The steady-state turbulent heat transfer coefficients in a short vertical Platinum (Pt) test tube for the flow velocities (u=4.01 to 13.62 m/s), the inlet liquid temperatures (T_<in>=294.00 to 304.29 K), the inlet pressures (P_<in>=802.12 to 859.08 kPa) and the increasing heat inputs (Q_0exp(t/τ), exponential periods, τ, of 6.04 to 25.67 s) were systematically measured by an experimental water loop comprised of a multistage canned-type circulation pump with high pump head. Measurements were made on a 59.2 mm effective length and its three sections (upper, mid and lower positions), which was spot-welded four potential taps on the outer surface of a 6 mm inner diameter, a 69.6 mm heated length and a 0.4 mm thickness of the Pt test tube. The outer surface temperature distribution of the Pt test tube was also simultaneously observed by an infrared thermal imaging camera at intervals of 3 seconds. Theoretical equations for turbulent heat transfer in a circular tube of a 6 mm in diameter and a 636 mm long were numerically solved for heating of water with heated section of a 6 mm in diameter and a 70 mm long by using PHOENICS code under the same condition as the experimental one considering the temperature dependence of thermo-physical properties concerned. The surface heat flux, q, and the surface temperature, T_s, on the circular tube solved theoretically were compared with the corresponding experimental values on heat flux, q, versus the temperature difference between heater inner surface temperature and liquid bulk mean temperature, ΔT_L [=T_s-T_L, T_L=(T_<in> + T_<out>)/2], graph. The theoretical solutions of q and ΔT_L are almost in good agreement with the corresponding experimental values of q and ΔT_L with the deviations less than ±10 % for the range of ΔT_L tested here. The theoretical solutions of local surface temperature, (T_s)_z, local average liquid temperature, (T_<f,av>)_z, and local liquid pressure drop, ΔP_z, were also compared with the corresponding experimental data on (T_s)_z, (T_<f,av>)z and ΔP_z versus heated length, L, or distance from inlet of the test section, Z, graph, respectively. The theoretical solutions of local surface temperature, (T_s)z and local average liquid temperature, (T_<f,av>)_z are within ±10 % of the corresponding experimental data on (T_s)_z and (T_<f,av>)_z, although those of local liquid pressure drop, ΔP_z, become 37.6 % lower than the experimental ones. It was confirmed in this study that authors' steady-state turbulent heat transfer correlation, Eq. (1), based on the experimental data (Hata and Noda, 2008) Nu_d=0.02Re^<0.85>_dPr^<0.4>(L/d)^<-0.08>(μ_1/μ_w)^<0.14> (1) can not only describe the experimental data of steady-state turbulent heat transfer but also the theoretical solutions within ±10 % difference for the wide ranges of temperature differences between heater inner surface temperature and liquid bulk mean temperature (ΔT_L=5 to 200 K) and flow velocity (u=4.01 to 13.62 m/s).