Experimental Study on Two-Phase Flow in Horizontal Rectangular Minichannel with Y-Junction

Agus Santoso et al. Int. Journal of Engineering Research and Application www.ijera.com
ISSN : 2248-9622, Vol. 6, Issue 2, ( Part -1) February 2016, pp.39-48
www.ijera.com 39 | P a g e
Experimental Study on Two-Phase Flow in Horizontal
Rectangular Minichannel with Y-Junction
Agus Santoso*, Rintaro Nagai*, Akifumi Mori*, Akimaro Kawahara*, Michio
Sadatomi *
*(Department of Advanced Mechanical Systems, Graduate School of Science and Technology, Kumamoto
University, Kurokami 2-39-1 Chuo-ku, Kumamoto City 860-8555, Japan)
ABSTRACT
An experimental study was conducted to investigate two-phase air-water flow characteristics, in horizontal
rectangular minichannel with Y-junction. The width (W), the height (H) and the hydraulic diameter (DH) of the
rectangular cross section for the upstream side of the junction are 4.60 mm, 2.50 mm and 3.24 mm, while those
for the downstream side are 2.36 mm, 2.50 mm and 2.43 mm. The entire test section was machined from
transparent acrylic block, so that the flow structure could be visualized. Liquid single-phase and air-liquid two-
phase flow experiments were conducted at room temperature. The flow pattern, the bubble velocity, the bubble
length, and the void fraction were measured with a high-speed video camera. Pressure profile upstream and
downstream from the junction was also measured for the respective flows, and the pressure loss due to the
contraction at the junction was determined from the pressure profiles. Two flow patterns, i.e., slug and annular
flows, were observed in the fully-developed region apart from the junction. In the analysis, the frictional pressure
drop data, the two-phase frictional multiplier data, bubble velocity data, bubble length data and void fraction data
were compared with calculations by some correlations in literatures. In addition, new pressure loss coefficient
correlations for the pressure drop at the junction has been proposed. Results of such experiment and analysis are
described in the present paper.
Keywords- Minichannel, two-phase flow, Y-junction, bubble velocity, bubble length
I. INTRODUCTION
Gas-liquid two-phase flow in mini-channels is a
phenomenon seen in compact heat exchanger with
phase changes, e.g., air conditioners, cooling devices
in electronic equipments. In many arrangements it is
necessary to divide the flow into two or more
channel motivated by area restrictions or process
requirements. There has been considerable interest
recently in compact heat exchangers with mini- and
micro-sized flow channels. These heat exchangers
contain flow passages of various cross-sections (e.g.,
circular and rectangular), as well as various types of
dividing tee junctions (e.g., branching and
impacting) [1, 2]. Under two-phase flow conditions
the behavior of the junction is complicated
considerably by the structure of the gas-liquid
mixture and, in particular, by its influence on the
relative division of the two phases to the main and
branch outlets, which becomes a parameter of great
significance in the overall design of two-phase flow
systems [3]. Flow distribution through the branches
has to be investigated in order to design the system
optimally.
Several investigations have been reported on
two-phase flows in dividing tee junctions. For the
case of impacting tees, a few studies have been
reported in literatures (e.g., [1, 4, 5, 6, 7]). Elazhary
and Soliman [2] investigated the single- and two-
phase pressure drops in a mini-size, horizontal,
impacting tee junction with a rectangular cross-
section (1.87-mm height x 20-mm width). The
single-phase experiments were conducted using air
or water in a wide range of Reynolds number, and
the two-phase experiments using air and water at
200 kPa (abs) and room temperature for various inlet
flow regimes. They reported the pressure loss
coefficient for the single-phase flows was found to
be dependent on Reynolds number in laminar flows
( ≤ 2000), but independent of Reynolds
number in turbulent flows ( ≥ 5000). Four
flow regimes were observed : bubbly, plug, churn,
and annular flows. El-Shaboury et al. [8] conducted
experiments for air-water flows in a horizontal
impacting tee junction (37.8-mm i.d.) with equal-
diameter sides at a system pressure of 1.5 bar
nominally. They obtained phase-distribution and
pressure drop and found that the phases did not
distribute themselves evenly between the two outlets
unless the mass split is equal.
