Advances in Materials Science and EngineeringVolume 2012 (2012), Article ID 650217, 7 pagesdoi:10.1155/2012/650217

Research Article

Effect of PVP Intermediate Layer on the Properties of SAPO 34 Membrane

Jugal K. Das, Nandini Das, and Sibdas Bandyopadhyay

Ceramic Membrane Division, Central Glass and Ceramic Research Institute, CSIR, Jadavpur, Kolkata 700 032, India

Received 30 September 2011; Accepted 5 December 2011

Academic Editor: Chang-An Wang

Copyright © 2012 Jugal K. Das et al. This is an open access article distributed under the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.

Abstract.

SAPO 34 zeolite membranes were prepared on a tubular mullite support. Before membrane preparation, the support surfaces were coated with seed crystals. Seeds particles were prepared by hydrothermal synthesis. Before seeding, the substrates were treated with polyvinylpyrrolidone (PVP) to orient the seeds. Both the treated and untreated supports were seeded, and membranes were synthesized on those support tubes by ex situ hydrothermal method. The PVP molecule exists in the two resonance structures. Hence the acylamino bond –N⁺ = C–O⁻– acts as intermediate linker between support surface and seed surface. Due to charge interaction, the seed crystals were anchored strongly to support surface. The synthesized membranes along with seed crystals were characterized by XRD, FESEM, and EDAX analysis. The single-gas permeation with CO₂ and H₂ was investigated. Up to 5 bar of feed pressure, the permselectivity of CO₂ and H₂ was as high as 4.2.

1. Introduction

Hydrogen is being considered as the most clean, reliable, environmentally benign and affordable future energy source [1–3]. Hydrogen can be produced by various routes such as biomass, water, coal, natural gas, nuclear power, renewable energies, and wastes [4]. To apply hydrogen as fuels and chemicals, transport and power energy source, we have to separate hydrogen from carbonaceous gas. Because CO₂ reduces the energy content of the gas, and it is acidic and corrosive in presence of water within the transport and storage system [5]. The traditional cryogenic distillation, adsorbent bed processes, and pressure swing methods are used for gas separation in many industries. But in recent times, however, membrane-based gas separation is becoming increasingly popular due to its inherent advantage over the more traditional method. These include low capital and operating cost, lower energy requirement, and generally ease of operation.

Silicoaluminophosphate (SAPO 34) with chabazite-(CHA-) type frame work having pore diameter 0.38 nm is an efficient member of zeolite family, has been studied for various applications, and, most notably, has shown excellent performance in separations, catalysis, and adsorption [6–11]. Considering their molecular sieving properties and uniform pore size, high thermal resistance, high mechanical strength, and order microporous structure, zeolite membrane have attracted great interest and successfully employed to separate carbon dioxide and hydrogen from different gases [12–15]. This small-pore SAPO 34 zeolite membrane has good H₂/CO₂ permeation ability due to a combination of difference in diffusivity and competitive adsorption. There are many reports on the improvement of the formation stages of the membranes like microwave heating [16, 17], addition of intermediate silane layer to increase the adhesion between gel layer and supporting substrate [18], vacuum seeding [19], and so forth. The in situ hydrothermal synthesis appears to be the best studied method, in which the porous support is immersed into the synthesis solution, and then the membrane is formed by direct crystallization. However, it is difficult to prepare high-quality membrane by this in situ crystallization method directly [20]. Coating the zeolite seed on the support surface before hydrothermal synthesis, which is also termed as secondary growth method, is an effective approach to develop a high-quality zeolite membrane. It is well known that the presence of seed on the support surface plays a vital role in membrane formation. Synthesis with seeds gives a better control of the membrane formation process by separating the crystal nucleation and growth with a shortened crystallization time [21]. In addition, the secondary growth ensures the formation of the phase pure zeolite crystal on the support. The secondary growth method which was proposed by Lovallo and Tsapatsis [22] exhibits many advantages such as better control over membrane microstructure and higher reproducibility [23].

