1 / 50

Heat Exchangers

Heat Exchangers. Design Considerations. Heat Exchangers. Key Concepts Heat Transfer Coefficients Naming Shell and Tube Exchangers Safety In Design of Exchangers Controls for Exchangers. Heat Exchangers. 4. Key Concepts. "Allow me to summarise:

Download Presentation

Heat Exchangers

An Image/Link below is provided (as is) to download presentation Download Policy: Content on the Website is provided to you AS IS for your information and personal use and may not be sold / licensed / shared on other websites without getting consent from its author. Content is provided to you AS IS for your information and personal use only. Download presentation by click this link. While downloading, if for some reason you are not able to download a presentation, the publisher may have deleted the file from their server. During download, if you can't get a presentation, the file might be deleted by the publisher.


Presentation Transcript

  1. Heat Exchangers Design Considerations

  2. Heat Exchangers • Key Concepts • Heat Transfer Coefficients • Naming Shell and Tube Exchangers • Safety In Design of Exchangers • Controls for Exchangers

  3. Heat Exchangers

  4. 4 Key Concepts "Allow me to summarise: Hot stuff this side, cold stuff that side. Make the cold stuff hotter, but use inbetween stuff to not let the cold stuff actually touch the hot stuff. Cold stuff and hot stuff not allowed to destroy inbetween stuff and vice versa. Some kinds of inbetween stuff works better than others. Might need pumps or fans to make the whole shebang work a little better, too.” - Topher Gayle

  5. General Sizing Method • Pick an exchanger type (S&T, Plate & Frame etc.) • Choose counter or co-current flow • Choose number of tube passes (for S&T) • draw Temp diag, Calculate the LMTD and Q • Calculate the LMTD Correction Factor (F) if more than two tube passes • Choose a U value based on tables • Calculate the Area , A = Q/ U LMTD F • Perform rigorous rating as required (not 470)

  6. 8-9 Key Concepts = Heat Lost Heat Transfer Heat Absorbed Q = U A Tln Either Q = m Cp T, or Q = m Hevap Either Q = m Cp T, or Q = m Hevap m Cp hot (T1-T2) = U A Tln = m Cp cold ( t1 - t2)

  7. 9 Combined Equations m Cp hot (T1-T2) = U A Tln = m Cp cold ( t1 - t2) • Calculate the unknowns • Determine the overall heat transfer coefficient (U) value in order to calculate the Area (A) to size the exchanger

  8. Duty Considerations - Q • Distillation Columns • Start-up and Shut-down usually require the column to operate at “full reflux” • Feed and Outlets are shut down • 100% of Overhead vapour being condensed • 100% of reflux being boiled • Compositions can be completely different (reactor not online), therefore diff. temps • Is the duty in the simulation truly the worst-case duty? • For our purposes assume yes

  9. T1 t2 Counter Current Exchanger Temp Profile t1 T1 t2 T2 T2 t1 26-27 Mean Temp Difference Always Draw This Graph !!

  10. 200 Exchanger Temperature Profile T1 Hot Side temp & flow direction T2 Cold Side temp & flow direction t2 30 45 38 t1 26-27 Mean Temp Difference • Correction for not strictly counter or co- current flow

  11. T1 = 200 t2 = 45 T2 = 38 t1 = 30 27-28 Temperature Correction Factor • Form of the heat transfer equations is: • The factor F is usually determined Graphically T1 = 200 T2 = 38 t1 = 30 t2 = 45 As A Single Pass Counter Current - temp cross?

  12. 27-28 Temperature Correction Factor • Form of the heat transfer equations is: • The factor F is usually determined Graphically T1 = 200 T2 = 38 t1 = 30 t2 = 45 T1 = 200 As a 2 Pass exch - temp cross - low F factor t2 = 45 T2 = 38 t1 = 30

  13. 28-39 Temperature Correction Factor R = 11.2, P = 0.0882 , F = 0.471

  14. 30 Condensing LMTD • Divide the Exchanger into segments • Evaluate U and LMTD for each segment • Multicomponent, noncondensables? Arghh!

  15. Counter to the Co-current • Use Counter Current • maximize LMTD (minimize Area, cost etc.) • minimize utility reqt’s • Use Co-current • minimize outlet utility temperatures during turn down - see later • reduced fouling

  16. 9-11 Determining U • Tables for U values • Determine U via fundamental equations • note that fouling factors often overshadow much of the accuracy that the fundamental equations provide • Details of exchanger configuration required • Computer Programs / Vendors • vendors can and will provide exch sizing • Be knowledgeable enough to critique their design

  17. 11-13 Determining U • Physical configuration affects U values • Tables assume certain things about the exchanger. If through poor configuration, (ie..inappropriate tube length, or number of tubes) the assumptions are invalidated, then the tables will mislead.

