Two-phase flow for gas-liquid, gas-solid, liquid-solid ...

Journal of Mechanical Engineering Research and Developments

ISSN: 1024-1752

CODEN: JERDFO

Vol. 43, No. 7, pp. 26-50

Published Year 2020

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Two-phase flow for gas-liquid, gas-solid, liquid-solid, and liquid-

liquid in a horizontal smooth and turbulator conduit – A review

Hyder M. Abdul Hussein†, Sabah Tarik Ahmed‡, Laith Jaafer Habeeb‡†

†University of Kufa – Faculty of Engineering ‡University of Technology – Mechanical Engineering Department

‡†University of Technology – Training and Workshop Center

*Corresponding Author Email: [email protected]

ABSTRACT: This paper presents a review of experimental investigations, the analytical formulations, and

numerical models of (gas-liquid), (gas-solid), (liquid-solid), and (liquid-liquid). Two groups of studies

turbulator and smooth in conventional passages tubes, pipe, and channels conduit are reviewed. Different

aspects such as flow pattern, pressure drop, maps, void fraction, and estimates of the kinetic energy and

momentum are of interest. The need to systematize the huge amount of manuscript published on the multiphase

flow and to understand the limitations of the techniques employed constitutes the motivation for this review.

Predicting flow pattern and transient flow conditions is developed at experiment (photographs, visual

observation, image processing, parallel wire conductance sensor and Particle Image Velocimetry visualization,

Planar Laser-Induced Fluorescence, Simultaneous two-line laser-based, high speed video-camera, Conductivity

needle Probe, and Gamma Densitometer) were used. In two-phase flows, the utmost decisive parameter is the

pressure gradient over the flow. Practically, the major thing for effective processes is a delicate prognostication

for the gradient of pressure over the flow of two-phase. An experimental study was generally obtained using

pressure transducer, and multi-tube manometer. Essentially, different kinds of patterns exist in order to identify

as a drift-flux pattern, homogeneous no-slip flow pattern as well as separated pattern. The numerical solution

has been steady state transitions to the unsteady state cases, which used code or commercial CFD software.

KEYWORDS: Multiphase flow, flow pattern, pressure drop, maps, and void fraction.

INTRODUCTION

The term multiphase flow is used to refer to any fluid flow consisting of more than one phase or component [1].

A phase is simply one of the states of matter and can be either a gas, a liquid, or a solid. Multiphase flow is the

simultaneous flow of several phases. Two-phase flow is the simplest case of multiphase flow [2]. The general

subject of multiphase fluid flow is widely used [3]. Multiphase flows in the context of fluid mechanics can be

perceived as a flow system that consists of two or more distinct phases flowing in a fluid mixture where the

level of separation between the phases is at a scale well above the molecular level [4]. Furthermore, the rate of

publication has been increasing in recent years. This work has been carried out at universities, national

laboratories, and at industrial research and design organizations in many countries of the world [5]. The

behaviors of multiphase flow under a wide range of flow conditions vertical, horizontal, and inclination angles

constitute an outstanding interdisciplinary problem with significant applications [6]. The condensation of steam

upon windows, the human body's blood flow as well as the rising of bubbles in a cold soda glass are models for

that. The constituents' nature and the relative distribution of them are the things on which these flows are

heavily dependent. The case that in which the same pure component is existing in two various phases for a flow

of two-phase is the simplest state of multiphase flow. The flow of steam - water is a model for that. Further, the

multicomponent flow is normally indicated to the flow that has various chemical substances.

Most common class for multiphase flows are two-phase flows and these include the following [7]:

1- Gas-liquid flows, which are probably the most important form of multiphase flow and is found widely in

industrial applications Such flow exists in a range of industrial plant which includes evaporators, condensers,

boilers, distillation towers, chemical reactors, air ejectors, pipelines for oil and natural gas, turbines, etc. [8].

mailto:[email protected]

Two-phase flow for gas-liquid, gas-solid, liquid-solid, and liquid-liquid in a horizontal smooth and turbulator conduit – A review

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2- Gas-solid flows, where solid particles are suspended in gases, which are of industrial importance in

pneumatic conveying, in the combustion of pulverized fuel and in fluidized beds.

3- Liquid-solid flows, which are widely encountered in hydraulic conveying of solid material. Suspensions of

solids in liquids also occur in crystallization systems.

4- Liquid-liquid flows, which include emulsion flows of oil and water in pipelines (of interest in the present

context) and flows through packed columns, pulsed columns, nuclear reactors, distillation columns, stirred

contractors and pipeline contractors in liquid-liquid solvent extraction.

Gas and liquid flow in horizontal pipes show a number of different interfacial configurations. Classification and

description of the flow distributions into different patterns are frequently very subjective [9]. This paper reviews

the multiphase flow in horizontal conventional conduit [10] smooth and ribbed walls which were done by

experimental and numerical work concerned with a system used gaseous, liquid, and solid phase for use in two-

phase. The main aim of this paper, given the significant recent to study the flow pattern, deference pressure,

flow pattern maps [11], and void fraction developments in experimental techniques and numerical solution, and

to provide broader guidance to experimentalists performing detailed, high-fidelity, numerical methods

aforementioned fluid-flow systems. Gas-liquid flows have received more attention than other forms of two-

phase flows and, in addition to the plethora of the experimental data, many predictive models have also been

developed [12]. Among the earliest studies in the gas-liquid field were by [13-21]. In the past, many studies that

are dedicated to the pipe of particle-laden as well as channel flows of various boundary conditions have been

issued. During one of the initial studies, developed for the one-dimensional flow of a gas, containing solid

particles of two different sizes was studied [22-25]. Tsuji and Morikawa gave an extremely itemized group of

tests for a gas-solid flow [26]. For the purpose of characterizing and parameterizing of turbulence modulation in

gas-solid flows Gore and Crowe they were frequently utilized [27]. By many researchers in horizontal pipes,

empirical data on the action of pressure gradient for systems of liquid-solid have been gained [28-33]. The

prediction of pressure drops and flow patterns is a complex problem and is treated mostly via correlations of

experimental data. Some of the empirical correlations claim to apply to all flow patterns for liquid-solid systems

[34-37]. At fully suspended flow, an uncomplicated model for the pressure drop has been mentioned by [38-40].

However, they based it upon an experimental relationship for the gradient of concentration. One of the first

studies in liquid-liquid flow was carried out where three flow patterns were identified by visual observations,

namely, stratified flow, bubble flow and mixed flow [41]. A number of studies have been conducted to develop

the efficiency of pumping for pipelines that crude oil transporting in it, however, these studies have been

performed in horizontal pipes [41-50]. The aims of the present review paper are: (1) to review and summarize

the recent studies focus in flow pattern, pressure drop, maps, void fraction, hold up, and estimates of the kinetic

energy and momentum for a two-phase flow with and without turbulator in conduit and (2) to present research

gaps which need to be considered for future research work in the area.

TWO-PHASE FLOW WITH TURBULATOR

Pipe and Channel that is coarser with turbulator or grooves are widely used in several applications such as

ventilation, turbine blades, heat exchangers, and refrigeration. Ribbed channels are commonly used for the

enhancement of convection heat transfer. Since the presence of ribs in the conduit generated a turbulence flow

by breaking the laminar sub-layer if compared with the smooth channel.

Gas-liquid flow

Zarnett and Charles [51] were the first to investigate the flow of air-liquid mixtures with continuous spiral ribs

having 1.57 and 2.79 of pitch-to-diameter ratios and the internal diameter is ¾ inch diameter Lucite tubes. The

main effect of the spiral rib was to move the gas phase away from the tube walls. Thereafter, Weisman [52]

performed testing of pressure drops as well as two-phase flow model through single and double helically

circular ribbed tubes both 2.54 and 5.1 cm circular tube and 3 m section with consistent wire spacing. 0.32, 0.64

and 1.27 cm heights were used for Helically ribbed of a circular cross-section. The ratios of helical twist

were1.2, 2.1, 2.3 and 2.5. It could be indicated from the results that the moment that the smallest velocity of

liquid passed, the flow of swirling annular noticed at low qualities. Consequently, over this smallest velocity of

the liquid, it is predictable that the critical heat flux would also be enhanced. Salcudean [53] investigated

experiments various obstruction shapes and sizes where pressure-loss coefficient along a 25.4 mm inside

diameter tube was measured. Then Hameed [54] examined an analytical with various obstruction shapes to


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investigate the pressure drop in horizontal air-water flow. Results gave a good agreement obtained between the

theoretical and experimental results for both 25% and 40% obstruction area, noting that the 40% obstruction

area has the best agreement than the 25%.

