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Satish Lele
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This Package includes
Design Programs for
DoublePipe
Exchanger
Heater
Cooler
Program for Design of Tubular Exchanger
to Download Demo Program for Design of Tubular Exchangers
OR
to Request for Demo Program.
Program for Heater (Heating by Steam)
How the Program Runs?

The program asks for parameters in the following dialog boxes, and based on these values, program designs.
Imperial or Metric
You can select the Foot-Inch units or Metric Units for the Design. All inputs will be in selected unit system.
Name of txt file
Type Name of txt file in which all process details will be written.
Double Pipe or Tubular
Select Double Pipe or Tubular Exchanger.
Units of flow
Flow in Pounds per hour or cubic feet per hour.
Tubular Exchanger
You can select type of Tubular Exchanger.
Properites of liquids in two streams.
Properites of liquids in two streams.
Physical Properties
Physical Properties of two Streams.
Baffles
You can select whether Baffles on Shell side required.
Heat Transfer Coefficients
Enter Higher and Lower Values of Heat Transfer Coefficients and Dirt Factor.
Pipe Sizes
Sizes of Pipes.
Tubular Exchanger
You can select either Square pitch or Triangular pitch.
Final Values
After Calculating it shows number of Tubes required.
here to see Dialog Boxes in Metric Units

How the Program Calculates?

Program first picks up flow rates, and then inlet and outlet temperatures for Liquid stream. It also picks up Steam Pressure. Based on Properties of steam at that pressure, it calculates flow rate of steam. It also asks for permissible pressure drop on two streams. It then calculates average temperature of liquid stream. Based on the average temperature, it asks for specific heat, viscocity and specific gravity of liquid stream.
Liquid stream is generally placed on Shell side and there are no baffles on shell side. Steam is placed on tube side, as steam is more corrosive. The number of passes on tube side is generally an even number (generally 2). You can select Square or Triangular Pitch for tubes.
It then calculates LMTD. Since steam temperature is same throughout the tube, correction factor for LMTD is not required. It then asks for expected Higher and Lower value of Overall Heat Transfer Coefficient and value of dirt factor. It then asks for OD, Pitch, Thickness and Length of tube. Based on these, calculation is done. Initially programs assumes number of tubes equal to number of passes. Based on this tube count, it assigns shell diameter (as per number of passes)
Calculation of number of Tubes:
For Shell: Program calculates Mass Velocity for shell by dividing shell side mass flow rate by shell cross sectional area. It then calculates equivalent diameter of tube. Based on this it calcuates Reynold's number. Based on Reynold's number, it picks up value of jH for shell automatically. It then calculates Overall Heat Transfer Coefficient, ho for outer side of tube.
For Tubes: Program calculates Mass Velocity for tube by dividing tube side mass flow rate by cross sectional area of tube. Based on this it calcuates Reynold's number based on inner diameter of tube. It then assigns Overall Heat Transfer Coefficient, hio for inner side of tube.
It then corrects the two values for viscocity of liquids at wall temperature. Overall Heat Transfer Coefficient is then calculated based on ho, hio and dirt factor. The heat transfer area required is calculated by dividing heat load by LMTD and value of Overall Heat Transfer Coefficient. Dividing heat transfer area by tube's outer surface area gives the number of tubes required. If calculated tubes are more than number of tubes assumed, program increases number of tubes assumed by one and recalculates. It follows this procedure till number of assumed tubes are same as number of calculated tubes.
Calculation Pressure Drop:
For Tube: Based on Reynold's number calculated earlier, it picks up value of friction factor. It picks up density of steam at that presure. Based on these, it calculates pressure drop.
For Shell: Based on Reynold's number calculated earlier, it picks up value of friction factor. Based on that, it calculates pressure drop.
If the pressure drops on both sides is within limit, design is good. Otherwise new combination of OD, Pitch, Thickness and Length of tube is tried to get the result.


Report Generated by Program
==============================================================
*Process Design
Units of Calculation : Imperial
Input Values in Imperial system
==============================================================
Type : Shell and Tube Heat Exchanger
==============================================================
Duty : Heating Chemical by Steam
==============================================================
*Input Parameters
Shell side flow rate : 200000.00 lb/h
Shell side inlet Temp : 122.00 Deg F
Shell side outlet Temp : 100.00 Deg F
Shell side Allowable Pressure Drop : 10.00 lb/sq.in.
Shell side liquid Specific Heat : 0.8614 Btu/lb-Deg F
Shell side liquid Viscosity : 1.30 cP
Shell side Specific Gravity : 1.8000
Tube side Steam Pressure : 5.00 lb/sq in
Tube side Steam Temp : 227.96 Deg F
Tube side liquid Viscosity : 0.0127 cP
==============================================================
Liquid on Shell side
Steam on Tube side
Number of Tube Side Passes : 2
Dirt Factor Rd : 0.0030
Heat Transfer Load : 3790160.00 Btu/hr
==============================================================
*Tube Data
Tube Outer Diameter : 3/4"
Length of Tube : 16'
Tube Thickness BWG : 16
Tube Pitch : 1"
Tube Configration : Square
==============================================================
*All Calculations done in Imperial Units
Tube Side Flow Area : 0.0765 sq. ft.
Tube Side Mass Velocity : 51570.79 ft/h
Tube Side Reynold's Number : 86695
Tube Side mean Temp : 227.96 Deg F
Tube side Heat Transfer Coefficient h : 1500 Btu/h-sq. ft. Deg F
Shell Side Flow Area : 0.5614 sq. ft.
Shell Side Mass Velocity : 356228.77 ft/h
Shell Side Reynold's Number : 17741
Shell Side jH value : 57.5000
Shell Side mean Temp : 111.00 Deg F
Shell side c Value : 1.30
Shell side k Value : 0.33
Shell side Heat Transfer Coefficient h : 281.96 Btu/h-sq. ft. Deg F
Shell side Heat Transfer Coefficient h (corrected for viscocity) : 283.20 Btu/h-sq. ft. Deg F
==============================================================
Number of Tubes : 74
Recommended Shell NB : 1'
==============================================================
*Pressure Drop Calculations in Imperial Units
Shell side Pressure Drop
Shell Side Reynold's Number : 17741
Shell side Friction Factor : 0.0019
Shell side Mass Velocity : 356228.77 ft/h
Shell ID : 1'
Shell Liquid specific gravity : 1.8000
Equivalent Dia of Tube : 15/16"
Shell side Pressure Drop : 0.0575 psi
--------------------------------------------------------------
Tube side Pressure Drop
Tube Side Reynold's Number : 86695
Tube side passes : 2
Tube side Friction Factor : 0.0002
Tube Liquid specific gravity : 0.0008
Tube Side Mass Velocity : 51570.79 ft/h
Length of Tube : 16'
Inside Dia of Tube : 5/8"
Tube side Pressure Drop : 2.9715 psi
==============================================================
Summary
Type : Shell and Tube Heat Exchanger
Tube Outer Diameter : 3/4"
Length of Tube : 16'
Number of Tubes : 74
Tube Thickness BWG : 16
Tube Pitch : 1"
Number of Tube Side Passes : 2
Tube Configration : Square
Recommended Shell NB : 1'
==============================================================
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