HEAT TRANSFER IN BOILER (METRIC)
********************************
FUEL TYPE : GASEOUS
LIQUID : WATER
BOILER TYPE : STEAM
MAXIMUM GAGE PRESSURE: 10 bar
BOILER DESIGN : 3-PASS
BOILER LOAD : 100%
BURNER TYPE : FORCED DRAFT
BOILER MATERIAL : CARBON STEEL
GAS DATA
--------
CH4-CONTENT = 100 vol%
LOWER HEATING VALUE = 35883 kJ/m3
HIGHER HEATING VALUE = 39819 kJ/m3
GAS DENSITY = .716 kg/m3
GAS OVERPRESSURE = 0 mbar
ATMOSPHERIC PRESSURE = 1013 mbar
GAS TEMPERATURE = 0 dC
RELATIVE GAS HUMIDITY= 0 %
BOILER GEOMETRY DATA
--------------------
FURNACE DATA
............
FURNACE IS HORIZONTAL
FURNACE IS CIRCULAR IN GAS FLOW DIRECTION
THERE IS CIRCULAR TURNAROUND CHAMBER AT FURNACE EXIT
NET DIAMETER = 1.05 m
WALL THICKNESS = .02 m
LENGTH IN GAS FLOW DIRECTION = 4.434 m
CROSS-SECTION AT FURNACE EXIT = 2.41 m2
NET DIAMETER OF TURNAROUND CHAMBER= 1.752 m
TURNAROUND CHAMBER LENGTH = .55 m
TURNAROUND CHAMBER COOLED AREA = 4.2572 m2
COOLED AREA OF TUBESHEET = 1.23 m2
FURNACE COOLED AREA = 21.294 m2
BOTTOM COOLED AREA PER.TO GAS FLOW= 2.41 m2
GEOMETRY DATA OF FIRST TUBE ASSEMBLY
....................................
TUBES ARE HORIZONTAL
NUMBER OF TUBES = 119
NET TUBE DIAMETER = .0571 m
WALL THICKNESS = .0029 m
COOLED TUBE LENGTH = 4.43 m
COOLED AREA = 94.566 m2
CROSS-SECTION BEFORE TUBES = 2.41 m2
CROSS-SECTION AFTER TUBES = 2.86 m2
GEOMETRY DATA OF TURNAROUND CHANNEL
...................................
CHANNEL IS HORIZONTAL IN GAS FLOW DIRECTION
SIDE WIDTH = 2.2 m
SIDE HEIGHT = 1.3 m
WALL THICKNESS = .02 m
LENGTH IN GAS FLOW DIRECTION = .5 m
COOLED AREA = 2.55 m2
GEOMETRY DATA OF SECOND TUBE ASSEMBLY
.....................................
TUBES ARE HORIZONTAL
NUMBER OF TUBES = 78
NET TUBE DIAMETER = .0571 m
WALL THICKNESS = .0029 m
COOLED TUBE LENGTH = 5.2 m
COOLED AREA = 72.759 m2
CROSS-SECTION BEFORE TUBES = 2.86 m2
CROSS-SECTION AFTER TUBES = 1.4 m2
GEOMETRY DATA OF CHANNEL AT BOILER EXIT
.......................................
CHANNEL IS HORIZONTAL IN GAS FLOW DIRECTION
SIDE WIDTH = 2 m
SIDE HEIGHT = .7 m
WALL THICKNESS = .02 m
LENGTH IN GAS FLOW DIRECTION = .5 m
COOLED AREA = 1.34 m2
OTHER DATA
----------
GAS RATE = 500 m3/h
COMBUSTION AIR TEMPERATURE = 0 dC
FEED LIQUID TEMPERATURE = 105 dC
LAMBDA VALUE = 1.1 -
STACK CONNECTOR IS CIRCULAR
INNER DIAMETER OF STACK CONNECTOR = .5 [m]
TOTAL COOLED AREA = 192.508 m2
TUBES/FURNACE AREA RATIO = 7.86
CALCULATION RESULTS
-------------------
ADIABATIC COMBUSTION TEMPERATURE = 1895.4 dC
RELEASED HEAT BY COMBUSTION = 4983.8 kW
CONDENSATE HEAT IN FLUE GAS = 528.2 kW
TEMPERATURE OF LIQUID/STEAM IN BOILER = 179.9 dC
GAS VELOCITY IN BOILER FLUE APERTURE = 14.5 m/s
GAS SIDE PRESSURE DROP IN BOILER = 6.261 mbar
QUANTITY OF FLUE GAS RELEASED = 5738.1 m3/h
BOILER THERMAL OUTPUT = 4482.7 kW
QUANTITY OF STEAM GENERATED = 6909.1 kg/h
FEED LIQUID RATE = 7238.9 l/h
AVERAGE AREA THERMAL LOAD = 23.3 kW/m2
PERCENTAGE OF HEAT TAKEN UP IN FURNACE = 57.9 %
GAS EXIT TEMPERATURE FROM BOILER = 215.5 dC
EFFICIENCY (BASED ON LOWER FUEL HEATING VALUE - DIN METHOD)
BOILER EFFICIENCY = 89.9 %
COMBUSTION (STACK) EFFICIENCY = 90.4 %
FLUE GAS LOSSES = 9.6 %
BOILER JACKET LOSSES (AS SET BY DIN 4702 T3) = .5 %
BOILER JACKET LOSSES (AS SET BY DIN 4702 T3) = 24.9 kW
HEAT TRANSFER IN FURNACE
........................
STEAM GENERATED = 4000.5 kg/h
GAS EXIT TEMP. = 975.7 dC
MEAN GAS TEMP. = 1377.3 dC
AREA THERMAL LOAD = 121.9 kW/m2
VOLUME THERMAL LOAD = 960 kW/m3
GAS VELOCITY = 9.8 m/s
RADIATION = 1723.1 kW
CONVECTION = 872.4 kW
HEAT TRANSFERRED = 2595.6 kW
WALL TEMP. ON GAS SIDE = 259.1 dC
WALL TEMP. ON LIQUID SIDE= 189.4 dC
GAS SIDE PRESSURE DROP = .268 mbar
HEAT TRANSFER ON REAR WALL = 799 kW
HEAT TRANSFER ON CIRCULAR PART = 1796.5 kW
WALL TEMP. OF CIRCULAR PART = 234.7 dC
TEMPERATURE OF REAR WALL = 321.7 dC
HEAT TRANSFER IN FIRST TUBE ASSEMBLY
....................................
STEAM GENERATED = 2499.1 kg/h
GAS EXIT TEMP. = 331.3 dC
MEAN GAS TEMP. = 568.3 dC
AREA THERMAL LOAD = 17.1 kW/m2
GAS VELOCITY = 16.1 m/s
RADIATION = 225.7 kW
CONVECTION = 1395.7 kW
HEAT TRANSFERRED = 1621.4 kW
WALL TEMP. ON GAS SIDE = 184.3 dC
WALL TEMP. ON LIQUID SIDE= 183.3 dC
GAS SIDE PRESSURE DROP = 2.264 mbar
HEAT TRANSFER IN TURNAROUND CHANNEL
...................................
STEAM GENERATED = 6.1 kg/h
GAS EXIT TEMP. = 329.7 dC
MEAN GAS TEMP. = 330.5 dC
AREA THERMAL LOAD = 1.5 kW/m2
GAS VELOCITY = 1.2 m/s
RADIATION = 4 kW
CONVECTION = 0 kW
HEAT TRANSFERRED = 4 kW
WALL TEMP. ON GAS SIDE = 182.3 dC
WALL TEMP. ON LIQUID SIDE= 181.7 dC
GAS SIDE PRESSURE DROP = .006 mbar
HEAT TRANSFER IN SECOND TUBE ASSEMBLY
.....................................