Figure 1. Shape and location of the obstruction in the channel. a- Central, b- Horizontal segment, c- Bottom

segment, d- Peripheral e- Vertical segment f- and Top segment.

Ansari and Arzandi [55] investigated experimentally adiabatic air-water two phase flow using rectangular ducts

that were smooth and ribbed to show the effect of ribs height on the boundaries, they also presented a flow map

diagram. Three ribs of different heights (1, 2, and 4 mm) were used shown in Figure 2. The rib width (10 mm)

and pitch (50 mm) were held on the bottom wall (waterside), on the top wall (airside) and on both the top and

bottom walls. The location of the ribs in the duct did not alter the shape of the flow regimes, but the regime

boundaries were considerably changed.

Figure 2. Geometry of the ribs.

Ansari [56] carried out experimentally at room temperature and atmospheric pressure was for the purpose of

investigating the impact of thickness for rib and pitch within a test section of rectangular ribbed having a length

of 3.6 m and 100×50 mm cross-section. For nine different configurations of rib, the transition boundaries and

the diagrams for flow model were achieved with 2, 4- and 8-mm thicknesses and 50, 60, and 80 mm pitches.

Unlike rectangular channel that is non-ribbed, the configuration of sidelong rib did not permit for the happening

of any stratified flow, boundary values undergo tangible changes. Despite wavy, slug, as well as plug flows

were parallel in both conditions of flow, the presence of rib created explicitly coarser forms of model, see Figure

3. Keeping the pitch constant, while increasing the rib thickness, results in various models of flow in order to

happen and spectacular variations in boundaries forms as well as positions.

a b c

f e d

In-Line H

H P

W

e


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Figure 3. Wavy flow model Samples in ribbed ducts.

Habeeb and Al-Turaihi [57] investigated the two-phase (air-water) flow around triangular–section obstacle in

rectangular channel experimentally and numerically for steady and unsteady flows. The horizontal rectangular

channel was made of transparent Perspex with dimension of (10 × 3 × 70 cm). The flow’s behavior and pressure

difference studied. Four different values of water flow rate (20, 25, 35 and 45 l/min), and four different values of

air flow rate (10, 20, 30 and 40 l/min) were used. CFD used to perform the numerical study by fluent package. It

found that the pressure difference increased as the flow rates of air or water increased, and more turbulence seen

which produced more bubbles and waves.

Huang [58] used the fluctuating pressure produced by a bluff body in order to identify the flow actions of gas-

liquid two-phase for introducing a disorganized property index as well as a correlation dimension. The inner test

pipe has a diameter D of (50 mm). The front face width cross section was (w = 14 mm) of the bluff body a

truncated isosceles triangle which inserted through the pipe, as shown in Figure 4. The bluff body to the test

section ratio was (0.28), that in the bluff body wake, it could produce intense and uniform vortex shedding. A

synthetic neural system trained to assist chosen proper parameters of flow which connected with correlation

dimension in order to create a new flow pattern map of gas-liquid, that had the ability to recognize among the

slug, plug, bubble/plug transitional, bubble as well as annular flows including sensible correctness. Moreover, a

quantitative relationship having the style of ug=AD2B uC was established by the universal fitting and the pattern-

specific fitting with the coefficients of determination R2 approaching to one. In view of the simplicity and the

convenience of vortex generation and pressure measurement, the correlation dimension-based method provided

an effective and practical idea to gas-liquid two-phase flows study.

Figure 4. Sectional view of the bluff body (a) Overall structure; (b) Dimensions of the bluff body in mm (c)

Side view.

Gas-solid flow


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For rib-welding wall as well as smooth wall, an equipment was planned and the identical test was done by Song

[59] for the purpose of verifying the results of CDF. Both computational by using k-ɛ model and results of the

experiment showed that wall erosion produced from the effects of the particle in the particular two-phase flow

was reduced by supplementing ribs on the wall. The wastage of the wall does not change linearly as the height

of the rib. The area of test section inlet is 300 × 125 mm, and the area of test section increases gradually along

the flow direction. Particles are coal ash with 57 µm mean particle size and arc let out influx of 10 kg/min.

When the width of rib width was tantamount to the gap among fibs and under a specific height of rib, it was

utmostly profitable to decrease erosion. In the zone that has relatively small size of the particle, the change of

the rate of wastage undergoes steeply variation, whereas the size of particle passes a criterion, the rate of

wastage undergoes smoothly variation, and for a specific flow. The wall wastage impact by the first angle of the

direction of movement among gas and particles

Bin [60] and Zhou [61] have been investigated vortex structures and particle dispersions inflows around a

circular cylinder. The first group researchers studied gas-solid two-phase flow across a single cylinder and two

tandem cylinders by using Lagrangian-Lagrangian model at high Reynolds number. The settlement, entrainment

and aggregation of solid particles moving with the large-scale coherent vortex structure in the wake of a single

cylinder and between two cylinders numerically investigated, and the effects of St Number on the distribution of

solid particles obtained. The second group researcher’s verification of vortex structures and particle dispersions

inflows around a circular cylinder by lattice Boltzmann method (LBM), with Non-equilibrium Extrapolation

Method (NEM) dealing with the computational boundaries. The Reynolds number (Re = 40-100) effectiveness

on the growth of the structures of vortex studied. Perfect deals of Strouhal number, the lift coefficient, as well as

drag coefficient, reached with prior searches. For both Stokes number and Reynolds number, it discovered that

they provide an important impact on the arrangement of particle. The small particles (St = 0.01) succeed the

fluid movement so strongly and have the ability to scatter within the core zones of the vortex frame.

Yan and Rinoshika [62] built an experiment pipeline test has a horizontal smooth acrylic tube of about 5 m

length and 80 mm inside diameter. The polyethene is particles diameters 2.3 and 3.3 mm with a density of 978

kg/m3 and 952 kg/m3 utilized as test materials. The arrangements of concentration and the time-averaged

particle velocity estimated at 0.45 kg/s and 0.40 kg/s of the flow rate of solid mass as well as the lower air

velocity in fully developed as well as the acceleration regimes. It was noticed that although the velocities of air

for utilizing fins are minimal as compared with that of non-fin, the concentration of particle for utilizing fins

presents nearly the same profile as that of non-fin. It suggests that the long fins easily accelerate the particles

and result in low-pressure drop and low air velocity. Within the low pipeline portion, the vertical particle

velocity reduces, because of the impact of fins oscillation, producing in the dispersal of particle and the decrease

of collision for particles-wall.

Figure 5. Mounted soft fins in a test pipe.

Borello [63] presented two-phase flow in a rib-roughened duct describing the turbine blade internal cooling

channel. Means of the k-ε-ζ-f elliptic relaxation model utilized for measuring of the flow field and validation

versus the data of LES executed. The well-validated T-Flows FV code as utilized in the purpose of calculations.

Particle-laden flow simulated considering actual properties of the particle. Particles are moved by carrier flow


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(here modelled with a steady RANS) utilizing a one-way coupling way in a Lagrangian framework.

Mechanisms of adhesion and impact reduced utilizing the Thornton and Ning way intending at recognizing the

zone at which deposit happens. The rotation impact upon the movements of the particle as well as the flow will

be studied within RANS intending at identifying the deposit regions adjustment while the particle-laden flow

submitted to Coriolis forces and centrifugal.

Figure 6. Comparison of LES and URANS streamlines and mean velocity field in the central vertical plane.

Liquid-solid flow

Pathak [64] numerically investigated the impact of the impediment bed on the dispersal of solid particles in a

flow of two-phase. In order to model this flow, an algebraic slip mixture model utilized and in order to

determine flow turbulence, the re-normalization group k-ɛ model utilized. For the purpose of investigating the

impact of three various sizes of solid particles on turbulence modulation, calculations were presented for them.

