Effect of Surface Biphilicity on FC-72 Flow Boiling in a Rectangular Minichannel

Introduction

With the decrease in the size of ICs (integrated circuits) and increase in their power density, new methods for heat dissipation become inevitable to maintain the working temperature below a critical value. Approaches for dissipating the generated power include natural convection (Florio and Harnoy, 2007), single phase heat transfer (Ahmadi and Erden, 20182018; Ahmadi and Erden, 2020), and forced convection combined with phase change (Hashemi and Noie, 2017; Sadaghiani et al., 2017). Boiling, whether pool boiling or flow boiling, is one of the most promising approaches to dissipate generated high powers and obtaining high heat transfer coefficients (HTC) due to both sensible heat transfer as well as latent heat of vaporization.

Surface wettability is one of the most important parameters affecting two-phase heat transfer due to modifications in the three phase contact line as well as the number of active nucleation sites (Basu et al., 2002). Experimental studies proved that hydrophobic substrates provide higher heat transfer coefficients in flow boiling in micro- (Choi et al., 2011; Kim and Lee, 2019) and minichannels (Phan et al., 2011; Zhao et al., 2021) in comparison with hydrophilic ones. Generally, low energy surfaces (hydrophobic) remarkably augment the onset of nucleate boiling and bubble departure, while high energy surfaces (hydrophilic) enhance liquid replenishment and raises the critical heat flux (Motezakker et al., 2019; Sadaghiani et al., 2020a; Tan et al., 2021). Therefore, recent studies suggest that surface modification is an effective method to improve heat transfer via phase-change heat transfer including droplet evaporation (Dai et al., 2014; Aboubakri et al., 2020), flow condensation (Chehrghani et al., 2021), flow and pool boiling (Shojaeian and Koşar, 2015). For instance, (Sadaghiani et al., 2020a; Sadaghiani et al., 2020b) studied the effect of artificial cavities on three phase contact line and reported an optimum ratio of diameter to pitch distance, which maximized the heat transfer coefficient in pool boiling. Similarly, it was reported that biphilic surfaces resulted in enhancements of pool boiling heat transfer (Motezakker et al., 2019) and flow boiling heat transfer (Ahmadi et al., 2020). According to Honda and Wei (Honda et al., 2002), micro structures such as micro-roughness and micro-porous coatings significantly facilitated the incipience of boiling, while delaying the CHF (critical heat flux). In another study, (Honda and Wei, 2004) conducted pool boiling experiments with FC-72 on silicon substrates modified by micro-pin-fins and obtained noticeable enhancements in the nucleate boiling regime and critical heat flux. Mixed wettability surfaces could be also achieved with surface modification. As an example, Wang et al. (Wang et al., 2019) investigated the effect of mixed wettability on flow boiling of water and reported that mixed wettability surfaces not only increase the nucleation site density but also ease the bubble departure. In the study of Kim et al. (Kim et al., 2018) on the effect mixed wettability surfaces in flow boiling of water, it was shown that hydrophobic stripes, regardless of their direction with respect to the flow direction, provided active nucleation sites. They also concluded that merging and confinement of the bubbles are the major mechanisms enhancing boiling heat transfer. In another study, Kim et al. (Kim et al., 2020) proved that compared to dotted patterns, parallel patterns possessed a better heat transfer performance at low water mass fluxes, while the dotted surfaces outperformed the parallel patterns at high mass fluxes.