STEAM GENERATED = 402.1 kg/h
GAS EXIT TEMP. = 215.8 dC
MEAN GAS TEMP. = 259.7 dC
AREA THERMAL LOAD = 3.6 kW/m2
GAS VELOCITY = 15.6 m/s
RADIATION = 11.8 kW
CONVECTION = 249 kW
HEAT TRANSFERRED = 260.9 kW
WALL TEMP. ON GAS SIDE = 182.2 dC
WALL TEMP. ON LIQUID SIDE= 182 dC
GAS SIDE PRESSURE DROP = 3.488 mbar
HEAT TRANSFER IN CHANNEL AT BOILER EXIT
.......................................
STEAM GENERATED = 1.3 kg/h
GAS EXIT TEMP. = 215.5 dC
MEAN GAS TEMP. = 215.6 dC
AREA THERMAL LOAD = .7 kW/m2
GAS VELOCITY = 2 m/s
RADIATION = .3 kW
CONVECTION = .6 kW
HEAT TRANSFERRED = .9 kW
WALL TEMP. ON GAS SIDE = 181.6 dC
WALL TEMP. ON LIQUID SIDE= 181.3 dC
GAS SIDE PRESSURE DROP = .235 mbar
********************************
FUEL TYPE : GASEOUS
LIQUID : WATER
BOILER TYPE : STEAM
MAXIMUM GAGE PRESSURE: 10 bar
BOILER DESIGN : 3-PASS
BOILER LOAD : 100%
BURNER TYPE : FORCED DRAFT
BOILER MATERIAL : CARBON STEEL
GAS DATA
--------
CH4-CONTENT = 100 vol%
LOWER HEATING VALUE = 35883 kJ/m3
HIGHER HEATING VALUE = 39819 kJ/m3
GAS DENSITY = .716 kg/m3
GAS OVERPRESSURE = 0 mbar
ATMOSPHERIC PRESSURE = 1013 mbar
GAS TEMPERATURE = 0 dC
RELATIVE GAS HUMIDITY= 0 %
BOILER GEOMETRY DATA
--------------------
FURNACE DATA
............
FURNACE IS HORIZONTAL
FURNACE IS CIRCULAR IN GAS FLOW DIRECTION
THERE IS CIRCULAR TURNAROUND CHAMBER AT FURNACE EXIT
NET DIAMETER = 1.05 m
WALL THICKNESS = .02 m
LENGTH IN GAS FLOW DIRECTION = 4.434 m
CROSS-SECTION AT FURNACE EXIT = 2.41 m2
NET DIAMETER OF TURNAROUND CHAMBER= 1.752 m
TURNAROUND CHAMBER LENGTH = .55 m
TURNAROUND CHAMBER COOLED AREA = 4.2572 m2
COOLED AREA OF TUBESHEET = 1.23 m2
FURNACE COOLED AREA = 21.294 m2
BOTTOM COOLED AREA PER.TO GAS FLOW= 2.41 m2
GEOMETRY DATA OF FIRST TUBE ASSEMBLY
....................................
TUBES ARE HORIZONTAL
NUMBER OF TUBES = 119
NET TUBE DIAMETER = .0571 m
WALL THICKNESS = .0029 m
COOLED TUBE LENGTH = 4.43 m
COOLED AREA = 94.566 m2
CROSS-SECTION BEFORE TUBES = 2.41 m2
CROSS-SECTION AFTER TUBES = 2.86 m2
GEOMETRY DATA OF TURNAROUND CHANNEL
...................................
CHANNEL IS HORIZONTAL IN GAS FLOW DIRECTION
SIDE WIDTH = 2.2 m
SIDE HEIGHT = 1.3 m
WALL THICKNESS = .02 m
LENGTH IN GAS FLOW DIRECTION = .5 m
COOLED AREA = 2.55 m2
GEOMETRY DATA OF SECOND TUBE ASSEMBLY
.....................................
TUBES ARE HORIZONTAL
NUMBER OF TUBES = 78
NET TUBE DIAMETER = .0571 m
WALL THICKNESS = .0029 m
COOLED TUBE LENGTH = 5.2 m
COOLED AREA = 72.759 m2
CROSS-SECTION BEFORE TUBES = 2.86 m2
CROSS-SECTION AFTER TUBES = 1.4 m2
GEOMETRY DATA OF CHANNEL AT BOILER EXIT
.......................................
CHANNEL IS HORIZONTAL IN GAS FLOW DIRECTION
SIDE WIDTH = 2 m
SIDE HEIGHT = .7 m
WALL THICKNESS = .02 m
LENGTH IN GAS FLOW DIRECTION = .5 m
COOLED AREA = 1.34 m2
OTHER DATA
----------
GAS RATE = 500 m3/h
COMBUSTION AIR TEMPERATURE = 0 dC
FEED LIQUID TEMPERATURE = 105 dC
LAMBDA VALUE = 1.1 -
STACK CONNECTOR IS CIRCULAR
INNER DIAMETER OF STACK CONNECTOR = .5 [m]
TOTAL COOLED AREA = 192.508 m2
TUBES/FURNACE AREA RATIO = 7.86
CALCULATION RESULTS
-------------------
ADIABATIC COMBUSTION TEMPERATURE = 1895.4 dC
RELEASED HEAT BY COMBUSTION = 4983.8 kW
CONDENSATE HEAT IN FLUE GAS = 528.2 kW
TEMPERATURE OF LIQUID/STEAM IN BOILER = 179.9 dC
GAS VELOCITY IN BOILER FLUE APERTURE = 14.5 m/s
GAS SIDE PRESSURE DROP IN BOILER = 6.261 mbar
QUANTITY OF FLUE GAS RELEASED = 5738.1 m3/h
BOILER THERMAL OUTPUT = 4482.7 kW
QUANTITY OF STEAM GENERATED = 6909.1 kg/h
FEED LIQUID RATE = 7238.9 l/h
AVERAGE AREA THERMAL LOAD = 23.3 kW/m2
PERCENTAGE OF HEAT TAKEN UP IN FURNACE = 57.9 %
GAS EXIT TEMPERATURE FROM BOILER = 215.5 dC
EFFICIENCY (BASED ON LOWER FUEL HEATING VALUE - DIN METHOD)
BOILER EFFICIENCY = 89.9 %
COMBUSTION (STACK) EFFICIENCY = 90.4 %
FLUE GAS LOSSES = 9.6 %
BOILER JACKET LOSSES (AS SET BY DIN 4702 T3) = .5 %
BOILER JACKET LOSSES (AS SET BY DIN 4702 T3) = 24.9 kW
HEAT TRANSFER IN FURNACE
........................
STEAM GENERATED = 4000.5 kg/h
GAS EXIT TEMP. = 975.7 dC
MEAN GAS TEMP. = 1377.3 dC
AREA THERMAL LOAD = 121.9 kW/m2
VOLUME THERMAL LOAD = 960 kW/m3
GAS VELOCITY = 9.8 m/s
RADIATION = 1723.1 kW
CONVECTION = 872.4 kW
HEAT TRANSFERRED = 2595.6 kW
WALL TEMP. ON GAS SIDE = 259.1 dC
WALL TEMP. ON LIQUID SIDE= 189.4 dC
GAS SIDE PRESSURE DROP = .268 mbar
HEAT TRANSFER ON REAR WALL = 799 kW
HEAT TRANSFER ON CIRCULAR PART = 1796.5 kW
WALL TEMP. OF CIRCULAR PART = 234.7 dC
TEMPERATURE OF REAR WALL = 321.7 dC
HEAT TRANSFER IN FIRST TUBE ASSEMBLY
....................................
STEAM GENERATED = 2499.1 kg/h
GAS EXIT TEMP. = 331.3 dC
MEAN GAS TEMP. = 568.3 dC
AREA THERMAL LOAD = 17.1 kW/m2
GAS VELOCITY = 16.1 m/s
RADIATION = 225.7 kW
CONVECTION = 1395.7 kW
HEAT TRANSFERRED = 1621.4 kW
WALL TEMP. ON GAS SIDE = 184.3 dC
WALL TEMP. ON LIQUID SIDE= 183.3 dC
GAS SIDE PRESSURE DROP = 2.264 mbar
HEAT TRANSFER IN TURNAROUND CHANNEL
...................................
