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## Brazilian Journal of Chemical Engineering

*Print version* ISSN 0104-6632

### Braz. J. Chem. Eng. vol.29 no.2 São Paulo Apr./June 2012

#### http://dx.doi.org/10.1590/S0104-66322012000200016

**PROCESS SYSTEMS ENGINEERING**

**Modelling of fertilizer drying in a rotary dryer: parametric sensitivity analysis**

**M. G. Silva ^{I}; T. S. Lira^{II}; E. B. Arruda^{III}; V. V. Murata^{I}; M. A. S. Barrozo^{I,*}**

^{I}School of Chemical Engineering, Federal University of Uberlândia, Phone: + (55) (34) 32394292, Fax: + (55) (34) 32394188, Av. João Naves de Ávila 2121, Uberlândia - MG, Brazil. E-mail: masbarrozo@pesquisador.cnpq.br

^{II}Departament of Engineering and Computation, Federal University of Espírito Santo, Rod. BR 101 Norte, km. 60, São Mateus - ES, Brazil

^{III}School of Integrated Sciences of Pontal, Federal University of Uberlândia, Av. José João Dib 2545, Ituiutaba - MG, Brazil

**ABSTRACT**

This study analyzed the influence of the following parameters: overall volumetric heat transfer coefficient, coefficient of heat loss, drying rate, specific heat of the solid and specific heat of dry air on the prediction of a model for the fertilizer drying in rotary dryers. The method of parametric sensitivity using an experimental design was employed in this study. All parameters studied significantly affected the responses of the drying model. In general, the model showed greater sensitivity to the parameters drying rate and overall volumetric heat transfer coefficient.

**Keywords:** Heat and mass transfer; Fertilizer drying; Rotary dryers; Parametric sensitivity.

**INTRODUCTION**

Rotary dryers are often used for drying in fertilizer industries. They consist basically of a long cylindrical shell inclined at a small angle to the horizontal. The inside portion of the shell is equipped with lifting flights (see Figure 1) to cascade solid material through a concurrent or counter-current gas stream (Sheehan *et al*., 2005). Wet feed is introduced into the upper end of the dryer and the dried product withdrawn at the lower end.

The performance of rotary dryers is dictated by three important transport phenomena, namely: solids transportation (Lisboa *et al*., 2007, Cao and Langrish, 1999; Renaud *et al*., 2000; Shahhosseini *et al*., 2000; Song *et al*., 2003; Britton *et al*., 2006), heat, and mass transfer (Arruda *et al*., 2009a; Lobato *et al*., 2008). The ability to estimate each of these transport mechanisms is essential for proper design and operation of rotary dryers (Krokida *et al*., 2002).

The movement of particles in rotating drums depends on the flights and shell design, as well as on the operating conditions. Thus, rotary dryers represent one of the greatest challenges in theoretical modelling of dryers (Sherrit *et al*., 1993). The complex combination of particles being lifted by the flights, sliding and rolling, then falling in spreading cascades through an air stream and re-entering the bed at the bottom, possibly with bouncing and rolling, is very difficult to analyze (Kemp, 2004).

The literature presents some drying models for conventional rotary dryers based on the application of mass and energy balance equations for both solid and fluid phases (Kemp and Oakley, 1997; Cao and Langrish, 2000; Zabaniotou, 2000; Iguaz *et al*., 2003; Xu and Pang, 2008; Arruda *et al*., 2009b). This approach requires constitutive equations for the heat transfer coefficients, drying kinetics, equilibrium moisture content and fluid dynamic characteristics.

Arruda (2008) developed a general model for the drying process in a conventional rotary dryer that could be applied to any type of particulate material. This author found good agreement of the simulated results from this model with experimental data for fertilizer drying. However, Fernandes *et al*. (2009) comment that the deviations of this model simulation from their experimental data for an industrial dryer could be explained by the imprecision of the parameters of the constitutive equations. Actually, the model proposed by Arruda (2008) is quite general and the parameters of the constitutive equations were obtained from specific studies, such as a thin layer dryer for the drying kinetics equation and a static method for equilibrium moisture content. Thus, this approach had no adjustable parameters, allowing a realistic analysis of the prediction from the model. Therefore, is very important to analyze the sensitivity of the responses of the model to the variation of the parameters in the main constitutive equations to identify possible weaknesses in the model prediction and thus improve the model. Thus, the purpose of this work was to analyze the influence of the following parameters: overall volumetric heat transfer coefficient, coefficient of heat loss, drying rate, specific heat of the solid and specific heat of dry air on the prediction model proposed by Arruda (2008). The method of parametric sensitivity using experimental design was employed in this study. The results of the simulation are compared with experimental data for granulated single superphosphate (SSPG) obtained from a rotary dryer in a pilot scale unit.

