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34 1 = 1 + 1 +Rw +Rf (t) [3.1.24] U hx hy Where hx and hy are the convective heat transfer coefficients of the two fluids in the heat exchanger. Rw and Rf(t) represent the tube-wall resistance and time-dependent fouling resistance respectively. Rw and Rf(t) are generally neglected for general models but can be integrated as design-specific data is available. The following order-of-magnitude values were used for single fluid heat transfer coefficients [Incropera, 2002]: h =1,000W liquid m2 h =140W vapor m2 h =10,000W two− phase m2 [3.1.25] The overall heat transfer coefficient calculated using this technique will not remain constant during off-design operation. The variation in U as a function of system load is determined as follows: Single phase convective heat transfer correlations are often formulated in the following manner [Incropera, 2002]: k k ⎛ 4 m& ⎞ 0 . 8 ⎛ C μ ⎞ 0 . 3 , 0 . 4 h= ⋅a⋅Re0.8 Pr0.3,0.4 = ⋅a⋅⎜ ⎟ ⎜ p ⎟ [3.1.26] d d ⎝πDμ⎠⎝k⎠ where the exponent on the Prandtl number is 0.3 when the fluid is being cooled and 0.4 when the fluid is being heated. Based on the reference value determined by equation [3.1.24] the part-load overall heat transfer coefficient can be calculated for each heat exchange process in the following manner: U U = k ⎛m&μ ⎞0.8⎛ Cμk ⎞0.3,0.4 ref ⎟ [3.1.27] ref ⎝ ref ⎠ ⎝ ref ref ⎠ ⎜ ref ⎟ ⎜ ref k ⎜ m& μ ⎟ ⎜ C μ k ⎟ Correlations of the form of equation [3.1.26] do not capture all of the effects occurring in the two-phase heat exchangers (evaporator and condenser). Two-phase heat transfer correlations are often formulated as a liquid phase heat transfer enhancement of the formPDF Image | Organic Rankine Cycle Solar-Thermal Powerplants
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