Flow boiling is one of the most effective heat transfer methods, especially in micro-scale and could provide a better performance relative to pool boiling as well as single phase flows (Saraceno et al., 2012). Amongst working fluids, the dielectric coolant FC-72 was proposed as a candidate in flow boiling (Kandlikar, 2010). The working coolant FC-72 is a colorless, odorless and non-flammable fluid with thermal and chemical stability. It also has a low toxicity and good compatibility with metals and plastics (Ma and Chung, 2001). Mudawar et al. (Gersey and Mudawar, 1992) conducted subcooled flow boiling experiments with FC-72. They observed that the boiling phenomenon delayed with the flow velocity. Hiendel et al. (Heindel et al., 1992) conducted flow boiling experiments on FC-72 and revealed that heat transfer was enhanced with the fluid velocity for partially developed boiling. However, for fully developed boiling, the effect of velocity was not significant. According to another study with FC-72, the increase in the fluid velocity and subcooling temperature led to reduced temperature excursion and boiling hysteresis (Samant and Simon, 1989). Martin-Callizo et al. (Martín-Callizo et al., 2007) concluded that even though the heat transfer coefficient generally increased with the heat flux, there was not any dependency for vapor qualities lower than 0.5.

Bubble dynamics study under reduced gravity in flow boiling experiments with FC-72 conducted by Ma and Chung (Ma and Chung, 2001) revealed that the departure time and size decreased with the flow rate. In another study, Yin et al. (Yin et al., 2000) performed flow boiling tests with R134a and demonstrated that the departure size and frequency decreased with liquid subcooling. Maurus et al. (Maurus et al., 2002) concluded that bubble nucleation increased and decreased with the heat flux and mass flux, respectively. Also, the same trend existed for bubble growth rate.

So far, even though pool boiling heat transfer on purposefully modified surfaces has been investigated by many researchers, flow boiling on biphilic surfaces needs further studies. In this regard, this article is the first study, which focuses on biphilic surfaces fabricated with a new method, on flow boiling of FC-72. Although this fluid has wide industrial applications, the information regarding flow boiling is relatively insufficient. The applied polymer, C₄F₈, possesses hydrophobic properties, and its islands constitute the hydrophobic part of the surface. The heat transfer performance and visualization were investigated for different biphilic surfaces in the following sections. It should be noted that since the hydrophobic surfaces typically provide higher heat transfer coefficients (Choi et al., 2011; Phan et al., 2011; Kim and Lee, 2019; Zhao et al., 2021), the heat transfer coefficients obtained from the biphilic surfaces are compared with a hydrophobic surface, which acts as a better reference in this study for comparison purposes.

Experimental Set-Up, Procedure, and Data Reduction

Experimental Set-Up and Test Section

Figure 1 represents the schematic of the closed loop experimental setup used in this study. The components used in this experimental setup consist of a micropump, a flow meter, the test section, a condenser, temperature and pressure sensors, and a reservoir. The test section, which is shown in Figure 1B, consists of an aluminum block enclosed by the Teflon part to reduce heat losses during experiments. Furthermore, in order to measure the pressure and temperature at the inlet and outlet of the test section, two different small reservoirs were designed. The test specimens and a transparent cover are the other parts used in the test section. The aluminum base can house eight heating cartridges, each having a length of 65 mm and a diameter of 6 mm. The test samples were placed in the designed area with dimensions of 51.0 mm × 15 mm. The depth of the channel is 1 mm. Before placing the samples, the designed area was treated with a thermal paste to minimize the contact thermal resistance between the test sample and the aluminum block. The Plexiglas, sealed with a sandwich mechanism, was used for further visualization access. The local temperatures and heat fluxes were acquired under steady state conditions, which were collected by the data acquisition system.

FIGURE 1

FIGURE 1. Schematic of (A) closed loop setup (B) test section (C) thermocouple locations.

Experimental Procedure

FC-72 was used as the working fluid in the experiments. The main physical properties of this fluid are summarized in Table 1. During the experiments, two different mass fluxes were provided by the gear pump. During the experiments, the inlet temperature was kept at 28 ± 1°C. The data acquired from the experimental test section was under steady state conditions. The average values of temperatures provided by the first and second thermocouple locations were considered to calculate the average temperature of the first half of the surface (Figure 1C). Similarly, the third and fourth thermocouple locations were used to measure the average surface temperature at the second half of the channel. In order to ensure the repeatability of the tests, each test was repeated for at least three times. The average values of the experiments were used in the data reduction part.