Within the region including the wake and stagnation regions, a deformity of the self-similar mean velocity

profile recognized containing the standard layered dispersal of solid particles and that was due to the retardation.

Its length rises with the size of particle. High preferred deposition of particles characterizes stagnation region,

while a low concentration gradient exists within the wake region. As the size of the particle develops, the impact

of wake vortices on particle dispersal reductions. The strength of turbulence develops with the size of the

particle, whereas within complex flow regions for larger-sized particles, comparative turbulence modulation

recognized.

Pathak and Khan [65] made a computational investigation within a solid-liquid two-phase flow in a rectangular

duct in order to investigate the impacts of the size of the particle on flow turbulence and inter-phase slip

velocity. In the simulation, the procedure of finite volume beside renormalization k-ε style and an algebraic slip

mixture style has been utilized. In order to explain the influences of three various sizes of particles upon mean

and turbulent flow characteristics, simulations have been done for these particles. In the recirculation and

stagnation regions, the existence of retardation varies the standard layered arrangement of microparticles where

the recirculation region identified by the low value of solid particles concentration and stagnation region

identified by high value. The slip velocity among the particles and liquid phases has recognized further within

the upstream than the downstream of the retardation. Slip velocities, as well as particles arrangements variation

made due to the existence of retardation, vanish at an appointed downstream distance of the retardation and the

characteristics of flow recapture their un-disturbed cases. The size of the particle is what this settling distance

relies on. The flow turbulence improves by particles, and for partials of large size, the impact in the region of

complex flow has noticed more. Although Stokes number connected with the flow is small, slip velocity as well

as the turbulence have developed because of the disruption of the flow formed by the retardation.

Liquid–Liquid flow

Wong [66] made in the flow of an oil-water mixture within a parallel-plate (single fracture) style, a study of the

pressure gradient/phase saturation relationship. For the relationship, it noticed that it consists on the interaction

among the two flowing fluids, or pattern of flow, that conversely ruled by the flow rate of water, fracture surface

roughness, viscosity ratio, fracture aperture, and injection method. Three distinguished patterns of flow

recognized, namely, mixed, dispersed, as well as channel flows. Determinations of phase saturation, as well as

pressure gradient, propose that the publicly utilized Romm’s proportional permeability correlation viable to


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channel flow in which water oil and phases were continuous in the split. In the flow that in which either the oil

or water phase was discontinuous, for dispersed or mixed flow, a Lockhart-Martinelli kind relationship formed

for the flow of gas-liquid within pipes must be correct not at high viscosity ratio and water flow rate but at low

viscosity ratio.

TWO-PHASE FLOW WITHOUT TURBULATOR

There are many common examples of two-phase flows. Some, such as fog, smog, smoke, rain, clouds, snow,

icebergs, quicksand, dust storms, and mud, occur in nature. Others, such as boiling water, tea making, egg

scrambling, and sugar stirring are frequent occurrences in kitchens and dining rooms.

Gas-liquid flow

In special, the channel permits the investigation of air/water slug flow at atmospheric pressure. Parallel to the

tests, CFD estimations provided by Höhne [99]. Under the HAWAC test facility, a specific inlet device presents

fully defined as well as changeable boundary conditions, that provide so great CFD-code effectiveness

possibilities. A picture series filmed through slug flow matched with the equivalent CFD simulation produced

by the code ANSYS CFX. The two-fluid model implemented with a specific turbulence damping method at the

free surface. An Algebraic Interfacial Area Density (AIAD) model based on the completed mixture model

presented and completed. It improved the physical modelling; discovery of the morphological model and the

identical switching of every relationship was now potential. While variations need continuity of the work, the

behavior of slug generation and propagation at the test system reproduced. Tests similar velocity and pressure

determinations designed and will permit quantitative comparisons at other superficial velocities.

Zeguai [67] done empirical research intends at explaining two-phase flow patterns of air-water for laminar flow

with accurately managed conditions in a horizontal tube. In order to create a two-phase flow in a glass tube

having an internal diameter of 3 mm with co-current water and air flows, empirical test equipment has been

introduced. For superficial velocity of the liquid and gas, the ranges of studies were from 0.78×10-3 ms-1 to

79×10-3 ms-1 and from 2.3×10-3 ms-1 to 3.54 ms-1 sequentially, unlike earlier investigations. a high-speed camera

has been utilized in order to record flow visualizations in the region of the entrance at L/D = 10 in

correspondence to the two phases mixing zone and far away downstream at L/D = 420. The effects utilized for

highlighting the patterns of flow in both regions. Various patterns of the flow namely annular, slug and bubbly

flow pattern gained inside the investigated ranges of superficial velocities. In the entry zone, extra complicated

patterns of flow conceived that develop to uncomplicated and fewer arrangement of flow with smoother,

interfaces downstream. Maps of the flow were drawn and submitted. They explain some rearrangements of the

pattern. In the paper, the physical explanation of the variety within the structure of flow among the two studied

regions and a full explanation has been provided.

McCaslin and Desjardins [68] conducted for three various groups of conditions in the flow regimes of stratified-

annular as well as annular within horizontal pipes, exploratory mathematical simulations of liquid-gas flows. In

order to select dominated parameters in a form that yields flow that were related to factual implementations of

engineering while resting computationally tractable, the accurate dimensional investigation was utilized.

Statistics of the height of the liquid film and the velocity field estimated as a circumferential location function in

the pipe, showing the presence of a viscous sublayer in the liquid film, and a viscous layer near the interface and

a log law zone in the core of gas. As the impacts of gravitational development, it has been noticed that, the dry-

out conditions’ possibility at the wall within the above sections of the pipe has been developed. In order to

inform the mechanisms that are probable for liquid film sustainment, analyzing of circumferential motion of the

phases of gas and liquid in the cross-section of pipe has been done. An uncomplicated model improved which

assists in aids in learning the secondary gas flow impact on the film circumferential motion as well as identify

the liquid annulus dynamics. Comparison for the asymmetry of film, a fraction of void and height of film

against the empirical relationships obtainable in the literature has been done.

Oliveira [69] characterized elongated bubbles at approximately atmospheric conditions in a horizontal pipe

analytically for the flow of air-water. The flow rates range used covered regimes at the transition from the


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elongated bubble to slug. In order to discover the interface of liquid-gas with the helping of a collection of photo

gates for synchronization passage of bubble with the acquisition of image, ensemble-averaged digital image

treatment techniques utilized. Quantitative data of tail, as well as front bubbles portions examined for various

velocities of mixture and the results, proved visible notes usually described during the literature. Near to

transition, a linear inclination of the nose of the bubble to proceed towards the centerline location of the pipe, for

frequently larger amounts of the Froude numbers, quantified as well as recognized. The hydraulic jumps are

noticed to be subject of Froude number and bubble tail shapes quantified, whilst the liquid volume fraction

governed the thicknesses of the liquid film. Variations on the properties of bubbles were clearly connected to

changes in the velocities of bubble and appear to display an opposition among inertia and viscous impacts.

Bae [70] conducted experiments using PIV visualization in a rectangular channel and a parallel wire

conductance sensor, that has 50 mm height and 40 mm width. During the tests, the condition of flow included

the gas Reynolds number Reg range of 14,000 to 70,000 and the liquid Reynolds number Rel range of 450 to

3540. The results showed that the kinds of perceived wave according to the conditions of flow within the

rectangular channel were comparable to those in a horizontal pipe. Complicated trends according to the

gathering of Rel and Reg have been displayed from the interfacial wave slope, frequency and height, which

impacts the wave breakup as well as coalescence. Particularly, the wave slope, as well as wave height, contain

adverse trends about the standard of Reg=34,000. The interfacial drag force significantly impacts the disturbance

wave slope and height for states in which Reg ≥34,000. On the other hand, for Reg < 34,000, the wave

development contains a significant impact on the parameters of the wave. Lastly, new empirical correlations for

the interfacial wave slope, frequency and height introduced for utilization to the improvement of a droplet

entrainment model in a horizontal stratified flow.

