docs: def Aggour(m, x, alpha, D, rhol, Cpl, kl, mu_b, mu_w=None, L=None, 
             turbulent=None):
      r'''Calculates the two-phase non-boiling laminar heat transfer coefficient  
      of a liquid and gas flowing inside a tube of any inclination, as in [1]_  
      and reviewed in [2]_.
  
      Laminar for Rel <= 2000:
  
      .. math::
          h_{TP} = 1.615\frac{k_l}{D}\left(\frac{Re_l Pr_l D}{L}\right)^{1/3}
          \left(\frac{\mu_b}{\mu_w}\right)^{0.14}
      
      Turbulent for Rel > 2000:
      
      .. math::
          h_{TP} = 0.0155\frac{k_l}{D} Pr_l^{0.5} Re_l^{0.83}
      
          Re_l = \frac{\rho_l v_l D}{\mu_l}
          
          V_l = \frac{V_{ls}}{1-\alpha}
  
      Parameters
      ----------
      m : float
          Mass flow rate [kg/s]
      x : float
          Quality at the specific tube interval [-]
      alpha : float
          Void fraction in the tube, [-]
      D : float
          Diameter of the tube [m]
      rhol : float
          Density of the liquid [kg/m^3]
      Cpl : float
          Constant-pressure heat capacity of liquid [J/kg/K]
      kl : float
          Thermal conductivity of liquid [W/m/K]
      mu_b : float
          Viscosity of liquid at bulk conditions (average of inlet/outlet 
          temperature) [Pa*s]
      mu_w : float, optional
          Viscosity of liquid at wall temperature [Pa*s]
      L : float, optional
          Length of the tube, [m]
      turbulent : bool or None, optional
          Whether or not to force the correlation to return the turbulent
          result; will return the laminar regime if False
  
      Returns
      -------
      h : float
          Heat transfer coefficient [W/m^2/K]
  
      Notes
      -----
      Developed with mixtures of air-water, helium-water, and freon-12-water and 
      vertical tests. Studied flow patterns were bubbly, slug, annular, 
      bubbly-slug, and slug-annular regimes. Superficial velocity ratios ranged 
      from 0.02 to 470.
  
      A viscosity correction is only suggested for the laminar regime. 
      If the viscosity at the wall temperature is not given, the liquid viscosity
      correction is not applied.
  
      Examples
      --------
      >>> Aggour(m=1, x=.9, D=.3, alpha=.9, rhol=1000, Cpl=2300, kl=.6, mu_b=1E-3)
      420.9347146885667
  
      References
      ----------
      .. [1] Aggour, Mohamed A. Hydrodynamics and Heat Transfer in Two-Phase 
         Two-Component Flows, Ph.D. Thesis, University of Manutoba, Canada 
         (1978). http://mspace.lib.umanitoba.ca/xmlui/handle/1993/14171.
      .. [2] Dongwoo Kim, Venkata K. Ryali, Afshin J. Ghajar, Ronald L. 
         Dougherty. "Comparison of 20 Two-Phase Heat Transfer Correlations with 
         Seven Sets of Experimental Data, Including Flow Pattern and Tube 
         Inclination Effects." Heat Transfer Engineering 20, no. 1 (February 1, 
         1999): 15-40. doi:10.1080/014576399271691.
      '''
      Vls = m*(1-x)/(rhol*pi/4*D**2)
      Vl = Vls/(1.-alpha)
      
      Prl = Prandtl(Cp=Cpl, k=kl, mu=mu_b)
      Rel = Reynolds(V=Vl, D=D, rho=rhol, mu=mu_b)
  
      if turbulent or (Rel > 2000 and turbulent is None):
          hl = 0.0155*(kl/D)*Rel**0.83*Prl**0.5
          return hl*(1-alpha)**-0.83
      else:
          hl = 1.615*(kl/D)*(Rel*Prl*D/L)**(1/3.)
          if mu_w:
              hl *= (mu_b/mu_w)**0.14
          return hl*(1-alpha)**(-1/3.)