SHELL AND TUBE HEAT EXCHANGER(KERN'S METHOD)
HOT FLUID-lube oil
SPECIFIC HEAT,Kj/KGc,CP: 1.96
VISCOSITY,µ 0.06
DENSITY ,Kg/m3,ρ; 880
THERMAL CONDUCTIVITY,w/mc; 0.13
MASS FLOW RATE Kg/s 302
INLET TEMPERATURE celsius 51.98
OUTLET TEMPERATURE,celsius 45
ΔTh 6.98
ASSUMED OVERALL HEAT TRANSFER COEFFICENT,U W/m2 c
LMTD 13.34 TOTAL HEAT WATTS,Q: 4131.6
FOULING FACTOR ,hd0,W/m2c 5000
PIPE SPECIFICATIONS SCH-40
INNER DIA M,di: 0.02
OUTER DIA ,M,do 0.03
THICKNESS M 0.01
LENGTH M,L 10
TUBE SIDE CO EFFICENT
AREA M2 0
AREA PER PASS 0.23
TUBE SIDE VELOCITY 0.02
REYNOLDS NO 1366.38
PRANDALT NO 0.89
NUSSELT NO 7.16
TUBE SIDE COEFFICENT hi 411.5
OVERALL HEAT TRANSFER COEFFICENT
PRESSURE DROP CALCULATIONS
TUBE SIDE PRESSURE DROP ΔPt,Kpa
23.73SHELL AND TUBE HEAT EXCHANGER(KERN'S METHOD)
HOT FLUID-lube oil
COLD FLUID/UTILITY-water
1.96 SPECIFIC HEAT,J/KGK,CP:
0.06 VISCOSITY,µ
880 DENSITY ,Kg/m3,ρ;
0.13 THERMAL CONDUCTIVITY,w/m2 k,K:
302 MASS FLOW RATE Kg/s
51.98 INLET TEMPERATURE celsius
45 OUTLET TEMPERATURE,celsius
6.98 ΔTc
ASSUMED OVERALL HEAT TRANSFER COEFFICENT,U W/m2 c 220
TEMPERATURE APPROACHES
AREA 1408.1 ΔT1 ΔT2
AREA OF ONE TUBE 0.84 NO OF TUBES Nt 1681.44
NO OF PASSES 4 NO OF TUBES PER PASS 420.36
SHELL SIDE COEFFICENT
BUNDLE DIAMETER Db 0.05
SHELL DIAMETER Ds 0.06
BAFFLE SPACING 0.01
TUBE PITCH,Pt 0.03
AREA OF CROSS FLOW ,As 0
EQUIVALENT DIAMETER de 0.02
SHELL AREA 0
SHELL SIDE VELOCITY 1.29
REYNOLDS NO 115944.36
PRANDALT NO 5.13
NUSSELT NO 49733.67
OVERALL HEAT TRANSFER COEFFICENT 268.02
PRESSURE DROP CALCULATIONS
COLD FLUID/UTILITY-water
SPECIFIC HEAT,J/KGK,CP: 4.19
VISCOSITY,µ 0.01
DENSITY ,Kg/m3,ρ; 996
THERMAL CONDUCTIVITY,w/m2 k,K: 0.62
MASS FLOW RATE Kg/s 156.67
INLET TEMPERATURE celsius 32
OUTLET TEMPERATURE,celsius 38.3 ΔTc 6.3 TEMPERATURE APPROACHES 13.68 13 LMTD PLOT LENGTH,X TEMPERATURE HOT FLUID 0 80 5 50 COLD FLUID 0 30 5 40
SHELL SIDE COEFFICENT
1 2 3 4 5 6 20 40 60 80 100
LMTD PLOT
Series1 length T E M P E R A T U R E1 2 3 4 5 6 20 40 60 80 100
LMTD PLOT
Series1 length T E M P E R A T U R EDOUBLE PIPE HEAT EXCHANGER
PROPERTIES OF FLUIDS
HOT FLUID-toluene
SPECIFIC HEAT,J/KGK,CP: 1842.19 0 DENSITY ,Kg/m3,ρ; 867 THERMAL CONDUCTIVITY,w/m2 k,K: 1.53MASS FLOW RATE Kg/s 4.81
INLET TEMPERATURE celsius 80
OUTLET TEMPERATURE,celsius 40
ΔTh 40
ASSUMED OVERALL HEAT TRANSFER COEFFICENT,U W/m2 c
LMTD 18.2
TOTAL HEAT WATTS,Q: 354437.36
FOULING FACTOR ,hd0,W/m2c 5000
PIPE SPECIFICATIONS
INNER TUBE
INNER DIA M,di: 0.06
OUTER DIA ,M,do 0.07
THICKNESS M 0.01
THICKNESS
INNER TUBE COEFFICENTS
AREA M2 0
TUBE SIDE VELOCITY 1.33
REYNOLDS NO 209770.23
PRANDALTT NO 0.48
NUSSELT NO 333.91
INSIDE HEAT TRANSFER COEFFICENT hi 7012.23
LOG MEAN RADIUS 0.13
OVERALL HEAT TRANSFER COEFFICENT U0,W/M2c
PRESSURE DROP CALCULATIONS
48603.91
DOUBLE PIPE HEAT EXCHANGER
PROPERTIES OF FLUIDS
HOT FLUID-toluene
COLD FLUID/UTILITY-water
SPECIFIC HEAT,J/KGK,CP: VISCOSITY,µ
DENSITY ,Kg/m3,ρ;
THERMAL CONDUCTIVITY,w/m2 k,K: MASS FLOW RATE Kg/hr INLET TEMPERATURE celsius OUTLET TEMPERATURE,celsius
