Heat Exchanger Design with HTRI

A: A: Cuts peak cross-flow velocity. Fouling trend slows and ΔP growth flattens without touching pressure envelope. B: Longer tubes raise shell-side residence time and ΔP. Trend keeps worsening. C: Tighter spacing spikes local shear. Heat transfer improves short-term, fouling accelerates offshore. D: Pass count change shifts tube-side hydraulics. Shell-side fouling mechanism stays untouched.

A: A: Q = U·A·ΔT. 12e6 / (600·25) lands just under 800 m². That's the right scale. B: Off by a factor of ten. Confuses heat flux with total duty. C: Assumes U an order lower than stated. That's crude fouling panic. D: Pass arrangement doesn't multiply area. Geometry changes effectiveness, not physics.

A: A: Added resistance lowers U. With fixed area, duty falls and outlet temps slide. B: LMTD is set by process temps, not fouling math. C: Tube fouling doesn't directly drive shell hydraulics. D: Metal temperature rise follows severe fouling, not the first-order effect.

A: A: Two-pass shell smooths temperature profile and vibration risk. B: Simplicity doesn't fix high local ΔT and tube excitation. C: K shell targets low ΔP, not temperature cross issues. D: J shell handles expansion but keeps the same thermal pinch.