MSCE  Vol.9 No.6 , June 2021
Predicting Mass Transfer Extraction with Steam Flow, Applying Boundary-Layer Concepts
Abstract: Theory and concepts of boundary layer mass transfer is applied to correlate experimental data on extraction of essential oils from vegetable leaves and stems, using steam. From these theory, concepts and experimental data with seven systems, two correlations are developed to predict the Sherwood number and mass transfer coefficient as function of Reynolds and Schmidt numbers. From these equations, the molar flux, the amount of solute extracted, and the yield of extraction is predicted. A steam of higher temperature normally improves the mass transfer and the yield. A method to estimate the enhancement for temperature increase is proposed. The correlations developed are applied to a case with industrial size that was no part of the data for correlation generation. Theory may be applied for industrial applications.

1. Introduction

Essential oil from plants is used in food, pharmacy, and fragrance industries due to their organoleptic and biological properties associated with their natural characteristics. Leaves and stem from plants are the raw material for the extraction of the essential oil. The total extraction of essential oil from vegetal leaves is usually small than 5% and there are several methods to perform the extraction. Hydro distillation with water in contact with the plant [1], steam distillation, with steam (but not water) contacting the plant, mechanical pressure (squeezing) [2], soxhlet extraction with organic solvents [3], extraction with supercritical solvents like CO2, and microwave extraction [4].

The extraction of essential oil by steam distillation uses a cylindrical column filled with vegetal leaves and stems. The steam flow through the leaves and stems, first heating them and then dissolving on it the essential oil, and taking out from the column with the flowing steam. The flowing steam that leaves the column is passing to a condenser where the oil and water usually form two different liquid phases and are separated in equipment called Florentine. Figure 1 shows a scheme of a steam distillation system and a typical diagram from experimental results taken from Cerpa’s Dissertation [5].

The experimental data of yield versus time of Figure 1(b) is modeled, by example with Xavier et al. [6] approach, using the mechanistic model proposed by Cerpa, Mato and Cocero [7], or some other.

In this manuscript, the final yield is modeled by using the concepts of boundary layer that were developed first for fluid flow by Ludwig Prandtl in 1904 who develop the first differential equations to model the hydraulic phenomena. Blausius helps to solve the mathematical model. Prandtl and other researchers began to apply it to heat transfer, Chilton-Coulburn and Guilliland-Sherwood applied it to mass transfer. Latter Bird Stewart and Lightfoot developed the concept of transport phenomena. This lead to apply the boundary layer theory to experimental and industrial cases, help the field of applied chemistry to be converted on chemical engineering and get maturity as science and engineering.

Chemical engineering applies the boundary layer concepts to correlate experimental data on flow of fluids, heat transfer, and mass transfer, as function of dimensionless numbers.

For mass transfer: Reynolds R e = U e f ρ V D c μ V , Schmidt S c = μ V ρ V D A B , and Sherwood S h = k C D C D A B . Basically:

S h = α 1 R e D c α 2 S c V α 3 (1)

Several series of experimental and reported data is used to get variation on

Figure 1. (a) Scheme of steam extraction system, (b) Yield of extraction versus time.

operational, physical properties, and geometrical parameters, to generate correlations to predict Sherwood number., and to calculate mass transfer, and yield of extraction.

2. Materials and Methods

2.1. Experimental Reported Data Used

Table 1 shows the systems used.

2.2. Boundary Layer Concept Applied to Mass Transfer

(Taken from [8] ) A concentration gradient is formed together to the hydrodynamic and thermal one. Let CAO be the concentration of the incoming flow to a plate made of a solid that is soluble in the liquid. CAO will be the concentration also at core of the flow, far from the plate. When the liquid is in contact with the plate the equilibrium is reached instantaneously at the interface liquid-solid. The concentration of A at the fluid, at the plane of contact with the solid surface will be that of saturation (CAs = CAi). The mass molecular diffusion at y direction will set that the concentration gradient be growing when the liquid advance in x.

Authors or researchers from Table 1, report the dynamic (yield versus time). In this study only the final yield is correlated with physical properties, geometrical characteristics, and operational parameters. Defining the variable γ = C A i C A (analogous to temperature in excess), the concentration gradient will be that of Figure 2. The dotted line is laminar underlayer.

The edge of the concentration boundary layer is then the geometric place where γ A = 0.99 γ A o , being γ A o = C A i C A o the maximum value de γ.

