2. Kern’s Description of Shell Side Flow in SHELL-AND-TUBE HEAT EXCHANGER P M V Subbarao Professor Mechanical Engineering Department I I T Delhi Another Peculiar Averaging Method.….

3. Shell-Side Reynolds Number Reynolds number for the shell-side is based on the equivalent diameter and the velocity based on a reference flow:

4. Shell Side Fluid Flow

5. Classification of Shell Side Flow

6. Thermodynamic Similarity of Counter & Cross Flow Heat Transfer

7. Fluid dynamic Similarity of Counter & Cross Flow Heat Transfer ?!?!?!

8. Tube Layout & Flow Structure A Real Use of Wetted Perimeter !

9. Tube Layout Tube layout is characterized by the included angle between tubes. Two standard types of tube layouts are the square and the equilateral triangle. Triangular pitch (30 o layout) is better for heat transfer and surface area per unit length (greatest tube density.) Square pitch (45 & 90 layouts) is needed for mechanical cleaning. Note that the 30°,45° and 60° are staggered, and 90° is in line. For the identical tube pitch and flow rates, the tube layouts in decreasing order of shell-side heat transfer coefficient and pressure drop are: 30°,45°,60°, 90°. The 90° layout will have the lowest heat transfer coefficient and the lowest pressure drop.

10. The square pitch (90° or 45°) is used when jet or mechanical cleaning is necessary on the shell side. In that case, a minimum cleaning lane of ¼ in. (6.35 mm) is provided. The square pitch is generally not used in the fixed header sheet design because cleaning is not feasible. The triangular pitch provides a more compact arrangement, usually resulting in smaller shell, and the strongest header sheet for a specified shell-side flow area. It is preferred when the operating pressure difference between the two fluids is large.

11. Tube Pitch The selection of tube pitch is a compromise between a Close pitch (small values of P T /d o ) for increased shell-side heat transfer and surface compactness, and an Open pitch (large values of P T / d o ) for decreased shell-side plugging and ease in shell-side cleaning. Tube pitch P t is chosen so that the pitch ratio is 1.25 < P T /d o < 1.5. When the tubes are to close to each other (P T /d o less than 1.25), the header plate (tube sheet) becomes to weak for proper rolling of the tubes and cause leaky joints. Tube layout and tube locations are standardized for industrial heat exchangers. However, these are general rules of thumb and can be “violated” for custom heat exchanger designs.

12. Identification of (Pseudo) Velocity Scale

13. Shell Side Pseudo Flow Area The number of tubes at the centerline of the shell is calculated by where is A s the bundle cross flow area, D s is the inner diameter of the shell, C is the clearance between adjacent tubes, and B is the baffle spacing

14. Pseudo Shell side Mass Velocity The shell-side mass velocity is found with

15. Selection of Shell Diameter

16. Shell Diameter The number of tubes is calculated by taking the shell circle and dividing it by the projected area of the tube layout. That is where A pro-tube is the projected area of the tube layout expressed as area corresponding to one tube, D s is the shell inside diameter, and CTP is the tube count calculation constant that accounts for the incomplete coverage of the shell diameter by the tubes, due to necessary clearances between the shell and the outer tube circle and tube omissions due to tube pass lanes for multitude pass design.

17. Projected area of Tube Layout Where P T is the tube pitch and CL is the tube layout constant.

18. Coverage of Shell Area

19. The CTP values for different tube passes are given below:

20. Pseudo Shell side Mass Velocity The shell-side mass velocity is found with

21. Shell side Equivalent (Hydraulic) Diameter Equivalent diameter employed by Kern for correlating shell side heat transfer/flow is not a true equivalent diameter. The direction of shell side flow is partly along the tube length and partly at right angles to tube length or heat exchanger axis. The flow area at right angles is harmonically varying. This cannot be distinguished based on tube layout. Kern’s experimental study showed that flow area along the axis showed excellent correlation wrt Tube layout, tube pitch etc….

22. Equivalent Counter Flow : Hydraulic or Equivalent Diameter The equivalent diameter is calculated along (instead of across) the long axes of the shell and therefore is taken as four times the net flow area as layout on the tube sheet (for any pitch layout) divided by the wetted perimeter.

23. Free Flow Area for Square Layout: Free Flow Area for Triangular Layout:

24. Perimeter for square Layout: Perimeter for triangular Layout: Equivalent diameter for square layout: Equivalent diameter for Triangular layout: