Solid-LiquidSeparation

固液分离技术

ISSN 0104-6632

Printed in Brazil .br/bjche

*To whom correspondence should be addressed

OF

*

Fax: +(55) (34) 239-4188,Bloco K,

CEP 38400-902, Uberlândia-MG, Brazil.

E-mail: masbarrozo@ufu.br

December 5, 2002 ; Accepted: September 23, 2004)

The objective of this work is to compare the

The experimental results

Solid-liquid separation;Hydrocyclone.

denominated the filtering hydrocyclone.

The hydrocyclone separates solid and liquid or

liquid and liquid by the difference in density between

the fluid and the material to be separated in this

equipment. Due to the fluid acquires a spiraling

motion caused by the tangent feeding, the material of

larger density is thrown against the wall of the

hydrocyclone and dragged to the underflow while

the one of smaller density proceeds for the overflow,

forming a free vortex (outer vortex) and a forced

vortex (inner vortex) in agreement with F igure 1.

The filtering hydrocyclone, wich is the subject of

this study, has another stream imposed of filtrate

originating in the filtration in the conical area. Figure

1 depicts a side view of the filtering hydrocyclone

and the trajectory of suspension for the conventional

hydrocyclone.

The objective of this work is to compare the

performances of filtering hydrocyclones of two

different designs, Bradley’s and Rietema’s

(Svarovsky, 1984, Rietema, 1961).

固液分离技术

144L. G. M. Vieira, E. A. Barbosa, J. J. R. Damasceno and M. A. S. Barrozo

Brazilian Journal of Chemical Engineering

Figure 1: Trajectory of suspension for the conventional hydrocyclone and filtering device scheme

MODELLING

Residence Time Theory

There are several theories for the describing the separation that takes place in hydrocyclones. Perhaps one of the best known is the residence time theory (Svarovsky, 1981). In this approach, first proposed by Rietema (1961), a particle of a given size will be collected if the time it remains inside the cyclone is equal to or greater than the time necessary for it to reach the wall. Under some assumptions, the residence time theory yields Eq.(1) for the prediction of cut size in cyclones:

(1)

where d 50 is the cut size, D C is the diameter of the cylindrical section of the cyclone,μ is the liquid viscosity, Q is the volumetric feed flowrate, ρ is the liquid density,ρs is the solid density and K is a parameter characteristic of each cyclone design,which is usually determined empirically.

It is important to highlight that the cut size obtained during operation of the hydrocyclone results not only from the action of the centrifugal field but also from the solid material carried by the downward stream fluid. Therefore, for the purpose of comparison with other hydrocyclones, the cut size due exclusively to centrifugal separation should be defined.This definition corresponds to the so-called

reduced cut size ('

50

d ), in which th

e flow-splitting effect (dead flux effect) is discounted (Svarovsky, 1984).

In order to allow estimation of the reduced cut

size, many authors suggested additional factors for Eq.(1) to account for the underflow-to-throughput ratio effect. Massarani (1997), for instance, put forth the following correlation for the prediction of reduced cut size:(2)

where

(3)

()(

)

V 4.5C V G C e =(4)

R L is the underflow-to-throughput ratio and C V is the volumetric feed concentration. It should be noted that the effect of the underflow-to-throughput ratio and the influence of the solids concentration on cut size are both considered.

Massarani (1997) proposed Eq.(5) for prediction of the underflow-to-throughput ratio:

(5)

where D U is the underflow diameter and B and C are constants for a given cyclone design.

F or Bradley’s and Rietema’s optimum designs,which are of interest in the present work, Massarani (1997) obtained the parameters shown in Table 1.

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Brazilian Journal of Chemical Engineering Vol. 22, No. 01, pp. 143- 152, January -March, 2005

Table 1: K, B and C parameters and Euler number for Bradley’s

and Rietema’s conventional designs.