Table 1. Characteristics of the studied systems.

Figure 2. Gradients of velocity, temperature, and concentration at boundary layers.

The continuity equation for A, if density ρ, and diffusivity DAB are constant, is:

υ x γ A x + υ y γ A y = D A B ( 2 γ A y 2 ) (2)

It has as boundary conditions: γ A ( x = 0 , y ) = γ A o ; γ A ( x , y = 0 ) = 0 ; γ A ( x , y = ) = γ A o

That is similar to the one Blasius solved, but now for mass transfer. The dependent variable is now = γ A γ A o = C A i C A C A i C A o that is function of the dimensionless variable η = y x R e x .

If it is desired a mathematical expression for the flux of A at the solid surface (NA in kmol/m2/s), it is needed to use Fick’s law to obtain

N A , x = 0.332 D A B ( C A i C A o ) R e x x (3)

Integrating over the plate length

N A = 0.664 D A B ( C A i C A o ) L R e L (4)

By analogy to the thermal boundary layer, the Schmidt number relates the diffusivities of mass and momentum, giving:

S c ν D A B = μ ρ D A B (5)

Equation (4) is valid only if Sc= 1. For the cases with Sc ≠ 1 it is necessary to introduce an experimental correction factor Sc1/3

N A = 0.664 D A B ( C A i C A o ) L R e L S c 1 / 3 (6)

Equation (6) has been experimentally tested.

2.3. Mass Transfer Coefficient

Equation (6) allows the calculation of the rate of mass transfer for molecular diffusion at forced convection for laminar flow. If the flow is turbulent or the geometry of the system is complex, as is the case in many practical cases. For this case it is necessary to use the mass transfer coefficient, defined by Equation (7):

k c N A Δ C A = N A C A i C A o (7)

Applying Equation (6) on Equation (7) we get:

k c = 0.664 D A B R e L L S c 1 / 3 (8)

This equation may be arranged and it provide the Sherwood dimensionless number:

S h = k c L D A B = 0.664 R e L S c 1 / 3 (9)

Sh is the Sherwood number, counterpart of Nusselt number in heat transfer. At turbulent flow, and for complex geometrical systems the mass transfer coefficient kC, will be empirical.

2.4. Application to Extraction with Steam Flow

From the reported data with the sources given in Table 1, we may calculate the amount of mass extracted with mextracted = mo yieldx 100 (kg) and convert it to kmol dividing it between the molecular weight of the solute extracted. Then the flux of A (NA, kmol/m2/s) will be this kmol divided between the transversal area to flow and also divided by the residence time of the flow. This last parameter may be calculated dividing the volume (m3) of extractor between the volumetric flows of steam (m3/s).

A program was developed with Excel software and applied to each series of data in Table 1. CAi is the concentration of solute at the surface of the vegetal leave (at y= 0). This may be taken as the solubility of the solute in kmol/m3. Because the steam does not contain solute: CAo = 0. Then using Equation (7):

k c = N A C A i C A o = kmol m 2 s kmol m 3 = m s (10)

Then with physical properties, we calculate Sherwood number (kcD/DAB), and calculating Reynolds number R e = U e f d e n V D C v i s c V = m s kg m 3 m kg m s and Schmidt number S c = v i s c d e n D A B = kg m s kg m 3 m 2 s and using a reasonable number of data points we can correlate coefficient and exponents (α1, α2, and α3).

2.5. Physical Properties

Table 2 shows some of the physical properties used in the Excel program.

Table 2. Physical properties of solutes that dissolves into steam.

Density and viscosity were taken from [8], diffusivities were predicted withthe correlation of Fuller et al. [15]. Solubility was taken from PubChem, National Library of Medicine, Center for Biotechnology Information, that usually is expressed as mg or gr/liter. We convert it to kg and to kmol dividing between the molecular weight and converting the volume at the denominator to cubic meters.

Most of the experimental extraction with steam used atmospheric pressure and temperature of 100˚C. Only some data from Roautby et al. [12] and Rondhame and Tizaoui [13] were at temperature above 100˚C. These data were processed in a different Excel program, to get the effect of temperature over the yield of extraction.

In the general study, steam at 100˚C was used and the physical properties density and viscosity keep constant values. Diffusivity varies a little depending of the solute.