**MATHEMATICAL MODELLING**

**Simultaneous Transfer of Mass and Energy in Rotary Dryers**

Modelling of the drying process in moving bed dryers is based on applying the equations of conservation of mass and energy to the fluid and particulate phases in infinitesimal volume elements of the dryer (Barrozo *et al*., 2001). Figure 2 shows the scheme of the infinitesimal volume element of a conventional rotary dryer operating in countercurrent flow (Arruda, 2008). The modelling approach considers the fluid dynamic characteristics of the dryer, as well as the intrinsic properties of the material, equilibrium moisture and drying kinetics.

In the formulation of this model, the following assumptions were made:

The particle axial velocity through the drum is constant (v_{s} = L/);

The drying rate is evaluated in each infinitesimal volume element volume of the dryer;

Grain shape and physicochemical properties of solid and fluid phases (Cp_{s}, Cp_{l}, Cp_{v}, Cp_{f} and λ) do not change during drying;

The initial conditions of solid feeding flow, temperature, and solid and air moisture are constant and known.

The equation system from the balances of mass and energy between drying gas and particulate material is presented next, where z is the dimensionless length, given by the proportion between a given position (x) and the total length of the dryer (L).

The system of differential equations of the model should be resolved simultaneously for the four variables involved, considering the contour conditions that follow: W(L)=W_{0} ; M(0)=M_{0} ; T_{f} (L)=T_{f0} ; T_{S}(0)=T_{S0}.

Drying in conventional cascading rotary dryers occurs mostly during the time in which the particles are falling from the flights, when they are in contact with the dry air, which corresponds to only a fraction of the residence time (Baker, 1983). As proposed by Arruda (2008), this fraction refers to the effective contact time between the solid and dry air (f_{tef}) and can be evaluated by the relation between the average falling time of the particle and total time of a cycle. This, in turn, corresponds to the time spent from material collection by the flight until its return to the particle bed on the bottom of the drum. This fraction can be evaluated by Equation (5), where the total number of cycles (N_{Ci}) is given by Equation (6) and the effective contact time between the gas and the particles (t_{ef}), by Equation (7). The total solids load in the dryer (H^{*}) is given by Equation (8).

For the conventional rotary dyer, the effective contact time between the gas and the particles (t_{ef}) substitutes the time t in the computation of the drying rate.

**Constitutive Equations**

**Equilibrium Moisture**

Based on experimental data of equilibrium moisture content of simple superphosphate fertilizer, Arruda (2008) performed a statistical study of discriminating rival models and concluded that the modified Halsey correlation (Ribeiro *et al*., 2005) best adjusted his experimental data. The modified Halsey equation with the parameters estimated by Arruda (2008) for superphosphate fertilizer is presented next.

**Drying Kinetics**

Arruda (2008) performed an experimental study in a thin layer dryer (Barrozo *et al*., 2006), and concluded that the best correlation to represent the drying kinetics of the fertilizer was Page's equation (1949). This equation, with the parameters estimated by Arruda (2008) for simple superphosphate, is presented subsequently:

where Z is equivalent to the time of drying.

Thus, the drying rate can be calculated by Equation (11).

**Heat Transfer Coefficients**

The best correlations for the overall volumetric heat transfer coefficient (U_{va}) and for the heat lost through the wall coefficient (U_{P}) were also determined by Arruda (2008). These equations with the parameters estimated in this previous work are:

**SENSITIVITY ANALYSIS USING EXPERIMENTAL DESIGN**

The values of the parameters for the simulations in this sensitivity analysis study were established using an orthogonal central composite design (Box *et al*., 1978), which involved a total of 46 simulations for each operating condition shown in Table 1.

