But have high pressure drop for shell-side and can't be mechanically cleaned. It's good to maximise the pressure drop through an exchanger as it generally means high velocities and high film heat transfer coefficients.Ģ) Check fouling resistances are realistic in line with TEMA recomendationsģ) I would normally check rhoV 2 values meet TEMA limits for inlet and outlet nozzle, program should flag up a warning if not met.Ĥ) Check for vibration warnings, if there are vibration warnings you need to look at design carefully.ĥ) Check tube pattern - HTEX with 30° triangular pattern cost less per m² heat transfer area (due to highest tube densities) and transfer more heat per m² heat transfer area (due to the high shell-side heat transfer coefficients).
Hydrocarbon ( 5 cP) / Hydrocarbon (> 5 cP) / 100 - 180Ĭondensing Steam / Hydrocarbon ( 5 cP) / 100 - 300ġ) Pressure drop is within allowable limits typically 0.5 bar to 1.0 bar. Hot-side fluid / Cold-side fluid / U (W/m².C)
Never used HTRI but have experience with HTFS Tasc.įirst thing I look at is the value for U (overall heat transfer coefficient) this must be realistic, and is dependant on the quality of the fluid physical properties inputted into the software, and the exchanger geometry, as a rule of thumb you can check U values against the table below which contains typical value:
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