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of the sink. This is very important because this effect will reduce the irreversibilities of the cycle, therefore resulting in higher efficiencies. To identify the impact of the mixed working fluids on the cycle shown in Figure 5, we used mixed working fluids consisting of pentane/iso-hexane, pentane/iso-butane, and iso-butane/iso- hexane. Four combinations of the above working fluids were analyzed (Table 4). For the sake of comparison with the pure component working fluid, the results for a mixture of pentane/iso- butane (90% pentane, 10% iso-butane) are presented here. This working fluid gave the highest efficiency among the cycles analyzed. All the assumptions and working conditions assumed for the pure component case were applied here. The heating and cooling curves for this case are shown in Figures 9 and 10. The state points for this cycle are given in Table 5. Table 4. Performance of ORC with Recuperation using Mixed Working Fluids Working Fluid Efficiency Composition ic4/ic6 (95/5) 19.2 ic4/c5 (5/95) 20.3 ic4/c5 (10/90) 20.4 c5/ic6 (95/5) 20.3 Gross Parasitic Electricity (kWe) (kWe) 995 101 1,118 124 1,134 130 1,091 113 HTF Flow lbm/hr 91,000 91,478 91,065 92,305 HTF outlet Temp. (°F) 351 340 337 346 Table 5. State Points for the ORC with Recuperation using Mixed Working Fluid Temperature F Pressure psi Vapor Frac Mole Flow Mass Flow Volume Flow cuft/hr Enthalpy MMBtu/hr 9.47E+01 2.00E+01 0.00E+00 9.37E+02 6.60E+04 1.75E+03 Mass Flow AIR OIL N-PEN-01 ISO-BUT lb/hr lbmol/hr lb/hr 1.03E+02 1.47E+01 1.00E+00 7.71E+04 2.23E+06 3.16E+07 1.37E+01 -6.84E+01 ACC-IN 1.55E+02 2.20E+01 1.00E+00 9.37E+02 6.60E+04 2.69E+05 ACC-OUT 9.47E+01 2.00E+01 0.00E+00 9.37E+02 6.60E+04 1.76E+03 AIR-IN 8.00E+01 1.47E+01 1.00E+00 7.71E+04 2.23E+06 3.04E+07 1.60E+00 2.23E+06 0.00E+00 0.00E+00 0.00E+00 AIR-IN1 8.03E+01 1.47E+01 1.00E+00 7.71E+04 2.23E+06 3.03E+07 1.75E+00 2.23E+06 0.00E+00 0.00E+00 0.00E+00 AIR-OUT LIQ-1 LIQ-2 9.99E+01 6.25E+02 0.00E+00 9.37E+02 6.60E+04 1.76E+03 -6.81E+01 LIQ-3 3.18E+02 6.10E+02 0.00E+00 9.37E+02 6.60E+04 2.50E+03 -5.84E+01 SF-IN 5.80E+02 5.00E+03 0.00E+00 7.10E+02 9.11E+04 3.84E+03 -5.32E+01 SF-OUT 3.37E+02 5.00E+03 0.00E+00 7.10E+02 9.11E+04 2.50E+03 -6.87E+01 -5.65E+01 -6.84E+01 0.00E+00 0.00E+00 5.94E+04 6.60E+03 0.00E+00 0.00E+00 5.94E+04 6.60E+03 2.23E+06 0.00E+00 0.00E+00 0.00E+00 0.00E+00 5.94E+04 0.00E+00 6.60E+03 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 0.00E+00 9.11E+04 9.11E+04 5.94E+04 5.94E+04 0.00E+00 0.00E+00 6.60E+03 6.60E+03 0.00E+00 0.00E+00 Figure 9 shows the heating curve of the mixed working fluid. The impact of the mixed working fluid is missed because the boiling is occurring under super-critical conditions. Therefore, the heating curve is not much different than the one experienced for a pure component (compare to Figure 6). However, Figure 10 shows the effect of using mixed working fluid during the cooling process. The cooling curve of the working fluid follows the heating curve of the air much closer, compared to the behavior of the pure fluid as shown in Figure 7. The efficiency of this cycle is 20.4%, which is very comparable to the pure fluid case. Therefore, for cycles operating under supercritical conditions, use of mixed working fluid does not provide any advantages. However, for the off-design or partial-load conditions where the boiler pressure falls below the critical 14PDF Image | Modular Trough Power Plant Cycle and Systems Analysis
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