STEAM GENERATED = 6.1 kg/h
GAS EXIT TEMP. = 329.7 dC
MEAN GAS TEMP. = 330.5 dC
AREA THERMAL LOAD = 1.5 kW/m2
GAS VELOCITY = 1.2 m/s
RADIATION = 4 kW
CONVECTION = 0 kW
HEAT TRANSFERRED = 4 kW
WALL TEMP. ON GAS SIDE = 182.3 dC
WALL TEMP. ON LIQUID SIDE= 181.7 dC
GAS SIDE PRESSURE DROP = .006 mbar
HEAT TRANSFER IN SECOND TUBE ASSEMBLY
.....................................
STEAM GENERATED = 402.1 kg/h
GAS EXIT TEMP. = 215.8 dC
MEAN GAS TEMP. = 259.7 dC
AREA THERMAL LOAD = 3.6 kW/m2
GAS VELOCITY = 15.6 m/s
RADIATION = 11.8 kW
CONVECTION = 249 kW
HEAT TRANSFERRED = 260.9 kW
WALL TEMP. ON GAS SIDE = 182.2 dC
WALL TEMP. ON LIQUID SIDE= 182 dC
GAS SIDE PRESSURE DROP = 3.488 mbar
HEAT TRANSFER IN CHANNEL AT BOILER EXIT
.......................................
STEAM GENERATED = 1.3 kg/h
GAS EXIT TEMP. = 215.5 dC
MEAN GAS TEMP. = 215.6 dC
AREA THERMAL LOAD = .7 kW/m2
GAS VELOCITY = 2 m/s
RADIATION = .3 kW
CONVECTION = .6 kW
HEAT TRANSFERRED = .9 kW
WALL TEMP. ON GAS SIDE = 181.6 dC
WALL TEMP. ON LIQUID SIDE= 181.3 dC
GAS SIDE PRESSURE DROP = .235 mbar
| BOILER DESIGN SOFTWARE FOR FIRE-TUBE BOILERS |
| HEAT TRANSFER CALCULATION EXAMPLES |
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HEAT TRANSFER IN BOILER (ENGLISH UNITS)
***************************************
FUEL TYPE : GASEOUS
LIQUID : WATER
BOILER TYPE : STEAM
MAXIMUM GAGE PRESSURE: 145 p.s.i.
BOILER DESIGN : 3-PASS
BOILER LOAD : 100%
BURNER TYPE : FORCED DRAFT
BOILER MATERIAL : CARBON STEEL
GAS DATA
--------
CH4-CONTENT = 100 vol%
LOWER HEATING VALUE = 963.1 BTU/cu.ft.
HIGHER HEATING VALUE = 1068.8 BTU/cu.ft.
GAS DENSITY = .04 lb./cu.ft.
GAS OVERPRESSURE = 0 psi
ATMOSPHERIC PRESSURE = 14.7 psi
GAS TEMPERATURE = 32 dF
RELATIVE GAS HUMIDITY= 0 %
BOILER GEOMETRY DATA
--------------------
FURNACE DATA
............
FURNACE IS HORIZONTAL
FURNACE IS CIRCULAR IN GAS FLOW DIRECTION
THERE IS CIRCULAR TURNAROUND CHAMBER AT FURNACE EXIT
NET DIAMETER = 41.339 in.
WALL THICKNESS = .787 in.
LENGTH IN GAS FLOW DIRECTION = 174.567 in.
CROSS-SECTION AT FURNACE EXIT = 25.941 sq.ft.
NET DIAMETER OF TURNAROUND CHAMBER= 1.752 m
TURNAROUND CHAMBER LENGTH = 21.654 in.
TURNAROUND CHAMBER COOLED AREA = 45.825 sq.ft.
COOLED AREA OF TUBESHEET = 13.24 sq.ft.
FURNACE COOLED AREA = 229.202 sq.ft.
BOTTOM COOLED AREA PER.TO GAS FLOW= 25.941 sq.ft.
GEOMETRY DATA OF FIRST TUBE ASSEMBLY
....................................
TUBES ARE HORIZONTAL
NUMBER OF TUBES = 119
NET TUBE DIAMETER = 2.248 in.
WALL THICKNESS = .114 in.
COOLED TUBE LENGTH = 174.409 in.
COOLED AREA = 1017.904 sq.ft.
CROSS-SECTION BEFORE TUBES = 25.941 sq.ft.
CROSS-SECTION AFTER TUBES = 30.785 sq.ft.
GEOMETRY DATA OF TURNAROUND CHANNEL
...................................
CHANNEL IS HORIZONTAL IN GAS FLOW DIRECTION
SIDE WIDTH = 86.614 in.
SIDE HEIGHT = 51.181 in.
WALL THICKNESS = .787 in.
LENGTH IN GAS FLOW DIRECTION = 19.685 in.
COOLED AREA = 27.448 sq.ft.
GEOMETRY DATA OF SECOND TUBE ASSEMBLY
.....................................
TUBES ARE HORIZONTAL
NUMBER OF TUBES = 78
NET TUBE DIAMETER = 2.248 in.
WALL THICKNESS = .114 in.
COOLED TUBE LENGTH = 204.724 in.
COOLED AREA = 783.166 sq.ft.
CROSS-SECTION BEFORE TUBES = 30.785 sq.ft.
CROSS-SECTION AFTER TUBES = 15.069 sq.ft.
GEOMETRY DATA OF CHANNEL AT BOILER EXIT
.......................................
CHANNEL IS HORIZONTAL IN GAS FLOW DIRECTION
SIDE WIDTH = 78.74 in.
SIDE HEIGHT = 27.559 in.
WALL THICKNESS = .787 in.
LENGTH IN GAS FLOW DIRECTION = 19.685 in.
COOLED AREA = 14.424 sq.ft.
OTHER DATA
----------
GAS RATE = 17657.3 cu.ft./h
COMBUSTION AIR TEMPERATURE = 32 dF
FEED LIQUID TEMPERATURE = 221 dF
LAMBDA VALUE = 1.1 -
STACK CONNECTOR IS CIRCULAR
INNER DIAMETER OF STACK CONNECTOR = .5 [in.]
TOTAL COOLED AREA = 2072.144 sq.ft.
TUBES/FURNACE AREA RATIO = 7.86
CALCULATION RESULTS
-------------------
ADIABATIC COMBUSTION TEMPERATURE = 3443.8 dF
RELEASED HEAT BY COMBUSTION = 508.4 HP
CONDENSATE HEAT IN FLUE GAS = 53.9 HP
TEMPERATURE OF LIQUID/STEAM IN BOILER = 355.8 dF
GAS VELOCITY IN BOILER FLUE APERTURE = 47.652 ft./s
GAS SIDE PRESSURE DROP IN BOILER = 2.5 in.W.C.
QUANTITY OF FLUE GAS RELEASED = 202638.9 cu.ft./h
BOILER THERMAL OUTPUT = 457.3 HP
QUANTITY OF STEAM GENERATED IN BOILER = 15232.1 lb./h
FEED LIQUID RATE = 1912.327 gal./h
AVERAGE HEAT TRANSFER INTENSITY = 4.53 sq.ft/HP
PERCENTAGE OF HEAT TAKEN UP IN FURNACE = 57.9 %
GAS EXIT TEMPERATURE FROM BOILER = 419.8 dF
EFFICIENCY (BASED ON HIGHER FUEL HEATING VALUE - ASME METHOD)
BOILER EFFICIENCY = 81.1 %
COMBUSTION (STACK) EFFICIENCY = 81.5 %
FUEL TO STEAM EFFICIENCY = 81.1 %
FLUE GAS LOSSES (LATENT HEAT INCLUDED) = 18.5 %
BOILER JACKET LOSSES (AS SET BY REGULATIONS) = .5 %
BOILER JACKET LOSSES (AS SET BY REGULATIONS) = 2.5 HP
HEAT TRANSFER IN FURNACE
........................
STEAM GENERATED = 8819.7 lb./h
GAS EXIT TEMP. = 1788.3 dF
MEAN GAS TEMP. = 2511.1 dF
HEAT TRANSFER INTENSITY = .87 sq.ft./HP
VOLUME THERMAL LOAD = 2.74 HP/cu.ft.
