Spreadsheet: benjamin_rogers__1176__Bernsteins's LM6000 Model
Sheet: SOURCEDATA

SOURCE DATA
TURBINE | 1 | 2 | 3 | 4 | 5 | 6 | 7 | 8 | 9 | 10
 |  |  |  |  |  |  |  |  |  |  |  |  | base $13800, $450Sprint, $62finfan
BOP |  |  |  |  |  |  |  |  |  |  |  |  | unit portion |  | 0.7 | took out HV breakers/switches
 |  |  |  |  |  |  |  |  |  |  |  |  | cost scale factor |  | 0.7
PIPELINE $/MILE | 4 | 10 | 16 | 24
 | 250 | 400 | 600 | 1000
POWER INTERCONNECTION |  | 69 | 138 | 240 | 345 | 500 | 745
 | base cost >> |  |  |  |  |  |  |  |  |  |  |  | base 69 kV - $50-building, $30-UPS/batt, $120-metering,$30-base site/fence
 | per bkr/Dend | 250 | 250 | 350 | 500 | 750 | 1000 |  |  |  |  |  | 138 kV breaker $$50K, 1 switch at $25k@, tubular buss 3 X 50' at $30/ft or $$5k, instrumentation $30k, deadend structure at $100k, construction at $40
 | per breaker> | 150 | 200 | 300 | 400 | 500 | 600 |  |  |  |  |  | assumes 1 breaker per CTG plus 1 breaker as outgoing and one breaker position at far end
 | 1 |  |  |  |  |  |  |  |  |  |  |  | table assumes paired units for ties to grid
 | 2 |  |  |  |  |  |  |  |  |  |  |  | 138 kV breaker $$50K, 1 switch at $25k@, tubular buss 3 X 200' at $30/ft or $$18k, instrumentation $10k, construction at $47
 | 3 |  |  |  |  |  |  |  |  |  |  |  | 230 kV breaker $$70K, 1 switch at $35k@, tubular buss 3 X 200' at $40/ft or $$24k, instrumentation $10k, construction at $60
 | 4
 | 5
 | 6
 | 7
 | 8
 | 9
 | 10
SCR | 1 | 2 | 3 | 4 | 5 | 6 | 7 | 8 | 9 | 10
 | 1000 |  |  |  |  |  |  |  |  |  |  |  | cost scale factor |  | 0.95
DUAL FUEL
 |  |  |  |  |  |  |  |  |  |  |  |  | cost scale factor |  | 0.9 | assume $280/CTG + fuel tank increase + filter - should add centrifuge if long downtimes or poor fuel
UNION PREMIUM | 0.2
BLACK START | 1000
COMPRESSION |  |  |  |  |  |  |  |  |  |  |  |  | suction press. | psig
INCREASE | 100 |  |  |  |  |  |  |  |  |  |  |  | discharge press. | psig | 700
 | 200 |  |  |  |  |  |  |  |  |  |  |  | suction temp. | F | 80
 | 300 | 900 |  |  |  |  |  |  |  |  |  |  | compressor efficiency | % | 0.82
 | 400 |  |  |  |  |  |  |  |  |  |  |  | design gas flow | MMscfd | 10
 | 500 |  |  |  |  |  |  |  |  |  |  |  | gas compressibility
 |  |  |  |  |  |  |  |  |  |  |  |  | compression ratio
 |  |  |  |  |  |  |  |  |  |  |  |  | compression power | kW
 |  |  |  |  |  |  |  |  |  |  |  |  | cost scale factor |  | 0.6
 |  |  |  |  |  |  |  |  |  |  |  |  | compression ratio factor |  | 1.1
DEMIN WATER
 | 600 |  |  |  |  |  |  |  |  |  |  |  | cost scale factor |  | 0.5 | assumes 2X100% based on my catalog data
SPARE PARTS
 | 500 |  |  |  |  |  |  |  |  |  |  |  | cost scale factor |  | 0.7
CHILLERS | 1 | 2 | 3 | 4 | 5 | 6 | 7 | 8 | 9 | 10
 | 1250 |  |  |  |  |  |  |  |  |  |  |  | cost scale factor |  | 0.85 | assumes at three CTG's goes to plant config
DEMIN WATER CONSUMPTION |  | gal/MWhr
 | cost | US$/1000gal | 3.5
 |  | US$/MWhr
RAW WATER CONSUMPTION |  | gal/MWhr
 | cost | US$/1000gal | 1.6
 |  | US$/MWhr
total water consumption |  | US$/MWhr
Estimated CTG accural |  | US$/CTGyr |  | includes gas compression/chillers
Estimated operating hours |  | hr/yr | 1314
Estimated CTG accural |  | US$/CTGhr