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Additional info for Advances in Multiphase Flow and Heat Transfer, Volume 2
Piela et al.  found that the phase inversion point did not depend on Reynolds, Weber or Froude numbers or the injection velocity of the dispersed phase when the mixture velocity was sufficiently large (above 2m/s in their system). It did, however, depend on the injection phase volume fraction, χ. Phase Inversion in Liquid-Liquid Pipe Flows Advances in Multiphase Flow and Heat Transfer Vol. 2 (2009) 47 This seems to suggest that phase inversion depends on the morphology/size of the dispersed phase; a lower addition rate of the dispersed phase allows the drops to break up and perhaps makes them more stable against coalescence that would lead to the larger region structures and to phase inversion.
These fluctuations lasted for about 350 s and during this time the average value of the signal changed from low (indicating oil continuous phase) to high (indicating water continuous phase). After this time the fluctuations reduced significantly and the conductivity value settled to that of a water continuous mixture. Similar behaviour can be seen in Fig. 4b for the pressure drop. Again pressure drop fluctuated significantly for about 350 s before settling to a new, lower, value where the fluctuations were very small.
Design, vol. 199, pp. 243-255, 2000. K. Vierow and V. E. Schrock, “condensation in a natural circulation loop with noncondensable gas present: Part I - Heat transfer”, Japan - U. S. ) 1992. S. Z. E. F. Peterson, “An investigation of condensation from steam–gas mixtures flowing downward inside a vertical tube”, Nuclear Eng. Design, vol. 177, pp. 53–69, 1997. H. Araki, Y. Kataoka and M. Murase, "Measurement of condensation heat transfer coefficient inside a vertical tube in the presence of noncondensable gas", J.