Hierarchical Low Si/Al Ratio Ferrierite Zeolite by Sequential Postsynthesis Treatment: Catalytic Assessment in Dehydration Reaction of Methanol

Catizzone, Enrico; Migliori, Massimo; Aloise, Alfredo; Lamberti, Rossella; Giordano, Girolamo

doi:https://doi.org/10.1155/2019/3084356

Journal of Chemistry

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Abstract Introduction Materials and Methods Results and Discussion Conclusions Data Availability Conflicts of Interest References Copyright Related Articles

Research Article | Open Access

Volume 2019 | Article ID 3084356 | https://doi.org/10.1155/2019/3084356

Hierarchical Low Si/Al Ratio Ferrierite Zeolite by Sequential Postsynthesis Treatment: Catalytic Assessment in Dehydration Reaction of Methanol

Enrico Catizzone,¹Massimo Migliori,¹Alfredo Aloise,¹Rossella Lamberti,¹and Girolamo Giordano¹

Academic Editor: Cláudia G. Silva

Received10 Sept 2018

Accepted06 Dec 2018

Published02 Jan 2019

Abstract

In contrast to high silica zeolites, it is difficult to obtain mesoporosity in zeolites with low Si/Al ratio (e.g., <20) via conventional NaOH-based treatment, making the obtainment of hierarchical zeolites with high acidity a challenging target. In this paper, we report the preparation of hierarchical FER-type zeolite at low Si/Al molar ratio (about 10) by postsynthesis etching involving a sequence of three treatments with NaAlO₂, HCl, and NaOH solutions and investigate the effect of both NaAlO₂ solution concentration and time of treatment on the textural properties. The obtained materials exhibit a mesoporous volume higher than the parent ferrierite with no significant effect on the sample acidity. The catalytic activity of some samples was investigated in vapour-phase methanol dehydration to dimethyl ether, revealing the superiority of hierarchical zeolites in terms of methanol conversion, although the presence of mesopores causes formation of light hydrocarbons at high temperatures.

1. Introduction

Zeolites are well-known crystalline aluminosilicates largely applied as catalysts in several industrial processes because of the unique molecular shape selectivity exhibited by these materials due to well-defined regular microporous structure. The possibility to tune the voids system in these materials (openings and spatial orientation of channels, size, and location of cages, etc.) allows to have a catalyst capable of directing the reaction pathway towards formation of desired products [1]. Beside shape selectivity, the acid-base properties of zeolites are of paramount importance in catalysis. Both Brønsted and Lewis acid sites are normally present in zeolites and their concentration, distribution, strength, and location are well-known factors affecting activity, selectivity, and deactivation of the catalyst. Beside these indisputable advantages, zeolites suffer from severe intracrystalline mass transfer limitations due to comparable size of the diffusing molecules and zeolite voids. In zeolites, the diffusing molecules are continuously affected by the interaction with the channel walls and this type of intracrystalline diffusion is known as configurational diffusion, in order to differentiate it from faster Knudsen-type diffusion. This constrained diffusion in zeolites hinders the reactant molecules to reach the active sites confined in the channels, negatively affecting the catalyst effectiveness. In order to overcome this problem, several strategies can be adopted trying to make more accessible the active sites to the reactant molecules.

As well discussed by Pérez-Ramírez et al. [2, 3], mass transfer limitations inside zeolite crystals can be improved by using zeolites with different porosity levels (e.g., hierarchical porosity) in which the molecular-sized channels are interconnected and connected to the external crystal surface through mesopores facilitating the reactants to access the active sites. During the last decade, several methods to obtain hierarchical micro/mesoporous zeolites are reported following either bottom-up (e.g., carbon-templating) or top-down (e.g., desilication) approaches, showing how hierarchization technique strongly affects physicochemical properties of zeolites (e.g., pore architecture, position, and topology of mesopores) and the catalytic performances as consequence. The chemical-physical properties of starting materials also play a crucial role in producing hierarchical zeolites. In particular, the efficiency in forming mesoporous surface of conventional NaOH postsynthesis treatment strongly depends on the Si/Al ratio of starting zeolite, showing the highest values in Si/Al range of 25–50. Indeed, for Si/Al < 15, the presence of framework aluminium prevents silicon leaching, limiting mesopores formation; on the other hand, for Si/Al > 200, alkaline treatment causes an excessive and uncontrolled Si extraction resulting in formation of macropores and loss of intrinsic micropore voids [4–6].