It was essential to estimate the impact of surface tension that change by large quantity (air/water = 72 dyne/cm

and gas/oil = 35 dyne/cm) on flow regime map for the purpose of improving flow regime maps generality,

which was done by Bageri [71]. Consequently, the aims of this study are the evaluation of the surface tension

influence upon the flow regime map and address its utilization. Development of a number of flow regime maps

gas-liquid flow area in horizontal pipes has been done. Moreover, some dimensionless groups and parameters of

the mappings are applied as coordinates in order to express the flow regime maps. The combination of

dimensionless number and parameters are utilized for the purpose of generalizing the applicability of the flow

regime maps. Consequently, many of empirical data is needed to create these maps and normally it is not

achievable to estimate the influence of every single parameter (viscosity, density, surface tension, geometry or

pipe size) upon the flow regime map. Evaluating the impact of surface tension flow regimes horizontal pipe for

the water system is the purpose of this research. For the purpose of evaluating the surface tension impact, the

tests were carried out with two-phase water-air system. Decreasing the surface tension with the support of

surfactant has been utilized in order to introduce the surface tension impact. In order to create a flow pattern

map, the test data was used and based on the change in the boundaries of various flow patterns, the surface

tension influence was estimated. For evaluating the impact of the surface on the boundaries of various flow

patterns, four various concentrations (0.01, 0.05 0.1, 0.5%) of surfactant have been chosen.

Silva [72] aimed to compare pressure gradients of natural gas and heavy oil mixture in a horizontal pipe for

various flow patterns utilizing the application Lockhart and Martinelli, ANSYS CFX 13.0, and Beggs and Brill

relationships. The study examined the outcomes for stratified, plug as well as bubbly flows. The results

displayed that Beggs and Brill over prophesied values of the pressure gradient. It additionally noted a great

correspondence among Lockhart and Martinelli and numerical relationship for flows of bubbly and plug,

including 5.78 and 19.55 per cent root-mean-square deviations (RMSD), sequentially. The results of numerical

displayed a weak correspondence as for cases of the stratified flow, including an RMSD higher than 90 per cent.

The high per cent variation for this flow regime was because of the increase in the gas input content. They

proposed the use of free surface and turbulence models and also various values of drag coefficient in the

numerical setup for estimating the high gas velocity influences and, therefore, develop the correspondence.

Eyo and Lao [73] used gas-liquid flows in annulus channels are considerably encountered in the underbalanced

drilling process when the gasified drilling fluid. For gain, a larger knowing of the behaviors of flow in the


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channels, therefore to secure an effective drilling process reached, an exact description of two-phase flow

regimes in such channels is critically essential. Test investigations concerning gas-liquid flows in a concentric

and fully unusual horizontal annulus were described in this paper. The experiment part settings of the flow loop

contain 10.8 m of length, with 0.060 m and 0.0768 m inner and outer diameters of pipe sequentially. At

atmospheric pressure, water and air formed the liquid and gas phases and the gas and liquid superficial

velocities range studied through this research was 0.14 – 24 m/s and 0.15 – 2.78 m/s sequentially. The observed

flow regimes in both annulus setups by high-speed camera imaging were annular, wavy annular, wavy slug,

slug, churn, elongated bubble and dispersed bubble. A complete explanation of the flow regimes including

various characteristics is displayed jointly with high-quality images.

For gaining more penetrations around the properties of the examined flow regimes, the local liquid holdup time

series jointly with its probability density function (PDF) is utilized. The investigating of the impacts of the

annulus eccentricity upon the detected flow regimes are also has been done. It is noticed that the structure as

well as the shape of the annular, wavy annular as well as elongated bubble flow regimes impacts by the annulus

eccentricity. It is further noted that the annulus eccentricity creates the transformation from an elongated bubble

to dispersed bubble for happening at higher superficial velocities of liquid. It is further observed that in the fully

eccentric annulus creates transitions between various flow regimes to happen at lower gas and higher liquid

superficial velocities as compared with that of concentric ones. By basing on liquid and gas Froude numbers

with integrating the results of analysis from this study with over 1000 data points observed in literature, an

enhanced flow regime map is introduced.

Baghernejad [74] used experiment technique to obtaining flow patterns of two-phase and associated transition

boundaries, for measuring flow patterns below various rotational speeds of pipe, an individual test set-up was

created. In order to enable direct noticing of flow pattern, a Plexiglas pipe, having an in diameter of 25.4 mm

and length of 4000 mm was utilized in tests. An electromotor coupled beside gearbox was utilized to turning of

the pipe that let various speeds of rotation. The set-up also carries inclination up to ±25°. The utilized liquid and

gas phases were water and air, sequentially. For the purpose of drawing flow pattern maps at six various

rotational speeds of 0, 50, 100, 200, 300 and 400 rpm in both 10° inclined as well as horizontal pipe, above 3800

tests were reached. findings of the test were examined with earlier study for a horizontal fixed pipe state for

validating the results. From results, it has been noticed that the rotation of pipe has an important impact on the

transition between boundaries and flow pattern map. Within horizontal pipe state, it was noticed that the

stratified smooth flow regime reduces as the pipe rotation rises and at high revolution speeds it vanishes.

Further, by rising pipe rotational speed, the annular regime increases. During a 10° inclined pipe, the stratified

wavy region seems as the pipe rotation speeds up. It was recognized that for both horizontal as well as inclined

pipe, pressure drop extremely develops as the pipe rotational speed improvements. Moreover, the influence of

inclination of pipe on the pressure drop is decreased as the rotational speed rises.

Gas-solid flow

Kussin and Sommerfeld [75] determinations in a detailed way within a developed particle-laden horizontal

channel flow (6 m in length, 35 mm in height, the length is about 170 channel heights) are displayed utilizing

phase-Doppler anemometry for simultaneous measurement of particle velocity and air. Spherical glass beads

particles including mean diameters in the range of 60 µm–1 mm was utilized. The conveying velocity could be

changed among around 10 m/s and 25 m/s, and the particle mass loading could approach values of around 2 (the

mass loading is described as the ratio of particle to gas phase mass flow rates), basing upon the size of the

particle. With the wall plates exchanging, the wall roughness degree could be transformed, for the first time. The

examination of the impact of these parameters and the seven effects of inter-particle collisions on the profiles of

particle mean and fluctuating velocities and the normalized concentration in the developed flow have been done.

It was explained that roughness of the wall reduces the particle mean velocity and improves fluctuating

velocities because of irregular bouncing of the wall and an improvement in wall impact frequency, i.e. decrease

in mean free path. Thereby, the bigger particles are principally further regularly distributed across the channel,

and gravitational settling is decreased. By developing mass loading because of inter-particle impacts and the

loss of momentum included, both elements of the particle velocity variation were decreased. Furthermore, the


35

impact of the particles upon turbulent variations as well as the air flow was investigated on the principle of

profiles in the developed flow and turbulence spectra defined for the stream wise velocity component. The

impact of the roughness of the wall was investigated in addition to the influence of mass loading as well as the

size of the particle upon modulation of turbulence. It was obviously noted that due to two-way coupling, within

an intensive turbulence dispersion, developing roughness of wall also occurs.

Figure 7. Installation of the PDA on the computer-controlled traversing system.

Laín [76] analyzed the influences of the size of particle, mass loading ratio of the particle as well as the

roughness of wall at the developing of secondary flow under turbulent conditions in a circular cross-section

horizontal pipe. The calculations based on the Euler-Lagrange suggestion estimating for collisions of inter-

particle as well as the roughness of wall (i.e., four-way coupling). The secondary flow consisting of two cells of

recirculation with an upward flow near the vertical (symmetry) axis and a downward flow waste to the walls if

inter-particle collisions ignored in the state of inertial particles. Moreover, during collisions of inter-particle

estimated for, the pattern depends on the concentration profile of particle besides approximately low roughness

walls (smooth), two recirculation cells located, except with rough walls four recirculation cells created. By

growing the mass loading ratio, a shift between two and four recirculation cells in the secondary flow could be

recognized for smaller particles.

