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21Journal of Siberian Federal University. Engineering & Technologies 1 (2013 6) 15-27
УДК 532.5
Micro-LIF and Numerical Investigation of Mixing in Microchannel
Andrey V. Minakova,b*, Anna A. Yagodnitsynab, Alexander S. Lobasova,b, Valery Ya. Rudyakb,c and Artur V. Bilskyb
a Siberian Federal University, 28 Kirensky Str., Krasnoyarsk, 660074 Russia b Institute of Thermophysics SB RAS, 1 Lavrentiev, Novosibirsk, 630090 Russia c Novosibirsk State University of Civil Engineering, 113 Leningradskaya Str., 630008 Russia
Received 11.02.2013, received in revised form 18.02.2013, accepted 25.02.2013
Flow regimes and mixing pattern in a T-type micromixer at high Reynolds numbers were studied by numerical solution of the Navier-Stokes equations and by particle image velocimetry (micro-PIV) and laser induced fluorescence (micro-LIF) experimental measurements. The Reynolds number was variedfrom 1 to 1000. The cross section of the mixing channel was 200 jm^400 jm, and its length was 3000 jm. Five differentflow regimes were identified: (I) steady vortex-free flow; (II) steady symmetric vortex flow with two horseshoe vortices; (III) steady asymmetric vortex flow; (IV) unsteady periodic flow; (V) stochastic flow. Maximum mixing efficiency was obtained for stationary asymmetric vortex flow. In this case, an S-shaped vortex structure formed in the flow field. Good agreement between calculation and experiment was obtained.
Keywords: Microflow, Micromixers, Microchannels, CFD, Micro-PIV, Micro-LIF.
Introduction
Liquid mixing is an important physical process which is widely used in various microfluidic devices. Since the characteristic flow times are usually extremely small, mixing is accelerated using special devices called micromixers. Micromixers are a key element of many MEMS and other devices that are used in various biomedical and chemical technologies, creating different micro heat-exchangers, microapparatus, etc. The operating principles of micromixers and their optimization have been the subject of a great deal of research (see, for example, [1-4] and references therein). Most papers consider laminar flow at low Reynolds numbers, which are usually characteristic of microflow. In practice, however, there are situations when microflows Reynolds number (Re) are high enough [5,6]. In addition, at relatively high Reynolds numbers in microchannels take place number of new interesting phenomena requiring study both a fundamental point of view and for practical purposes.
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* Corresponding author E-mail address: [email protected]
Thus, in the study of T-type micromixers the existence of critical Reynolds number at which the Dean vortices in a microchannel lost symmetry was experimentally demonstrated [1]. The critical Reynolds number about 150 for channel dimensions 600|amx300|amx300|am was found. Strong dependence of the critical Reynolds number from the channel size was shown. Transient flow regimes (at Reynolds number Re = 300-700) by the instrumentality of numerical simulation have been investigated in [7], but the mixing processes have not been studied. The mixing of two fluids in the range of Reynolds numbers from 50 to 1400 was studied experimentally and numerically in [8]. In [9] the existence of unsteady perlootic reg[me fos ceutoio values oU the Reynolds numbeo fiost dsmonstrated numerically. The most compreheorivn experimental study of mixing in a T-sUaped microchannel at moderate Reynolds numbers (100-4100) in [10] was carried out. Thssr, using |i-LIF and |i-PIV measurements of the velocity and concentration fields in the various secti-ns of the mixeo wds ntudied. For the first time the mixinn efficiency w-r me asure d.
.n spite of the relatively large number of paperr covered the studu of flow and mixing in T-type mlcromixers at moddraie Reynolds numbers, in fact, sufficient syrtemaoic da0h about flow regimes and mixing procerses eook palace in it is still absent. The present work covers systematic modeling of incomprets[blo flow and mixing in a T-type micrtimixer at Reynolds numUers from 10 to 1000. The problem was sslveeluumeoically ou the basis of the NaviereStokes equations for an incompressible fluid. Verification of rbe simulation data wos corried ouh expe:rimenoal-y. The measurements were perfoemed by awo methods: paruide image velocimetru (micro-PIV) ¡and iaaeo induced fluoeescence (nUare-LIF).
Mathematical Model and Numerical Algorithm
The incompressible flows? of multicomponent Newtonian fluids, which dynamics is described by the Navier-Stokes werec onsidered
ofi + V-dpv) = 0, + V- (pvv) = -Vp + V-T, (1)
de de '
where p is fluid de=sity, p is preseure, v is its velocity, +nd T is the viscous stsess tensor. Density and vircosity op the mixture ie determined by the masa foactiou of mixture components pa the partial density p,- and moleculas viscosity on the pure cnmponents °
P = Z f,Pi > V = lLf, "H-i >
i i
and the evolution of the mass concenirations determined by the equation
Seao^-ipo-r^v-ODdy;.), (2)
de
where A os the difforion coenkhent t^f thuei o-componsnl.
As boundary uondiUone on the channd walls for the velocity vectoe components used slip or nonslip conditions. In this papee usod the second one.
Tomlve the system -f equations mentioned above CFD nooiware ptckage cFlow is used. A deoailed description of the psogram nume rical algorithm is give n in [H,!, The developed algorithm
used in solving a wide range of problems of external and internal flows [11-13]. Its applicability to describe the microflows shown in [14,15].
The investigation re sults of flow and mixing in T-type mic romixers are presented in this paper. Width of the narrow chaenel part is 200 (tm, width of the wide channel patt is 400 (m, thickness of the channel is 200 (m and length of the mixing channel is 3000 (m. The problem is considered in the spatial and timetdependent formufatk>n fn the general care. Titer ugh the left channel input pure weter is fed at a flow rate Q. Through the right channel inpun water is fed at the same
flow rote. The drnsity of both fluids equals 1000 kglm3, the vircosity equale 0.001 Paxf, the diffusion co efitr it nt of tte dye in weter, D = 2,6n b10-1 0 m2/r. Thus, the value of Srhmtdt number for this problem is 3,800. As the boundary conditions et ehe mie-amcr of the chanoel steady vetbcity profile was set. At the exti of rhe mioing cltanne/ Nenmttm tteditions wos set, i.e. iv/1.!^:ii;:i:i;sl;:i]L:nit oli tin normaf to the output surface component of derivative of all scalar quantities.
The study was conducted for diffeeent vnt/es of Reynolds number, whtch is defined as follows: Re = (ptM(i) wliere U = (//(2pH) is ite iElow rate-based average velofity id the mixing channel, H = 200(m is height of the channel and d = 267 (m is hydraulic diameter.
For the quantitative chrracterizatioe of thb mixing efficiency the following parameter was used:
M = 1 - e^(e/cn0 , where 1- = f • J" (/ - /^d r it tie coitcereratfon t r componentfst t^Iic:Cгl:rd deviation from
V V
its ^eai^ "Vi.ii^KS f by the volume (V) olie^ee, ct0 = /(l- f) i s the maximum stendaed deviation.
Experimental Set Up
The diagram of experimental setup is shown in Fig. 1. Imaging system consisted of epifluorescence inverted microscope (Carl Zeiss AxioObserver.Z1) with lenses 20x/NA = 0.3 and 5x/NA = 012 (number 1 in Fig.f) for micro-PIV aed micro-LIF experimentt, respectively. Lighting and rec otd that iLr^ir ggetti 0 n e digital camera using a measuring complex "POLIS" (number 3 in Fig. 1) were caroied out. This complex mcluded a eouble-puised Nd:YAG llascr with 50 mJ energy, «2 nm wcvelengte ^n<t. 88 Hz pulte repetitioh coeering the flow "hrough Ihe lens of the
micnostcoiTiu. ti1«:) emering the light iI/lto tbe microscope the liquid light gurde ¡and the Hers interface unit io the opticttl path (g]t the mierosfope weerc^ usedr Ir]Lghlltin^ of ehe microchannel during the micro-LiF e;;>i;tie^r^ri[ie;n^!^ carried out using a mercury lamp. Cnoetrorreiation digital camera recorded the imagec witt 2048hpixels resohttion, whith jarri; teen transhetred Ito a personal computed hoa processmg. Synchronization oC the rystem war cfrried out uaing a pprogrammable processor. Contnolling of thee experiment and data processing wece ctrried out using the software package ActualFlow.
Fluid motion control usrng infusron syringe pump (numJjeo 5 in Fig. 1) with adjustable liquid flow rate was carried out The flow oe liquid sow by fluorescent ihfterc from DukeScirntiíic firm. The particles were composed of melamine resin, labeled with fluorescent dye Rhodamine B. The particle dentity it L05 g/cmh tverage diameter is 2 (m; thr stondard deviation is 0.04 (nm. To register the light emiytfd zfro^m the partieles, and lhe fuppr2trton the ltght Oram the channel, beam-splitting
cube, consisting of a dichroic mitror and two filtets for - xcttation aed dftection of Rhodamine B was used.
T-c+ianneJ
Fig. 1. The experimental setup
Micro-PIV and micro-LIF experiments were conducted at Reynolds numbers ranging from 10 to 300. The measurements were carried out in three regions of the T-mixer (so that the velocity field has been calculated up to seven calibers from the mixing channel entrance).
