Skip to main content
main-content
powered by

## Weitere Artikel dieser Ausgabe durch Wischen aufrufen

01.12.2020 | Original Article | Ausgabe 1/2020 Open Access

# Effect of Agitator’s Types on the Hydrodynamic Flow in an Agitated Tank

Zeitschrift:
Chinese Journal of Mechanical Engineering > Ausgabe 1/2020
Autoren:
Mohammed Foukrach, Mohamed Bouzit, Houari Ameur, Youcef Kamla
Nomenclature
a
Blade length (m)
b
Blade width (m)
B
Width of baffles (m)
c
Impeller of-bottomed clearance (m)
C
Torque (N·m)
d
Impeller diameter (m)
d sh
Shaft diameter (m)
D
Tank diameter (m)
e
Disc thickness (m)
g
Disc diameter (m)
H
Vessel tank height (m)
N
Impeller rotational speed (s−1)
N P
Power number (dimensionless)
P
Power (W)
R
Radial coordinates (m)
Re
Reynolds number (dimensionless)
V z
Axial velocity (m/s)
V θ
Tangential velocity (m/s)
V r
Radial velocity (m/s)
W
Baffle length (m)
Greek Letters
ρ
Fluid density (kg/m3)
μ
Viscosity (Pa·s)
θ
Angular coordinate (°)
ω
Angular velocity (rad/s)
Subscripts
CFD
Computational fluid dynamic
LDA
Laser eddy anemometry
LES
Large eddy simulation
RT
Rushton turbine
CBT
Circular blades turbine
DTBT
Diverging triangular blades turbine
CTBT
Converging triangular blades turbine
CHCB
Circular horizontal cut baffle
MRF
Multiple reference frame
RRF
Rotating reference frame
VB
Vertical baffles

