lf cue cost 3 seattle

8/10/2019 Lf Cue Cost 3 Seattle

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CUECost - Air Pollution Control Systems Economics Spreadsheet

Economic I nputs

Cost Basis -Year Dollars Year 1998 2009 2009 2009 2009 2009

Sevice Life (levelization period) Years 30 20 20 20 20 20

Inflation Rate % 3.00% 3.00% 3.00% 3.00% 3.00% 3.00%

After Tax Discount Rate (current $'s) % 9.20% 9.20% 9.20% 9.20% 9.20% 9.20%

AFDC Rate (current $'s) % 10.80% 10.80% 10.80% 10.80% 10.80% 10.80%

First-year Carrying Charge (current $'s) % 22.30% 22.30% 22.30% 22.30% 22.30% 22.30%

Levelized Carrying Charge (current $'s) % 16.90% 16.90% 16.90% 16.90% 16.90% 16.90%

First-year Carrying Charge (constant $'s) % 15.70% 15.70% 15.70% 15.70% 15.70% 15.70%

Levelized Carrying Charge (constant $'s) % 11.70% 11.70% 11.70% 11.70% 11.70% 11.70%

Sales Tax % 6% 6.5% 6.5% 6.5% 6.5% 6.5%

Escalation Rates:

Consumables (O&M) % 3% 3% 3% 3% 3% 3%

Capital Costs:

Is Chem. Eng. Cost Index available? Yes / No Yes Yes Yes Yes Yes Yes

If "Yes" input cost basis CE Plant Index. Integer 388 561 561 561 561 561

If "No" input escalation rate. % 3% 3% 3% 3% 3% 3%

Construction Labor Rate $/hr $35 $35 $35 $35 $35 $35

Prime Contractor's Markup % 3% 3% 3% 3% 3% 3%

Operating Labor Rate $/hr $30 $35 $35 $35 $35 $35

Power Cost Mills/kWh 25 53.3 53.3 53.5 53.3 53.3

Steam Cost $/1000 lbs 3.5 3.5 3.5 3.5 3.5 3.5

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APC Technology Choices

Description Units Input 1 Input 2 Input 3 Input 4 Input 5

FGD Process Integer 1 1 2 2 2

(1 = LSFO, 2 = LSD)

Particulate Control Integer 2 2 2 2 2

(1 = Fabric Filter, 2 = ESP)

NOx Control Integer 1 2 1 2 4

(1 = SCR, 2 = SNCR, 3 = LNBs, 4 = NGR)

INPUTS

Description Units Input 1 Input 2 Input 3 Input 4 Input 5

General Plant Technical I nputs

Location - State Abbrev. WA WA WA WA Wa

MW Equivalent of Flue Gas to Control System MW 22.5 22.5 22.5 22.5 22.5

Net Plant Heat Rate Btu/kWhr 10,500 10,500 10,500 10,500 10,500

Plant Capacity Factor % 95% 95% 95% 95% 95%

Total Air Downstream of Economizer % 120% 120% 120% 120% 120%

Air Heater Leakage % 12% 12% 12% 12% 12%Air Heater Outlet Gas Temperature F 300 300 300 300 300

Inlet Air Temperature F 55 55 55 55 55

Ambient Absolute Pressure In. of Hg 29.4 29.4 29.4 29.4 29.4

Pressure After Air Heater In. of H2O -12 -12 -12 -12 -12

Moisture in Air lb/lb dry air 0.013 0.013 0.013 0.013 0.013

Ash Split:

Fly Ash % 80% 80% 80% 80% 80%

Bottom Ash % 20% 20% 20% 20% 20%

Seismic Zone Integer 3 3 3 3 3

Retrofit Factor Integer 1.6 1.6 1.6 1.6 1.6

(1.0 = new, 1.3 = medium, 1.6 = difficult)

Select Coal Integer 6 6 6 6 8

Is Selected Coal a Powder River Basin Coal? Yes / No Yes yes Yes Yes yes

Economic I nputs

Cost Basis -Year Dollars Year 2009 2009 2009 2009 2009

Sevice Life (levelization period) Years 20 20 20 20 20

Inflation Rate % 3% 3% 3% 3% 3%

After Tax Discount Rate (current $'s) % 9% 9% 9% 9% 9%

AFDC Rate (current $'s) % 11% 11% 11% 11% 11%

First-year Carrying Charge (current $'s) % 22% 22% 22% 22% 22%

Levelized Carrying Charge (current $'s) % 17% 17% 17% 17% 17%

First-year Carrying Charge (constant $'s) % 16% 16% 16% 16% 16%

Levelized Carrying Charge (constant $'s) % 12% 12% 12% 12% 12%

Sales Tax % 7% 7% 7% 7% 7%

Escalation Rates:

Consumables (O&M) % 3% 3% 3% 3% 3%

Capital Costs:

Is Chem. Eng. Cost Index available? Yes / No Yes Yes Yes Yes Yes If "Yes" input cost basis CE Plant Index. Integer 561 561 561 561 561

If "No" input escalation rate. % 3% 3% 3% 3% 3%

Construction Labor Rate $/hr $35 $35 $35 $35 $35

Prime Contractor's Markup % 3% 3% 3% 3% 3%

Operating Labor Rate $/hr $35 $35 $35 $35 $35

Power Cost Mills/kWh 53.3 53.3 53.5 53.3 53.3

Steam Cost $/1000 lbs 3.5 3.5 3.5 3.5 3.5

L imestone Forced Oxidation (LSFO) I nputs

SO2 Removal Required % 95% 95% 95% 95% 95%

L/G Ratio gal / 1000 acf 125 125 125 125 125

Design Scrubber with Dibasic Acid Addition? Integer 2 1 2 2 2

(1 = yes, 2 = no)

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Adiabatic Saturation Temperature F 127 127 127 127 127

Reagent Feed Ratio Factor 1.05 1.05 1.05 1.05 1.05

(Mole CaCO3 / Mole SO2 removed)

Scrubber Slurry Solids Concentration Wt. % 15% 15% 15% 15% 15%

Stacking, Landfill, Wallboard Integer 1 1 1 1 1

(1 = stacking, 2 = lanfill, 3 = wallboard)

Number of Absorbers Integer 1 1 1 1 1

(Max. Capacity = 700 MW per absorber)

Absorber Material Integer 1 1 1 1 1

(1 = alloy, 2 = RLCS)Absorber Pressure Drop in. H2O 6 6 6 6 6

Reheat Required ? Integer 2 2 2 2 2

(1 = yes, 2 = no)

Amount of Reheat F 0 0 0 0 0

Reagent Bulk Storage Days 60 60 60 60 60

Reagent Cost (delivered) $/ton $15 $15 $15 $15 $15

Landfill Disposal Cost $/ton $30 $30 $30 $30 $30

Stacking Disposal Cost $/ton $6 $6 $6 $6 $6

Credit for Gypsum Byproduct $/ton $2 $2 $2 $2 $2

Maintenance Factors by Area (% of Installed Cost)

Reagent Feed % 5% 5% 5% 5% 5%

SO2 Removal % 5% 5% 5% 5% 5%

Flue Gas Handling % 5% 5% 5% 5% 5%

Waste / Byproduct % 5% 5% 5% 5% 5%

Support Equipment % 5% 5% 5% 5% 5%Contingency by Area (% of Installed Cost)

Reagent Feed % 20% 20% 20% 20% 20%

SO2 Removal % 20% 20% 20% 20% 20%


Waste / Byproduct % 20% 20% 20% 20% 20%

Support Equipment % 20% 20% 20% 20% 20%

General Facilities by Area (% of Installed Cost)

Reagent Feed % 10% 10% 10% 10% 10%

SO2 Removal % 10% 10% 10% 10% 10%


Waste / Byproduct % 10% 10% 10% 10% 10%


Engineering Fees by Area (% of Installed Cost)

Reagent Feed % 10% 10% 10% 10% 10%

SO2 Removal % 10% 10% 10% 10% 10% Flue Gas Handling % 10% 10% 10% 10% 10%

Waste / Byproduct % 10% 10% 10% 10% 10%


Lime Spray Dryer (L SD) I nputs

SO2 Removal Required % 30% 30% 30% 30% 25%

Adiabatic Saturation Temperature F 127 127 127 127 127

Flue Gas Approach to Saturation F 20 20 20 20 20

Spray Dryer Outlet Temperature F 147 147 147 147 147

Reagent Feed Ratio Factor 0.31 0.31 0.31 0.31 0.26

(Mole CaO / Mole Inlet SO2)

Recycle Rate Factor 19.5 19.5 19.5 19.5 30

(lb recycle / lb lime feed)

Recycle Slurry Solids Concentration Wt. % 50% 50% 50% 50% 50%Number of Absorbers Integer 1 1 1 1 1

(Max. Capacity = 300 MW per spray dryer)

Absorber Material Integer 1 1 1 1 1

(1 = alloy, 2 = RLCS)

Spray Dryer Pressure Drop in. H2O 5 5 5 5 1

Reagent Bulk Storage Days 60 60 60 60 60

Reagent Cost (delivered) $/ton $0 $0 $0 $0 $0

Dry Waste Disposal Cost $/ton $0 $0 $0 $0 $0

Maintenance Factors by Area (% of Installed Cost)

Reagent Feed % 5% 5% 5% 5% 5%

SO2 Removal % 5% 5% 5% 5% 5%


Waste / Byproduct % 5% 5% 5% 5% 0%


Contingency by Area (% of Installed Cost)



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Reagent Feed % 20% 20% 20% 20% 20%

SO2 Removal % 20% 20% 20% 20% 20%


Waste / Byproduct % 20% 20% 20% 20% 0%


General Facilities by Area (% of Installed Cost)

Reagent Feed % 10% 10% 10% 10% 10%

SO2 Removal % 10% 10% 10% 10% 0%


Waste / Byproduct % 10% 10% 10% 10% 10% Support Equipment % 10% 10% 10% 10% 10%

Engineering Fees by Area (% of Installed Cost)

Reagent Feed % 10% 10% 10% 10% 10%

SO2 Removal % 10% 10% 10% 10% 10%


Waste / Byproduct % 10% 10% 10% 10% 10%


Particulate Control I nputs

Outlet Particulate Emission Limit lbs/MMBtu 0.001 0.001 0.001 0.001 0.001

Fabric Filter:

Pressure Drop in. H2O 6 6 6 6 6

Type (1 = Reverse Gas, 2 = Pulse Jet) Integer 2 2 2 2 2

Gas-to-Cloth Ratio ACFM/ft2 3.5 3.5 3.5 3.5 3.5 Bag Material (RGFF fiberglass only) Integer 2 2 2 2 2

(1 = Fiberglass, 2 = Nomex, 3 = Ryton)