An important approach to the preparation of SAPO 34 zeolite monolayer with solid packing was binding zeolite crystals to the support substrate through a molecular linker by covalent bonding, ionic linkage, and hydrogen bonding [24–26]. Molecular linkers are nothing but the intermediate buffer layer of high importance in the fabrication of a uniformly oriented zeolite monolayer as they can bind and form homogeneous closely packed membrane layer on the support.

In this work, we report a simple technique for proper orientation of SAPO 34 seed crystals on support surface to synthesize a SAPO 34 zeolite membrane layer on clay alumina substrate by secondary growth method. Almost-dense zeolite membrane was synthesized on properly seeded substrate. The ultimate performance of the membrane was characterized by gas permeation studies.

2. Experimental

2.1. Membrane Synthesis

2.1.1. Seeds Synthesis

The materials used for the synthesis were boehmite powder (SASOL), silica sol (Ludox 40 AS), phosphoric acid (Qualigens Fine Chemicals, India), and morpholine (SD fine chemicals, India), as well as distilled water. Two reactant mixtures were prepared, respectively, dissolving boehmite powder, phosphoric acid, and required amount of water (mixture 1) to the reaction mixture. The mixture was stirred for overnight. In another mixture (mixture 2), silica sol and morpholine were added, and the remaining amount of water was added to the reaction mixture. After stirring mixture 2 for 1 h, it was mixed slowly under stirring at room temperature with mixture 1. The resulting mixture was stirred vigorously for 15–30 min and kept under stirring for overnight to produce a homogeneous sol. The molar composition of the sol used for the synthesis was Al₂O₃ : SiO₂ : P₂O₅ : H₂O 1 : 0.3 : 1 : 66. The prepared homogeneous sol was kept in a Teflon line hydrothermal bomb and heated at 170°C for 120 h. At the end of synthesis, the seeds were centrifuged at 12000 rpm for 20 min and washed with distilled water. The procedure was repeated 4 times. The resultant precipitate was dried overnight and calcined at 100°C for 1 h.

2.1.2. Seeding of the Substrate

SAPO 34 seed crystals were dispersed in deionised water under ultrasonication for 2 h. Indigenous mullite tube of diameter 10 mm and thickness 3 mm and 60 mm length was used as substrate for synthesis of SAPO-34 membranes. Before seeding, the substrates were cleaned with acetone in an ultrasonic cleaner (Vibracell, USA) for 5 minutes. The outer surface of the support tubes was wrapped with Teflon sheet so that the zeolite layer was formed inside the tube. Before addition of seed crystals, the support substrate was coated with 3% aqueous solution of PVP. To increase the orientation of the seed crystals on support surface, an intermediate PVP layer was applied. The treated and untreated support substrate was dipped in a 3% SAPO 34 zeolite suspension in deionized water 5 times for duration of 15 s. After the dipping procedure, the seeded supports were dried at 80°C for 24 h.

2.1.3. SAPO-34 Membrane Synthesis

The seeded substrate was placed vertically in an autoclave. The autoclave was filled with reaction mixture having composition Al₂O₃ : SiO₂: P₂O₅ : H₂O 1 : 0.3 : 1 : 66. The procedure was same as seed synthesis. The synthesized membranes were calcined in air at 550°C for 5 h to remove the templates.

2.2. Membrane Characterization

The crystalline structure of the as-synthesized membrane was determined by XRD pattern. XRD was carried out on a Philips 1710 diffractometer using CuKα radiation (α = 1.541 Å).

Microstructure and morphology of the growth layer were examined using scanning electron microscopy (FESEM: model Leo, S430i, UK).

Single-gas permeation for H₂ and CO₂ was measured by a specially designed permeation cell developed in our laboratory. The gas permeance of the membranes was measured by soap film flow meter under the feed pressure of 2 to 5 kg/cm² and at room temperature. The permselectivity of two gases G₁/G₂ was defined as the permeance ratio of G₁ and gas G₂. The gas permeation measurement of each single gas was repeated until the permeance data for the successive 10 tests were closed.

