Abstract
With the considerable use of pipelines and reactors in the engineering industry, determining the deposition velocity enabling hydraulic transport is of utmost importance. This has been investigated throughout the years, scrupulously in several types of reactors used in water treatment and solid transport. The primary focus has been extended to torus reactors, due to their significant advantage in chemical, biochemical and mixing processes. In the present work, we have studied the solid-liquid suspension in a torus reactor. We elaborated an experimental method based on visual assessment SBAM (Steady Bed Angle Method), which enabled us to analytically determine the just suspended speed ‘Njs’ at which no solid remains stationary at the bed and further parametrically study the effect of several parameters including solid loadings, particle sizes and densities. The just suspended speed values obtained experimentally have been compared to a modified Zwietering's correlation.
NOMENCLATURE
- N
Rotation speed (rpm)
- Njs
The just suspended speed (rpm)
- Sv
Geometry coefficient (non dimensional)
Liquid density (kg/m3)
Density difference (kg/m3)
Solid mass concentration (%)
- D
Tank diameter
Deposing velocity (m/s)
Froude criterion (non dimensional)
Average particle diameter (m)
Impeller diameter (m)
Rotation speed (rpm)
Fluid velocity (m/s)
Pitched angle of impeller blade (deg)
- Dt
Inner diameter of pipe/torus reactor (m)
- Rt
External radius of reactor (m)
- Lt
Circumference length of reactor (m)
- d2
Impeller axe diameter (m)
Solid density (kg/m3)
Liquid density (kg/m3)
Maximum bed angle (deg)
- R
Ratio of bed angle (non dimensional)
- SBAM
Steady Bed Angle Method
Constants
Constants
- NjsSim
Simulated just suspended speed (rpm)
- NjsObs
Observed just suspended speed (rpm)
Observed just suspended speed for the ith experience(rpm)
Simulated just suspended speed for the ith experience (rpm)
Observed average just suspended speed (rpm)
Simulated average just suspended speed (rpm)
Standard deviation of measured Njs
INTRODUCTION
Stirred reactors are widely used in industrial processes for heterogeneous chemical reactions and wastewater treatment; this type of reactor requires working at low stirring speed, causing solid particles to deposit on reactor walls, limiting both mass and heat transfer.
For this exact reason, manufacturers recommend increasing the agitation speed to reach the complete suspension necessary for solid-liquid transport. At values lower than the just suspended speed, Njs, the solid-liquid exchange surface is partial with some particles remaining stationary at the bottom of the reactor, some suspended, and a few denominated as jumping particles. This leads to a decrease in mass and heat transfer crucial to some solid-liquid operations for the completion of the reaction in a heterogeneous mixture according to Cohen et al. (2018). Contrarily, at values superior to the just suspended speed Njs, the solid-liquid mass-transfer is inconsequential, it is of note that all particles in this case possess the same concentration. Hence, we observe a significant drop in productivity and an unnecessary power consumption. In order to hinder this problem, researchers focused on determining the minimal suspension speed. Davoody et al. (2015) worked on maximizing the particle interfacial area while also minimizing the agitation cost. In addition, Tamburini et al. (2016b) were able to effectively augment the solid loading per reactor unit volume while keeping the operation costs as low as possible.
Zwietering (1958), Nienow (1968) and Baldi et al. (1977) studied back in the 1950s and 1970s the dependence of the critical speed (Njs) on physical and geometrical parameters of the reactor and the operating conditions.
A slight effort has been devoted to investigating solid-liquid suspension in unbaffled stirred tanks, used preferably for wetting and drawing down particles into liquids. The issue of solid particles suspension in this kind of reactor was tackled for the very first time by Brucato et al. (2010). In order to avoid vortex formation and dead volume at high stirring speed, they opted for a cover on top of the tank. A significant mass transfer coefficient was observed in unbaffled tanks compared to baffled ones, for the same power dissipation and a difference of density between solid and liquid phases. Moreover, turbulence is generally predominant in unbaffled tanks due to excellent heat and mass transfer, improving the chemical reaction according to Li et al. (2015). Tamburini et al. (2015) also observed a significant power saving when using the unbaffled tank, for processes where the mixing time is not a limiting factor.
