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In this study, a single bubble behavior in dielectric viscous fluid under the uniform magnetic field has been simulated numerically by using a level set method in two-phase bubbly flow. The two-phase bubbly flow considered to be laminar and homogenous. Deformation of the bubble was considered due to buoyancy and magnetic forces induced from the external applied magnetic field. A computer code was developed to solve the problem with flow field, interface of two-phases, and the magnetic field. The Finite Volume method was applied using SIMPLE algorithm to differentiate the governing equations. Using this algorithm enables us to calculate the pressure parameter which was eliminated by previous researchers due to complexity of the two-phase flow. The Finite Difference method was used to solve the magnetic field equation. The results outlined in the present study well agree with the existing experimental data and numerical results. The results show that the magnetic field affects and controls the shape, size, velocity and location of the bubble.

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Two-phase flow modeling has been the subject of many investigations. However, fewer studies are corresponded for two-phase flow within a porous medium, because of additional complications. In this paper, two-phase flow with the density and viscosity ratio of 1, within a porous medium is simulated by Shan and Chen model. Due to inherent limitations and weaknesses of this approach in an independent control of surface tension, investigation of parameters such as Reynolds number, Froude and Weber is not applicable. However, porous medium parameters such as Darcy number and contact angle could be studied by changing the porous medium and contact angle. Competition between opposing forces against the drop and the capillary effect because of increasing the number of particles in the porous media is described using the Darcy number. Also the effect of the contact angle between liquid-gas phases and the solid surface is evaluated on the droplet penetration inside the porous medium.

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Abstract It has been proved that developing a supercaviting flow over under-water projectiles has an important role on their drag reduction, so many of researchers have focused on this subject during recent decade. In this research, the geometrical characteristics of supercavitaties developed behind three different conical cavitators with conic angles of 30, 45 and 60 degrees are studied numerically and experimentally. The experiments were done in an open-loop water tunnel. The fluid flow velocity in the test section was between 27 to 38 m/s. Also the 3D multiphase fluid flow over the cavitators within the test section are modeled and analyzed numerically by solving the corresponding governing equations using finite volume method and mixture model. Good agreement was observed in comparison between the numerical and experimental results. Finally, effects of some important parameters .i.e. the cavitation index, inlet velocity and conic angle of the cavitators on the geometrical characteristics of the supercavities are discussed

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This study is an experimental investigation of two-phase water-air flow in hilly-terrain duct.The inclination angles for hill and valley configuration is ±7.5o. Review of the related literature showstheir results are limited to slug regime only. In the present study, flow regime map and pressure traces are investigated. This study reveals that the possible slug flow behavior categories exist along a valley and hill configuration are four and two, respectively. In an attempt to relate the qualitative flow behavior at a valley and hill to the flow pattern maps of upstream and downstream, this qualitative classification is superimposed on flow pattern maps where obtained independently for the upstream and downstream sections. The results show, flow has different behavior in hill in compare to valley at relatively low gas flow rates. However, at higher gas velocity, difference between hill and valley behavior decreases.It can be concluded, that the effect of hill and valley behavior are similar on flow regime at relatively high gas flow rates.

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In this article, two-phase slug flow is simulated numerically in a horizontal duct with rectangular cross-section using Volume Of Fluid (VOF) method. Conservation equations of mass, momentum and advection equation are solved in open source OpenFOAM code accompanying k-ω SST turbulence equations. Simulation is conducted based on the experimental results in the duct with rectangular cross-section. The results shows, due to Kelvin-Helmholtz (K-H) instability criteria slug initiation forms in the air-water interface during three dimensional turbulence modeling. Water level was increased slightly at interface in both numerical simulation and experiment. This level increase satisfies the K-H instability to generate a slug at interface. During slug initiation, the pressure behind slug is increased significantly. Big pressure gradient at the beginning of the slug in compare to the end of it causes the slug length to be increased as propagate along the duct. The numerical simulation of present research is capable of predicting the slug length accurately in accordance with experiment; however, the slug position with 22% inaccuracy was obtained. Comparison of the results with the numerical and experimental results of other researchers confirms higher accuracy of flow prediction in the present work.