The parameters studied here were: drying rate (R_{w}), overall volumetric heat transfer coefficient (U_{va}), coefficient of heat loss (U_{p}), specific heat of the solid (Cp_{s}) and specific heat of dry air (Cp_{f}). Solid moisture content (M) and solid temperature (T_{s}) were used as response variables. Equations (14) to (18) present the dimensionless form of these parameters and Table 2 shows the levels of the parameters applied in this work. R_{w}, U_{va} and U_{p} at different levels in Table 2 were obtained by multiplying Equations (11) to (13), respectively, by a factor.

where x_{1}, x_{2}, x_{3}, x_{4} and x_{5 }are the dimensionless forms of the R_{w, }U_{va}, U_{p}, Cp_{s,} and Cp_{f} parameters, respectively.

The levels -1 and +1 of each parameter were chosen so that the difference between the extreme values of the interval (-α and α) and the central level did not exceed 10% of the parameter's original value. The value of α (extreme dimensionless level) of the experimental design was 1.784. This value leads to an orthogonal central composite design, i.e., a design in which the variance and covariance matrices are diagonals, and the parameters are uncorrelated.

**RESULTS AND DISCUSSION**

Figure 3 show the results of the comparisons between experimental data (Arruda 2008) for the solids moisture content, obtained at the end of the dryer (z=1), and those computed by the model with the parameters in the central levels of Table 2. The experimental data were obtained by Arruda (2008) with a conventional rotary dryer equipped with three-segmented angular flights. The flights had the dimensions: first segment = 0.02 m, second and third segment = 0.007 m; the length of the flights was 1.5 m, with an angle of 135º between segments. The operating conditions of the experiments performed by Arruda (2008) are presented in Table 3.

A good agreement between the simulated values of solids moisture content and those obtained experimentally in the rotary cascading dryer can be observed in the results presented in Figure 3. The average deviation of the simulation results in relation to the experimental data was 7.7 %. These deviations were probably caused by measurement imprecision and/or inaccuracy of the model parameters.

The resolution of the differential equation system (Equations (1) to (4)) was obtained by the technique of normal collocation with 10 placement points for the 4^{th} order polynomial approximation, using the sub-routine "bvp4c" of MATLAB^{®} software. The relative tolerance used was 10^{-6}. The simulated results (values of response variables at the end of the countercurrent rotary dryer, i.e., for the solid at z = 1) were analyzed statistically using STATISTICA^{®} software, with each of the responses subjected to an analysis of variance. The parameters whose level of significance exceeded 5% were neglected (in a hypothesis test using Student's distribution) and the respective parameters were considered irrelevant.

Equations (19) and (20) represent the matrix forms of the equations fitted for the solid moisture content (M) and solid temperature (T_{s}) in condition 2, respectively, as functions of the dimensionless parameters (overall volumetric heat transfer coefficient: x_{1}; coefficient of heat loss: x_{2}; drying rate: x_{3}; specific heat of solid: x_{4}; and specific heat of dry air: x_{5}). In the equations, the interactions and quadratic effects (r = 0.999) are present, beyond the main effects. It was observed that the highest values of the coefficients of the main effects in Equations (19) and (20) were for the parameters drying rate (x_{3}) and overall volumetric heat transfer coefficient (x_{1}). These results demonstrate that both U_{va} and R_{w} are the most important parameters to be considered in the model. Moreover, all coefficients were retained in Equation (19), because all parameters were significant for the solid moisture content, i.e., the levels of significance did not exceed 5% as shown in Table 4. In Equation (20), the coefficients of the quadratic term (x_{2}^{2}) and interaction terms (x_{2}x_{4} and x_{4}x_{5}) were equal to zero because these coefficients were irrelevant for the solid temperature, i.e., the levels of significance exceeded 5% (see Table 5).

where:

where:

Response surfaces were generated from Equations (19) and (20) for the solid moisture content (M) and the solid temperature (T_{s}) as functions of the most important parameters (Figures 4 and 5, respectively). Even though most of the quadratic and interaction coefficients are significant, the response surfaces look rather flat, because the quadratic and interaction coefficients are orders of magnitude smaller than the linear coefficients.