TABLE 1

TABLE 1. Physical properties of FC-72 and water.

Data Reduction

During the experiments, the obtained voltage, current, and temperature data were reduced to obtain heat transfer coefficient. The mass flux G was calculated as:

$G=\frac{\dot{m}}{A_c}(4)$

Here, $\dot{m}$is the mass flow rate (kg/s), and $A_c$is the cross-sectional area of the microchannel (m²). Moreover, the measured voltage and current values during the experiments were used to obtain the applied power as:

$P=V.I(5)$

where $P$ is the applied power (W), and $V$and $I$are the measured voltage (V) and current (A), respectively. Considering that some percentage of the applied power was lost, the heat flux applied to the surface was calculated as:

$q^{\text{′′}}=\frac{(P-{\dot{Q}}_{loss})}{A_s}(6)$

Here, ${\dot{Q}}_{loss}$ is the heat loss, and $A_s$ is the area of the heated surface. ${\dot{Q}}_{loss}$ was calculated from single phase flow heat transfer. In doing so, single phase FC-72 is introduced to the test section and the inlet and outlet temperatures were measured. Considering that the mass flow rate and specific heat of the working fluid were known, the heat-loss was obtained as:

$Q_{loss}=P-\dot{m}{c}_p(T_{out}-T_{in})(7)$

Using the curve fit technique, the heat losses were estimated at higher temperatures. The heat transfer coefficient (HTC) was found as:

$h=\frac{q^{\text{′′}}}{(T_w-T_f)}(8)$

where $T_W$ is the temperature of the heated surface (°C), and $T_f$ is the temperature of the working fluid (°C). In order to calculate the temperature at the surface ($T_W$), the temperature measured at the jth location of temperature measurement and the calculated heat fluxes were used as follows:

$T_{w,j}=T_j-q^{\text{′′}}(\frac{L_{Al}}{K_{Al}}+R_P+\frac{L_{Si}}{K_{Si}})(9)$

Here, $T_{w,j}$ is the temperature of the substrate at the jth location (j = 1–4), $T_j$ is the temperature read from the jth thermocouple location. Moreover, $L_{Al}$ and $L_{Si}$ are the thickness of aluminum and silicon samples, respectively, while $K_{Al}$ and $K_{Si}$ are their thermal conductivities. Furthermore, $R_P$ is the thermal resistance of the thermal paste.

For subcooled boiling experiments, the fluid temperature was calculated via the energy balance equation (equation 5). Since the pressure drop is not substantial (less than 1 kPa Pa), the saturation temperature is assumed to be constant along the channel. Considering constant heat flux applied to the system, the temperature of the fluid could be obtained as:

$T_{f,x}=T_i+\frac{q^{\text{′′}}.A_x}{\dot{m}{c}_p}{T}_{f,x}<T_{sat}{T}_{f,x}=T_{sat}{T}_{f,x}\ge T_{sat}(10)$

Here, $T_i$ is the inlet temperature (°C), and $c_p$ is the specific heat capacity of the fluid (J.kg-1°C -1). Moreover, $A_x$ is the heated area starting from the inlet to the point of interest. Using the uncertainty analysis proposed by Coleman and Steel (Coleman and Steele, 2018), the maximum uncertainty in the HTC was found as ± 7% (Table 2).