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Experimental investigation conducted on Taylor bubble characteristics in a large bend including three consecutive inclinations. For this purposes, flow maps were obtained for the bend and horizontal section of upstream of the bend to define the area of this regime and mechanism of Taylor bubble formation. The effect of superficial gas-liquid velocities and the duct slope were studied on average velocity, length and frequency of bubbles. The results show, the bubble velocity and length increase as gas superficial velocity increases and the duct slope decreases. However, liquid velocity increase has decreasing effect on this characteristics. Bubble frequency is independent of slope change and reduces as gas superficial velocity increase. However, bubble frequency reduces at first and then increase as liquid superficial velocity increases. Regarding the safety regulation for industry, the minimum of the bubble frequency should be generated for the required liquid mass flow rate. Meanwhile, for the gas velocity, some optimization is required between frequency reductions with Taylor bubble velocity increase in addition to bubble length reduction. Regarding the background of the present field with shortage of results on Taylor bubbles frequency, some correlations based on the superficial Reynolds number of phases were presented for each inclination.

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Experimental investigation of two-phase air-water flow was conducted at consecutive inclinations of a large bend (with three equal slopes in respect to each other) and including the horizontal sections of the inlet and outlet of the bend. The results show that the elongated bubble regime flows without any effect of duct inclination change and consistent for all three zones of horizontal sections of before and after the bend and the bend itself. It was also noticed, as the duct inclination decreases along the route, vortex misty flow transmits to misty annular flow at higher gas flow rates. The annular flow regime was noticed only at the first slop of the bend. Slug flow was observed at the horizontal sections upstream and downstream of the bend. The slug flow at the upstream generated by the interfacial instabilities but at the downstream formed by Taylor bubbles. Slug flow area in the flow diagram increases as liquid flow rate increase at both horizontal sections. In addition, the void fraction change rate with phases mass flow rate was considered at the duct inlet.

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In this paper, two-phase air–water flow was investigated experimentally and simulated numerically using VOF method. The tests are conducted in Multiphase Flow Lab. of Tarbiat Modares University. In order to evaluate the rib effect on flow regimes, experimental investigation was conducted with ribs of different width and pitch where assembled on front and back side walls (side walls) of the duct during different test runs. The rib width and pitch were held constant during each test. The experimental work considered for different regimes of wavy, plug and slug which generated in the ducts with and without rib applying various phase velocities. The effects of using ribs on regime boundaries are presented in the flow diagrams and discussed in details. Compared to the smooth duct, the ribbed duct affects the different regime boundary positions noticeabily. The results showed that in the duct with small sizes ribs, the first slug initiates at longer time and distance in compare to the duct equipped with bigger size ribs. The results show that for normal operational flow velocities, the ribbed duct decreases the slug area on flow diagram map in compare to smooth duct. However, ribs facilitate the slug regime initiation for phase velocities in accordance with slug generation, which is not benefit of operational condition.

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In this paper, a non - isothermal and two-phase flow in the cathode gas diffusion layer (GDL) of PEM fuel cell is modeled. To achieve more accurate boundary conditions, other components of fuel cell (membrane and anode GDL) are modeled. Governing equations including energy, mass and momentum conservation and auxiliary equations are solved by numerical method and the effect of gas mixture pressure in channels, relative humidity and effect of contact and mass exchange between two phases are investigated. Results show, it is necessary that both the contact and mass exchange between the gas and liquid phase to be considered. The performance curve and temperature distribution for single and two phase flow are compared for different amount of cathode channel humidity. The relative value of performance and temperature for single and two phase flow depends on the humidity of cathode channel. With increasing the cathode pressure from 0.5 to 5atm the value of water content in membrane and gas diffusion interface will increase about 20%. With increasing the water content in the membrane therefore the ohmic loss is reduced. With the reduction in the ohmic loss the temperature distribution along the fuel cell decreases but if the anode pressure increases the temperature distribution along the fuel cell increases. Keywords