For the case of branching tees, more than ten
studies were reported by [9, 10, 11, 12, 13, 14, 15,
16, 17, 18, 19]. They studied the two-phase flow
through a dividing T with 90 degree branch arms.
However, there are few studies about the two-phase
flows through a Y-junction. Ishiguro et al. [20]
carried out experiments to separate gas from
downward gas-liquid two-phase flows using a Y-
RESEARCH ARTICLE OPEN ACCESS

junction of poor wettability. The branch angle was
90 degree, and the inner diameters of the main pipe
and two branches were 10 mm. One side of the
channels downstream from the Y-junction was
coated with repellent to change its wettability. Air
and water were used as the working fluids.
Guangbin et al. [21] reported the characteristics of
gas–solid two-phase flows through a Y-shaped
branch pipes (0.032-m i.d) with a fixed branch angle
and the other adjustable branch angle. Micro-glass
bead and millet particles with similar diameter but
different density were used in this experimental
system. As a result, the trend of solids mass ratio
flowing in the adjustable branch and pressure drop
on each branch pipe were analyzed to study flow
distribution characteristics and resistance properties.
It was found that the solids flow distribution and
pressure drop for the two materials have similar
trend and were significantly affected by the branch
angle and gas velocity. Chen et al. [22] performed an
experimental study of nitrogen-pure water two-phase
flow splitting at microchannel junctions with the
square cross-section of 0.5 x 0.5 mm2
, and with five
different branch angles varying from 30 to 150
degree. The inlet superficial velocities were varied
from 0.8 to 21.3 m/s for the gas phase, and from
0.019 to 0.356 m/s for the liquid phase. Data
analysis shows that the phase split at microchannel
junctions depends strongly on inlet flow patterns.
The liquid taken off from the branch did not
decrease with increasing of the branch angle for all
inlet flow patterns. Likewise, some researcher have
studied computationally the flow through Y-junction
such as, [23, 24, 25, 26].
The literature survey indicates that the research
on two-phase flow in rectangular minichannel with
Y-junction is limited. Therefore, the purpose of the
present work is to investigate experimentally the
two-phase flow in horizontal rectangular
minichannel with the hydraulic diameter (DH) for the
channel upstream from the junction 3.24 mm, and
that for the downstream channel 2.43 mm. The high
speed video technique was used to analyze the fluid
dynamics of two-phase distribution at the junction.
The experimental and the analytical results are
compared with the data from previous studies and
are presented in the present paper.
II. EXPERIMENTS
A schematic diagram of the test facility used in
the present study is shown in Fig. 1. As the test
fluids, water was used for the liquid phase, and air
for the gas phase. Pressurized air from a compressor
pushed the water in a tank and supplies it to the test
channel. Thus, no mechanical pump was used in the
present experiment to avoid pulsation by the pump
and also to avoid contamination by the pump. Figure
2 shows a schematic diagram of test channel with
branch placed on a horizontal plane. The branch
angle was 60o
. The test channel had a rectangular
cross-section and made of transparent acrylic resin
for visual observation. Table 1 shows the cross-
sectional dimensions of the test channel on the width
(W), the height (H) and the hydraulic diameter (DH).
Those for the channel upstream from the junction
(Upstream I) were 4.60 mm, 2.50 mm and 3.24 mm,
while those for the channel downstream
(Downstream II and Downstream III) were 2.36 mm,
2.50 mm and 2.43 mm. In Fig. 2, the port #1 was the
liquid inlet port, while the port #2 and #3 were the
gas inlet ports. Therefore, two phases were supplied
through the section 1 as a gas-liquid mixer. The port
#4 and #5 were the gas-liquid mixture outlet to
individual separator tanks. Volume flow rate of air
was measured with a flow meter (KEYENCE, FD-
A10 AND FD-A1 depending on the flow rate range)
within 2 %, while that of water with a flow meter
(KEYENCE, FD-S) within 1 %.