## 1 Introduction

Mixing is one of the most widely used unit operations in the chemical, bio-chemical, pharmaceutical, petrochemical, and food processing. The objective of mixing is homogenization, manifesting itself in a reduction of concentration or temperature gradients or both simultaneously, within the agitated system [ 1]. A stirred tank unit typically consists of a rotating impeller in a vessel. Fluid motion is promoted by the transfer of energy from the impeller into the process fluid.
The agitation of liquid in these tanks is an operation more or less simple to realize, but always complex to characterize, because of the nature of the flows and the geometry of the system. Today, the majority of the operations of agitation and mixture are carried out by means of a pendulum agitator turning around a shaft, placed in a tank, generally of cylindrical form. In literature, the study of the systems of agitation started in several works relating to the characterization of the turbulent flows. As an indication, one can quote the work of Refs. [ 27].
The agitation system consists of the agitator and the baffles, the baffles are used to break the liquid flow to increase turbulence and mixing efficiency. There are a number of comprehensive studies on baffled tanks that investigate their hydraulic efficiency [ 810].
The present work aims to determine the influence of geometrical parameter of a stirred vessel with down pumping direction from a pitched blade turbine (PBT 45°) on the hydrodynamic flow structure. The effect of the addition of a cylindrical bump in the center of dished bottom tank and the reduction of the bottom height with the same distance by realizing four geometries are also investigated. In planes r- z the effect from the reduction on the bottom height for all configurations tank with bump allows good growth parameters mixture for turbulent viscosity, turbulent kinetic energy and mean velocity [ 11].
They study an effect of the tubular baffles configuration in an agitated vessel with a high-speed impeller on the power consumption. Aqueous solutions of CMC were agitated within transitional range of the non-Newtonian liquid flow in the agitated vessel of inner diameter equal to 0.6 m. Eight different types of the impellers were tested: Rushton or Smith turbines, turbine with straight blades, pitched blade turbines and propeller. The results show that geometry of the tubular baffles mostly affects the power number for the system with radial flow Rushton turbine [ 12].
Agitating liquids in unbaffled stirred tank leads to the formation of a vortex in the region of the impeller shaft when operating in the turbulent flow regime. A numerical model is presented here that captures such a vortex. The volume of fluid model, a multiphase flow model was employed in conjunction with a multiple reference frame model and the shear stress turbulence model [ 13].
Power characteristics for an agitated vessel equipped with planar short baffles of length L and pitched blade turbine of pitch β are presented in the paper. The studies were carried out in the vessel of inner diameter D = 0.6 m, where the baffles were located in the distance p from the vessel bottom ( p +  L =  H). The effects of the pitch β and geometrical parameter p/ H on the power number Ne were determined mathematically. The results showed that, for the assumed value of the angle β, the function Ne =  f ( L/ H) decreases with the decrease in the baffle length L (i.e., with the increase in the parameter p). The greatest differences between power numbers Ne were observed for the turbine with the flat blades ( β = 90°) [ 14].
They make a comparative study enters of the baffled tanks and other not baffled, these tanks equipped with a mobile with agitation of the Maxblend type. They found that the consumption of energy is higher in the tanks baffled by reports/ratios with the not baffled tanks [ 15]. He studies the effect of the design of the tanks on the flow models, the size of the tank and the power consumption. The three shapes of different tanks were carried out: a flat-bottomed cylindrical tank, a dished bottom cylindrical tank and a closed spherical tank. The comparison between the results obtained for the three configurations of tank showed that the spherical forms provide uniform flows in all the volume of the tank and require a less of power consumption per report/ratio the others (flat bottom and dished bottom) [ 16].
They studied by digitally simulates the effect of the curve of the baffles on the power number, they tested several geometrical configurations with the striping curve of baffles vary from 0 up to 7/30, they showed that the baffles curved also influence the stability of the free face [ 17].
They studied the effect of the baffles on the consumption of energy in a tank agitated by a Rushton turbine. Three types of the tanks were used: without baffles, with baffle and a tank with slits placed at the perimeter external of its vertical wall. The effect the length of the slit was studied. The comparison between numerical results envisaged and the experimental data available shows a satisfactory agreement. They found new indicates tank which minimizes the consumption of energy [ 18].
They tested by a numerical study the effect of the angle of inclination of the baffles, several angles tested in this work 25°, 32°, 45°, 70° and 90°. They found that the angle of inclination of the baffles 25° ensures a good mixture at a time reduced and with an energy consumption reduced to. In addition, the free face is more stable in the tanks equipped with baffles tilted 25° [ 19].
They studied a digital simulation of the flow of the fluids pseudo-plastics in a tank mechanically agitated by a Rushton turbine. The presence of the baffles in the tank has an important influence on the vortex size. The width of these baffles must be optimized. The determination of the size of these vortices is highlighted and the influence of the theological and hydrodynamic parameters of the fluids is studied. They concluded when the baffle width is sufficient, the vortex is removed, but the consumption is then a maximum.
The power of agitation increases with the increase in the structural index, because of the viscous forces, and it varies slightly starting from the transitory mode [ 20]. The technique of particle image velocimetry is used to analyze the vortices of wake and to elucidate their relationship to the properties of turbulence in a tank agitated by four various agitators, Rushton turbine; turbine with a disc with blades: concave, semi elliptic, parabolic [ 21]. The results showed that more the curve is broad plus the vortex resides longer at the blade tip, a longer distance between the higher and lower vortex, one longer life span and leads to the formation of smaller and more robust vortices.
The turbulent kinetic energy decreases more the curve is large, because of the progressive reduction in the power provided for the same Reynolds number; the area of larger, dissipated power ε and turbulent kinetic energy κ is the zone between the higher and lower vortex; as well as the difference in distribution of κ and ε of the four turbines is associated with different axes from the vortex of wake due to the shape of the blades.
In the present work, single-phase flow patterns in a stirred vessel have been investigated using (CFX 16.0) in a turbulent flow regime using four different agitator’s types, a Rushton turbine (RT), a circular blade turbine (CBT), a diverging triangular blade turbine (DTBT) and converging triangular blade turbine (CTBT). Comparisons have been made of the flow fields produced when the impellers are operated in the down- and up-pumping modes. These velocity fields have been assessed by examining the power consumption and vortex sizes.
Hence, the objective of this work is to:
• Analyze and determine the effect of the agitator’s types on the hydrodynamic flow structure.
• Reduce the power consumption and vortex size.
• Our attention is focused on the effect: baffle height rotation, impeller angle, circular horizontal cut baffle and impeller clearance ratio.