Recent works showed that FER-type zeolite can be considered a selective acid catalyst to produce dimethyl ether (DME) via both methanol dehydration and one-pot CO₂ hydrogenation. DME is a reliable alternative fuel for diesel engines due to its high cetane number and soot-free emissions [7, 8]. Moreover, DME can be produced from biomass or CO₂ and, as it can also be used as an intermediate to produce olefins and chemicals, it is considered a promising energetic vector of the future for introducing renewable energy in the chemical industry [9–11]. The valorisation of biomass by using zeolites is receiving a growing attention because it opens new ways for application of these materials in low temperature and liquid phase reactions of biomass or biomass-derived compounds [12, 13]. Compared with other zeolites such as MFI, BEA, EUO, MTW, the 2-D small/medium pore system of FER-type zeolite inhibits the coke formation and offers high DME selectivity during methanol dehydration reaction [14, 15]. In particular, FER-type zeolite with Si/Al = 8–10 exhibits a higher activity and higher TOF than zeolite with higher Si/Al [16]. Furthermore, a recent study showed the superiority of FER-type zeolite over commercial γ-Al₂O₃ (the industrial catalyst of vapour phase methanol-to-DME process), in terms of catalytic resistance in the presence of water, this being a product of reaction that strongly inhibits the activity of γ-Al₂O₃ [17]. The superiority of FER-type zeolite over other zeolites was also reported for one-pot CO/CO₂ hydrogenation to DME process, revealing reliable DME productivity [15–19]. Prasad et al. [18] report that the superiority of ferrierite over other investigated zeolites (i.e., ZSM-5, NaY, and HY) is related to the suitable acid properties as well as a suitable channel topology that retards catalyst deactivation. Similar results were also found by Montesano et al. [19], showing that DME is the main dehydration product obtained during the syngas-to-DME process. Kang et al. [20] and Bae et al. [21] showed that the catalytic behaviour of Cu/ZnO/Al₂O₃-ferrierite systems modified with zirconia exhibit higher stability during the reaction. The high activity of ferrierite-based catalysts was also found for bio-syngas or CO₂ one-pot conversion to DME [22, 23]. In particular, Bonura et al. report that deactivation of ferrierite-based catalyst depends on both acidity and the crystal size of zeolite [24]. Nevertheless, a very little attention has been paid to investigate the catalytic behaviour of hierarchical FER zeolite. The aim of this study is to investigate on the possibility to obtain hierarchical FER-type zeolites, starting from an FER zeolite with a low Si/Al value of 10 and to assess the effect of generated mesopores on catalysis during methanol dehydration to dimethyl ether.

2. Materials and Methods

2.1. Synthesis of Samples

Parent FER-type zeolite was synthesised with a Si/Al value of 10 by using pyrrolidine (Py) as a structure directing agent by adopting the following molar gel composition [25]:

The starting synthesis gel was prepared at room temperature as follows: 0.25 g of NaOH (Aldrich) and 2 g of NaAlO₂ (54 wt.% Al₂O₃, Aldrich) were dissolved in 57.1 g of distilled water. Afterwards, 9 g of pyrrolidine (99%, Aldrich) was added, and the system was kept in closed PP bottle under stirring for 30 min, then 31.7 g of colloidal silica (LUDOX AS40, Aldrich) was added in drops, resulting in an opaque gel under vigorous stirring for 1 h. The crystallization was performed in a 100 ml PTFE-lined stainless steel autoclave in a tumbling oven (tumbling speed = 25 rpm) kept at 180°C for 3 days. After synthesis, the autoclave was quenched in cold water and the solid was recovered by suction filtration followed by careful washing with distilled water. Organic SDA was removed by calcination in static air at 550°C for 8 h, and after this treatment, the H-form of the synthesised zeolites was prepared by a double ion-exchange with 1 M NH₄Cl solution (100 ml/g_zeolite) at 80°C, followed by calcination in static air at 550°C for 8 h.

