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## Journal of the Brazilian Society of Mechanical Sciences

*versión impresa* ISSN 0100-7386

### J. Braz. Soc. Mech. Sci. v.24 n.4 Rio de Janeiro nov. 2002

#### http://dx.doi.org/10.1590/S0100-73862002000400003

**On-site calibration of a phase fraction meter by an inverse technique**

**V. P. Rolnik ^{I}; P. Seleghim Jr.^{II}**

^{I}vanessa@sc.usp.br

^{II}Núcleo de Engenharia Térmica e Fluidos Departamento de Engenharia Mecânica Escola de Engenharia de São Carlos - USP Av. Dr. Carlos Botelho, 1465 13566-590 São Carlos, SP. Brazil seleghim@sc.usp.br

**ABSTRACT**

The formal calibration procedure of a phase fraction meter is based on registering the outputs resulting from imposed phase fractions at known flow regimes. This can be straightforwardly done in laboratory conditions, but is rarely the case in industrial conditions, and particularly for on-site applications. Thus, there is a clear need for less restrictive calibration methods regarding to the prior knowledge of the complete set of inlet conditions. A new procedure is proposed in this work for the on-site construction of the calibration curve from total flown mass values of the homogeneous dispersed phase. The solution is obtained by minimizing a convenient error functional, assembled with data from redundant tests to handle the intrinsic ill-conditioned nature of the problem. Numerical simulations performed for increasing error levels demonstrate that acceptable calibration curves can be reconstructed, even from total mass measured within a precision of up to 2%. Consequently, the method can readily be applied, especially in on-site calibration problems in which classical procedures fail due to the impossibility of having a strict control of all the input/output parameters.

**Keywords: **Multiphase flow, phase fraction meter, calibration, inverse problem

**Introduction**

The continuous measurement of physical parameters in multiphase flows is of great interest, not only for the monitoring and control of industrial equipment, but also to obtain phenomenological insight in research applications. In particular, the development of phase fraction sensors is a subject very frequently found in the related scientific literature, considering that this parameter is one of the most adequate when describing and analyzing two-phase flows.

A good illustration of this is the determination of composition and flow rates in the petroleum industry (Fischer, 1994). In the absence of an acceptable on-line measurement device, the most common procedure is to adopt a strategy based on the continuous separation of the fluid constituents and subsequent measurement by conventional single-phase techniques followed by recombination. Despite the extensive number of applications based on this approach, its efficiency and economic feasibility are not satisfactory. The large size of conventional separation equipment, such as hydro-cyclones and other centrifugal separators, is frequently restrictive and even prohibitive in offshore production systems for instance. In addition to this, in some situations, special thermal or chemical methods are required to deal with emulsion formation. Also, the flashing of dissolved gases from the liquid phase requires a more elaborate temperature and pressure control system implying in more complex operation conditions (Rajan *et al.*, 1993). Thus, the development of simple, robust and inexpensive non-intrusive multiphase flow sensors suited for industrial applications is still an open problem.

In this context, and regarding the measurement of spatially averaged phase fractions, electrical sensing techniques are particularly attractive due to its capability of resolving fast changes in the flow structure, besides being simple to implement and not expensive as well. Its general principle of operation is based on differences or contrasts in the electrical properties of the phases of the mixture, and also on the assumption that the electromagnetic sensing field is instantaneously modulated by the flow (Chang and Watson, 1994). In general, problems associated with electrical sensing are related to electrochemical effects (Hemp, 1994), electrostatic stray charges (Green and Thorn, 1998), nonlinearly due to the influence of flow regimes (Andreusi *et al., *1988), and electrode erosion or coating. One way of overcoming these problems is to design the sensor and the sensing strategy specifically for the desired application, therefore the need for on-site calibration methods (Duncan and Trabold, 1997).

The formal calibration procedure of a measurement device is based on the construction of the output/input relation by imposing known inputs and registering the corresponding outputs. In the case of a phase fraction probe this is not sufficient because, in addition to being correlated to the phase fraction, the probe's response will be also strongly correlated to the flow regime. In other words, the same phase fraction may result in different responses depending on the topological organization of the constituent phases within the sensing volume (see for instance the work of Andreussi *et al.*, 1988). Attempts have been made aiming to minimize the influence of the flow regime, mostly relied on the optimization of the electrodes (Seleghim and Hervieu, 1998) or on the sensing strategy (Klug and Mayinger, 1994). A very promising approach is based on fuzzy and neural signal processing techniques and is implemented so to previously identify the flow regime and subsequently take the correct calibration curve (Tsoukalas *et al.* 1997; Mi *et al.* 1998; Crivelaro and Seleghim, 1999).