## 2 Description of the Stirred System

The geometry consisted of a flat-based fully baffled cylindrical vessel filled with fluid to a height, H, equal to the diameter D. The diameter of cylindrical vessel D = 0.6 m, the diameter of rotating shaft d sh =  d/5. The four metallic baffles were D/10 in width and about D/200 in thickness, vertical and close to the wall. The stirrers used were four different types of agitators with six blades, fixed on a disc: Rushton Turbine (RT), Circular Blades Turbine (CBT), Diverging Triangular Blades Turbine (DTBT) and Converging Triangular Blades Turbine (CTBT), with the same volume, positioned at a clearance c =  D/3 from the bottom of the tank (Figure  1). The dimensions of the four agitators are presented in Table  1.
Table 1
Impellers geometrical proprieties
Agitators
Impeller diameter
d (mm)
Blades length
a (mm)
Blades width
b (mm)
Disc diameter
g (mm)
Shaft diameter
d sh (mm)
RT
198
49.5
39.6
148.5
39.6
CBT
198.45
49.81
49.81
148.5
39.6
DTBT
198
49.5
79.2
148.5
39.6
CTBT
198
49.5
79.2
148.5
39.6

## 3 Theoretical Backgrounds

The working fluid is pure water at room temperature 20 °C with density ρ = 997 kg/m 3 and viscosity μ = 0.89 × 10 −3 Pa·s. They are the same as the experimental study of Ref. [ 22].
The manner most used to characterize an agitated system is the determination of the dimensionless numbers. These characteristic parameters can be expressed starting from the fundamental units (mass, length, time). The Reynolds number ( Re) provides information on the relation between the inertias and the forces viscous acting on a fluid. This value indicates if the fluid has a laminar behavior ( Re < 20) or turbulent ( Re > 10 4).
The Reynolds number of the flow in a stirred vessel is defined as:
$$Re = \frac{{\rho ND^{2} }}{\mu },$$
(1)
where ρ is the density, N is the number of impeller revolutions ( ω = 2π N, ω is the angular velocity), μ is the dynamic viscosity of the working fluid.
The radial ( R) and axis ( Z) coordinates are normalized as:
$$R^{*} = 2R/Z,Z^{*} = Z/D.$$
(2)
The tangential, radial and axial velocities are normalized with the blade tip velocity:
$$V_{\theta }^{*} = V_{\theta } /V_{tip} ,V_{r}^{*} = V_{r} /V_{tip} ,V_{z}^{*} = V_{z} /V_{tip} ,V_{tip} = \pi ND.$$
(3)
In a dimensionless form, the power number is defined by:
$$N_{P} = \frac{P}{{\rho N^{3} D{}^{5}}}.$$
(4)
The power consumption ( P) depends on all the parameters characterizing the external geometry of the vessel, the stirrer geometry, flow regime and the rotating speed of the impeller. The power is calculated according to a determination of the couple necessary to make turn the agitator, by the use of an assembly of dynamometer making it possible to measure the cable which is exerted on the shaft actuating the agitator.
The losses with the frictions on the parts moving are evaluated with the no-load tests in which agitation turns in the air.
The consumption is obtained by the equation:
$$P = 2\pi (C - C_{0} ),$$
(5)
where C the couple in load and C 0 the couple in vacuum.