TABLE 2

TABLE 2. Uncertainty parameters and analysis

Validation

In order to make sure that the experimental setup works properly and the obtained results are reliable, single-phase heat transfer tests were performed to validate the setup. First, the heat flux was applied, and the temperatures were measured at the inlet and outlet of the test section. Meanwhile, the temperature at the different locations of the surface was measured. Considering the obtained temperatures at the inlet and outlet, the heat transfer to the fluid was calculated as: $\dot{Q}=\dot{m{c}_p}(T_{out}-T_{in})$. Later on, the average heat transfer coefficient was obtained as:

$h=\frac{\dot{Q}}{\text{A}(T_{wall}-T_f)}(11)$

where $T_f$ and $T_{wall}$ are the average temperatures of the fluid and surface, respectively. Considering that the heat transfer coefficient was known, the Nusselt number was calculated as $Nu=\raisebox{1ex}{$h{D}_H$}\!\left/ \!\raisebox{-1ex}{$k$}\right.$, where $D_H$ and $k$ are the hydraulic diameter of the channel and heat conductivity of the fluid, respectively. The obtained Nusselt numbers were compared with the correlations provided by Shah and London (Shah and London, 2014):

$Nu=1.953{(Re.Pr.\raisebox{1ex}{$D_H$}\!\left/ \!\raisebox{-1ex}{$L$}\right.)}^{\raisebox{1ex}{$1$}\!\left/ \!\raisebox{-1ex}{$3$}\right.}\text{where,}\left(Re.Pr.\raisebox{1ex}{$D_H$}\!\left/ \!\raisebox{-1ex}{$L$}\right.\right)\ge 33.3(2)$

$Nu=4.364+0.0722(Re.Pr.\raisebox{1ex}{$D_H$}\!\left/ \!\raisebox{-1ex}{$L$}\right.)\text{where,}\left(Re.Pr.\raisebox{1ex}{$D_H$}\!\left/ \!\raisebox{-1ex}{$L$}\right.\right)<33.3(3)$

The comparison of the results is presented in Figure 2. As seen in the figure, the obtained experimental results are in good agreement with the predictions of the correlation.

FIGURE 2

FIGURE 2. Validation of the experimental setup.

Sample Preparation

Plasma Polymerization has attracted much attention during the recent years, particularly due to changes in surface wettability (Iqbal et al., 2019; Falde et al., 2016; Siow et al., 2015), which can be performed at both subatmospheric (Sadaghiani et al., 2017) and atmospheric (Park et al., 2017) pressures. Plasma Polymerization offers methods to change the surface geometric and chemistry structures for manipulating the wettability of surfaces (Feng et al., 2002). This ability has motivated many researchers in the field of two-phase heat transfer (Bertossi et al., 2015; Çıkım et al., 2014; Elkholy and Kempers, 2020). Similarly, as mentioned before, C₄F₈ polymer was used in the fabrication of biphilic surfaces. In this innovative fabrication method, different steps were carried out. Firstly, the silicon wafers were washed with Acetone, Isopropanol and DI water, and then N₂ gas was blown on the substrate to get rid of any contaminations. Next, in plasma environment (Oxford PlasmaLab System 100 ICP 300 Deep RIE), the wafers were deposited with C₄F₈ polymer (Figure 3A Step I). During this process, the pressure, RF power, ICP power, and deposition temperature were 30 mTorr, 5 Watt, 1500 Watt, and 5°C, respectively. Also, the plasma polymerization occurred under the continuous wave (CW). It should be noted that this machine was usually used for etching of semiconductors, including both etching and deposition steps. However, the etching process was deactivated over this fabrication method. After having the fully polymer-coated substrates, a layer of AZ 4562 photoresist (PR) was coated on the silicon substrates at 4,000 rpm for 45 s and was baked for 1 min at 110°C. Even though coating of photoresist on hydrophobic surfaces seems to be challenging, the process did not face any failure. However, a layer of SiO₂ could be used as a sacrificial layer for photoresist coating (Zhang et al., 2017). The next step was the UV light exposure (115 mJ/ cm²) using a mask aligner UV-Lithography (Midas aligner) (Figure 3A Step II). Next, by taking advantage of the designed acetate masks, the wafers were patterned using the photolithography fabrication method (Figure 3A Step III). Afterwards, the AZ 726 MIF developer was used to develop the substrates for 40 s before putting them on the hot plate. In this step the patterning process was finished, and the areas to be hydrophobic were covered with PR, which was resistant against etching (Figure 3A Step IV). The silicon wafers were put in the Oxford ICP-RIE machine again to etch the polymer until reaching to the silicon areas (Figure 3A Step V). Finally, the substrate shown in Figure 3A Step VI is obtained. Figure 3B shows the macroscopic view of the fabricated surfaces, which were fabricated on a six-inch silicon wafer. The bright areas of the wafer are the silicon areas, while the darker regions correspond to the C₄F₈ polymer areas. Moreover, in order to display the quality of the coated polymer, a microscopic analysis of the wafer is attached. As seen in Figure 3C, the tolerance of hydrophobic spots is smaller than 2 μm.