The exponent α3 in Equation (1) keep a constant value of 1/3 or 0.33 for the Schmidt number in the hydrodynamic bounder layer as well as for the Prandtl thermal boundary. Then, here for mass transfer, we are going to take this exponent constant: α3 = 0.33.

3. Results and Discussion

3.1. Results from Excel Program for T = 100˚C

Table 3 shows some of the results of the Excel program applied to the data at 100˚C. It is noted that the Reynolds number is less than unity for the systems of Cerpa et al. and Masango et al., and is bigger for all other systems, reaching values above 2000 for the systems of Roautby et al. and Ozek.

Figure 3 shows the plot of Ln(Sh/Sc(1/3)) versus Ln(ReDc) obtained when α3 = (1/3) for all data for the several systems used. From this data, Equation (11) provides the first correlation equation.

S h = α 1 R e D c α 2 S c α 3 = 0.2754 R e D c 1.5338 S c 0.333 (11)

If we pass the line at the intersection Sh/Sc0.33 = 1.0 to get ReDc = 0, we get the equation y = 1.2964 x + 1 and from this equation we get the second correlation Equation (12). The prediction with Equation (11) and Equation (12) is shown in Figure 4(a) and Figure 4(b). The two correlations may be considered limits for prediction.

S h = α 1 R e D c α 2 S c α 3 = 2.7182 R e D c 1.2964 S c 0.333 (12)

3.2. Results for Temperature Increase

Rouatby et al. [12] studied the extraction of essential oil of thyme by superheated steam. They used steam temperatures of 100˚C, 175˚C, and 250˚C. They found that at higher temperatures the yield of extraction increases. Because the physical

Table 3. Parameters and mass transfer coefficient and exponent, from correlated data, for α3 = 1/3.

Figure 3. Ln(Re) versus Ln(Sh/Sc0.33) used to get α1 and α2.

Figure 4. Prediction of Sherwood number for all data. (a) For RE < 2, (b) ALL DATA.

properties changed, most of the parameters changed as well. Table 4 shows some of the values obtained.

The last two rows of Table 4 provide the ratio of the property or parameter at 175˚C/100˚C, and 250˚C/100˚C. When that ratio is unity, the values are similar for the three temperatures.

When the ratio is fractional, by example the volumetric flow of steam: Q 175 Q 100 = 0.132 means that the volumetric flow rate of steam at 175˚C is 0.132 times the volumetric flow rate at 100˚C. This happen because the density of steam at 175˚C is 7.56 times higher than at 100˚C.

For the flow at 250˚C the ratio is Q 250 Q 100 = 0.030 this means that the flow rate of steam at 250˚C is about 3% of the volumetric flow rate of steam at 100˚C.

When the ratio is higher than unity, by example Y 175 Y 100 = 1.205 this means that the yield of extraction is 1.205 higher at 175˚C than at 100˚C.

Note that the superficial and effective velocities are higher at low temperatures (100˚C) than at 175˚C or 250˚C, residence time, density, viscosity, diffusivity, and the mass extracted are higher for bigger temperatures. Reynolds, Schmidt,

(a) (b) (c)

Table 4. Some values for Data of Roautby et al. [12] for the extraction of thyme leaves.

and Sherwood numbers, as well as the molar flux and the mass transfer coefficient are lower for the higher temperatures. For predicted Sherwood number:

S h 175 S h 100 = 0.306 (13)

S h 250 S h 100 = 0.100 (14)

Figure 5 provides a method to estimate the Sherwood number at different temperatures of steam.

4. Case of Study, Prediction of Yield

The data on the paper of Koul et al. [16] will be taken as example to predict the yield of experiments 3, 4, 5, 6, and 7. In this case lemon grass oil is obtained by steam distillation of lemon grass (Cymbopogon spp.) the main solute is citral or geranial (C10H16O), that has the same formula than camphor then (DAB = 1.17E−5 m2/s) but the solubility is CAi = 0.003289 kmol/m3.

The first two experiments used mo= 70 kg, and the last three used 1000 kg. These are industrial quantities. In Table 1 the data of Ozek use the biggest equipment size (0.5 m3) and the highest quantity of vegetal leaves (24 - 38 kg). We era going to use the data of Ozek to estimate the volume of cylinder needed for Koul experiments. Ozek [14] used V = 0.5 m3 for 35 kg of mass. Then for Koul:

V 1 = 0.5 × 100 / 35 = 1.428 m 3 and V 2 = 0.5 × 1000 / 35 = 14.286 m 3

Choosing a diameter of Dc = 2.0 m, A= 3.1416*Dc2/4 = 3.1416 m2, and V = A*z, then z1 = V1/A = 1.428/3.1416 = 0.46 m = z1, and z2 = V2/A = 14.286/3.1416 = 4.55 m = z2.

