1. CONTENTS DESIGN PROBLEM INTRODUCTION FLOW CHART OF DESIGN
NECESSARY RELATIONS
PROPOSED DESIGN
CONCLUSIONS
BIBLIOGRAPHY

2. DESIGN PROBLEM
Design a shell and tube heat exchanger for heating 370 tons/hr of crude oil (sp gr. of at 15 C and normal boiling point 241 C) from 65 C to 90 C using kerosene (sp. gr at 15 C and normal boiling point of C) available at a temperature of 150 C. Choose the flow rate of kerosene so that it does not vaporize

3. INTRODUCTION Most versatile type of heat exchangers
Applications - Process industries, Conventional and nuclear power stations
Provide relatively large ratios of heat transfer area to volume
Used in many alternative energy applications including ocean, thermal and geothermal
2. Used in process industries where heat exchange is in between liquids and heat transfer coefficient is high

4. DESIGN FLOWCHART

5. TO CALCULATE UNSPECIFIED W ASSUMING T
MAKE ENERGY BALANCE
TO CALCULATE UNSPECIFIED W
ASSUMING T
COLLECT
ASSUME OVERALL COEFFICIENT
Uo(52 – 88) btu.ft-2. . F-1
Decide upon the no. of
Shell and tube passes, ΔTlm,Ft
Calculate Area
Ao = [Q / (Uo * ΔTm )]

6. DECIDE TUBE SIZE,LENGTH CALCULATE No, TUBES, SHELL DIAMETER
ESTIMATE TUBE SIDE HEAT
TRANSFER Coef.
DECIDE BAFFLE SPACING AND
SHELL SIDE HEAT TRANSFER
COEFFICIENT
CALCULATE OVERALL HEAT
TRANSFER Coef INCLUDING
DIRT FACTORS

7. NO
YES
CALCULATE TUBE SIDE
SHELL SIDE Pre DROPS
WITH IN
SPECIFICATIONS ? NO
YES

8. In the present situation the max allowable Pressure drop is 13.48psi
SUCCESSFUL DESIGN
If the Shell side Pressure drop comes out to be less than the maximum Allowable pressure drop then there is no vaporization of Kerosene
In the present situation the max allowable Pressure drop is 13.48psi
The Pressure drop calculated using our design comes out to be psi

9. RELATIONS

10. RELATIONS

11. Results Hio=88.48 BTU/ft-2 F-1 Ho = 320.62 BTU/ft-2F-1
Uo(assumed) = 53 BTU/ft-2F-1
Uc (Clean Coefficient) = BTU/ft-2F-1
Uod (calculated) = BTU/ft-2F-1
Error = 8.3 %(within tolerance)
∆Ps = psi
∆Pt =12.19 psi

12. Proposed Design 1 Shell pass,2 Tube Pass(1-2 Heat Exchanger)
Length of the Tube = 30 feet
Number of tubes = 822
Tube O.D = 0.75” Triangular Pitch = ”
Tube Inner Diameter = 0.56”
Shell inner Diameter = 31”
Baffle Spacing = 17”
Overall Heat Transfer Coefficient = BTU/ft-2F-1

13. Conclusions
Pressure Drop results – less than the maximum allowable Pressure drop for this Equipment
Heat exchanger dimensions suggested – within the range used as thumb rules in Industry
Heat Transfer Area can be increased – Put more Tubes, use finned-tube Heat exchanger
Satisfactory Design was proposed

14. Bibliography Kern, Donald Q., “Process Heat Transfer”
Ludwig, Ernest E., “Applied Process Design for chemical and petrochemical plants”, vol.3, Ed.3.
Ozisik, Nekati M., “Heat Transfer”
Perry’s Chemical Engineers’ Handbook. (software edition)