Bag Diameter inches 6 6 6 6 6

Bag Length feet 20 20 20 20 20

Bag Reach 3 3 3 3 3

Compartments out of Service % 10% 10% 10% 10% 10%

Bag Life Years 5 5 5 5 5

Maintenance (% of installed cost) % 5% 5% 5% 5% 5%

Contingency (% of installed cost) % 20% 20% 20% 20% 20%

General Facilities (% of installed cost) % 10% 10% 10% 10% 10%

Engineering Fees (% of installed cost) % 10% 10% 10% 10% 10%

ESP:

Strength of the electric field in the ESP =E kV/cm 10.0 10.0 10.0 10.0 10.0

Plate Spacing in. 12 12 12 12 12

Plate Height ft. 36 36 36 36 36 Pressure Drop in. H2O 3 3 3 3 3

Maintenance (% of installed cost) % 5% 5% 5% 5% 5%




NOx Control Inputs

Selective Catalytic Reduction (SCR) Inputs

NH3/NOX Stoichiometric Ratio NH3/NOX 0.9 0.9 0.9 0.9 0.9

NOX Reduction Efficiency Fraction 0.90 0.90 0.90 0.90 0.90

Inlet NOx lbs/MMBtu 6.93 6.93 6.93 6.93 6.93

Space Velocity (Calculated if zero) 1/hr 0 0 0 0 0

Overall Catalyst Life years 3 3 3 3 3Ammonia Cost $/ton 280 280 280 280 282

Catalyst Cost $/ft3 356.34 356.34 356.34 356.34 356.34

Solid Waste Disposal Cost $/ton 11.48 11.48 11.48 11.48 11.48

Maintenance (% of installed cost) % 1.5% 1.5% 1.5% 1.5% 1.5%




Number of Reactors integer 2 2 2 2 2

Number of Air Preheaters integer 1 1 1 1 1

Selective NonCatal ytic Reduction (SNCR) I nputs

Reagent 1:Urea 2:Ammonia 2 2 2 2 2

Number of Injector Levels integer 3 3 3 3 3



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Number of Injectors integer 18 18 18 18 18

Number of Lance Levels integer 0 0 0 0 0

Number of Lances integer 0 0 0 0 0

Steam or Air Injection for Ammonia integer 2 2 2 2 2

NOX Reduction Efficiency Fraction 0.40 0.40 0.40 0.40 0.40

Inlet NOx lbs/MMBtu 6.93 6.93 6.93 6.93 6.93

NH3/NOX Stoichiometric Ratio NH3/NOX 1.2 1.2 1.2 1.2 1.2

Urea/NOX Stoichiometric Ratio Urea/NOX 1.2 1.2 1.2 1.2 1.2

Urea Cost $/ton 225 224.95 224.95 224.95 224.95

Ammonia Cost $/ton 280 280 280 280 280Water Cost $/1,000 gal 0.407 0.407 0.407 0.407 0.407





Low NOX Burner Technology I nputs

NOX Reduction Efficiency fraction 0.35 0.35 0.35 0.35 0.35

Boiler Type T:T-fired, W:Wall T T T T T

Retrofit Difficulty

L:Low, A:Average,

H:High A A A A A

Maintenance Labor (% of installed cost) % 0.8% 0.8% 0.8% 0.8% 0.8%

Maintenance Materials (% of installed cost) % 1.2% 1.2% 1.2% 1.2% 1.2%

Natural Gas Reburn ing I nputs

NOX Reduction Efficiency fraction 0.61 0.61 0.61 0.61 0.61

Gas Reburn Fraction fraction 0.15 0.15 0.15 0.15 0.15

Waste Disposal Cost $/ton 11.48 11.48 11.48 11.48 11.48

Natural Gas Cost $/MMBtu 1.04 1.04 1.04 1.04 1.04







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SCR (high-dust) - Preliminary Case1 Case2 Case3 Case4 Case5

Ammonia Injection Rate lb/hr 545 545 545 545

Space Velocity 1/hr 2,673 2,673 2,673 2,673 2,

Gross Catalyst Volume ft3

1,163 1,163 1,163 1,163 1,

SCR Capital Costs Case1 Case2 Case3 Case4 Case5Cost Basis (Year) 2009 2009 2009 2009 2009

Reactor Housing and Installation $ 1,316,707 1,316,707 1,316,707 1,316,707 1,316,485

Ammonia Handling and Injection $ 1,663,119 1,663,119 1,663,119 1,663,119 1,663,119

Flue Gas Handling:Ductwork and Fans $ 851,019 851,019 851,019 851,019 850,815

Air Preheater Modifications $ 145,068 145,068 145,068 145,068 145,028

Misc. Other Direct Capital Costs $ 226,217 226,217 226,217 226,217 226,217 Equipment Capital Cost Subtotal $ $4,202,130 $4,202,130 $4,202,130 $4,202,130 $4,201,664

Instruments & Controls $ $84,043 $84,043 $84,043 $84,043 $84,033

Taxes $ $273,138 $273,138 $273,138 $273,138 $273,108

Freight $ $210,107 $210,107 $210,107 $210,107 $210,083

Total Di rect Cost $4,769,418 $4,769,418 $4,769,418 $4,769,418 $4,768,888

Total Direct Cost with Retrofit Factor $ $7,631,069 $7,631,069 $7,631,069 $7,631,069 $7,630,221

General Facilities $ $381,553 $381,553 $381,553 $381,553 $381,511

Engineering Fees $ $763,107 $763,107 $763,107 $763,107 $763,022

Contingency $ $1,526,214 $1,526,214 $1,526,214 $1,526,214 $1,526,044

Total Plant Cost (TPC) $ $10,301,943 $10,301,943 $10,301,943 $10,301,943 $10,300,799

Total Plant Cost (TPC) w/ Prime Contractor's Markup $ $10,611,001 $10,611,001 $10,611,001 $10,611,001 $10,609,823

Total Cash Expended (TCE) $ $10,611,001 $10,611,001 $10,611,001 $10,611,001 $10,609,823

All ow. for Funds Dur ing Constr. (AFDC) $ $0 $0 $0 $0 $0

Total Plant I nvestment (TPI) $ $10,611,001 $10,611,001 $10,611,001 $10,611,001 $10,609,823

Preproduction Costs $ $285,109 $285,109 $285,109 $285,109 $285,483

Inventory Capital

Initial Ammonia(60 days) $ $104,472 $104,472 $104,472 $104,472 $105,218

Initial Catalyst $ $414,396 $414,396 $414,396 $414,396 $414,252

Total Capital Requir ement (TCR) $ $11,414,978 $11,414,978 $11,414,978 $11,414,978 $11,414,776

$/kW $507 $507 $507 $507 $507

SCR O&M Costs Case1 Case2 Case3 Case4 Case5

Cost Basis (Year) 2009 2009 2009 2009 2009

Ammonia $/yr 635,535 635,535 635,535 635,535 640,

Catalyst Replacement $/yr 138,132 138,132 138,132 138,132 138,

Catalyst Disposal $/yr 107 107 107 107

Electricity $/yr (2,342) (2,342) (2,351) (2,342) (2,

High-dust SCR Steam $/yr 60,327 60,327 60,327 60,327 60,

Operating Labor $/yr 51,158 51,158 51,158 51,158 51,Maintenance $/yr 154,529 154,529 154,529 154,529 154,

Total O&M Costs $/yr 1,037,447 1,037,447 1,037,438 1,037,447 1,041,

SNCR - Preliminary Case1 Case2 Case3 Case4 Case5

Number of Wall Injectors integer 18 18 18 18 18

Number of Lances integer 0 0 0 0 0

Urea Injection Rate lb/hr 1277 1277 1277 1277 1277

Ammonia Injection Rate lb/hr 727 727 727 727 727

SNCR Capital Costs Case1 Case2 Case3 Case4 Case5Cost Basis (Year) 2009 2009 2009 2009 2009

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Urea Based SNCR Costs

Urea Storage & Handling $ $0 $0 $0 $0 $0

Urea Injection $ $0 $0 $0 $0 $0

Controls/Miscellaneous $ $0 $0 $0 $0 $0

Air Heater Modifications $ $0 $0 $0 $0 $0

Ammonia Based SNCR Costs

Ammonia Storage, Handling, Injection, Controls $ $424,704 $424,704 $424,704 $424,704 $424,704

Air Heater Modifications $ $92,417 $92,417 $92,417 $92,417 $92,378

Total Di rect Cost $ $517,121 $517,121 $517,121 $517,121 $517,082

Total Direct Cost with Retrofit Factor $ $827,394 $827,394 $827,394 $827,394 $827,331



Contingency $ $165,479 $165,479 $165,479 $165,479 $165,466

Total Pl ant Cost (TPC) $ $1,116,982 $1,116,982 $1,116,982 $1,116,982 $1,116,897

Total Plant Cost (TPC) w/ Prime Contractor' s Markup $ $1,150,492 $1,150,492 $1,150,492 $1,150,492 $1,150,404


All ow. for Funds Dur ing Constr. (AFDC) $ $0 $0 $0 $0 $0



Inventory Capital $ $139,295 $139,295 $139,295 $139,295 $139,295

Total Capital Requirement (TCR) $ $1,394,913 $1,394,913 $1,394,913 $1,394,913 $1,394,822

$/kW $62.0 $62.0 $62.0 $62.0 $62.0

SNCR O&M Costs Case1 Case2 Case3 Case4 Case5

Cost Basis (Year) 2009 2009 2009 2009 2009

Operating and Supervisory Labor $/yr 76,650 76,650 76,650 76,650 76

Maintenance Labor and Materials $/yr 16,755 16,755 16,755 16,755 16

Reagent $/yr 847,380 847,380 847,380 847,380 847

Electricity $/yr 42,216 42,216 42,374 42,216 42

Water $/yr - - - -

Steam (for steam atomization) $/yr - - - -

Total O&M Costs $/yr 983,001 983,001 983,160 983,001 983

Low NOX Burner Technology Capital Costs Case1 Case2 Case3 Case4 Case5

Cost Basis (Year) 2009 2009 2009 2009 2009

Total Capital Requirement with Retrofit (TCR) $ $1,852,731 $1,852,731 $1,852,731 $1,852,731 $1,852,731

$/kW $82.3 $82.3 $82.3 $82.3 $82.3

Low NOX Burner Technology O&M Costs Case1 Case2 Case3 Case4 Case5

Cost Basis (Year) 2009 2009 2009 2009 2009

Maintenance Labor $/yr 14,822 14,822 14,822 14,822 14

Maintenance Materials $/yr 22,233 22,233 22,233 22,233 22

Control, Administration, Overhead $/yr 4,447 4,447 4,447 4,447 4

Total O&M Costs $/yr 41,501 41,501 41,501 41,501 41



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Natural Gas Reburn ing - Preliminary Case1 Case2 Case3 Case4 Case5