Thus, in a strict sense, the calibration of a phase fraction meter requires the ability to impose known phase fractions at known flow regimes, which can be straightforwardly done in laboratory conditions. In industrial conditions this is rarely the case. For instance, if it is necessary to calibrate a fraction meter placed on a pneumatic conveying line, the control of the flow conditions would require the addition of auxiliary equipment that would produce significant disturbances in the operating conditions and, consequently, compromising the final result. Still, the majority of industrial scale pneumatic conveyors are designed to operate at nonpermanent flow conditions, which may take the form of discrete structures such as solid plugs and rolling dunes, or alternating flow regimes associated with varying inlet mass flow rates. This justifies the need for less restrictive calibration methods, in particular with regard to the prior knowledge of the complete set of inlet conditions.

The purpose of this paper is to contribute in this direction by proposing a new inverse procedure for the on-site construction of the calibration curve of a phase fraction meter from less restrictive data, i.e. not the instantaneous flow rate signal but its integral value. The problem will be precisely stated in section 2 and a numerical simulation will be presented in section 3 (in which the consequences and a solution for the problems associated with the inverse nature of the formulation will be shown). A final conclusion and the references are presented respectively in section 4 and 5.

**Nomenclature**

a = volumetric solid fraction

= solids (particulate) mass flow rate

Q_{s} = solids volumetric flow rate

r _{s} = solids density

C = inter-electrode capacitance

M_{s} = total solids mass

f (·) = calibration curve to be reconstructed

a_{i} = expansion coefficients of f ( · )

e = error functional

**Statement of the Problem**

Consider the homogeneous flow of a two-phase mixture trough a capacitive fraction meter installed on a light phase pneumatic transport system (Fig. 1). The volumetric solid fraction (a ) is defined as the ratio between the volumes occupied by the solids (V_{s}) and the total sensing volume (V_{s}+V_{a}), which, according to the one-dimensional one-velocity model (Bergels *et al.*, 1981), can be written as

in which the volumetric flow rates (Q_{s} and Q_{a}), solid density r _{s} and mass flow rate is defined in Fig. 1.

The capacitance (C) measured between the sensing electrodes depends on how the electrical field traverses the sensing volume, which is related to the permittivity of the medium and also to the geometric organization of the different phases. Thus, the capacitance is strongly correlated to the solid fraction and to the flow regime (homogeneous by assumption), and the formal relation between these variables, i.e.

is known as the meter's calibration curve as mentioned before. Substituting equation (2) into (1) and isolating the solid mass flow rate yields:

In an industrial pneumatic conveying system the instantaneous values of the air volumetric flow rate (the continuous phase) can be readily determined, for instance with an orifice plate or simply from the blower's performance curve by measuring its rotation and pressure rise. However, the measurement of the instantaneous values of the solid flow rate is quite complex without modifying the piping to install auxiliary equipment. In addition, the solid flow rate must be measured at the fraction meter's section since it can vary significantly along the transport line as well as in time (Ostrowski *et al.*, 1999). A more convenient variable to measure would be the total solid mass (M_{s}) conveyed in a given time interval:

This expression can be obtained from the integration of equation (3), with the additional assumption (for simplicity and without loss of generality) of a constant volumetric air flow rate. It will then result

To obtain the calibration curve a = f ( C ) it is necessary to solve the integral equation (5) on the input data M_{s}, r _{s}, Q_{a} and C = C( t ), the instantaneous capacitance values delivered by the fraction meter. Equation (5) can also be seen as a special case of an inhomogeneous Fredholm equation of the first kind, which is known to be ill conditioned. Consequently, as it will be shown on the sequel, if specific methods to deal with the ill-conditioned nature of the problem are not employed, the calibration curve will be extremely sensitive to small changes in the input parameters, which in fact are likely to happen due to intrinsic experimental errors. This is so because the integration of the unknown function in (5) causes an information loss. A proper method to deal with this must, in some way, restore the lost information from some prior knowledge or from redundant measurements.