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In the present research, two-phase flow is studied adiabatically in vertical plexigalss tubes with inner diameters of 40 mm and 70 mm in heights of 1.73 m and 3.22 m. Flow pattern maps are presented for both tubes and effect of diameter and height on the transition curves between flow patterns is investigated. Air and water are used as working fluids. Superficial velocities of air and water for 40 mm tube are 0.054-9.654 m/s and 0.015-0.877 m/s; and for 70 mm tube are 0.038-20.44 m/s and 0.036-1.530 m/s, respectively. By changing the tube diameter from 40 mm to 70 mm, slug pattern region shrinks considerably. Inlet is designed to be "annular" for which bubbly flow in 70 mm tube is not observed in low water superficial velocities. However, this pattern is observed in higher water and lower air superficial velocities. For both tubes, the main flow regimes observed are bubbly, slug, churn and annular. The results obtained using image processing technique show that bubbly regime in 40 mm can be divided into three sub-patterns called dispersed, agitated and agglomerated bubbly. In addition, two sub-patterns are recognized in slug regime as large slug and small slug. Also semi-annular pattern is observed as an independent flow pattern in tube with inner diameter of 70 mm which has not been analyzed accurately up to now.

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Present research has been done with the aim of investigating hydrodynamic behavior of slug flows in a transparent acrylic tube with inner diameter of 40 mm and height of 3.33 m. The vertical experimental system constructed in Two-Phase Flow lab in Tarbiat Modares University was used to perform needed experiments. By using image processing technique, recorded movies of flow structures were analyzed and some important characteristics of slug flow such as length and velocity of Taylor bubbles and liquid slugs between them were extracted. In addition, the average path line of Taylor bubble nose was computed in a proper range of the tube length. The acquired probability density functions show that there is a direct relationship between the increasing of Taylor bubble length and liquid slug length moving after it. Also rising velocity of shorter Taylor bubbles is more than longer ones. Results show that bubble nose does not violate ± 20 % around the center line of the tube. An experimental correlation based on the Taylor bubble velocity and total superficial velocities of phases is presented which shows that the famous Nicklen correlation does not work well for this tube diameter.

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Phenomenon of dispersion and deposition of nano- and micro-particles in turbulent flows been focused in the past decades. In this paper, particle dispersion and deposition in gas-particle two-phase turbulent flow inside a two-dimensional channel with rectangular artificial roughness is studied using an Eulerian–Lagrangian method. The RSM turbulence model with enhanced wall treatment was used to simulate the anisotropic turbulent gas phase flow. The gas phase flow predictions were validated by comparing the results with available experimental data for a fully developed asymmetric turbulent channel flow. In discrete phase, Lagrangian approach was applied for particle tracking. The Lagrangian equation of particle motion includes drag, gravity, Saffman lift, and Brownian forces. The particle phase simulation results were validated by comparing the present work with available equations and valid data for a gas particles turbulent flow inside a two-dimensional smooth channel. The gas phase simulation results show that by increasing the artificial roughness height, a recirculation region which is created in the space between two ribs, becomes larger. The particle phase results show that the rate of deposition in the channel with artificial roughness is a function of gravity force and flow pattern in the space between two ribs. The rate of deposition for small particle is affected significantly by gas flow pattern in the space between two ribs. However for large particles the gravity force is more dominant.

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In the present research, the high-order DG-ADER method is used to solve governing equations of two-phase drift flux model. The drift flux model is suitable for studying two-phase flows where the phases are strongly coupled. This model is composed of three differential equations including two continuity equations for two phases and a mixture momentum equation. The mixture model uses also an algebraic relation to link the velocity of the phases. The high-order DG-ADER numerical method, which is a new scheme to get high order accuracy of results, is used to solve the governing equations. The DG-ADER is a nonlinear method in which the reconstruction process is performed using WENO method and the time evolution part is achieved by discontinues Galerkine approach. The results are compared with those reported by other researchers. Three problems including two two-phase shock tubes and a pure rarefaction test problem are solved using this method. The results show that DG-ADER method can solve the two-phase flow problems with a very good accuracy even on a coarse grid. The drawback of this method is presenting numerical fluctuations with limited domain at the position of shock waves.