Fraction of heat input as reburn fuel fraction 0.15 0.15 0.15 0.15 0.15

Bottom Ash Rate tons/yr 91 91 91 91 94

Natur al Gas Reburning Capital Costs Case1 Case2 Case3 Case4 Case5

Cost Basis (Year) 2009 2009 2009 2009 2009

Gas Pipeline from Fenceline to Boiler $ $501,678 $501,678 $501,678 $501,678 $501,678Fuel Injectors, Overfire Air Ports and Associated Piping, Valves, Windbox and

Control Dampers $ $1,274,466 $1,274,466 $1,274,466 $1,274,466 $1,274,466

Total Di rect Cost $ $1,776,145 $1,776,145 $1,776,145 $1,776,145 $1,776,145




Contingency $ $568,366 $568,366 $568,366 $568,366 $568,366


Total Plant Cost (TPC) w/ Prime Contractor's Markup $ $3,863,754 $3,863,754 $3,863,754 $3,863,754 $3,863,754


All ow. for Funds Duri ng Constr. (AFDC) $ $0 $0 $0 $0 $0



Inventory Capital $ $0 $0 $0 $0 $0


$/kW $175.3 $175.3 $175.3 $175.3 $175.3

Natural Gas Reburning O&M Costs Case1 Case2 Case3 Case4 Case5

Cost Basis (Year) 2009 2009 2009 2009 2009

Electrical Consumption Savings $/yr (19,416) (19,416) (19,489) (19,416) (19,4

Maintenance $/yr 56,236 56,236 56,236 56,236 56,2

Waste Disposal Savings $/yr (12,981) (12,981) (12,981) (12,981) (13,3

Natural Gas Consumption $/yr (134,479) (134,479) (134,479) (134,479) (134,4

Total O&M Costs (110,641) (110,641) (110,714) (110,641) (110,9



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LSFO Materi al Balance - Preliminary Case1 Case 2 Case 3 Case 4 Case 5

Fl ue Gas, Downstream of I D F ans

Temperature F 295 295 295 295 295

Pressure in. H2O 10 10 10 10 10

Flow Rate SCFM 58,015 58,015 58,015 58,015 57,995

Flow Rate ACFM 83,634 83,634 83,634 83,634 83,605

CO2 lb/hr 50,489 50,489 50,489 50,489 50,535 N2 lb/hr 184,042 184,042 184,042 184,042 183,960

SO2 lb/hr 301 301 301 301 188

O2 lb/hr 14,693 14,693 14,693 14,693 14,687

HCl lb/hr 28 28 28 28 28

Other Gases lb/hr 66 66 66 66 66

H2O lb/hr 17,793 17,793 17,793 17,793 17,805

Fly Ash lb/hr 0 0 0 0 0

Total (gas only) lb/hr 267,412 267,412 267,412 267,412 267,269

Flue Gas, to Absorber

Temperature F 295 295 295 295 295

Pressure in. H2O 10 10 10 10 10

Flow Rate SCFM 58,015 58,015 58,015 58,015 57,995

Flow Rate ACFM 83,634 83,634 83,634 83,634 83,605

CO2 lb/hr 50,489 50,489 50,489 50,489 50,535 N2 lb/hr 184,042 184,042 184,042 184,042 183,960

SO2 lb/hr 301 301 301 301 188

O2 lb/hr 14,693 14,693 14,693 14,693 14,687

HCl lb/hr 28 28 28 28 28


H2O lb/hr 17,793 17,793 17,793 17,793 17,805



Flue Gas, from Absorbers (total)

Temperature F 127 127 127 127 127

Pressure in. H2O 4 4 4 4 4

Flow Rate SCFM 60,374 60,374 60,374 60,374 60,249

Flow Rate ACFM 68,672 68,672 68,672 68,672 68,531

CO2 lb/hr 50,702 50,702 50,702 50,702 50,675 N2 lb/hr 184,988 184,988 184,988 184,988 184,552

SO2 lb/hr 15 15 15 15 9

O2 lb/hr 14,907 14,907 14,907 14,907 14,821

HCl lb/hr 0 0 0 0 0


H2O lb/hr 23,773 23,773 23,773 23,773 23,762



Heat Capacities

O2 Btu/lbmolF 7.203 7.203 7.203 7.203 7.203

CO2 Btu/lbmolF 9.263 9.263 9.263 9.263 9.263

N2 Btu/lbmolF 6.990 6.990 6.990 6.990 6.990

H2O Btu/lbmolF 8.048 8.048 8.048 8.048 8.048

NO Btu/lbmolF 7.151 7.151 7.151 7.151 7.151

SO2 Btu/lbmolF 9.771 9.771 9.771 9.771 9.771 HCl Btu/lbmolF 6.951 6.951 6.951 6.951 6.951

O2 Btu/lbF 0.225 0.225 0.225 0.225 0.225

CO2 Btu/lbF 0.210 0.210 0.210 0.210 0.210

N2 Btu/lbF 0.249 0.249 0.249 0.249 0.249

H2O Btu/lbF 0.447 0.447 0.447 0.447 0.447

NO Btu/lbF 0.238 0.238 0.238 0.238 0.238

SO2 Btu/lbF 0.153 0.153 0.153 0.153 0.153

HCl Btu/lbF 0.191 0.191 0.191 0.191 0.191

Reheated Gas Temperature: C 52.8 52.8 52.8 52.8 52.8

K 325.8 325.8 325.8 325.8 325.8

FGD Outlet Temperature: C 52.8 52.8 52.8 52.8 52.8

K 325.8 325.8 325.8 325.8 325.8

Total Btu/hr Btu/hr 0 0 0 0 0

Hot Reheat Air

Temperature F 440 440 440 440 440


Flow Rate SCFM 0 0 0 0 0

Flow Rate ACFM 0 0 0 0 0

N2 lb/hr 0 0 0 0 0

O2 lb/hr 0 0 0 0 0

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H2O lb/hr 0 0 0 0 0

Total lb/hr 0 0 0 0 0

Heat Capacities of Hot Reheat Ai r

O2 Btu/lbmolF 7.322 7.322 7.322 7.322 7.322

N2 Btu/lbmolF 7.104 7.104 7.104 7.104 7.104

H2O Btu/lbmolF 8.316 8.316 8.316 8.316 8.316

O2 Btu/lbF 0.229 0.229 0.229 0.229 0.229

N2 Btu/lbF 0.254 0.254 0.254 0.254 0.254

H2O Btu/lbF 0.462 0.462 0.462 0.462 0.462

Heated Temperature: C 226.7 226.7 226.7 226.7 226.7

K 499.7 499.7 499.7 499.7 499.7

FGD Outlet Temperature: C 52.8 52.8 52.8 52.8 52.8

K 325.8 325.8 325.8 325.8 325.8

Heat Capacities of I nlet Reheat Ai r

O2 Btu/lbmolF 7.295 7.295 7.295 7.295 7.295

N2 Btu/lbmolF 7.077 7.077 7.077 7.077 7.077

H2O Btu/lbmolF 8.254 8.254 8.254 8.254 8.254

O2 Btu/lbF 0.228 0.228 0.228 0.228 0.228

N2 Btu/lbF 0.253 0.253 0.253 0.253 0.253

H2O Btu/lbF 0.458 0.458 0.458 0.458 0.458

Heated Temperature: C 226.7 226.7 226.7 226.7 226.7

K 499.7 499.7 499.7 499.7 499.7

Inlet Air Temperature: C 12.8 12.8 12.8 12.8 12.8

K 285.8 285.8 285.8 285.8 285.8

Requir ed Heat Btu/hr 0 0 0 0 0

Oxidation Air (total)

Temperature F 60 60 60 60 60


Flow Rate SCFM 276 276 276 276 173

Flow Rate ACFM 281 281 281 281 176

N2 lb/hr 946 946 946 946 592

O2 lb/hr 285 285 285 285 179

H2O lb/hr 16 16 16 16 10

Total (gas only) lb/hr 1,248 1,248 1,248 1,248 781

Limestone to Ball M il l


Wt.% Solids wt. % 100% 100% 100% 100% 100%

Inerts lb/hr 25 25 25 25 16

CaCO3 lb/hr 507 507 507 507 331

Total lb/hr 532 532 532 532 348

L imestone Slurr y to L imestone Slurr y Tank


Flow Rate GPM 1.9 1.9 1.9 1.9 1.2

Wt.% Solids wt. % 40% 40% 40% 40% 40%

Inerts lb/hr 25 25 25 25 16

CaCO3 lb/hr 507 507 507 507 331

H2O lb/hr 797 797 797 797 521

Total lb/hr 1,329 1,329 1,329 1,329 869

Limestone Slur ry to Reaction M ix Tank (total)


Flow Rate GPM 4.4 4.4 4.4 4.4 2.9

Wt.% Solids wt. % 20% 20% 20% 20% 20%

Inerts lb/hr 25 25 25 25 16

CaCO3 lb/hr 507 507 507 507 331

H2O lb/hr 2,127 2,127 2,127 2,127 1,390

Total lb/hr 2,658 2,658 2,658 2,658 1,738

Slurr y to Absorber

Temperature F 126 126 126 126 126

Flow Rate GPM 8,479 4,748 8,479 8,479 8,462

Wt.% Solids wt. % 15% 15% 15% 15% 15%

CaSO3*1/2H2O lb/hr 0 0 0 0 0

CaSO4*2H2O lb/hr 655,593 367,132 655,593 655,593 634,723

Inerts lb/hr 21,333 11,947 21,333 21,333 21,582

CaCl2 lb/hr 35,923 20,117 35,923 35,923 55,648

CaCO3 lb/hr 19,056 10,671 19,056 19,056 18,449 H2O lb/hr 4,147,468 2,322,582 4,147,468 4,147,468 4,138,947

Total lb/hr 4,879,374 2,732,449 4,879,374 4,879,374 4,869,350

Slur ry fr om Rxn Tank to Thickener

Temperature F 126 126 126 126 126



11/25


Flow Rate GPM 9.9 9.9 9.9 9.9 6.4

Wt.% Solids wt. % 15% 15% 15% 15% 15%

CaSO3*1/2H2O lb/hr 0 0 0 0 0

CaSO4*2H2O lb/hr 768 768 768 768 480

Inerts lb/hr 25 25 25 25 16

CaCl2 lb/hr 42 42 42 42 42

CaCO3 lb/hr 22 22 22 22 14

H2O lb/hr 4,858 4,858 4,858 4,858 3,132

Total lb/hr 5,715 5,715 5,715 5,715 3,685

LSFO Equipment Capital Costs Case1 Case 2 Case 3 Case 4 Case 5Cost Basis (Year) 2009 2009 2009 2009 2009