Concentration range in which the luminescence intensity of the fluorophore has a linear dependence on concentration was determined to calibrate the measurements. For this purpose, the T-channel is fed aqueous solutions of Rhodamine 6J in the following concentrations: 0 mg/l, 10 mg/l, 25 mg/l and 40 mg/l, 50 mg/l, 62.5 mg/l and 75 mg/l. For every concentration of the fluorophore the image of the channel was registered. As a result, linear dependence of the fluorophore radiation intensity was found at concentrations less than 62.5 mg/l. Thus, the relationship between the concentration of the fluorophore and the intensity of the image at each point of the channel was obtained.
Comparison of Calculations with Experimental Data
The Reynolds number in the range from 1 to 1000 was varied in the calculations. At low Reynolds numbers (Re < 5) in the mixer occurs steady irrotational flow. Mixing in this case occurs due to usual molecular diffusion and mixing efficiency is quite low [15] (see Fig. 2). Further, with increasing Reynolds number a pair of symmetrical horseshoe vortices (Dean vortices) formed in the mixer. They generated at the left end of the mixer wall (see Fig. 3, left) and extended into the channel on the mixing length, depending on the Reynolds number. Horseshoe vortices appear due to the development of secondary flows caused by the centrifugal force associated with rotation of the flow. Dean vortex structure is shown in Fig. 4 with isosurface X2. Here X2 is the second eigenvalue of the tensor (SS + fifi), where S is the rate of strain tensor, and fi is the vorticity tensor.
The flow in this case is symmetric about the central longitudinal plane of the mixer. Each horseshoe vortex, being in the range of one liquid, does not cross the media mixing boundary, so the boundary between the media remains almost flat. This is clearly seen on the Fig. 3 (right). And because the diffusion Peclet number increased with increasing Reynolds number, the mixing efficiency decreased (see Fig. 2).
Re
Fig. 2. Mixing efficiency versus Reynolds number
Fig. 4. Izolines of the dye concentrations in 4 longitudinal sections of the mixer: Re = 186 (left), Re = 600 (right)
When the Reynolds number reaches 150, the vortices lose their symmetry (see Fig. 3, right). They are rotated through an angle of 45° relative to the central plane of the mixer cross-section. S-shaped vortex formed. This is particularly clearly shown in Fig. 4 (left), where mixing is shown by isolines of the dye concentration in the four cross sections of the mixer. First left section is located at the entrance to the mixing channel, second - at the distance of 100 ^m from the entrance, third - at the distance of 200 |im and fourth - at the distance of 400 ^m. It is important to emphasize that flow is still stationary.
However, due to the fact that the intensity of the vortices in the asymmetric flow regime increases significantly, they extend through the mixing channel up to the exit. The presence of swirling flow in
0.005 0.0055 0.006 0.0065 0.007 0.0075
Fig. 5. The flow velocity versus time in point located at the mixer outlet. Red - Re = 300, blue - Re = 600, green -Re = 1000
the mixing channel leads to a layered structure of the miscible fluids formation. The contact surface of the miscible fluids in the layered structure is developed, which leads to a sharp increase of the mixing efficiency (see Fig. 2). In the transition from a symmetric flow regime (Re < 150) to the asymmetric (Re > 150), the mixing efficiency increases by 25 times.
Described stationary asymmetric flow regime is observed in the range of Reynolds numbers from 140 to 240. Starting from a Reynolds number of approximately equal 240, flow ceases to be stationary. In the range of Reynolds numbers 240 < Re < 400 implemented periodic flow regime. In particular, it means that the flow velocity is also a periodic function of time. In Fig. 5 this flow regime corresponds to the lower curve. The flux oscillation frequency f is determined by many factors: the geometry of the channel, the fluid viscosity, the Reynolds number. To describe this dependence, we introduce the Strouhal number St = /^/(vRe), which is actually the dimensionless frequency of flow oscillations normalized by the Reynolds number (v is the kinematic viscosity). A diagram of the Strouhal number versus Reynolds number is shown in Fig. 6 (squares). The oscillation frequency increases monotonically to a value of Re = 300 and then decreases slightly.
Our calculations data are correlated accurately with experimental one [16], which in Fig. 6 are marked with red tags. Maximum differences are observed at high Reynolds numbers, but it should be noted that the experimental data were obtained for a channel with cross-sectional dimensions of 600^mx300^m.
Meanwhile, the layered mixing structure which was formed at Re > 150 is preserved in whole, and due to transverse flow fluctuations in the unsteady flow regime the mixing efficiency increases to about M = 40% (see Fig. 2).
