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Energies 2020, 13, 4014 10 of 18 4. Transcritical Cycles with Mixtures of Carbon Dioxide It is possible to vary the critical point of the resulting mixture of two fluids in different proportions and consequently alter its thermodynamic and thermophysical properties. Therefore, it is possible—at least in principle—to find the correct working fluid for any application [25]. For example, it is possible to produce condensation in hot environments or to control the pressure expansion ratio or the minimum and maximum pressures [38–41]. In particular, mixtures of carbon dioxide as working fluids in closed power cycles have already been considered by some authors in the past [42–45]. Figure 9a shows the pressure–temperature (P–T) envelopes for different mixtures of carbon dioxide (component 1) and propane (component 2) evaluated by Aspen Plus⃝R V9. The critical locus is calculated by a code based on the approach described in [46], where the Peng–Robinson equation of state in its simpler and original formulation has been implemented [47] (pp. 208, 423). The experimental points available in the data bank of Aspen Plus⃝R V9 are reported for comparison. The developed code is capable of computing both stable and metastable critical points at given composition of any binary mixture without any initial estimation. In Figure 9b, we present the P–T envelopes and critical loci for mixtures of carbon dioxide and the refrigerant R134a. With the composition of the mixture, the critical temperature and the critical pressures change continuously from that of pure carbon dioxide (z1 = 1.0) to that of pure R134a (z1 = 0.0). At z1 = 0.7, the critical temperature is about 60 ◦C and the critical pressure is 70 bar, thus allowing condensation with a bubble temperature of 35 ◦C. Figure 10a,b shows values of the thermodynamic cycle efficiency ηth and of the total efficiency η = ηthφ as a function of the maximum cycle pressure, respectively, for mixtures of carbon dioxide and R134a. (a) (b) Figure 9. Pressure–temperature (P–T) envelopes and critical loci for mixtures of carbon dioxide. The symbols represent experimental points from different data sets in Aspen Plus⃝R V9. (a) Carbon and propane. (b) Carbon dioxide and refrigerant R134a. The mixture corresponding to z1 = 0.7, at P3 = 200 bar yields an η equal to 0.143—a value only slightly lower than the optimum value for the pure R134a (0.15), but with a halved expansion ratio, as shown in Figure 11. On the other hand, a carbon dioxide cycle with a maximum pressure of 200 bar has a total efficiency of only 0.107.PDF Image | CO2 Mixtures as Working Fluid for High-Temperature Heat Recovery
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