Sizing Criteria

Reagent Feed System $ kpph Reag. $10,344,623 $10,344,623 $10,344,623 $10,344,623 $10,326,592

Ball Mill & Hydroclone System $ TPH Reag. $2,690,576 $2,690,576 $2,690,576 $2,690,576 $2,687,591

DBA Acid Tank (pump, heater, agitator) $ gpm DBA $0 $108,960 $0 $0 $0

SO2 Removal System $ kpph SO2 $2,769,943 $2,769,943 $2,769,943 $2,769,943 $2,764,290

Absorber Tower $ kACFM $4,034,765 $4,034,765 $4,034,765 $4,034,765 $4,033,979

Spray Pumps $ slurry gpm $287,420 $203,511 $287,420 $287,420 $287,068

Flue Gas Handling System $ * $2,132,534 $2,132,534 $2,132,534 $2,132,534 $2,132,196

ID Fans $ ACFM $397,788 $397,788 $397,788 $397,788 $397,694

Waste / Byproduct Handling System $ kpph SO2 $117,459 $117,459 $117,459 $117,459 $117,168

Thickener System $ TPH solids $171,232 $171,232 $171,232 $171,232 $169,247

Support Equipment $ MW $1,766,858 $1,766,858 $1,766,858 $1,766,858 $1,766,858

Chimney $ ACFM $2,624,233 $2,624,233 $2,624,233 $2,624,233 $2,622,125

TOTAL $ $27,337,430 $27,362,481 $27,337,430 $27,337,430 $27,304,808* Based on flue gas flow and reheat temperature.

Capital Costs with Retrof it F actors

Reagent Feed System $ $16,551,396 $16,551,396 $16,551,396 $16,551,396 $16,522,547

Ball Mill & Hydroclone System $ $4,304,922 $4,304,922 $4,304,922 $4,304,922 $4,300,146

DBA Acid Tank (pump, heater, agitator) $ $0 $174,336 $0 $0 $0

SO2 Removal System $ $4,431,909 $4,431,909 $4,431,909 $4,431,909 $4,422,865

Absorber Tower $ $6,455,625 $6,455,625 $6,455,625 $6,455,625 $6,454,367 Spray Pumps $ $459,872 $325,618 $459,872 $459,872 $459,309

Flue Gas Handling System $ $3,412,054 $3,412,054 $3,412,054 $3,412,054 $3,411,514

ID Fans $ $636,460 $636,460 $636,460 $636,460 $636,310

Waste / Byproduct Handling System $ $187,935 $187,935 $187,935 $187,935 $187,469

Thickener System $ $273,971 $273,971 $273,971 $273,971 $270,794

Support Equipment $ $2,826,972 $2,826,972 $2,826,972 $2,826,972 $2,826,972

Chimney $ $4,198,773 $4,198,773 $4,198,773 $4,198,773 $4,195,400

TOTAL $ $43,739,888 $43,779,970 $43,739,888 $43,739,888 $43,687,693

General Facili ties


Ball Mill & Hydroclone System $ $430,492 $430,492 $430,492 $430,492 $430,015


SO2 Removal System $ $443,191 $443,191 $443,191 $443,191 $442,286

Absorber Tower $ $645,562 $645,562 $645,562 $645,562 $645,437

Spray Pumps $ $45,987 $32,562 $45,987 $45,987 $45,931

Flue Gas Handling System $ $341,205 $341,205 $341,205 $341,205 $341,151

ID Fans $ $63,646 $63,646 $63,646 $63,646 $63,631



Support Equipment $ $282,697 $282,697 $282,697 $282,697 $282,697

Chimney $ $419,877 $419,877 $419,877 $419,877 $419,540

TOTAL $ $4,373,989 $4,377,997 $4,373,989 $4,373,989 $4,368,769

Engineeri ng Fees


Ball Mill & Hydroclone System $ $430,492 $430,492 $430,492 $430,492 $430,015 DBA Acid Tank (pump, heater, agitator) $ $0 $17,434 $0 $0 $0


Absorber Tower $ $645,562 $645,562 $645,562 $645,562 $645,437



12/25


Spray Pumps $ $45,987 $32,562 $45,987 $45,987 $45,931


ID Fans $ $63,646 $63,646 $63,646 $63,646 $63,631




Chimney $ $419,877 $419,877 $419,877 $419,877 $419,540

TOTAL $ $4,373,989 $4,377,997 $4,373,989 $4,373,989 $4,368,769

Contingency





Absorber Tower $ $1,291,125 $1,291,125 $1,291,125 $1,291,125 $1,290,873

Spray Pumps $ $91,974 $65,124 $91,974 $91,974 $91,862


ID Fans $ $127,292 $127,292 $127,292 $127,292 $127,262




Chimney $ $839,755 $839,755 $839,755 $839,755 $839,080TOTAL $ $8,747,978 $8,755,994 $8,747,978 $8,747,978 $8,737,539


Total Plant Cost (TPC) w/ Prime Contractor's M arku $ $63,072,918 $63,130,717 $63,072,918 $63,072,918 $62,997,654


All ow. for F unds Duri ng Constr. (AFDC) $ $0 $0 $0 $0 $0


Preproduction Costs $ $1,494,583 $1,490,904 $1,494,649 $1,494,583 $1,491,184

Inventory Capital $ $5,742 $5,742 $5,742 $5,742 $3,753

Total Capital Requir ement (TCR) $ $64,573,243 $64,627,363 $64,573,309 $64,573,243 $64,492,591$/kW $2,870 $2,872 $2,870 $2,870 $2,866

Maintenance Cost by Area Case1 Case 2 Case 3 Case 4 Case 5

TPC w/o Retrofi t F actor


Ball Mill & Hydroclone System $ $3,874,430 $3,874,430 $3,874,430 $3,874,430 $3,870,131



Absorber Tower $ $5,810,062 $5,810,062 $5,810,062 $5,810,062 $5,808,930

Spray Pumps $ $413,885 $293,056 $413,885 $413,885 $413,378


ID Fans $ $572,814 $572,814 $572,814 $572,814 $572,679




Chimney $ $3,778,895 $3,778,895 $3,778,895 $3,778,895 $3,775,860

TOTAL $ $39,365,899 $39,401,973 $39,365,899 $39,365,899 $39,318,924

Fir st Year M aintenance Costs

Reagent Feed System $ $744,813 $744,813 $744,813 $744,813 $743,515




Absorber Tower $ $290,503 $275,978 $290,503 $290,503 $290,447

Spray Pumps $ $20,694 $13,920 $20,694 $20,694 $20,669Flue Gas Handling System $ $153,542 $153,542 $153,542 $153,542 $153,518

ID Fans $ $28,641 $28,641 $28,641 $28,641 $28,634




13/25




Chimney $ $188,945 $188,945 $188,945 $188,945 $188,793

TOTAL $ $1,968,295 $1,944,869 $1,968,295 $1,968,295 $1,965,946

LSFO O&M Data and Costs Case1 Case 2 Case 3 Case 4 Case 5Cost Basis (Year) 2009 2009 2009 2009 2009

Parameters

Reagent Required lbs/hr 532 532 532 532 348

lbs/MMBtu 2.250 2.250 2.250 2.250 1.471

DBA Required lbs/hr 0.0 2.9 0.0 0.0 0.0

Percent SO2 Removal % 95% 95% 95% 95% 95%

FGD Sludge to Disposal lbs/hr, dry 857 857 857 857 553

Steam to FGD System lbs/hr 0 0 0 0 0

Total FGD Power Consumption kW 450 370 450 450 450

FGD Byproduct lbs/hr 0 0 0 0 0

Fixed O&M Costs

Number of Operators 3 3 3 3 3

(40 hrs/week) Operating Labor Cost ** $/yr $250,341 $250,341 $250,341 $250,341 $250,341

Maint. Labor & Matls. Cost $/yr $1,968,295 $1,944,869 $1,968,295 $1,968,295 $1,965,946

Admin. & Support Labor $/yr $311,298 $308,487 $311,298 $311,298 $311,016

TOTAL $/yr $2,529,934 $2,503,697 $2,529,934 $2,529,934 $2,527,303

Variable Operating Costs **

Reagent Costs $/yr $33,182 $33,182 $33,182 $33,182 $21,691

DBA Costs $/yr $0 $5,112 $0 $0 $0

Disposal Costs $/yr $21,402 $21,402 $21,402 $21,402 $13,800

Credit for Byproduct $/yr $0 $0 $0 $0 $0

Steam Costs $/yr $0 $0 $0 $0 $0

Power Costs $/yr $199,603 $164,293 $200,352 $199,603 $199,603

TOTAL $/yr $254,188 $223,990 $254,937 $254,188 $235,094

** These costs assume inputs are in current dollars (no escalation included).

I ntermediate Materi al Balance Calcs. Case1 Case 2 Case 3 Case 4 Case 5

Sulfi te Reaction

SO2 lbmole/hr 4.46 4.46 4.46 4.46 2.79

CaCO3 lbmole/hr 4.46 4.46 4.46 4.46 2.79

H2O lbmole/hr 2.23 2.23 2.23 2.23 1.39

CaSO3*1/2H2O lbmole/hr 4.46 4.46 4.46 4.46 2.79

CO2 lbmole/hr 4.46 4.46 4.46 4.46 2.79

SO2 lb/hr 286 286 286 286 179

CaCO3 lb/hr 446 446 446 446 279

H2O lb/hr 40 40 40 40 25 CaSO3*1/2H2O lb/hr 576 576 576 576 360

CO2 lb/hr 196 196 196 196 123

Sulfate Reaction

CaSO3*1/2H2O lbmole/hr 4.46 4.46 4.46 4.46 2.79

O2 lbmole/hr 2.23 2.23 2.23 2.23 1.39

H2O lbmole/hr 6.69 6.69 6.69 6.69 4.18

CaSO4*2H2O lbmole/hr 4.46 4.46 4.46 4.46 2.79

CaSO3*1/2H2O lb/hr 576 576 576 576 360

O2 lb/hr 71 71 71 71 45

H2O lb/hr 121 121 121 121 75

CaSO4*2H2O lb/hr 768 768 768 768 480

Water in Absorber

Mole Fraction H2O in Absorber % 0.1389 0.1389 0.1389 0.1389 0.1389

Moles H2O in Absorber lbmole 1,319.20 1,319.20 1,319.20 1,319.20 1,318.58

DBA Feed Calculations

SO2 Removed lbs/hr 286 286 286 286 179



14/25


DBA Added lbs/hr 0.00 2.86 0.00 0.00 0.00

DBA Added GPM 0.00 0.00 0.00 0.00 0.00



15/25


LSD Material Balance - Preliminary Case1 Case 2 Case 3 Case 4 Case 5

F lue Gas, Downstream of A ir Heater

Temperature F 300 300 300 300 300

Pressure in. H2O -12 -12 -12 -12 -12

Flow Rate SCFM 58,015 58,015 58,015 58,015 57,995

Flow Rate ACFM 88,958 88,958 88,958 88,958 88,927

CO2 lb/hr 50,489 50,489 50,489 50,489 50,535 N2 lb/hr 184,042 184,042 184,042 184,042 183,960

