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VFR 13.57 21.59 9.79 14.13 19.80 29.94 3.3. Heat source temperature of 300 oC 50 40 30 20 10 0 0 5 10 15 20 25 30 35 40 45 50 55 60 Maximum operation pressure (bar) cyclopentane hexane pentane R245fa butane propane (α) 50 40 30 20 10 0 0 5 10 15 20 25 30 35 40 45 50 55 60 Maximum operation pressure (bar) Hexane/Pentane Cyclopentane/Hexane Butane/Cyclopentane Pentane/Propane Cyclopentane/Pentane Butane/Pentane Butane/Hexane R245fa Butane Propane Cyclopentane/Propane Hexane/Propane (b) Fig. 11 Exergy efficiency a) pure fluids and b)binary zeotropic mixtures at a heat source temperature of 300 oC 3.3.1. Pure fluids-THS,in=300oC Due to the high value of the heat source temperature the decrease of the ηHS,u as the turbine inlet temperature rises is relatively smaller than in the previous cases (Sections 3.1 and 3.2) examined. At the same time, the positive effect of the enhancement of the energetic efficiency of the working fluids for increasing maximum operating pressures remains unaffected. The overall result is the disappearance of the bell shaped ηex-p curves (Fig. 11). Consequently, for all the pure fluids and binary mixtures, the exergetic efficiency of the WHR-ORC rises monotonously with increasing pressure and is maximized when the latter takes its highest value. The initial decrease of the ηex at the lower range of the supercritical operating pressures can be again attributed to the non continuous increase of the maximum operating temperature of the ORC. Under both subcritical and supercritical conditions, Pentane exhibits the highest exergetic efficiency (43.17 and 46.49% respectively). Nevertheless, for evaporating pressures below 25 bar, hexane has a consistently higher efficiency of around 40%. This is in accordance with the relation between the 21 Exergetic efficiency (%) Exergeticc efficiency (%)PDF Image | Thermodynamic investigation of waste heat recovery
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