## 4 Numerical Details

In this study, the commercial software CFX 16.0 was used to simulate 3D flow fields in stirred vessels equipped with a four agitator’s type (RT, CBT, DTBT and CTBT). The geometry was created and meshed the computational domain by tetrahedral cells (Figure  2). The computational grids were defined by unstructured, non-uniformly. Numerical test were carried out to confirm the effect of mesh size on the calculated results. Table  2 shows a total grid of 501312 was enough to get mesh independence resolution.
Table 2
Comparison of power number between simulation with different grid number and experimental of baffled tank (at Re  = 10 5)

Simulation
Experimental
Grid number
210680
376680
501312

Power number
5.221
5.432
6.0
6.0
In unbaffled tanks, the stirrer rotation was modeled by using the Rotating Reference Frame (RRF) method. Here, the impeller is kept stationary and the flow is steady relative to the rotating frame, while the outer wall of the vessel is given an angular velocity equal and opposite to the velocity of the rotating frame. This approach can be employed due to the absence of baffles [ 23].
The Multiple Reference Frame (MRF) approach was used in baffled tanks; this technique consists of dividing the computational domain into two parts: an inner rotating cylindrical volume enclosing the turbine and an outer stationary volume containing the rest of the tank. Other details of this technique are found in Ref. [ 18]. Several studies have focused on the MRF approach like Refs. [ 2427].
The multiple reference frames (MRF) method is the most suitable method to simulate impeller rotation in mixing systems. Precise determination of stationary and moving zones in MRF method leads to accurate results in mixing performance [ 28].
In this study, the Reynolds number is varying from 10 4 to 10 5. The RANS, RNG κε model used for modeling the turbulent flow in the agitated tanks and gives a good result; we can quote some work on this model by Refs. [ 2932]. The effect of the modeling approach, discretization scheme and turbulence model on mean velocities, turbulent kinetic energy and global quantities, such as the power and circulation numbers, has been investigated.
The type of the turbulence model was limited to the κε and RNG models due to convergence difficulties encountered with a Reynolds Stress Model (RSM) and there was found to be little effect of these models on the mean flow and turbulent kinetic energy [ 7]. They studied the effect of three models of turbulence ( κε, RNG and RSM) in a stirred tank by using an MRF approach on the tangential velocity field. They found that the RNG model reduced the unphysical reverse swirl region in the upper tank predicted by simulations [ 33].
The mathematical modeling and numerical simulation of the turbulent, two-phase flow of liquid and gas in a gas induced agitated stirred- tank reactor using computational fluid dynamics (CFD) techniques. A three-dimensional (3D), transient, Euler-Euler two-phase flow model is developed and used to investigate the turbulent flow and mixing of liquid and bubbles in the stirred-tank reactor, applying the sliding mesh approach. Turbulence is simulated by means of several available models, the Renormalization Group (RNG) κε model being the one finally recommended as the most appropriate of the ones studied, for the present application [ 34]. The re-normalization group (RNG) κε model, large eddy simulation (LES) model and detached eddy simulation (DES) model were evaluated for simulating the flow field in the stirred tank.
All turbulence models can reproduce the tangential velocity in an unbaffled stirred tank with a rotational speed of 150 r/min, 250 r/min and 400 r/min, respectively. LES model and RNG κε model predict the better tangential velocity and axial velocity, respectively [ 35]. Simulations was converted when normalized residuals for pressure and velocities drop below 10 −5. Most calculations required 1700–2000 iterations and about 8‒10 h.