SO2 lb/hr 301 301 301 301 188

O2 lb/hr 14,693 14,693 14,693 14,693 14,687

HCl lb/hr 28 28 28 28 28


H2O lb/hr 17,793 17,793 17,793 17,793 17,805

Fly Ash lb/hr 1,808 1,808 1,808 1,808 1,855


F lue Gas, to Spray Dryer

Temperature F 300 300 300 300 300

Pressure in. H2O -12 -12 -12 -12 -12

Flow Rate SCFM 58,015 58,015 58,015 58,015 57,995

Flow Rate ACFM 88,958 88,958 88,958 88,958 88,927

CO2 lb/hr 50,489 50,489 50,489 50,489 50,535 N2 lb/hr 184,042 184,042 184,042 184,042 183,960

SO2 lb/hr 301 301 301 301 188

O2 lb/hr 14,693 14,693 14,693 14,693 14,687

HCl lb/hr 28 28 28 28 28


H2O lb/hr 17,793 17,793 17,793 17,793 17,805

Fly Ash lb/hr 1,808 1,808 1,808 1,808 1,855


F lue Gas, fr om Spray Dr yers (total)

Temperature F 147 147 147 147 147

Pressure in. H2O -17 -17 -17 -17 -13

Flow Rate SCFM 63,810 63,810 63,810 63,810 63,627

Flow Rate ACFM 79,166 79,166 79,166 79,166 78,124

CO2 lb/hr 50,489 50,489 50,489 50,489 50,535

N2 lb/hr 184,042 184,042 184,042 184,042 183,960

SO2 lb/hr 229 229 229 229 151

O2 lb/hr 14,689 14,689 14,689 14,689 14,685

HCl lb/hr 0 0 0 0 0


H2O lb/hr 34,317 34,317 34,317 34,317 33,854

Fly Ash lb/hr 3,356 3,356 3,356 3,356 3,006


F lue Gas Downstream of Particul ate Control Device

Temperature F 147 147 147 147 147

Pressure in. H2O -20 -20 -20 -20 -16

Flow Rate SCFM 63,784 63,784 63,784 63,784 63,605

Flow Rate ACFM 79,758 79,758 79,758 79,758 78,706

CO2 lb/hr 50,489 50,489 50,489 50,489 50,535

N2 lb/hr 184,042 184,042 184,042 184,042 183,960 SO2 lb/hr 211 211 211 211 141

O2 lb/hr 14,688 14,688 14,688 14,688 14,684

HCl lb/hr 0 0 0 0 0


H2O lb/hr 34,248 34,248 34,248 34,248 33,793



F lue Gas Downstream of I D F ans

Temperature F 152 152 152 152 152


Flow Rate SCFM 63,784 63,784 63,784 63,784 63,605

Flow Rate ACFM 76,207 76,207 76,207 76,207 75,992

CO2 lb/hr 50,489 50,489 50,489 50,489 50,535

N2 lb/hr 184,042 184,042 184,042 184,042 183,960 SO2 lb/hr 211 211 211 211 141

O2 lb/hr 14,688 14,688 14,688 14,688 14,684

HCl lb/hr 0 0 0 0 0


H2O lb/hr 34,248 34,248 34,248 34,248 33,793

254276149.xls.ms_office, LSD Cost & Tech. Results 15 12/9/2014, 12:59 PM


16/25




Lime to Ball M ill


Wt.% Solids wt. % 100% 100% 100% 100% 100%

Inerts lb/hr 9 9 9 9 5

CaO lb/hr 81 81 81 81 42

Total lb/hr 90 90 90 90 47

Water to Ball M ill


Flow Rate GPM 1 1 1 1 0

Wt.% Solids wt. % 0% 0% 0% 0% 0%

H2O lb/hr 296 296 296 296 154

Total lb/hr 296 296 296 296 154

L ime Slurr y to Head Tanks (Total)

Temperature F 110 110 110 110 110


Wt.% Solids wt. % 30% 30% 30% 30% 30%

Ca(OH)2 lb/hr 107 107 107 107 56

Inerts lb/hr 9 9 9 9 5

H2O lb/hr 270 270 270 270 140

Total lb/hr 386 386 386 386 201

Lime Slur ry from Head Tank

Temperature F 110 110 110 110 110


Wt.% Solids wt. % 49% 49% 49% 49% 50%

CaSO3*1/2H2O lb/hr 112 112 112 112 48

CaSO4*2H2O lb/hr 50 50 50 50 21

Flyash / Inerts lb/hr 1,541 1,541 1,541 1,541 1,283

Ca(OH)2 lb/hr 87 87 87 87 38

CaCl2 lb/hr 82 82 82 82 59

H2O lb/hr 1,945 1,945 1,945 1,945 1,471

Total lb/hr 3,818 3,818 3,818 3,818 2,920

L ime Slurr y to Atomizer

Temperature F 104 104 104 104 104

Flow Rate GPM 33 33 33 33 32

Wt.% Solids wt. % 10% 10% 10% 10% 8%

CaSO3*1/2H2O lb/hr 112 112 112 112 48

CaSO4*2H2O lb/hr 50 50 50 50 21


Ca(OH)2 lb/hr 87 87 87 87 38

CaCl2 lb/hr 82 82 82 82 59

H2O lb/hr 16,515 16,515 16,515 16,515 16,041

Total lb/hr 18,388 18,388 18,388 18,388 17,490

Solids fr om Spray Dryers (Total)

Temperature F 150 150 150 150 150

Wt.% Solids wt. % 98% 98% 98% 98% 98%

CaSO3*1/2H2O lb/hr 22 22 22 22 10

CaSO4*2H2O lb/hr 10 10 10 10 5 Flyash / Inerts lb/hr 301 301 301 301 280

Ca(OH)2 lb/hr -2 -2 -2 -2 -3

CaCl2 lb/hr 42 42 42 42 42

H2O lb/hr 8 8 8 8 7

Total lb/hr 380 380 380 380 341

Baghouse/ESP Soli ds to Recycle

Particulate Removal Efficiency % 99.99% 99.99% 99.99% 99.99% 99.99%

Temperature F 150 150 150 150 150

Wt.% Solids wt. % 98% 98% 98% 98% 98%

CaSO3*1/2H2O lb/hr 90 90 90 90 37

CaSO4*2H2O lb/hr 40 40 40 40 17

Flyash / Inerts lb/hr 1,230 1,230 1,230 1,230 999

Ca(OH)2 lb/hr -17 -17 -17 -17 -14

CaCl2 lb/hr 40 40 40 40 17 H2O lb/hr 27 27 27 27 21

Total lb/hr 1,371 1,371 1,371 1,371 1,060

Recycle Soli ds to Slu rry Tank

Temperature F 150 150 150 150 150



17/25


Wt.% Solids wt. % 98% 98% 98% 98% 98%

CaSO3*1/2H2O lb/hr 112 112 112 112 48

CaSO4*2H2O lb/hr 50 50 50 50 21


Ca(OH)2 lb/hr -19 -19 -19 -19 -18

CaCl2 lb/hr 82 82 82 82 59

H2O lb/hr 35 35 35 35 28

Total lb/hr 1,792 1,792 1,792 1,792 1,417

Blowdown Water to Recycle Solids Tank Temperature F 60 60 60 60 60


Wt.% Solids wt. % 0% 0% 0% 0% 0%

H2O lb/hr 1,640 1,640 1,640 1,640 1,302

Total lb/hr 1,640 1,640 1,640 1,640 1,302

Recycle Slurry to Head Tanks (Total )

Temperature F 110 110 110 110 110


Wt.% Solids wt. % 50% 50% 50% 50% 50%

CaSO3*1/2H2O lb/hr 112 112 112 112 48

CaSO4*2H2O lb/hr 50 50 50 50 21


Ca(OH)2 lb/hr -19 -19 -19 -19 -18

CaCl2 lb/hr 82 82 82 82 59 H2O lb/hr 1,675 1,675 1,675 1,675 1,330

Total lb/hr 3,432 3,432 3,432 3,432 2,719

Dry Solids

Temperature F 100 100 100 100 100

Wt.% Solids wt. % 98% 98% 98% 98% 98%

CaSO3*1/2H2O lb/hr 136 136 136 136 71

CaSO4*2H2O lb/hr 61 61 61 61 32


Ca(OH)2 lb/hr -26 -26 -26 -26 -27

CaCl2 lb/hr 84 84 84 84 84

H2O lb/hr 41 41 41 41 40

Total lb/hr 2,114 2,114 2,114 2,114 2,060

Solids to Landfi ll Temperature F 100 100 100 100 100

Wt.% Solids wt. % 80% 80% 80% 80% 80%

CaSO3*1/2H2O lb/hr 136 136 136 136 71

CaSO4*2H2O lb/hr 61 61 61 61 32


Ca(OH)2 lb/hr -26 -26 -26 -26 -27

CaCl2 lb/hr 84 84 84 84 84

H2O lb/hr 518 518 518 518 505

Total lb/hr 2,590 2,590 2,590 2,590 2,524

LSD Equipment Capital Costs Case1 Case 2 Case 3 Case 4 Case 5Cost Basis (Year) 2009 2009 2009 2009 2009

Sizing CriteriaReagent Feed System $ * $5,553,775 $5,553,775 $5,553,775 $5,553,775 $5,526,459

SO2 Removal System $ Wt. % S $1,834,342 $1,834,342 $1,834,342 $1,834,342 $1,907,952

Spray Dryers $ kACFM $3,120,143 $3,120,143 $3,120,143 $3,120,143 $3,119,624

Flue Gas Handling System $ kACFM $834,503 $834,503 $834,503 $834,503 $829,836

ID Fans $ ACFM $297,927 $297,927 $297,927 $297,927 $295,232

Waste / Byproduct Handling System $ kpph SO2 $1,565,513 $1,565,513 $1,565,513 $1,565,513 $1,513,201

Support Equipment $ MW $2,045,839 $2,045,839 $2,045,839 $2,045,839 $2,045,839

Chimney $ ACFM $2,733,206 $2,733,206 $2,733,206 $2,733,206 $2,730,198

TOTAL $ $17,985,249 $17,985,249 $17,985,249 $17,985,249 $17,968,343

* Based on lbs/hr of lime feed and GPM of lime slurry.

