# Hydraulic Performance Modifications of a Zeolite Membrane after an Alkaline Treatment: Contribution of Polar and Apolar Surface Tension Components

Authors: Patrick Dutournié; Ali Said; T. Jean Daou; Jacques Bikaï; Lionel Limousy
Journal: Advances in Materials Science and Engineering
 (2015)

---

## Abstract

Hydraulic permeability measurements are performed on low cut-off Na-mordenite (MOR-type zeolites) membranes after a mild alkaline treatment. A decrease of the hydraulic permeability is systematically observed. Contact angle measurements are carried out (with three polar liquids) on Na-mordenite films seeded onto alumina plates (flat membranes).  A decrease of the contact angles is observed after the alkaline treatment for the three liquids. According to the theory of Lifshitz-van der Waals interactions in condensated state, surface modifications are investigated and a variation of the polar component of the material surface tension is observed. After the alkaline treatment, the electron-donor contribution (mainly due to the two remaining lone electron pairs of the oxygen atoms present in the zeolite extra frameworks) decreases and an increase of the electron-receptor contribution is observed and quantified. The contribution of the polar component to the surface tension is attributed to the presence of surface defaults, which increase the surface hydrophilicity. The estimated modifications of the surface interaction energy between the solvent (water) and the Na-mordenite active layer are in good agreement with the decrease of the hydraulic permeability observed after a mild alkaline treatment.


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## Body

## 1. Introduction

Membrane processes are an interesting technology for the treatment or the separation of ionic and nonionic solutions. Many applications using membranes are commonly performed in industry as wastewater treatment [1], food-processing industry [2], or chemical and pharmaceutical operations [3, 4]. One of the challenges of these next years is to develop membranes with specific filtration properties (for ionic rectification [5]) able to have several functionalities or properties, as, for example, bactericidal properties [6]. For this, mineral membranes and specially zeolite ones are very interesting. Indeed, zeolitic membranes are selective in size and shape and display various relevant properties depending on the zeolite nature or chemical composition. Numerous previous studies have shown that changes in the Si/Al molar ratio and the internal or surface defects density have a significant effect on water interactions and transport with or within the zeolites [7–10].The scientific community agrees to say that separation performances are functions of pore size, surface electric charge, and dielectric effects. These last ones deal with the confinement, the nature of the solvent, the nature of the surface, and the interactions between the solvent (or the solute) and the porous medium. The major difficulty is to measure and predict these effects. Indeed, the experimental estimation of these ones is not currently feasible. In many cases, they are estimated by indirect methods such as membrane potential experiments [11] or numerical investigations [12] obtained through the filtration of salt solutions with NF membranes. Nevertheless, the estimated result remains an average contribution (in the pore), acting on ionic solutes only.Experimental results reported in the literature [13], which were obtained with zeolite membranes, show that these interactions can have a significant effect on membrane performances. Indeed, experimental tests carried out with ultrafiltration (low cut-off) membranes have shown that monovalent salts can be partially retained while an apolar solute (Vitamin B 12) is completely transmitted. These observations can neither be explained by steric or electric effects nor be explained by influence of confinement. From this observation, the membrane performances can be explained only by the interactions between the membrane surface, the solvent, and the solute.The purpose of this work is to investigate the modifications of these interactions after filtration of an alkaline solution. For this, contact angle measurements are performed on a flat Na-mordenite membrane to estimate the apolar and polar components of the surface tension.