## 5 Results and Discussion

In practice, the flow in the stirred tanks is three-dimensional. However, the absence of baffles does not ensure a good quality of mixing, this is due to the fact that the flow is mainly tangential, on the other hand the mixing becomes more efficient if the steering system comprises baffles, and that this translated by the transformation of the predominantly tangential flow into a three-dimensional flow. The different configurations of the agitator types (RT, CBT, DTBT, and CTBT) are shown in Figure  3 for tanks without baffles.
In order to verify the reliability of the calculation code and the simulation method used, reference was made to the work of Ref. [ 22]. Note that the same geometric conditions as those undertaken as well as the same fluid, were simulated. The numerical predicted results for the power consumed in a cylindrical vessel without baffles on the left and with baffles on the right (Figure  4) and were compared with those of Karcz and Major [ 22]: a satisfactory agreement was noticed.
Figure  5 illustrates the power number N P in a cylindrical vessel without baffles provided with different agitator’s types (RT, CBT, DTBT, CTBT) according to the Reynolds number Re which varies between 10 4 and 2 × 10 5. From the graph, it can be noted that the tanks which have agitators: DTBT and CTBT are identical with a mean power number about 2.5 and the others (RT and CBT) N P about 1.
When the stagnant areas exist in a stirred tank, mass transfer and heat is lower with higher temperature gradients, which makes it is necessary to eliminate these undesirable regions in the tank [ 36]. The effect of certain parameters on the flow fields is presented.
Figure  6 illustrates the different flow structures obtained for the four agitator’s types (RT, CBT, DTBT, CTBT) with Reynolds number Re = 4 × 10 4. It can be seen that the intensity of the speed is higher at the end of the blades (RT, CBT, and DTBT) and less intense for the CTBT agitator as well as a large swept area up and down the blades for RT and DTBT and low area scanned for the CTBT. These types of turbine split the flow into two streams: one going towards the bottom of the tank and the other towards the free liquid surface, resulting thus is the formation of two vortices above and below the turbine.
Figure  7 illustrates axial speeds of the agitated tanks with vertical baffles of different agitator’s types (RT, CBT, DTBT, CTBT) with Reynolds number Re = 4 × 10 4, R * = 0.18 and Z * = 0.183. In the figure on the left the axial speed with length for the height of the tank, we can notice that agitators (RT and CTBT) are identical; an important value axial speed in agitator DTBT varies approximately 0.035 and low value axial speed in agitator CBT.
On the right the axial speed with a length of the radius of the tank, axial speeds of the four agitators remain almost constant for R * varies between 0.05 and 0.25 then to increase for reaching a maximum value for agitator DTBT vary approximately 0.025.
The vortex size of the four agitator’s types (RT, CBT, DTBT, and CTBT) is presented in Figure  8 according to the values of Reynolds number Re varies from 10 4 to 10 5. We can notice a maximum value of the vortex size approximately 0.655 of two agitators (DTBT and CTBT) with Re = 104 then a major reduction varies approximately 0.4 of two agitators (RT and CBT) for Re = 4 × 10 4 then to increase until reaching a value of 0.55 for DTBT with Re = 10 5.
The power consumption is a global parameter to describe the performance of a mechanically agitated system. Table  3 shows the variation of the power number N P with Reynolds number Re = 4 × 10 4 in a tank with baffles and the other without baffles with four agitator’s types: RT, CBT, DTBT, CTBT and we compared our numerical results with the experimental ones of Ref. [ 18]; one obtains a good value with the experimental one for the agitator RT and a decrease for the others in the baffled tanks and an increase of the NP for the unbaffled tanks (CTB, DTBT, CTBT), it is noted that the CTBT stirrer reduces the power consumption about 43.83% in the baffled tank.
Table 3
Power number of different agitator’s types of tanks with and without baffles
Agitators
RT
CBT
DTBT
CTBT
Exp. of Ref. [ 18]
Baffled tank
6.0
4.24
5.15
2.63
6.0
Unbaffled tank
0.79
1.12
2.57
2.39
0.82

