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Energies 2020, 13, 2259 6 of 24 Energies 2020. 13. x FOR PEER REVIEW 6 of 26 Figure 2. Entropy Temperature (T-s) diagram of organic fluids. Figure 2. Entropy Temperature (T-s) diagram of organic fluids. According to Equation (1), the fluid type is defined based on the slope of the saturation line. According to Equation (1), the fluid type is defined based on the slope of the saturation line. This This slope classifies the working fluids by value of E = ∂s obtaining for dry fluids E > 0 isentropic ∂s ∂T slope classifies the working fluids by value of Ε = obtaining for dry fluids Ε > 0 isentropic fluids, E ≈ 0, and wet fluids E < 0 [37]. ∂T fluids, Ε ≈ 0, and wet fluids Ε < 0 [37]. Cp n·T−T+1 H rH 𝐶𝑛∙𝑇−𝑇+1 E= 𝑝− 𝐻 𝑟𝐻 ∆HH (1) where T𝑇 r𝑟H𝐻 𝑇T 𝐻H is the enthalpy of evaporation. 2.3. Thermodynamic Analysis - - - - - - - The components were assumed as open systems in a stable state condition. 𝑇C 𝐶 Ε= − 2 𝛥𝐻 (1) TH TH2·(1 − TrH) 𝐻 𝑇 𝑇∙(1−𝑇) 𝐻 𝐻 𝑟𝐻 , , and ∆𝛥𝐻H T 𝐻H TheconsiderationadoptedforcarryingoutthecombinedBraytonS-CO andORCthermodynamic The consideration adopted for carrying out the combined Br2ayton S-CO2 and ORC modeling are listed below [29]: thermodynamic modeling are listed below [29]: = 2.3. Thermodynamic Analysis - - - - - - - To .calculate the working fluid exergy as.a function of the ambient conditions, Equation (3) is where Q is the heat at the boundary in kW, W is the conversion of energy by work in kW, h is the The components were assumed as open systems in a stable state condition. The atmospheric temperature and pressure were set to 25 °C and 101.3 kPa, respectively. The atmospheric temperature and pressure were set to 25 ◦C and 101.3 kPa, respectively. The kinetic and potential energy was not considered in the energy balance. The kinetic and potential energy was not considered in the energy balance. The Brayton-CO2 compressor is studied under similar turbine conditions. The Brayton-CO2 compressor is studied under similar turbine conditions. The consequences of pressure fluctuations are not known. The consequences of pressure fluctuations are not known. Pressure drops in the tubing are not known. Pressure drops in the tubing are not known. Pressure drops in structure heat exchangers are estimated depending on the geometry and Pressure drops in structure heat exchangers are estimated depending on the geometry and flow flow regime characteristics. regime characteristics. The energy balance in steady-state for the devices is presented in Equation (2) The energy balance in steady-state for the devices is presented in Equation (2) ̇̇ 𝑄−𝑊+∑𝑚̇𝑖𝑛 ·h𝑖𝑛 −∑𝑚̇𝑜𝑢𝑡 ·h𝑜𝑢𝑡 =0 (2) ̇ ...̇. where 𝑄 is the heat at the boundary in kW, 𝑊 is the conversion of energy by work in kW, h is the Q−W+ min·hin− mout·hout =0 (2) specific enthalpy value for the working fluid in kJ/kg·K, and 𝑚̇ is the mass flow rate in kg/s. . specific enthalpy value for the working fluid in kJ/kg·K, and m is the mass flow rate in kg/s. 𝑒=h−h+𝑇𝑠−𝑇𝑠 (3) 𝑖𝑖0000𝑖 used.PDF Image | S-CO2 Brayton Cycle Coupled with ORC as Bottoming Cycle
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