## 2. Experimental

### 2.1. Membrane Preparation

α-alumina plates (2 × 2 cm2) were purchased from Rott, France. Alumina tubular supports (length = 25 × 10−2 m; internal diameter = 7 × 10−3 m) were provided by Pall Exekia (Bazet, France). Pretreatment of the substrates (alumina plates or tubes) was fully described by Lauridant and coauthors [14] and consists in cleaning the substrates in an aqueous solution of detergent (Alconox, 3 g in 400 mL of distilled water) heated to 60°C for 1 h. They were then rinsed with distilled water, dried at 70°C, and cooled down to ambient temperature.A gel of Na-mordenite was prepared according to the operating procedure detailed by Hincapie et al. [15]. Starting from this gel, Na-MOR tubular membranes were produced by seeded hydrothermal synthesis onto the alumina tubular support. The spin coating process was used for the impregnation of the gel on the internal surface of the alumina tubes. The impregnated alumina tubes were then transferred in a 500 mL Teflon lined stainless steel autoclave (Top Industrie, France) and heated at 150°C for 42 h. Five membranes were synthesized and calcined at different temperature (M1 at 300°C, M2 at 300 and then at 400°C, M3 and M5 at 400°C, and M4 at 500°C) for 2 h.In the case of the flat membranes synthesis two plates vertically fixed on a PTFE (Teflon) holder were immersed into the as-prepared Na-MOR-type zeolite gel, placed in 48 mL Teflon lined stainless steel autoclave (Top Industrie, France), and heated at 150°C for 42 h. Na-mordenite crystals grew all over the surface of the plates and formed a homogeneous layer. These plates were used for contact angle measurements.For comparison, a part of the gel was systematically reserved to produce Na-MOR-type zeolite powder. The flat and tubular membranes and the powder were simultaneously calcined between 300°C and 500°C for 4 h. Hereafter the different obtained tubular membranes will be defined by a number going from 1 to 5 depending on the calcination temperature (Table1).Table 1
Evaluation of the hydraulic permeability from pure water filtration tests performed before and after an alkaline treatment.
Membrane
T calcination
Hydraulic permeability
Nature of the treatment
Hydraulic permeability
Ratio
(°C)
(m
3
m
memb
-
2)
(m
3
m
memb
-
2)
M1
300
2.7
E
-
14
Na2CO3—6.6 mM
1.8
E
-
14
0.67
M2
300 & 400
8.8
E
-
15
Na2CO3—6.6 mM
7.6
E
-
15
0.86
M3
400
3.6
E
-
14
Na2CO3—6.6 mM
2.74
E
-
14
0.76
M4
500
5.3
E
-
14
NaOH—0.1 mM
4.77
E
-
14
0.90
M5
400
4.6
E
-
14
Na2CO3—6.6 mM
2.8
E
-
14
0.61
Tests performed after two acid[HCl—12 mM]/base treatments for M3
M3
400
10.2
E
-
14
Na2CO3—6.6 mM
5.7
E
-
14
0.56
M3
400
5.0
E
-
14
Na2CO3—6.6 mM
3.9
E
-
14
0.78


### 2.2. Filtration Test Experiments

The filtration tests are carried out using a laboratory pilot-plant (T.I.A., Bollène, France) described in previous works and Na-mordenite tubular membranes (described above) [12, 13]. Pure water filtration tests are performed by cross-flow rate experiments (constant flow rate of 700 L h−1) for various transmembrane pressures (volumetric pump). The fluid flow is controlled by an electromagnetic flow meter and pressure is measured by two sensors upstream and downstream of the membrane and the regulation is carried out by a manual valve. Experiments are carried out at 25°C. The volume of the water tank is 5 L. Pure water flux is measured for various transmembrane pressures (Δ
P) in order to estimate membrane performances. Membrane hydraulic permeability can be expressed from a macroscopic point of view by
(1)
J
w
=
L
p
μ
Δ
P
,
where J
w is the flux of water through the membrane and µ is the dynamic viscosity of water.The hydraulic permeability is assessed by pure water filtration tests before and after each alkaline treatment.


### 2.3. Contact Angle Experiments

Contact angle (θ) measurements are performed with an OCA 15EC goniometer from DataPhysics Instruments GmbH. The experiments are carried out with three different liquids (distilled water, glycerol, and ethylene glycol) in order to determine disperse and polar surface energies with the OWRK method (Owens, Wendt, Rabel, and Kaelble) [16]. All the plates are hydrated or put in contact with the alkaline solution (Na2CO3, 6.6 mM, pH = 10.8) for 2 h at 25°C and then rinsed with distilled water to evacuate the carbonate ions, before being dried at 60°C for 48 h.Supplementary experiments were performed withα-alumina plates without Na-mordenite to estimate the contribution of the support. All the experiments showed that the liquids immediately penetrate the porous medium due to the high macroporosity of the support. Then, the influence of the support on the measurement of the surface energy can be neglected.


### 2.4. Characterizations

The Si/Al molar ratio of the Na-mordenite layers coated on the plates was achieved by X-ray wavelength fluorescence (XRF) measurements, performed with a MagiX Philips (2.4 kW) apparatus. The morphology of the Na-mordenite crystals present at the surface of theα-alumina plates and the homogeneity and the thickness of the Na-mordenite layer were performed with a scanning electron microscope (Philips XL 30 FEG).


