With the elasticity considered further, [PERSON] et al. theoretically calculated the flow of a Phan-Thien-Tanner fluid in a channel with a temperature difference between the wall and the fluid from the inlet [37]. The results correct the expressions of the Nusselt number and the friction factor for the non-Newtonian fluids. The corrections are shown to be dependent less on the viscous dissipation but largely on the elasticity that is represented by the Weissenberg number. [PERSON] et al. used control volume finite difference method to solve the flow of non-Newtonian fluids described by Ostwald-de Waele power law in circular channels, but with the consideration of the wall slip [38]. The results demonstrate that the change on the Nusselt number due to the slip and no-slip is particularly pronouncing for higher power index. As the slip coefficient increases, the center-line velocity decreases but the Nusselt number increases. The flow of non-Newtonian fluids in channel bends has been studied systematically, but with no heat transfer involved. [PERSON] et al. used lattice Boltzmann method to simulate the flow of Herschel-Bulkley fluids in 90\({}^{\circ}\) bent circular channels, with the power-law index, yield stress and the curvature radius of the channel varied [39]. They concluded that the flow resistance increases with the power index, yield stress and the curvature radius, while the additional pressure loss due to the bend reduces with the curvature radius. The bend introduces the Dean vortex secondary flow, whose intensity decreases as the yield stress or the power index increases, because the larger viscosity hinders the centrifugal force. [PERSON] et al. derived an analytical expression for the velocity profile of a Bingham fluid in a two-dimensional curved pipe [40]. As the Bingham number increases, the fluid velocity and stress at the inner wall decreases. For a fixed Bingham number, the width of the unyielded plug is smaller for the larger curvature. [PERSON] et al. numerically solved the flow of shear thickening fluids in a pipe with curvature [41]. Since the flow in the bend part is not fully developed when the curvature radius is small, the numerical friction factor was demonstrated to be much greater than the classical empirical predictions given by [PERSON] and [PERSON]. They concluded a new experienced expression for the friction factor based on two shear thickening rheological models: the power-law model and Quadratic model, respectively. In this study, we used CFD approach to simulate the flow of non-Newtonian coal slurries in straight and curved channels at different conveying rates and under different thermal isoflux on the wall. In the formulas employed in the simulations, the thermal conductivity of the fluid is only a function of temperature, while the viscosity is dependent on both shear rate and temperature. In straight channels, we studied the temperature distribution at the cross section, and the pressure drop that is affected by the temperature since the viscosity changes as the heat transfer processes. In the curved channels, we looked at the secondary flow structures in the bend and the impacts of heat transfer, which, to our knowledge, have not been specifically addressed in earlier studies.