In order to obtain accurate time averaged values
of air and water flow rates and pressures, the output
signals from the respective sensors were fed to a
personal computer via A/D converter over 10 sec. at
nominally 1 kHz. P1 to P15 are the pressure taps, and
the pressure at P4 in Fig. 2 was measured with a
gauge type pressure transducer (Yokogawa, FP101-
L31-L20). The pressures at other pressure taps were
determined from the difference in pressure between
there and P4 tap measured with a differential
pressure transducer (Validyne, DP15-32 and DP15-
26 depending on the pressure range). The accuracy
of the pressure measurement was within 4 Pa from a
calibration test. The gas-liquid mixture discharged to
each separator was separated. The air from the top of
each separator was metered by a gas flow meter
(SINAGAWA, DC-1C, 10 ~ 1100 L/h) before
exhausting to the atmosphere. During the flow rate
measurement, the water levels in the separator tanks
were monitored to be in the respective constant
levels. The water flow rate from the bottom of each
separator tank was calculated by measuring the mass
of water discharged per a enough measurement time.
In the present experiment, the water flow rates of the
two branch channels were adjusted to be equal each
other as possible by changing the openings of two
valves between the channel exit and the separator
tank.

GF GF
Compressor
Regulator
Tank
Air
Mini-channel
with Y-junction
Gas flowmeter
Valve
ΔP
Pg
Air
T
GF
GF
LF
Liquid
flowmeter
Differential pressure
transducer
Pressure gauge
Separator
Thermoelectric
couple
Fig. 1 : Test apparatus
Flow pattern was observed with a high-speed
video camera (KEYENCE, VH-Z00R, frame rate :
1000 ~ 8000 frame/s, shutter speed 1/1000 ~
1/8000s) in four observation area marked with
broken circles in Fig. 2, and bubble velocity, uG, in
slug flow in the test channel was also measured.
Furthermore, void fraction, α, data was obtained by
substituting the measured uG and the gas volumetric
flux, jG, into = ⁄ . For single-phase water
flow experiments, the ranges of Reynolds number
(= , where is the mean velocity of water,
and the density and viscosity of water) in the
upstream channel was from 762 to 4661. For two-
phase air-water flow experiments, the ranges of
volumetric fluxes of the liquid and the gas were 0.2
< jL < 1.5 m/s and 0.2 < jG < 5.0 m/s.
Fig. 2 : Test channel with Y-junction
Table 1 : Dimension of test channel cross section
W
[mm]
H
[mm]
DH
[mm]
Upstream I 4.60 2.50 3.24
Downstream II, III 2.36 2.50 2.43
III. RESULTS AND DISCUSSION
3.1 Flow pattern
Figure 3 shows the flow pattern map in the
present two-phase flow experiment. The ordinate
and abscissa are the volumetric fluxes of water and
air. The flow regimes observed with a high-speed
video camera covered in a range of 0.2 ≤ jG ≤ 5.0
m/s and 0.2 ≤ jL ≤ 1.5 m/s. Two flow regimes were
observed, i.e., slug flow and annular flow under the
present flow conditions.
Fig. 3 : Flow pattern map in the present experiment
Figures 4 (a) and (b) show typical flows in the
test channel, respectively for a slug flow at jG, I = 0.5
m/s, jL, I = 0.5 m/s and an annular at jG, I = 5.0 m/s,
jL, I = 0.5 m/s. The flow regimes among upstream I,
and downstream II and III are similar at all the
experimental conditions.
