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Energies 2020, 13, 4014 15 of 18 the simple supercritical carbon dioxide cycle which presented a total efficiency of 0.12 at the same maximum pressure. • Moreover, in comparison with pure R134a Rankine cycles, the transcritical cycle with a CO2-R134a mixture (0.3 mole fraction of R134a) yielded the same total efficiency but with almost half the expansion ratio. In summary, the transcritical cycle with the CO2-R134a mixture (0.3 mole fraction of R134a) showed a good compromise between the simple R134a Rankine cycle and simple supercritical carbon dioxide cycles due to its good thermodynamic efficiencies, lower maximum operating pressures, lower expansion enthalpy drop and reasonable turbine volume flow ratios. The standard enthalpy of formation per bond is proposed as a rough indicator of the thermal stability of the considered working fluids with reference to pure carbon dioxide; furthermore, a correlation to estimate the binary interaction parameters for carbon dioxide binary mixtures for which experimental VLE data are not available is suggested. This allows the calculation of thermodynamic properties, critical points and P–T envelopes of some new carbon dioxide mixtures and preliminary calculations of the thermodynamic performance of cycles. In this way, is it possible to analyze a broad spectrum of carbon dioxide mixtures to select the most promising components and—only after this preliminary analysis—to carry out the necessary experimental liquid–vapor measurements. As in all transcritical and supercritical power cycles, the efficiency of the recuperator plays an importantrole,astherecoveredheatisgenerallyveryhigh.Forexample,theratioQ ̇R/W ̇ isabout4.5 for simple supercritical carbon dioxide cycles at a maximum pressure of 250 bar and about 2.9 for the mixture CO2 (0.7)-R134a (0.3). The use of mixture of carbon dioxide in transcritical power cycles seems a promising solution to obtain (i) reasonable global efficiencies at a reasonable maximum pressure and (ii) with a conceptually simple plant configuration. On the other hand, points to investigate for a better design of the engine are (i) the vapour–liquid equilibria at different temperatures and pressures and, given the important role of the heat exchangers and of the turbomachines, (ii) the main transport properties (viscosity and thermal conductivity) of the most promising mixtures—properties that, for mixtures, are not simple to estimate properly for all of the relevant thermodynamic conditions. Author Contributions: Author Contributions: conceptualization, C.M.I.; methodology, C.M.I.; software, A.A., C.M.I.; investigation, A.A., C.M.I.; writing—original draft preparation, A.A., C.M.I.; revision and final editing, G.D.M., P.I. G.M. All authors have read and agreed to the published version of the manuscript. Funding: This research received no external funding. Conflicts of Interest: The authors declare no conflict of interest. Abbreviations The following abbreviations, symbols and subscripts are used in this manuscript: CP CV m ̇ H MITAR MITAPHE MITAC PC Pc Q ̇ R R rC rT Heat capacity at constant pressure (kJ kg−1 K−1) Heat capacity at constant specific volume (kJ kg−1 K−1) Mass flow rate of the flu gas (kg s−1) Minimum Internal Temperature Approach in the recuperator (◦C) Minimum Internal Temperature Approach in the primary heat exchanger (◦C) Minimum Internal Temperature Approach in the radiator/condenser (◦C) Condensation pressure (bar) Critical pressure (bar) Recovered thermal power in the recuperator (kW) Gas constant (kJ kg−1 K−1 ) Compression ratio (P2/P1) Expansion ratio (P3/P4)PDF Image | CO2 Mixtures as Working Fluid for High-Temperature Heat Recovery
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