GAS VELOCITY = 32.065 ft./s
RADIATION = 175.8 HP
CONVECTION = 89 HP
HEAT TRANSFERRED = 264.8 HP
WALL TEMP. ON GAS SIDE = 498.4 dF
WALL TEMP. ON LIQUID SIDE= 373 dF
GAS SIDE PRESSURE DROP = .11 in.W.C.
HEAT TRANSFER ON REAR WALL = 81.5 HP
HEAT TRANSFER ON CIRCULAR PART = 183.3 HP
WALL TEMP. OF CIRCULAR PART = 454.4 dF
TEMPERATURE OF REAR WALL = 611.1 dF
HEAT TRANSFER IN FIRST TUBE ASSEMBLY
....................................
STEAM GENERATED = 5509.6 lb./h
GAS EXIT TEMP. = 628.4 dF
MEAN GAS TEMP. = 1054.9 dF
HEAT TRANSFER INTENSITY = 6.15 sq.ft./HP
GAS VELOCITY = 52.882 ft./s
RADIATION = 23 HP
CONVECTION = 142.4 HP
HEAT TRANSFERRED = 165.4 HP
WALL TEMP. ON GAS SIDE = 363.7 dF
WALL TEMP. ON LIQUID SIDE = 362 dF
GAS SIDE PRESSURE DROP = .91 in.W.C.
HEAT TRANSFER IN TURNAROUND CHANNEL
...................................
STEAM GENERATED = 13.4 lb./h
GAS EXIT TEMP. = 625.5 dF
MEAN GAS TEMP. = 626.9 dF
HEAT TRANSFER INTENSITY = 68.09 sq.ft./HP
GAS VELOCITY = 4.042 ft./s
RADIATION = .4 HP
CONVECTION = 0 HP
HEAT TRANSFERRED = .4 HP
WALL TEMP. ON GAS SIDE = 360.2 dF
WALL TEMP. ON LIQUID SIDE= 359.1 dF
GAS SIDE PRESSURE DROP = 0 in.W.C.
HEAT TRANSFER IN SECOND TUBE ASSEMBLY
.....................................
STEAM GENERATED = 886.4 lb./h
GAS EXIT TEMP. = 420.5 dF
MEAN GAS TEMP. = 499.4 dF
HEAT TRANSFER INTENSITY = 29.43 sq.ft./HP
GAS VELOCITY = 51.085 ft./s
RADIATION = 1.2 HP
CONVECTION = 25.4 HP
HEAT TRANSFERRED = 26.6 HP
WALL TEMP. ON GAS SIDE = 360 dF
WALL TEMP. ON LIQUID SIDE= 359.6 dF
GAS SIDE PRESSURE DROP = 1.4 in.W.C.
HEAT TRANSFER IN CHANNEL AT BOILER EXIT
.......................................
STEAM GENERATED = 3 lb./h
GAS EXIT TEMP. = 419.8 dF
MEAN GAS TEMP. = 420.2 dF
HEAT TRANSFER INTENSITY = 162.08 sq.ft./HP
GAS VELOCITY = 6.686 ft./s
RADIATION = .03 HP
CONVECTION = .06 HP
HEAT TRANSFERRED = .09 HP
WALL TEMP. ON GAS SIDE = 358.8 dF
WALL TEMP. ON LIQUID SIDE= 358.3 dF
GAS SIDE PRESSURE DROP = .094 in.W.C.
***************************************
FUEL TYPE : GASEOUS
LIQUID : WATER
BOILER TYPE : STEAM
MAXIMUM GAGE PRESSURE: 145 p.s.i.
BOILER DESIGN : 3-PASS
BOILER LOAD : 100%
BURNER TYPE : FORCED DRAFT
BOILER MATERIAL : CARBON STEEL
GAS DATA
--------
CH4-CONTENT = 100 vol%
LOWER HEATING VALUE = 963.1 BTU/cu.ft.
HIGHER HEATING VALUE = 1068.8 BTU/cu.ft.
GAS DENSITY = .04 lb./cu.ft.
GAS OVERPRESSURE = 0 psi
ATMOSPHERIC PRESSURE = 14.7 psi
GAS TEMPERATURE = 32 dF
RELATIVE GAS HUMIDITY= 0 %
BOILER GEOMETRY DATA
--------------------
FURNACE DATA
............
FURNACE IS HORIZONTAL
FURNACE IS CIRCULAR IN GAS FLOW DIRECTION
THERE IS CIRCULAR TURNAROUND CHAMBER AT FURNACE EXIT
NET DIAMETER = 41.339 in.
WALL THICKNESS = .787 in.
LENGTH IN GAS FLOW DIRECTION = 174.567 in.
CROSS-SECTION AT FURNACE EXIT = 25.941 sq.ft.
NET DIAMETER OF TURNAROUND CHAMBER= 1.752 m
TURNAROUND CHAMBER LENGTH = 21.654 in.
TURNAROUND CHAMBER COOLED AREA = 45.825 sq.ft.
COOLED AREA OF TUBESHEET = 13.24 sq.ft.
FURNACE COOLED AREA = 229.202 sq.ft.
BOTTOM COOLED AREA PER.TO GAS FLOW= 25.941 sq.ft.
GEOMETRY DATA OF FIRST TUBE ASSEMBLY
....................................
TUBES ARE HORIZONTAL
NUMBER OF TUBES = 119
NET TUBE DIAMETER = 2.248 in.
WALL THICKNESS = .114 in.
COOLED TUBE LENGTH = 174.409 in.
COOLED AREA = 1017.904 sq.ft.
CROSS-SECTION BEFORE TUBES = 25.941 sq.ft.
CROSS-SECTION AFTER TUBES = 30.785 sq.ft.
GEOMETRY DATA OF TURNAROUND CHANNEL
...................................
CHANNEL IS HORIZONTAL IN GAS FLOW DIRECTION
SIDE WIDTH = 86.614 in.
SIDE HEIGHT = 51.181 in.
WALL THICKNESS = .787 in.
LENGTH IN GAS FLOW DIRECTION = 19.685 in.
COOLED AREA = 27.448 sq.ft.
GEOMETRY DATA OF SECOND TUBE ASSEMBLY
.....................................
TUBES ARE HORIZONTAL
NUMBER OF TUBES = 78
NET TUBE DIAMETER = 2.248 in.
WALL THICKNESS = .114 in.
COOLED TUBE LENGTH = 204.724 in.
COOLED AREA = 783.166 sq.ft.
CROSS-SECTION BEFORE TUBES = 30.785 sq.ft.
CROSS-SECTION AFTER TUBES = 15.069 sq.ft.
GEOMETRY DATA OF CHANNEL AT BOILER EXIT
.......................................
CHANNEL IS HORIZONTAL IN GAS FLOW DIRECTION
SIDE WIDTH = 78.74 in.
SIDE HEIGHT = 27.559 in.
WALL THICKNESS = .787 in.
LENGTH IN GAS FLOW DIRECTION = 19.685 in.
COOLED AREA = 14.424 sq.ft.
OTHER DATA
----------
GAS RATE = 17657.3 cu.ft./h
COMBUSTION AIR TEMPERATURE = 32 dF
FEED LIQUID TEMPERATURE = 221 dF
LAMBDA VALUE = 1.1 -
STACK CONNECTOR IS CIRCULAR
INNER DIAMETER OF STACK CONNECTOR = .5 [in.]
TOTAL COOLED AREA = 2072.144 sq.ft.
TUBES/FURNACE AREA RATIO = 7.86
CALCULATION RESULTS
-------------------
ADIABATIC COMBUSTION TEMPERATURE = 3443.8 dF
RELEASED HEAT BY COMBUSTION = 508.4 HP
CONDENSATE HEAT IN FLUE GAS = 53.9 HP
TEMPERATURE OF LIQUID/STEAM IN BOILER = 355.8 dF
GAS VELOCITY IN BOILER FLUE APERTURE = 47.652 ft./s
GAS SIDE PRESSURE DROP IN BOILER = 2.5 in.W.C.