(a) Slug flow (jG, I = 0.5 m/s, jL, I = 0.5 m/s)
(b) Annular flow (jG, I = 5.0 m/s, jL, I = 0.5 m/s)
Fig. 4: Typical flows in the test channel
3.2 Data reduction in pressure drop
Figures 5 (a) and (b) show typical pressure
distributions for water single- and air-water two-
phase flows upstream and downstream of Y-

junction. The ordinat is the gauge pressure, while the
abscissa is the distance from the junction. There are
five pressure taps, tap #1 to tap #5, for the upstream
channel from the junction and the another ten taps,
tap #6 to tap #15, for the downstream channel. The
total pressure drop across the Y-junction, ∆pb, was
determined by the extrapolations of the axial
pressure profiles upstream and downstream from the
junction, as shown in Figs. 5 (a) and (b).
(a) Single-phase flow (Re = 4700)
(b) Two-phase flow (JG = 1.0 m/s, JL = 1.5 m/s)
Fig. 5 : Pressure distribution along the channel
with Y-junction
In order to check the pressure measurement
accuracy, the single-phase friction factors were
determined from the fully developed pressure
gradients upstream and downstream from the
junction. Figs. 6 (a) and (b) show the Darcy friction
factor data respectively for the channels upstream
and downstream from the junction. The data are
plotted against the Reynolds number, based on the
hydraulic diameter. The present data in laminar flow
region are compared with calculated curve by Shah
and London [27] which is a function of aspect ratio,
∗(= ⁄ ), for a rectangular channel :
= 96(1 − 1.3553 ∗
+ 1.9467 ∗
1.7012 ∗
+
0.9564 ∗
− 0.2537 ∗ ). (1)
In addition, the data in turbulent flow are compared
with familiar calculated curves by Blasius,
= 0.316 .
, (2)
and Nikuradse :
= 0.0032 + 0.221 .
. (3)
(a) λ vs. Re (Upstream I)
(b) λ vs. Re (Downstream II, III)
Fig. 6 : Single-phase friction factors in channels
upstream and downstream from the junction
3.3 Pressure drop at Y-junction
The pressure drop at the Y-junction can be
evaluated by the change in dynamic pressure
between the flows in channels upstream and
downstream from the junction. Since the two-phase
flow energy per unit time is composed of two
components as follows :
= 2 +⁄ 2⁄ . (4)
Thus, the dynamic pressure, i.e., the flow energy/the
total volume flow rate, is given by
, = 2⁄ + (1 − ) 2.⁄ (5)
Here ρ, Q and u are the density, the volume flow rate
and the mean velocity, and the homogeneous void
fraction defined as = (⁄ + ). Since the first
term in the right hand side of Eq. (5) is much smaller

than the second term in bubble and slug flow
regimes. , can be approximated as :
, = (1 − ) 2⁄ (6)
Here, (= (1 − )⁄ ) is the mean liquid velocity
and can be approximated as (1 − )⁄ because
≈ in the present experimental range as shown in
Fig. 14, the last figure of the present paper. And
then, Y-junction loss coefficients for single- and
two-phase flows are defined as follows :
kSP,ⅠⅡ =
∆PbSP,ⅠⅡ
ρLuL,Ⅰ
2 2⁄
(7)
kSP,ⅠⅢ =
∆PbSP,ⅠⅢ
ρLuL,Ⅰ
2 2⁄
(8)
kTP,ⅠⅡ =
∆PbTP,ⅠⅡ
( ) , ⁄
(9)
kTP,ⅠⅢ =
∆PbTP,ⅠⅢ
( ) , ⁄
(10)
Figures 7 (a) and (b) show the junction loss
coefficient for single- and two-phase flows,
respectively. In Figure 7 (a) both , and
, data are simultaneously plotted. The
abscissa is the Reynold number of the channel
upstream from the junction. The vertical doted line
on the figure is the critical Reynold number ( =
2300), between laminar flow and turbulent flow.
