Simple Models for Diffusion in Thin Plates or Membranes

Two simplified models, linear and nonlinear, were used in a cementation process on a homogeneous thin carbon steel plate. The parameters for these models, as obtained by the least squares’ method the first one in a global way while the other parameters refer to the second model—were estimated by a set of local minimums. To compare the performance of these models we used theoretical data, for the same diffusion problem obtained by a one-dimensional transient model considering the concentrations in the mean plane of the plate. The results for carbon concentrations in weight percentage in the plate (%pC) as a time-only dependent function with these simplified models to represent the analyzed diffusion process were in good agreement with those from a stricter model. The diffusion flows of these models were determined and a reasonable agreement can be seen in relation to the flow obtained by the theoretical model on the surface of the plate. This study shows that it is possible to use this methodology with the given restrictions adopted here to describe the concentration and the diffusion flow of other solutes in thin membranes.


Introduction
The one-dimensional diffusion in a medium is limited by two parallel planes, for example, in 0 x = and x L = of such thin thickness, so that the entire diffusive process occurs through these sheets or membranes, while only a negligible amount occurs through the lateral faces, which is well known [1] [2]. In particular, if on the face 0 x = the concentration of the diffusing substance is constant and equal to 1 C and on the other x L = it is a constant 2 C , and if the initial  ∂ ∂ [2] using, for example, the method of separating variables or through the Laplace Transform [3]. The solution of this problem via the separation of variables involves an infinite series of sine terms combined with an exponential function with a negative factor in each term of the series, which albeit complicated, quickly converges, except for small values of [4]. The solution obtained by the Laplace Transform lies in the calculation of the ( ) erf x function or Gauss error function, whose values are given in tables for different values of 2 x Dt . In general, diffusion is three-dimensional process, but sometimes the problem is simplified using a smaller number of dimensions. According to Fox et al. [5], for many problems found in engineering, a one-dimensional analysis is adequate to provide approximate solutions with the precision required in engineering practice. Recently, Araújo e Márquez [6] used transient one-dimensional diffusion in a cementing process of a homogeneous metal sample of carbon steel with a thickness of less than two millimeters to obtain information on carbon concentration in a semi-infinite plate where the Gauss error function was replaced by a fifth-degree polynomial.
The cementation process consists of the hardening of the surface of steel to higher levels to that of its interior by the diffusion or transport of carbon atoms at high temperatures in an atmosphere rich in hydrocarbon gas such as CH 4 methane gas [7]. The question we pose in this article is whether there is a simpler model that can be adopted to estimate the concentration of carbon in diffusion in thin plates or membranes. Although recognizing that the process of diffusion of materials through cell membranes is quite complicated, Bassanezi and Ferreira Jr. [8] and Bassanezi [9] presented two diffusion models through cell membranes based on a simplification of Fick's Law [7]. These diffusion models are applied when the concentration difference between the cell medium and the homogeneous liquid medium where the cell is immersed is small and the cell has the area and volume constant throughout the process. For this, it is also assumed in a natural way that the flow of molecules goes in both directions until the concentration inside the cell is equal to the concentration of the medium it is suspended in. The first model is represented by the linear ordinary differential equation given by where C e is the concentration of the medium surrounding the membrane, and k is a membrane permeability constant, A is the surface area, V is the constant volume of the cell, while C(t) it is the concentration of the diffusing solute in the cell in t time. The k constant depends on each solution, the thickness and the Journal of Applied Mathematics and Physics structure of the membrane, so it needs to be estimated for each situation. The second model, also simplified, but with two parameters, is given by an ordinary non-linear differential equation as The term in square brackets is the function for solute flowing into the cell [8].
According to Bassanezi and Ferreira Jr. [8], the experimental obtaining of the constant can be difficult and sometimes impossible to obtain, in which case the two-parameter model can be useful for the theoretical analysis of the problem understudy, but not for the specific study. Although agreeing that the experimental achievement of these parameters is not trivial, their estimates are possible in our understanding, provided that experimental data ( ) ( )

Materials and Methods
Consider a homogeneous metal plate formed by an Iron-gamma Carbon alloy, indicated by, Fe γ -C which hast to be hardened through a process of cementation [7]. The steel part is exposed in an atmosphere rich in hydrocarbon gas (such as methane gas, CH 4 ), under 1000 C T =  . The homogeneous plate with the properties shown in Table 1, has an uniform concentration of carbon The carbon concentration is kept constant and equal ( ) to the flat face 0 x = , and also constant and equal ( ) to the flat face 0.001 m x L = = with 0 t ≥ . Under these conditions, the goal is to obtain theoretical data on the process at different moments in time, in hours for the mean plane of the plate, that is, in 0.0005 m x = . Figure 1 shows in simplified form the metal plate subjected to the conditions given in the cementation process described above.
The thickness is so small that it will be assumed that the entire diffusion process happens through these sheets or membranes, while a negligible amount Journal of Applied Mathematics and Physics    Table 1 shows the parameters for the carburizing process, notation and assumed values, and the initial conditions of the diffusion process.

