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4.1 Thermodynamic analysis 53 1500 1000 500 0 100 150 200 250 300 350 400 o AA, BCA T =50 C c o c LA T =50 CA, AH T =50 C c o AA, BCA T =100 C c o LA T =100 C c o CA, AH T =100 C c C o o Critical temperature, [ C] 6000 5000 4000 3000 2000 1000 0 C 250 300 o LS T =50 C c o CS T =50 C c o LS T =100 c o CS T =100 C c (a) o Critical temperature, [ C] (b) 350 400 30 25 20 15 10 5 0 FC T c o =50 C FC T c o =100 C 100 120 140 160 180 200 o Critical temperature, [ C] (c) Figure 4.4: Relation between the critical temperature and the process expansion ratio with hydro- carbons (a), siloxanes (b), and fluorocarbons (c). Two different condensing temperatures of 50 °C and 100 °C were considered by the low vapor density at the low pressure side of the process. The volumetric flow rate is closely connected to the sizing of the heat exchangers at the cycle low-pressure side, namely on the sizing of the recuperator and condenser. Therefore, a large volumetric flow rate is estimated to lead to the use of large-sized heat exchangers on the process low pressure side when compared to the fluids having a low volumetric flow rate. 4.1.4 Enthalpy change over the turbine The results of the relation between the critical temperature and the enthalpy change over the turbine are presented in Figure 4.5a and Figure 4.5b. The enthalpy change over the turbine is important parameter because it has a large impact on the turbine design, mainly on the selection of the number of turbine stages and on the turbine rotational speed. The Expansion ratio, [−] Expansion ratio, [−] Expansion ratio, [−]PDF Image | WORKING FLUID SELECTION AND DESIGN OF SMALL-SCALE WASTE HEAT RECOVERY SYSTEMS BASED ON ORGANIC RANKINE CYCLES
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