Mallouppas and Wachem [77] scrutinized the Large Eddy Simulation (LES) method for emulation the

performance in a turbulent channel flow for interacting particles. For investigating the significance of the single

physical phenomena happening inflows of particle-laden, a set of simulations that were completely (four-way),

two-way and one way coupled completed. Further, hard sphere as well as the soft sphere forms, that explain the

communication among interfering particles, compared with each other and the disadvantages and benefits of

every algorithm presented. Various styles for describing the sub-grid scale stresses with LES compared.

Eventually, the rough walls of the channel’s emulations considering to compared to simulations among smooth

walls. Discussion of the simulations results was conducted including the aid of the data of test of Kussin J. and

Sommerfeld M., at Reynolds number 42,000 depending upon the whole height of the channel. A three-

dimensional domain of 0.175 m × 0.035 m × 0.035 m were used for the simulations in which the direction of

gravity was perpendicular to the flow. It has been shown from the results of the simulation that collisions of

inter-particle as well as rough walls, still for very dilute flows, contain an essential impact into particles

redistributing over the channel. Introducing of a new model of roughness has been done and it takes into account

the reality that within the model of a soft sphere, a collision was completely resolved and it is explained that the

fresh model was in so great approval with the obtainable data of the experiment.

van Wachem [78] described a total system for prognosticating the behavior of interacting non-spherical

particles within a turbulent flow among high Stokes numbers. For describing the collisions between non-

spherical particles and a rough wall, a model of particle-rough wall interaction established forward too. For

simulation, the behavior of horizontal turbulent channel flow among 5 variously formed particles: a sphere, two

kinds of ellipsoids, a disc, and a fiber, the structure was linked with a DNS-LES program. By using the

correlations that obtained utilizing true DNS, the torque, lift as well as drag forces on the particles have been


36

measured. By following their longest axis perpendicular to the local flow direction, the results of simulation

present that non-spherical particles direct to locally maximize the drag force. Making resolved direct numerical

simulations of an ellipsoid in flow produced a more explaining for this phenomenon. These simulations showed

that if an axis of the non-spherical particle not aligned with the flow, the high-pressure zone on the acute sides

of a non-spherical particle occurs in a torque.

If the axis of the particle was perpendicular to the local direction of the flow, this torque was just zero. Further,

if the longest axis was aligned perpendicular to the flow, the particle was most stabilized. Non-spherical

particles holding a higher average velocity balanced to spherical particles having the similar equivalent diameter

caused because of the arrangement of the longest axis of a non-spherical particle perpendicular to the local flow.

It additionally explained that disc-shaped particles flow in a steadier trajectory balanced to elongated particles,

like fibers as well as elongated ellipsoids. This linked to the measure of the pressure gradient on the non-

spherical particles acute side. Eventually, it explained that the wall roughness impact influences non-spherical

particles variously as compared with spherical particles. Especially, a non-spherical particle collision with a

rough wall causes a notable measure of rotational energy, whereas an identical collision with a spherical particle

produces in mostly a variation in translational movement. The size, shape, sphericity and the definition of the

angle of attack of the five particles considered is shown in table below.

Zhou [79] studied the distributions for particle in a fully developed horizontal channel of a turbulent gas-solid

boundary layer, and with particle image velocimetry (PIV) with main upstream speeds of Uh = 2.1 m/s, 5.2 m/s,

and 8.74 m/s, the gas phase velocity field was gained. The particle phase was carborundum powders including

diameters of 38 μm and 60 μm and ghost particles were used that were titanium dioxide nanoparticles. It noticed

that within a logarithmic region, the peak of the particle distribution happens. The peak move toward the wall

according to an expansion of particle size. The peak moves toward the center of the channel as the velocity

improvements. The sweeps, as well as gravity, contain impact toward the motion of particle motion to the wall;

collisions of particle–wall, ejections, and the Magnus lift force contain impact toward the motion of particle to

the center of the channel. The presence of ejections, as well as sweeps created by quasi-flow vortices, has

approved within the examination of shear strain distribution and the velocity field within the gas boundary layer.

Meantime, it observed that the peak of shear strain happened near the wall and that wall-normal inconstancy and

shear strain through high flow rate was significantly larger than at low flow rate; these properties were uniform

with the distribution of the particles within the boundary layer.

Abdelhamid [80] conducted a detailed experimental investigation within ejectors for studying the (air-air)

single-phase and the (air-solid) two-phase flows. A try produced via presenting modifications of design for the

mixing part of the ejector for developing the quantity of solids that transported. The duct of mixing has

increased by a tail part. Mixing ducts of three various geometries besides ejector tail section has designed,

fabricated as well as experimentally examined. The impacts of tail part forms, as well as the mixing duct on the

performance of ejector, have been studied. Moreover, the impacts of the solid particles mass flow rate, as well

as air motive pressure against the produced vacuum pressure as well as the static pressure distribution, have


37

been investigated too. The results collected explained that the mixing duct geometry of convergent-constant-

divergent provides suitable results showing of the ejector as well as greater vacuum pressure. Inlet particle

volume fraction, particle phase material density, as well as particle diameter, were three major parameters

dominating the flow physics of dispersed gas-particle flows.

Liquid-solid flow

Toda [81] numerically analyzing of cared out the limit-deposit velocity at which in the bottom of a pipe, a

deposit of solid starts to build-up on the basis of a two-dimensional flow model and a compare is formed with

the results of the experiment. The model describes fully the reality that with an improvement in the solids,

concentration can be achieved, the limit-deposit velocity raises and it reduces progressively at greater

concentrations next to attaining a maximum point at a specific concentration. It is explained that the shear stress

effecting on the surface of the bed of particles is the governing factor for moving the solids at weaker solid

concentrations, while the drag force of fluid in the bed presents a highly significant performance at greater

concentrations.

Transmission of Solid-liquid slurry has been studied [40]. Within a horizontal slurry flow, novel data of test on

pressure drop was obtained. For the prognostication of flow properties in solid-liquid flow, a theoretical model

was produced. The theory is dependent on a model of a two-layer. The solid-fluid characteristics are; the flow

rate of slurry, the geometry of conduit as well as input concentration are defined, it permits the prognostication

of flow patterns as well as pressure drop. The prognostications model is examined to the novel experimental

data and to some generally applied relationships.

The experiment or theoretically investigation of the flow of solid-liquid mixture at low velocities was done by

Takahash [82]. The creation of dunes within the pipe is a standard flow property that within their motion it

creates a pressure vacillation. As the mixture mean velocity developed, the dunes velocity improved. As the

concentration of solid developed up to 10%, the fluctuation of pressure developed somewhat. For investigating

the periodicity, the Power Spectral Density function (PSD) of the fluctuation of pressure was collected too. The

presence of a dominant frequency has been shown from the results. This dominant frequency was linked to the

dunes motion and it improved according to the dune’s velocity improvement. Depending on a supposed PSD,

the fluctuation of pressure was simulated numerically. The results of pressure fluctuation that simulated were in

great dealing with the tests.

Doron and Barnea [83] studied various flow patterns which could be encountered in a solid-liquid pipeline, that

affect the hydrodynamic characteristics of the flow. A method for displaying their range of existence by means

of flow maps was presented. The maps were drawn from the results of a phenomenological model. The effect of

the various operational conditions on the flow pattern transitions was obtained easily using the maps.

Figure 8. Superficial velocities flow pattern map, ρs = 1240 kg/m3, D = 50 mm, dp = 3 mm, ----- three-layer

model, - -, Turian et al. (1987) correlation, ---- Turian & Yuan (1977) correlation, ○ experimental data (Doron

& Barnea 1995b).


38

Figure 9. Mixture velocity-delivered concentration flow pattern map, ρs = 1240kg/m 3, D = 50ram, dp = 3 mm.

For the purpose of obtaining the numerical solution in a sand-water slurry flow, a simplified 3D Algebraic Slip

Mixture (ASM) model was submitted by [84]. The turbulent model of RNG k–ɛ was applied beside the ASM

model in order for the investigation to achieve the precise numerical solution in a flow of fully developed

turbulent. For solving the dominant equations, a control volume finite variation process was applied, and to

discretize the entire computational domain, an unstructured (block-structured) non-uniform grid was selected.