The stirred tank and pipe have been fully explored in the study of solid-liquid mixing with many studies carried out experimentally to determine the just suspended speed for complete suspension (Taghavi et al. 2014). The minimum liquid velocity necessary to prevent deposition of solids of horizontal pipes in hydraulic transport of sand and water has been investigated by Durand (1952).
Taghavi et al. (2014) designed a new mixing mechanism for conventional stirred tank reactors, improving its mixing characteristics.
Limited research has been devoted to solid-liquid suspension in loop reactor, tackled for the very first time in slurry polymerization of olefins. This type of reactor has potential applications in both biochemical reactions and processing of highly viscous liquids According to Sato et al. (1979); Murakami et al. (1982); and Nouri et al. (1997), it presents various advantages such as the prevention of polymer deposition at high Reynolds number and a heat transfer area per unit of reactor volume larger than stirred tank reactors. To proceed toward bulk polymerization of olefins, the loop reactor is operated at high Reynolds number in order to prevent polymer deposition, this leads to an increase in power consumption that must be taken into account for the design and operation of the reactor according to Murakami et al. (1982). For polymer suspension, adhesion of polymer on reactor walls ought to be prevented. Laederach & Widmer (1984) recommended an intensive mixing in order to ensure homogeneous distribution of phases and a full-on suspension of micro-organisms. At high impeller speed, no decrease of hydrolysis of wheat proteins was observed, as reported by Nouri et al. (1997) and Nasrallah et al. (2008), who stated that the main flow and mixing influencing parameters were the rotating speed, diameter and type of impeller.
According to Laederach & Widmer (1984), micro-organisms often tend to deposit in thick layers on the walls of the reactor, resulting in the depletion of active organisms in the reaction solution and a significant drop in productivity and/or product quality mainly because the organisms forming the layer are subject to a substrate limitation. Therefore, they suggested a high recirculation frequency, which has the effect of increasing the power dissipated by the stirrer.
Almost all researchers recommend working at high Reynolds number (high agitation speed) in order to prevent solid particles' deposition at the reactor walls and impeller (Sato et al. 1979; Murakami et al. 1982; Laederach & Widmer 1984; Tanaka et al. 1989). The minimal rotational speed at which all the solid particles were to be suspended has never been determined in a torus reactor.
The aim of this work is to experimentally determine the just suspended speed (Njs) in a torus reactor, comparing it to a modified Zwietering's correlation calculated value. A parametric study of the Njs has also been conducted (concentration, particles size, density). An experimental method based on visualization (Steady Bed Angle Method, SBAM) was elaborated to identify Njs in a torus reactor.
MATERIALS AND METHODS
Theoretical approach
Some efforts have been directed towards estimating the value of Njs using theoretical models; however, not all of these models can be considered as universally applicable. Most of these are solely based on the distinction between suspended and non-suspended particles. Tamburini et al. (2016a) in their work identified the complete suspension conditions. Zwietering back in the 1950s studied the suspension of particles and considered them completely suspended if they did not remain stationary at the bottom of the pipe or the reactor more than 1 s.
is the just suspended agitation speed (rpm), Sv the geometry coefficient (non dimensional), dp the particle diameter (m), 
the density difference between solid particles and liquid (kg/m3), 
the weight of the solid in suspension per weight of liquid, times 100 (non dimensional) and D, the tank diameter (m).