3. Results and Discussion

Figure 1(a) depicts the XRD pattern of SAPO 34 seeds crystals prepared by hydrothermal technique at 170°C for 120 h. The characteristics of the peaks of seed crystals are designed by their (hkl) values. The morphology of those SAPO 34 crystals is shown in Figure 1(b). Comparing the XRD and FESEM, the size range of seed crystals is ~100 nm. The surface area of the synthesized powder was 660 m²/g. In order to form a continuous zeolite membrane on support surface, the coverage of the seed crystals must be high. For higher coverage, smaller-sized seed crystals are most suitable. According to the formation mechanism of zeolite membrane on the porous support, the nucleation of zeolite on the support gel interface and that in the bulk synthesis mixture are competitive processes. Thus to develop a continuous membrane layer, the nucleation of zeolite in the bulk synthesis mixture must be inhibited, while the nucleation of zeolite on the support surface must be increased. Another advantage of surface seeding for preparation of membrane layer on support surface is formation of zeolite phase is accelerated. Polycrystalline zeolite membrane contains defects, that is, inter-crystalline pathway which is also called non-zeolitic pores. The transport mechanism of gas molecules through non-zeolitic pores is difficult, and it is difficult to quantify, because the pore size of these non-zeolitic pores is not well defined. Usually non-zeolitic pores are larger than zeolitic pores. Presence of non-zeolitic pores reduces the selectivity of the gases. The main sources of non zeolitic pores result from cracks and defects of the membrane layer. The main cause of the crack is due to the lack of good adherence between zeolite layer and substrate layer. Considering this fact and to obtain a crack-free membrane layer on the substrate, proper seeding on the surface is desirable. In our previous work [27], we have reported that application of intermediate layer between substrate and seed reduces the defects. The PVP molecule exits in the two resonance structures. In case of PVP, the oxygen atom is more electronegative than nitrogen atom, and it is expected that negative charge on PVP prefers to reside on oxygen atom. Figure 2 shows resonance structure of the PVP molecule. The partial positive charge nitrogen atom and partial negative charge on the oxygen atom can behave as electron acceptor and, donor respectively. Hence the acylamino bond –N⁺ = C–O⁻– acts as intermediate linker between support surface and seed surface. Due to charge interaction, the seed crystals were anchored strongly to support surface. Figure 3 depicts the schematic representation of anchoring between support surface and seed crystals. The seeded supports were hydrothermally treated at 170°C from 48 h to 120 h. Figure 4 shows the XRD pattern of SAPO 34 membrane synthesized for 48 h, 72 h, 96 h, and 120 h and compared with standard pattern of SAPO 34 zeolite. As the diffraction intensity of the SAPO 34 zeolite membrane on support surface was too weak to detect by XRD, the diffraction pattern of the bulk powders collected from hydrothermal container was studied. It is clear from the XRD pattern that after 48 h of synthesis some crystalline phase started to form and continued up to 72 h, but the phase was not SAPO 34. After prolonged heating, at 96 h, the crystalline phase was converted into amorphous phase, and on further heating, it was transformed into SAPO 34 after 120 h. Figures 5(a) and 5(b) show the FESEM images of membrane synthesized at 120 h with properly seeded support surface. To ensure the proper formation of membrane layer on support substrate and uniform distribution of component elements, the elemental mapping along with EDAX analysis of the SAPO 34 membrane was studied. Figure 6(a) shows the corresponding membrane layers with homogeneous interlocked structure. Elemental mapping (Figures 6(b)–6(e)) and EDAX analysis (Figure  6(f)) confirm the formation of SAPO 34 membrane layer. The quantitative elemental analysis of the synthesized SAPO 34 as membrane coating is described in table, inside the spectral figure. However XRD and FESEM can only indicate whether a continuous membrane was formed or not on the support, but cannot confirm the quality of zeolite membrane. The quality of zeolite membrane can only be evaluated by gas permeation properties of the membrane. It is well known that performance of a membrane will increase with decreasing defects.

(a)

(b)

Figure 1: (a) XRD pattern and (b) FESEM of SAPO 34 crystals used as seed for membrane synthesis.

Figure 2: Schematic of the resonance structures of PVP molecule.

Figure 3: Schematic representation of seeded membrane with PVP intermediate layer.

