOR 

### 302 COST DUE TO OVERTIME

-
18,551,000 18,551,000 5-10•s 304 PER DIEM

- 

## a $10 PER HOUR
16,952,000 16,952,000 305 SPARE PARTS


# a 1% Of 1,894,000

1,894,000 EQUIPMENT 306 

### FREIGHT

Q 

### 5% OF **~~iER!Al**


### 2,147,000
2,147,000Sargent

& Lundy Chicago ACCT.NO.

C 0 S T OESCIUPTlOfl INDIRECT EXPENSES ESCAi.ATJflil SALES/USE TAX CONTINGENCY TOTAl PROJECT COST AFUDC (Compounded Annually) GRAND TOTAL COST SUMMARY REPORT TOTAL TOTAl EQUIPMENT COST **~TERIAL** COST TOTAL lABOR COST FINANCIAL ASSUMPTIONS: EScAlATIOM RATES: Equipment 3.000% ' Material 3.000% Labor 3.000% tndirecta 3.000% SALES/USE TAX RATES: Equipment 0.000% Material O.OGOX CONTINGENCY RATES: Equipment 20.0% Material 20.0% Labor 20.0% Indirects 20.0% AFUDC Rate 6.240% from 2010

Page:

2 Estimate No: 23334A TOTAL. COST 48,417,000 49,599,000 106,617,000 639.702.000 105.,110,000 744,812,000Sargent

& Lundy Chicago Price level: 2008 SUMMARY CASH FLOW ENTERGY WHITE BLUFF STATION CQHCEPTUAL COST ESTIMATE WET FGO CONCEPTUAL DESIGN COSTS PROJECT START: JAN10; FlNtSH: SEP13 COMMERCIAL OPERATING DATE: SEP13 1\lote: At L costs are in thousards
of dol Lars 2010 2011 2012 2013 2014 2015 2016 TOTAl DIRECT AND

A 81105 220402 141037 40942 !liD IRECT COST

c 81105 301507 442544 483486 ESCAlATION COST

A 4939 20437 17702 6521 c 4939 25376 43078 49599 CONTINGENCY

A 1n09 48168 31747 9493 c tno9 65377 97124 106617 TAXES

A

0

0

0

0 c

0

0

0

0 

## --------- TOTAl CASH FLOIJ

A 103253 21!9007 190486 56956 c 103253 392260 582746 639702 AFUDC

A 2029 18592 42941 41548 c 2029 20621 63562 105110 

## --------- GRAIID TOTAL COST

A 105282 307599- 233427 98504 c 105282 412881

- 646308 744812

2017 2018 Page:

3 Estimate No: 23334A Project No: 12303004 Prepared by: RIC /PAG/ Estimate Date: 15MAY08 Cash flow by Year 2019 2020 2021WHITE BLUFF STATION UNITS

