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262 263 264 265 266 267 268 • 269 270 271 272 273 274 275 w The correction factors J of the heat transfer coefficient in the shell side have been neglected. The heat transfer coefficient for the boiling process is calculated by the approach developed by Bromley et al. [48], it is used to predict the film boiling heat transfer coefficient for a horizontal tube. The heat transfer correlation used for internal condensation in horizontal tubes is proposed by Carey [49] and Ould Didi et al. [50]. The overall pressure drop due to the evaporation process was obtained by the Martinelli-Nelson’s correlation [51]. The data on fouling factors were given by Ludwing [52]. The both side fouling factor was fixed to 0.0003 m2 ◦C/W. Single-pass crossflow plate-fin exchangers have been chosen for the gas-vapor heat transfer. A similar step- by-step method for rating the single-pass crossflow plate-fin exchanger is used in order to obtain following information: Reynolds numbers, surface basis characteristics, corrections to the surface basic characteristics due to temperature-dependent properties, heat transfer coefficients and fin efficiencies, wall thermal resistance and overall thermal conductance, NTU, exchanger effectiveness, heat transfer rate and pressure drops on each fluid side [42]. The condenser is placed the behind the grille and cooled directly by the ambient. The vehicle speed is fixed at 90 km/h due to its frequent occurrence as road truck speed, irrespective of the load and engine speed. n μ 0.14 (Φs) = μ (5) 276 The operating points with greater reduction in bsfc for each configuration studied were considered in order to 277 evaluate the space requirement. Table 4 shows the selected operating points with dT=10◦C (from 1i to 4i). The 278 dimensions and pressure drops required of the heat exchanged designed are listed in Table 4. 279 Figure 8 shows the heat exchanger volume obtained by using the previous criteria. The evaporator is the biggest 280 heat exchanger in the RC and the ORC configurations of case A (Point 1i and 2i), due to the large heat transfer that 281 takes place during the evaporation process. The heating process during the liquid phase presents a low heat exchange, 282 because the working fluid at the pump outlet is near to the saturation curve. The volume of the evaporator in case A is 283 also high enough to allow such a high heat exchange rate without a high pressure drop in the shell side. The evaporator 284 absolute pressure in the RC configuration with all the heat sources (1i) is above 0.3 bar. This implies that the heat 285 exchanger must be designed with a large diameter and extreme length in order to avoid a high relative pressure drop 286 as shown Table 5. This effect is less important in the ORC (2i), because the evaporator pressure is higher and the 287 relative pressure drop is lower. The superheater size in both cases (1i and 2i) is almost neglectable compared to the 288 size of the pre-heater and evaporator. 289 In case B (Point 3i and 4i), the largest heat exchange process is the liquid heat transfer process to the saturation 290 curve. The heat transfer area in this process must be very high due to the higher evaporation temperature than in 291 case A. The low temperature difference between the cold and hot flow to heat the liquid implies large areas in the 292 heat exchange. The superheater size in (3i) and (4i) is also neglectable compared to the size of the pre-heater and 293 evaporator. 10PDF Image | Methodology to design a bottoming Rankine cycle
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