Hierarchical FER-type zeolites were prepared on the basis of the method proposed by Verboekend et al. [26]. The H-form parent FER powder was subjected to consecutive treatments with NaAlO₂, HCl, and NaOH solutions. In the first step, about 1 g of parent zeolite was treated with NaAlO₂ (10 ml_sol/g_zeolite) at 80°C in a closed PP bottle under vigorous stirring. The effect of both concentration and contact time was investigated by using 1 M, 1.5 M, and 2 M NaAlO₂ solutions for 0.5, 1.5, and 3 h; afterwards, the solution was quenched in an ice-water bath. According to Verboekend et al. [26], the secondary step consists of removing extra-framework aluminium species by treating the solid with a 3 M HCl solution (10 ml_sol/g_zeolite) under stirring at 80°C. Finally, the third step consists of an alkaline treatment with a 0.2 M NaOH solution (30 ml/g_zeolite) under stirring at 60°C for 30 min in order to remove silicon-rich debris. After each step, the solid was recovered by filtration, washed with distilled water until neutral pH, and dried overnight. The resulting solid was then transformed to protonic form by the same procedure reported for the parent sample. Table 1 reports the treatment conditions adopted in this work.

2.2. Characterization

Powered X-ray diffraction patterns of synthesised samples were obtained with APD 2000 Pro GNR instrument (Cu Kα radiation, λ = 1.5406, 40 kV, 30 mA, 5–50° 2θ range, scanning step 0.2°·s⁻¹). Crystal habit was observed via scanning electron microscopy (FEI model Inspect). Nitrogen isotherms adsorption/desorption measurements were carried out at −196°C with Micromeritics ASAP 2020 instrument, following the procedure discussed elsewhere. For comparative purpose with published studies on hierarchical ferrierite zeolites [27–31], specific surface area was estimated from Brunauer‐Emmett‐Teller (BET) equation whilst both micropore volume and external surface were calculated by the t-plot method, adopting the Harkins–Jura as the master isotherm [32–36], although such methods may have some limitation for micro/mesoporous materials [37]. Pore size distribution was obtained by applying the Barrett–Joyner–Halenda (BJH) to the adsorption branch of the isotherms. Chemical composition of the investigated samples was determined via atomic absorption spectroscopy (GBC 932). Surface acidity was assessed by temperature programmed desorption of ammonia (NH₃-TPD) measurements with a TPDRO1100 (ThermoFisher) equipped with a thermal conductivity detector (TCD), according to the following procedure. Dried sample (100 mg, powder form) was loaded in a linear quartz microreactor and pretreated at 300°C in helium flow (20 STP ml·min⁻¹, STP referred at 0°C and 1 bar) for 1 h to remove the adsorbed water. The sample was cooled down to 150°C and saturated with 10% v/v NH₃/He mixture with a flow rate of 20 STP ml·min⁻¹ for 2 h. Ammonia physically adsorbed was removed by purging in helium at 150°C for 1 h until TCD baseline stabilization. Desorption measurement was carried out in the temperature range of 100–550°C (10°C·min⁻¹) using a helium flow rate of 20 STP ml·min⁻¹.

2.3. Catalytic Tests

Vapour-phase methanol dehydration was used to assess the effect of hierarchical pore structure on catalytic behaviour of ferrierite samples. Catalytic tests were carried out in a continuous packed bed quartz reactor loaded with about 70 mg of dried sample. Before feeding methanol, the catalyst was treated under nitrogen flow at 250°C for 2 h in order to remove residual moisture. After setting the reactor temperature to the desired set point, a mixture of methanol (0.06 mol/mol) and nitrogen as a carrier (60 STP ml/min) was fed to the reactor at the weight hourly space velocity (WHSV) of 4.5 g_MeOH/(g_cat·h). The reactor out-stream was analyzed by GC (Agilent 7890 A) equipped with a capillary column (J&W 125−1032) and a FID detector. The detector was kept at 250°C whilst the column was heated from 40°C to 150°C with a ramp of 10°C using hydrogen as carrier with a constant flow of 8 STP ml·min⁻¹.

3. Results and Discussion

3.1. Physical-Chemical Characterization

Figure 1 shows the XRD patterns in the 2 theta range 20–30° of parent zeolite and the treated samples with 1 M and 2 M NaAlO₂ solution for 6 h and 3 h in acid form, respectively. XRD shows that no significant phase change occurs after treatments, even though a little decrease in intensity can be observed.