1 AND 2

Sl.009510 APPENDIX

E Financial Analysis Summary

# . ' Entergy.

._., AIUIAJISAI, 

# IlK. 

# WHITE BLUFF STATION UNITS 1 AND 2 EVALUATION OF WET VS

. DRY FGD TECHNOLOGIES 

# Economic Parameter Inputs

**r---~** 

# 11.1
.. 

# -1...--

**~-'--'1--.**



# BBSis for Fixed Charges Evaluation 

# Period (years) Book Life· 

# Regutatad (years) on



# BBSa Year tor Expressing Costs 

# C<lmmercial Operating 

# Dale Compliance 

# Dale Escalation Rates Capllal Costs ('/,/year) 

# Q&M.Costs (%/yoar) 

# Prop11rty TW<es ('Myear) • Property TCill Rate 

# Insurance Rate 

# Tai< Rate 

# for Deferred Taxes Common 

# Equity Fractlon Preferred 

# Stock Fraction Debt 

# Fracllon Return on Common Equ i ty 

# Return on 

# Preferred Stock

Federal and State 

# tax rate,% Beforo lax eos1 

# of mone y Aner 

# tax eos1 

# of money Wei(lhted Annuity Factor Total Capital Requ i rement 

# Fixed Charge Rat& Parameter& tnveslmenl Book Depreclatlon 

# lT C Normalized Preferred AFUDC Recovery 

# Equity 

# AFUDC Recovery Det>t Book DepreciaUon Preler:red Book Depredation Equity Book

_ OepreclaUon Input Assumptions Source 

# Case 5 

# ·Wet FGD



# 7-Vear 

# Amort

PRBCoa l



# - ... • Econ Pall!millers

. 5-12-06 Econ ParameleiS. 5-12-06 

# 2008 2013 9/27/2013 Econ Parameters

. 5-12-08 Econ Parameters. 5-12-06 Econ Parametern. 5-12-06



# . Ema o s-1s.oa Econ Parameters.,5-12-08 Email5-15-06 Econ Parameters. 5-12-06 

# Included In Property 

# Tax 

# Econ Parameters. 5-12-08 Econ Parameters. 5-12.08 Econ Peramelera. 5-12-08



# ~;i~;L:i.~ Ecoo Paramelers.. 5-12.08



# . .. 8
. 23% 7.19"· 

# 7.67% 819 ,29 4,000 

# 20.482.350
8,596,442

909,416 10,976,491

**eNT!lRG~AR~ANSA8** 

# WBl·l DRY VS WlH fGDSTIJDY 

# !lEV l.A 

# ISSUED lllJ/.08 Projo<IIZJQl.$4

- 

# . case echno loiiY



# m~ :e- 1 ·Wet FGD 

# C... 2 • 

# Drv FGD 

# cas& 3 • Wet 

# FGD · 

# Cese 4 • 

# Drv FGO · ':\.r,

- 

# c- 6 • Wet 

# FGIP


# . t •

2'.Bl'

t#J 

# """"'"'-"'

! ' 

# , .. I Tax 

# r.veas Amort. 

# 7-Veer 

# Amort. 7-Year 

# Amort. 7-Yea< Amort. 7-Year 

# Amort.

MS/yl 

# ,..,
101.01
. 113

. 7& 

# 110.47 160.U 

# Fuel rv110 PRBCoal PRBCoal PRB Coal PRB 

# Coal PRBCoal

M$/yr 

# dl:y

**1~2** 

# lH.OI> 11 1 .7 1 .8$ 

# APPENDIX E SL-4:109510



# ---- -- -- - -- - ,.

# .EnietgY. 

# --"""
WHITE BLUFF STATION UNITS 1 ANO 2 EVAlUATION OF WET VS. DRY FGD 'TECHNOLOGIES



# Technology Base Year Cost·and Performance Inputs

Net Plant Capacity (MW) 

# Capadly Fodor (at 

# lo-&tv!te Oala) 

# Equl\iolenl 

# "••iloblllty Fa- 

# lwl. Paww (MW) 

# """ Power (UWI'olyuor 

# at lull 

# load) 

# Conallud!co 

# Ounollcn (monttu) Tle.ln Oulojje Outation 

# (ll'<ll\11\8)



# Amount 

# r. Exca,. o! 

# Normol Oulojje 

# Base Yaar ln-SoMmYear Total Water CooauntlliJQn (0\lm) 

# Waalo 

# Dlscooal (lll/hr) 

# Unit 

# Rata (IOMilV)

. 

# llmeslana Rate (ll>n>AY)



# O&M(lQQB $) 

# Bag Replo-t 

# Cost 

# Line, $/ton Umeatcna, 

# $Jton 

# Total 

# Water ReQUiremonl, 

# $/IOQQ 1181 

# Baa Cool

**l!.NTbii.OY~Wbl•l** 

# Olt\ ' Vt; Wli T rODST1Jl)Y

**~"\' lA~**  **~1)-').41** 

# tn;oa llJOJ-004

- **531,~.000** 

# Email 5-16-06 54,5S9,000 Emoll 5-11>08 

# 117 ,Z79,000 Email 

# 5-111-011 0 

# Email f>.1!M)II 

# 115 , 621,000 

# ErnaU

**Sol~** 

# 819,294,000 

# 819,294,000 

# 485 

# 22.569 APPEHlllX E SL.coi51Q

# I'I$<1UIIr••""''lru • Case 1

:2013 2014 :ztt1G 20Hi 2017 2f11!