Design K B C Eu

Bradley 0.01654.6 2.617000Rietema

0.039

145

4.75

1200

F or a specific hydrocyclone design, this author considers that the relationship between static pressure drop through the cyclone (-ΔP) and dynamic pressure,calculated from the characteristic velocity u c (ρ2c u /2),i.e., the Euler number, is constant, in according to Eq. (6):

(6)

We emphasize that the aforementioned equations and parameters apply only to the conventional hydrocyclone, i.e., a nonfiltering device. Correlations like these have been estimated in this work, while considering the characteristics of the filtering medium.Conical Filtration

As the conical sections of filtering hydrocyclones are permeable, a conical filtration occurs through them as the suspension circulates through the device. By applying the motion equation in cylindrical coordinates and Darcy’s law to the conical wall, a simplified mathematical model for this filtration is deduced as shown below.

F or an incompressible radial flow obeying Darcy’s law across the filtering cone in steady state, as shown in F

igure 2, the motion equation in cylindrical coordinates yields

(7)

where dP/dr is the pressure gradient through the porous wall,Q F is the filtrate flowrate,K m is the medium permeability,ε is the medium thickness and A L is the lateral area of the cone surface. Alternatively, K m and A L might be expressed as follows:

(8)

m L is the lateral area of the cone surface, which might be expressed as a function of the lowest radius.(9)

where L is the hydrocyclone length, L 1 is the length of the cylindrical section and D inf is the lowest internal diameter of the cone.

Substituting Eq. (8) and Eq. (9) into Eq. (7):

(10)

F or a uniform pore distribution (i.e., R m does not depend on the position inside the cone) and an isothermal system (μ and ρ are constant), Eq. (10) can be integrated from (D inf /2) to (D inf /2 +ε). Doing this and isolating the filtrate flowrate (Q

F ) we obtain Eq. (11):(11)

Eq. (11) represents the volumetric filtrate

flowrate obtained in a conical filtration as a function of the difference between the pressure directly applied to the filtering wall and the atmospheric pressure (ΔP m ) and the dimensions of the cone. It can be rearranged in order to allow estimation of the resistance of the filtering medium.(12)

Thus, the relationship between the filtrate flowrates (Q F ) and pressure drops through the filtering cone (-ΔP m ) is linear. The value of R m may be estimated through linear regression of a data set.It might be argued that filter cake resistivity should be included in the formulation, analogous to flat filtration. Nevertheless, during the experiments it was verified that no cake is formed, owing to the high tangential velocity of the slurry within the hydrocyclones (Souza, 2000).

固液分离技术

146L. G. M. Vieira, E. A. Barbosa, J. J. R. Damasceno and M. A. S. Barrozo

Brazilian Journal of Chemical Engineering

Figure 2:EXPERIMENTAL

Material

The particulate material used was pyrochlore (65% Nb 2O 5), which has a suitable density (ρs =4030 kg.m -3). The particle size distribution of the samples was determined by the gamma-ray attenuation unit. Am 241 was the radioactive source utilized. The relationship between the beams counted by the equipment and the volumetric solids concentration (C V ) in a given suspension may be derived from Lambert’s equation. Eq. (13), for example, was obtained for pyrochlore aqueous suspensions:

(13)

where I is number of the gamma-ray beams counted for a uniform suspension and I o is the number of gamma-ray beams counted for pure water.

With the aid of an axial stirrer, the slurry was made uniform and its concentration calculated according to Eq. (13). The particles were allowed to settle further this time gravitationally, and the Stokes diameters and the cumulative mass fractions could be obtained by means of Eqs.(14) and (15),respectively. This procedure usually required approximately 25 minutes.

(14)

(15)

where d Stk is the Stokes diameter,μ is the liquid viscosity, H is the position of measurement, t is the time of measurement, ρ is the liquid density, ρs is the solid density and I t is the number of gamma-ray beams counted for a suspension at time t elapsed from the beginning of the settling.

In F igure 3 the fitting of the pyrochlore to the Rosin-Rammler-Bennet size distribution model is shown (Allen, 1997). Hydrocyclones

Table 2 shows the dimensions of the hydrocyclones studied in this work (Bradley’s and Rietema’s designs).

The filtering hydrocyclones had cylindrical section diameter (D C ) of 3.10-2 m and underflow diameters (D U ) of 3.10-3, 4.10-3 and 5.10-3 m. Three filtering cones R1, R2, R3, were made of sinter bronze for the hydrocyclone of Rietema’s design. Besides, two cones of sinter bronze and one of polypropylene referred to as B1, B2 and P, respectively, were made in accordance with Bradley’s design.

固液分离技术

Performance Analysis and Design

147

Brazilian Journal of Chemical Engineering Vol. 22, No. 01, pp. 143- 152, January -March, 2005

Table 2: Dimensions of Rietema’s and Bradley’s hydrocyclones

D i /D C

D o /D C L/D C Angle Rietema 0.280.34 5.00200Bradley

1/7

1/5

6.8

90

Experimental Apparatus and Procedure

F igure 4 illustrates the unit where the experiments were carried out. It basically comprises a well-stirred tank, whose volume was approximately 0.25 m 3, a 5HP centrifugal pump, valves, a pressure gauge and the filtering hydrocyclone itself. The system was operated as follows: after filling the tank with the slurry, the stirrer was switched on in order to achieve efficient mixing. Then the pump was turned on and the pressure drop was set to the desired value by either opening or closing the valves. The system was allowed to stabilize, a process which normally took about five minutes.Samples of all the streams, feed, overflow, underflow and filtrate, were then collected for further evaluation of mass flowrates, concentrations and particle size distributions. Gravimetric techniques were used to determine the mass flowrates. The properties of the fluid (μ and ρ) were estimated by measuring of the temperature of the suspension.

Figure 4:Experimental apparatus

固液分离技术

148L. G. M. Vieira, E. A. Barbosa, J. J. R. Damasceno and M. A. S. Barrozo

Brazilian Journal of Chemical Engineering

Characterization of the Filtering Media

To apply Eq. (11) in determining of the filtering medium resistances (R m ), the filtering cones were fed with pure water at low flowrates at 25.5 o C. This was done to avoid the formation of vortices and to guarantee exertion of constant pressure on the wall.The experiments were carried out in a simple unit,similar to the one shown in Figure 4, but consisting of a peristaltic pump and a U-tube manometer. The underflow orifice and overflow tube were closed and the respective filtrate flowrates (Q F ) and pressure drops (ΔP m ) were varied and measured for each cone.

RESULTS AND DISCUSSION

In Table 3 the values of filtering medium resistance (R m ), obtained for the fitting of the experimental data to Eq.(11), are displayed the conventional hydrocyclones (without a filtering cone) were referred to as BC and RC for Bradley’s and Rietema’s designs, respectively.

The Table 3 demonstrates that similar ranges of the filtering medium resistances were used to Bradley and Rietema hydrocyclones. In the studied operational conditions, the P filtering hydrocyclone was the most permeable device while the B1 filtering hydrocyclone presented the smallest permeability.

Table 3: Filtering medium resistances (R m ) for the hydrocyclones

Cone of Bradley’s hydrocyclone Cone of Rietema’s hydrocyclone

B1

B2P BC R1R2R3RC R m (m -1)

10.63.1011

6.5.1011

0.579.1011

∞

6.3

7.1011

4.9

5.1011

4.54.1011

∞

Figure 5: Medium underflow-to-throughput ratio for all the hydrocyclones

The Underflow-to-Throughput Ratio

The underflow-to-throughput ratio in both designs was changed significantly by the filtering medium, as shown in F igure 5. By analyzing this figure, it is possible to conclude that the underflow-to-throughput ratios of both designs changed due to filtration. The more pronounced changes were seen

for which hydrocyclones Rietemas’s design, which supplied more diluted underflow streams.