QUANTITY OF FLUE GAS RELEASED = 202638.9 cu.ft./h
BOILER THERMAL OUTPUT = 457.3 HP
QUANTITY OF STEAM GENERATED IN BOILER = 15232.1 lb./h
FEED LIQUID RATE = 1912.327 gal./h
AVERAGE HEAT TRANSFER INTENSITY = 4.53 sq.ft/HP
PERCENTAGE OF HEAT TAKEN UP IN FURNACE = 57.9 %
GAS EXIT TEMPERATURE FROM BOILER = 419.8 dF
EFFICIENCY (BASED ON HIGHER FUEL HEATING VALUE - ASME METHOD)
BOILER EFFICIENCY = 81.1 %
COMBUSTION (STACK) EFFICIENCY = 81.5 %
FUEL TO STEAM EFFICIENCY = 81.1 %
FLUE GAS LOSSES (LATENT HEAT INCLUDED) = 18.5 %
BOILER JACKET LOSSES (AS SET BY REGULATIONS) = .5 %
BOILER JACKET LOSSES (AS SET BY REGULATIONS) = 2.5 HP
HEAT TRANSFER IN FURNACE
........................
STEAM GENERATED = 8819.7 lb./h
GAS EXIT TEMP. = 1788.3 dF
MEAN GAS TEMP. = 2511.1 dF
HEAT TRANSFER INTENSITY = .87 sq.ft./HP
VOLUME THERMAL LOAD = 2.74 HP/cu.ft.
GAS VELOCITY = 32.065 ft./s
RADIATION = 175.8 HP
CONVECTION = 89 HP
HEAT TRANSFERRED = 264.8 HP
WALL TEMP. ON GAS SIDE = 498.4 dF
WALL TEMP. ON LIQUID SIDE= 373 dF
GAS SIDE PRESSURE DROP = .11 in.W.C.
HEAT TRANSFER ON REAR WALL = 81.5 HP
HEAT TRANSFER ON CIRCULAR PART = 183.3 HP
WALL TEMP. OF CIRCULAR PART = 454.4 dF
TEMPERATURE OF REAR WALL = 611.1 dF
HEAT TRANSFER IN FIRST TUBE ASSEMBLY
....................................
STEAM GENERATED = 5509.6 lb./h
GAS EXIT TEMP. = 628.4 dF
MEAN GAS TEMP. = 1054.9 dF
HEAT TRANSFER INTENSITY = 6.15 sq.ft./HP
GAS VELOCITY = 52.882 ft./s
RADIATION = 23 HP
CONVECTION = 142.4 HP
HEAT TRANSFERRED = 165.4 HP
WALL TEMP. ON GAS SIDE = 363.7 dF
WALL TEMP. ON LIQUID SIDE = 362 dF
GAS SIDE PRESSURE DROP = .91 in.W.C.
HEAT TRANSFER IN TURNAROUND CHANNEL
...................................
STEAM GENERATED = 13.4 lb./h
GAS EXIT TEMP. = 625.5 dF
MEAN GAS TEMP. = 626.9 dF
HEAT TRANSFER INTENSITY = 68.09 sq.ft./HP
GAS VELOCITY = 4.042 ft./s
RADIATION = .4 HP
CONVECTION = 0 HP
HEAT TRANSFERRED = .4 HP
WALL TEMP. ON GAS SIDE = 360.2 dF
WALL TEMP. ON LIQUID SIDE= 359.1 dF
GAS SIDE PRESSURE DROP = 0 in.W.C.
HEAT TRANSFER IN SECOND TUBE ASSEMBLY
.....................................
STEAM GENERATED = 886.4 lb./h
GAS EXIT TEMP. = 420.5 dF
MEAN GAS TEMP. = 499.4 dF
HEAT TRANSFER INTENSITY = 29.43 sq.ft./HP
GAS VELOCITY = 51.085 ft./s
RADIATION = 1.2 HP
CONVECTION = 25.4 HP
HEAT TRANSFERRED = 26.6 HP
WALL TEMP. ON GAS SIDE = 360 dF
WALL TEMP. ON LIQUID SIDE= 359.6 dF
GAS SIDE PRESSURE DROP = 1.4 in.W.C.
HEAT TRANSFER IN CHANNEL AT BOILER EXIT
.......................................
STEAM GENERATED = 3 lb./h
GAS EXIT TEMP. = 419.8 dF
MEAN GAS TEMP. = 420.2 dF
HEAT TRANSFER INTENSITY = 162.08 sq.ft./HP
GAS VELOCITY = 6.686 ft./s
RADIATION = .03 HP
CONVECTION = .06 HP
HEAT TRANSFERRED = .09 HP
WALL TEMP. ON GAS SIDE = 358.8 dF
WALL TEMP. ON LIQUID SIDE= 358.3 dF
GAS SIDE PRESSURE DROP = .094 in.W.C.
| 2-PASS WET BACK REVERSE FLUE STEAM BOILER |
| HEAT TRANSFER IN BOILER (METRIC) ******************************** FUEL TYPE : GASEOUS LIQUID : WATER BOILER TYPE : STEAM MAXIMUM GAGE PRESSURE: 10 bar BOILER DESIGN : 2-PASS BOILER LOAD : 100% BURNER TYPE : FORCED DRAFT BOILER MATERIAL : CARBON STEEL GAS DATA -------- CH4-CONTENT = 100 vol% LOWER HEATING VALUE = 34014.1 kJ/m3 HIGHER HEATING VALUE = 37745.1 kJ/m3 GAS DENSITY = .678 kg/m3 GAS OVERPRESSURE = 0 mbar ATMOSPHERIC PRESSURE = 1013 mbar GAS TEMPERATURE = 15 dC RELATIVE GAS HUMIDITY= 0 % BOILER GEOMETRY DATA -------------------- FURNACE DATA ............ FURNACE IS HORIZONTAL FURNACE IS CIRCULAR IN GAS FLOW DIRECTION FURNACE IS REVERSING NET DIAMETER = 1.333 m WALL THICKNESS = .018 m LENGTH IN GAS FLOW DIRECTION = 3.581 m CROSS-SECTION AT FURNACE EXIT = 2.6 m2 FURNACE COOLED AREA = 17.696 m2 BOTTOM COOLED AREA PER.TO GAS FLOW= 1.4 m2 COOLED AREA OF TUBESHEET = 1.3 m2 DISTANCE TO TUBESHEET FROM DOOR = .4 m GEOMETRY DATA OF TUBE ASSEMBLY AFTER FURNACE ............................................ TUBES ARE HORIZONTAL THERE ARE COILED WIRE TURBULATORS IN TUBES TURBULATOR LENGTH = 100% TUBE LENGTH TURBULATOR DIAMETER= .065 m WIRE DIAMETER = .008 m NUMBER OF TUBES = 120 NET TUBE DIAMETER = .07 m WALL THICKNESS = .0032 m COOLED TUBE LENGTH = 4.039 m COOLED AREA = 106.587 m2 CROSS-SECTION BEFORE TUBES = 2.6 m2 CROSS-SECTION AFTER TUBES = 2.6 m2 GEOMETRY DATA OF CHANNEL AT BOILER EXIT ....................................... CHANNEL IS HORIZONTAL IN GAS FLOW DIRECTION CHANNEL IS CIRCULAR IN GAS FLOW DIRECTION NET DIAMETER = 2.6 m WALL THICKNESS = .018 m LENGTH IN GAS FLOW DIRECTION = .4 m COOLED AREA = 2.4 m2 OTHER DATA ---------- GAS RATE = 480 m3/h COMBUSTION AIR TEMPERATURE = 15 dC FEED LIQUID TEMPERATURE = 105 dC LAMBDA VALUE = 1.1 - STACK CONNECTOR IS CIRCULAR INNER DIAMETER OF STACK CONNECTOR= .5 [m] TOTAL COOLED AREA = 126.683 m2 TUBES/FURNACE AREA RATIO = 6.02 CALCULATION RESULTS ------------------- ADIABATIC COMBUSTION TEMPERATURE = 1806.9 dC RELEASED HEAT BY COMBUSTION = 4562.4 kW CONDENSATE HEAT IN FLUE GAS = 507.1 kW