### 5.1 Effect of Baffle Height Ration (L/H)

Experimentally, they studied the effect of baffle height for different agitator’s types (Rushton turbine, propeller, radial blade turbine, flat and inclined) on the turbulent energy consumption [ 22]. They found than the Rushton turbine type characterized by higher energy consumption by comparing to the different mobiles studied.
In this section, the effect of the baffle height is studied. For this task, four Geometric configurations are realized, which are: L/ H = 0.83, 0.67, 0.5 and 0.33 for the cylindrical tanks with RT, CTB, DTBT and CTBT, respectively.
Figures  9, 10, 11 and 12 show the streamlines of the tanks with vertical baffles provided by four agitator’s types with four cases of the baffle height, which are: L/ H = 0.83, 0.67, 0.5 and 0.33 with a Reynolds number Re = 4 × 10 4. We note that the upper vortex size for each similar remainder and we also observe that the baffle height increases vortex size decreases ( L/ H = 0.83 and 0.67), a significant increase in the size vortex for heights ( L/ H = 0.5 and 0.33) due to damage to the agitator.
The axial speed profiles for different agitator’s types with various baffles heights along the vessel radius, at R * = 0.233 and Re = 4 × 10 4 are schematized in a dimensional form to show clearly the vortex size (Figure  13).
The graphs of two agitators (RT and CTBT) are identical and the size of the zone of recirculation increases continuously, one finds a maximum value of axial speed for L/ H = 0.67 approximately 0.15 and 0.13 in the top and bottom of the turbine for agitator DTBT and low value for agitator CBT approximately 0.03 in the top and bottom of the turbine and a light value axial speed in the free face of the liquid for the four reports/ratio L/ H.
A comparison was present in Figure  14 of the variation of the power number N P, according to the baffle height ( L/ H = 0.83, 0.67, 0.5 and 0.33) of four agitator’s types (RT, CTB, DTBT and CTBT), the N P values almost constant for agitators (DTBT, CBT and RT) with ( L/ H = 0.33, 0.5 and 0.67) then increases slightly, one can also see, an important value of power number ( N P = 0.455) with the height of the baffle ( L/ H = 0.83) for agitator DTBT. An important reduction of the power consumption for CTBT with an N P median value approximately 2.5.
The vortex size against the baffle height is presented in Figure  15, one can observe that the vortex size reaches a maximum value of 0.655 for CBT and DTBT with L/ H = 0.33 then decreases with the other heights ( L/ H = 0.83, 0.67 and 0.5) up to a minimal value of 0.4 for CBT with L/ H = 0.83. We can deduce that a reduction of the vortex size of agitators CBT, DTBT and CTBT reduced by comparison to RT with the increase baffle height.

### 5.2 Effect of Impeller Angle ($$\theta$$)

In this part we interested to study the effects of the impeller angle of four agitator’s types (RT, CTB, DTBT and CTBT) on the hydrodynamic flow in tanks with vertical baffles, five angles are tested ( $$\theta$$ = 10°, 25°, 45°, 60° and 90°) with Reynolds number Re = 4 × 10 4.
Figure  16 shows vectors speed for baffled tanks with four agitator’s types and various angles $$\theta$$, by comparison, we can notice that the intensity of the vectors raised around the turbine for two agitators (CBT and DTBT) east decreases when moves away because of the baffles which play a role of obstacle which slows down the fluid and formation of the dead zones of recirculation (stagnant) behind the baffles. The angles $$\theta$$ = 25° and 90° for CBT and DTBT give a better distribution of vectors.
The five impeller angles ( $$\theta$$ = 10°, 25°, 45°, 60° and 90°) for baffled tanks with four agitator’s types with Reynolds number Re = 4 × 10 4 are studied and drawing the graphs of axial velocities along the vessel radius, at R * = 0.333 as shows in Figure  17. By comparison, between the four graphs, one notes that axial speeds almost identical for the various angles $$\theta$$ of the four agitator’s types, one observes a maximum value axial speed approximately 0.035 in the high part of the turbine and almost 0.033 in the lower part of the turbine for agitator DTBT and minimal value for the agitator CTBT about 0.02 and 0.018 tops and low of the turbine for impeller angles ( $$\theta$$ = 25° and 90°) and null in the free face of the liquid.
Figure  18 illustrates the vortex size for different agitator’s types with various impeller angles with Reynolds number Re = 4 × 10 4, we can note that the values of vortex size varied with the impeller angles $$\theta$$. A maximum value of the vortex size is about 0.66 and minimal approximately 0.4 of CTB. The agitator DTBT give a good reduction of the vortex size of the impeller angles by report/ratio the other agitators.
The power number according to the impeller angles of the tanks equipped with four agitator’s types is found in Figure  19. We can note that all the graphs constant with all the angles and one observes an important power number value N P approximately of 5.2 of the two agitators (RT and DTBT) who are identical and a minimal value N P = 2.7 for agitator CTBT, therefore, this agitator reduces the power consumption almost half.

