Analysis of oxygen permeation through dense ceramic membranes with chemical reactions of finite rate
Introduction
Dense fast ion-conducting ceramic membranes are of considerable interest for academia and industry (Kilner, 2000; Lin, 2001). Those are applied extensively as a tunable oxygen separation media in electrocatalytic and membrane reactors either for power generation or conversion of light hydrocarbons to value-added products. Particularly, the mixed ionic and electronic conducting perovskite structured lanthanum membranes (Balachandran et al., 1995; ten Elshof et al., 1995a; Tsai et al., 1997; Xu and Thomson, 1998; Zeng et al., 1998), and fluorite (Fagg et al., 2007) or fluorite-like (Horovistiz et al., 2007) structured ceramic membranes have been investigated most extensively in the past decade. However, inconsistent oxygen permeation fluxes, with difference as large as one order of magnitude, were reported frequently even for a nominally identical membrane material. Teraoka et al. (1985) reported an oxygen permeation flux as high as 2.31×10−6 mol cm−2 s−1 at 850 °C for a SrCo0.8Fe0.2O3−δ membrane; while the data for the same membrane with a same thickness measured under similar experimental conditions from Kruidhof et al. (1993) and Qiu et al. (1995) were 1.8×10–7 and 6.3×10−7 mol cm−2 s−1, respectively. Conflicting results were also reported concerning the effect of A-site substitution in the perovskite by different cations. Teraoka et al. (1988) and Tsai et al. (1998) showed that the oxygen permeation fluxes of A-site substituted LaCo1−yFeyO3−δ membrane had an order Ba>Ca>Sr, however, Stevenson et al. (1996) and Li et al. (1999) reported a different order Sr>Ba>Ca.
Several research groups have noticed and tried to explain the discrepancies. Differences in experimental details, such as the gas atmosphere which modifies the membrane surface (Yi et al., 2005; Arnold et al., 2007), the sealing material (Qiu et al., 1995) and the difference in preparation procedure (Kharton et al., 2001; Qi et al., 2000; Wu et al., 2006; Zhang et al., 1999) have been suggested to account for such discrepancies. Yi et al. (2005) found that the co-presence of CO2 and H2O in air had profound effects on the phase composition, microstructure, and oxygen permeability of a Sr0.95Co0.8Fe0.2O3−δ membrane, and attributed these effects to the formation of bicarbonate on the membrane surface. Wu et al. (2006) examined the effect of pH during synthesis via a citrate process on the properties of the resulting perovskite membrane and reported that the crystallinity and the oxygen permeability of the La0.6Sr0.4Co0.4Fe0.6O3−δ membrane can be tailored. Qi et al. (2000) investigated the electrical conductivity and the oxygen permeability of a La0.8Sr0.2Co0.6Fe0.4O3−δ membrane prepared from powders synthesized by four different techniques, i.e. the citrate, solid state, spray-pyrolysis and coprecipitation methods. They found that a substantial deviation from the desired stoichiometry existed for the membranes prepared by different methods and proposed that this deviation was the major reason for the discrepancies in the reported oxygen permeability data for the membranes with similar composition.
Akin and Lin (2004) recently analyzed the effect of downstream conditions on oxygen permeation flux through ionic and mixed-conducting ceramic membranes by a simple mathematical model for special cases with extremely slow and fast reaction rate. They reported that the downstream gas reactivity with oxygen and flow rate and pattern can have a strong effect on oxygen permeation flux through these membranes. This work not only examined the effects of the operating conditions on oxygen permeation flux but also provided the direction to study oxygen permeation through this group of membranes under more realistic reaction conditions with a finite reaction rate. Such a study is very important to explain the discrepancy in oxygen permeation flux data and development of ionic or mixed-conducting ceramic membrane reactors for partial oxidative reactions. The present paper reports the study of oxygen permeation through this group of membranes with a reaction of finite rate in the membrane downstream by a much improved mathematical model considering oxygen permeation, reactor configuration and reaction kinetics.
Section snippets
Model development
In membrane reactors, an ionic or mixed-conducting ceramic membrane separates an oxygen containing upstream (typically air) and a downstream containing a reactant, such as methane, with or without an inert carrier gas, as schematically illustrated in Fig. 1.The reactant in the downstream reacts with oxygen permeating through the membrane from the upstream. The driving force for oxygen permeation is the Gibbs energy for the reaction but is often stated in the literature as the difference between
Results and discussion
The reaction side oxygen partial pressure is dependent on the constants chosen in Eq. (1). Here, we use the parameters for Bi1.5Y0.3Sm0.2O3−δ (BYS) to represent a p-type membrane and those for La0.6Sr0.4Co0.2Fe0.8O3−δ (LSCF) to represent an n-type membrane, as listed in Table 1. It should be noted that the use of term “n- or p-membrane” is to indicate membrane materials whose oxygen permeation flux equations can be described by either Eq. (2) or Eq. (3). It does not necessarily mean the
Conclusions
An oxygen permeation membrane reactor model taking into account of the different transport mechanisms, i.e. with p-type and n-type flux equations was developed to analyze the oxygen permeation through an oxygen ionic or mixed-conducting ceramic membrane under reaction conditions. The simulation results show that the oxygen partial pressure in the reaction side decreases with the increase in the reaction rate for both the p-type and n-type membranes. As a consequence, for both the two kinds of
Notation
A effective oxygen permeation area, cm2 F Faraday constant, C mol−1 dimensionless oxygen permeation parameter, , oxygen permeation rate, mol cm−2 min−1 k1, n1, constant k2, n2, kCO kinetic parameter, mol min−1 ml−1 atm−1.5 dimensionless kinetic parameter, L membrane thickness, cm p oxygen partial pressure ratio between the reaction side and air side, P pressure, atm oxygen partial pressure at the air side, atm
Acknowledgments
This work has been supported by the Natural Science Foundation of China under Contract numbers 20425619 and 20736007. The work has been also supported by the Program of Introducing Talents to the University Disciplines under File number B06006, and the Program for Changjiang Scholars and Innovative Research Teams in Universities under File number IRT 0641.
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