FIGURE 3

FIGURE 3. (A) schematic of the fabrication process, (B) microscopic view of the fabricated surfaces, (C) macroscopic representation of the C₄F₈ islands on the silicon surface, (D) AFM images of the coated C₄F₈.

The roughness of a substrate significantly affects the obtained heat transfer coefficient (Dong et al., 2014; Shojaeian and Koşar, 2015). To ensure that any possible enhancement in heat transfer does not stem from the roughness of the coated polymer, the roughness of the surfaces was measured using 2D and 3D Atomic Force Microscopy (AFM) in dynamic mode (ezAFM, Nanomagnetics Instruments). The AFM images are provided in Figure 3D. According to the obtained results, the average roughness of the surfaces was 0.87 nm, while the root mean square was obtained as 1.11 nm. It is noteworthy to mention that the contact angles of a 5 μL water droplet on the silicon and the C₄F₈ islands were 55° and 110°, respectively, as depicted in Figure 4.a. Furthermore, Figure 4B shows the configurations of the tested samples. As shown in Figure 4B, the biphilic samples are divided into three regions including fully hydrophobic, biphilic, and fully hydrophilic surfaces. Table 3 summarizes the characteristics of the tested substrates. It should be noted that the biphilic surfaces do not necessarily change the contact angle of the droplet but the hydrophobic spots provide potential nucleation sites. When a droplet is placed on a tested surface, different scenarios could occur. In order to have a better understanding of the contact angles, some simulations were made using the Surface Evolver 1.30 software. The results are presented in Figure 4C. Upon placing a droplet on a totally hydrophobic or totally hydrophilic surface, an agreement in the contact angles with the measured contact angles could be seen (Figures 4C-i and ii, respectively). However, when a droplet is placed on the biphilic regions, the shape of the triple contact line depends on the size of the droplet. A large droplet (25 μL in Figure 4C-iii) has a larger size than the hydrophobic areas, which results in a contact angle almost the same as a totally hydrophilic surface. Similarly, a small droplet, which could fit inside the hydrophobic spots (5 μL in Figure 4C-iv), has a contact angle almost the same as the totally hydrophilic sample. However, the contact lines of a droplet with a medium size (15 μL in Figure 4C-v) include the both hydrophilic and hydrophobic regions. In this case, the contact line on the hydrophobic areas is repelled towards the center of the droplet.

FIGURE 4

FIGURE 4. (A) Contact angles of hydrophobic (C₄F₈) and hydrophilic (Silicon) parts (B) schematic representations of Sample#1 and Sample#2 (C) different scenarios for droplets regarding contact angles.

TABLE 3

TABLE 3. Characteristics of the tested samples

Result and Discussion

In this section, the obtained results from the flow boiling experiments, which cover both heat transfer and visualization results, are presented. For the experiments, the applied heat flux ranged from 2 W/ cm² and 16 W/ cm². Moreover, two different mass fluxes of 90 kg/ m²s and 130 kg/ m² s were considered. The obtained HTCs along along with the boiling curves are depicted in Figure 5, 6. In both Figures, the results shown on the right side and left side represent the data obtained for the first and second halves of the channel, respectively. Later on, the visualization results are discussed and compared with the obtained results from a previous study, where water was used as the working fluid (Ahmadi et al., 2020).