## 2.1. Membrane Preparation

α-alumina plates (2 × 2 cm2) were purchased from Rott, France. Alumina tubular supports (length = 25 × 10−2 m; internal diameter = 7 × 10−3 m) were provided by Pall Exekia (Bazet, France). Pretreatment of the substrates (alumina plates or tubes) was fully described by Lauridant and coauthors [14] and consists in cleaning the substrates in an aqueous solution of detergent (Alconox, 3 g in 400 mL of distilled water) heated to 60°C for 1 h. They were then rinsed with distilled water, dried at 70°C, and cooled down to ambient temperature.A gel of Na-mordenite was prepared according to the operating procedure detailed by Hincapie et al. [15]. Starting from this gel, Na-MOR tubular membranes were produced by seeded hydrothermal synthesis onto the alumina tubular support. The spin coating process was used for the impregnation of the gel on the internal surface of the alumina tubes. The impregnated alumina tubes were then transferred in a 500 mL Teflon lined stainless steel autoclave (Top Industrie, France) and heated at 150°C for 42 h. Five membranes were synthesized and calcined at different temperature (M1 at 300°C, M2 at 300 and then at 400°C, M3 and M5 at 400°C, and M4 at 500°C) for 2 h.In the case of the flat membranes synthesis two plates vertically fixed on a PTFE (Teflon) holder were immersed into the as-prepared Na-MOR-type zeolite gel, placed in 48 mL Teflon lined stainless steel autoclave (Top Industrie, France), and heated at 150°C for 42 h. Na-mordenite crystals grew all over the surface of the plates and formed a homogeneous layer. These plates were used for contact angle measurements.For comparison, a part of the gel was systematically reserved to produce Na-MOR-type zeolite powder. The flat and tubular membranes and the powder were simultaneously calcined between 300°C and 500°C for 4 h. Hereafter the different obtained tubular membranes will be defined by a number going from 1 to 5 depending on the calcination temperature (Table1).Table 1
Evaluation of the hydraulic permeability from pure water filtration tests performed before and after an alkaline treatment.
Membrane
T calcination
Hydraulic permeability
Nature of the treatment
Hydraulic permeability
Ratio
(°C)
(m
3
m
memb
-
2)
(m
3
m
memb
-
2)
M1
300
2.7
E
-
14
Na2CO3—6.6 mM
1.8
E
-
14
0.67
M2
300 & 400
8.8
E
-
15
Na2CO3—6.6 mM
7.6
E
-
15
0.86
M3
400
3.6
E
-
14
Na2CO3—6.6 mM
2.74
E
-
14
0.76
M4
500
5.3
E
-
14
NaOH—0.1 mM
4.77
E
-
14
0.90
M5
400
4.6
E
-
14
Na2CO3—6.6 mM
2.8
E
-
14
0.61
Tests performed after two acid[HCl—12 mM]/base treatments for M3
M3
400
10.2
E
-
14
Na2CO3—6.6 mM
5.7
E
-
14
0.56
M3
400
5.0
E
-
14
Na2CO3—6.6 mM
3.9
E
-
14
0.78


## 2.2. Filtration Test Experiments

The filtration tests are carried out using a laboratory pilot-plant (T.I.A., Bollène, France) described in previous works and Na-mordenite tubular membranes (described above) [12, 13]. Pure water filtration tests are performed by cross-flow rate experiments (constant flow rate of 700 L h−1) for various transmembrane pressures (volumetric pump). The fluid flow is controlled by an electromagnetic flow meter and pressure is measured by two sensors upstream and downstream of the membrane and the regulation is carried out by a manual valve. Experiments are carried out at 25°C. The volume of the water tank is 5 L. Pure water flux is measured for various transmembrane pressures (Δ
P) in order to estimate membrane performances. Membrane hydraulic permeability can be expressed from a macroscopic point of view by
(1)
J
w
=
L
p
μ
Δ
P
,
where J
w is the flux of water through the membrane and µ is the dynamic viscosity of water.The hydraulic permeability is assessed by pure water filtration tests before and after each alkaline treatment.


## 2.3. Contact Angle Experiments

Contact angle (θ) measurements are performed with an OCA 15EC goniometer from DataPhysics Instruments GmbH. The experiments are carried out with three different liquids (distilled water, glycerol, and ethylene glycol) in order to determine disperse and polar surface energies with the OWRK method (Owens, Wendt, Rabel, and Kaelble) [16]. All the plates are hydrated or put in contact with the alkaline solution (Na2CO3, 6.6 mM, pH = 10.8) for 2 h at 25°C and then rinsed with distilled water to evacuate the carbonate ions, before being dried at 60°C for 48 h.Supplementary experiments were performed withα-alumina plates without Na-mordenite to estimate the contribution of the support. All the experiments showed that the liquids immediately penetrate the porous medium due to the high macroporosity of the support. Then, the influence of the support on the measurement of the surface energy can be neglected.