is the deposing velocity (m/s). Wasp et al. (1977) have compared the Durand correlation given by Equation (2) with data from Durand (1952) and Wicks (1968) to predict the deposition velocity of sand and water slurries. They concluded that the Durand correlation gives excellent prediction with an exception for low solids concentration (1% by volume). Wasp et al. (1977) modified Equation (2) for the deposition velocity of high concentrations in fully turbulent flow based on Wicks (1968) as follows:
and the rotation speed 
of the marine screw impeller and it is represented as follows:
is the fluid velocity (m/s), 
the impeller diameter (m), and 
the pitched angle of the impeller blade (deg). According to Zwietering (1958) and Nienow (1968), Equation (1) could be used to calculate Njs in a tank reactor. Wasp et al. (1977) and Kaushal et al. (2002) have used Equations (2) and (3) to estimate the deposition velocity in horizontal pipes. The just suspended speed (Njs) in a torus reactor can be calculated by combining Equation (3) proposed by Wasp et al. (1977) and Equation (4) proposed by Sato et al. (1979). The combined form of these equations allowed us to lay a modified version of Zwietering's correlation, which is expressed as follows:
Validation criterion
The model was validated using two methods: a graphical method, using correlation curves and a statistical method using validation criteria. Simulated results were compared to experimental (observed) data. Two criteria were adopted for this study.
represents the measured value of Njs for the ith experience and 
the simulated value.
and 
represent respectively the measured and simulated average rate with n, the number of experiences.
represents the standard deviation of measured Njs. RSR varies from zero, which indicates a low residual variability and therefore perfect model simulation, to a positive value. Table 1 shows the values of RSR and R² criteria corresponding to different degrees of performance of the model (Khemissi et al. 2019).General performance ratings for recommended statistical criteria
| Rating | RSR (%) | R2 (%) |
|---|---|---|
| Very good | 0 ≤ RSR ≤ 50 | 75 < R2 ≤ 100 |
| Good | 50 < RSR ≤ 60 | 65 < R2 ≤ 75 |
| Satisfactory | 60 < RSR ≤ 70 | 50 < R2 ≤ 65 |
| Unsatisfactory | RSR > 70 | R2 ≤ 50 |
| Rating | RSR (%) | R2 (%) |
|---|---|---|
| Very good | 0 ≤ RSR ≤ 50 | 75 < R2 ≤ 100 |
| Good | 50 < RSR ≤ 60 | 65 < R2 ≤ 75 |
| Satisfactory | 60 < RSR ≤ 70 | 50 < R2 ≤ 65 |
| Unsatisfactory | RSR > 70 | R2 ≤ 50 |
Description of the experimental device
The torus reactor used in this study and presented in Figure 1 is similar to that used by researchers (Belleville et al. 1992; Nouri et al. 2008; Nasrallah et al. 2008). Our device has been built using transparent pipes of inner diameter (Dt) of 50 mm, and a circumference length of 1,400 mm, which corresponds to a total volume of 2.9 L as shown in Figure 1(a). The mixing was achieved by a marine screw impeller as shown in Figure 1(b). The stirring was driven by a variable speed motor (IKA-WERK RW20).
Schematic of the torus reactor. (a) Description of settling bed. (b) The marine screw impeller.
Schematic of the torus reactor. (a) Description of settling bed. (b) The marine screw impeller.
This type of reactor has been formerly used in wastewater treatment by Alouache et al. (2017), geometrical characteristics of both the torus reactor and the marine screw impeller are given in Table 2.
Characteristics of the torus reactor and the marine screw impeller
| Torus reactor | Dt (mm) | Lt(mm) | Rt(mm) |
| 50 | 1,600 | 250 | |
| Marine screw impeller | d1(mm) | d2(mm) |  |
| 40 | 6 | 45° |
| Torus reactor | Dt (mm) | Lt(mm) | Rt(mm) |
| 50 | 1,600 | 250 | |
| Marine screw impeller | d1(mm) | d2(mm) | |
| 40 | 6 | 45° |
Measurement techniques and procedure
A large number of researchers have focused on the study of the just suspended speed for particles suspension, with the assessment based on experimental visualization (Armenante et al. 1992; Legrand 2007; Kuzmani et al. 2008; Brucato et al. 2010; Jirout & Rieger 2010; Ravelet et al. 2013). For this reason (Brucato et al. 2010) proposed an experimental method (the Steady Cone Radius Method, SCRM) in order to determine (Njs) in stirred tank reactor. According to (Zwietering 1958) for new systems such as in our case, the torus reactor, new experimental trials would be more accurate.
The experiment has been performed using transparent torus reactor fixed upon a table made of glass under which a mirror is accurately placed to capture its bottom. Only visual observations were made, no samples were taken from the suspension vessel, a simple digital camera was used for images acquisition. Solid particles of different materials and size were tested in water solution. The characteristics of solid particles are presented in Table 3.
Characteristics of solid particles
| Material | dp (μm) | Average dp (μm) |  (kg/m3) |
|---|---|---|---|
| Sand | 160–315 | 237.5 | 2,400 |
| 315–450 | 357.5 | ||
| 400–500 | 450 | ||
| Siporex | 315–450 | 357.5 | 1,900 |
| Biomass | 50–160 | 105 | 1,200 |
| 200–250 | 225 | ||
| 400–500 | 450 |
| Material | dp (μm) | Average dp (μm) | (kg/m3) |
|---|---|---|---|
| Sand | 160–315 | 237.5 | 2,400 |
| 315–450 | 357.5 | ||
| 400–500 | 450 | ||
| Siporex | 315–450 | 357.5 | 1,900 |
| Biomass | 50–160 | 105 | 1,200 |
| 200–250 | 225 | ||
| 400–500 | 450 |
In the present case, and for (Njs) measurement, an experimental method (Steady Bed Angle Method) based on visualization was elaborated and enabled us to identify the just suspended conditions in torus reactor as illustrated in Figure 2(a). The solid particles were introduced into the reactor, followed by an additional amount of water until reaching the reactor's volume.
Njs measurement (SBAM) apparatus: (a) global schemas of measurement device, (b) settling bed, (c) partial suspension (low speed), (d) partial suspension (high speed).
Njs measurement (SBAM) apparatus: (a) global schemas of measurement device, (b) settling bed, (c) partial suspension (low speed), (d) partial suspension (high speed).
The reactor is agitated at a high speed, permitting a homogeneous distribution of solid particles, after which the engine is stopped, leading to a precipitation of all the particles along the circumference reactor bottom, forming a particles settling bed with an angle
as shown in Figure 2(b).
By gradually increasing the stirring speed, the solid particles in the vicinity of the marine screw impeller are suspended, causing the decrease of the bed length of solid particles deposited at the reactor bottom. The angle formed between the two ends of the bed is measured by a protractor as shown in Figure 2(c) and 2(d). The camera is installed above the reactor; allowing visualization of the reflected image of the reactor bottom by the mirror placed below the reactor.
The choice of placing the camera above the reactor is aimed at: a better acquisition of the image of the reactor bottom; avoid that the support of the camera would be an obstacle for taking pictures.
The images taken by the camera are transmitted and visualized on a computer thus making it possible to manually adjust accurately the needles placed on both ends of the bed formed by the solid particles deposited at the reactor bottom. The angle 
measurement is made between the bed boundaries, it was taken with agitation and until a stable bed was formed.
. For each value of the stirring speed N, we obtain a certain angle α to calculate the ratio R as a function of N (rpm) for each concentration (Cv) of the solid particles. The increase in agitation speed leads to a decrease in the angle formed by the settling bed from 
(partial suspension) to
(complete suspension). The ratio R presented in Equation (9) can be exploited to determine the agitation speed at which no particles remain steady on the reactor bottom (complete suspension), this corresponds to (R = 0). And according to (Zwietering 1958) it corresponds to no particles remaining stationary at the bottom of the reactor more than 1 s.
Figure 3 shows the plot of R according to N for different solid particles concentration Cv in the reactor. For low values of the stirring speed (N) of less than 300 rpm, the ratio R tends to 1, which indicates that the bed formed by the solid particles remain almost stable throughout the bottom of the reactor. When increasing the stirring speed, the angle α decreases to the point where its visual measurement becomes difficult. The plot of the experimental points has a polynomial shape, its extrapolation towards the abscissa axis makes it possible to reach the value of the ratio R = 0 which corresponds to the angle α = 0, where there will be no more solid particles deposited on the reactor bottom for more than 1 to 2 s (Zweitering). The stirring speed at this point represents the just suspended speed (Njs) computed by second-order polynomial interpolation. All experiments were performed at least twice.
Njs determination.
The SBAM method has the advantage of avoiding measurement subjectivity and gives excellent reproducibility. Same remarks were observed by (Brucato et al. 2010) in stirred tank reactor.
The well mixed zone contains suspended particles in opposite of the transport zone which corresponds to the bed formed by the settling and jumped particles.
At the just suspended speed (Njs), the volume of the transport zone tends to zero which corresponds to 
, the torus reactor would then be composed only by the well mixed zone. As a result, an improvement of the mixture is obtained. The hydrodynamics of the fluid depend on the characteristics of solid particles, liquid phase, reactor geometry and the stirring parameters, which affect the suspension of these solid particles in the solution (Taghavi et al. 2014).
In torus reactor experiments, the suspension phenomenon can be explained by the existence of two zones as illustrated in Figure 1(a). A well-mixed zone as in case of a constant stirred tank reactor upstream and downstream the impeller, and a transport zone as in case of a plug flow. There is a boundary existing between the two zones contained in the torus volume. When a variation of agitation speed occurs, not only the volumes of the zones vary but their location within the torus evolves counter-clockwise (Dieulot et al. 2005). For a positive variation in impeller speed, the volume of the well-mixed zone increases whereas that of the transport zone decreases.
RESULTS AND DISCUSSION
Effect of particle concentration
For different sizes of sand particles, the dependence of Njs on solid mass concentration (Cv) is illustrated in Figure 4(a). In the same figure and for comparison purposes, lines reporting the Njs values for all particle sizes calculated by Equation (5) are reported. It can be seen that increasing (Cv) increases the required (Njs) to remove the settling bed and keep all particles suspended.
(a) Dependence of Njs on particles concentration of sand for different particle size. (b) Correlation curve of observed Njs (NObs) and simulated Njs (NSim) of sand for different particle size.
(a) Dependence of Njs on particles concentration of sand for different particle size. (b) Correlation curve of observed Njs (NObs) and simulated Njs (NSim) of sand for different particle size.
For small sand diameters, it was found that the majority of the observed Njs values (experimental) are contained in the two theoretical envelope curves resulting from Equation (5). Taking into account R2 and RSR, the best results for these criteria: (R2 > 92%) and RSR (RSR = 53%) are obtained for small sand particle sizes (dp = 237.5 μm), see Table 3. The (Njs) dependence on particle concentration in the torus reactor is similar compared to that given by Equation (5) 
where 
. The criteria used to validate the model are shown in Table 4.
Validation criteria of simulated model for different dp with Cv as a variable
| Biomas | Sand | |||||
|---|---|---|---|---|---|---|
| R2 (%) | RMSE (rpm) | RSR (%) | R2 | RMSE (rpm) | RSR (%) | |
| dp = 105 μm | 91.19 | 160.97 | 54 | / | / | / |
| dp = 225 μm | 0.02 | 32.02 | 211 | / | / | / |
| dp = 237,5 μm | / | / | 92.08 | 210.94 | 53 | |
| dp = 355.5 μm | / | / | 92.39 | 32.04 | 248 | |
| dp = 450 μm | 42.13 | 70.36 | 58 | 15.81 | 64.32 | 347 |
| Biomas | Sand | |||||
|---|---|---|---|---|---|---|
| R2 (%) | RMSE (rpm) | RSR (%) | R2 | RMSE (rpm) | RSR (%) | |
| dp = 105 μm | 91.19 | 160.97 | 54 | / | / | / |
| dp = 225 μm | 0.02 | 32.02 | 211 | / | / | / |
| dp = 237,5 μm | / | / | 92.08 | 210.94 | 53 | |
| dp = 355.5 μm | / | / | 92.39 | 32.04 | 248 | |
| dp = 450 μm | 42.13 | 70.36 | 58 | 15.81 | 64.32 | 347 |
However, for large diameters 355 and 450 μm, Unsatisfactory results have been obtained, these results are illustrated in the correlation curve showed in Figure 4(b), where there is an overestimation of Njs simulated by the Equation (5).
To apply these results in wastewater treatment, we have studied a solid particle widely used in this field, named ‘Pleurotus mutilus biomass’, used in small portions in order to remove toxic components of low concentrations. Njs was tested for low biomass concentrations as illustrated in Figure 5(a). It can be seen that for different particles concentration investigated. Njs values ranged between 800 and 1,000 (rpm).
(a) Dependence of Njs on particles concentration of biomass for different particle size. (b) Correlation plot of observed Njs (NObs) and simulated Njs (NSim) of biomass for different particle size.
(a) Dependence of Njs on particles concentration of biomass for different particle size. (b) Correlation plot of observed Njs (NObs) and simulated Njs (NSim) of biomass for different particle size.
For biomass, proceeding similarly to sand particles described above. It can be seen that the theoretical model gives a very good values for smaller particle diameters (dp = 105 μm), with (R2 > 91%) and (RSR = 54%). However, the model cannot simulate large diameters. This observation was verified graphically by the correlation curve shown in Figure 5(b). Indeed the model overestimates the values of Njs for large values of dp.
Effect of particle size
According to the experimental tests carried out in the laboratory on the range of selected granulometry, we found that the suspension speed Njs decreases with the increase in particle size. The Njs values presented in Figure 6(a) are plotted as a function of particle size dp. In the same figure are reported the calculated values of Njs for sand particles using Equation (5) for low concentration (solid line) and high concentration (dotted line) validated later on with the experimental results. It is found that the majority of the values of the Njs given experimentally are contained in the two theoretical envelope curves resulting from Equation (5). The validation criteria given in Table 5 show a very good appreciation of the theoretical model with R2 values range (71–99%); however, good appreciations of RSR values are obtained for low values of Cv (1%, 2%).
Validation criteria of simulated model for different concentrations with dp as a variable
| Cv = 1% | Cv = 2% | Cv = 3% | Cv = 4% | Cv = 5% | Cv = 6% | Cv = 7% | |
|---|---|---|---|---|---|---|---|
| R2 (%) | 70.65 | 93.44 | 79.20 | 76.61 | 89.34 | 95.22 | 99.75 |
| RMSE (rpm) | 41.78 | 48.71 | 161.40 | 172.38 | 230.28 | 255.94 | 274.68 |
| RSR (%) | 57.60 | 42.33 | 120.12 | 197.86 | 131.02 | 195.70 | 199.49 |
| Cv = 1% | Cv = 2% | Cv = 3% | Cv = 4% | Cv = 5% | Cv = 6% | Cv = 7% | |
|---|---|---|---|---|---|---|---|
| R2 (%) | 70.65 | 93.44 | 79.20 | 76.61 | 89.34 | 95.22 | 99.75 |
| RMSE (rpm) | 41.78 | 48.71 | 161.40 | 172.38 | 230.28 | 255.94 | 274.68 |
| RSR (%) | 57.60 | 42.33 | 120.12 | 197.86 | 131.02 | 195.70 | 199.49 |
(a) Dependence of Njs on particle size of sand for different concentrations. (b) Correlation plot of observed Njs (NObs) and simulated Njs (NSim) of sand for different concentrations.
(a) Dependence of Njs on particle size of sand for different concentrations. (b) Correlation plot of observed Njs (NObs) and simulated Njs (NSim) of sand for different concentrations.
