For the investigation of the non-premixed combustion process, a tabulated combustion model based on the flamelet concept is employed. Multicomponent phase separation processes are considered by means of a minimization of the Gibbs energy. Consequently, real-gas effects are included inherently. Cubic equations of state and the departure function concept form the basis of the thermal and caloric closure. The thermodynamic framework relies on a rigorous and fully conservative description of the thermodynamic state. A double-flux scheme specifically tailored for real-gas flows is the core of the density-based solver. The first comprises different formulations of the pressure equation to cover a wide range of Mach numbers. Both a pressure- and a density-based solver framework are introduced. This work presents a CFD tool that enables the thorough investigation of these processes. Here, especially one thermodynamic topic is of paramount interest within recent years: phase separation processes under initially supercritical conditions. Computational fluid dynamics (CFD) can contribute to a better understanding of the injection, mixing and combustion processes within these types of engines. This arises from the fact, that LREs will remain an essential component for payload launchers in the foreseeable future and that GEs fired with hydrogen or natural gas are a possible solution to gradually diversify towards cleaner energy conversion machines. Driven by the demand for higher efficiency and reduction of pollutants, intensive investments are made in recent years in the further development of especially two types of fuel-fired engines: liquid-propellant rocket engines (LREs) and gas engines (GEs). (14.5) and (13.Injection, mixing and combustion under high-pressure conditions are key processes in modern energy conversion machines. 1982.the equation of state expresses Z as a function of Y and T, as is most oftencase, Eqs. However, Applications to Phase Equilibria, app. Classical Thermodynamics ofNonelectrolyte Solutions: Withoperations of Eqs. (3.31) expresses Z as a function of P and T, the m.,th,em.atiCl! t H. No exactH1< = (-0.05545)(8.314)(323.15) = -149.0 J mol-' theory like that for the virial equations prescribes this composition dependence,S1< = (-0.04040)(8.314) = -0.3359 J mol-' K-' and we rely instead on empirical mixing rules to provide approximate relation- Since Eq. ' The application of cubic equations of state to mixtures requires that the '\" = 0.9851 equation-of-state parameters be expressed as functions of composition. 3.10, PVT equations of state that are cubic in molar volume are capable of describing the behavior of both liquid V = ZRT (0.9850)(8,314)(323.15) = 105850 em' mol-' and vapor phases of pure fluids.