**~019** 

# 21)20 2021 2022 

# 20i3 202.& 202.5 l'lij d( .t f> 

# 1 l Ill U U I)



# 7.142"'

2A5 

# 1.\149 14,200% 

# 2.51

**~.1..00**


# 0 

# 15,3111 978,576 

# 145,6515 

# 121.f.IB 

# 42.79 123.88 0.75 

# .... 14.286% 

# 14.200% 14.5&% U<181 

# 13.67% lQ.8a3.875



# 150,704 I!<. IT.! 

# 1.5125 

# 0 0.8104



# 1,0<>



# 11U,7M.005 24ii,9'\2,U6 

# 14.2.86% 2.51 

# 1.1657

0 18,521 

# 1,017,261 

# 151,72\1 

# 124-.73

**·~t65** 

# 126.36

0,71 

# 9.85 

# 14,286% 

# 1<.28ll% 13.ll!l% 

# 1.1717 78.74% 11.347,933



# 186,236 64.61 2.5733 

# 0 0.8Xi!D



# 1.00

104.991,625 3,51.903,7$4 

# 1•US6'rt 2.65 

# 1.1!H9

0 78,63-4 

# 1,(}18..738 1&1.944

**127.~** 

# 44.52 

# \28.68 0,7\J 10.05 

# 14.286'1\ 1<.28.,1 13.01% 1..1951 

# TaRS% n,364,11ll



# 1Ba,500

87,47 

# a ..

oo 0 0,7575



# 1.00



# 9<,194.203 «6,097,957 14.l6G% 2.72 1.2167

0 

# 7;3,5$$ 9SZ,938 142,130 

# 130.<1:() 45.41 

# t31.Mi



# o.ao 1Cl.25 

# 14.265% 14.285% 12.24% 1.2190 

# 71.89% 10,830,119



# 118,330 68.81 

# 2...7193 0 0.7067

\,00



# 83,29M31 529,39&,.38.4 

# 14.25&'1\ 2.'1'9



# '~" 0 

# 7l,7M 

# 955,9G1· 142,660 1.33.34 

# 46.32 1$4.09

0.82 

# 10.45 

# 14.200% 14.2®% 11.46'% \.2434 

# 72.12% 10,663,001



# 175,1!89 7U,QT 

# 2.7863 0 0.8593



# 1.00



# 74,fiGMl52 604,363,440 

# 14.286% 2.1l7 

# 1.Z142.

**~** 

# fi5,912 853,928 

# 127.382. 1:\<1.3< 

# 47.25 

# 13S.n

0.1\4 10.66 

# 14.265% H.;tOO% 

# 10,ft8% 1..2682 IJ.4AZ% 9,5Z5,100



# 158,009 84.01), 

# 2.8663 0 0.6151



# 1.00

66,077,869 

# 670,<441,329 

# 7.142% 

# 2.% 1.J02ll

0 

# G&,087 1\i\2,006 

# 131.584 13&41 

# 46.19 

# 139.51



# o ... 1<l8B
7.1.2% 

# 7.142% 10.13% 

# ,..,.,. 66.$% 9.{1:39.929



# 163,222 >Z.96 

# 2.9<8!1 0 O,ST39



# 1.00

60,859.836 731.,101;1.85 

# o.ooor. J.02 \,3322



# 0 10,8-iQ 

# 911',816 

# 1:1<1,SOO 142.5< <t9,11l 

# 142..30

O.Sll 

# 11.og:
0.000% 

# 0.000% 9.90% 1.3195

**8~.24%** 

# 10.239,052



# 16SI.B4Z

00.0<> 

# 3.Q23S 

# u 0.$354



# \,00

56,560.800 

# 161,662.063 

# U.OOO% 311 1.3621



# c 76.1-&.l J.JB6,9M 

# 147,208 14!),75 

# 50.14 

# 145.14 0.90 

# 1U2
O.IJOO% 

# O.OOO."A 

# 9.16% 1,3459 74.46% 11,0t0,Ul6



# 1lt2,6J1

8S.1S 

# 3,1070 0 0.41}9$



# 1.00



# 5.3.5,1,631

**1141~173.694** 

# (),{100% 

# 3.19 

# 1,:Wl6

0 

# 75,379 SY8,S78 

# 145.655 i49.03 !H.H 

# 141.1:.05

0.92 11.54


# .tJ.OOO% ftOOO% 

# 11.62"4 1.37Z8 

# 73.81% tO,fi93,815



# 180,704 t02.3Q 

# 3.1811 0 O..t!XiO

1.00

49.733,873 

# 890.9(}7 ,001 iJ,OOO% 0.000% 3.27 

# :.t;JS 1AZ41

**L~M2**


# 0 

# 78.521 '1,011,281 

# 151.72!:1

0.000% 

# 0.000'1. 0.000% 0.000% a.47%; 1.4002 78.14% 

# 11).4.7,93-9



# 1l!ll.z36 105-.H 

# 3.2710 0 

# 0,4347



# '·"' 

# ,.,.

**cooo~**



# 3.39 '.4.689 

# APPENtllX £

**S'-"""111~**



# O.OOC%

.'}>17 

# 't-5224



# O.D:I.JO"h fi,OOQ"'Ji. 

# o.ooor. G.()()O"S,



# ~·~---------------------------------------------------------------------------------------------------------------------------------



