Basin Elecric 11786-001

9/20/2011

Study Assumptions

Basin Electric Basin Electric

HighDust Low Dust

1) Fuel to be Fired Dry Fork Dry Fork

2) SCR Design Temperature, F 700 600

3) Inlet NOx, lb/MBtu 0.20 0.20

4) Required Efficiency, % 85.00 85.00

5) Inlet Dust loading, lb/MBtu 4.80 0.015

6) Catalyst Pitch, mm 8.4 5.0

7) Initial catalyst life, years 2 3

8) Gas Gas Heat Exchanger No Yes

9) In duct heating No Superheated steam

10) SO2 to SO3 Oxidation, % 3.00 2.00

Sargent & Lundy
SCR Power Consumption (High/Low Dust)

High Dust Low Dust

Gross Power, MW 440 440

ID fans

 Increase in Fan HP 3,625 8,157

 Increase in Motor kW 2,705 6,085

Ammonia System Power

 Ammonia Consumption, lb/hr 1091 873

 Power Consumption, kW 109 87

2 x 20 kW Heaters 2 x 20 kW Heaters

Dilution Air Blower

 Power Consumption, HP 128.0 102.0

 Power Consumption, kW 95.5 76.1

 Connected Air Blowers, kW 2 x 20 2 x 20

Dilution Air Heaters

 Power Consumption, kW 387.1 309.7

 Connected Heaters, kW 2 x 75 2 x 75

Ammonia Pump

 Power Consumption, HP 2.4 1.9

 Power Consumption, kW 1.8 1.4

Seal Air Fans

 Power Consumption, HP 88 88

 Power Consumption, kW 66 66

 Connected Seal air fan, kW 2 x 125 2 x 125

Sub-Total Power Consumption, kW 3363 6625

Electrical and Control Power 

Consumption, kW 168 331

Total Power Consumption, kW 3531 6956

% of Gross 0.80 1.58
Basin Elecric 12109-001

9/20/2011

EXHIBIT 1a

COST EFFECTIVENESS ANALYSIS

TAIL-END SCR PLUS ASOFA AT LELAND OLDS UNIT 2

Units

Fox Revised 

Cost I

INPUT DATA

Design Coal Lignite Lignite

SCR Configuration Tail End Tail End 

Capacity MW 440 440

Heat Input MBtu/hr 5,130 5,130

Inlet NOx Emissions lb/MMBtu 0.67 0.48

Outlet N0x Emissions lb/MMBtu 0.05

Control Efficiency % 93 90

NOx Removed lb/hr 3,181 2,216

NOx Removed tons/yr 12,050 10,517

Ammonia Required lb/hr 1,253 873

Ammonia Cost $/ton 475 700

Pressure Drop across catalyst in w.c. 4 4

Pressure Drop in w.c. 18 18

Power Consumption kW 6,956 6,956

Power Cost $/MWh 38 50

Temperature Rise Across Steam to Flue 

Gas Reheater F 50 50

Natural Gas Requirement MMBtu/hr 66 115

(30 F rise) (50 F rise)

Natural Gas Cost $/MMBtu 5.5 12.0

Unit Capital Cost SCR + SOFA+SI (2009) $/kW 388 388

Unit Capital Cost SCR + SOFA (2009) $/kW 376

Unit Capital Cost ASOFA (2009) $/kW 26 26

Unit Capital Cost SCR (2009) $/kW 350

Unit Catalyst Cost $/m3

7,500 7,500

Initial Catalyst Volume m

3

440 530

Coal Cost $/MBtu 1.00 1.00

Catalyst Cost $ 3,300,000 3,960,000

Annual Capacity Factor % 86.5 92.3

Cost of Outage $/week 0 3,696,000

Outage Duration weeks 0 4

Catalyst Replacement 24,000 hrs 6 months

Number of Catalyst Layers 3 1

Future Worth Factor 0.31 1

Capital Recovery Factor 0.08718 0.08718

Levelized Annual O&M Factor 1 1.19314

TOTAL CAPITAL COST (2010)