Capital Costs with Retrofit Factors



Spray Dryers $ $4,992,229 $4,992,229 $4,992,229 $4,992,229 $4,991,399


ID Fans $ $476,683 $476,683 $476,683 $476,683 $472,371



18/25


Waste / Byproduct Handling System $ $2,504,820 $2,504,820 $2,504,820 $2,504,820 $2,421,121


Chimney $ $4,373,130 $4,373,130 $4,373,130 $4,373,130 $4,368,317

TOTAL $ $28,776,398 $28,776,398 $28,776,398 $28,776,398 $28,749,348

General Facil iti es


SO2 Removal System $ $293,495 $293,495 $293,495 $293,495 $0

Spray Dryers $ $499,223 $499,223 $499,223 $499,223 $0Flue Gas Handling System $ $133,521 $133,521 $133,521 $133,521 $0

ID Fans $ $47,668 $47,668 $47,668 $47,668 $0



Chimney $ $437,313 $437,313 $437,313 $437,313 $436,832

TOTAL $ $2,877,640 $2,877,640 $2,877,640 $2,877,640 $1,890,512

Engineeri ng Fees



Spray Dryers $ $499,223 $499,223 $499,223 $499,223 $499,140


ID Fans $ $47,668 $47,668 $47,668 $47,668 $47,237



Chimney $ $437,313 $437,313 $437,313 $437,313 $436,832

TOTAL $ $2,877,640 $2,877,640 $2,877,640 $2,877,640 $2,874,935

Contingency



Spray Dryers $ $998,446 $998,446 $998,446 $998,446 $998,280

Flue Gas Handling System $ $267,041 $267,041 $267,041 $267,041 $0

ID Fans $ $95,337 $95,337 $95,337 $95,337 $0

Waste / Byproduct Handling System $ $500,964 $500,964 $500,964 $500,964 $0


Chimney $ $874,626 $874,626 $874,626 $874,626 $873,663TOTAL $ $5,755,280 $5,755,280 $5,755,280 $5,755,280 $4,905,624


Total Plant Cost (TPC) w/ Prime Contractor' s $ $41,495,566 $41,495,566 $41,495,566 $41,495,566 $39,573,031


All ow. for F unds Duri ng Constr. (AFD $ $0 $0 $0 $0 $0

Total Plant I nvestment (TPI ) $ $41,495,566 $41,495,566 $41,495,566 $41,495,566 $39,573,031



Total Capital Requirement (TCR) $ $42,472,280 $42,472,280 $42,472,303 $42,472,280 $40,490,629$/kW $1,888 $1,888 $1,888 $1,888 $1,800

Maintenance Cost by Area Case1 Case 2 Case 3 Case 4 Case 5

TPC w/o Retrof it Factor



Spray Dryers $ $4,493,006 $4,493,006 $4,493,006 $4,493,006 $4,117,904

Flue Gas Handling System $ $1,201,685 $1,201,685 $1,201,685 $1,201,685 $912,820

ID Fans $ $429,015 $429,015 $429,015 $429,015 $324,755

Waste / Byproduct Handling System $ $2,254,338 $2,254,338 $2,254,338 $2,254,338 $1,815,841


Chimney $ $3,935,817 $3,935,817 $3,935,817 $3,935,817 $3,931,486

TOTAL $ $25,898,758 $25,898,758 $25,898,758 $25,898,758 $24,525,413



19/25


F ir st Year M aintenance Costs



Spray Dryers $ $224,650 $224,650 $224,650 $224,650 $205,895

Flue Gas Handling System $ $60,084 $60,084 $60,084 $60,084 $0

ID Fans $ $21,451 $21,451 $21,451 $21,451 $0

Waste / Byproduct Handling System $ $112,717 $112,717 $112,717 $112,717 $0


Chimney $ $196,791 $196,791 $196,791 $196,791 $196,574

TOTAL $ $1,294,938 $1,294,938 $1,294,938 $1,294,938 $1,073,600

LSD O& M Data and Costs Case1 Case 2 Case 3 Case 4 Case 5Cost Basis (Year) 2009 2009 2009 2009 2009

Parameters

Reagent Required lbs/hr 90 90 90 90 47

lbs/MMBtu 0.380 0.380 0.380 0.380 0.198

Percent SO2 Removal % 30% 30% 30% 30% 25%

FGD Solids - dry lbs/hr 2,072 2,072 2,072 2,072 2,019

- wetted lbs/hr 2,590 2,590 2,590 2,590 2,524

Fresh Water to FGD gpm 1 1 1 1 0

Blowdown Water to FGD gpm 33 33 33 33 33

Total FGD Power Consumption kW 158 158 158 158 158

Fixed O&M Costs

Number of Operators 3 3 3 3 3

(40 hrs/week)

Operating Labor Cost ** $/yr $182,758 $182,758 $182,758 $182,758 $182,758

Maint. Labor & Matls. Cost $/yr $1,294,938 $1,294,938 $1,294,938 $1,294,938 $1,073,600

Admin. & Support Labor $/yr $210,220.07 $210,220 $210,220 $210,220 $183,660

TOTAL $/yr $1,687,916 $1,687,916 $1,687,916 $1,687,916 $1,440,018

Variable Operating Costs **

Reagent Costs $/yr $0 $0 $0 $0 $0

Disposal Costs $/yr $0 $0 $0 $0 $0 Credit for Byproduct $/yr $0 $0 $0 $0 $0

Steam Costs $/yr $0 $0 $0 $0 $0

Fresh Water Costs $/yr $177 $177 $177 $177 $92

Power Costs $/yr $69,861 $69,861 $70,123 $69,861 $69,861

TOTAL $/yr $70,038 $70,038 $70,301 $70,038 $69,953




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Fabri c F il ter - Preliminary Case1 Case 2 Case 3 Case 4 Case 5

Fl ue Gas, Upstream of Fabri c Fi lter

Temperature F 300 300 147 147 147

Pressure in. H2O -12 -12 -17 -17 -13

Flow Rate SCFM 58,015 58,015 63,810 63,810 63,627

Flow Rate ACFM 88,958 88,958 79,166 79,166 78,124

CO2 lb/hr 50,489 50,489 50,489 50,489 50,535 N2 lb/hr 184,042 184,042 184,042 184,042 183,960

SO2 lb/hr 301 301 229 229 151

O2 lb/hr 14,693 14,693 14,689 14,689 14,685

HCl lb/hr 28 28 0 0 0


H2O lb/hr 17,793 17,793 34,317 34,317 33,854

Fly Ash lb/hr 1,808 1,808 3,356 3,356 3,006


Total Fabric Requir ed Ft2

25,416 25,416 22,619 22,619 22,321

Surf ace Ar ea per Bag Ft2

31.4 31.4 31.4 31.4 31.4

Requir ed No. of Bags (no spare compartments) 809 809 720 720 710

Fi nal No. of Bags 890 890 792 792 782

No. of Casings 1 1 1 1 1

Fabric Fi lter Dimensions (per Casing) Ft2

874 874 778 778 767

Length Ft 42 42 39 39 39

Width Ft 21 21 20 20 20

Capital Cost Case1 Case 2 Case 3 Case 4 Case 5

Cost Basis (Year) 2009 2009 2009 2009 2009

Fabric Filter $ $1,098,464 $1,098,464 $1,011,319 $1,011,319 $1,001,864

Bags $ $67,784 $67,784 $60,323 $60,323 $59,529 Ash Handling System $ $346,222 $346,222 $372,812 $372,812 $366,805

ID Fan(s) $ $176,894 $176,894 $164,575 $164,575 $163,230

Equipment Cost Subtotal $ $1,689,364 $1,689,364 $1,609,030 $1,609,030 $1,591,428


Taxes $ $109,809 $109,809 $104,587 $104,587 $103,443

Freight $ $84,468 $84,468 $80,451 $80,451 $79,571

Purchased Equipment Cost Subtotal $ $1,917,429 $1,917,429 $1,826,249 $1,826,249 $1,806,271

Installation $ $1,284,677 $1,284,677 $1,223,587 $1,223,587 $1,210,202





Contingency $ $1,024,674 $1,024,674 $975,947 $975,947 $965,271

Total Plan t Cost (TPC) $ $7,172,717 $7,172,717 $6,831,631 $6,831,631 $6,756,899Total Plan t Cost (TPC) w/ Prime Contractor' s M $ $7,387,898 $7,387,898 $7,036,579 $7,036,579 $6,959,606

Total Cash Expended (TCE ) $ $7,280,307 $7,280,307 $6,934,105 $6,934,105 $6,858,252

All ow. for F unds Dur ing Constr. (AFDC) $ $387,327 $387,327 $368,908 $368,908 $364,873





$/kW $347.6 $347.6 $331.1 $331.1 $327.4

O&M Data and Costs Case1 Case 2 Case 3 Case 4 Case 5

Cost Basis (Year) 2009 2009 2009 2009 2009

Power Required Excluding ID Fan(s) kW 42 42 38 38 37

ID Fan Power for FF Delta P kW 90 90 80 80 79

Total Power kW 132 132 118 118 116

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Power Cost ** $/yr $58,563 $81,065 $72,526 $72,255 $71,317