# 4~

# 1018 "t211 

# ,n:to 5n'l ?tt>.J" 

# 'M'f 21\3>t

__ 

# 10P 2M$ 2037 2038: 21J3G ZU40 Z!i41

**~** 

# ~1l1if,l44lf 

# '' 

# u 1a: 1., :w l'l 

# u·-- --:o **--l.--~~-i,--~6-----i:;:------,-,---~** 

# 0.0001<. 0.0001<. 0.000% 

# O.OOIJ'.\

**0.000~** 

# 0.000%

**0.000~4** 

# ~000% 

# 0.000,.. MOO% MOO% (HKIO'llo- 0-ll<l<n>



# JXt5 3.54 3,7:t 

# :t-.18 

# 100 

# "'"" •t.01 4.06 

# ·4.18 

# ,,, '"''

**~-32** 

# H4 4,$4 

# 1.5567 1.5Q17 

# US0115 1.tifi42 

# 1.7018 T-.73$9 1.1"790 

# 1.8TGt l,SQW 

# 1.${116 

# 1.9446 UU84 

# ZU189 

# 2.1256 

# ' 0 

# 0 0 0 0 

# 0 

# 0 0 0 

# 0 

# £8,061 70.845 7t'i.183 75,379 78,521 

# 76,634 73.555 

# 73.78a 65.912 68,007 882.096 tH7,87G- 

# aoo..saa 976,576 

# 1,017,251 1.()18,138. 

# 1152,93l! 9S5,J.m1 fi5J.028 

# 8S2.000 

# 131,584 136.900 

# t.t7,200

**t4fi,~li!S** 

# 151,72& 151.9« 

# 142.130

**1~500** 

# 127,362 131,564 170.31 174.15 178JlS 

# 182.07 1a&.11 

# 100.3£ 1JW,64 199.02 

# 203.00 57.00 58.75

**59.~** 

# 81.12 

# 62.34 

# ..... 

# ..... 66.16 67.48 

# 1Gttn 170.00 173..16 176.93 160.41 

# 184.00 187.76 

# 191 • .51 195,34 

# t.05 1.07 1,10 

# t.t2 

# 1.15 

# 1.17

. 1,2_0

**1~3** 

# 1.26 13.00 

# 132• 13.52 

# 13.71! 

# 14-.07 14.15 

# 14-,&4- 1.(,Jl3 1S.2:) 

# OJlOO% 

# ll.OOIJ'.\ 0.000% ll.llOO'I. 0.000% OJ)(I'O% 

# 0.000% O.OOO!h 

# a coo" ll.OOO'J;, 0.000';;. 

# "'"""" tLOOO% 

# O.OW'Y.

**~000%** 

# 0.0001<. o-.000% 0.000% 0.000%- 

# 0.000% 

# 0.00-D% 

# 0.000% 0.000% 0.000% 0.000% 

# 0.000% S.OO!'A- 

# 8.52% &.311% 3-.27% 8.14% 

# """" 1.lffi% 

# 1.77% 7.6$•4 7.54% 1.5768 1.8084. 

# 1.fMOO 1.1)734 

# 1.7009 

# 1.H10 1.775a 

# 1.8t14 1.6476 

# 1.8a4S: 

# 1lll24% 74.46% 71117% 

# 78.14% 7il.85%: 71.811%- 12.1:2lK 

# ..

**~** 

# .... OO.SS%

**72\~** 

# 10,Z3S.OQ2 11.()11l,01tl 

# 1Q,6.l03-.675 

# 11,347,933 

# 11.364,183 ,0.630,17ll 10,003,90-1 

# !1,5-25,708 R,.8-JG,029 

# 10,&4&.554

169,1l42 182,631 

# t80,7CW. 183.236 188,506 

# 176.330 118,38!) 

# 156,000 1&3.2.22 178,6n2 

# 122.0-5 124.80 

# 12HJ.1 130.46 

# 133.41 1J6.41 

# 139,.(8 

# 142.1>2 145,.83 

# l<\9.11 ;.t72.16 3.1884 3,0021 

# 3 .... 5 4.00Sil 4.(11!11' 

# 4.1585 

# ·Ut29 4.2683 4.324Q 

# 0 0 

# 0 0 

# 0 0 0 

# 0 0 0 0.2ae& 

# 0.26714 

# 0..2495 0.2321 0.2:171 0.2028 0.1890 0.1763 lt164fi 

# 0.1535

1.00 \.00 

# 1.00 1.(10 

# "'"' 1.00 1.00 1.00 1Jl0 1.00

25,303.416 26,308,855 24,841,721 

# 1.182.020,8:81 1,.208.320.7t8 1.2l3,171A37

# &wi'Wil@ll'f~--



# '"""

0.000% 0.000% 0.000% , Q,f.)(i()'il., 

# 0.000'¥. 

# O.(loi)('}% 0.000% 0..01)0% 

# 0.000% 0.000:%



# 4.!14 

# .os 4.86 4.91 

# s.oe 5.19 s.a1 &.43

**~.55** 

# s.ur 2, f7J5 2.1224 2.272.4 2.3235 2.3758 Z.42Dl l.-4839 2.53$6 0!:.5!)63

**2Ji5~** 

# 0 {) 0 0 0 t} f) 

# 0 0 

# 73,666 T..l,W!J 

# 73,006 73,668 73,006 73,006 73.868 7'3,66:6 73,006 954.406 954,400 !.l54,4oo i54,4oe s:s...•os 96-4.406 954,406 954,<4:06 lfS4,-toa 

# 142,348 142.348 1<42,346 142,344 142,345 1.¢2.348 142,348-

**14~.346** 

# 142,346 237.19 243.14 2At1.62 254.21 2SIUJ3 285.111 .271.76 

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# o.aa: 0.00 10.SS 11,1)9 

# """
7.142% 

# 0.000% O.OOO'i't 7;\42% 

# 0.000% 0,000'1'. 10..13% 9.!10% 

# A.16% 1.293(1 1.3195 1.345!J 

# 66.55% 89.24% 

# 7-4.46% 1),839,92.!}

**10.~9.662** 

# 11.01(}.016 137,572 

# 143,1$3 153,931



# 02.96 (16,00 

# 99.15

**2.~69** 

# 3.0236 

# 3..1070 

# 0 0 0 0.5739 0.5:).54 0.41l!l5



# 1.00 

# 1.00 1.00 

# nllOO% 0.000% 3.111 3.27 

# 1.Ja2a U2<41
54,269 

# Sll.$31 0 0 820,739 

# 854,!148 

# 115.044 11lM:139 1-'3.03 

# 1.52.36 51.14 

# 52.17 148,0:5 151.01



# 0.02 

# M4

**H.~** 

# 11.'17


# 0.000'¥. 0.000% O,OOIY'J. {\.\/00%. 1Ui2%

**~M1~** 

# 1.3728 1.4002 

# 73..67% 

# '711.14% 10,893,875 

# 11..347,938

1S2,308 153,656 

# 102.39' 105.7-i 3.1871 3.2710 

# 0 0 0.4680 0.4M7 

# '1.QO. 1.00 

# 0.0-00% 3.35 

# 1.4562
5fl.ti12 0 1156,113 

# 121:>,011 1&5,81 

# 53.21 154,03



# .... 12.01 

# o.ooor. o.uoor. !),33% 

# 1A21!> 7lUJS%. 

# 11,364.193

150.663 

# 109.2U 3.3498



# 0 0..4056



# 1.00 1).000% 3,3'il' 

# 1,4006

0.000% OJlDO'I, !UO% 

# 1.4S68 71.89% 

# 1o,m,17v

148.821 

# 111,00 l.394S 

# 0 0.37&4



# 1.00 APf'ENDiX!9. &l...ooi\S'\11

0.000:%



# 3.41 

# 1.5224I l : L

# '""' mft

0.000% .O.!X!O% 

# 0.000% 0.0011% 

# "·""""' 0.000% 

# 0,000% 0.000%

**0.~%** 

# 0.000*4

4.64 

# .... <.111 

# 5.08 5.19 5.31 5,A;3 

# 5.55 567

**~1T:l5** 

# 2.2124 

# >323! ·2,3756 

# 2.421)2: 

# l

. .C&'Jl) 