FIGURE 5

FIGURE 5. Heat transfer coefficients (HTCs) and boiling curves corresponding to the mass flux of 90 kg/ m² s.

FIGURE 6

FIGURE 6. Heat transfer coefficients (HTCs) and boiling curves corresponding to the mass flux of 130 kg/ m² s.

As shown in Figure 5 at a mass flux of the 90 kg/ m² s, both biphilic surfaces show a better performance compared with the entirely uniform hydrophobic surface in terms of boiling HTC. At the first half of the channel, the obtained results suggest that at heat fluxes lower than 5 W/ cm² the biphilic surfaces have no significant influence compared to their hydrophobic counterpart. This result stems from the reason that at the mentioned heat fluxes boiling does not ensue. As can be inferred from the boiling curves (Figure 5) for heat fluxes lower than 5 W/ cm², the wall superheats obtained for different surfaces are close to each other. However, as the heat flux increases from 5 W/ cm² to 12 W/ cm², the biphilic surfaces yields higher HTCs compared to the hydrophobic surface. The higher HTC is due to nucleation sites provided by the hydrophobic islands. Sisman et al. (Şişman et al., 2016) showed that an increase in density of nucleation sites could decrease HTC. They concluded that close nucleation sites might result in sudden coalescence of bubbles. The sudden coalescence, in turn, results in extending the thermal boundary layer of the bubble beyond the stability limit. Therefore, the corresponding nucleation site is canceled, and a temporal condensation might occur inside the bubble. The hydrophobic islands are not relatively close in this study to result in cancelations of the nucleation sites. Moreover, it should be noted that surface#2, due to the biphilicity at the entrance region, exhibits a slightly better performance than surface#1. At the heat fluxes higher than the 12W/cm², all surfaces have HTCs close to each other. Regarding the subcooling of the working fluid at the inlet part along with the high temperature of the surfaces under this condition, all the surfaces provide almost the same numbers of nucleation sites, which result in HTCs close to each other.

Similar to the first half, biphilic surfaces have better performances compared to the hydrophobic surface at the second half of the channel (Figure 5). At heat fluxes lower than 9W/cm², the average HTCs for the biphilic surfaces are significantly higher than the hydrophobic surface. As mentioned before, along the first half of the channel, at heat fluxes lower than 5 W/ cm², the performances of all surfaces are similar. However, at the second half, considering that the subcooled fluid mainly reaches the saturation temperature during the first half of the channel along with the nucleation points provided by the hydrophobic islands, higher HTCs are obtained. Moreover, as the heat flux is raised to values higher than 9 W/ cm², due to partial dry out of the surfaces, all surfaces exhibit similar behavior. The wall superheats on surface#2 is lower than surface#1 at the applied heat flux of 14 W/ cm², while they correspond to similar HTCs at lower heat fluxes. The presence of biphilic islands at the region#1 of surface#1 delay the dryout condition at high heat fluxes. At the mentioned mass flux, the maximum enhancement was more than 50% compared to the hydrophobic surface and was reached at the heat flux of 4 W/ cm².

The results regarding HTCs at the mass flux of 130 kg/ m²s are displayed in Figure 6. At the first half of the channel, as the boiling is not initiated at low heat fluxes, the biphilic surfaces lead to the almost same heat transfer coefficients compared to their hydrophobic counterpart, as they have almost the same wall superheats. This trend is the same for the previously mentioned mass flux for heat fluxes lower than 5 W/ cm². Lie et al. (Lie et al., 2007) reported that the required heat flux for the onset of nucleation increases with the mass flux. This phenomenon explains the delay in the transition of the dominant heat transfer mechanism from single-phase to phase-change, as the mass flux increases. At heat fluxes higher than 9 W/ cm², since the nucleation points are visible on the hydrophobic islands, biphilic surfaces have a better performance than the wholly hydrophobic surface. As shown in boiling curves of Figure 6, the wall superheats obtained for surface#2 are smaller than surface#1, which implies that the hydrophobic islands at the entrance region of surface#2 lead to a slight difference in heat transfer.