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In this article, a numerical solution of incompressible two-phase flow in isothermal condition, based on wetting pressure-wetting saturation formulation (Pw,Sw) using high order primal discontinuous Galerkin (DG) methods is considered which can capture the shock fronts of two-phase flow in heterogeneous porous media. In this presented model, the velocity field is reconstructed by a H(div) post-process in lowest order of Raviart-Thomas space (RT0). Also in this study, the scaled penalty and weighted average (harmonic average) formulation significantly improve the especial discretization formulation of governing equations which cause to reduce the instabilities in heterogamous media. The modified MLP slope limiter is used to remove the non-physical saturation values at end of each time step. In this study, the slope limiter should be considered as one of the main novelties due to the impressive effects in results stabilization. The proposed model is verified by pseudo 1D Buckley-Leverett and Mcwhorter problems. Two test cases, a problem for modeling the secondary recovery of petroleum reservoirs and other one a problem for detecting immiscible contamination are used to show the abilities of shock capturing two phases interface in porous media.

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The aim of this paper was to study the thermophoresis effect on the deposition of nano-particles from diesel engine exhaust after the dilution tunnel using a computational modeling approach. Dilution tunnel was used in order to dilute the exhaust gas to the extend that was suitable for the measurement systems. The Lagrangian particle tracking method was used to model the dispersion and deposition of nano-particles. For the range of studied particle diameters (from 5 to 500 nm), the Brownian, thermophoresis, gravity and Saffman Lift forces are considered. After verifying the code, the importance of different forces was evaluated. Due to the temperature gradient between the exhaust gas and the pipe walls, particular attention was given to include the thermophoresis force in addition to the other forces acting on nano-particles. The results showed that for the range of nano-particle diameters studied, the Brownian force was the dominant force for particle deposition. Furthermore, the thermophoresis force was important even for relatively low temperature gradient and cannot be ignorable especially for larger particles. The maximum thermophoresis effect occurred for 100 nm particles. The gravity had negligible effects on nano-particle deposition and can be ignorable for particles with diameter less than 500 nm. The Saffman lift also had negligible effects and its effect was noticeable only for the deposition of 500 nm particles. The results of this paper could provide an understanding of two-phase flow emission from diesel engines especially after the dilution tunnel.

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Spillways have long been of practical importance to safety of dams, therefore these structures have to be built strong, reliable and highly efficient. Ski jump dissipator is one the flow energy dissipators which is applicable downstream of spillway chutes with velocity over 20 m/s. Flow over a flip-bucket is a two-phase and strongly turbulent flow. Turbulence modeling is one of the most limiting factors in accurate computer simulation of flows. By fixing the grid resolution and the discretization scheme, the difference of computation time is mainly attributed to the turbulence model. The choice of turbulence model depends on factors such as the physics encompassed in the flow, the level of accuracy required, the available computational resources, and the amount of time available for the simulation. It is a fact that no single turbulence model is universally accepted as being superior for all classes of problems.
The main purpose of the present study is numerical investigation of two-phase turbulent flow over a triangular flip-bucket to evaluate effects of different turbulence models in this type of flow. Hence, using FLUENT® software, two dimensional Reynolds averaged Navier-Stockes equations have been solved in unsteady state. Different turbulence models consist of k-ε, k-ω and RSM; have been used. To simulate two-phase flow, volume of fluid (VOF) method has been applied.
Standard k-ε and stress-omega RSM models with low-Reynolds number modifications have the best performance among the other turbulence models. In standard k-ε model when low-Reynolds number modification was activated, the effects of molecular viscosity were taken into account in near-wall regions. Therefore, in low-Reynolds number k-ε model, maximum dynamic pressure over the bucket was predicted more accurately in comparison with standard k-ε model. Regarding modification in strain-pressure terms in turbulence equations, effects of anisotropic Reynolds stress tensor were taken into account in stress-omega RSM model with low-Reynolds number modifications. Thus, compared to other turbulence models, numerical results of this model are in a better agreement with experimental results. Different k-ε models could not predict the jet trajectory after the bucket very well. Due to blending function in SST k-ω model, this turbulence model effectively blended the robust and accurate formulation of the k-ω model in near-wall regions with the free-stream independence of the k-ε model in the far field. In estimation of maximum dynamic pressure over the bucket, this model had a better performance than standard k-ω model and relatively similar results to k-ε model. In addition, SST k-ω model has shown the best prediction of the jet trajectory among other turbulence models. Eventually, with respect to computation cost and accuracy of results, SST k-ω turbulence model has been introduced as the most suitable turbulence model to predict the flow pattern of a triangular flip-bucket.