The comparison of the mean pressure gradients from the numerical solutions with the experimental data was

carried out. When the slurry mean velocity is greater than the corresponding critical deposition velocity, the

solutions were observed to be in great correspondence. Furthermore, several major properties of slurry flow

have been displayed from the numerical studies, like slurry density, volume fraction distributions, slurry mean

skin friction coefficient distributions, slurry mean velocity distributions and slip velocity magnitude within a

fully developed region, that have never been presented in the tests.

Tanaka [85] executed an analysis in a solid-liquid two-phase flow on the interaction between Karman vortices

and concentrated particles (hereafter named the Cluster). Utilizing the moving of a cylinder within a shoal

region container, the Karman vortices have gained. The particle density was approximately similarly as that of

liquid. For distinguishing the Cluster velocity from the vector area of the around flow, we have utilized high-

resolution PIV. It decided that the Clusters improve the flow along the vortices and the steady rigid body

rotation of the Karman vortices from the data that collected. Moreover, the Clusters remain their rotational

movement and do not support the flow along the vortices totally.

Figure 10. The towing tank.

Kaushal [86] conducted experiments within a horizontal pipe which has a diameter of 54.9 mm on two sizes of

glass beads of which mean diameter and geometric standard deviation are 440 µm & 1.2 and 125 µm & 1.15,

sequentially, and a mixture of the two sizes in similar fraction by mass. Flow velocity was up to 5 m/s and for

each velocity, the overall concentration up to 50% by volume. Concentration profiles, as well as pressure drop,

estimated. The profiles presented crossing isokinetic sampling examinations in vertical planes, 45˚ inclined as

well as the horizontal having the pipe axis. Samples of slurry from the mixture, obtained in the vertical plane


39

investigated for concentration profiles of every particle batch forming the mixture. It was discovered that the

pressure drops reduced for the mixture at large concentrations except for 5 m/s and a special variety of

concentration profiles was recognized for particles of 440 µm showing a sliding bed regime, while in the

horizontal plane, the profiles stay relatively fixed irrespective of the kind of slurry, overall concentration as well

as flow velocity.

Goharzadeh and Rodgers [87] an experimental investigation on solid particle conveys through a horizontal pipe

of gas-liquid slug flow with two kinds of tests carried. By utilizing high-speed photography, the impact of the

length of the slug on transportation of solid particle is described. The division of velocity through the slug body

is estimated by utilizing mixed Particle Image Velocimetry (PIV) with Refractive Index Matching (RIM) and

fluorescent tracers (two-phase oil-air loop). A penetration is given toward the physical mechanism of solid

particle transportation due to slug flow by mixing these empirical analyses. It was recognized that mobility of

the solid particle is largely affected by the slug body. It was discovered that the physical mechanism of solid

particle transportation was discontinuous. The inactive region (inwards of solid particle transportation) upstream

of the slug nose was quantified as a function of the size of solid particle and composition of gas-liquid. An

important drop in the quantity of velocity instantly upstream of the slug nose and subsequently the critical

velocity for solid particle lifting is touched additional upstream and all of that have been noticed from the

calculated velocity distributions.

Capecelatro and Desjardins [88] performed calculations of liquid-solid slurries within horizontal pipes for

investigating the dynamics of complex multiphase flow joined with conditions of operating over and under the

velocity of critical deposition. Under a flow of fully developed turbulent, a high-fidelity simulation frame was

connected beside a Lagrangian particle-tracking solver to estimate polydispersed settling particles. The two

phases completely linked by momentum exchange terms as well as volume fraction, and a two-step filtering

method applied to relieve each reliance of the liquid-phase mesh size on the diameter of particle, allowing the

arrest of an extended domain of spatial turbulent scales. An employment of completely stable immersed

boundary system for estimating the geometry of pipe on a regular Cartesian mesh has been done. Two states

simulated, every with a geometry of pipe and particle size distribution meeting an empirical investigation of

Roco & Balakrishnam, which estimates a mean volumetric solid concentration of 8.4%, matching to only above

16 million particles. The first state estimates a Reynolds number depending on 85,000 of the liquid bulk flows,

occurring within a heterogeneous suspension of particles in all places of the cross-section of pipe.

Best correspondence with the results of test has been shown from statistics on the particle phase velocity as well

as concentration for this state. In regards of a lower Reynolds number of 42,660 in second case has been done

which leads to the creation of a fixed bed of particles. Corresponding to a rigid bed at the bottom of the pipe, an

extremely collisional shear flow just above the bed, and a dilute suspension of particles far away from the bed

are three distinguished areas recognized within the second state. Computational results indicated division within

the size of the particle over the vertical direction, by the smallest particles placed at the top, growing

monotonically till the surface of the bed, at which the biggest particles were placed. The velocity, as well as

concentration covariance of every phase, introduced, providing more penetration on the dynamics of multiphase.

For every state, the statistics on the single mechanisms that provide to each particle movement, namely forces

due to drag, the surrounding fluid viscous stresses and pressure gradient, and collisions, have been provided. It

recognized that for the preponderance of the pipe cross-section, the drag force controls for every state, that

stabled by gravity in the vertical direction and by collisions of inter-particle in the stream wise direction. For

investigation of closures from Reynolds average modeling of multiphase flows, simulation results are utilized

too.

Titus and Aidil [89] studied simulation of a computational fluid dynamics (CFD) which approves the Eulerian-

Eulerian inhomogeneous two-fluid form in ANSYS CFX-15 which was utilized to investigate the impact of (90

µm to 270 µm) size of particle and (10% to 40%) in situ particle volume fraction on the radial arrangement of

the concentration of particle and velocity and frictional pressure loss. The robustness of different turbulence

models like eddy viscosity transport, the k-epsilon (k-ɛ), SSG Reynolds stress, k-omega (k-ω), shear stress

transport was examined in prognosticating data of test data of particle concentration profiles. The style of k-


40

epsilon exactly met the experimental data strongly as compared with the other models of turbulence. As the size

of the particle developed at fixed particle volume fraction, a reduction in frictional pressure loss has been shown

from the results. Moreover, the radial distribution of concentration of the particle developed with developing the

size of the particle, where at the bottom of the pipe, a large concentration of particles happened, for a constant

particle volume fraction. Particularly for the large particle volume fraction of 40%, particles of size 90 µm were

approximately buoyant. The CFD study explains that if the perception of pipeline wear, particle attrition, or

agglomeration is to be forward, observations of the variation of these parameters with pipe position is very

important.

Leporini [90] noticed an ingrained issue for both the production of natural gas and oil that was sand particles

precipitation within the pipeline, that could guide to difficulties like the descent of production, immoderate

pressure drops, erosion of pipeline, and defeat of equipment. Within various operations of flow like sand

multiphase mixtures, the description of sedimentation, as well as transport of sand particles, is necessary to

prognosticate entrainment processes within carrying pipelines of gas and oil as well as the transport velocity of

sand. Despite, it appears that no model subsists having the ability to carefully describe the deposition as well as

transport of sand within the multiphase pipeline. Actually, during the previous contract, some investigators

attempted to develop the modeling of liquid-solid flow to gas-liquid-solid flow, however, no respectable

outcomes have been achieved, mainly in slug flow condition because of the complication of the phenomenon.

More and more experimental data are required for developing and validating a mathematical model suitably

expressed for sand critical deposition velocity estimation within the flow of gas-liquid. A preparatory

experimental study within a horizontal pipe for three-phase flows (air-water-sand) submits in this paper and the

sand-liquid model's application submits in literature. Through the experimental study, important considerations

were presented from which some inferences were formed. The establishing of various sand flow regimes were

done using physical investigation and data analysis: stationary bed, moving dunes as well as fully dispersed

solid flow. The determining of critical deposition velocities at various concentrations of sand were done. It was

achieved that the critical deposition velocity, as well as properties of sand transport, are completely based on the

concentration of sand as well as on the flow regime of gas-liquid.