### 5.3 Effect of Circular Horizontal Cut Baffle (CHCB)

They find that the cylindrical vessel with cut horizontal circular baffle (CHCB) at an angle of 20° decreases the size of the vortex and reduces power consumption by comparing a cylindrical vessel with four designs (CHCB) is a better design to avoid damage to the agitator [ 37].
Four configurations have been realized to study the influence of the cut circular horizontal baffle (CHCB) with an angle of 20° in cylindrical tanks with RT, CTB, DTBT and CTBT as shown in Figure  20.
Figure  21 allows to compare the effect of CHCB with an angle of 20° and Reynolds number Re = 4 × 10 4 on the cavernous size of the flow (zone of intense motion forms around the stirrer) for tanks containing RT, CBT and DTBT and low intensity area of CTBT especially above the turbine. The streamlines are almost similar to the four agitator’s types, it is noted that there is a decrease in the size of the large vortex compared to tanks with vertical baffles. These results indicate that CHCB at an angle of 20° affects the flow field.
Axial and radial velocities for different agitator’s types along the vessel radius, at R * = 0.216 and Reynolds number Re = 4 × 10 4 are presented in Figure  22. We can note that the profiles of axial speed are almost identical for the agitators (DTBT, RT and CBT) with maximal value about 0.035 and 0.043 in the upper and the under of turbine for agitator DTBT and 0.015 in the free face of the liquid. The profiles of radial speed are similar to light variation, we see a maximal value of 0.15 on the edge of the blades and minimal about 0.05 under the blades for agitators CBT and DTBT, in a free face a null value can see.
The vortex size and power number are shown in Table  4 in a cylindrical vessel equipped with different agitator’s types with CHCB s with an angle of 20°. Our numerical results were compared with the work of Ref. [ 37], we found similar results concerning the vortex size of the different agitator’s types and power number slightly varied, and we also noticed a significant decrease in power number of the CTBT agitator.
Table 4
Vortex size & power number for different agitator’s types of tanks with CHCB

RT
CBT
DTBT
CTBT
Ref. [ 33]
Vortex size
0.381
0.383
0.371
0.398
0.382
N P
3.66
3.39
4.20
2.59
3.64