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In this paper, gas-liquid two-phase flow in the annulus of a real well during under-balanced drilling operations is simulated numerically. Oil and gas flow from the reservoir in to the annulus is considered due to under-balanced drilling condition. A numerical code based on one-dimensional form of steady-state single pressure two-fluid model in the Eulerian frame of reference is developed and its results are validated using experimental data from two real wells. The results of numerical simulation show better accuracy in comparison with other researches. Given the importance of prediction and control of the bottom-hole pressure and the amount of oil and gas production during the drilling operations, the effects of controlling parameters such as liquid and gas injection flow rate and choke pressure are discussed. Also, the effects of different controlling parameters on the characteristics of two-phase flow pattern, including liquid and gas void fractions, liquid and gas velocities and pressure distribution along with the annulus are discussed. According to the results, the effects of choke pressure and injected liquid flow rate on the production of the oil from the reservoir are independent of the values of each other and are dependent on the injected gas flow rate.

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In this paper, the non-Newtonian immiscible two-phase polymer flow in a petroleum reservoir has been investigated numerically. The fluid flow in a porous medium is simulated as a compressible flow. The Carreau-Yasuda constitutive equation is employed as the model of non-Newtonian fluid. The IMPES method is used for numerical simulation, in which the pressure equation is discretized and solved by an implicit approach and the saturation equation is solved by an explicit method. Results reveal that zero-shear rate viscosity has a high impact on the sweep efficiency of the reservoir and also controls the channeling and viscous fingering effects. In addition increasing the viscosity of non-Newtonian fluid improves cumulative oil production and diminishes the viscous fingering phenomenon caused by injected fluid. The relaxation time of Carreau-Yasuda fluid, which is the elastic characteristic of the non-Newtonian fluid, for low permeability values cannot influence flow characteristics inside the reservoir, however for higher permeability values its effect becomes more sensible. Increasing the injection rates leads to the increase of fluid production, while the injection rate has an optimum range to reach the optimum oil production. In addition, the effect of variation of the injected fluid properties on the polymer breakthrough time has been investigated and results presented.

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In this research, counter-current two phase flow is investigated adiabatically in vertical Plexiglas tubes with internal diameters of 60 mm, 80 mm and 110 mm. All of tubes have the same height of 2 m. So far, there have been few studies on counter-current flows in large diameter tubes. Water and air flow downward and upward through the tubes, respectively. Superficial velocities of air and water ranges are 1.77-7.17 m/s and 0.05-0.11 m/s for 60 mm tube, 0.99-4.03 m/s and 0.03-0.09 m/s for 80 mm tube and 0.55-2.26 m/s and 0.01-0.05 m/s for 110 mm tube. In addition to reverse flow, other main regimes can be observed as slug, churn and annular in the tubes. Our efforts in drawing the flow patterns map were aimed at minimizing uncertainties at the boundaries. Based on the obtained experimental results, slug and annular regimes gradually comprise smaller regions of the flow map as the tube diameter increases. However, churn regime contains larger area of the flow pattern maps. Moreover, Kelvin – Helmholtz instability is observed in tubes and experimental and analytical results represent appropriate consequent in comparison. Eventually, validation of experimental flow patterns map accomplished by theoretical results.

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In the present study, flow regimes of co-current, air-water two-phase flow in a vertical tube with 70 mm internal diameter were investigated. Simulation accomplished by open source software, OpenFOAM, and One Fluid model has been used to simulate two-phase flow, which in this model, the interface of two-phase flow has been followed by Volume of the Fluid model. Hitherto, most of the researchers conducted experimentally and the researchers in many of numerical studies just investigated the small tubes. The simulation had investigated according to boundary conditions of the vertical tube. Air and water superficial velocities in inlet and pressure in outlet were constant. Moreover, a no-slip condition in the internal tube walls has been considered. The main purpose of this study is to identify the flow regimes based on the superficial velocities of air and water in the inlet. Moreover, the diagrams of density distributions of phases were obtained, with respect to the behavior of each two-phase flow pattern which can be identified. Superficial velocity of air and water were in the range of 0.01-15 m/s and 0.1-1.5 m/s, respectively. By analysis of results, bubbly, slug, churn and annular regimes; furthermore, semi-annular and Cap-Bubbly sub-regimes were observed.