docs: def turbulent_Sieder_Tate(Re, Pr, mu=None, mu_w=None):
      r'''Calculates internal convection Nusselt number for turbulent flows
      in pipe according to [1]_ and supposedly [2]_.
  
      .. math::
          Nu = 0.027Re^{4/5}Pr^{1/3}\left(\frac{\mu}{\mu_s}\right)^{0.14}
  
      Parameters
      ----------
      Re : float
          Reynolds number, [-]
      Pr : float
          Prandtl number, [-]
      mu : float
          Viscosity of fluid, [Pa*s]
      mu_w : float
          Viscosity of fluid at wall temperature, [Pa*s]
  
      Returns
      -------
      Nu : float
          Nusselt number, [-]
  
      Notes
      -----
      A linear coefficient of 0.023 is often listed with this equation. The
      source of the discrepancy is not known. The equation is not present in the
      original paper, but is nevertheless the source usually cited for it.
  
      Examples
      --------
      >>> turbulent_Sieder_Tate(Re=1E5, Pr=1.2)
      286.9178136793052
      >>> turbulent_Sieder_Tate(Re=1E5, Pr=1.2, mu=0.01, mu_w=0.067)
      219.84016455766044
  
      References
      ----------
      .. [1] Rohsenow, Warren and James Hartnett and Young Cho. Handbook of Heat
         Transfer, 3E. New York: McGraw-Hill, 1998.
      .. [2] Sieder, E. N., and G. E. Tate. "Heat Transfer and Pressure Drop of
         Liquids in Tubes." Industrial & Engineering Chemistry 28, no. 12
         (December 1, 1936): 1429-35. doi:10.1021/ie50324a027.
      '''
      Nu = 0.027*Re**0.8*Pr**(1/3.)
      if mu_w and mu:
          Nu *= (mu/mu_w)**0.14
      return Nu