Table 2 reports the relative crystallinity of investigated samples calculated considering the sum of intensity of peaks at 22.3°, 22.6°, 23.6°, 25.3°, and 25.6° and taking the parent zeolite as reference.

Table 2 shows that crystallinity decreases by increasing both NaAlO₂ concentration and treatment time. Samples after 3 h of treatment with NaAlO₂ (e.g., C1, C1.5, and C2) show a crystallinity of 91%, 85%, and 79% when the concentration of NaAlO₂ solution was 1 M, 1.5 M, and 2 M, respectively. Similarly, by increasing the treatment time the sample shows a lower crystallinity.

Furthermore, after postsynthesis treatments, a shift of reflections towards the lower angle is observes, suggesting some modification of unit cell parameters. Assuming an orthorhombic configuration, the unit cell volume is 1943 Å³, 1953 Å³, and 1947 Å³ for P, D1, and C2 sample, respectively, indicating a negligible change of zeolite lattice after treatment.

Nitrogen adsorption isotherms reported in Figures 2(a) and 2(b) confirm the microporous structure of parent ferrierite sample. On the contrary, for treated samples the nitrogen uptake at a middle-high relative pressure significantly increases by increasing ether contact time (Figure 2(a)) or NaAlO₂ concentration (Figure 2(b)). The introduction of additional mesopores after treatment is also highlighted by BJH pore size distribution reported in Figure 3. In particular, by increasing the contact time and NaAlO₂, the mesopore volume increases significantly in the range 2–50 nm even if no centered mesoporosity is observed. Similar results were observed also by Verboekend et al. [26], for FER zeolite with Si/Al = 27 after similar treatments. Figure 4 shows a comparison between N₂ isotherms and BJH PSD of parent ferrierite and DesNaOH sample revealing that the treatment with NaOH is less effective in terms of mesopore generation than the combined NaAlO₂ + HCl + NaOH sequential method [26].

(a)

(b)

(a)

(b)

(a)

(b)

Table 3 reports both chemical and textural properties of investigated zeolites. Chemical analysis reveals that the hierarchization technique does not significantly affect the Si/Al ratio that is kept in the range 10–12 and only a small reduction of silicon content is found for the sample treated with NaOH. The postsynthesis treatment strongly affects the textural properties of investigated ferrierite as reported in Table 3. The mesopore surface increases as function of both treatment time and NaAlO₂ concentration, preserving the micropore volume in the range 0.11–0.13 cm³/g.

With the aim to have more information on the effect of each treatment, Table 4 reports the main physicochemical properties of each step to produce the D1 sample. In particular, the Si/Al ratio strongly reduces after treatment with NaAlO₂ solution, indicating the precipitation of aluminate species on zeolite crystals. This causes a strong reduction of micropore volume and crystallinity of materials (Figure 5). After HCl washing, both crystallinity and microporosity are recovered due to etching of aluminium species. The subsequent alkaline treatment allows to improve crystallinity and to restore the initial Si/Al ratio. After ion-exchange with NH4Cl solution (pH = 5.5), the crystallinity of the sample was further improved.

The results indicate that the applied method is suitable to obtain hierarchical ferrierite with no significant change in microporosity, which is a key point to preserve the shape selectivity of zeolites. The highest increment in mesoporous surface areas and mesoporous volume was obtained for D1 and C2 samples, respectively; therefore, further characterization and catalytic tests were carried out for these samples.

The NH₃-TPD profiles are reported in Figure 6 for parent, D1, and C2 samples displaying two main bands characterized by different ammonia maximum desorption temperature peaks (T_M) as indicator of different acid sites family (the higher is T_M, the stronger is the acid sites).