In contrast to the mass flux of 90 kg/ m² s, where the phase-change heat transfer was dominant for all the heat fluxes at the second half of the channel, at the heat fluxes lower than 4 W/ cm², single-phase heat transfer is the dominant heat transfer mechanism since boiling does not incept at these heat fluxes along the channel, and as depicted, the wall superheats are close to each other, and all the surfaces exhibit similar HTCs at heat fluxes lower than 4 W/ cm². However, as the heat flux increases, the HTCs of the biphilic surfaces strongly deviate from the hydrophobic surface. It should be noted that the tested surfaces have a maximum enhancement of 26% with respect to the hydrophobic surface, which happens at the heat flux of 9 W/ cm².

The results regarding the visualization are presented in Figure 7, for the mass flux of 90 kg/ m² s. As seen in Figure 7, the surface conditions strongly affect the bubble dynamics inside the channel. At the heat flux of 5 W/ cm², at the first half of the channel, the hydrophobic surface and surface#1 have almost single-phase flow conditions. However, the hydrophobic islands on the entrance region of surface#2 result in the generation of bubbles, since the hydrophobic islands provide active nucleation sites. According to the heat transfer results in Figure 5, these nucleation points are not capable of increasing the HTC noticeably. At the second half of the channel, however, the generated bubbles strongly affect HTC. As seen in Figure 7, on the totally hydrophobic surface, the coalescence of the bubbles results in larger bubbles, and transition from bubbly flow regime to slug-flow (heat flux of 7 W/ cm²). However, on both biphilic surfaces, slug flow cannot be observed.

FIGURE 7

FIGURE 7. Visualization results regarding mass flux of 90 kg/ m² s.

In our previous study (Ahmadi et al., 2020), we reported that one of the reasons for HTC enhancement in the biphilic surfaces could be due to bubble break-up during the slug-flow regime, rather than their coalescence. The obtained results of this study are in agreement with the previous study. As shown in Figure 8, the coalescence of small bubbles on the hydrophobic surface results in an elongated bubble. However, on the biphilic surface, where the hydrophobic islands provide potential nucleation points, the generated bubbles are relatively close. Moreover, the bubbles are generated on previously designed islands and are well dispersed. These generated bubbles in turn block the effective cross-sectional area, and the velocity of the working fluid will be higher at the remaining cross-section area (shown by red arrows in Figure 8) The higher velocity gradient results in a higher shear force applied to the bubbles. Considering that the bubbles remain intact as long as the shear force is smaller than its surface tensional counterpart (Sun et al., 2017), the higher shear force results in break-up of the bubbles on biphilic surfaces and prevents effective coalescence of the bubbles. It should be noted that in our previous study, water was used as the working fluid and the slug flow regime was observed on both hydrophobic and biphilic surfaces. However, since the surface tension of FC-72 fluid is much smaller than water and there exists a larger distance between nucleation sites, the bubbles tend to break up on biphilic surfaces easier than the bubbles in the case of water.

FIGURE 8

FIGURE 8. Comparison of bubble dynamics on the hydrophobic surface with a biphilic surface.

At higher heat fluxes (q > 9 W/ cm²), both surface#1 and surface#2 provide larger number of nucleation sites than the totally hydrophobic surface. Compared to surface#1, the larger amount of designated nucleation sites at the inlet part of surface#2 increases the number of generated bubbles. As can be seen in Figure 5, this results in a slightly better performance of surface#2 with respect to surface#1.