Starting from a Reynolds number of 450, the frequency of flow oscillations gradually decays. Firstly flow becomes quasiperiodic (450 < Re < 600), and then almost chaotic (Re > 600). The frequency spectrum of the velocity field becomes sufficiently filled, and is close to the continuous. This is clearly seen in Fig 5 (see also Fig. 4 (right)), where the Reynolds number 600 corresponds to the medium curve, and the Reynolds number 1000 corresponds the top one.
Re
Fig. 6. Strouhal number versus Reynolds number
The distribution of the flow pulsation kinetic energy e by frequencies for Re = 600 is shown in Fig. 7. This spectrum is obtained for a point located in the center of the mixing channel at a distance of 400 (im from the enteance. Straight dashed line on the graph corresponds to the univereal law of ehe Kolmogorov-Obukhov.
Although for Re = 600 the spectrum can not; be considered complete continuous, as in the cate of developed turbulent flow, nevertheless, therr aee a larno number eel" frequencies and the inertial range, which suggerts, at least availability of trine transotional flow regime. Such oarly beginning of turbulence for channels flow occurs due to the development of Kelvin-Helmholtz instability at the entrance of the mixing channel.
However, calculations show that if mixing channel is long enough, then with increasing of the distance from the flow confluence the pulsations gradually damped, the flow became laminar and,
1.8/Re0'25
0.1 -1-1- 3
1 10 100 1 -10
Fig. 8. Friction factor versus the Reynolds number
as expected, the steady velocity profile is formed. The length of the velocity profile establishment, of course, depends on the Reynolds number. To show it the problem for a channel 7000 ^m length was solved. The obtained data is illustrated in Fig. 10, where compares the velocity profiles for the two Reynolds numbers: 30 and 120.
This coefficient is determined by formula I = (2APd)/(pU2L) where AP is the pressure drop in the channel, and L is the length of the channel. The dark mark and the line connecting them correspond to calculation. To compare the results the values of friction factor for steady laminar flow in a rectangular channel is shown on the graph by the dashed line.
For a channel with height-to-width ratio equal to 0.5 the friction factor is close to 64/Re. Nevertheless, the analysis shows that for small Reynolds numbers the friction factor in micromixer on average 20-30% higher than for steady flow. Then the friction factor dramatically deviate from the dependence I = 64/Re, indicating the laminar-turbulent transition. The calculated data of the friction factor in micromixer at moderate Reynolds numbers is well described by the dependence I = 1.8/Re025. Obtained value of the friction factor is almost six times higher than the classical Blasius dependence (I = 0.316/Re025) for the developed turbulent flow in the direct channel. Such large difference is due to the presence of a turning flow at the channel inlet, and its vortex in the mixing channel. In particular, the pressure along the channel does not change monotonically. In the transition to turbulence, S-shaped vortex structure, that was formed in the mixing channel at Re > 150 and existed in the transient regime collapses. The flow is divided into a set of sufficiently large eddies. Because of it the contact area between the miscible liquids reduced. And so mixing efficiency slightly decreased on transition to turbulence (see Fig. 2). Naturally, with further increase of the Reynolds number a lot of small-scale vortices appeared in the flow.
As a consequence, the mixing efficiency in the developed turbulent flow far exceeds suitable value for laminar flow.
Comparison of the experimentally measured by micro-PIV and calculated velocity profiles in the central section of the mixing channel at 2.5 calibers from the input are shown in Fig. 9. The appearance
0 5 ID 5 1 10 4 1.3 10 4 MO 4 15-10 4 MO 4 3.5-10 4
£111
Fig. 9. Velocity profiles in the central cross section of the channel.
of curve bends in the velocity profiles associated with the occurrence of an S-shaped structure. Overall agreement between the experimental and calculated data is quite good, the maximum error does not exceed 10%, but with increasing Reynolds number it's increased. This is due to essentially three-dimensional structure of the flow at a given Reynolds number.
For example, in micro-PIV measured velocity field is the average depth of correlation (in this experiment it was equal to the depth of correlation 37 microns), the gradient of the longitudinal velocity of the channel depth has led to a smoothing of the velocity profile in the micromixer. A qualitative comparison of calculated and experimental velocity fields in the central longitudinal section of the mixer is shown in Fig. 10. Here also there is quite satisfactory agreement between the calculated and experimental data.
To compare the concentration fields obtained by numerical simulation and in the experiment the spatial averaging of the calculated data on the depth of the T-mixer was carried out. The concentration field in the 11 sections of XY plane on the depth of the T-mixer symmetrical about its center was taken to average.
