COMPARISION OF LNG VAPORIZERS IN PLL

TYPES OF LNG VAPORIZER

Open Rack Vaporizer (ORV)

Direct Forced Draft Ambient Air Vaporizer

Direct Natural draft Ambient Air Vaporizer (AAV)

Ambient Air Heat Exchanger with Heat Transfer Fluid (AAV-

HTF)

Submerged Combustion

Vaporizer (SCV)

TYPES OF LNG VAPORIZERS AROUND THE WORLD

VAPORIZER IN PLL

SHELL AND TUBE VAPORIZER

SUBMERGED COMBUSTION VAPORIZER

E-109

SHELL AND TUBE VAPORIZER

LNG

WARM GW WATER

NG

COLD GW WATER

AIR HEATERS

GW PUMP

SHELL AND TUBE VAPORIZER

SHELL AND TUBE VAPORIZERE-104A/G E-105A/G (Units-14)

SHELL SIDE (ETHYLENE GYLCOL)

TUBE SIDE (LNG)

INLET OUTLET INLET OUTLET

TOTAL FLOW(t/hr) 1187.3 88.175

OPERATING TEMPERTURE (°C)

16 2 -156 0

DESIGN TEMPERATURE(°C)

-165/60 -165/60

OPERATING PRESSURE (barG)

2.5 91.8

DESIGN PRESSURE (barG)

10 130

SUBMERGED COMBUSTION VAPORIZER

• BLOWER• HOT WATER

PUMP

BURNER MODE

• FUEL GAS CONSUMPTION

• BLOWER

COMBINED MODE

• BURNER• COGEN

E-107A/B & E-106A/BUNITS -4

SCV PRINCIPLE

• The SCV system uses natural gas/ hot water from CPP as its heat source and requires electrical power to operate combustion air blowers and circulating water pumps.

• LNG is routed to a stainless steel tube bundle that is submerged in a water bath.

• Transfer of heat takes place from gas water mixture to the tube coil & then to process fluid.

DESIGN CONDITIONS

FUEL GASCONDITIONS

CAPACITYAIR CONDITIONS

PARAMETERS

E-109

LNG

WARM GW WATER

NG

COLD GW WATER

GW PUMPPLATE AND FIN

EXCHANGER

HW

HW

E-109

SHELL SIDE (ETHYLENE GYLCOL)

TUBE SIDE (LNG)

INLET OUTLET INLET OUTLET

TOTAL FLOW(t/hr) 247.3 99.35

OPERATING TEMPERTURE (°C)

90 12 -153.6 0

DESIGN TEMPERATURE(°C)

-165/173 -165/173

OPERATING PRESSURE (barG)

5.14 60

DESIGN PRESSURE (barG)

10 130

PARAMETERS

COST/ENERGY CALCULATIONS OF VAPORIZERS

• REVIEW POWER CONSUMPTION.docx

EQUIPMENT NAME

TOTAL ENERGY CONSUMPTION PER

DAY(Kwh)

OPERATIONAL COST

PER DAY (Rs)

CAPITAL COST(per

vaporizer)

STV (PHASE-1) 12,048 35,023.53 18 cr

STV (PHASE-2) 12,288 35,721.21 20 cr

SCV(COGEN) 10,248 29,790.93

31.25 CrSCV(BURNER)

(Phase-1)7080+ Rs 233,304

253,885.00

E-109 2880 8,372.16

POWER/COST CALCULATIONS

OUTPUT COMPARISIONEQUIPMENTS OUTPUT

FLOWRATE (ton/hr)

PER DAY OUTPUT

FLOWRATE(ton/DAY)

FLOWRATE (MMBTU/DAY)

OUTPUT GAS

PRICE/Day

STV(PHASE-1) 88.175 2116.2 100,519.5 29,854,143

STV(PHASE-2) 88.175 2116.2 100,519.5 29,854,143

SCV(COGEN)(PHASE-1)

100 2400 114,000 33,858,000

SCV(BURNER)(PHASE-1)

100 2400 114,000 33,858,000

E-109 99.35 2384.4 122,550 36,397,350

BREAKEVEN ANALYSIS

STV

24 dayz for breakeven

SCV(cogen)

38 dayz for breakeven

CONCLUSIONVAPORIZATION TECHNOLOGY

TECHNICAL RISKS

ENVIORNMENTAL CONCERS

COSTS (CAPITAL)

COSTS (OPERTING)

OPERABILITY & MAINTENANCE

LAYOUT ISSUES

SUBMERGED COMBUSTION VAPORIZATION ….. .. O O O ….. ..O O O …O O ….O

SHELL AND TUBE VAPORIZTION …O O …O O ..O O O …O O ..O O O …O O

E-109 ..O O O ..O O O …O O ..O O O ..O O O …O O