Figure 9 shows the comparison of flow patterns of FC-72 with water. In both the present and previous studies (Ahmadi et al., 2020), since the subcooled liquid is supplied to the channel, boiling does not incept at the first region (Region I). In region II, which is known as the bubbly flow region, the density of the generated bubbles is larger for FC-72 flow compared to water (Ahmadi et al., 2020). This is due to two main reasons. First, the contact angles on the islands fabricated in this study are larger than the previous one (110° vs. 90°). Second, the latent heat of vaporization of FC-72 is smaller than water, and a larger amount of vapor is generated and observed at a fixed heat flux in the present study. Moreover, it should be noted that since FC-72 has a higher density and a smaller surface tension in comparison with water, a larger drag force and a smaller surface tension force are present. Therefore, the generated bubbles in FC-72 detach within a shorter time with respect to water. In other words, the frequency of bubble generation in FC-72 is smaller than that in water. Regarding these differences, the duration of bubbly flow regime in FC-72 is extended in comparison with water.

FIGURE 9

FIGURE 9. Different flow boiling patterns in: (A) FC-72 medium and (B) water medium.

Region III represents the slug flow regime. Considering that break-up of a bubble occurs whenever the applied shear force becomes larger than its surface tension counterpart, the size of elongated bubbles generated from FC-72 is relatively smaller than bubbles generated from water vapor, due to the smaller surface tension of FC-72 compared with water. Moreover, slug flow in water is the dominant flow pattern in water, while bubbly flow is the dominant flow regime in FC-72. In region IV (known as churn flow regime), generally, the middle of the channel is blocked by the vapor core. Similar to slug flow regime, the lower surface tension of FC-72 results in a smaller vapor core in comparison with water. It should be noted that in churn flow regime, the density of the liquid core in FC-72 is higher than water, since FC-72 is more wettable than water.

Conclusion

This study investigates the effect of surface mixed wettability on flow boiling of FC-72 in a rectangular minichannel. The surfaces, including two biphilic surfaces and one hydrophobic surface, were fabricated and tested at the mass fluxes of 90 kg/ m² s and 130 kg/ m² s and heat fluxes ranging from 1 W/ cm² to 16 W/ cm². The main conclusions driven from this study are as follows:

• Surface mixed wettability is an effective method for BHT enhancement especially effective for coolants with smaller surface tension and latent heat of vaporization. The effect of biphilicity on such coolants are more dominant at the second half of the channel.

• The main mechanisms in heat transfer enhancement with FC-72 are the uniform distribution of nucleation sites on the superheated surface and the bubble break-up in the channel.

• Biphilic surfaces could provide enhancements in flow boiling heat transfer up to 50% compared to the wholly hydrophobic surface.

• The surface with hydrophobic islands at the inlet region of the channel shows slightly better performance in terms of BHT compared to the surface with a hydrophobic entrance.

The obtained results of this study prove that the biphilic surfaces are promising candidates of modified surfaces in high heat flux cooling with flow boiling.

Data Availability Statement

The raw data supporting the conclusions of this article will be made available by the authors, without undue reservation.

Author Contributions

Conceptualization, VA, AA, SC, AS, KS, and AK; investigation, VA, S.C. and AA; methodology, VA, AA, and AS; supervision, KS and AK; validation, VA, AA, and AS; writing (original draft preparation), VA, AA, AS, and AK; writing (review and editing), AS, KS, and AK. All authors have read and agreed to the published version of the manuscript.

Funding

This study was funded by the Scientific and Technological Research Council of Turkey (TUBITAK) and Royal Academy of Engineering through the 1601-Bilateral Newton-Katip celebi Cooperation Programme-Project number: 4180047.

Conflict of Interest

The authors declare that the research was conducted in the absence of any commercial or financial relationships that could be construed as a potential conflict of interest.

Publisher’s Note

All claims expressed in this article are solely those of the authors and do not necessarily represent those of their affiliated organizations, or those of the publisher, the editors and the reviewers. Any product that may be evaluated in this article, or claim that may be made by its manufacturer, is not guaranteed or endorsed by the publisher.

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