The junction loss coefficient in laminar flow region
( < 2300) is nearly constant, and it decreases
with increasing of ReI in turbulent flow region
( > 2300). Thus, the data for the single-phase
flow in this study is correlated with
Laminar flow region (Re < 2300) = 0.67, (11)
Turbulent flow region (Re > 2300) = 291 ×
10 .
. (12)
Figure 7 (b) shows the junction loss coefficient for
two-phase flow, , against the volumetric flux of
gas in the channel upstream from the junction, , . It
can be seen that the loss coefficient for two-phase
flow is nearly constant at 0.0001, independent of ,
and , except for in annular flows. The data
at , = 0.2 m/s seem to be inaccurate because ,
data become quite small with decreasing of , .
(a) Single-phase flow
(b) Two-phase flow
Fig. 7: Y-junction loss coefficient
Figures 8 (a) and (b) show the present two-
phase frictional pressure drop data for the channels
upstream and downstream from the junction,
⁄ , against the mass quality, x. In general,
the pressure gradient increase with the quality, x, and
total mass flow flux, (= + ).
(a) Upstream I

(b) Downstream II, III
Fig. 8 : Frictional pressure drop for two-phase flow
The frictional pressure drop data are commonly
correlated with the following two-phase friction
multiplier, (Lochhart & Martinelli, [28]) :
= , (13)
where ⁄ is the frictional pressure drop
when the liquid flows alone in the same channel. A
widely used correlation for the friction multiplier is
that proposed by Chisholm and Laird (1958) :
= 1 + + , (14)
where X is the Lockhart-Martinelli parameter given
by
=
⁄
⁄
, (15)
where ⁄ is the frictional pressure drop
when the gas flows alone in the same channel.
Figures 9 (a) and (b) show the two-phase friction
multiplier data against the Lockhart-Martinelli
parameter, X, for the channels upstream and
downstream from the junction. The dot-dashed line
is the calculated curve by Mishima-Hibiki [29], who
proposed the C correlation as follows :
C = 21(1 -e-0.319DH ). (16)
where DH is the hydraulic diameter of the channel.
Here, the unit of DH should be in millimeter. The
data are well correlated with the Lockhart-Martinelli
parameter, and is a little bit lower than the
calculation by Mishima-Hibiki [29].
(a) Upstream I
(b) Downstream II, III
Fig. 9 : Two-phase frictional multiplier data against
Lockhart & Martinelli parameter
3.4. Bubble velocity
Figure 10 shows the bubble velocity data, uG,
for the respective channels in the present experiment
against the total volumetric flux of gas and liquid,
+ . The solid line of = is applicable to
homogenous flows. It can be seen the data agree
reasonably with = . Figure 11 shows a
comparison of the bubble velocity between
experiment and calculation by the drift flux model of
Zuber and Findlay [30] :
= + (17)
Here, VGj, is the drift velocity, was taken as zero
because of horizontal flow. The distribution
parameter, , was determined by Kawahara et al.’s
correlation [31] :
C = αB 0.19
ReL
-0.01
WeG
0.01
(18)
and the distribution parameter, C , in this study are
proposed :
C = 1.02B 0.19
ReL
-0.01
WeG
0.01
for upstream I (DH =
3.24 mm) (19)

C = 1.82B 0.19
ReL
-0.01
WeG
0.01
for downstream II and
III (DH = 2.43 mm) (20)
In Eqs. (19) and (20), B is the Bond number, ReL
the liquid Reynolds number and WeG the gas Weber
number. As seen in Fig. 11, the calculations agree
well with the data within root mean square errors of
15% for both the upstream and the downstream
channels.
Fig. 10 : Bubble velocity data
Fig. 11 : Comparison of bubble velocity between
experiment and calculation
3.5. Bubble length
Figure 12 shows the bubble length data divided
by the channel width, .⁄ The abscissa is the ratio
of the gas volume flow rate to the liquid one,
⁄ . The solid curve represents calculation by
Garstecki et al.’s correlation [32] :
= 1 + (21)
whereas the dashed lines represents the calculation
by Miyagawa’s correlation [33] :
= 1 + × 5 (22)
The data for both the upstream and the
downstream channels have a similar trend to both
the solid curve and the dashed curve, however it
approaches to the value calculated by Miyagawa’s
correlation as ⁄ increases.