  18. 11-13 U Values & Velocity

  19. 11-13 Physical Config & U Values The following factors all affect the velocities of the fluids in the exchanger • Tube Length • Tube Dia • Number of Tube Passes • Number of Tubes / Bundle dia • Baffle Spacing Note: This does not apply to condensers or boiling

  20. 11-13 U Values & Velocity • Adding a Tube Pass doubles the velocity of the liquid on the tube side • Decreasing Baffle Spacing Increases Velocity Shellside

  21. Physical Configuration & U values • Tube Layout Triangular (high heat x-fer) Square Rotated Square Preferred for cleaning 26

  22. 13 Velocity Limitations • Maximum Velocity is Dictated by: • Vibration • Erosion • Hydraulic • Exchanger Physical Size

  23. 13-15 Velocity Limitations - Vibration • Usually a Shell Side Issue • Vibration Can Cause • Collision Damage, Baffle Damage, Fatigue & Tubejoint Failure • Causes • Turbulent buffeting • Fluidelastic whirling • Vibration induced by flow parallel to the tubes

  24. 13-15 Velocity Limitations - Vibration • Analysis • determine the natural frequency of the tubes • vibration of tubes between baffles • vibration on U bends • account for damping (fluid properties, tube stresses etc.) • determine critical flow velocity • minimum cross flow velocity that the span may vibrate unacceptably large amplitudes. • Analysis by Programs or TEMA Standards

  25. 15 Tube Side Velocity Limitations - Erosion • High Velocity causes thinning of the metal walls (erosion). • It can be avoided by maintaining velocities (ft/sec) below those given by this equation. (about 12 ft/sec for water) • TEMA say ru2 < 6000 to eliminate tube end erosion

  26. 15-16 Velocity Limitations - Hydraulics • Available pressure drop will limit velocity • The P rises to the square of the velocity 60 psig EXCH 0 psig CV P

  27. 16-17 Velocity Limitations - Physical • Limitations on Shipping, • Floor space etc. all make a difference (don’t forget about pulling the tube bundle)

  28. U values of interest • Condensing U values are very high (500 to 800) • Reboiler U values are very high ( 700) • liq / liq U values in middle (100 - 300) • Cooling / heating gases (desuperheating) have very low U values (<30)

  29. Shell Side Fluid Leaks to Atmosphere TEMA Easier to Clean Expensive Large Annular Space = Low U Value Less Costly Cheap, Hard to clean

  30. Exchanger Selection • Require a U-tube or Floating head, instead of fixed tube sheet, when thermal expansion between shell and tubes is an issue • i.e. shell side fluid and tube side fluid temperatures differ by more than 200 °F • Require a Floating Head, instead of U-tube • When cleaning tubes mechanically is important (dirty fluids on tube side) • When errosion may occur on tube side

  31. Nucleate Boiling Film Boiling 52 Reboilers • Boiling Phenomena • Nucleate boiling at shell/tube T = 20 to 50 °F

  32. 53-57 Reboilers • Sizing • Common to use “maximum heat flux” • 15,000 BTU/hr sq ft • Fundamental Equations can be used to determine the best DT • Max Flux is a function of the Number of active nucleation which is in turn affected by the materials of construction, the fluid properties and the temperature difference

  33. 55 Reboilers • Heat Flux can be increased with special systems (i.e. sintering, brazing, flame spraying, electrolytic deposition). Sand blasting , scoring tends not to provide stable long term enhancement. Trapped Vapour Nucleation Sites

  34. Heat Exchanger Safety • What Can Fail? • Control System Failure • Shell & Tube • Tube can rupture • Tubes separate from Tube Sheet • Blocked in exchanger causes cool fluid to experience temperatures of hot fluid • Plate & Frame • Gaskets can leak mixing hot and cold sides , or releasing either fluid to surroundings

  35. Heat Exchanger Safety • Implications • Fires, Explosions, Toxic Releases

  36. Design Duty Reduced Duty Hot In Hot In Cold Out Cold Out Hot Out Hot Out Q = m c T Cold In Cold In Controlling Exchangers Q = U A Tln • A is fixed • U varies slightly with velocity • Tln is the controlling variable

  37. 58 Controls • Liquid / Liquid - control on cooling media C/w

  38. 59 Controls • Liquid / Liquid - control on process C/w

  39. 60 Controls - Steam Heating • Steam Pressure Control T

  40. Steam Trap

  41. 61 Controls - Steam Heating • Condensate Level Control

  42. Duty: 153 x 106 KJ/hr T1 = 213.3 °C T2 = 35 °C t1 = 30 °C dew point: 150 °C (to be confirmed in PRO 2) U gas/water - 0.51 kW/ m2 °C U condensing / water - 0.85 kW/ m2 °C Workshop - Size “Condenser”

  43. No Class Friday ? END

  44. DEVIZE

  45. DEVIZE

  46. DEVIZE

  47. DEVIZE

  48. DEVIZE

  49. DEVIZE

More Related