# 2.539& 2.5969 

# 2.6554 53,037 

# 53,031· 53,031 

# 53,037 53,037 

# 53,037 53,037 

# 53.037 Sl,037 

# 0 0 

# 0 0 

# 0 

# 0 0 

# 0 

# 0 802,100 S02,10S 

# !l02,10Ei 802,100 802,100 

# 802.100 

# 8:02.100. 001,108 802,106 112,432 

# 112.431' 112,432. 112,.132 

# 112.432 112.432 112.432 \12.432 

# 112,<32 237,70: 2.C3.1.t 

# 248.62 254.21 

# 259.113 265.78 271.78 

# 271,8.1

**2841~** 

# T1.!i2· 1il,07 

# ac.ss !lZ.<!l 63.91 85.56 87.:30 

# 68.04 

# oo.u 22;A:.39: 

# 22JI.B8 233.45 238.12 242.86

**~7.74** 

# 252.70 

# 257.75 262.5t



# 1A7 

# uso 1.53 1.57 

# ·uo 1.64 

# 1Jlll 

# 1.71 1.75 17.50 

# 17,85 16.20 1&57 18.1ilol 

# 19.32 19.7{) 

# 20.10 

# 20
... 0.000% 0.11001\ 

# 0.000% 0.000% 0.000'11 

# OJlOO% 0.000% OJJOO% !),000%. 

# 0.000% (l.tXIO% 0.000% 

# 0.000% 0.000% 

# 0.000% 0.000% 

# ...... ... % t\.78% 

# ...... U9% 6
. .41)%' 

# f1.40% 

# 6.32'11 6.13% 

# 2.0007 2...1223 2,1641 

# ,2.2Ce(l 

# 2.2622 2.2972 2.3432 

# ?.3901 2.437!} '72.00% 72.00% 

# 72.001\ 72.00% 11.00% 

# 12'.00% 72.00%. 

# nco% 72.00% 

# 10,&4&.554 

# 10.6411.554 10,64&,554 

# 1G,646,564 10.6<16,554 

# 10,6<18.554 10,640.554 \0,646,554 1M<6.554

148.650 

# 1.46,800 H8,85Q 

# 1-i6,8.56 

# 14a,a.50 148,850

**t~tl.850** 

# 1.<\8,850 'U&,aso 

# 16&.00 17().41 1'1'.4.24 178.18 

# 1RZ.17 166.27 190
. 

# .48 194.75 

# 199.13 

# 4.7.89 

# """"' <4.9650 

# 5.0161 5.10:10 UJI7B 5.4272 

# 5.5493 

# S.tlT-42 0 0 

# 0 0 0 

# G 0 0 0 

# a. toes
... 0,1.012 O.Q!1.44 

# o.oaat 0.0822 0.0787 0.0715 

# 0,0067 0.0022.



# tOO 

# 1.00 1.00, 

# 1.00 1.00 

# too \.00 1.00 1.00 50JID4,246 4G,Q14,l09 40,182.231 46,468:,547 

# .C7,713,81G 47,09B:,58S.

. "",443,4B8 <45,8®,050 

# 45,1SS,l.tS7 13.422,500 13.500,950 13,004,788 14.241.00:..

- 14,528.94a 14,&19,524 1$.115.915 15.418.233 15.726.597 (I 

# 0 0 0 0 0 0 

# .o .0 

# 24,007.179 2.5,345,340 25,936,000 28,51i,M2 27;11$.313 2T,12S,430 2.8,3$0,275 26,988.156 2!l.S40,390 3,326,832 3,392,349 · 

# a.•oo.too 3,5Zi,400 3.,!119:,988 

# :t,an,sar 3,74.5.427 3.820,338 J,aaa.7.t2 12,811,850 12.Mfl.71!l 13.185,872 1l,462.M! 13,7M,it2 14,096,095 14,.tt3.2ST 1A.737,55S 15,06&,100 0 0 0 0 0 0 0 0 0 

# 1,176..504 1.202,976 1,230»42 1,257,718 1.2.88.017 1.314,952 1.344-.539 1,374,791 1,40:5,123 1.967.021 Z.006.361 2.046.4B& 2.087,418: 2,129,1titi 2,,71,150

**2.215,1~** 

# 2,2$9,-400 ;!,3:Q+,fJ78

.. -.n

**~~-** 

# •-

**--~** 

# --- 

# 10,28&,7i6 &,651,\19 9,0SS,TOZ 8,500,«7 7,JNl2.4$1 7,499',148 

# 1,041,003 1,433,594,Dt12 1,443.246,112 1,452,301,814 1,460,802.261 1,461.7&·V42 1.-473,2&3,600 1,483,331,874



# 4-

# .&leJBY.

**-·~--** WHITE &lUFf S T ATlON 

# UNITS t AND 2

**~AlOATION** 

# Of 

# 'HEr \'1 

# DRY fG.D TECHWOLOGI.ES


# Table E-5: Annual Revenue Roqulromenta

- Ca•• 5 Cese 5 ·Wet FGD PRB Coal Cak!l.'!!!Y!!t

**CIGiliill'l£i't•a~** 

# o\nnal F"'*r& aftll 

# Prion:

**fne!~**

**T-.~** 

# l·Yf/IWAtrwort. F..-. Pneq

**('$1~)** 

# PRB Coal 

# """""''"""'

**·-~** l.lrM ( WJnl}

**~(ton•**

**)**

**Tota.IWfltMfta,QW~1(1000aga**



# Wn.AIIA~(blt} 

# l.>na.$1\oo 

# """'-"""'

...

**Cot~$**

**Teui'N.tl4f~n>efll.511000-v-!**

**w...,.Ntt~Siron**



# C~uL.t.dV.W. 

# Tax.,._

........... E-Poriod 

# --c:no.vo-

**O&M~F.a«** 

# c..,.ctyf"""

........ ,..,_., (>Mb J

-- ( IA'MIJ A.u.l.. 

