By Ramesh K. Shah, Dusan P. Sekulic
Complete and distinct resource integrates the cloth frequently allotted between a part a dozen sources.
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Additional resources for Fundamentals of Heat Exchanger Design
2) should be replaced by where h is the fluid specific enthalpy, J/kg (Btu/lbm). If the change of state is a phase change, enthalpy differences should be replaced by enthalpies of phase change (either enthalpy of evaporation or enthalpy of condensation). However, cp can be assumed as infinity for condensing or evaporating single-component fluid streams. Hence, the phasechanging stream can be treated as a "single-phase" fluid having A T = q/C or dT = d q / C , with C being infinity for a finite q or dq since the A T or dT = 0 for isothermal condensing or evaporating fluid streams (see Fig.
The C,,, fluid experiences a smaller temperature change than the temperature change for the Cminfluid in the absence of extraneous heat losses, as can be found from the energy balance: q = ch AT, = c, AT, In counting, we have considered only one dependent variable of Eq. 7). 57) THE E-NTU METHOD 119 where the temperature ranges AT, and AT, are Let us reemphasize that for a condensing or evaporating fluid at ideally constant temperature, the A T range (rise or drop) is zero, and hence the heat capacity rate C approaches infinity for a finite q = C AT.
No passage-to-passage or viscosity-induced maldistribution occurs in the exchanger core. Also, no flow stratification, flow bypassing, or flow leakages occur in any stream. The flow condition is characterized by the bulk (or mean) velocity at any cross section. Assumptions 1 through 5 are necessary in a theoretical analysis of steady-state heat exchangers. Heat losses to the surroundings, if small, may be taken into account approximately by using the effective heat capacity rate Cefffor the hot fluid instead of the actual C (= h c P )in the analysis.