Linear Least Squares: Discrete Case
Given a set of points As the i λ coefficients appear linearly in the definition of the ( ) x ϕ approximation function, this model is called linear [10]. The choice of ( ) The equations obtained from Equation (5) give rise to a linear system of n n × order given by where, according to Ruggiero e Lopes [10] matrix entries can be obtained by unique way of Equation (6).

Nonlinear Least Squares: Discrete Case
is not a linear model of the parameters as in Equation (3), the equation of the critical points no longer produces a linear system as obtained in Equ- Therefore, as ( ) R λ is a vector function for residues in the m R space and is a vector of adjustable parameters of the n IR space. With this notation, the k-th residue of this approximation is defined by (4), that is, the Equation (5) Using a Taylor series expansion [11] to the first order for each where ( ) ( ) ( ) 1 , , The Jacobian matrix of the ( ) From Equations ( (10), (11)) we have a linear system of n n × order given by Equation (12) is the basis for an iterative process and is known as a modified Newton method [12]. Taking

The One-Dimensional Diffusion Equation
The solution of the transient one-dimensional diffusion equation for the diffusion problem in thin membranes with constant surface concentrations and initial distribution with uniform concentration, that is, can be obtained by the method of separation of variables, whose solution is given

Results and Discussions
Model 1 as given and reported by Equation (1) is given by as proposed by Bassanezi [9] and based on Fick's Law for the diffusion of materials through permeable membranes [4]. In Equation (15), the permeability constant of the membrane can be given, for example, in m/s and where ( ) From Equation (16) results the ( ) C t expression for given by where ( ) In Equation (15), an analogy with Fick's first law for one-dimensional diffusion in a steady state [7], making it possible to interpret the term  as the amount of mass that crosses the membrane per unit area, in a given direction per unit of time. Model 2, as proposed by Bassanezi and Ferreira [8] and already mentioned in the introduction (Equation (2)) is given formally by or, From Equation (15) we have seen that  represents a flow of molecules into the cell, then replacing that term with the given ( ) f C flow function as in Equation (18), we obtain the two-parameter formulation for cell diffusion only reported by Bassanezi and Ferreira Jr. [8] to obtain Equations (2) or (18), (24) Using the fact that  (17) and (24) we will use the theoretical data obtained from the cementation process, whose parameters are shown in Table 1 obtained by means of Equation (12), that is, the one-dimensional transient diffusion model (MD) or as we will call theoretical model.  In applying the Neperian Logarithm to Equation (26) we obtain Thus, using the discrete points in Table 2 we can write (1) as, ( ) Thus, the matrix of the system given by Equation (4) is of an order of 1 1 × , that is, As a result, kA V λ = − and A, V are given as shown in Table 1, Similarly, for MD21, MD21 6.2% ε < while for the MD22 model, MD22 6.5% ε < .
The highest divergence between concentrations took place in the 2.0 h t ≤ time interval. Based on the criteria analyzed, and because the MD1 model has its parameter estimated in a global way, and due to its greater simplicity, it is at first the model to be adopted to estimate the mean carbon concentration in the thin plate. Figure 2 shows the adjustment in the half-plane estimated in %pC obtained with the different adjustment models analyzed. One of the advantages of these simplified models is that their expressions for ( ) C t are analytical, as opposed to the solution obtained by Equation (14) which is given in terms of an infinite series. Figure 2 shows a little more, that is, on the more superficial layers it is expected that models MD21 and MD22 are closer to the estimates of theoretical concentrations, as a greater spread is seen above the continuous graph obtained by the MD model for the mean plate plane.
If we consider the 0.00025 m x = plane of the plate, the maximum percentage The flow functions from simple models are dependent on the difference in concentration between the media, so it is to be expected that the 2 J flow will be less pronounced than the 1 J flow. to the same terms of the MD1 model, indicating that the diffusion for models MD21 and MD22 is "less apparent" in relation to the 1 J model. Figure 3 shows the carbon diffusion profile diffusion on the flat faces of the plate, confirming this observation.
After two hours of the cementation process, the carbon transfer rates through the flat section on the surface of the plate were in good agreement when compared with the data provided by the theoretical model. A possible explanation for the discrepancy of flows estimated by the simplified models for times under two hours can be credited to the fact that the parameters estimated for the models were based on the data of the theoretical concentrations obtained for the mean plane, and not the surface plane where the concentration was kept fixed during the cementation process.

Conclusion
The analyzes showed that the simplified diffusion models in cell membranes analyzed in this study may be an alternative to the transient one-dimensional models used for the description of membrane diffusion processes. The simplest models depend on parameters that can be obtained globally using known function adjustment methods, such as that of the least squares. In particular, they were used to obtain percentages by weight of carbon in a cementation process with restricted thickness conditions. The results obtained were in good agreement when compared with the estimates of the theoretical model used for this purpose. The simplified model with one parameter was shown to be the best option to represent the average estimate of the concentration of carbon solute in the diffusion process due to the concentration difference on the plate or membrane, and this is due to the fact that this model uses only one parameter and that it can be obtained non-iteratively; that is, in a global way.