# P"vwe' CoM 

# tSIM'M'I} 

# '""Prioo{;lrrml!") 

# '""' """"""- 

# -- Pr¥ent 

# vq 

# F.acr

**E~PonodF~**

**f:ili4~** 

# f lx odOUtl 

# ..... Fuol 

# ---
... 

# - 1..\mo. 

# ,_.,_.,.,.

**<DIWIWR~** 

# :I:"'""'"""""' PI"'-"V.W.{PVM } 

# ~~~

**c.mw.t~,.** 

# PVRII

**~~\'.,.,** 

# .. 2 , 09&.266.52-4

**~(Siy6W)** 

# 1t0.84M32

**1:)(TD!lV~W&**

**4-Da. Vf.WliT**  **ND mllVUVa~fQ..-t.Gt**  

# .......,_ I DOWIM 

# I iOU

**2G1~**

**~** 

# .. ....,., 1.46 

# :1.51 

# ut<4a t1A00



# • 0 4.11.l , l1111 

# <7a.2l<l t , Oll,\20 

# t
. m.m 

# ..

**~,.,.** 

# ;:;!.2,71!8 11G.30 121.9! 

# ..... 42.7Q 

# 121.45 113.80 

# 0.74 0
. 75 

# 9
. 

# .47 

# ...
7
. 142% 14.298% 7
. 1-U% 

# ,.....,. 15..ml 

# ....... um 1
. 1417 

# ,. 

# ..... 73..,... 11 , 0U\Ch0 

# tQ.BU.815

26).510 

# :zeo , no 

# ..... 

# . ... , 2.A<2l 

# ...... 0 0 

# o.am M704

1,00 1.00
,,1,13-4 , 966 119 , 42t1.!08

**a.~~·** 

# 9 .1 &4.21' 0 

# 0 11.lt1,290 

# 1 S.02G_DI 0 

# • 0 

# • :zo .

zn.B75 l0.485 , G48 

# 780 , 236 7681,1-43 

# uU!tfll 

# ntH


# ..... ..., taa..3M.CI72 152,97f1 , 7M 

# 189.30$,072 

# ll2.281.857 

# U2 QtW;1' 

# iUd I

**.., 3G**  **WWH~•** 

# 2915 2()11 

# 1017 

# ,.,,

IU
..... 

# tot ..2M% 

# t•..zatl'!l. 1U86'!1t



# 2-51 2.65 

# 2
. 12 

# u• 1,1657 

# 1.1G1i 1..2187 1.24SZ

Q 

# 0 Q 

# • 418,1&3 

# ....... , 411,6·U 468 , 12$ 

# 1 , 01S&,829 1
..... ,.. 

# 087 • • 7111 

# t , OOO,W 911,687 

# m.ow 011).21)0 

# ...... , 124.73 127.53 t30 , 4Q 

# 1>3.3< 

# ..... ..... 45AI 

# . ..,. 126
. 30 12AM 131..&6 

# ....... 0
. 77 0
. 70 

# .... ... , us IO.OS 

# uus 10
. (5
1o4.288% 1'-2.86% 

# , .. .2&6% 

# 1'.21!Mio 14.2tll!l'4 14.288'4 

# ........ 14.2
.... 13.80% 

# 13.01% 1Z.2.4"' 1t.40'Yt 

# 1.1717 

# 1.1951 1.2100 1
..... 1ll
. 74
.. 7U5% 

# 71.10% 72
. 12% 11..:W7,931 11.364.193 

# lG..OlO.fTU! 111.B63,00\



# l71.SU 

# l1U41 254 , 419 

# :!55.216 

# s.uu 87
. 47 

# IIUI 71.01 

# 2.573) 

# 2.6490 2.7193 

# 2.1083 0 0 0 0 

# 0.6120 0.7575

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# ......

1.00 1.00 1.00 

# I .DO

113
. 023 , 64.0



# 101~::.:: 100,2(2',768 

# aJ.&M.S'Q

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# .. . UH,1)7 9,9HJ.640 D 

# • D 

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**17~7,013** 

# la.M0,<3<1 

# 17.S00.793 19.·U-' , t51)3 

# • 0 0 0 D 

# 0 0 

# • 21,7+t,405 

# 22,211,0o5:2 21.UJt,07e 21,1&4,W



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# . ..... ..... 13Q,707.863 128,T&8.,431 

# 112 .226 ,SII18 102.3&4.973 

# .661.QIW.72G 

# 681.7U.I51 7Q0.86l',007 

# ltl3.3!12
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# 2.90 lJll 3
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# 3.39 

# ,., 1.21<2 1.302P 

# 1.3322 1.3021 

# ·= 142<4;1

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# t.S2:2ot

0 0 D 

# 0 0 

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# 0 416.101



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# 4l6.,Zl0 41&.1!) 40& , &67 

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# .... ,,. t.Ol3.120 I.Ol2.222

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# 139.41

**14~54** 

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**14~03** 

# 152.)4 

# 15.5.11 1&9.32 

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# ...ltl I>B.TT 

# 13:t
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# . . .. 0.111 

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# 11.ll 11
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# 1 2:.01 1Z.215 

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# O
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# 1.4282 