Through nonlinear regression, the experimental underflow-to-throughput ratios for both designs were correlated as a function of the underflow holes and filtering medium resistances. The correlations for Bradley’s and Rietema’s filtering hydrocyclones are represented by Eq. (16) and Eq. (17), respectively.

(16)

where D U Diameter of the underflow R L

Underflow-to-throughput ratio R1,R2,R3Rietema’s filtering hydrocyclones RC

Rietema’s conventional hydrocyclone

B1, B2, P Bradley’s filtering hydrocyclones BC Bradley’s conventional

hydrocyclone

固液分离技术

Performance Analysis and Design 149

Brazilian Journal of Chemical Engineering Vol. 22, No. 01, pp. 143- 152, January -March, 2005

where

99

m C 0.174.10R D 5.315.10≤

≤(17)

where

99

m C 1.362.10R D 3.185.10≤≤Feed Flowrate and Euler Number

hydrocyclones behaved differently respective conventional devices. Figure 6 shows that while the volumetric feed flowrates decreased for Rietema’s filtering hydrocyclones, there was an increase in this same variable for Bradley’s filtering hydrocyclones,when compared with the conventional hydrocyclone.As well as the changes in the volumetric feed flowrates, the filtering hydrocyclones had new values for the Euler numbers, as can be seen in F igure 7. Within the limits of the experimental region studied in this work, Rietema’s filtering hydrocyclones had higher Euler numbers than the conventional device, while the Bradley’s filtering hydrocyclones reductions in this same variable.

In accordance with experimental data, the Euler numbers for the Bradley’s filtering hydrocyclones were mainly influenced by the resistance of the filtering medium and the underflow-to-throughput (Eq. (18)), while this same variable for Rietema’s filtering hydrocyclones was only dependent on the Reynolds number and the underflow dimension (Eq.

U

固液分离技术

150L. G. M. Vieira, E. A. Barbosa, J. J. R. Damasceno and M. A. S. Barrozo

Brazilian Journal of Chemical Engineering

(18)

where

99

m C 0.174.10R D 5.315.10≤

≤(19)

where

10221

Re 16394

≤≤Overall Efficiency

Changes in the underflow-to-throughput ratios affected overall efficiency in both designs that were employed in this study, as shown in Figure 8.

The overall efficiency of Rietema’s filtering hydrocyclones increased more than that of the conventional device. This characteristic behavior of overall efficiency occurred due to the increase in the values of the underflow-to-throughput ratio, which were responsible for the higher drag of solids by the underflow stream. F or Bradley’s filtering hydrocyclones the opposite occurred because the reduction in the underflow-to-throughput ratio caused lower overall efficiencies than that of the conventional hydrocyclone.

Based on the experimental data collected on the filtering hydrocyclones, Eq. (20) and Eq. (21) were proposed for Bradley’s and Rietema’s designs,respectively. These expressions elucidate how the well-defined of separation changes as a function of volumetric feed flowrate and underflow-to-throughput ratio.

(20)

(21)

In this context, it could be verified that the main modifications in reduced cut sizes occurred due to the new values of underflow-to-throughput ratio. In both filtering hydrocyclones, this variable reflects all the influences of the filtration process, as observed in function F(R L ).