**Numerical Simulation and Ma-Naging the Ill-Conditioned Nature of the Inverse Problem**

In order to demonstrate the statements above consider the following numerical simulations. First, suppose that the calibration curve is given by the following representative formula (taken from previous laboratory experiment – Hervieu, 1999):

This equation is not known a priori and will have to be reconstructed from experimental data. Suppose now that, due to a specific operating condition, the instantaneous measured solids fraction values follow the equation

This being, the substitution of (7) into (6) yields the instantaneous capacitance values delivered by the probe:

The resulting instantaneous solids mass flow rate for homogeneous flow can be determined by introducing (7) into expression (3), which yields

The following figure illustrates the behavior of these curves for r _{s} = 3000 kg/m^{3} and Q_{a} = 0.01 m^{3}/s

The inverse problem, such as formulated above, consists in reconstructing the calibration curve (2) (which was imposed to follow (6)) from measurements of the total mass M_{s} and the instantaneous capacitance values (8). To do this we can start by expressing (2) according to

where {j _{i}( a )} is a convenient set of known functions. Subsequently, substituting (8) into (10) and the result in (5) we obtain

The difference between both sides of the expression above constitutes an error functional expressing how well is the approximation given by (10). The influence of experimental errors in the measurements can be introduced, for instance, by randomly perturbing M_{s}. and C. We thus define:

where d and e ( t ) are centered random variables.

The reconstruction of the calibration curve can now be achieved by searching the minimum of equation (12).

The steepest descent method is employed in this work, with increments calculated from an arbitrated step Da, according to the rule expressed in equation (13). Consider d = e ( t )= 0 to illustrate the ill-posed nature of the problem. In this case, the minimum of (12) is associated with better-reconstructed curves as the order of the approximation in (10) is increased, as shown in Figure 4.

As it can be seen, the reconstruction works adequately under the assumption of no experimental errors. In a real situation however, these errors must be taken into account and, due to the inverse nature of the problem, this will produce an extremely negative affect. This can be illustrated by performing the same reconstruction as shown in Figure 4.b (third order approximation) and considering only a centered experimental error in the measurement of M_{s}, i.e. e ( t ) = 0 while d varies randomly between ± d _{max}. The following figure shows the influence of increasing values of d _{max} in the reconstructed calibration curve. Although neglecting the error in the measurement of the instantaneous capacitance values, even unrealistic experimental errors the order of d _{max} = 10^{-6} have a disastrous effect.

As mentioned before, this problem is probably triggered by the integration of the unknown function f ( C ) in (5) rendering the problem extremely ill conditioned. To deal with this there are some mathematical methods, mostly based on the construction of regularizing operators from a priori information. Another way of overcoming the problem, which in fact is more natural in the case we are dealing with, consists in reintroducing the lost information by redundant measurements.

Consider then a set of measurements of the total mass M_{s}^{(k)} and the corresponding capacitance historic C^{(k)}( t ), performed over different time intervals Dt^{(k)} (k = 1,2,... M). For the purposes of this numerical simulation, these data can be generated by randomly varying d and e ( t ), i.e.

in which

Within these definitions, the error associated with each measurement can be quantified by the following

and a global error function can be defined by calculating the Euclidean norm of {e^{(k)}}:

The problem can now be solved by searching for the minimum of (18) instead of (12). Figure 6 shows the results for increasing error in the measurement of the total mass (d _{max}) and time intervals varying randomly in between 10 and 30s and one can readily conclude that the admissible error have been significantly increased.

To illustrate how the ill-conditioned nature of the problem manifests itself at the formulation proposed here some numerical simulations were carried out with a reduced number of parameters. The graphic in Fig. 7 shows (18) with N = 2, i.e. E = E( a_{0}, a_{1} ), to allow visualization, and M = 100 (that is 100 evaluations of (17) with different values of d). It is possible to observe that there exists a pronounced minimum at the point (2.0, -1.0) which corresponds to the calibration curve.

Equation (19) corresponds to the projection of the actual calibration curve (6) onto the subspace of all possible linear calibration curves. It is also important to stress that the topology of the (18) have particular features which will induce severe difficulties regarding the convergence of the minimization procedure (a tradeoff between setting very small iteration steps and intense oscillatory behavior of the global error function).

**Conclusion**

The proposed solution to this is based on minimizing an error functional constructed from a set of redundant measurements, which restores the lost information associated to the integration of the instantaneous mass flow rate in the one-dimensional one-velocity flow model in equation (5). Numerical simulations performed for increasing errors demonstrate that acceptable calibration curves can be reconstructed, even from total mass measurements within a precision of up to 2%. Thus, the method can readily be applied, especially in on-site calibration problems in which classical procedures fail due to the impossibility of having a strict control of all the input/output parameters.

**Acknowledgements**

The authors would like to acknowledge the financial support provided by FAPESP through grants 98/12921-1 and 99/02821-2, and CNPq through the grant 520.723/97-0.

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Article received April, 2001

Technical Editor: Aristeu da Silveira Neto