It is shown that for both channels, the wall temperatures increase along the flow direction and attain

a horizontal asymptote at the downstream flow. For the channel 41, all the measurement locations show a very low wall temperature variation (approximately isotherm) along the channel, leading a uniform distribution of the big bubbles along the channel. Wall temperature distribution along the channel is related to the boiling flow structure where it increases with the size of the bubbles in the channel. Moreover, three zones along the flow direction are observed as shown in Figure 7. The first zone (Figure 7a) is at the channel entrance where the nucleate boiling begins and a small number of isolated bubbles move just after their apparition https://www.selleckchem.com/products/tpca-1.html along the liquid flow. The first zone length may be reduced by decreasing the fluid mass flow rate or by increasing the heat flux. Bubbles leaving the first zone combine with bubbles formed in the second zone (Figure 7b)

to form bigger bubbles occupying the middle KU55933 molecular weight part of the channel. The increase of the bubble size decreases the contact of water with the heat exchange surface and increases the wall temperature. At the upstream flow, a third zone is observed (Figure 7c), where the temperature and void fraction attain their maximum values causing probably a partial dry regions near the channels’ outlet. As a result, wall temperature and local vapor quality increase along the flow direction. Figure 6 Wall temperature measurements of channels 1 and 41 with 348 kg/m 2 s pure water mass flux at (a) 8-mm depth and (b) 0.5-mm depth. Figure 7 Boiling flow pattern at different locations along the flow direction. (a) x ≤ 80

mm, (b) 60 mm ≤ x ≤ 110 mm, and (c) 100 mm ≤ x ≤ 160 mm. The effect of the water mass flux on the wall temperature evolution is presented in Figure 8a,b. The profiles of wall temperatures measured at the first and 41th channel along the flow direction using microthermocouples located at 0.5 mm below the heat exchange surface are shown. The pure water mass fluxes for these profiles are 174, 261, 348, 435, and 566 kg/m2s, where the total power supplied Fluorouracil to the heated plate is 200 W. Figure 8a shows a strong dependence of the wall temperature on the liquid’s mass flux. As the liquid’s mass flux increases, the wall temperature decreases and vice versa. Moreover, all the curves attain a horizontal asymptote at the end of the channel length, i.e., at the maximum local vapor quality. In addition, it can be noticed that the zone’s length where the wall temperature becomes asymptotic increases as liquid’s mass flux decreases and vice versa. In fact, for the same heat flux, the decrease of the mass flow rate increases both the local void fraction and the local wall temperature.