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Sustainability 2015, 7 15378 also low for this system, and this can be attributed to the low temperature differences between the environment and the working fluid at the input state (see Table 1). There are large improvement potentials for the boiler and the expander. The system using toluene has the lowest power production and has a large exergy destruction rate in the expander. The systems using iso-pentane and n-pentane have similar exergy destruction rates for the expander and the boiler. This is due to their similar chemical makeup of the working fluids. Note, however, that the exergy destroyed in the condenser is higher for the system using n pentane than the one using iso-pentane. Table 6 shows the exergy destruction breakdowns for the systems using various working fluids. These results can help guide the selection of working fluid. Table 6. Working fluid exergy destruction percentage breakdown. Working Fluid R134a R123 R227ea R245fa R600 Iso-butane Iso-pentane n-pentane Toluene Exergy Destruction (% of Total in System) Boiler Expander 59.67 32.18 65.44 25.76 56.31 29.14 64.53 25.99 59.77 30.79 57.91 32.07 63.16 26.46 64.16 25.61 44.54 49.85 Condenser Pump Regenerator 0.3 0.61 7.25 0.35 0.08 8.37 0.66 0.53 13.38 0.09 0.13 9.25 0.28 0.24 8.92 0.25 0.39 9.37 0.25 0.09 10.04 0.58 0.06 9.59 1.05 0.04 4.52 4.2. Exergo-Economic Analysis The exergo-economic cost balance equations are used in the analysis to determine the unit cost rate of electricity for an optimized exergy efficiency. The equation for exergy efficiency depends on the electrical power output and the heat input rate. The maximized value of exergy efficiency does not necessarily represent the maximum power output for the system at a particular pressure ratio. Optimizing the cost of electricity for systems using R134a and iso-butane is done by requiring EES to minimize the function for ce (electricity unit cost rate), which is found in the cost rate balance for the expander. The same two independent variables, pressure ratio and superheat, are used. The bounds for the analysis do not change. Five unit exergy costs for input heat are considered: 0.001, 0.002, 0.004, 0.006 and 0.008 USD/kWh. These costs are used for comparison purposes to assess the sensitivity of the system to such changes. The same assumptions are used as outlined in the exergo-economic analysis section. Figure 6 shows the minimized values for electricity rate for systems using R134a and iso-butane.PDF Image | Selection of Optimum Working Fluid for Organic Rankine Cycles
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