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Energies 2020, 13, 2447 5 of 18 calculation is to determine the amount of waste heat and its parameters. To make the calculations, it was decided to use the data achieved in a previous preformed analysis [2]. As the amount of waste heat and its parameters during the year did not differ significantly for particular compressor units, it was decided to use the average parameters of flue gases. Table 1 shows the exhaust gas average properties and mole fraction of each component. Table 1. Exhaust gases average properties [2]. Component of Wet Waste Gases Molar Participation (% mol) 5.10 9.40 73.55 11.95 Carbon dioxide Oxygen Nitrogen Water vapor Stream parameters Mh = 3.55 kg/s TIN = 616.38 K To compare the performance of different cycle operation parameters under the same exhaust gas conditions, the working out of a thermodynamic model was preceded by the following assumptions: • The maximum operating pressure is limited to 22.5 MPa (compressor outlet pressure) in order to avoid high capital costs and to create a realistic S-CO2 power cycle model. The maximum temperature (turbine inlet temperature) is limited by the exhaust gas temperature. • Constant temperature and pressure of working medium at the compressor inlet were assumed. The values of 35 ◦C (308.15 K) and 7.7 MPa were appropriately assumed to assure that the heat sink temperature is not very far from the ambient temperature while the fluid in the cycle maintains the supercritical state. • Compression and expansion of the S-CO2 is an adiabatic process. • The temperature difference between CO2 and flue gas at the heat exchanger inlet and outlet is always constant for the analyzed variant. • The limit temperature to which exhaust gases can be cooled is 100 ◦C (373.15 K). • Irreversibilities such as due to turbine and compressor isentropic efficiencies, finite temperature differences, pressure losses in the heat exchanger and recuperator were also considered so as to generate thermodynamic data for real cycles. For the sensitivity analysis of cycles, component efficiency and heat exchanger effectiveness are based on the literature review. For convenience, the pressure losses in each heat exchanger and recuperator are considered as 0.5% of the inlet pressure. Pressure losses in exhaust gas side are neglected in this paper because it has practically no effect on the energy efficiency of the system. However, it should be remembered that in reality the heat exchanger must be chosen in such a way that the pressure drops of the exhaust gases do not exceed the limit value given by the manufacturer of the compressor unit. In the case of the compressor station under consideration, the value for installed machines is 100 kPa. The model of S-CO2 cycle was prepared with the use of CoolProp [24] and REFPROP [25] database. Table 2 shows the S-CO2 assumptions and constraints. For the purposes of this section, all subscripts represent the cycle stages, as in Figure 1. As already mentioned, compression stage is treated as adiabatic process because the heat losses are negligible. Due to this assumption, and information about pressure and temperature of CO2 at the inlet to the compressor, as well as the desired value of pressure at the outlet from the compressor, it is possible to calculate the actual temperature of CO2 after compression which is given by Equation (1): T2′ = T2 − T1 + T1 (1) ηcPDF Image | Supercritical CO2-Brayton Cycle Nat Gas Compression Station
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