## 2.4. Characterizations

The Si/Al molar ratio of the Na-mordenite layers coated on the plates was achieved by X-ray wavelength fluorescence (XRF) measurements, performed with a MagiX Philips (2.4 kW) apparatus. The morphology of the Na-mordenite crystals present at the surface of theα-alumina plates and the homogeneity and the thickness of the Na-mordenite layer were performed with a scanning electron microscope (Philips XL 30 FEG).


## 3. Results and Discussion

Previous investigations carried out with Na-mordenite membranes have shown that their filtration properties are deeply modified after an alkaline treatment. Indeed, no salt rejection was observed during filtration tests of pure salt-water solutions (5 mM of NaCl, NaF, Na Br, NaI, and Na2SO4). After the alkaline treatment (filtration of a 6.6 mM Na2CO3 solution at pH = 10.8 for 2 hours), ion rejection rates are more and less significant [13, 17].In these works the modification of the membrane properties (in terms of salt rejections) was attributed to a modification of the surface polarity [18] and more precisely to the modifications of the van der Waals forces (London, Keesom and Debye interactions) and Lewis-Brönsted acid-base interactions. For short distances (d < 10 nm), these interactions decrease with distance as d
-
2 [19] and as d
-
3 beyond 10 nm [20, 21]. The investigation of the surface thermodynamics of acid-base interactions (Lewis-Brönsted) was recently performed by studying the surface acidity of Na-mordenite [22]. The results show a significant modification of the surface chemistry of the Na-mordenite crystals after the mild alkaline treatment explained by the transformation of some Brönsted surface sites |H|[Al–Si–O] into pseudo-Lewis acid sites |Na+|[Al–O−] after silicon extraction.All these observations lead to the hypothesis that after the alkaline treatment, the surface polarity of the Na-mordenite crystals increases significantly. This should modify the transfer of pure solvent. In order to confirm the presence of significant interactions between water molecules and the surface of the Na-MOR-type zeolite crystals after the alkaline treatment, pure water filtration tests were carried out on different Na-mordenite tubular membranes. Figure1 shows the experimental results obtained for two membranes (1 and 5) before and after the alkaline treatment. The slope of each experimental series corresponds to the hydrodynamic permeability (L
p) of the membrane.Figure 1
Extraction of the hydraulic permeabilities of different zeolite tubular membranes from the representation of the permeation flux versus the transmembrane pressure (membranes 1 (dotted lines) and 5 (full lines) before (black) and after the alkaline treatment (grey)).Hydraulic permeabilities of different Na-MOR-type zeolite membranes are reported in Table1. In the first part of Table 1, we present the evolution of the hydraulic permeabilities induced by an alkaline treatment performed just after the conditioning step [23]. At the bottom of Table 1 we show the evolution of the hydraulic permeability of M3 after two acid/base treatments (filtration of a HCl solution 1 mM during 2 hours, rinsing with pure water, and filtration of a sodium carbonate solution at a concentration of 6.6 mM). An estimation of the membrane pore radius has been systematically performed by filtration of a neutral compound (Vitamin B 12) after the alkaline treatments in order to observe an eventual modification of the pore size [24].The results indicate systematically a drop of the hydraulic permeability without a decrease of the membrane porosity (constant rejection of VB 12) and, at the same time, we observe a partial rejection of the salts mentioned above after the alkaline treatment. It is known that an alkaline treatment could be at the origin of mesopore formation in zeolites when it is performed at high concentration [25, 26]. Nevertheless, the alkaline treatment we use is a mild one, which may only induce a modification of the mordenite surface crystals.Some authors have used the extended solution-diffusion model to describe the volumetric flux obtained during the filtration of water. This model initially developed for nonporous membrane has been modified to describe the transfer of water through NF/RO porous membranes [27].In this way, the volumetric flux can be expressed as for pure water by the following [28]:
(2)
J
w
=
K
d
D
w
∞
ε
Δ
x
1
-
λ
w
2
exp
⁡
-
Δ
G
w
k
B
T
V
w
R
T
Δ
P
,
where K
d
D
w
∞ is the diffusion coefficient of water in the porous media, ε
/
Δ
x the ratio between porosity and thickness of the active layer, (
1
-
λ
w
)
2
=
(
1
-
r
w
/
r
p
)