TEMPERATURE OF LIQUID/STEAM IN BOILER = 179.9 dC GAS VELOCITY IN BOILER FLUE APERTURE = 14.9 m/s GAS SIDE PRESSURE DROP IN BOILER = 3.466 mbar QUANTITY OF FLUE GAS RELEASED = 5508.6 m3/h BOILER THERMAL OUTPUT = 3979 kW QUANTITY OF STEAM GENERATED = 6132.8 kg/h FEED LIQUID RATE = 6425.5 l/h AVERAGE AREA THERMAL LOAD = 31.4 kW/m2 PERCENTAGE OF HEAT TAKEN UP IN FURNACE = 54.8 % GAS EXIT TEMPERATURE FROM BOILER = 250.5 dC EFFICIENCY (BASED ON LOWER FUEL HEATING VALUE - DIN METHOD) BOILER EFFICIENCY = 87.7 % COMBUSTION (STACK) EFFICIENCY = 88.9 % FLUE GAS LOSSES = 11.1 % FLUE GAS LOSSES = 502.1 kW BOILER JACKET LOSSES (AS SET BY DIN 4702 T3) = .5 % BOILER JACKET LOSSES (AS SET BY DIN 4702 T3) = 22.7 kW HEAT TRANSFER IN FURNACE ........................ STEAM GENERATED = 3360.6 kg/h GAS EXIT TEMP. = 1000.3 dC MEAN GAS TEMP. = 1357.9 dC AREA THERMAL LOAD = 123.2 kW/m2 VOLUME THERMAL LOAD = 903 kW/m3 GAS VELOCITY = 5.8 m/s RADIATION = 1667.7 kW CONVECTION = 512.7 kW HEAT TRANSFERRED = 2180.4 kW WALL TEMP. ON GAS SIDE = 239.4 dC WALL TEMP. ON LIQUID SIDE= 187.7 dC GAS SIDE PRESSURE DROP = .18 mbar HEAT TRANSFER ON REAR WALL = 443.5 kW HEAT TRANSFER ON CIRCULAR PART = 1636 kW HEAT TRANSFER ON TUBESHEET = 100.9 kW WALL TEMP. OF CIRCULAR PART = 225 dC TEMPERATURE OF REAR WALL = 303 dC TEMPERATURE OF TUBESHEET = 213.8 dC HEAT TRANSFER IN TUBE ASSEMBLY AFTER FURNACE ............................................ STEAM GENERATED = 2768.2 kg/h GAS EXIT TEMP. = 251.8 dC MEAN GAS TEMP. = 487.3 dC AREA THERMAL LOAD = 16.9 kW/m2 GAS VELOCITY = 14.7 m/s RADIATION = 277.3 kW CONVECTION = 1518.7 kW HEAT TRANSFERRED = 1796 kW WALL TEMP. ON GAS SIDE = 184.4 dC WALL TEMP. ON LIQUID SIDE= 183.3 dC GAS SIDE PRESSURE DROP = 3.045 mbar HEAT TRANSFER IN CHANNEL AT BOILER EXIT ....................................... STEAM GENERATED = 4 kg/h GAS EXIT TEMP. = 250.5 dC MEAN GAS TEMP. = 251.1 dC AREA THERMAL LOAD = 1.1 kW/m2 GAS VELOCITY = .6 m/s RADIATION = 1.6 kW CONVECTION = 1 kW HEAT TRANSFERRED = 2.6 kW WALL TEMP. ON GAS SIDE = 181.3 dC WALL TEMP. ON LIQUID SIDE= 181.1 dC GAS SIDE PRESSURE DROP = .24 mbar |
| HEAT TRANSFER IN BOILER (ENGLISH UNITS) *************************************** FUEL TYPE : GASEOUS LIQUID : WATER BOILER TYPE : STEAM MAXIMUM GAGE PRESSURE: 145 p.s.i. BOILER DESIGN : 2-PASS BOILER LOAD : 100% BURNER TYPE : FORCED DRAFT BOILER MATERIAL : CARBON STEEL GAS DATA -------- CH4-CONTENT = 100 vol% LOWER HEATING VALUE = 913 BTU/cu.ft. HIGHER HEATING VALUE = 1013.1 BTU/cu.ft. GAS DENSITY = .04 lb./cu.ft. GAS OVERPRESSURE = 0 psi ATMOSPHERIC PRESSURE = 14.7 psi GAS TEMPERATURE = 59 dF RELATIVE GAS HUMIDITY= 0 % BOILER GEOMETRY DATA -------------------- FURNACE DATA ............ FURNACE IS HORIZONTAL FURNACE IS CIRCULAR IN GAS FLOW DIRECTION FURNACE IS REVERSING NET DIAMETER = 52.48 in. WALL THICKNESS = .709 in. LENGTH IN GAS FLOW DIRECTION = 140.984 in. CROSS-SECTION AT FURNACE EXIT = 27.986 sq.ft. FURNACE COOLED AREA = 190.481 sq.ft. BOTTOM COOLED AREA PER.TO GAS FLOW= 15.069 sq.ft. COOLED AREA OF TUBESHEET = 13.993 sq.ft. DISTANCE TO TUBESHEET FROM DOOR = 15.748 in. GEOMETRY DATA OF TUBE ASSEMBLY AFTER FURNACE ............................................ TUBES ARE HORIZONTAL THERE ARE COILED-WIRE TURBULATORS IN TUBES TURBULATOR LENGTH = 100% TUBE LENGTH TURBULATOR DIAMETER = 2.6 in. WIRE DIAMETER = .3 in. NUMBER OF TUBES = 120 NET TUBE DIAMETER = 2.756 in. WALL THICKNESS = .126 in. COOLED TUBE LENGTH = 159.016 in. COOLED AREA = 1147.29 sq.ft. CROSS-SECTION BEFORE TUBES = 27.986 sq.ft. CROSS-SECTION AFTER TUBES = 27.986 sq.ft. GEOMETRY DATA OF CHANNEL AT BOILER EXIT ....................................... CHANNEL IS HORIZONTAL IN GAS FLOW DIRECTION CHANNEL IS CIRCULAR IN GAS FLOW DIRECTION NET DIAMETER = 102.362 in. WALL THICKNESS = .709 in. LENGTH IN GAS FLOW DIRECTION = 15.748 in. COOLED AREA = 25.833 sq.ft. OTHER DATA ---------- GAS RATE = 16951 cu.ft./h COMBUSTION AIR TEMPERATURE = 59 dF FEED LIQUID TEMPERATURE = 221 dF LAMBDA VALUE = 1.1 - STACK CONNECTOR IS CIRCULAR INNER DIAMETER OF STACK CONNECTOR= .5 [in.] TOTAL COOLED AREA = 1363.605 sq.ft. TUBES/FURNACE AREA RATIO = 6.02 CALCULATION RESULTS ------------------- ADIABATIC COMBUSTION TEMPERATURE = 3284.4 dF RELEASED HEAT BY COMBUSTION = 465.4 HP CONDENSATE HEAT IN FLUE GAS = 51.7 HP TEMPERATURE OF LIQUID/STEAM IN BOILER = 355.8 dF GAS VELOCITY IN BOILER FLUE APERTURE = 49.03 ft./s GAS SIDE PRESSURE DROP IN BOILER = 1.4 in.W.C. QUANTITY OF FLUE GAS RELEASED = 194533.4 cu.ft./h BOILER THERMAL OUTPUT = 405.9 HP QUANTITY OF STEAM GENERATED IN BOILER = 13520.5 lb./h FEED LIQUID RATE = 1697.444 gal./h AVERAGE HEAT TRANSFER INTENSITY = 3.36 sq.ft/HP PERCENTAGE OF HEAT TAKEN UP IN FURNACE = 54.8 % GAS EXIT TEMPERATURE FROM BOILER = 482.9 dF EFFICIENCY (BASED ON HIGHER FUEL HEATING VALUE - ASME METHOD) BOILER EFFICIENCY = 79.1 % COMBUSTION (STACK) EFFICIENCY = 80.2 % FUEL TO STEAM EFFICIENCY = 79.7 % FLUE GAS LOSSES (LATENT HEAT INCLUDED) = 19.8 % FLUE GAS LOSSES (LATENT HEAT INCLUDED) = 102.9 HP BOILER JACKET LOSSES (AS SET BY REGULATIONS) = .5 % BOILER JACKET LOSSES (AS SET BY REGULATIONS) = 2.3 HP HEAT TRANSFER IN FURNACE ........................ STEAM GENERATED = 7408.9 lb./h GAS EXIT TEMP. = 1832.5 dF MEAN GAS TEMP. = 2476.3 dF HEAT TRANSFER INTENSITY = .86 sq.ft./HP VOLUME THERMAL LOAD = 2.57 HP/cu.ft. GAS VELOCITY = 19.134 ft./s RADIATION = 170.1 HP CONVECTION = 52.3 HP HEAT TRANSFERRED = 222.4 HP WALL TEMP. ON GAS SIDE = 462.9 dF WALL TEMP. ON LIQUID SIDE= 369.9 dF GAS SIDE PRESSURE DROP = .07 in.W.C. HEAT TRANSFER ON REAR WALL = 45.2 HP HEAT TRANSFER ON CIRCULAR PART = 166.9 HP HEAT TRANSFER ON TUBESHEET = 10.3 HP WALL TEMP. OF CIRCULAR PART = 437.1 dF TEMPERATURE OF REAR WALL = 577.4 dF TEMPERATURE OF TUBESHEET = 416.8 dF HEAT TRANSFER IN TUBE ASSEMBLY AFTER FURNACE ............................................ STEAM GENERATED = 6102.8 lb./h GAS EXIT TEMP. = 485.2 dF MEAN GAS TEMP. = 909.2 dF HEAT TRANSFER INTENSITY = 6.26 sq.ft./HP GAS VELOCITY = 48.227 ft./s RADIATION = 28.3 HP CONVECTION = 154.9 HP HEAT TRANSFERRED = 183.2 HP WALL TEMP. ON GAS SIDE = 363.8 dF WALL TEMP. ON LIQUID SIDE = 362 dF GAS SIDE PRESSURE DROP = 1.22 in.W.C. HEAT TRANSFER IN CHANNEL AT BOILER EXIT ....................................... STEAM GENERATED = 8.8 lb./h GAS EXIT TEMP. = 482.9 dF MEAN GAS TEMP. = 484 dF HEAT TRANSFER INTENSITY = 98.14 sq.ft./HP GAS VELOCITY = 1.815 ft./s RADIATION = .16 HP CONVECTION = .1 HP HEAT TRANSFERRED = .26 HP WALL TEMP. ON GAS SIDE = 358.4 dF WALL TEMP. ON LIQUID SIDE= 357.9 dF GAS SIDE PRESSURE DROP = .096 in.W.C. |
| TUBULAR FINNED ECONOMIZER |
| HEAT TRANSFER IN TUBULAR ECONOMIZER (METRIC) ******************************************** LIQUID : WATER BOILER TYPE : STEAM MAX. GAGE PRESSURE : 25 bar FUEL DATA --------- FLUE GAS TEMPERATURE= 300 dC FLUE GAS QUANTITY = 9817.6 m3/h CARBON-CONTENT = 40.4 % WATER-CONTENT = 11.6 % SULFUR-CONTENT = .14 % HYDROGEN-CONTENT = 4.48 % OXYGEN-CONTENT = 35.85 % NITROGEN-CONTENT = 1.53 % ASH-CONTENT = 6 % LOWER HEATING VALUE = 14612 kJ/kg HIGHER HEATING VALUE= 15859.9 kJ/kg GEOMETRY DATA OF TUBULAR ECONOMIZER ................................... MATERIAL: CARBON STEEL TUBE ROWS HAVE PLAIN ARRANGEMENT THERE ARE CIRCULAR FINS ON ECONOMIZER TUBE FIN HEIGHT ABOVE TUBE = .013 m FIN THICKNESS = .001 m DISTANCE BETWEEN FINS = .015 m FINNED PARTITION LENGTH OF TUBE = 1.145 m ECO BOX CROSS-SECTION FOR GASES = 1.3 m2 GIVEN TOTAL TUBE LENGTH = 196 m TUBE SECTION LENGTH = 1.4 m NUMBER OF TUBE ROWS = 14 DISTANCE BETWEEN TUBE ROWS = .08 m NUMBER OF TUBES IN ROW = 10 DISTANCE BETWEEN TUBES IN ROW = .09 m TUBE OUTER DIAMETER = .032 m TUBE WALL THICKNESS = .0032 m OTHER DATA ---------- FUEL RATE = 1250 kg/h COMBUSTION AIR TEMPERATURE = 20 dC LIQUID TEMPERATURE ENTERING ECO = 105 dC LAMBDA VALUE = 2 - CALCULATION RESULTS ------------------- HEAT TRANSFER IN TUBULAR ECONOMIZER ................................... HEAT CONTENT OF ENTERING GASES = 1134.4 kW HEAT TRANSFERRED = 347.8 kW MEAN TEMP. IN ECONOMIZER = 244.2 dC LIQUID EXIT TEMP. FROM ECONOMIZER= 141.6 dC GAS EXIT TEMPERATURE = 210.1 dC GAS VELOCITY AROUND TUBES = 6.4 m/s LIQUID VELOCITY IN TUBE = .5 m/s WALL TEMPERATURE ON GAS SIDE = 129.5 dC WALL TEMPERATURE ON LIQUID SIDE = 128.3 dC HEAT TRANSFERRED BY FINS = 272.3 kW MIN. DISTANCE BETWEEN FINS CAN BE= .00344 m GAS SIDE PRESSURE DROP = 7 mbar LIQUID RATE THROUGH ECONOMIZER = 9700.3 l/h |
| HEAT TRANSFER IN TUBULAR ECONOMIZER (ENGLISH UNITS) *************************************************** LIQUID : WATER BOILER TYPE : STEAM MAX. GAGE PRESSURE : 362.5 psi FUEL DATA --------- FLUE GAS TEMPERATURE= 572 dF FLUE GAS QUANTITY = 346705.3 cu.ft./h CARBON-CONTENT = 40.4 % WATER-CONTENT = 11.6 % SULFUR-CONTENT = .14 % HYDROGEN-CONTENT = 4.48 % OXYGEN-CONTENT = 35.85 % NITROGEN-CONTENT = 1.53 % ASH-CONTENT = 6 % LOWER HEATING VALUE = 45088.6 BTU/gal. HIGHER HEATING VALUE= 48939.5 BTU/gal. GEOMETRY DATA OF TUBULAR ECONOMIZER ----------------------------------- MATERIAL: CARBON STEEL TUBE ROWS ARE IN PLAIN ARRANGEMENT THERE ARE CIRCULAR FINS ON ECONOMIZER TUBE FIN HEIGHT ABOVE TUBE = .512 in. FIN THICKNESS = .039 in. DISTANCE BETWEEN FINS = .591 in. FINNED PARTITION LENGTH OF TUBE = 45.1 in. ECO BOX CROSS-SECTION FOR GASES = 14 sq.ft. GIVEN TOTAL TUBE LENGTH = 643 ft. TUBE SECTION LENGTH = 55.118 in. NUMBER OF TUBE ROWS = 14 DISTANCE BETWEEN TUBE ROWS = 3.15 in. NUMBER OF TUBES IN ROW = 10 DISTANCE BETWEEN TUBES IN ROW = 3.543 in. TUBE OUTER DIAMETER = 1.26 in. TUBE WALL THICKNESS = .126 in. OTHER DATA ---------- FUEL RATE = 728 lb./h COMBUSTION AIR TEMPERATURE = 68 dF LIQUID TEMPERATURE ENTERING ECO = 221 dF LAMBDA VALUE = 2 - CALCULATION RESULTS ------------------- HEAT TRANSFER IN TUBULAR ECONOMIZER ................................... HEAT CONTENT OF ENTERING GASES = 115.7 HP HEAT TRANSFERRED = 35.5 HP MEAN TEMP. IN ECONOMIZER = 471.6 dF LIQUID EXIT TEMP. FROM ECONOMIZER= 286.9 dF GAS EXIT TEMPERATURE = 410.2 dF GAS VELOCITY AROUND TUBES = 20.981 ft./s LIQUID VELOCITY IN TUBE = 1.521 ft./s WALL TEMPERATURE ON GAS SIDE = 265 dF WALL TEMPERATURE ON LIQUID SIDE = 262.9 dF HEAT TRANSFERRED BY FINS = 27.8 HP MIN. DISTANCE BETWEEN FINS CAN BE= .1354 in. GAS SIDE PRESSURE DROP = 2.8 in.W.C. LIQUID RATE THROUGH ECONOMIZER = 2562.5 gal./h |