Figure 4: XRD pattern of SAPO 34 crystals synthesized for different time ranging from 48 h to 120 h.

(a)

(b)

Figure 5: FESEM micrograph of (a) substrate with PVP intermediate layer with seed layer, (b) membrane layer synthesized on seeded substrate.

(a)

(b)

(c)

(d)

(e)

(f)

Figure 6: (a) FESEM micrograph of SAPO 34 membrane, and (b–e) represent the elemental mapping (O, Al, Si, and P) of the developed membrane and (f) corresponding EDAX spectra of the membrane layer along with atomic percentage.

The permeation of CO₂ and H₂ were measured at room temperature directly after calcining the membrane. The permeation of gas through the micropores of the zeolite can be explained quantitatively by adsorption-diffusion mechanism, where the permeated flux is expressed as the diffusion rate through the micropores between the two sides of the membrane. The diffusion rate becomes significantly smaller where the kinetic diameter of the gas becomes larger than the size of the zeolitic pores due to the molecular sieving effect. The molecular kinetic diameters of H₂ and CO₂ are 0.29 and 0.33 nm, respectively, which are close to the pore size of SAPO 34 zeolite. The configurational diffusion and the difference in molecular size between H₂ and CO₂ result in the difference in the rate of diffusion through the SAPO 34 zeolite channels. The diffusion rate of H₂ is faster than that of CO₂, and therefore, H₂ and CO₂ can be separated by SAPO 34 zeolite membrane. So the single-gas permeation depends on the kinetic diameter of the gases. Tables 1 and 2 describe the permeability of CO₂ and H₂ through the SAPO 34 membrane prepared without any intermediate layer and PVP intermediate layer, respectively, before seeding, under different pressure. CO₂ has a lower permeance than H₂. The rate of change of permeance with pressure is less for CO₂ than H₂. At high pressure, CO₂is adsorbed more strongly on SAPO 34 zeolite membrane surface than H₂, and the rate of desorption of CO₂ from the membrane surface also decreased. As a result, flux rate decreases. Therefore, the H₂/CO₂ selectivity is changed from 1.16 to 4.2. Comparison of the permeability values described in both tables confirms that “reduced defect” membrane is formed with PVP as intermediate layer. Table 2 describes the change of selectivity of the above-mentioned gases at different pressure. In case of H₂ and CO₂, the separation is controlled by competitive adsorption and diffusion. The combined effect of these two determines the ultimate selectivity.

Table 1: Room temperature single gas permeation for H₂ and CO2 through SAPO 34 membrane on untreated support at 30°C.

Temperature (°C )
Pressure (kg/cm2 )
Permeance (mol/m²·sec-pa)
Selectivity

H₂
CO₂

30
2
10.23
12.0
0.85

30
3
22.5
23.2
0.96

30
4
29.5
27.5
1.07

30
5
40.1
15.0
2.67

Table 2: Room temperature single-gas permeation for H₂ and CO₂ through SAPO 34 membrane on the support treated with PVP at 30°C.

Temperature (°C)
Pressure (kg/cm²)
Permeance (mol/m²·sec-pa )
Selectivity

H₂
CO₂

30
2
6.0
1.8
3.33

30
3
7.0
6.0
1.16

30
4
16.0
4.0
4

30
5
21.0
5.0
4.2

4. Conclusion

SAPO 34 membranes were synthesized on clay alumina tubular support. The membrane in this study was synthesized by ex situ hydrothermal technique. Application of intermediate layer confirms the formation of “reduced defect” SAPO 34 membrane. The intermediate PVP layer helps in formation of uniform seeded layer, which on further treatment forms “reduced defect” membrane. Single gas permeation studies showed that selectivity (permeability ratio) of the permeance increases with increasing feed pressure. The selectivity of the H₂/CO₂ slightly increases with increasing pressure. At higher pressure, competitive adsorption and difference in diffusivity due to molecular kinetic diameter are responsible for selectivities of H₂/CO₂.

Acknowledgment

The authors would like to thank CSIR, India, for financial support in the Project no. SIP 0023 and also thankful to Dr. I. Manna Director, CGCRI, for his kind permission to publish the research work.

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