ΔTc
ASSUMED OVERALL HEAT TRANSFER COEFFICENT,U W/m2 c 305 TEMPERATURE APPROACHES
ΔT1
AREA 63.83 ΔT2
LENGTH OF EXCHANGER
PIPE SPECIFICATIONS
OUTER TUBE
0.06 INNER DIA M,di: 0.13
0.07 OUTER DIA ,M,do 0.14
0.01 THICKNESS M 0.01
0.06
INNER TUBE COEFFICENTS
OUTSIDE TUBE COEFFICENTS
AREA M2 TUBE SIDE VELOCITY
REYNOLDS NO PRANDALTT NO
NUSSELT NO
OVERALL HEAT TRANSFER COEFFICENT U0,W/M2c 379.15
PRESSURE DROP CALCULATIONS
DOUBLE PIPE HEAT EXCHANGER
COLD FLUID/UTILITY-water
4664.6 0 999.87 0.62 3.8 30 50 20 30 10 143.87 0.13 0.14 0.01OUTSIDE TUBE COEFFICENTS
0.02 0.24 45530.86 5.13 200.23 877.99
SHELL AND TUBE HEAT EXCHANGER(KERN'S METHOD)
HOT FLUID-toluene
SPECIFIC HEAT,J/KGK,CP: VISCOSITY,µ DENSITY ,Kg/m3,ρ; THERMAL CONDUCTIVITY,w/m2 k,K: MASS FLOW RATE Kg/sINLET TEMPERATURE celsius OUTLET TEMPERATURE,celsius
ΔTh
ASSUMED OVERALL HEAT TRANSFER COEFFICENT,U W/m2 c
LMTD 26.8 TOTAL HEAT WATTS,Q: 265828.02
FOULING FACTOR ,hd0,W/m2c 5000
PIPE SPECIFICATIONS SCH-40
INNER DIA M,di: OUTER DIA ,M,do
THICKNESS M LENGTH M,L
TUBE SIDE CO EFFICENT
AREA M2 0
AREA PER PASS0.03
TUBE SIDE VELOCITY#DIV/0!
REYNOLDS NO#DIV/0!
PRANDALT NO 0.48
NUSSELT NO #DIV/0!
TUBE SIDE COEFFICENT hi#DIV/0!
OVERALL HEAT TRANSFER COEFFICENT
PRESSURE DROP CALCULATIONS
TUBE SIDE PRESSURE DROP ΔPt,Kpa
SHELL AND TUBE HEAT EXCHANGER(KERN'S METHOD)
HOT FLUID-toluene
COLD FLUID/UTILITY-water
1842.19 SPECIFIC HEAT,J/KGK,CP:
0 VISCOSITY,µ
867 DENSITY ,Kg/m3,ρ;
1.53 THERMAL CONDUCTIVITY,w/m2 k,K:
4.81 MASS FLOW RATE Kg/hr
80 INLET TEMPERATURE celsius
50 OUTLET TEMPERATURE,celsius
30 ΔTc
ASSUMED OVERALL HEAT TRANSFER COEFFICENT,U W/m2 c 305
TEMPERATURE APPROACHES AREA 32.52 ΔT1 ΔT2 265828.02 5000 PIPE SPECIFICATIONS SCH-40
0.03 AREA OF ONE TUBE 0.52 0.03 NO OF TUBES Nt 62.01 0.01 NO OF PASSES 2
5 NO OF TUBES PER PASS 31
TUBE SIDE CO EFFICENT
SHELL SIDE COEFFICENT
BUNDLE DIAMETER Db 0.05
SHELL DIAMETER Ds 0.06
BAFFLE SPACING 0.01
TUBE PITCH,Pt 0.04
AREA OF CROSS FLOW ,As 0
EQUIVALENT DIAMETER de 0.02
SHELL AREA 0
SHELL SIDE VELOCITY #DIV/0!
REYNOLDS NO #DIV/0!
PRANDALT NO #DIV/0!
NUSSELT NO #DIV/0!
OVERALL HEAT TRANSFER COEFFICENT #DIV/0!
PRESSURE DROP CALCULATIONS
COLD FLUID/UTILITY-water
SPECIFIC HEAT,J/KGK,CP: 4664.6
VISCOSITY,µ 0
DENSITY ,Kg/m3,ρ; 999.87
THERMAL CONDUCTIVITY,w/m2 k,K: 0.62
MASS FLOW RATE Kg/hr 3.8
INLET TEMPERATURE celsius 30
OUTLET TEMPERATURE,celsius 45 ΔTc 15 TEMPERATURE APPROACHES 35 20 LMTD PLOT LENGTH,X TEMPERATURE HOT FLUID 0 80 5 50 COLD FLUID 0 30 5 40
PLATE HEAT EXCHANGER
HOT FLUID-lub oil
SPECIFIC HEAT,Kcal/kgc,CP: 0.47
VISCOSITY,µ 0.06
DENSITY ,Kg/m3,ρ; 880
THERMAL CONDUCTIVITY,kcal/hrc; 0.13
MASS FLOW RATE Kg/s 302
INLET TEMPERATURE celsius 51.98
OUTLET TEMPERATURE,celsius 45
PLATE HEAT EXCHANGER
COLD FLUID/UTILITY-water
SPECIFIC HEAT,J/KGK,CP: 1 VISCOSITY,µ 0.01 DENSITY ,Kg/m3,ρ; 996 THERMAL CONDUCTIVITY,w/m2 k,K: 0.54MASS FLOW RATE Kg/s
INLET TEMPERATURE celsius 32
OUTLET TEMPERATURE,celsius 38.3