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# , ...... 76..7<1%

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# o .. na.m 1Q,lW.062 11 , 010,0W 1Q,eu:l,II'T6 

# 11
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# 10.630
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# 117.80<1 2>6.805

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# "" · "" 271 , 691 

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# 17.A07.J'W 13.011,4!.2 

# &1 , 125..2'50 7 9. 9ol8
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# 7& , m . 7oa l'7 , 81i.!iTl 1& , 41:U & 1 

# 75.ll8.\fi1 10,111.033 10,)20.»1 10.6ZI,IOl 10-,JJT , »S 

# 10.852.0841 11.\71 , 126 

# 11,»4,540 t1
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# 2!1,7\.0 , &43 Zi-701,150 

# 2&.407,1&6 

# • 0 0 

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# 0 1i,T51.)42 20.817,2!2 .22.094,U7 24,2ll.&9S 

# 24,457.t21 25.,9&e.576 

# Z8,SU.27S 26.32!1.37!

75UIIKI 

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**0'3$.67~** 

# I,QOO,.OS<

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# 1100.21< 

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**1~ u~:liWI**  10eM , 4116 

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. W , Ui 1 0. 767.016 1 1. .U0
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# 13
... 119,.104,19! 

# 83.788
. 136 

# 7B, 1 U , 66fi 711,2-4lUW7 71 , \04.23-i 61 , 7110
. 178

**&l.801~7 m.~.427**  

# 54 , 1V.7,7'M 09l.15<,%24 

# 970.!14070 

# 1.05<.091.215 1,1:t:U3&.612 1.2<13."3.111 1.271.233.709 1.33<,!37,l26 l .l!lt661.753 1 , 4-MI,IS0.536



# 4~

# -·-·-~- 

# ___ **1Q~_** 

# . **----~30** 

# 2931 2032: 2033 

# %OM.. ::lO:lS 2Cl38 2037 20l!J 2b3Q U. 

# It 

# 1$. If }0 

# 21 U 

# lf l. l1 1•


# 0.000% Q,OO()"A 

# 0.000% 

# 0.00<1% 0.000% 

# "·""""' 0.000% 0 ...... 

# o.O<J<W. 0.!100% 

# MOO% 

# '·""""' 3.64 

# 3..72 3.711 3.88 

# 3.114 4.01 t1)6 .4.16 

# 4.21 4.21 4.3-:Z 

# 1,:iB'IT 

# 1,627.5 t,664Z 

# 1.1016 1.739$ 

# \.rna 1.8191 

# 1.11600 1.9013 1,1).446 

# t9ea4 

# 0 0 0 

# 0 0 0 

# 0 0 0 

# 0 0 .4.3.1,!115-t M9A7S. 483,319: 

# 478,22:0 4l18.,1S3 

# 496.667

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# 4eB,I25 

# 418,181 43l,B.S4 

# 467.$4

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# 000,778 ,,033.,120 1.022.221 

# ,,064,!123' 1,0&6,354 997,479 1,00Q,.643

. 

# an3,1W1 

# 923.3i6- Wl9,01S 

# ........ 8.78,7ZO 9-42,733 

# 932.,788 

# 971,667 

# 973,059 910,209 !}13..097 81$,1>39 

# 64;1:,54.4 

# rut,an 170,31 

# 17-415 178,00 182.07 

# 1a6.1T \<l<l.31i '[94.&4 1f.l9.!l2

**:1:03.~** 

# 208.00 

# 212.76 57,£0 SU.75 

# o.a.a2 81.12 62.3<

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# ... ,. t7.48 

# mun 70.41 1£6.72 

# 170,00 173.48 178.93 1t'I0.47 

# 164.00 161.78 

# 191.51 1.$5.34

**1~.2$** 

# ZJ3.23

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# 1.12 1.15 

# 1.17 1.20 1.23 1.28 

# 1.28.

**~.31 ~3.00**  

# 13,26

**'\3.~2** 

# 13.79 

# 'l4.11T t4,3S 

# 1•UW '\4.93 15.23 

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# 1.6084 1.64011 1,6734 

# 1,7069. 1,7410 1..7758 1.811<1 U478 

# UM!$ 

# 00.$.$'1\ 

# """"" 74..46% 73.61'%

**16.1~%** 

# 78.8:5% 

# 71.8S%. 72.1Z'I. 

# 6<1,.4-2% 66,55% 

# 12.-. if,83$,!129 1Q,2':!W,062 

# 11,(!10,016

**10,89~875** 

# 11,MT,Il3& 

# 11,36.(,193 10,63.0.179

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.... 9.029 10,646,554 

# 23S.50S l45,1l58 

# .263.510 

# 2.50,730 

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# 121-81 

# 13'0-.48 

# 133,41 136.41 139.46 1.UJU

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