| Example No.1: Three-pass wet back steam boiler Example No.2: Two-pass wet back steam boiler Example No.3: Single pass waste heat tubular boiler Example No.4: Tubular finned economizer |
| 3-PASS WET BACK STEAM BOILER |
| SINGLE PASS WASTE HEAT TUBULAR STEAM BOILER |
| HEAT TRANSFER IN BOILER (METRIC) ******************************** FUEL TYPE : WASTE HEAT LIQUID : WATER BOILER TYPE : STEAM MAXIMUM GAGE PRESSURE : 20 bar BOILER DESIGN : TUBULAR SINGLE PASS BOILER MATERIAL : CARBON STEEL WASTE GAS DATA -------------- TEMPERATURE = 900 dC RATE = 12500 m3/h CO2-CONTENT = 8 % H2O-CONTENT = 4.8 % N2-CONTENT = 76.6 % O2-CONTENT = 10.6 % INLET DENSITY = .304 kg/m3 NORM DENSITY = 1.304 kg/m3 BOILER GEOMETRY DATA -------------------- INLET APERTURE CROSS-SECTION= 1.3 m2 GEOMETRY OF TUBE ASSEMBLY ......................... TUBES ARE HORIZONTAL NUMBER OF TUBES = 200 NET TUBE DIAMETER = .0562 m WALL THICKNESS = .0036 m COOLED TUBE LENGTH = 5.3 m COOLED AREA = 187.151 m2 CROSS-SECTION BEFORE TUBES = 2.5 m2 CROSS-SECTION AFTER TUBES = 2.5 m2 OTHER DATA ---------- COMBUSTION AIR TEMPERATURE = 20 dC FEED LIQUID TEMPERATURE = 105 dC STACK CONNECTOR IS CIRCULAR INNER DIAMETER OF STACK CONNECTOR= .5 [m] CALCULATION RESULTS ------------------- HEAT CONTENT OF WASTE GAS ENTERING BOILER = 4567.3 kW CONDENSATE HEAT IN FLUE GAS = 324.9 kW TEMPERATURE OF LIQUID/STEAM IN BOILER = 214.9 dC GAS VELOCITY IN BOILER FLUE APERTURE = 38.8 m/s GAS SIDE PRESSURE DROP IN BOILER = 5.682 mbar BOILER THERMAL OUTPUT = 3011 kW STEAM RATE = 4597.4 kg/h FEED LIQUID RATE = 4816.9 l/h GAS EXIT TEMPERATURE FROM BOILER = 326.1 dC EFFICIENCY (BASED ON LOWER FUEL HEATING VALUE - DIN METHOD) BOILER EFFICIENCY = 65.9 % COMBUSTION (STACK) EFFICIENCY = 68 % FLUE GAS LOSSES = 32 % FLUE GAS LOSSES = 1463.3 kW BOILER JACKET LOSSES (AS SET BY DIN 4702 T3) = .5 % BOILER JACKET LOSSES (AS SET BY DIN 4702 T3) = 23 kW HEAT TRANSFER IN TUBE ASSEMBLY .............................. STEAM GENERATED = 4597.4 kg/h MEAN AREA THERMAL LOAD = 16.1 kW/m2 MEAN GAS TEMPERATURE = 529.3 dC GAS VELOCITY = 20.6 m/s RADIATION = 269.9 kW CONVECTION = 2741.1 kW HEAT TRANSFERRED = 3011 kW WALL TEMP. ON GAS SIDE = 218.9 dC WALL TEMP. ON LIQUID SIDE= 217.8 dC GAS SIDE PRESSURE DROP = 5.682 mbar |
| HEAT TRANSFER IN BOILER (ENGLISH UNITS) *************************************** FUEL TYPE : WASTE HEAT LIQUID : WATER BOILER TYPE : STEAM MAXIMUM GAGE PRESSURE : 290 psi BOILER DESIGN : TUBULAR SINGLE PASS BOILER MATERIAL : CARBON STEEL WASTE GAS DATA -------------- TEMPERATURE = 1652 dF RATE = 441433.3 cu.ft./h CO2-CONTENT = 8 % H2O-CONTENT = 4.8 % N2-CONTENT = 76.6 % O2-CONTENT = 10.6 % INLET DENSITY = .019 lb./cu.ft. NORM DENSITY = .081 lb./cu.ft. BOILER GEOMETRY DATA -------------------- INLET APERTURE CROSS-SECTION= 14 sq.ft. GEOMETRY OF TUBE ASSEMBLY ......................... TUBES ARE HORIZONTAL NUMBER OF TUBES = 200 NET TUBE DIAMETER = 2.213 in. WALL THICKNESS = .142 in. COOLED TUBE LENGTH = 208.661 in. COOLED AREA = 2014.476 sq.ft. CROSS-SECTION BEFORE TUBES = 26.91 sq.ft. CROSS-SECTION AFTER TUBES = 26.91 sq.ft. OTHER DATA ---------- COMBUSTION AIR TEMPERATURE = 68 dF FEED LIQUID TEMPERATURE = 221 dF STACK CONNECTOR IS CIRCULAR INNER DIAMETER OF STACK CONNECTOR = .5 [in.] CALCULATION RESULTS ------------------- HEAT CONTENT OF WASTE GAS ENTERING BOILER = 465.9 HP CONDENSATE HEAT IN FLUE GAS = 33.1 HP TEMPERATURE OF LIQUID/STEAM IN BOILER = 418.7 dF GAS VELOCITY IN BOILER FLUE APERTURE = 127.325 ft./s GAS SIDE PRESSURE DROP IN BOILER = 2.3 in.W.C. BOILER THERMAL OUTPUT = 307.2 HP STEAM RATE = 10135.6 lb./h FEED LIQUID RATE = 1272.49 gal./h GAS EXIT TEMPERATURE FROM BOILER = 619 dF EFFICIENCY (BASED ON HIGHER FUEL HEATING VALUE - ASME METHOD) BOILER EFFICIENCY = 61.5 % COMBUSTION (STACK) EFFICIENCY = 63.6 % FUEL TO STEAM EFFICIENCY = 63.1 % FLUE GAS LOSSES (LATENT HEAT INCLUDED) = 36.4 % FLUE GAS LOSSES (LATENT HEAT INCLUDED) = 182.4 HP BOILER JACKET LOSSES (AS SET BY REGULATIONS) = .5 % BOILER JACKET LOSSES (AS SET BY REGULATIONS) = 2.3 HP HEAT TRANSFER IN TUBE ASSEMBLY .............................. STEAM GENERATED = 10135.6 lb./h HEAT TRANSFER INTENSITY = .007 sq.ft/HP MEAN GAS TEMP. = 984.8 dF GAS VELOCITY = 67.484 ft./s RADIATION = 27.5 HP CONVECTION = 279.6 HP HEAT TRANSFERRED = 307.2 HP WALL TEMP. ON GAS SIDE = 426 dF WALL TEMP. ON LIQUID SIDE= 424 dF GAS SIDE PRESSURE DROP = 2.3 in.W.C. |