Fig. 12 : Dimensionless bubble length data against
gas-liquid volume flow rate ratio in the upstream
and the downstream channels
Figure 13 shows the ratio of bubble length, LG,
to unit cell length, L (= + ; is the liquid slug
length) against homogeneous void fraction =
/( + ) in the upstream and the downstream
channels. The solid curve shows the calculation by
Kawahara et al.’s correlation [34] :
=
. .
. . ≅ .
(23)
Eq. (23) was proposed based on the data for
horizontal straight microchannels with square and
circular cross-sections. The ⁄ data for both the
upstream and downstream channels distribute
around the curve. Therefore the junction does not
affect ⁄ data, the Kawahara et al.’s correlation
can be applied, irrespective of the channel geometry.
Fig. 13 : Length ratio of large gas bubble to unit
cell against homogenous void fraction

3.6 Void fraction
Figure 14 shows the void fraction data, α, in the
present experiment against the homogeneous void
fraction, = ( + )⁄ . The solid line of α = β is
applicable to homogeneous flow, and the dashed
lines represents the Armand’s correlation [35],
= 0.833 . The void fraction, α, data especially for
downstream III case, agree reasonably with the
homogeneous flow. Almost all the data are higher
than Armand’s correlation.
Fig. 14 : Void fraction against homogeneous void
fraction
IV. CONCLUSIONS
Water single-phase flow and air-water two-
phase flow experiments were conducted at room
temperature and at near atmospheric pressure using a
horizontal rectangular minichannel with Y-junction.
The width (W), the height (H) and the hydraulic
diameter (DH) for the upstream channel from the
junction were 4.60 mm, 2.50 mm and 3.24 mm,
while those for the downstream channel were 2.36
mm, 2.50 mm, 2.43 mm. The main findings can be
summarized as follows:
1. Two type of flow patterns, i.e., slug flow and
annular flow are observed under the present
flow conditions.
2. The junction pressure loss coefficient in the
single-phase laminar is constant independent of
Reynolds number, but decreases with increasing
of it in turbulent flow. The coefficient in two-
phase flow is nearly constant, independent of jL
and jG except for in annular flows.
3. Frictional pressure drop for two-phase flows,
⁄ , increases with the mass quality at
a fixed mass flow flux, G, for both the upstream
and the downstream channels from the junction.
In addition, ⁄ increases with G at a
fixed mass quality.
4. Two-phase frictional pressure drop data are a
little bit lower than the calculation by the
Chisholm and Laird correlation with Mishima-
Hibiki’s correlation.
5. The bubble velocity data, uG, for both the
upstream and the downstream channels agree
reasonably with that calculated by homogenous
flow model. The data were well correlated with
the drift flux model with Kawahara et al.’s
modified parameter correlation.
6. The bubble length data, LG, for both the
upstream and the downstream channels have a
similar trend to both the Garstecki et al.’s
correlation and Miyagawa’s correlation,
however it approaches to a value calculated by
Miyagawa’s correlation as ⁄ increases.
7. The ratio of bubble length to unit cell length
data, ⁄ , can be predicted by the Kawahara et
al.’s correlation, irrespective of channel aspect
ratio.
8. The void fraction data, α, especially for
downstream III case, agree reasonably with
those for homogeneous flow.
Acknowledgements
The authors deeply appreciate DIKTI of
Indonesian government and State Polytechnic of
Cilacap for the fellowship and the permission to Mr.
Agus Santoso to study in Kumamoto University.
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Experimental Study on Two-Phase Flow in Horizontal Rectangular Minichannel with Y-Junction

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Experimental Study on Two-Phase Flow in Horizontal Rectangular Minichannel with Y-Junction