For the small diameters range and for the low solid concentrations, we found a slight difference between experimental results and simulated ones of the proposed correlation, which could be representative. For low solid concentration, and low dp the (Njs) dependence on particle size in the torus reactor is similar to that given by Equation (5) 
where 
.
The correlation curves given in Figure 6(b) confirm the previous observation that of an overestimation of Njs for larger values of Cv
For the range of particle size investigated here, It can be seen that the dependence of Njs is much smaller for large particle sizes, and the correlation is no longer applicable, similar results were observed by Brucato. An increase in particle size has little effect on the Njs value; according to these results one may ideally think to use the largest particle size without increasing the stirring speed necessary to have complete suspension. The extrapolation of these results outside the size range investigated in this study presents risks and cannot be extended to large particle sizes. The same remarks were presented by (Brucato et al. 2010) in stirred tank reactor.
We noticed the decrease in Njs with the increase of particle sizes .As a matter of fact, the fine particles develop a larger contact area and thus greater shear stresses, (Westerholm et al. 2008; Chang & Powell 2013) whereas for large particle sizes, we notice the exact opposite. The detachment of small particles requires a greater inertia force. Thus a higher Njs speed, which justifies the surprising experimental values found.
Effect of particle density
Different types of solid have been studied such as: sand, siporex, and biomass. Figure 7(a) represents (Njs) plotted as a function of 
, the (Njs) is largely dependent on the difference in relative density between solid particles and liquid. We note that the higher density increases the rotational speed limit Njs necessary to get complete suspension in solution within the limits of experimental errors. Therefore, the density has the same impact as the concentration of solid particles.
(a) Dependence of Njs on relative particle density difference. (b) Correlation curve of observed Njs (NObs) and simulated Njs (Nsim) for different particle density of solids.
(a) Dependence of Njs on relative particle density difference. (b) Correlation curve of observed Njs (NObs) and simulated Njs (Nsim) for different particle density of solids.
The (Njs) dependence on liquid/solid relative density difference in the torus reactor is similar to that given by Equation (5) 
where 
.
According to the curves of Figure 7(a) and 7(b), a perfect correlation is observed between the measured values of Njs and the simulated ones, with a very appreciable values of R2 (97.41%) and RSR (16%).
CONCLUSION
Experiments in solid-liquid suspension for the torus reactor were performed. A new experimental method (Steady Bed Angle Method, SBAM) based on visualization has been elaborated to enable the visual assessment of the just suspended speed Njs.
We have studied various solid particles widely used in wastewater treatment and chemical reaction (biomass, sand). For each solid concentration, we have determined the just suspended speed (Njs), above which mass and heat transfer are inconsequential. This explains some kinetic reaction where mass transfer is a limiting factor.
The parameters affecting Njs, such as particle concentration, particle diameter and particle density, were investigated and compared with that calculated by our modified Zwietering's correlation. Similarity between experimental and theoretical values has been noted for the just suspended speed (Njs) for particle concentration and density difference.
It seems that the suspended speed in a torus reactor is proportional to the concentration and particle density and particle size, noting that the dependence on the particle diameter is negligible for large particle size. Deducing that our results are quite similar to researchers, the correlations give a good agreement for low concentration and small diameters.
For future research in torus reactor, these results can be exploited to ensure a homogeneous solution in wastewater treatment, and expand research toward optimization of speed values to avoid solid deposition and increase mass and heat transfer.
This type of reactor has promising applications in solid transportation and wastewater treatment. It can be suggested that it should be in continuous mode to facilitate its industrial application. The research results indicate that accurate calculation of the minimal velocity necessary for complete suspension could serve as an efficient method for solid-liquid mixing. This study is expected to lead to further research on suspension for different types of solid particles used in the engineering industry, as well as the geometric and physical parameters that affect the just suspended speed while also reducing costs of operations.
ACKNOWLEDGEMENTS
The authors are thankful to Aoudia Cherif, engineer at Eurl ANFM Bordj el BahriAlgiers for building the reactor and its accessories.