(a)

(b)

(c)

As suggested by Niwa and Katada [38], the interpretation of peak with T_M < 300°C may be quite misleading because the desorption effect may also be related to physically adsorbed ammonia hydrogen bonded to NH₄⁺ ions generated by ammonia effectively adsorbed onto acid sites. In this condition, having comparable desorption energy, the presence of weak acid sites, may be partially hidden by physisorbed ammonia. On the contrary, the peaks having 300°C < T_M < 500°C are associated with ammonia molecules desorbed from medium-strong acid sites (both Brønsted and Lewis acid sites). Quantitative results of NH₃-TPD measurements reported in Table 5 reveal that postsynthesis treatment does not significantly affect neither the total amount nor the weak/strong distribution of acid sites, since all the samples disclose similar acidic properties. The total acidity calculated from NH₃-TPD measurements is lower than that theoretically calculated from aluminium content measured by chemical analysis (about 1500 µmol/g for P and D1 and about 1400 µmol/g) indicating that about 30% of aluminium is not acidic or is not accessible for ammonia titration.

3.2. Catalytic Tests

The catalytic activity of synthesised samples was investigated by performing methanol-to-dimethyl ether reaction. Figure 7 shows the methanol conversion as a function of reaction temperature. The reported data are the average value over three independent measurements during 30 min of time-on-stream, always resulting in conversion relative variation below 10%.

Catalytic results clearly show that hierarchical zeolites are more active than parent zeolite, mainly at lower temperatures. For temperatures higher than 220°C, all the catalysts exhibit a similar methanol conversion level approaching the equilibrium value at 240°C. In order to take into account the effect of acidity on catalytic activity, the apparent turnover frequency (TOF_app) can be calculated by considering the acid sites concentration measured by NH₃-TPD. At 180°C, the apparent TOF_app is 90, 167, and 229 h⁻¹ for P, D1, and C2 samples, clearly indicating the beneficial role of increase of both area and volume of mesopores on accessibility of acid sites and then on catalytic activity. Only DME is observed in the reactor out-stream up to 240°C whilst, at higher temperatures, other hydrocarbons, mainly methane, ethene, and propene are formed. At 280°C, although similar conversion level is achieved from each sample, the DME selectivity is 0.98, 0.96, and 0.94 for P, D1, and C2 samples, respectively, indicating that the presence of mesopores may be responsible for shape selectivity loss and a more rapid formation of intermediates for light hydrocarbon production [39–42].

Figure 8 reports the by-products distribution after 5 min reaction at 280°C, clearly showing that C2 sample exhibits a marked tendency to form propene, whilst P and D1 samples show a similar distribution without any significant difference between small hydrocarbons. During 5 h reaction, no conversion loss was observed for all the samples, whilst DME selectivity progressively approaches the unity, probably due to coke deposition partially deactivating the strong acid sites that are mainly responsible for methanol-to-hydrocarbon conversion.

In order to assess the coke deposition, after 5 h reaction at 280°C the samples were subjected to thermogravimetric analysis by following a procedure detailed elsewhere [42]. The results of TGA show that the coke deposited during the reaction was 40 mg/g, 37 mg/g, and 41 mg/g for P, D1, and C2 samples, indicating no significant effect of textural properties on coke deposition under the investigated conditions.

4. Conclusions

The preparation of hierarchical zeolite by desilication starting from zeolites with low Si/Al is a challenge faced in this work. A sequence of postsynthesis modification of ferrierite zeolite with Si/Al = 10 was carried out. The method consists of three steps:

Step 1. Treatment with NaAlO₂ solution at 80°C.

Step 2. Treatment with 3 M HCl solution at 80°C.

Step 3. Treatment with 0.2 M NaOH solution at 60°C.

The effect of both NaAlO₂ concentration and duration of step 1 on textural properties was assessed. Porosimetry analysis clearly shows that both surface area and volume of mesopores can be increased by increasing both NaAlO₂ molarity and treatment time. On the contrary, alkaline treatment with NaOH does not significantly increase mesoporosity of investigated ferrierite. Although there is a significant change in textural properties, both Si/Al and acidity were preserved during the treatment. Methanol dehydration to DME reaction was used as a “probe reaction” aiming to assess the effect of mesopores on accessibility of acid sites. Critical data show that hierarchical zeolites exhibit a higher activity in terms of methanol conversion. On the contrary, the presence of mesopores causes a drop selectivity at 280°C, where hydrocarbons (mainly propene) are formed.

Data Availability

The experimental data used to support the findings of this study are included within the article.

Conflicts of Interest

The authors declare that there are no conflicts of interest regarding the publication of this paper.

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Copyright © 2019 Enrico Catizzone 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.

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