(a) (b) (c)

(d) (e)

Figure 11. Various kind of observed sand flow regimes: (a) Suspension, (b) Moving bed, (c) and (d) Moving

dunes, (e) Stationary bed (images of the bottom of the pipe) - the flow direction from the right to left.

Liquid-liquid flow

The different results. as well as notions undergone in gas-liquid of two-phase flows, cannot easily be turned to

liquid-liquid operations; a basis for creating a general two-fired flow pattern map was formed from an effort that

made by [91]. The variation from a steady layered arrangement to another bounding flow patterns has

investigated the representation of the relations between the states for the actuality of characteristics and


41

instability stander, that result from searching the dominated equations stability as well as well-posedness.

Basing on mechanistic models, the transitive boundaries among the other flow patterns met in operations of

liquid-liquid are achieved. For enormous domains of physical and geometry characteristics, a parametric study

presented, as met liquid-liquid operations, involved too. Sensible correspondence has been shown in

comparisons of the introduced transitional standard with (limited) obtainable data liquid-liquid operations. The

meeting of the highly viscous core flows data, on the one hand, and the common standards to the excess data of

gas-liquid, on the other hand, is satisfying.

Both experimentally and theoretically studying of the transition of Oil/water flow-pattern within horizontal

pipes have been done [92]. A new state-of-the-art oil/water test facility was designed, constructed, and operated.

A transparent test section (5.013 cm inside diameter × 15.54 m long) can be inclined at any angle, to study both

upward and downward flow simultaneously. Mineral oil and water were the working fluids (µo/µw= 29.6, ρo/ρw

=0.85. and σ = 36 dynes/cm at 25.6°C). Stability analyses exhibit that the stratified/unstratified transition should

be treated with the total two-fluid model. While the ST&MI flow pattern is prognosticating by inviscid KH

theory prognosticated, the viscous Kelvin-Helmholtz (KH) analysis are used for prognosticating stratified flow.

The prognosticated drop sizes from the Hinze and Levich models are adjusted to estimate for the impact of the

concentration of dispersed phase, for the dispersed flow pattern. The water fraction is the dominating parameter

for the coalescence phenomena. The execution of the model is premium and matches with published data fully.

Figure 12. Experimental flow-pattern map. Figure 13. Experimental flow-pattern map (mixture

velocity).

Angeli and Hewitt [93] used two methods for the identification of flow pattern, namely definition of the local

phase fractions with a high-frequency impedance probe and high-speed video recording, while the recognition

of the continuous phase in dispersed flows has been done with a conductivity needle probe. Determinations are

done for input water volume fractions from 6% to 86% and mixture velocities ranging from 0.2 to 3.9 m/s.

Several various flow patterns, changing from stratified to fully mixed recognized over this field of conditions.

Annular flow did not seem. Generally, at lower mixture velocities within the steel pipe, the mixed flow pattern

seemed as compared with that within the acrylic pipe, where, also, the continuous phase for a wider range of

conditions was oil. By utilizing the high-frequency impedance probe, the visible noticing was regular with the

determinations. The arrangement of the phases changed dramatically between the acrylic pipes and the stainless

steel, within specific conditions limits. The average in-situ velocity ratios of the two phases in the acrylic pipe

estimated from the phase distribution determinations were, in common, lower than unity.

Fairuzov [94] used a 16-in pipeline carrying light crude oil during the tests. In order to control the input water

volume fraction, the line was joined to a network of freshwater. The oil flow rate controlled by a gate valve

placed at the inlet of the pipeline. Estimating the transversal water fraction profile was used for determining the

transition from stratified flow to dispersed flow. A specific device, the multi-point sampling probe, was

designed and placed within the pipeline for this objective. Mobile sampling tubes are present with the probe that

support getting samples together at six points over the pipe diameter. For minimizing the impact of the probe on

the determined water fraction profile, the retraction rate of every sample was regulated using a needle valve

according to the velocity of the mixture. A standard system for measuring the water fraction in crude oils was

utilized for analyzing the samples for water content in a laboratory. A flow pattern map was formed, based on


42

the data collected. The empirical stratified/unstratified transition boundary was matched with two theoretical

standards received in the linear stability analysis of stratified two-phase liquid-liquid flow. The outcomes of this

investigation can be helpful for the validation of unltifield multidimensional models of two-phase flow and for

the design and operation of pipelines carrying crude oil.

Shi [95] have been experimentally investigated in a horizontal pipe that has a diameter of 10 cm, two-phase oil-

water flows for studying the surfactant impact on distributions of oil-water. At input water cut of 20 per cent and

below, results explained that the water layer velocity is lower than mixed layer velocity up to an input mixture

velocity of 1.6 m/s. Nevertheless, at 40 per cent input water cut and higher, the water layer velocity is lower

than the mixed layer velocity up to an input mixture velocity of just 0.8 m/s. At the medium input water cuts

between 40 and 60 per cent, oil and water are very easier to be mixed. The degree of oil-water mixing flow

improves by the addition of surfactant. By improvement of the concentration of surfactant, the water layer

vanishes, mixing of water and oil at lower mixture velocity begin, and the homogeneous flow pattern was seen

at a very lower velocity of input mixture. Further, the mixed layer involves a very higher fraction of the pipe.

These show that at lower input superficial mixture velocity besides surfactants in oil-water flows, corrosion

could be decreased.

Oil–water two-phase flow experiments were conducted [96] within a length of 15 m, a diameter of 8.28 cm,

inclinable steel pipe utilizing mineral oil (830 kg/m3 density and 7.5 mPa s viscosity) and brine (1060 kg/m3

density and 0.8 mPa s viscosity ). Steady-state data on flow patterns, two-phase pressure gradient and holdup

were achieved across -5°, -2°, -1.5°, 0°, 1°, 2° and 5° of the entire range of flow rates for pipe inclinations. By

noticing recorded movies and via analysis of the relative deviation from the homogeneous performance, the

classification of boundaries of flow patterns and their characterization was obtained. A stratified wavy flow

pattern including no mixing at the interface was recognized in an upward and a downward flow. For exact

determination of the absolute in situ volumetric fractions (holdup) of every phase for whole flow patterns, two

gamma-ray densitometers provided. Comprehensive results of two-phase pressure gradient and hold up as a

function of inclinations, flow pattern and the superficial velocities were described. The new experimental data

were matched with outcomes of a flow pattern subordinate prognostication model, which utilizes the

homogeneous model for dispersed flow and the area-averaged steady-state two-fluid model for stratified. For

whole flow patterns noticed, prognostication rigor for pressure gradients and oil/water holdups were displayed

as a function of pipe inclination. There is a possibility for perfection for in specific dual-continuous flow

patterns.

Vielma [97] studied the characteristics of oil-water flow such as pressure drop, flow patterns, droplet size and

phase fraction, as function of flow patterns in horizontal pipes. The tests were conducted in a 5.08 cm. Various

data were acquired from horizontal test section utilizing water and mineral oil (0.85 g/cm3 of density and 15 cp

of viscosity) beside ranging from0.025 m/s to 1.75 m/s for superficial velocities. For measure droplets,

identifying flow patterns, a high-speed video camera was utilized and to gain phase distributions, ten

conductivity probes were utilized. For fully dispersed flows, three probabilistic distributions have been

experimented. Over the pipe diameter, Sauter Mean Diameter (SMD) analysis was conducted. For flow pattern

of dispersed oil in water and water (D o/w & w), an experimental relationship to prognosticate the SMD profile

of droplets over cross section of the pipe was improved. The experimental relationship provided agreeable

outcomes. Comparisons of model explained that none of them could certainly describe the data of test. The

novel data can guide to better modeling and design of dispersed systems and the new data on droplet sizes can

have an important influence on the design of separator. Furthermore, the description of production logs in

horizontal wells heavily relies on the performance of flow.


43

Figure 14. Experimental Observations Compared with

Trallero's Theoretical Transition Boundaries.

Figure 15. Experimental Pressure Gradients.