SCR + ASOFA Capital Cost $ 175,561,000 170,720,000

SCR Capital Cost $ 164,121,000

SO3 Mitigation Capital Costa

$ 0 0

 Total Installed Capital Cost $ 175,561,000 170,720,000

 Annual Capital Cost $/yr 15,305,408 14,883,370

FIXED O&M COST

Operating Labor Cost $/yr $0 $0

Maintenance Materials Cost $/yr $527,000 $512,000

Maintenance Labor Cost $/yr $351,000 $341,000

Administrative and Support Labor $/yr $0 $0

 Total Fixed O&M Cost $/yr $878,000 $853,000

VARIABLE O&M COST

Ammonia Cost $/yr 2,255,000 2,471,000

Catalyst Cost $/yr 342,000 7,920,000

Power Cost $/yr 2,003,000 2,813,000

Gas Penalty $/yr 2,767,000 11,161,000

Outage Penalty $/yr 0 14,784,000

Sorbent Injection $/yr 0 207,000

 Total Variable O&M Cost $/yr 7,367,000 39,356,000

40,209,000

TOTAL O&M COSTS $/yr 8,245,000 47,974,966

Cost Effectiveness $/ton 1,954 5,977

Sargent & Lundy
Basin Elecric 12109-001

9/20/2011

EXHIBIT 1b

COST EFFECTIVENESS ANALYSIS

TAIL-END SCR PLUS ASOFA AT LELAND OLDS UNIT 2

Units

Fox Revised 

Cost I

INPUT DATA

Design Coal Lignite Lignite

SCR Configuration Tail End Tail End 

Capacity MW 440 440

Heat Input MBtu/hr 5,130 5,130

Inlet NOx Emissions lb/MMBtu 0.48 0.48

Outlet N0x Emissions lb/MMBtu 0.05

Control Efficiency % 90 90

NOx Removed lb/hr 2,206 2,216

NOx Removed tons/yr 8,357 10,517

Ammonia Required lb/hr 869 873

Ammonia Cost $/ton 475 700

Pressure Drop across catalyst in w.c. 4 4

Pressure Drop in w.c. 18 18

Power Consumption kW 6,956 6,956

Power Cost $/MWh 38 50

Temperature Rise Across Steam to Flue 

Gas Reheater F 50 50

Natural Gas Requirement MMBtu/hr 66 115

(30 F rise) (50 F rise)

Natural Gas Cost $/MMBtu 5.5 12.0

Unit Capital Cost SCR + SOFA+SI $/kW 388 388

Unit Capital Cost SCR + SOFA $/kW 376

Unit Capital Cost ASOFA $/kW 26 26

Unit Capital Cost SCR $/kW 350

Unit Catalyst Cost $/m3

7,500 7,500

Initial Catalyst Volume m

3

440 530

Coal Cost $/MBtu 1.00 1.00

Catalyst Cost $ 3,300,000 3,960,000

Annual Capacity Factor % 86.5 92.3

Cost of Outage $/week 0 3,696,000

Outage Duration weeks 0 4

Catalyst Replacement 24,000 hrs 6 months

Number of Catalyst Layers 3 1

Future Worth Factor 0.31 1

Capital Recovery Factor 0.08718 0.08718

Levelized Annual O&M Factor 1 1.19314

TOTAL CAPITAL COST

SCR + ASOFA Capital Cost $ 170,720,000

SCR Capital Cost $ 164,121,000

SO3 Mitigation Capital Costa

$ 0 0

 Total Installed Capital Cost $ 164,121,000 170,720,000

 Annual Capital Cost $/yr 14,308,069 14,883,370

FIXED O&M COST

Operating Labor Cost $/yr $0 $0

Maintenance Materials Cost $/yr $492,000 $512,000

Maintenance Labor Cost $/yr $328,000 $341,000

Administrative and Support Labor $/yr $0 $0

 Total Fixed O&M Cost $/yr $820,000 $853,000

VARIABLE O&M COST

Ammonia Cost $/yr 1,564,000 2,471,000

Catalyst Cost $/yr 342,000 7,920,000

Power Cost $/yr 2,003,000 2,813,000

Gas Penalty $/yr 2,767,000 11,161,000

Outage Penalty $/yr 0 14,784,000

Sorbent Injection $/yr 0 207,000

 Total Variable O&M Cost $/yr 6,676,000 39,356,000

40,209,000

TOTAL O&M COSTS $/yr 7,496,000 47,974,966

Cost Effectiveness $/ton 2,609 5,977

Sargent & Lundy