## 3 Results and Discussion
The pressure of the working fluid in the pump is compressed to 20 bar. It is assumed that the pump and turbine in the cycle are isentropic. An amount of 865 kW of thermal energy from the FG was used to increase the temperature of the fluid. The temperature of the fluid after the evaporator is 435 K. In the turbine, the fluid expands to the condenser pressure. Finally, the fluid at 200 K temperature is condensed and the cycle is completed. Figure 2 depicts a schematic of energy flows that illustrates potential interconnections between the district-level gas, heat, and electricity networks. Because of the close connections between the networks, oxygen, and electricity, an integration analysis is necessary to represent the heat HX networks. Any type of energy conversion component should be able to be included in the model, and it should be able to evaluate how it affects the technical functioning, flows, and losses of every network. In the end, this would also enable the computation of energy costs, carbon emissions, and energy efficiency in addition to a Sankey diagram depicting the energy flows over several networks under various circumstances. According to the Sankey diagram in Figure 5, it is seen that 610 kW of the 3006.5 kW thermal energy of the FG can be recovered as electrical energy. In addition, it is observed that a total of 854 kW of thermal energy is wasted into the atmosphere from the HXs. It turns out that 1048 kW of thermal energy is transferred to the oxygen line to be used in the combustion processes that require enrichment with oxygen in other units in the facility. While there is 766.62 kW of thermal energy to produce a network in the SRC, this value has increased to 1535.23 kW thanks to the application of reheating, resulting in a network generated of 337.2 kW. In the proposed system, FG thermal energy was used first in SRC, then in ORC, and finally in KC, according to temperature classification. It is thought that a significant amount of thermal energy thrown into the atmosphere from the HXs in this system can be used in various industrial applications according to the temperature classification. Figure 4: T\(-\)s diagram of ORC. To observe system reaction in relation to pressure, temperature, and mass flowrate, thermal analysis is necessary. This part presents the optimization of the proposed system, including the net power production determined by temperature difference, the total system thermal efficiency, and the costs associated with energy generation. Table 5 presents the values derived from the combined cycles as a consequence of the parametric analysis. [PERSON] et al. (2021) provide a reference for determining turbine inlet temperature (TIT) and SRC pressure. For the SRC, the mass flow rate is determined to be 0.24 kg/s, while the TIT is 873 K, and its pressure is 150 bar. The mass flow rate resulted in a 333.5 kW SRC net power output. The SRC's working fluid has a turbine output temperature of 369.5 K and a pressure of 0.7 bar [29]. Based on these parameters, the temperature at the boiler entrance was determined. The fluid enters the boiler with a steam quality of x = 0. There is a constant pressure heat intake in the SRC evaporator. Figure 5: Schematic energy flow in the system. \begin{table}
\begin{tabular}{c c c c c c} \hline
**Stream** & **T [K]** & **P [bar]** & **h [kJ/kg]** & **S [kJ/kgK]** & **\(\dot{\text{m}}\) [kg/s]** \\ \hline  
\hline \end{tabular}
\end{table} 
Table 5: Mass and energy balance of the proposed system. EES was used to determine the thermodynamic parameters (enthalpy, entropy, and specific volume) based on this input data. Operating under the current conditions, SRC produces turbines with an output power of 337.2 kW and an efficiency of 0.34. Every SRC component's equipment acquisition cost was determined.