Maintenance Costs $/yr $224,147 $224,147 $213,488 $213,488 $211,153

Periodic Replacement Items $/yr $67,784 $67,784 $60,323 $60,323 $59,529

First Year Cost. Bags Replaced Every 5 Years 5 Years 5 Years 5 Years 5 Years


ESP Case1 Case 2 Case 3 Case 4 Case 5

Fl ue Gas, Upstream of ESP

Temperature F 300 300 147 147 147

Pressure in. H2O -12 -12 -17 -17 -13

Flow Rate SCFM 58,015 58,015 63,810 63,810 63,627

Flow Rate ACFM 88,958 88,958 79,166 79,166 78,124

CO2 lb/hr 50,489 50,489 50,489 50,489 50,535

N2 lb/hr 184,042 184,042 184,042 184,042 183,960

SO2 lb/hr 301 301 229 229 151

O2 lb/hr 14,693 14,693 14,689 14,689 14,685

HCl lb/hr 28 28 0 0 0


H2O lb/hr 17,793 17,793 34,317 34,317 33,854

Fly Ash lb/hr 1,808 1,808 3,356 3,356 3,006


I nlet Particul ate Loading lb/hr 1,808 1,808 3,356 3,356 3,006

gr/ft3 2.37 2.37 4.95 4.95 4.49

Overall PM Collection Ef fi ciency % h 100.0% 100.0% 100.0% 100.0% 100.0%

ESP Requi rements

k dimensionless 0.451 0.451 0.451 0.451 0.451

E kV/cm 10.0 10.0 10.0 10.0 10.0

Ash Compositi on

Na2O wt% in Ash 2.80 2.80 2.80 2.80 2.80

Fe wt% in Ash 9 9 9.00 9.00 9.00

MgO wt% in Ash 20.90 20.90 20.90 20.90 20.90

CaO wt% in Ash 0.00 0.00 0.00 0.00 0.00

Fl ue Gas Composition

H2O Vol% 10.77 10.77 19.57 19.57 19.34

SO2 ppm 512 512 367 367 242

SO3 ppm 3.8 3.8 2.7 2.7 1.8

Fl ue Gas Temperature

TF F 300 300 147 147 147

TC C 149 149 64 64 64

TK Kelvin 422 422 337 337 337

Resistivity Calculati ons

Volume Resistivity

rv1 Log10(ohm-cm) 8.31 8.31 8.31 8.31 8.31rv2 Log10(ohm-cm) 8.07 8.07 8.07 8.07 8.07

iv Log10(ohm-cm) 1.14 1.14 1.14 1.14 1.14

rv Log10(ohm-cm) 11.41 11.41 14.00 14.00 14.00

rv(TK=1000/2.4) Log10(ohm-cm) 11.54 11.54 11.54 11.54 11.54

Volume Resistivity ohm-cm 2.5602E+11 2.5602E+11 9.9638E+13 9.9638E+13 9.9638E+13

Surface Resistivity

rs1 Log10(ohm-cm) 9.78 9.78 9.78 9.78 9.78

rs2 Log10(ohm-cm) 9.55 9.55 8.42 8.42 8.45

rs3 Log10(ohm-cm) 8.94 8.94 7.81 7.81 7.84

rs4 Log10(ohm-cm) 8.70 8.70 7.57 7.57 7.60

rs4(with E=12) Log10(ohm-cm) 8.64 8.64 7.51 7.51 7.54

rs0 Log10(ohm-cm) 10.01 10.01 10.00 10.00 10.00

rs Log10(ohm-cm) 9.20 9.20 4.17 4.17 4.24

Surface Resistivity ohm-cm 1.5767E+09 1.5767E+09 1.4717E+04 1.4717E+04 1.7216E+04

rvs1 ohm-cm 1.5670E+09 1.5670E+09 1.4717E+04 1.4717E+04 1.7216E+04

rs2(with H2O=10) Log10(ohm-cm) 9.65E+00 9.65E+00 9.65E+00 9.65E+00 9.65E+00

rs3(with H2O=10) Log10(ohm-cm) 9.04 9.04 9.04 9.04 9.04

rs4(with H2O = 10) Log10(ohm-cm) 8.80 8.80 8.80 8.80 8.80

rs4(with H2O = 10, E = 12) Log10(ohm-cm) 8.74 8.74 8.74 8.74 8.74

rs0(with H2O = 10) Log10(ohm-cm) 10.01 10.01 10.01 10.01 10.01

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rs(with H2O = 10, TK = 1000/2.4) Log10(ohm-cm) 9.20 9.20 9.20 9.20 9.20

rvs1(with H2O=10, TK = 1000/2.4) ohm-cm 1.5830E+09 1.5830E+09 1.5830E+09 1.5830E+09 1.5830E+09

rvs2 Log10(ohm-cm) 9.44 9.44 9.44 9.44 9.44

Acid Resistivity

ia1 Log10(ohm-cm) 0.29 0.29 0.29 0.29 0.29

ra1 Log10(ohm-cm) 7.53 7.53 7.53 7.53 7.53

sa -2.05 -2.05 -2.05 -2.05 -2.05

ia2 Log10(ohm-cm) 8.76 8.76 8.76 8.76 8.76

ra2 Log10(ohm-cm) 7.58 7.58 7.88 7.88 8.25

acid_v index value 2 2 1 1 1

atom_v index value 1 1 1 1 1

sa1 -28.39 -28.39 -4.74 -4.74 -4.74

ia3 Log10(ohm-cm) 75.72 75.72 19.25 19.25 19.62

ra3 Log10(ohm-cm) 8.45 8.45 5.19 5.19 5.56

ra Log10(ohm-cm) 8.37 8.37 5.89 5.89 6.17

Acid Resistivity ohm-cm 2.3400E+08 2.3400E+08 7.8246E+05 7.8246E+05 1.4960E+06

Total Resistivity

rvsa ohm-cm 2.0359E+08 2.0359E+08 1.4445E+04 1.4445E+04 1.7020E+04

Migration Velocity

w k 1000ft/minute 0.060 0.060 0.091 0.091 0.091

Specifi c Collection Area

SCA ft2/1000acfm 2155 2155 1633 1633 1601

Total Collector Plate Area ft2

191,669 191,669 129,297 129,297 125,105

ESP Footprint Area ft2

5,324 5,324 3,592 3,592 3,475

Capital Cost Case1 Case 2 Case 3 Case 4 Case 5

Cost Basis (Year) 2009 2009 2009 2009 2009

ESP $ $763,689 $763,689 $687,816 $687,816 $679,686

Ash Handling System $ $346,222 $346,222 $372,812 $372,812 $366,805

ID Fan(s) $ $176,894 $176,894 $164,575 $164,575 $163,230 Equipment Cost Subtotal $ $1,286,805 $1,286,805 $1,225,203 $1,225,203 $1,209,721


Taxes $ $83,642 $83,642 $79,638 $79,638 $78,632

Freight $ $64,340 $64,340 $61,260 $61,260 $60,486

Purchased Equipment Cost Subtotal $ $1,460,524 $1,460,524 $1,390,606 $1,390,606 $1,373,033

Installation $ $1,183,024 $1,183,024 $1,126,391 $1,126,391 $1,112,157





Contingency $ $845,935 $845,935 $805,439 $805,439 $795,261


Total Plan t Cost (TPC) w/ Prime Contractor ' s M $ $6,099,194 $6,099,194 $5,807,214 $5,807,214 $5,733,829


All ow. for Funds Dur ing Constr. (AFDC) $ $319,764 $319,764 $304,456 $304,456 $300,609





$/kW $287.0 $287.0 $273.2 $273.2 $269.8

O&M Data and Costs Case1 Case 2 Case 3 Case 4 Case 5

Cost Basis (Year) 2009 2009 2009 2009 2009

Power Required Excluding ID Fan(s) kW -103 -103 -21 -21 -17 ID Fan Power for FF Delta P kW 45 45 40 40 39

Total Power kW -58 -58 19 19 22

Power Cost ** $/yr ($25,649) ($35,505) $11,709 $11,665 $13,515

Maintenance Costs $/yr $185,048 $185,048 $176,190 $176,190 $173,963


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FUEL AND COMBUSTION CALCULATIONS Case1 Case 2 Case 3 Case 4 Case 5

FUEL ANALYSIS FOR SPECIFI ED COALS

PROXIMATE ANALYSIS (wt. %)

Moisture wt% 25.2 25.2 25.2 25.2 25.2

Volatile Matter wt% 36.4 36.4 36.4 36.4 36.4

Fixed Carbon wt% 30.3 30.3 30.3 30.3 30.3

Ash wt% 8.15 8.15 8.15 8.15 8.36 TOTAL 100.05 100.05 100.05 100.05 100.26

COAL ULTIMATE ANALYSIS (wt. %)

Moisture wt% 25.2 25.2 25.2 25.2 25.2

Carbon wt% 51.52 51.52 51.52 51.52 51.52

Hydrogen wt% 3.29 3.29 3.29 3.29 3.29

Nitrogen wt% 0.69 0.69 0.69 0.69 0.69

Chlorine wt% 0.1 0.1 0.1 0.1 0.1

Sulfur wt% 0.56 0.56 0.56 0.56 0.35

Ash wt% 8.15 8.15 8.15 8.15 8.36

Oxygen wt% 10.49 10.49 10.49 10.49 10.49

TOTAL 100 100 100 100 100

HIGHER HEATING VALUE (HHV)

Modified Mott Spooner - calc Btu/lb 8789 8789 8789 8789 8781

COAL COST $/MMBtu 1.50 1.50 1.50 1.50 1.50COAL ASH ANALYSIS (ASTM, as rec'd)

SiO2 wt% 27.00 27.00 27.00 27.00 27.00

Al2O3 wt% 19.00 19.00 19.00 19.00 19.00

TiO2 wt% 1.08 1.08 1.08 1.08 1.08

Fe2O3 wt% 9.00 9.00 9.00 9.00 9.00

CaO wt% 18.50 18.50 18.50 18.50 18.50

MgO wt% 2.40 2.40 2.40 2.40 2.40

Na2O wt% 2.80 2.80 2.80 2.80 2.80

K2O wt% 0.45 0.45 0.45 0.45 0.45

P2O5 wt% 0.42 0.42 0.42 0.42 0.42

SO3 wt% 18.85 18.85 18.85 18.85 18.85

Other Unaccounted for wt% 0.50 0.50 0.50 0.50 0.50

TOTAL wt% 100.00 100.00 100.00 100.00 100.00

PROXIMATE ANALYSIS (lbs/MMBtu) Moisture lbs/MMBtu 28.67 28.67 28.67 28.67 28.70

Volatile Matter lbs/MMBtu 41.42 41.42 41.42 41.42 41.45

Fixed Carbon lbs/MMBtu 34.47 34.47 34.47 34.47 34.51

Ash lbs/MMBtu 9.27 9.27 9.27 9.27 9.52

TOTAL lbs/MMBtu 113.84 113.84 113.84 113.84 114.18

COAL ULTIMATE ANALYSIS (lbs/MMBtu)

Moisture lbs/MMBtu 28.67 28.67 28.67 28.67 28.70

Carbon lbs/MMBtu 58.62 58.62 58.62 58.62 58.67

Hydrogen lbs/MMBtu 3.74 3.74 3.74 3.74 3.75

Nitrogen lbs/MMBtu 0.79 0.79 0.79 0.79 0.79

Chlorine lbs/MMBtu 0.11 0.11 0.11 0.11 0.11

Sulfur lbs/MMBtu 0.64 0.64 0.64 0.64 0.40

Ash lbs/MMBtu 9.27 9.27 9.27 9.27 9.52

Oxygen lbs/MMBtu 11.94 11.94 11.94 11.94 11.95

TOTAL lbs/MMBtu 113.78 113.78 113.78 113.78 113.88

COAL ULTIMATE ANALYSIS (lbmoles/MMBtu)