### 5.4 Effect of the Impeller Clearance Ratio (c/D)

In a standard tank, the height of the liquid is equal to the tank diameter. The impeller is positioned at a distance c generally measured from lower impeller edge to the vessel bottom; to know the influence of impeller clearance on the hydrodynamic structure, four cases of c/ D ratios are tested ( c/ D = 0.17, 0.33, 0.5 and 0.67) for cylindrical vessels equipped with four agitator’s types (RT, CBT, DTBT, CTBT).
The evolution of the vector speed in the horizontal plane of the tank with CHCB with an angle 20° and for the four agitators with four impeller clearance ratio c/ D with Reynolds number Re = 4 × 10 4 are represented in Figure  23. We can observe that the intensity of the vector speed is higher around the turbines and important in the medium and on the wall of the tanks for the four agitators with ratio c/ D = 0.33 and low intensity for the ratio c/ D = 0.17, 0.5 and smaller for c/ D = 0.67, one can as see, as the direction of the vector speed around the turbines and in the middle of the tanks is different. It is deduced that the ratio c/ D = 0.33 gives a good distribution of the vector speed. Therefore, better an agitation of the fluid.
The profiles of axial speed with various impeller clearance ratios c/ D for different agitator’s types along the vessel radius, at R * = 0.25 and Reynolds number Re = 4 × 10 4 are shown in Figure  24.
For ratio c/ D = 0.17, a maximum value of axial speed under the turbine reaches almost 0.055 At Z * = 0.2 then slightly decreases up to the value of 0.005 at Z * = 0.2 on top of the turbine then null to the free face of the liquid for agitators DTBT and RT, for c/ D = 0.33 the height of the vortex size varies approximately 0.03 under turbine with V * z = 0.04 and 0.02 upper turbine with V * z = 0.025 of agitator DTBT.
For c/ D = 0.5, V * z = 0.04 and 0.045 in the under and upper of turbine for agitators DTBT and the values of V * z in the free face of the liquid varies between 0.015 to 0.035 for all agitators. For c/ D = 0.67 the axial speed is maximized with a value of 0.06 because the agitator is closer to the free face of the liquid for agitator DTBT and minimal approximately 0.03 at Z * = 0.2 for agitator RT.
Figure  25 shows the variation of vortex size versus the impeller clearance ratio ( c/ D = 0.17, 0.33, 0.5 and 0.67) for cylindrical vessels equipped with four agitator’s types (RT, CBT, DTBT, CTBT), it can be seen that all the graphs of four agitators are identical. A maximum value of the vortex size approximately 0.98 with c/ D = 0.17 then decreases until reaching a value of 0.3 with c/ D = 0.67. Thus the size of the vortex decreases with the increase of the impeller clearance ratio ( c/ D).
We compare and validate our numerical results with the experimental one of Ref. [ 38], in Figure  26 the variation of the power number N P versus impeller clearance ratio c/ D was introduced. It can be seen that the power number increases slightly with an increase of the ratio. We deduce also, the agitator CTBT gives an important profit on the power consumption per report/ratio the others, his power number about N P = 2.

## 6 Conclusions

The geometrical shape of the baffle and the agitator is a factor very influencing on the performances of a mechanically agitated system. The baffles are essential devices in the construction of the agitated tanks.
The role of the baffles is to transform the tangential flow generated by the mobile of agitation into flow three directional, mainly axial, radial and tangential, and to also avoid the formation of the vortices on the level due to the centrifugal force. In our work, we interested to study four agitator’s types (RT, CBT, DTBT, and CTBT) in tanks without and with baffles (VB and CHCB) in a mode of turbulent flow.
Several parameters are tested, such as the effect of: vertical baffles baffle height, impeller angle, and circular horizontal cut baffle and impeller clearance.
In the unbaffled tank, we find that agitator CBT gives the power number similar to agitator RT and the CTBT stirrer reduces the power consumption about 43.83% in the baffled tank. We can deduce that a reduction of the vortex size of agitators CBT, DTBT and CTBT reduced by comparison to RT with the increase baffle height.
The agitator DTBT give a good reduction of the vortex size of the impeller angles by report/ratio the other agitators.
We compare and validate our numerical results with the experimental one of Ref. [ 38], we deduce that the agitator CTBT gives an important profit on the power consumption per report/ratio the others, his power number about N P = 2.

### Competing Interests

The authors declare no competing financial interests.
Open AccessThis article is licensed under a Creative Commons Attribution 4.0 International License, which permits use, sharing, adaptation, distribution and reproduction in any medium or format, as long as you give appropriate credit to the original author(s) and the source, provide a link to the Creative Commons licence, and indicate if changes were made. The images or other third party material in this article are included in the article's Creative Commons licence, unless indicated otherwise in a credit line to the material. If material is not included in the article's Creative Commons licence and your intended use is not permitted by statutory regulation or exceeds the permitted use, you will need to obtain permission directly from the copyright holder. To view a copy of this licence, visit http://​creativecommons.​org/​licenses/​by/​4.​0/​.
Literatur
Über diesen Artikel

Zur Ausgabe

## Marktübersichten

Die im Laufe eines Jahres in der „adhäsion“ veröffentlichten Marktübersichten helfen Anwendern verschiedenster Branchen, sich einen gezielten Überblick über Lieferantenangebote zu verschaffen.

Bildnachweise