As expected, the lowest values of solid moisture content (M) were achieved for the highest values of drying rate (R_{w} or x_{3}) and overall volumetric heat transfer coefficient (U_{va} or x_{1}). Lower values of solid temperature (T_{s}) were achieved for higher values of drying rate and lower values of overall volumetric heat transfer coefficient. However, from these results it is possible to quantify the effects of these important drying parameters and their respective sensitivities on the drying responses.

Additional simulations with perturbations of ± 20% in the values of the parameters (U_{va}, U_{p}, R_{w}, Cp_{s}, Cp_{f}) were performed. The impact (in percentage) of the perturbations (± 10% and ± 20%) in solid temperature (T_{s}) at the end of the dryer are shown in Table 6 for the three operating conditions presented in Table 1. In general, it is observed that the variations of solid temperature (T_{s}) were up to -10.5%, i. e., values greater than the experimental uncertainty. Again, the parameters that affected the solid temperature (T_{s}) the most were the drying rate (R_{w}) and the overall volumetric heat transfer coefficient (U_{va}).

Figures 6 and 7 show the solid moisture content (M) profiles as a function of the dimensionless length of the dryer (z) for several values of the overall volumetric heat transfer coefficient (U_{va}) and drying rate (R_{w}). Figures 5 and 7 show that the drying rate (R_{w}) has a much greater influence on solid moisture content (M) than the overall volumetric heat transfer coefficient (U_{va}). Figures 8 e 9 show the solid temperature (T_{s}) profiles as a function of the dimensionless length of the dryer (z) for several values of the overall volumetric heat transfer coefficient (U_{va}) and drying rate (R_{w}). It was observed again the great influence of both R_{w} and U_{va} on the solid temperature (T_{s}).

The results of this study showed that the high sensitivity of the drying rate indicates a need to be careful in the choice of the equation to represent the drying kinetics and in the reliability of its parameters. Likewise, the choice and accuracy of the parameters of the equation for the overall heat transfer coefficient are of fundamental importance.

**CONCLUSIONS**

The method of parametric sensitivity using experimental design was employed to analyze the influence of the following parameters: overall volumetric heat transfer coefficient (U_{va}), coefficient of heat loss (U_{p}), drying rate (R_{w}), specific heat of the solid (Cp_{s}) and specific heat of dry air (Cp_{f}) on the prediction of the model proposed by Arruda (2008) for fertilizer drying in rotary dryers. All variables studied significantly affected the model, although some of the parameters are very small (e.g., second order parameters) compared with the linear effect of each variable.

The statistical results indicated that the drying rate (R_{w}) and the overall volumetric heat transfer coefficient (U_{va}) are the parameters that most strongly influence the solid moisture content (M) and solid temperature (T_{s}). The sensitivities of these parameters were quantified. Thus, the choices of the equation to represent the drying kinetics and the overall heat transfer coefficient, as well as the reliability of their parameters are fundamental to improving the model prediction.

A good agreement was found between the simulated values of solids moisture content and those obtained experimentally by Arruda (2008) in the rotary cascading dryer.

**ACKNOWLEDGEMENT**

The authors thank FAPEMIG and CNPq for financial support.

**NOMENCLATURE**

Cp | specific heat | J kg |

D | dryer diameter | m |

f | effective time factor | (-) |

g | mass velocity | kg/sm |

G | mass flow rate | kg/s |

H* | dryer total load | kg |

L | dryer length | m |

M | solid moisture content | kg |

MR | dimensionless moisture | (-) |

N | total number of cycles | (-) |

RH | air relative humidity | (-) |

R | drying rate | s |

T | temperature | oC |

U | overall volumetric heat transfer coefficient | kWm |

U | heat loss coefficient | kWm |

s | velocity | m s |

W | air absolute humidity | kg |

x | position along the dryer | [m] |

| average fall height | m |

z | = x /L, dimensionless length | (-) |

*Greek Letters*

α | dryer inclination | (º) |

average residence time | s | |

λ | latent heat of pure water vaporization | kJ kg-1 |

*Subscripts*

amb | Environment |

ef | effective |

eq | equilibrium |

f | fluid |

l | liquid |

s | solid |

v | vapor |

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(Submitted: August 22, 2011 ; Revised: September 18, 2011 ; Accepted: December 22, 2011)

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