Grassi [98] presented experimental flow-pattern maps as well as pressure drops connected to oil and water flow

within slightly inclined as well as horizontal pipe, where the selected liquids characterized by about 800:1 of an

oil-to-water viscosity ratio at 20 °C. Different theoretical models have examined, with special notice to core-

annular flow two-fluid model and oil-in-water dispersion homogeneous no-slip model for the prognostication of

connected pressure drops, and flow-pattern map transition criteria including the regimes encountered in the

empirical experiments. The theoretical prognostications have then matched to the experimental outcomes. A

satisfying correspondence has gained particularly as interests pressure drop comparisons. Boundaries

superimposed on the identical flow-pattern maps, the ‘free’ parameters have provided based on observations and

experimental results, and the last correspondence was great in the prognostication of both the transition to oil-in-

water dispersion and the core-annular flow region of presence, as regards the prognosticated transition. No

inference can be represented on transition rules including stratified flow, which just hardly has noticed in the

completed tests.

Wang and Gang [100] had been made an experimental study of high viscosity mineral oil-water flow through a

horizontal pipe loop. Results indicate that phase inversion for oil phase with high viscosity occurs much earlier

than low viscosity oil, and phase inversion tends to be delayed, with the increment in experimental temperature.

The influence of mixture velocities on the inversion process could be neglected in the range of mixture

velocities that we studied. Phase inversion for oil phase with high viscosity occurs much earlier than low

viscosity oil, and inversion point tends to be delayed with the increment in experimental temperature. Inversion

does not take place at the same time and at all locations in the pipe loop. It starts at a certain location and grows

as it flows downstream.

Oliemans [101] verified the oil/water model approach in detail by using pipe flow data for an oil/brine system

with a viscosity ratio of 9.5. Two very simple modeling approaches have considered the two-fluid model for

stratified oil/water flow with complete phase separation and the homogeneous model for dispersed oil/water

pipe flow conditions. That is not the case for the transitions between stratified-flow and stratified-flow with

mixing. The current flow pattern maps over-estimates the stratified flow region. A transition to stratified-flow

with mixing occurs already at much lower phase velocities than currently predicted. The calculation errors for

the two-fluid model version for stratified flow were quite large, in particular for the oil/water pressure losses.

Typically, average errors of 20-40% and maximum errors of about 100% are quite common. Although the

average errors for the water hold-ups were lower (about 10%), here the calculations were also rather inaccurate

with maximum errors of 50%. When the model used in an inverse mode to compute from measured water hold-

up and oil/water pressure loss the oil and water superficial velocities, the errors were unacceptably high: average

errors of 45% with maximum errors of 200-300% clearly make these results not suitable to determine

production rates in oil wells in a reliable way.


44

Flow pattern transition prediction models were presented [102] for oil-water flow in horizontal pipes. The

transition between stratified and unstratified flow is predicted using Kelvin–Helmholtz (KH) stability analysis

for long waves. New, simplified, and more practical physical mechanisms/mechanistic models were proposed

for the prediction of the transition boundaries to semi dispersed and to fully dispersed flow. The proposed flow

pattern classification significantly simplifies the flow pattern map for liquid-liquid flow and agrees well with the

experimental data.

Desamala [103] presented complete investigation on the prognostication of radial distribution of velocity,

volume fraction and pressure of a pair of immiscible liquids within a horizontal pipeline as well as flow pattern

maps by computational fluid dynamics (CFD) simulation utilizing ANSYS FLUENT 6.3. The fluid pair for

research that has been used was moderately viscous oil and water. For prognosticating different patterns of flow

by co-axial flow, unsteady flow assuming, constant liquid characteristics and immiscible liquid pair, volume of

fluid (VOF) system has been applied. Chosen 47 037 number of quadrilateral mesh components for the entire

geometry, from the grid independent research. Simulation strongly prognosticates about all the flow patterns

(slug, plug, stratified wavy, annular and stratified mixed), excepting dispersion of water in oil as well as the

dispersion of oil in water. The results that simulated are certified with test results of flow pattern map and oil

volume fraction. Radial distribution velocity profile, volume fraction and pressure explain the reality of flow

pattern of the annular, stratified mixed and stratified wavy. These profiles support to advancing the

phenomenological relationships of interfacial properties in two-phase flow.

Shi [104] employed the CFD package FLUENT to horizontal oil-water flow simulation in some various regimes

of flow (core annular flow, oil plugs/bubbles in water and dispersed flow) with matched density and medium

viscosity ratio (µo / µw =18.8). The oil-water flow modelling performed by the volume of fluid (VOF)

multiphase flow process and the SST k-ω scheme with turbulence damping were applied to simulate. For a core-

annular flow (CAF) case, the impacts of wall contact angles, as well as the turbulence schemes on the results of

simulation, were studied. The comparison between the results of simulation and experimental counterparts were

made. Satisfying a good correspondence in the prognostication of flow patterns for oil plugs/bubbles in water

were achieved and CAF.

The results of simulation also showed several particular flow properties of CAF with approximately low-

viscosity oil (oil viscosity one order higher than the water viscosity in the existing research matched to the

largely investigated CAF with oil viscosity being two to three orders higher than the water viscosity). Various

from the high-viscosity oil CAF velocity profiles where there is an intense difference in the velocity gradient at

the phase interface with velocity over the oil core being roughly flat, there is no intense difference in the

velocity gradient at the phase interface for CAF with approximately low-viscosity oil.

Santos [105] carried out mixtures of paraffin oil in water including various oil phase concentrations which were

studied in an empirical and a simulation investigation. As regards to the empirical investigation three procedures

were utilized to obtain data on the distribution of oil phase within the pipe cross-section: Electrical Impedance

Tomography (EIT), sample collection in various radial positions for oil quantification, and photographs of the

flow. Concerning the EIT system, a relative protocol was utilized in the acquiring because it permits for further

accurate reconstruction of the images in the stratified flows state. For simulations carried principally in 2D, the

COMSOL Multiphasic modeling software was utilized, for describing the phenomenon in the oil/water interface

in joining with the k-ε turbulence model, the level set model was using.

The very high computational time required for simulations of 3D carried which did not show further accurate

too. In a present pilot rig, the experimental tests were achieved. superficial oil inlet velocity varied between 0.17

and 1.27m/s superficial water inlet velocity in the interval between 0.30 and 0.45 m/s, during the course of the

investigation. The dominance variable was a pressure drop across the test section, and a great suitable was

reached between simulations in a 2D geometry and tests, 9.7% was the highest variation between the empirical

and simulated pressure drops.


45

CONCLUSIONS

This review paper presented a number of previously employed experimental and numerical two-phase flow

systems (gas-liquid, gas-solid, liquid-solid, and liquid-liquid) reported in the literature. From these studied,

some conclusions are reported:

1. The previous studies are divided into two main groups: the first where the researches did an actual project that

needs to be studied, the second where assumed case study which achieved to understand the behavior and action

of different fluids.

2. Most previous studies depend on the experimental method using of visualization optical methods such as

direct photography, laser-induced fluorescence, laser Doppler velocimetry or phase Doppler anemometry,

particle image or tracking velocimetry a digital camera, and this method lacks precision to determine the

difference of pressure and distribution of velocity through the tubes or ducts.

3. Computational methods are promising in the view of the availability of fast computing tools. Investigations

have been very limited to the basic process of bubble bursting and droplet generation. However, the CFD tools

have great potential to model the basic two-phase processes taking place at the interface with techniques like

Level set methods, VOF, Volume tracking and front tracking methods etc.

4. There is a wide area of research in the field of two-phase flow especially in liquid-solid and liquid-liquid,

which are important areas of industry and applied research.

There is a further need for a review of experimental and numerical works done in this field, in order to assist

researchers in setting up their numerical simulations and finding gaps in it. The target of the present review is:

1. To highlight the developed measurement techniques for two-phase systems and provide more experimental

studies under various conditions, which leads to more accurate conclusions in terms of measuring the pressure

difference and velocity of the fluids.

2. To report the employ numerical simulations of two-phase flows to confrontation challenges and problems.

Also, the key findings of numerical research in points of using the models, discretization, and case setting.

3. To more achieving research that focuses on the behavior of liquid-liquid two-phase flow.

4. To discuss the different types of turbulator and study their effect on flow pattern and change pressure

difference in the closed conduit.

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