Moisture lbmoles/MMBtu 1.5915 1.5915 1.5915 1.5915 1.5930

Carbon lbmoles/MMBtu 4.8804 4.8804 4.8804 4.8804 4.8848

Hydrogen lbmoles/MMBtu 1.8569 1.8569 1.8569 1.8569 1.8586

Nitrogen lbmoles/MMBtu 0.0280 0.0280 0.0280 0.0280 0.0280

Chlorine lbmoles/MMBtu 0.0016 0.0016 0.0016 0.0016 0.0016

Sulfur lbmoles/MMBtu 0.0199 0.0199 0.0199 0.0199 0.0124

Ash lbmoles/MMBtu 9.2730 9.2730 9.2730 9.2730 9.5206

Oxygen lbmoles/MMBtu 0.3730 0.3730 0.3730 0.3730 0.3733

F lue Gas, Downstream Of Economizer

Flue Gas (lb-moles/MMBtu)

CO2 lbmoles/MMBtu 4.856 4.856 4.856 4.856 4.860

NOx lbmoles/MMBtu 0.009 0.009 0.009 0.009 0.009 HCl lbmoles/MMBtu 0.003 0.003 0.003 0.003 0.003

SO2 lbmoles/MMBtu 0.020 0.020 0.020 0.020 0.012

Total O2 Req'd - * lbmoles/MMBtu 6.529 6.529 6.529 6.529 6.526

N2 lbmoles/MMBtu 24.584 24.584 24.584 24.584 24.572

O2 lbmoles/MMBtu 1.088 1.088 1.088 1.088 1.088

H20 lbmoles/MMBtu 4.096 4.096 4.096 4.096 4.099

Total Dry lbmoles/MMBtu 30.560 30.560 30.560 30.560 30.545

Total Wet lbmoles/MMBtu 34.656 34.656 34.656 34.656 34.644

Wet Flue Gas PPMV & % Vol

% O2 % Vol 3.140 3.140 3.140 3.140 3.139

% CO2 % Vol 14.012 14.012 14.012 14.012 14.030

% N2 % Vol 70.936 70.936 70.936 70.936 70.928

NOx ppmv 268.765 268.765 268.765 268.765 268.903

HCL ppmv 92.604 92.604 92.604 92.604 92.721 SO2 ppmv 573.395 573.395 573.395 573.395 358.822

% H2O % Vol 11.818 11.818 11.818 11.818 11.831

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Dry Flue Gas PPMV & % Vol

% O2 % Vol 3.561 3.561 3.561 3.561 3.561

% CO2 % Vol 15.890 15.890 15.890 15.890 15.912

% N2 % Vol 80.444 80.444 80.444 80.444 80.446

NOx ppmv 304.786 304.786 304.786 304.786 304.985

HCL ppmv 105.015 105.015 105.015 105.015 105.162

SO2 ppmv 650.243 650.243 650.243 650.243 406.969

% H2O % Vol 0 0 0 0 0

F lue Gas, Air & Ash Downstream Of Economizer

Flue Gas (lbs/MMBtu) O2 lbs/MMBtu 34.818 34.818 34.818 34.818 34.802

CO2 lbs/MMBtu 213.711 213.711 213.711 213.711 213.905

N2 lbs/MMBtu 688.834 688.834 688.834 688.834 688.517

NOx lbs/MMBtu 0.280 0.280 0.280 0.280 0.280

HCl lbs/MMBtu 0.117 0.117 0.117 0.117 0.117

SO2 lbs/MMBtu 1.273 1.273 1.273 1.273 0.796

H2O lbs/MMBtu 73.786 73.786 73.786 73.786 73.838

Gas Dry lbs/MMBtu 939.033 939.033 939.033 939.033 938.418

Gas Wet lbs/MMBtu 1012.819 1012.819 1012.819 1012.819 1012.256

% H2O wt% 7.285 7.285 7.285 7.285 7.294

Theoretical Wet Air lbs/MMBtu 757.293 757.293 757.293 757.293 756.944

Actual Total Wet Air lbs/MMBtu 908.752 908.752 908.752 908.752 908.333

Mol Wt Wet, Lb/Lb-Mol lbs/lb-mole 29.225 29.225 29.225 29.225 29.219

Total Ash lbs/MMBtu 9.566 9.566 9.566 9.566 9.814 Fly Ash lbs/MMBtu 7.653 7.653 7.653 7.653 7.851

Bottom Ash lbs/MMBtu 1.913 1.913 1.913 1.913 1.963

NOx - Flue Gas lbs/MMBtu 0.280 0.280 0.280 0.280 0.280

Carbon Loss lbmoles/MMBtu 0.024 0.024 0.024 0.024 0.024

* - Theoretical + Excess O2 Required for Combustion, Not O2 in Flue Gas

Gases, Downstream Of Ai r H eater

Flue Gas (lb-moles/MMBtu)

CO2 lbmoles/MMBtu 4.856 4.856 4.856 4.856 4.860

NOx lbmoles/MMBtu 0.009 0.009 0.009 0.009 0.009

HCl lbmoles/MMBtu 0.003 0.003 0.003 0.003 0.003

SO2 lbmoles/MMBtu 0.020 0.020 0.020 0.020 0.012

N2 lbmoles/MMBtu 27.802 27.802 27.802 27.802 27.790

O2 lbmoles/MMBtu 1.944 1.944 1.944 1.944 1.943

H2O lbmoles/MMBtu 4.181 4.181 4.181 4.181 4.183

Total Dry Flue Gas lbmoles/MMBtu 34.634 34.634 34.634 34.634 34.618

Total Wet Flue Gas lbmoles/MMBtu 38.815 38.815 38.815 38.815 38.801

Dry Air Addition lbmoles/MMBtu 4.074 4.074 4.074 4.074 4.072

Wet Air Addition lbmoles/MMBtu 4.159 4.159 4.159 4.159 4.157

Wet Flue Gas PPMV & % Vol

% O2 % Vol 5.01 5.01 5.01 5.01 5.01

% CO2 % Vol 12.51 12.51 12.51 12.51 12.53

% N2 % Vol 71.63 71.63 71.63 71.63 71.62

PPMV NOx ppmv 239.97 239.97 239.97 239.97 240.09

PPMV HCL ppmv 82.68 82.68 82.68 82.68 82.79

PPMV SO2 ppmv 511.96 511.96 511.96 511.96 320.38

% H2O % Vol 10.77 10.77 10.77 10.77 10.78

TOTAL 100.00 100.00 100.00 100.00 100.00

Dry Flue Gas PPMV & % Vol

% O2 % Vol 5.61 5.61 5.61 5.61 5.61

% CO2 % Vol 14.02 14.02 14.02 14.02 14.04

% N2 % Vol 80.27 80.27 80.27 80.27 80.28

NOx ppmv 268.93 268.93 268.93 268.93 269.11

HCL ppmv 92.66 92.66 92.66 92.66 92.79

SO2 ppmv 573.76 573.76 573.76 573.76 359.09

% H2O % Vol 0 0 0 0 0

TOTAL 100.00 100.00 100.00 100.00 100.00

F lue Gas & Air Downstream Of Ai r H eater

Flue Gas (lbs/MMBtu)

O2 lbs/MMBtu 62.194 62.194 62.194 62.194 62.168

CO2 lbs/MMBtu 213.711 213.711 213.711 213.711 213.905 N2 lbs/MMBtu 779.013 779.013 779.013 779.013 778.665

NOx lbs/MMBtu 0.280 0.280 0.280 0.280 0.280

HCl lbs/MMBtu 0.117 0.117 0.117 0.117 0.117

SO2 lbs/MMBtu 1.273 1.273 1.273 1.273 0.796

H2O lbs/MMBtu 75.314 75.314 75.314 75.314 75.365

Gas Dry lbs/MMBtu 1056.587 1056.587 1056.587 1056.587 1055.931

Gas Wet lbs/MMBtu 1131.901 1131.901 1131.901 1131.901 1131.297

Wt % H2O wt% 6.654 6.654 6.654 6.654 6.662

Total Wet Air lbs/MMBtu 1027.834 1027.834 1027.834 1027.834 1027.374

Mol Wt Wet, Lb/Lb-Mol lbs/lb-mole 29.162 29.162 29.162 29.162 29.156

Boi ler Losses & Ef fi ciencies

Dry Gas % 6.295 6.295 6.295 6.295 6.292

Moisture % 7.172 7.172 7.172 7.172 7.178

Carbon % 0.413 0.413 0.413 0.413 0.414 Radiation % 0.352 0.352 0.352 0.352 0.352

Manufacturers Margin % 1.5 1.5 1.5 1.5 1.5

Ash Losses % 0 0 0 0 0

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Total Losses % 15.732 15.732 15.732 15.732 15.736

Boiler Efficiency % 84.268 84.268 84.268 84.268 84.264

Coal F low Rates

Btu Input Rate to Boiler MMBtu/hr 236.25 236.25 236.25 236.25 236.25

Coal Input Rate to Boiler tons/hr 13.4 13.4 13.4 13.4 13.5

Coal Input Rate to Boiler lbs/MMBtu 113.8 113.8 113.8 113.8 113.9

Economizer Outlet

Flue Gas SCFM/MMBtu 13,156 13,156 13,156 13,156 13,152 Flue Gas SCFM 51,803 51,803 51,803 51,803 51,785

Wet Flue Gas lb/hr 239,278 239,278 239,278 239,278 239,145

Wet Air SCFM 47,076 47,076 47,076 47,076 47,054

Wet Air lb/hr 214,693 214,693 214,693 214,693 214,594

Total Air % 120% 120% 120% 120% 120%

Excess Air % 20% 20% 20% 20% 20%

Air Heater Outlet

Flue Gas SCFM/MMBtu 14,735 14,735 14,735 14,735 14,730

Flue Gas SCFM 58,020 58,020 58,020 58,020 58,000

Wet Flue Gas lb/hr 267,412 267,412 267,412 267,412 267,269

Wet Air SCFM 53,245 53,245 53,245 53,245 53,221

Wet Air lb/hr 242,826 242,826 242,826 242,826 242,717

Wet Air Leakage SCFM 6,169 6,169 6,169 6,169 6,167

Wet Air Leakage lb/hr 28,133 28,133 28,133 28,133 28,123 Equivalent Total Air % 135.7% 135.7% 135.7% 135.7% 135.7%

Equivalent Excess Air % 35.7% 35.7% 35.7% 35.7% 35.7%

Flue Gas Temperature F 300 300 300 300 300

Pressure in. H2O -12 -12 -12 -12 -12

Flue Gas ACFM 88,965 88,965 88,965 88,965 88,934

Ash Parameters

Fly Ash tons/hr 0.90 0.90 0.90 0.90 0.93

Bottom Ash tons/hr 0.23 0.23 0.23 0.23 0.23

Total Ash tons/hr 1.13 1.13 1.13 1.13 1.16

lf cue cost 3 seattle

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