固液分离技术

Performance Analysis and Design

151Brazilian Journal of Chemical Engineering Vol. 22, No. 01, pp. 143- 152, January -March, 2005CONCLUSIONS The experimental results obtained with the filtering hydrocyclones under the same operational conditions as those for the corresponding conventional devices, allow the following conclusions to be drawn.The performance of the hydrocyclones of Bradley’s and Rietema’s designs is significantly influenced by the filtering medium. The underflow-to-throughput ratios of both filtering devices underwent changes in relation to the corresponding conventional devices increasing for Rietema’s filtering hydrocyclone and decreasing for Bradley’s filtering hydrocyclone. While Rietema’s filtering hydrocyclones had a lower volumetric feed flowrate than the conventional device, Bradley’s filtering hydrocyclones showed increases in this same variable. While the Euler numbers for Rietema’s filtering hydrocyclones increased move under the same operational conditions, than that of the conventional device, for the Bradley’s filtering hydrocyclones they decreased. In both designs,overall efficiency was influenced by the underflow-to-throughput ratio. F or Rietemas’s filtering hydrocyclones the underflow-to-throughput ratio contributed to the increase overall efficiency. The overall efficiency of the Bradley’s filtering hydrocyclones decreased compared to the conventional device, due to the reduction in solids in the underflow stream. F iltration and design were equally important at the same degree for understanding the separation process in the filtering hydrocyclone.NOMENCLATURE A L lateral area of the cone surface (m 2)B and C parameters in Eq. (5)(-)C V volumetric solid concentration (m

3solid /

m 3suspension )D C diameter of the cylindrical section of the hydrocyclone (m)

D i inlet diameter of the hydrocyclone (m)D inf lowest internal diameter of the filtering cone (m)D O overflow tube diameter (m)D U underflow orifice diameter (m)d Stk Stokes diameter

(m)50d cut size

(m)'50d reduced cut size (m)Eu Euler number (-)g gravity (-)H position of gamma-ray

measurement (m)I gamma-ray beams counted for suspension (-)I o gamma-ray beams counted for pure water (-)I t gamma-ray beams counted for suspension as a function of time (-)K parameter in Eq.(1) and Eq.(2)(-)K m filtering medium permeability (m 2)l vortex finder length (m)L hydrocyclone length (m)L 1length of the cylindrical section of the hydrocyclone (m)P pressure of gas inside the filtering cone (kg m -1s -2)P atm atmospherie pressure (kg m -1s -2)Q volumetric feed flowrate (m 3s -1)Q F volumetric filtrate flowrate (m 3s -1)Re Reynolds number (-)R L underflow-to-throughput ratio

(-)R m filtering medium

resistance

(m -1)t time

(s)u c speed of the suspension

in the cylindrical area

(m s -1)X cumulative mass

fraction (-)Greek Letters

εfiltering medium thickness (m)P Δpressure drop between

the feed volumetric and

overflow streams

(kg m -1s -2)μliquid viscosity (kg m -1s -1)θincluded angle of the

cone (-)ρ,s ρliquid and solid density,

respectively

(kg m -3)

固液分离技术

152L. G. M. Vieira, E. A. Barbosa, J. J. R. Damasceno and M. A. S. Barrozo

Brazilian Journal of Chemical Engineering

ACKNOWLEDGMENTS

It is necessary to acknowledge our gratitude to the Postgraduate Program in Chemical Engineering at the F ederal University of Uberlândia, to the F APEMIG,CNPq and to the CAPES, Brazilian institutions that made available the resources necessary for the development and conclusion of this work.

REFERENCES

Allen, T., Particle Size Measurement, 5th ed.,London: Chapman and Hall, 524p. (1997).

Barrozo, M.A.S., Damasceno, J.J.R. and Lanna, A.E.,Estudo do Desempenho de um Hidrociclone Filtrante, Revista Ciência & Engenharia, 1, pp. 175-186 (1992).

Massarani, G., F luidodinâmica em Sistemas Particulados, Rio de Janeiro: Editora UFRJ, (1997).Rietema, K., Performance and Design of Hydrocyclone. Chemical Engineering Science, 15,pp. 298-325 (1961).

Souza, F .J., Vieira, L.G.M., Damasceno, J.J.R. and Barrozo, M.A.S., Analysis of the Influence of the F iltering Medium on the Behaviour of the F iltering Hydrocyclone, Powder Technology, vol. 107, pp.259-267 (2000).

Svarovsky, L., Solid-liquid Separation, London-UK:Butterworths, (1981).

Svarovsky, L., Hydrocyclones, New York: Holt,Rinehart and Winston (1984).

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