## 2 Materials and Methods
### System Design  
The FG rejected from the AF at a temperature of 1093.15K transfers its heat to the RC evaporator through HX1 (point a). In the RC, water is compressed in the pump from 369.5 K and 0.7 bar to 373.18 K and 150 bar. Afterwards, it is heated to 873 K with the heat recovered from the FG in the evaporator and transitions to the superheated vapor phase. The superheated steam exits as a saturated liquid at 369.5 K and 0.7 bar through the intermediate heated turbine. Afterwards, the condensation energy in the RC condenser is transferred to the CO\({}_{2}\) cycle at constant pressure. Afterwards, the FG enters the ORC evaporator (HX3) at 661.4 K (point b). R245 fa is used as the working fluid in ORC, is compressed from 298 K 1.5 bar to 299 K 20 bar in the pump. Afterwards, it is heated to 435 K using the heat recovered from the FG in the ORC evaporator. In the superheated vapor phase, R245 fa expands in the turbine to 416 K and 1.5 bar. Afterwards, it is cooled at 298 K at constant pressure in the ORC condenser. FG enters the KC evaporator at 461 K (HX4) and transfers its waste heat to the ammonia water mixture. The working fluid of the KC is a binary combination of ammonia and water that goes through a special mechanism to change the ammonia content all throughout the system. Heat recovery efficiency is greatly increased by this procedure. The addition of ammonia permits boiling at lower temperatures, allowing for the effective use of waste heat. After that, a heat exchanger (HX4) is used to transfer the energy from flue gas remaining to the binary working fluid (NH\({}_{3}\)-H\({}_{2}\)O mixture) of the KC. The energy that is produced is then used to power the KC, which generates electricity using standard methods. The pump, separator, turbine, regenerator, expansion valve, mixer, condenser, and steam generator are the essential parts of the KC, as shown in Figure 1. At state point 17, the NH\({}_{3}\)-H\({}_{2}\)O combination's liquid and vapor mixture enter the separator. The separator's job is to fully separate the vapor and liquid; at state point 18, which is the turbine entry, the mixture bifurcates into a rich combination of NH\({}_{3}\)-H\({}_{2}\)O and a lean mixture at state 20. In order to generate power, the turbine expands the rich NH\({}_{3}\)-H\({}_{2}\)O combination to a low condensation pressure. The rich mixture from the turbine discharge enters the mixer at state point 19, while the weak mixture of NH\({}_{3}\)-H\({}_{2}\)O exiting the separator (state 20) passes through the regenerator, where it releases energy into the NH\({}_{3}\)-H\({}_{2}\)O mixture's basic solution. The basic solution then enters the heat recovery vapor generator (HX4) at state point 17. At state point 21, the weak combination then experiences a decrease in temperature. Allowing the weak mixture to expand through the valve lowers its temperature even more (state 24). The rich mixture and weak mixture combine in the mixer to create the high-energy basic solution of the NH\({}_{3}\)-H\({}_{2}\)O combination (State 22). The condenser is now subjected to the high energy basic solution, which discharges at state 23 (HX6). At state 16, the condensed NH\({}_{3}\)-H\({}_{2}\)O combination is pumped to the vapor generator. The ammonia-water mixture's temperature, pressure, and concentration at the turbine's inlet are all kept constant during the KC. By doing this, the steady heat input required to keep the KC running is guaranteed. By modifying the mass flow rate of the NH\({}_{3}\)-H\({}_{2}\)O mixture in the KC, variations in the amount of heat delivered by the FG are offset. Finally, all cycles release their waste heat using C1, C2, and C3 to the pure oxygen line, which is used to enrich the oxygen available in the factory. Using the Engineering Equation Solver (EES V10 561 3D), a mathematical model is created to examine the integration of waste heat and the power cycles [15].