Concentration field for each section averaged spatially using a "running average" filter with a round window the same diameter as the point spread function diameter in this section. The resulting concentration field was calculated as the arithmetical mean of 11 sections. The averaged concentration field obtained by numerical simulation and in the experiment for different Reynolds numbers are shown in Fig. 11 and Fig. 12. In whole, there is good qualitative agreement.
Conclusions
Thus, this modeling allows to sort out for the incompressible fluid flow in T-type micromixer following flow regimes:
• The steady vortex-free flow, realized at low Reynolds numbers (Re < 5).
- 23 -
Fig. 10. Average experimental and calculated velocity field in the central section of micromixer for Reynolds numbers equals 30 and 120
Re = 90 numerical Re = 186 numerical
Fig. 11. Averaged concentration field in the central section of micromixer for Re=90 and Re=186
• The steady symmetric vortex flow with two symmetric horseshoe vortices at the mixing channel inlet. This regime realized when the Reynolds numbers vary in the range 5 < Re < 150.
• Steady asymmetric vortex flow is observed in the range of Reynolds numbers 150 < Re < 240. Formed at the entrance horseshoe vortices lose their symmetry and rotated at 45° relative to the central longitudinal plane of the mixing channel. S-shaped vortices formed.
• Unsteady periodic flow is realized in the range 240 < Re < 400.
• Almost a stochastic flow regime (400 < Re < 1000). S-shaped vortex structures observed at lower Reynolds numbers collapsed.
The mixing efficiency increases dramatically during formation the S-shaped vortex structures in the flow and then continues to grow in an unsteady periodic regime. In paper [15] was shown that the mixing efficiency can be substantially increased by changing flow rate at the inlet of the
Fig. 12. The normalized concentration profiles across the mixing channel for Re = 30
mixer in a certain way by harmonical law. In fact, here we have some "autocontrol" of the mixing process.
Usually to ensure the efficient mixing, the mixer length should be large enough. Naturally, this leads to a significant loss of pressure caused by friction at the walls. On the other hand, such losses can be reduced by using hydrophobic or even ultrahydrophobic coats. In microflows the slip length can reach tens of microns. As it shown in [15], if the Reynolds numbers were low the mixing efficiency particularly didn't change. However, the situation is changing at moderate Reynolds numbers. The presence of wall slip leads to a significant change in flow regimes. If there are slip conditions the flows are rebuilt. Simulations show, for example, that at Reynolds numbers equals 200 and sufficiently large slip lengths the two-vortex structure mentioned above is transformed into one-vortex. Naturally, the mixing efficiency increased too. For this mixer an increase is about 30%. On the other hand, the pressure drop decreases monotonically with increasing the slip length (for investigated mixer for about 30-40%). Thus, using a hydrophobic coats (slip conditions) one can control the flow regimes.
Acknowledgment
This work was supported in part by the Russian Foundation for Basic Research (Grants №. 10-01-00074 and 11-08-01268) and the Federal Special Program "Scientific and scientific-pedagogical personnel of innovative Russia in 2009-2013" (№ 16.740.11.0642, 14.A18.21.0344, 14.132.21.1750, 8756).
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Micro-LIF и численное исследование смешения в микроканале
А.В. Минаковаб, А.А. Ягодницынаб, А.С. Лобасоваб, В.Я. Рудякбв, А.В. Бильскийб
а Сибирский федеральный университет, Россия 660074, Красноярск, ул. Киренского, 28 бИнститут теплофизики СО РАН, Россия 630090, Новосибирск, пр. Лаврентьева, 1 вНовосибирский государственный архитектурно-строительный университет, Россия 630008, Новосибирск, ул. Ленинградская, 113
В статье с помощью численного моделирования и экспериментальных методов micro-PIV и micro-LIF исследованы режимы течения и смешения жидкостей в микромиксере Т-типа в широком диапазоне значений числа Рейнольдса от 1 до 1000. Поперечное сечение канала равнялось 200 мкм*400 мкм, а длина канала была равна 3000 мкм. Было обнаружено пять различных режимов течения: (I) стационарное безвихревое течение;
(II) стационарное симметричное вихревое течение с двумя подковообразными вихрями;
(III) стационарное асимметричное вихревое течение; (IV) нестационарное периодическое течение; (V) хаотическое течение. Максимальное значение эффективности смешения наблюдается при стационарном асимметричном вихревом течении. В этом случае в потоке формируются S-образные вихревые структуры. Показано хорошее соответствие расчётных и экспериментальных данных.
Ключевые слова: микротечение, микромиксеры, микроканалы, CFD, Micro-PIV, Micro-LIF.