2 the steric exclusion (ratio between stokes radius of water and pore radius), V
w the molar volume, Δ
P the transmembrane pressure, R the gas constant, T the temperature, k
B the Boltzmann constant, and Δ
G
w the water-membrane surface interaction energy.There is no reason why the mild alkaline treatment leads to a decrease of the active layer thickness as well as the pore size distribution of the Na-mordenite layer (no modification of Vitamin B 12 transmission). The only way to explain the drop of permeability is a modification of the water-surface interaction energy. Indeed, the ratio of the water fluxes before (J
1
,
w) and after treatment (J
2
,
w) is given by
(3)
J
1
,
w
J
2
,
w
=
exp
⁡
-
Δ
G
1
,
w
-
Δ
G
2
,
w
k
B
T
.
As J
1
,
w is higher than J
2
,
w, it means that the interaction energy between water and the membrane surface has increased after the alkaline treatment. The rise of the interaction energy should be experimentally expressed by an increase of the surface tension or a decrease of the contact angle.According to the theory of Lifshitz-van der Waals interactions in condensated state [32–34], the interaction energy between water molecules and a surface Δ
G
w (the membrane surface in the present case) can be related to surface tension via the Young-Dupré equation:
(4)
Δ
G
w
=
-
A
w
s
1
+
cos
⁡
θ
γ
w
,
where A
w
s is the contact area between the water molecule and the membrane surface, γ
w is the apparent surface tension of water, and θ is the contact angle between the water drop and the Na-mordenite surface.As it was previously described, these interactions are the sum of two components: the apolar Lifshitz-van der Waals interactions (LW) and the polar interactions due to the presence of hydrogen bonding [35]. The set of these interactions (hydrogen bonding) are often called Lewis acid-base (AB) interactions.From this hypothesis, the apparent surface tension (or the interaction energy) can be expressed as the sum of two contributions:(5)
γ
=
γ
LW
+
γ
AB
.
If the apolar interactions (Lifshitz-van der Waals) are symmetrical, the polar interactions (AB) are essentially asymmetrical. To take into account this asymmetry, two polar components of the surface tension are defined: an electron acceptor γ
+ and an electron donor γ
- [36].The Young-Dupré equation can be expressed for a liquid (L) in contact with a surface (S) by (6) derived from the van Oss et al. approach [34]:
(6)
Δ
G
=
Δ
G
LW
+
Δ
G
AB
=
-
A
L
S
1
+
cos
⁡
θ
γ
=
-
2
A
L
S
γ
S
LW
γ
L
LW
+
γ
S
+
γ
L
-
+
γ
S
-
γ
L
+
.
First, by a single contact angle measurement with the studied liquid, the apparent interaction energy can be estimated. Second, by contact angle measurements performed with three liquids (presenting distinct polarities), the different contributions of the surface tension can be estimated by solving (6) for the three liquids. For each liquid, this requires the knowledge of apolar and polar components of the surface tension. In this work, we choose to use water, ethylene glycol, and glycerol as references for the contact angle measurements in order to solve (6). Table 2 lists apolar and polar contributions of the surface tension for these liquids, extracted from the literature. The values of polar contributions (electron-acceptor and electron-donor) available in the literature are very different. Taking into account these significant differences, the calculations are performed with three sets of data from three different sources.Table 2
Apolar (Lifshitz-van der Waals) and polar (Lewis acid-base: electron-acceptor and electron-donor contributions) surface tension components (mN m−1) for water, ethylene glycol, and glycerol.
Water
Glycerol
Ethylene glycol
γ
L
LW
γ
L
AB
γ
L
LW
γ
L
AB
γ
L
LW
γ
L
AB
(γ
L
+)
(γ
L
-)
(γ
L
+)
(γ
L
-)
(γ
L
+)
(γ
L
-)
Jańczuk et al. [29]
21.8
25.5
25.5
33.6
9.89
22.3
31.5
5.98
11.6
Costanzo et al. [30]
21.8
25.5
25.5
34
3.92
57.4
29
3
30.1
Lee [31]
21.8
34.2
19
34
5.30
42.5
29
2.6
34.8SEM investigations were performed on the Na-mordenite plates. The aim of these characterizations was to evaluate the behavior of the Na-mordenite crystal present at the surface of the plates after hydration or alkaline treatment. SEM images corresponding to the hydrated and treated plates are presented in Figure2. The observation of the plate surface after an alkaline treatment (Figure 2(c)) indicates that the Na-mordenite crystals remain agglomerated and no modification of the surface is observed.SEM photographs of the hydrated ((a) and (b)) and the treated Na-mordenite plates obtained at different enlargement ((c) and (d)).
(a)
(b)
(c)