The steam flow rate Qi in m3/s used in Koul experiments were: 15, 12, 160, 125 and 140 L/h (0.015, 0.012, 0.125, 0.140 m3/h, or 4.166E−6, 3.33 E−6, 4.44E−5, 3.472E−5, 3.88E−5 m3/s).

Figure 5. Prediction for temperature of steam effect on Sherwood number.

For the yield calculation, experiments 3 - 7 were: 385, 330, 5725, 5215, 5315 mL of citral oil at 5 h = 300 minutes = 18,000 seconds. With a density of citral of 0.9 gr/ml or 900 kg/m3 and the 70 kg of lemon grass for experiments 3 and 4 and 1000 kg of lemon grass for experiments 5 - 7, we get: y3 = 0.495, y4 = 0.424, y5 = 0.515, y6 = 0.469, y7 = 0.478.

With the cylinder dimensions Dc = 2 m y z1 = 0.46, and z2 = 4.55 m, we get A = pi*Dc2/4 = 3.1416 m2, and V1 = 1.44 m3, V2 = 14.2 m3. Dividing volumetric flow rate between area we get Superficial velocities, and dividing these between void fraction, we get effective velocities Uef3 = 0.0000018, Uef4 = 0.0000014, Uef5 = 0.0000188, Uef6 = 0.0000147, Uef7 = 0.0000165 m/s.

Residence time of steam may be calculated dividing volume between steam volumetric flow rate, and we get: tr3 = 346,888.1, tr4 = 433,974.8, tr5 = 321,943.2, tr6 = 411,701.6, tr7 = 368,409.3 seconds.

Now, we can calculate Reynolds numbers with Equation (15)

R e i = U e f i d e n v a p D c V i s c v a p (15)

And Schmidt and Sherwood numbers with Equation (16) and Equation (11) or Equation (12)

S c = v i s c v a p d e n v a p D A B (16)

Table 5. Calculated values for Kaoul et al. [16] yields.

Figure 6. Prediction on Koul [16], using the present model.

With Sherwood number, we can get the mass transfer coefficient kc, and from this, the flux NA, then, mA, and finally the yield yA with Equations (17)-(20). Because the steam does not have solute CAo = 0

k C = S h D A B D C (17)

N A = k c ( C A i C A o ) (18)

m A = N A × A × t R × P M A (19)

y a i = ( m A m o ) × 100 (20)

Table 5 provides the main calculated values, and Figure 6 provides the comparison between reported and predicted values.

On Figure 6 it is observed that both predictions 1 and 2 follow the order of the reported data. Prediction 1 underpredicts 0.31, and prediction 2 overpredicts 3.32 the values of reported yield of extraction from Koul et al. [16].

5. Conclusions

The proposed Equation (11) and Equation (12) provide correlations to predict the yield of extraction, by first estimating the dimensionless numbers Reynolds, Schmidt, and Sherwood numbers, and using equations for the mass transfer involved in the extraction of solute from vegetable leaves to steam, using boundary layer concepts and definitions like molar flux and mass transfer coefficient.

The predicting Equation (11) and Equation (12) provide limits to experimental or reported yields and predict well the effect of steam flow.

Figure 5 and Equation (21) help to predict Sherwood number for superheated steam at temperatures above 100˚C.

S h ( T ˚ C ) S h ( 100 ˚ C ) = 4.591 exp 0.015 × T ( ˚ C ) (21)

Using steam at temperatures higher than 100˚C improves the extraction yield, but at temperatures above 200˚C, the temperature degrades some components of the mixture of essential oil.

Cite this paper: Rocha-Uribe, J. , Soto-Armenta, L. , Hernandez-Ruiz, A. and Jimenez-Ocaña, J. (2021) Predicting Mass Transfer Extraction with Steam Flow, Applying Boundary-Layer Concepts. Journal of Materials Science and Chemical Engineering, 9, 46-58. doi: 10.4236/msce.2021.96004.

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