(d)At a higher enlargement (Figures2(b) and 2(d)) we can see that the external texture of the Na-mordenite crystals seems to be different after the alkaline treatment (Figure 2(d)). The Si/Al molar ratio of Na-mordenite was determined by XRF spectroscopy and seems to slightly decrease after the alkaline treatment (Si/Al = 5.85 before the treatment and 5.78 after the treatment). It means that silicon atoms are extracted from the surface of the Na-MOR-type zeolite, as suggested by the modification of the external texture observed by SEM (Figure 2(d)).The contact angles obtained with the three liquids are presented in Table3. We observe a significant decrease of the contact angles for the treated Na-mordenite plates whatever the liquid is. The estimated surface tension is very close to the one of pure water (72.3 versus 72.8 mN m−1 for water) for the untreated Na-mordenite plate.Table 3
Estimation of the surface tension of the treated and the nontreated Na-mordenite plates from the contact angles obtained with water, ethylene glycol, and glycerol.
Before alkaline treatment
After alkaline treatment
γ
θ
γ
θ
(mN m−1)
(degree)
(mN m−1)
(degree)
Water
—
18.6
—
9.5
Glycerol
—
33.1
—
23
Ethylene glycol
—
20.4
—
15.2
72.3
77From (6), we obtain an equation with three variables for each liquid. The solvation of the equation set leads to the estimation of γ
s
LW, γ
s
+, and γ
s
- (before and after the alkaline treatment). Table 4 summarizes the estimated values for the apolar and the polar components of the surface tension.Table 4
Estimation of the surface tension components (mN m−1) of the Na-mordenite layer from the contact angle measurements obtained with three liquids (Table 3).
Jańczuk et al. [29]
Costanzo et al.  [30]
Lee [31]
γ
S
LW
γ
S
AB
γ
S
LW
γ
S
AB
γ
S
LW
γ
S
AB
(γ
S
+)
(γ
S
-)
(γ
S
+)
(γ
S
-)
(γ
S
+)
(γ
S
-)
Before treatment
4.8
22.1
53.6
2.4
18.3
69.5
4.7
21.2
32.9
After treatment
2.3
49.6
34.6
0.2
29.4
71.8
1.7
32.9
31.6Even if the polar components of the surface tension are different according to the source we used [29–31], the results we obtained show the same tendencies for the three references. The calculations show that the apolar component (Lifshitz-Van der Waals) is very little. Before the alkaline treatment, the polar component corresponds in major part to the electron-donor contribution of the Lewis acid-base interactions. This is mainly due to the presence of two remaining lone pairs of electrons on the oxygen atoms present at the surface of the zeolite crystals. After the alkaline treatment, some silicon atoms are extracted from the extra framework of the zeolite that induces the apparition of surface defaults corresponding in major part to pseudo-Lewis acid sites and then surface hydroxyl groups. This modification of the surface properties induces an increase of electron-acceptor contribution in the polar component of the surface tension.The calculation ofΔ
G
w (the water-membrane surface interaction energy) shows an increase of interaction energy (in absolute value) after the alkaline treatment: Δ
G
w
1 = −5.95 × 10−21 J and Δ
G
w
2 = −6.46 × 10−21 J, respectively. The ratio of water flux after and before the treatment (or the hydraulic permeability modification) calculated using (3) is 0.88. This result is comparable with the observed permeability drop obtained with the five membranes, which is in the range 0.6–0.9.


## 4. Conclusion

Experimental filtration tests were performed with pure water before and after a mild alkaline treatment. The hydraulic permeabilities of the different membranes synthesized for this study decrease after the treatment. These observations cannot be explained by a modification of the pore size. Only a modification of the surface interactions between the material and the solvent can explain these results. Contact angle measurements are performed on flat mordenite membranes to investigate the effect of the alkaline treatment. These results are analyzed according to the Lifshitz-van der Waals theory of surface tension. The apolar and polar components of the surface material are estimated. The results show that the major contribution is the polar component and more precisely the electron-donor contribution. After the alkaline treatment, an increase of electron-receptor contribution in the polar component of the tension surface is observed probably due to the presence of surface defaults that increases significantly the surface hydrophilicity.The water-membrane surface interaction energies are deduced from this investigation and allow the explanation and the quantification of water flux to decrease after a mild alkaline treatment.



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